CN1688720A

CN1688720A - Sugar juice purification system

Info

Publication number: CN1688720A
Application number: CNA038240688A
Authority: CN
Inventors: D·O·桑德斯
Original assignee: Ondeo Nalco Co
Current assignee: ChampionX LLC
Priority date: 2002-08-13
Filing date: 2003-08-13
Publication date: 2005-10-26
Anticipated expiration: 2023-08-13
Also published as: CZ2005129A3; AU2003268149A1; NO20051124L; MXPA05002603A; SK50202005A3; WO2004015144A3; RU2370542C2; EP1534866A2; ZA200501998B; RU2005106272A; NZ538632A; WO2004015144A2; CN1688720B; CA2497236A1; CA2537038A1

Abstract

The present invention relates to a method of purifying the syrup obtained from plants, which includes the following step: The syrup (1) is exposed in gas (3) with a characteristic which can transfer at least one substance from the syrup into the gas, so that the quantity of the substance in the syrup is reduced. The present invention also relates to a syrup-purifying system used to realize the method, and a product produced by the method.

Description

The syrup purification system

The right that No. 60/403,594, this international Patent Cooperation Treaty (PCT) patent application requirement U.S. Provisional Patent Application, this application is hereby incorporated by.

Technical field

The present invention relates to contain the system of processing that the sucrose syrup is made sugar and other products with what a kind of plant materials by for example sugarcane, sugar beet or sweet sorghum and so on obtained.The invention still further relates to and be used to make equipment that contains the sucrose syrup and the method that solute content reduces.The invention still further relates to and tradition sugaring system transformed this solute content reduces contains the sucrose syrup to make or to use.

Technical background

Sucrose, C ₁₂H ₂₂O ₁₁, a kind of disaccharides is the condensation molecule that has connected glucose monose and a fructose monose.Sucrose is natural to be present in botanic many fruits and vegetables, for example sugarcane, sugar beet, sweet sorghum, gomuti fibre or sugar maple.In many factors, the processing between the sucrose amount that plant obtains depends on weather conditions in genetic strain, soil or fertilizer factor, the process of growth, plant sickness rate, maturity or harvesting and processes.

Sucrose is concentrated in some position of plant, for example the stem of sugarcane plants or sugar beet root.Can collect the part that sucrose in whole plant or the plant concentrates and shift out (remove) or extract the plant syrup to obtain to contain the syrup of finite concentration sucrose.Usually, the method that from plant materials, shifts out or extract syrup comprise mill, lixiviate (diffusion), squeezing or its combination.Milling is the method that a kind of tradition is used for extracting from sugar-cane syrup.Sugar-cane can be cut into the small pieces of desired size, then by the roller syrup of squeezing out.This process can repeat for several times to guarantee shifting out all sugarcane syrups substantially along a series of runner millings.

Lixiviate is considered to traditional method of extracting syrup from the sugar beet root.Sugar beet is cut into little that is known as " cossettes ", then it is added extraction unit one end, for example making simultaneously, the lixiviate of warm water enters the other end with liquid.When using this convection current to add man-hour, can extract in cossettes or the sugar beet material about 98% sucrose.The liquid that contains sucrose that obtains so-called " leaching syrup ".The cossettes or the sugar beet slices that are come out by extraction unit are still very wet, and still contain some sucrose in its juice (88-92% is a water).Therefore, can in the squeezing machine of screw press or other types, squeeze so that therefrom squeeze out syrup as much as possible these cossettes or sugar beet slices.The pH value of the syrup of this so-called " pulp press water " is approximately 5, and is sent back in the extraction unit in some cases.The beet pulp that obtains (pulp) contains about 75% moisture.In the squeezing charging, add the charged squeezing auxiliary agent of positively charged ion and the moisture content of beet pulp can be reduced about 1.5 to 2%.Also can take out sucrose in the cane stalk by lixiviate.A kind of leach extraction method that is used for sugarcane comprises that the moving-bed of the sugarcane fragment that makes meticulous preparation by extraction unit, can leach sucrose from sugarcane.

Extraction, grinding method, from plant materials, extract syrup or make the plant syrup enter the additive method of the aqueous solution, produce the syrup that contains sucrose, non-sucrose and water.The property quality and quantity of non-sucrose does not wait in the syrup that is made by these methods, can comprise all kinds of botanical derivatives and non-plant derivative, includes but not limited to: insoluble substance, for example vegetable fibre or grogs; And soluble substance, for example carbohydrate, organic and inorganic non-sugar, organic acid, gas dissolved, protein, mineral acid, organic acid, phosphoric acid salt, metal ion (for example iron, aluminium or magnesium ion), pectin, coloring matter, saponin, wax, fat or natural gum, its association or connection portion, the or derivatives thereof beyond fertilizer, sucrose, the sucrose.

These non-sucroses are height lookization, thermally labile or disturb some procedure of processing or the quality or the quantity of sugar product that purifying technique is obtained have a negative impact in others usually.Estimate, average one pound of non-sucrose can make the weight of the sugar product that is obtained by purifying technique reduce 1 to 1.5 pound.Wish can from lixiviate, mill or other is used for extracting from plant materials and separates the syrup that the method for syrup obtains or remove all or part of these non-sucroses.Good lixiviate operation can be removed the impurity that mixes of 25-30%.Beet pulp that reclaims or carbonation extrude water can reduce to 17-20% with this level, but since following some, it remains economical: the sugar of the make-up water of recovery of heat, saving, the contaminated wastewater of reduction, recovery.

Traditional system of processing utilization by lixiviate, mill or other be used for from plant materials extract syrup method (for example United States Patent (USP) 6,051,075,5,928,42,5,480, the method described in 490, each patent all is hereby incorporated by; Or as " SugarTechnology, Beet and Cane Sugar Manufacture (production of sugared technology, beet sugar and sucrose) " (1998) such as P.W.van der Poel; " Beet-Sugar Technology (the beet sugar technology) " that R.A.McGinnis writes, the third edition (1982); Or James C.P.Chen, CaneSugar Handbook:A Manual for Cane Sugar Manufacturers and TheirChemists (the sucrose handbook: the sucrose producer and chemist's thereof handbook) of Chung Chi Chou, method described in the 12nd edition (1993), each document all is hereby incorporated by) the remaining plant materials or the syrup that obtain make following various material: processing is with syrup (process juice); The solid that obtains or in its clarification, purification or treating process, separate with syrup by remaining plant materials from this processing; The syrup that contains sugar or sucrose; The sugar or the sucrose that go out by this syrup crystallization that contains sugar or sucrose; The crystalline mother solution of this sugar or sucrose, with and the various combinations of product or derived products, displacement, every kind of material all contains procedure of processing a certain amount of and described herein or its any part, or the actual compatible impurity of procedure of processing that utilizes in its production, or the impurity compatible with the traditional standard of a class or a kind of following product: wherein a class or a kind of product include but not limited to, removed the animal-feed that contains plant materials of syrup, for example filterable beet section of drop, beet pulp, bagasse, or from processing isolated other solid or syrup the syrup; Using the plant materials of having removed syrup to act as a fuel makes water boiling generation high pressure steam be used for the low-pressure steam of this system of processing or produce low heat to drive turbine generation or to produce with generate energy; To adding the syrup that seasonings and colorant were handled, or adding Nulomoline is to prevent the syrup of crystallization of sucrose, for example golden syrup from the pure sucrose solution syrup of those solution of for example being sold to the industrial user; By removing all or the crystallizable sucrose of any amount or sugared molasses or the molasses derived product that makes, for example molasses (treacle); By the distillable alcohol of molasses; Use sulfurous gas (SO ₂) carry out direct white sugar (blanco directo) or the plantation white sugar (plantation sugar) that sulphiting produces as SYNTHETIC OPTICAL WHITNER; By making the syrup that contains sucrose or sugar boil to juggeri or the raw sugar that substantially dry produces; By melt refining white sugar or the syrup that obtains by the syrup that can further decolour; " or in the whole food industry of North America, be called the monocrystalline sucrose of " evaporation sugar cane juice " (evaporated canejuice) (in order to describe the minimum and monocrystalline sucrose that easily flows that obtains of processing stage) in Britain or other area so-called " not refined sugar " (unrefined sugar), Europe; Grind sucrose (milled cane); Brown sugar (demerara); Muscovado; Rapedura; Panela; Turbina; Contain 94 to 98% sucrose, all the other are molasses, ash content or other micro-raw sugar; Exquisite sugar, for example water white and contain at least 99.9% sucrose, particle is thin especially and its quality for based on specified " bottled " quality of National Soft Drink Association (American soft drinks industry association); Extraordinary white sugar, for example castor sugar, rock sugar, sugar cube or anticorrosion sugar (preservingsugar); By the brown sugar that the method with molasses sprinkling and fusion white refined sugar makes, its characteristic according to molasses can be light brown sugar or dark brown sugar; Or in pulverizing mill by granulated sugar being worn into the Icing Sugar of the various fineness that powder obtains, it can further contain W-Gum or other chemical to prevent caking.This inventory does not represent tradition sugaring system is produced the qualification of product, provides some examples but be expressed as the multiple sugaring system product that is produced.

Be appreciated that traditional system of processing partly comprise gradually clarify, purify or to by lixiviate, mill or other is used for extracting the syrup that the method for syrup obtains from plant materials and carries out the purified step.Usually, can use one or more for example the mechanical means of sieving remove the insoluble or suspended matter of part in the sucrose syrup of containing that derives from plant materials.The filterable syrup of the sieve that obtains when deriving from sugar beet, may contain the sucrose of the water of about 82wt%-85wt%, about 13-15wt%, dissolving non-sucrose or impurity and a certain amount of remaining insoluble substance of about 2.0-3.0wt%.

Usually, can the pH of syrup is raise to the volume that obtains be that the sucrose syrup that contains of 1000 to 2500 gallon per minute is handled by adding alkali gradually.In some traditional system of processing, the pH value of syrup can be from about 5.5pH to approximately being elevated to about 11.5pH to approximately between the 11.8pH between the 6.5pH, thereby make some non-sucrose that is contained in these syrups can reach their iso-electric points separately.This step so-called " preliming ".Yet the back uses this term not represent that the step that will add alkali in containing the sucrose syrup is limited only those systems of processing that the adding of this alkali are called " preliming ".It should be understood that in various traditional syrup systems of processing, wish at first to utilize alkali to make the pH value rising of syrup, carry out procedure of processing subsequently again, for example United States Patent (USP) 4,432, and 806,5,759, described filtration steps such as No. 283; As English Patent 1,043, No. 102 or United States Patent (USP) 3,618,589,3,785,863,4,140,541 or 4,331,483,5,466, described ion-exchange step such as No. 294; As United States Patent (USP) 5,466,294,4,312,678,2,985,589,4,182,633,4,412,866 or 5,102, described chromatographic steps such as No. 553; Or as United States Patent (USP) 4,432, described ultrafiltration steps such as No. 806; As United States Patent (USP) 6,051, described being separated such as No. 075; As United States Patent (USP) 4,045, the 242 described systems of processing that in last carbonator, add active substance, it can be used as the main another kind that adds traditional syrup procedure of processing of ash and carbonation and selects, and above reference is hereby incorporated by.

The use of term " alkali " comprises the material that use can make syrup pH value raise, and includes but not limited to, uses the underflow of the technology of lime or employing lime.The use of term " lime " generally includes concrete use unslaked lime or by heat the calcium oxide that calcium (normally Wingdale form) generates in oxygen.Preferred milk of lime in many syrup systems of processing, its according to following reaction by calcium hydroxide (Ca (OH) ₂) the suspension formation:

Term " iso-electric point " comprises the pH value when solute in the syrup or colloidalmaterial (for example protein) current potential are zero.When these solutes or colloidalmaterial reached its specified iso-electric point, it can form many solid particulates, throw out or cotton-wool thing.

Can in syrup, add the lime carbonate material with further enhancing throwing out, form on this throwing out function can with the core or the substrate of solid particulate or floe binds.This method increases particulate size, weight or density, thereby has promoted the filtration or the sedimentation of these solid particulates or material and promoted it by removing in the syrup.

The mixture of the syrup that obtains, remaining lime, excess calcium carbonate, solid particulate, flocculation agent or cotton-wool thing can be dropped into aforesaid subsequent process steps then.Particularly, about be used for to the syrup that the previous sugar beet course of processing is produced clarify, purification or purified system of processing, can at first carry out cold master and add ash (cold main liming) step so that the Pickering that forms in the preliming step to mixture.This cold master adds grey step can be included in about 30 ℃ of other lime (or adding more according to the quality of preliming syrup) that add the about 0.3-0.7wt% that accounts for the preliming syrup to about 40 ℃ temperature.

Then cold master is added grey syrup and carry out the main ash (hot main liming) that adds of heat further to make Nulomoline and to unsettled other component degradation of this step.Heat is main to be added ash and can comprise further adding lime and be elevated to about 12pH to the level between about 12.5pH so that add the pH value of grey syrup (limed juice).This solvable non-sucrose that causes part not influenced by previous alkali that adds or lime decomposes.Specifically, the heat master who adds grey syrup adds ash and can decompose by the part of Nulomoline, amino acid, acid amides and other dissolving non-sucrose and reach thermally-stabilised.

After cold or hot master adds ash, can add grey syrup to the master and carry out the first carbonation step, in this step, carbon dioxide is added grey syrup with the master and mix mutually.Carbon dioxide reacts with the main remaining lime that adds in the grey syrup and generates the lime carbonate of precipitation form.Not only can remove remaining lime (can remove the remaining lime of about 95wt% usually) by this program, the surfactivity precipitation of calcium carbonate can also be caught quite a large amount of residue dissolving non-sucroses.In addition, precipitation of calcium carbonate can also add physics ash and the carbonation juice and removing the effect of playing flocculating aids in the process of solid matter from main.

Then can with the clarification syrup input that obtains by the first carbonation step other as mentioned above add grey step, heating steps, carbonation step, filtration step, membrane ultrafiltration step, chromatrographic separation step or ion-exchange step or its in conjunction with, replace or the step of deriving, thereby further the syrup that obtains in the first carbonation step is clarified or purified, make the processing syrup of so-called " rare syrup ".

Can carry out multiviscosisty to this further clarifying syrup or " rare syrup " by the method for evaporation section moisture, to obtain tradition and be called the product of " syrup ".The evaporation of part moisture can be carried out in multi-step evaporator.Use this technology to be because it is a kind of mode of effective use steam and if desired, it can also produce the rudimentary steam that another kind can be used for driving follow-up crystallisation process.

The clarification syrup of multiviscosisty or " syrup " can be placed in the container, and this container can hold 60 tons or more usually.In this container, boil and evaporate more water is fit to sucrose or sugar up to environment crystal growth.Because may be difficult to make the crystal of sucrose or sugar to be grown well, the crystal seed that adds some sucrose or sugar is crystal formation to cause.In case crystal grows up to, just can separate crystal that obtains and the mixture that remains syrup.Traditionally, use whizzer to separate this two kinds of materials.Then isolated sucrose or sugar crystal are dried to required humidity, pack subsequently, store, transport or further refining or carry out similar operation.For example, can after transporting to use state, shipment make with extra care raw sugar.

For the product that obtains by plant materials that contains sucrose and syrup, there is an emulative global commerce market.Even the market of the product that is obtained by the plant materials that contains sucrose is enough big so that the reduction slightly of single system of processing step cost also can be saved the money of considerable and required degree.Therefore, the dealer who exists huge motivation to make independent studies person and can make a profit from the chemical of novel system of processing and equipment studies to obtain the system of processing saving the sugaring or the syrup system of sugar industry, and in some cases, the other compensation of the per-cent of this technology saving also is another motivation when making improvements.

Yet, even the improvement at least 1000 years is being established and passed through to the system of processing that the sucrose syrup purifies that contains that obtains from the certain plants body, especially for sugar beet, there be more than 100 year in the industrialization system of processing, even exist huge motivation to promote in sugar or syrup system of processing, to improve, but still there is significant problem in the processing aspect for the syrup that is obtained by plant materials.

A significant problem of tradition sugaring system is acquisition and uses alkali (for example calcium oxide) so that the expense that the pH value that contains liquid sucrose or syrup that is obtained by plant materials raises.As mentioned above, can in syrup, add calcium oxide or calcium hydroxide, from solution, separate out thereby make some solute can be used as solid, throw out or cotton-wool thing to improve the pH value.Calcium oxide obtains by calcined limestone usually, wherein in the presence of oxygen Wingdale is heated in kiln and discharges carbonic acid gas, generates calcium oxide.

As shown in Figure 5, calcine very expensive, because it need buy kiln (40), Wingdale (41) and fuel (42), for example gas, oil, coal, coke etc., these fuel can burn is enough to discharge carbonic acid gas (43) so that kiln temperature is increased to from Wingdale (41).The utility appliance of carrying Wingdale and fuel and shifting out the gained calcium oxide in kiln from kiln must be furnished with some kiln gas of washing and particulate equipment in the kiln waste gas that discharges simultaneously from the limestone calcination process.Naturally manpower be must be equipped with operation and maintenance of equipment, the gas that the quality and will monitoring of the calcined limestone of generation discharges in the kiln operating process and the removing of particulate also will be monitored.

In addition, the calcium oxide of calcining generation must change into calcium hydroxide to be used for typical syrup system of processing.This comprises purchase of equipment again so that calcium oxide is dwindled into the particle of appropriate size and these particles are mixed generation calcium hydroxide with water.Equally, must be equipped with manpower with operation and this equipment of maintenance.

At last, the investment of using relevant equipment and manpower with calcium oxide increases with the increase of consumption.This comprise be used for extra calcium hydroxide and syrup mutually the extra manpower of blended increased point out that perhaps it can comprise the expenditure that equipment increased that the working load capacity is bigger or power is more powerful.

Is the processing of the product of generation when dissolved organic acid or mineral acid react in the processing of excess base or alkali and the syrup with the manufacturing of alkali in traditional system of processing with using another relevant prominent question.For example, when system of processing was used one or more carbonation step when syrup being clarified or purify, the amount of other salt of so-called " used lime " of lime carbonate or generation was in direct ratio with the amount of lime that adds in the syrup.Briefly, the amount of lime that adds in the syrup is big more, and the sedimentary amount that generates in the carbonation step is just big more usually.Can make " carbonatization lime " to be deposited to the carbonation container bottom, be called the material of " lime mud " when being formed with.Can or board-likely separate lime mud by rotary vacuum filter with the frame squeezing machine.The products known as of Xing Chenging " lime cake drainage " (lime cake) then.Lime cake drainage or lime mud can major part be lime deposits, but also can contain sugar, other organic or inorganic thing or water.These isolated throw outs almost always with other system of processing waste material separate treatment, and can, for example, starched with water and the zone that becomes with pump suction settling pond or by dyke or transport to refuse landfill pond (land fills).

Perhaps, can calcine again lime, lime mud or the lime cake drainage of carbonatization.Yet calcining kiln is much also more expensive than the kiln of calcined limestone with the cost of the peripherals that is used for used lime is carried out again.In addition, the quality of incinerating " carbonatization lime " is different with calcined limestone again.It can be to take a single example 92% to 77% that the purity of calcined limestone is compared with calcinating carbonate fossil ash again.Therefore, also corresponding higher to the neutralize amount of required lime kilning again of the oxonium ion of same amount in the syrup.Similarly, the carbon dioxide content of used lime is more much higher than Wingdale.Therefore, not only the manufacturing of calcined limestone is very expensive again, but also the CO that generates when need using much bigger gas duct and equipment to calcine used lime again to shift ₂, need bigger handling equipment to carry again lime kilning, to need bigger carbonation groove or similar devices.

In addition, no matter used lime be disposal in the pond, in the refuse landfill pond or by recycling processing, the amount of lime of using in the particular process system is big more, the expense of usually conduct used lime is just high more.

Another significant problem of tradition sugaring system is that the treatment capacity of system of processing is with processing increasing progressively and successively decrease with employed amount of lime in the syrup.This problem is on the one hand to make or is supplied to the amount or the speed of lime of syrup procedure of processing limited.As mentioned above, must calcine before Wingdale is used as alkali in the syrup system of processing to make calcium oxide.The amount of the lime that obtains is subjected to the restriction of Wingdale utilization ratio, kiln capacity, fuel availability or similar factor.Make lime and can generate size, kind and the quantity of equipment according to lime, available manpower or similar factor and change with the speed of supplying with the syrup system of processing.The amount of lime used in this system of processing that is on the other hand of this problem can make the volume reducing that is used to hold syrup in the system of processing pro rata.For example the increase of the alkali consumption of lime also needs to use bigger volumetrical zone, conduit or similar devices to keep the syrup treatment capacity of equal volume.

Another significant problem of tradition sugaring system is to extract the excessive acid that produces in the plant materials before the plant syrup.Organic acid plays the effect of buffering system in the acid-alkali balance of vegetable cell, thereby keeps required pH value in plant tissue.The source of these acid can be divided into two groups, and first group is the acid that plant absorbs from soil in growth cycle, and second group is the acid that forms by biological chemistry or microbial process.When the acid of absorbing from soil was not enough, plant can be synthesized organic acid, mainly is oxalic acid, citric acid and oxysuccinic acid, with the pH value of the health that keeps plant cell liquor.Therefore, the syrup of extracting from plant tissue contains a certain amount of various organic acid.

Except this in plant tissue naturally occurring organic acid, acid can also mainly form by microbial process in storage process.Serious rotten plant materials may produce lot of organic acids, mainly is lactic acid, acetate and citric acid.Total acid content in the plant tissue can increase three times or more in some cases.

In addition, because the destruction of natural basicity in the syrup can produce carbonic acid gas (CO2) in plant tissue.In this process, bicarbonate ion and carbanion can change into carbonic acid gas.The carbonic acid gas that still keeps dissolved state that generates can produce carbonic acid, and carbonic acid is a source of oxonium ion.Contained organic acid is all or part of in the plant cell liquor, is retained in the syrup that is obtained by plant materials.Therefore, for the pH value that makes syrup raises, must be with alkali these organic and mineral acids that neutralize.The concentration of organic acid or mineral acid is high more in the syrup, and it is just many more to make the pH value of syrup be elevated to the required alkali number of expected value.

Another significant problem of tradition sugaring system is that the plant materials handled with the antimicrobial chemical product or the acid content of syrup are higher than untreated plant materials or syrup.For example, can continuously or add sulfurous gas (SO intermittence ₂) or ammonium bisulfite (NH ₄HSO ₃) to help the controlling microbial growth or to infect.SO ₂Add-on depend on the severity of microorganism growth or infection.Can monitor or follow the trail of to determine the severity of microorganism growth or infection the amount of lactic acid and nitrite.Can use the SO that reaches about 1000ppm ₂Impact or the processing infected system.Can add continuously and reach 400-500ppm with control infection.The SO that is used for antimicrobial protection and adds ₂Or NH ₄HSO ₃The pH value and the basicity of syrup are reduced.Because naturally occurring bicarbonate ion changes into CO ₂Or carbonic acid, basicity can reduce.

Another significant problem of tradition sugaring system is the formation of incrustation scale in the container of for example vaporizer or sugared crystallizer.The calcium salt of oxalic acid constitutes the main component of incrustation scale usually.Oxalate has low solubility in solution, and this solubleness can reduce with the increase of calcium amount in the solution.Even after the syrup purification becomes " rare " or " dense " syrup, also exist abundant calcium to impel oxalate from solution, to separate out in the solution.The method that descale is removed on slave unit surface is very expensive, includes but not limited to by slowing down and efficiency losses with production, or the cost that produced of equipment effective service life reduction.

Another significant problem of tradition sugaring system is not recognize to be used for obtaining the syrup extraction equipment of syrup or the pH value that method can change or reduce the syrup that extracts from plant materials.As for the extraction unit that is used for extracting syrup, do not recognize that the pH value of sugar beet juice can change or reduce in leaching process from the sugar beet material.Be on the other hand the not recognize distinct device or the different methods that are used for from sugar beet material lixiviate syrup of this problem are changing or are reducing the pH value that makes syrup in varying degrees.The improvement of microwave leaching technology has made the pH that makes syrup benefit on duty for the day reduce substantially, and thus, these equipment and method greatly differ from each other from solution provided by the invention.

Another problem of tradition sugaring system be dissolve in from sugar beet extract, shift out or syrup that lixiviate goes out in or add organism, gas dissolved or other material in the syrup that this extracts or lixiviate goes out, before the preliming step that the tradition sugaring is purified, can not tend to be balanced or reach balance with atmosphere dividing potential drop or selected dividing potential drop gaseous mixture.Therefore, solute should be transferred in atmosphere or other the selected gaseous mixture from the syrup of extracting, shifting out or leach, thereby reduce dividing potential drop or the concentration of those solutes in leaching syrup, but now still carry out preliming, initially add ash, lime add step before or directly facilitate simultaneously or combine with other pH regulator method in the syrup and facilitate the reduction of leaching syrup pH value indirectly.As mentioned above, lower pH value can cause using more lime to reach the desired pH of syrup.

Problem about the lixiviate (or other shifts out or extract the conventional method of syrup or material from plant) of traditional sugar beet silk; It is on the one hand traditional extraction equipment or is used for can not providing or be not enough to provide the material of surface interface between the selected or desired gas mixture of the liquid that leaches syrup or contain the plant material that is extracted or removed and atmosphere or other (this interface be used for making being dissolved in leach that syrup or other contain extraction or the liquid of the plant material removed out) to tend to be balanced from other legacy equipment that plant shifted out or extracted syrup or other material, can fully reduce like this these materials and contain concentration in the liquid of the plant material that is extracted or removed at syrup or other.

This problem is that on the other hand traditional sugar beet-leach extraction method or equipment (or be used for removing or extracting from plant materials syrup or other material other legacy equipment) can't provide atmosphere dividing potential drop or other selected dividing potential drop gas in equipment abundant recirculation contains the partial pressure difference between the solute concentration the liquid of the plant material that is extracted or removed to keep syrup or other, this partial pressure difference can reach balance potentially with the dividing potential drop gas that exists on the liquid-vapo(u)r interface, thereby reduces material and realize required leaching in the liquid that syrup or other contain the plant material that is extracted or removed pH effectively, potential or possible reduction.Therefore, the partial equilibrium of dividing potential drop inter gas or complete equipilibrium hinder or have slowed down the further reduction of pH reduction material, compound or gas concentration in the leaching syrup in dividing potential drop gas that exists on the liquid surface and the solution.

This problem third aspect is that traditional sugar beet-leach extraction method or equipment other legacy equipment or the method for syrup or other material (or be used for removing or extracting from plant materials) do not make and leaches the syrup thorough mixing to being enough to that the leaching syrup (or other contains the liquid of the plant material that is extracted or removed) of impelling the reduction of pH value of whole volumes or enough volumes and other gaseous mixture on atmosphere or the liquid-gas interface are tended to be balanced.

This problem fourth aspect is that traditional sugar beet-leach extraction method or equipment other legacy equipment or the method for syrup or other material (or be used for removing or extracting from plant materials) will not leach liquid heat that syrup or other contain the plant material that is extracted or removed and leach syrup or other solubleness that contains the liquid of the plant material that is extracted or removed is reduced to the temperature that is achieved following aspect to being enough to make: the concentration the dividing potential drop gas that the concentration trend liquid-gas interface that makes pH reduce material exists or reach balance with it, or shifting balance point is so that the concentration of pH reduction material is reduced to required, potential or possible concentration; With desired rate or the required potential or possible balancing speed that maybe can reach and the trend of the dividing potential drop gas on the liquid-vapo(u)r interface or reach balance.

Another significant problem of tradition sugaring system is that other that extract or leach syrup its surface exists can be with atmosphere dividing potential drop or syrup cooling the time contains gaseous mixture that greater concn pH reduces material and tend to be balanced or reach balance.When leaching syrup or other and contain the liquid cooling of the plant material that is extracted or removed, the solubleness of atmosphere or other gaseous mixture can increase.Therefore, when leaching the syrup cooling, dissolve in the gas in the syrup or the concentration of other material (including but not limited to that pH reduces material) and improve.Take a single example, before preliming or adding grey step, when the leaching syrup is cooled between about 20 ℃ to about 30 ℃ between about 55 ℃ to about 70 ℃ in the lixiviate step, Atmospheric CO ₂Solubleness increase.Be exposed to CO ₂In the atmosphere dividing potential drop or be exposed to have and be enough to when syrup is cooled off with CO ₂Transfer to the CO in the syrup ₂In the time of in any gaseous mixture of dividing potential drop, the amount when higher with respect to temperature leaches the CO in the syrup ₂Concentration has improved.Leach the CO that improves in the syrup ₂Concentration can reduce the pH value of syrup.Therefore, leach CO in the syrup ₂Or the raising of other gas concentration requires to add at subsequently lime interpolation, preliming or other and adds more lime in grey step to reach required or necessary pH value.

Another problem of tradition sugaring system is the dividing potential drop gas that leaches on the liquid-vapo(u)r interface of liquid that syrup or other contain the plant material that is extracted or removed, and setting up effectively is enough to leaching the concentration that syrup or other concentration gradient essential or that required part is volatilized, moves, removed or otherwise shifts that contains the liquid of the plant materials that is extracted or removed leach the pH value of syrup or reduce pH reduction material in the leaching syrup with abundant raising.

The invention provides a kind of syrup system of processing, it includes equipment and the method that solves above-mentioned each problem.

Summary of the invention

Therefore, main purpose of the present invention provides a kind of syrup system of processing that contains liquid sucrose or syrup preparing product that is obtained by plant materials of using.Aspect of this main purpose provides the surrogate of a kind of traditional syrup or sugared system of processing.Thus, the invention provides one and apply mechanically the complete system of processing that the liquid that contains sucrose or syrup obtain product, comprise equipment and method.This main purpose second aspect has provided the syrup system of processing method with traditional syrup or sugared system of processing method compatibility.As for this purpose, the invention provides further to add, replace or change and be used to process liquid or the traditional method of syrup and the method steps and the equipment of equipment that contains sucrose.

Second main purpose of the present invention is to reduce with containing the liquid of sucrose or the cost of syrup preparing product.Aspect of this purpose of the present invention is that the syrup process throughput that all or part of utilization ratio that is subjected to alkali is limit improves, and for example be subjected to the reduction of Wingdale utilization ratio or Wingdale is changed into the scarce capacity of calcium oxide, or similar factor is limit.This purpose is to be processed into the alkali (for example lime) that product institute must use and to measure so that the saving of cost to be provided by reducing the liquid will contain sucrose or syrup on the other hand.This purpose third aspect of the present invention is to reduce the refuse amount that generates, and for example reduces the used lime amount.

The 3rd main purpose of the present invention provides liquid product that contains sucrose or the syrup product that a kind of the present invention of use obtains.Aspect of this purpose provides for example water-soluble acid, volatile organic compounds, gas dissolved (CO for example ₂Or SO _s), the solute content of ammonia or similar substance or concentration reduce contain liquid sucrose or syrup product.This purpose second aspect is that liquid that contains sucrose or the syrup product with higher pH value is provided after handling according to the present invention.This purpose third aspect provides a kind of liquid that contains sucrose or syrup product that has higher pH value need not to use any alkali to handle according to the present invention after.Even a fourth aspect of the present invention is to have added the alkali of a certain amount of for example lime or during from the underflow of traditional syrup processing or similar substance, also can provide liquid that contains sucrose or syrup product with higher pH value before handling according to the present invention.This purpose the 5th aspect provides liquid product that contains sucrose or the syrup product that a kind of ability that generates oxonium ion reduces.This purpose of the present invention the 6th aspect provides liquid that contains sucrose or the syrup product that the less alkali of a kind of needs rises to the pH value desirable value, solute is carried out isoelectrofocusing, the preliming or the master that carry out in traditional system of processing add grey step, make the Nulomoline degraded, or otherwise obtain product by liquid that contains sucrose or syrup.

The 4th main purpose of the present invention provides and is used for making by for example squeezing, mill or the solute content of the syrup that traditional syrup extraction procedure of lixiviate obtains or the method and apparatus that concentration reduces.Aspect of this purpose provide a kind of need not to add alkali, must add alkali or prior to the situation that adds alkali under solute content or concentration are reduced method.A second aspect of the present invention provide a kind of can be before in liquid that contains sucrose or syrup, adding alkali, among or the method that solute content in this syrup or concentration are reduced used afterwards.This purpose third aspect provides a kind of method that helps to make the solute content that contains in liquid sucrose or the syrup or concentration to reduce.This purpose fourth aspect provides a kind of and includes but not limited to aforesaid preliming, the main traditional juice,liming of ash, ion-exchange or filtration method or the method that makes the solute minimizing that contains in liquid sucrose or the syrup of method of purification compatibility of adding.

The 5th main purpose of the present invention provides various equipment and the methods that make the interfacial area increase that contains liquid sucrose or syrup and required dividing potential drop inter gas.

The 6th main purpose of the present invention provides the various equipment that are used for injecting, adding or otherwise sneak in the syrup that is obtained by plant materials required dividing potential drop gas.Aspect of this purpose provides injects the equipment of syrup so that the syrup mixed flow that contains syrup and required dividing potential drop gas to be provided with gaseous mixture.

The 7th main purpose of the present invention provides various being used for and will reach partially or completely equilibrated gaseous mixture with solute, perhaps contained or institute's dissolved dividing potential drop gas delivery or the equipment removed in the syrup.

The 8th main purpose of the present invention is under the temperature that responds or regulate with respect to following condition (can manually or automatically regulate) liquid that contains the plant materials that is extracted or removed to be assessed, monitor, made or preserves: time loss; Any predetermined substance or the component concentrations that are wherein contained; Detailed process or step that this liquid is purified or otherwise processed; From this plant materials, extract, remove or the method for these materials of lixiviate; Or any preparation or storing mode that is used for the solubility of substances that the pH that makes this liquid is reduced or the material concentration of potential reduction is controlled is made as this liquid of certain limit or particular value.

The 9th main purpose of the present invention provides and is used for the liquid that leaches syrup or contain the material that extracts or shift out from plant materials being handled before adding so that stop dividing potential drop gas on the liquid-gas interface, it minimized or it is controlled at initial lime and the lime subsequently of adding.Equipment and method.

Thereby the of the present invention ten main purpose provides and volume required or syrup that must volume and liquid-gas interface interacted make material to transfer to equipment and method in atmosphere dividing potential drop or the selected dividing potential drop gas as required or necessarily from leach syrup.

Naturally, the other parts at specification sheets and accompanying drawing disclose other purpose of the present invention.

Description of drawings

Fig. 1 represents an embodiment that is used for making the syrup substances content minimizing that is obtained by plant materials of the present invention, it comprises the gaseous mixture that has in the syrup of the being transported to syrup e Foerderanlage with the mixed flow that produces syrup and gaseous mixture, this device further comprises gas distribution elements, for example pipeline or the groove in the syrup handling equipment, or the impeller of pump.

Fig. 2 represents an embodiment that is used to make the syrup that substances content reduces of the present invention.

Fig. 3 represents second embodiment that is used to make the syrup that substances content reduces of the present invention.

Fig. 4 represents the 3rd embodiment that is used to make the syrup that substances content reduces of the present invention.

Fig. 5 represents the embodiment that is used to make the syrup that substances content reduces of the present invention, and it further is included in to reduce and contains the water yield to make before the syrup or before sugared crystallization, uses to add ash and carbonation further to make this juice,liming or purification.

Fig. 6 represents the embodiment that is used to make the syrup that substances content reduces of the present invention, and it further is included in and reduces water content to make before the syrup or before sugared crystallization, to use ion-exchange further to make this juice,liming or purification.

Fig. 7 represents the embodiment that is used to make the syrup that substances content reduces of the present invention, its minimizing contain the water yield with before making syrup or the filtration step that before sugared crystallization, further comprises for example ultrafiltration further to make this juice,liming or purification.

Fig. 8 represents that these syrups, leaching syrup or the processing of other syrup can reduce with the solubleness of some material, material or the component that contain in the liquid along with syrup, leaching syrup or the processing of other syrup rising with fluid temperature.

Fig. 9 represents several embodiment of processing the sugar beet silk by the mode that reduced some material in pulp syrup or the leaching syrup before the preliming step of the present invention.

Figure 10 represents the embodiment that another kind of the present invention is processed the sugar beet silk by the mode that reduced some material in pulp syrup or the leaching syrup before the preliming step.

Figure 11 represents a specific embodiment of the present invention.

Figure 12 represents the vertical view of a specific embodiment of the present invention, and it has shown cross section A-A.

Figure 13 represents the side-looking cross section A-A of embodiment shown in Figure 12.

Embodiment

Generally speaking, present invention resides in to evaporate before excess water or the sucrose fractional crystallization and do not adding alkali or adding the syrup system of processing of under the situation of less alkali syrup being purified.Particularly, the invention provides the syrup that solute content reduces, gas dissolved reduces, the pH value is higher or basicity is lower that is used for the syrup purification system.

As mentioned above, can obtain syrup by for example plant materials of sugar beet, sugarcane, sweet sorghum.Naturally, for the product that must obtain syrup with the plant materials of other kind, may there be very big commercial market or niche market (niche markets), and should be appreciated that and the invention is not restricted to the syrup that from any position of the plant of any particular types or plant of collecting or plant materials, shifts out, extract or obtain.In addition, the term syrup can be broadly construed any syrup or the liquid that contains sucrose in any step of any system of processing before sugared crystallization.Thus, contain liquid sucrose or be two examples of syrup by what plant materials obtained by milling or squeezing step by the syrup that the step of lixiviate plant materials makes.As mentioned above, the term syrup comprises the liquid that contains sucrose, non-sucrose and water, and its ratio is indefinite, the step that this depends on the character of plant materials and is used for shifting out from plant materials syrup.Can expect to remove or be partly dissolved thing, because the quality or the quantity of its height lookization, thermally labile or the sugar product that otherwise interferes with each other with some procedure of processing or purification process is obtained have a negative impact.The term syrup also comprises by what these various clarifications or purification step obtained and contains liquid sucrose.

The specific embodiment of the present invention comprises removing and is partly dissolved thing, volatile matter, gas dissolved, water-soluble acid or similar substance at least, for example can form the carbonic acid gas or the sulfurous gas of water-soluble acid, can in solution, produce oxonium ion like this, change the concentration of oxonium ion in the syrup or the pH value of reduction syrup.

For example, when containing enough positively charged ions in the syrup, hydroxide ion OH-can serve as negatively charged ion, and it can make carbonic acid gas CO ₂With carbanion (CO ₃) ^-2, or with bicarbonate ion HCO ₃ ^-Form be dissolved in the syrup.HCO ₃ ^-Disassociation a kind of very weak acid is provided.Yet the positively charged ion that contains in syrup counts deficiency so that dissolved CO ₂When forming carbanion or bicarbonate ion, at carbonic acid gas and carbonic acid H ₂CO ₃Between can produce balance.Carbonic acid can serve as strong acid in the pH scope of preparation syrup.The oxonium ion of Chan Shenging has improved the existing concentration in the syrup subsequently, causes the pH value to reduce.

Similarly, can in syrup, add sulfurous gas (SO ₂) or ammonium bisulfite (NH ₄HSO ₃) with control, reduction or elimination microorganism active, sucrose hydrolysis, the formation of Nulomoline or the loss of sucrose, perhaps the pH value is turned down.Similarly, in syrup, contain enough positively charged ions, for example during calcium, can produce for example sulphite of calcium sulfite.Yet the positively charged ion that contains in syrup counts deficiency so that dissolved sulfurous gas (SO ₂) when forming sulphite, at sulfurous gas (SO ₂), sulfurous acid (H ₂SO ₃) and sulfuric acid (H ₂SO ₄) between can produce balance.Sulfuric acid and sulfurous acid can play the effect of strong acid.The generation of oxonium ion has subsequently improved the existing concentration in the syrup, causes lower pH value.

In addition, plant can produce other water-soluble acid in the normal growth process, and other acid of microbial process generation, include but not limited to phosphoric acid, hydrochloric acid, sulfuric acid, citric acid, oxalic acid, succsinic acid, fumaric acid, lactic acid, oxyacetic acid, pyrrolidone-carboxylic acid, formic acid, acetate, butyric acid, toxilic acid, lactic acid etc.

In addition, the conversion of amino acid whose decomposition or ammonium bisulfite of for example adding in the syrup and so on material can produce other solute.

Now mainly with reference to Fig. 1, a specific embodiment of the present invention can comprise the mode that increases by the interfacial surface area (4) that can make between syrup (1) and the mixture (3), and it is total to make the syrup (1) that is obtained by plant materials (2) be exposed to gaseous mixture (3).By the interfacial surface area (4) between syrup (1) and the gaseous mixture (3) is increased, when each component concentrations of solute (5) be tending towards with gaseous mixture (3) in this component concentrations when reaching balance, can improve the transfer rate of various solutes (5) from syrup (1) to gaseous mixture (3).Can select gaseous mixture (or stripping gas) to make unwanted solute (5) from syrup (1), transfer to required dividing potential drop in the gaseous mixture (3) to provide.Gaseous mixture (3) can be regenerated, perhaps and syrup (1) between adjust dividing potential drop gas to prevent reaching balance between gaseous mixture (3) and the solute (5) continuously or intermittently on the interfacial surface area (4) that increases, make thus that solute (5) is lasting to be transferred in the gaseous mixture (3) from syrup.

Use when of the present invention, can from syrup, remove solute or volatile matter, for example volatility mineral compound, volatile organic compounds or gas dissolved (for example carbonic acid gas, sulfurous gas or ammonia).The syrup product that uses the present invention to obtain is compared with not using identical syrup of the present invention, and ability or the oxonium ion concentration that the minimizing of solute content, gas dissolved reduce, produce oxonium ion reduces, basicity is lower or the pH value is higher.Take a single example, can fully reduce concentration of carbon dioxide in the syrup when using the atmosphere dividing potential drop that syrup is carried out stripping (strip).The pH value of the syrup product that is obtained by this method can improve 0.05pH, 0.1pH, 0.2pH, 0.3pH, 0.4pH, 0.5pH, 0.6pH, 0.7pH, 0.8pH, 0.9pH, 1.0pH, 1.1pH, 1.2, pH1.3, pH1.4, pH1.5, pH1.6, pH1.7, pH1.8, pH1.9,2.0pH, yet, can save quite a lot of money and commercial very important to adjusted to what the initial pH value of undressed syrup was carried out any degree ground pH value.The reality that begins from the initial pH value regulated quantity that makes progress depends on the kind and the quality of the syrup that the present invention handles usually, the increase degree of the interfacial surface area that produces by the syrup volume, the time length that gaseous mixture responds to the interfacial surface area that increases, and the dividing potential drop that provides in the gaseous mixture.Thus, with regard to employed the specific embodiment of the present invention, the regulated quantity that makes progress of pH value is indefinite.For example, change the volume or the amount of the syrup of unit time processing, and use identical the specific embodiment of the present invention, can aspect the change of pH value, produce different increments in others.

The present invention also further may further comprise the steps: compare with the syrup of untreated syrup or conventional process, make for reach must or required pH value, oxonium ion concentration or basicity reduce to some extent at the alkali number that per unit weight or unit volume add in the syrup that the present invention handles.After the solute minimizing that makes in the syrup that the present invention handles, the alkali that adds much less just can reach required pH value, between for example about 11.0 to about 12.0 or between about 11.5 to about 12.5 or be used for the pH scope of " preliming ", " the main ash that adds ", " centre adds ash ", or reach with syrup in the corresponding pH value of iso-electric point of any specific non-sucrose, or the acidity or alkalinity that reaches syrup is adjusted to the required pH value of prescribed concentration.As for lime consumption, for example, compare with untreated syrup or through the syrup of conventional process, use various embodiment of the present invention to reduce and reach about 30% consumption.

Now mainly with reference to Fig. 2; the specific embodiment of the present invention comprises gaseous mixture (3), its can contain atmospheric gas or air, through one or more strainers with reduce or the atmospheric gas of abiotic particle of basically eliminate or biological particles (for example bacterium, virus, pollen, microcosmic flora or fauna or other pathogenic agent) or air, through chemical scrubber or through atmospheric gas or air, Purge gas or its combination or the displacement of otherwise processed to produce required dividing potential drop gas concentration or concentration range.

The specific embodiment of the present invention may further include the gas filter (6) that gaseous mixture (3) stream is responded.This gas filter (6) can be positioned at gaseous mixture (3) is play before or after the flow generator (7) of fluidic response effect.The gas filter (6) that gaseous mixture (3) stream is responded can comprise the macrobead or the microparticle strainer of high efficiency particulate air filter (Hepa filter) or ultra-high efficiency air filter (Ulpa filter) or other type.Also can use other prefilter to capture particle in the gaseous mixture before entering flow generator (7), or can flow generator (7) afterwards but use before at gas filter (6).

Unfiltered air mixture (3) can be sucked in the one-level prefilter (8), then by secondary prefilter (9), then by flow generator (7).Make pre-filterable gaseous mixture flow through gas filter (6) (high efficiency particulate air filter, or the strainer of ultra-high efficiency air filter or other type) then.The mixture of filtrated air that obtains (from gaseous mixture (3), remove when using high efficiency particulate air filter all little to about 0.3 micron particle, reach 99.99% particle), from gaseous mixture (3), remove when using the ultra-high efficiency air filter reach 99.99% little of about 0.12 micron particle) can between syrup (1) and gaseous mixture (3), produce the interfacial surface area (4) of increase then or it is responded.As for other embodiments of the present invention, gaseous mixture (3) or syrup (1) can be exposed in the short wavelength ultraviolet source of radiation (10) to reduce the quantity of pathogenic agent particle or bacteria particles.The present invention may further include Temperature-controlled appliance (11) so that make gaseous mixture (3) reach required temperature before the interfacial surface area (4) to syrup (1) or increase responds.Temperature-controlled appliance (11) is responded to temperature sensor (12), the latter can detected gas mixture (3) or the temperature of syrup (1) and send signal or impel Temperature-controlled appliance (1 1) with the temperature regulation of gaseous mixture (3) and/or syrup (1) to temperature required.

For embodiments more of the present invention, no matter whether gaseous mixture (3) filter, and can be used for forming or the auxiliary interfacial surface area (4) that increases that forms.For example, can syrup (1) be sent into gas syringe (13) or under the pressure that pump (14) or other liquid transfer element produce, send into by gravity feed.Gas syringe (13) can have syrup (1) enters gas syringe (13) by this import import (15), syrup (1) is left the outlet (16) of gas syringe (13) by this outlet, and at least one gaseous mixture (13) is sent into by this injection port and contained in this gas syringe (13) or through wherein the injection port (17) to the small part syrup (1).

When gas syringe (13) has (gas syringe is charging and emptying periodically) when being used for processing the structure of syrup in batches, for certain embodiments of the present invention, import (15) can be identical mouth with outlet (16).Be used for pulsating flow processing (the liquid stream of syrup (1) can periodically reduce or interrupt to increase the residence time of syrup (1) in gas syringe (13)) or Continuous Flow processing (liquid of syrup (1) flows Continuous Flow through gas syringe (13) when gas syringe (13) has, speed or volume through syrup gas coming through syringe (13) can be regulated) structure the time, import (15) and the outlet (16) can be discrete.

For each embodiment of the present invention, gaseous mixture (3) can capacity inject syrup (1) under competent pressure, or inject with certain distribution pattern (for example diffusion or with the small bubbles form), with the interfacial surface area (4) of the required increase of generation between syrup (1) and gaseous mixture (3).The interfacial surface area (4) that increases can provide being partly dissolved thing (5) at least and can transferring to interface in the gaseous mixture (3) from syrup (1) through it in syrup.

No matter its be configured to of the present invention in batches, pulsation, intermittently or embodiment operation continuously, gas syringe (13) can further stir, turn round, stirs or otherwise provide mixing equipment (18) so that gaseous mixture (3) further is distributed in the syrup (1) with further increase interfacial surface area (4).When the structure of gas syringe (13) produces syrup (1) stream, no matter be continuously, pulse or intermittently produce, gaseous mixture (3) is injected the mixed flow (19) that syrup (1) can produce syrup.Gaseous mixture in the syrup mixed flow (19) can further be distributed in syrup (19) mixed flow by set up parts (extensions), raceway groove or the like that is connected on gas syringe (13) internal surface.Determine direction that these set up parts or pipeline so as in gas syringe (13) to syrup miscarriage give birth to required disturbance.The present invention can further provide injection pressure conditioning equipment (20), and flow generator (7) responds this equipment to improve or to reduce pressure or the amount of injecting, sneaking into or spray into the gaseous mixture of syrup (1).In embodiments more of the present invention, injection pressure conditioning equipment (20) can be independently or is comprised a variable adjustment limiting device that is positioned between flow generator (7) and the injection port (17) in combination.

With regard to some embodiment, the present invention can produce starting point concentration than syrup and more be dissolved in gas in the syrup fully.It can reach and under atmospheric pressure make saturated about 10 times of obtaining concentration of syrup.The pressure that injects the gaseous mixture (3) of syrup (1) can arrive between the pressure of about 20 crust at the original pressure that syrup (1) applies.

Can use a plurality of gas syringes (13) of serial or parallel connection, each gas syringe in parallel or placed in-line can be in substantially the same position or different positions have a plurality of gas injection port (17).Each injection port (17) can be independently or changeably the volume and the pressure of the gaseous mixture (3) that injects syrup (1) is controlled.The injection port of variable adjustment (17) can respond to volume, the residence time, the concentration of syrup (1) middle solute or the concentration of amount or syrup (1) middle solute etc. of syrup in gas syringe (13) of syrup (1).

For other embodiments of the present invention, can before gaseous mixture (3) be injected syrup (1) at pump (14), pump (14) can play gaseous mixture (3) is distributed to the effect to produce mixed flow (19) and interfacial surface area (4) is increased in syrup (1) stream like this.According to the type of pump, mixed flow can contain at least 35% gaseous mixture in (19), and wherein syrup stream (1) almost is full of by the bubble 100% of gaseous mixture (3).Take a single example, can use the Shanley pump to produce mixed flow (19).The Shanley pump is hereby incorporated by.Can as required a plurality of pumps (14) serial or parallel connection be turned round so that process the syrup (1) of certain volume in predetermined time duration.

For other embodiments of the present invention, can further dispose syrup (1) stream so that Venturi effect to be provided, or otherwise produce response syrup stream (1) and the pressure of minimizing, so that gaseous mixture (3) is sucked in the syrup stream (1), suction can be pulsed, continuous or intermittent mode.

For some embodiment of the present invention, only some syrup stream (1) is exposed in the gaseous mixture (3).For example,, syrup (1) flow point can be opened then, part syrup (1) is exposed in the gaseous mixture (3) if contain minimal amounts of dissolved thing (5) in the syrup (1).Then syrup (1) stream is reconsolidated according to required ratio.

Mainly with reference to Fig. 3,, can spray to syrup (1) now by the syrup distributed component (21) of for example nozzle for other embodiments of the present invention.Syrup distributed component (21) can produce very fine and closely woven syrup drop (22) or particulate spraying.Therefore, spraying increases interfacial surface area (4).Syrup can be sprayed in ventilated container (23), and no matter whether gaseous mixture (3) carried out filtering or washing as mentioned above, can be exposed in the spraying syrup drop.Syrup can be sprayed onto the top area (for example passing through fog nozzle) of ventilated container (23), is exposed to then in the gaseous mixture (3) by this ventilated container (23).The direction that gaseous mixture can drip (22) with syrup become convection current ground by ventilated container (23) so that the solute (5) in the syrup (1) is transferred to efficient raising in the gaseous mixture (3).Ventilated container (23) can be, for example, and 150 gallons groove, but what can expect is that the size and dimension of this groove is according to the difference of the syrup amount of being processed and different.

In some embodiment of the present invention, ventilated container (23) can further contain syrup distribution surface (24).Syrup (1) can be distributed to this syrup and distribute surface (24) upward so that interfacial surface area (4) is increased.In addition, syrup can be sprayed onto the top area of ventilated container (23), is distributed on the syrup distribution surface (24), is exposed to then in the gaseous mixture (3) by ventilated container (23).In addition, gaseous mixture (3) can flow by ventilated container (23) in pairs with the approximate flow directions of syrup (1) on syrup distributes surface (24), so that the efficient that the solute (5) in the syrup (1) is transferred in the gaseous mixture (3) improves.

For these embodiments of the present invention of using ventilated container (23), can collect syrup (1) and repeatedly cycle through ventilated container (23) as required.

Mainly with reference to Fig. 4, in other embodiments of the present invention, syrup (1) can be transported in the syrup container (25) now, and adds gaseous mixture (3) by syrup (26) is sprayed in syrup (1).Can regulate the pressure and the volume of gaseous mixture (3) with respect to the volume of syrup (1) and the size of syrup container (25).The syrup container can further combine with above-mentioned ventilated container (23).

Chemical Engineer ' s Handbook (chemical engineers handbook), Perry, write., the general discussion about gas absorption that (1950) the 668th pages of McGraw-Hill Book Company (Machill books company) and following content or the like are provided is incorporated herein by the reference of the scope of General Principle necessity of understanding gas absorption.

Can recognize, can be equipped with various conventional catheters, valve or other device (for example pressure warning unit) so that produce and the process of in gas syringe (13), ventilated container (23) or syrup container (25), carrying syrup (1), the amount and the pressure of the gaseous mixture (3) that injects, sprays or spray, the relevant relevant informations such as amount of the solute (5) in the syrup (1).

Again mainly with reference to Fig. 2, the present invention may further include gas separator (27) and contains gaseous mixture (3) by the solute of input in the syrup (1) with release.In some embodiment of the present invention, when using ventilated container (23) as mentioned above, gas separator (27) can comprise the perforate in the ventilated container, makes gaseous mixture to be discharged in the atmosphere by ventilated container.Comprise in the specific embodiment of the invention of atomizer that in those gas syringes (13) gas separator (27) can be to make the gaseous mixture (3) that contains solute be discharged into perforate in the atmosphere.Gaseous mixture (3) is added in the specific embodiment of the invention of syrup (1) stream with generation syrup mixed flow (19) by gas syringe (13) at those, no matter this process be continuously, pulsation or intermittent with the conduit of atmospheric isolation in transmit, gas separator (27) can comprise that a part further provides the conduit of the internal volume that is connected with atmosphere by fluidics.Particularly, the gas separator that links to each other with atmosphere by fluidics (27) can comprise that a part is configured to or is defined for the conduit of adjusting mixed flow (19) to the atmospheric time of response.

Particularly, a kind of structure of gas separator (27) can be the increase of conduit internal volume so that mixed flow (19) is dispersed on the internal surface of conduit so that syrup prolonged by the hold-time that fluidics links to each other with atmosphere, and/or the surface-area increase when syrup is linked to each other with atmosphere by fluidics.In some embodiment of gas separator (27), syrup can be distributed on the enough big surface-area so that make the gaseous mixture (3) in the syrup (1) just reach balance basically with the atmosphere dividing potential drop before syrup shifts in by gas separator (27), and the internal surface of gas separator (27) can further be configured to be furnished with sets up parts, corrugated groove (corrugates), groove or similar structures further to mix or stirring syrup (1) is transferred to speed the atmosphere with raising gaseous mixture (3) from syrup (1) in gas separator (27).

Can pass through a Reduced pressure source (29) device separated from the gas (27) is linked to each other, thereby produce the air-flow of transferring to the gaseous mixture (28) the atmosphere from syrup (1).Decompression is included in the surface-area (4) of syrup (1) increase and goes up the partial pressure of transferring to the solute dividing potential drop in the gaseous mixture (3) that is lower than that produces.Be understandable that when the dividing potential drop of the gaseous mixture of the solute of removing (5) surpassed normal atmosphere, Reduced pressure source (29) can be an atmosphere in containing by syrup.For embodiments more of the present invention, as mentioned above, can by increase mixed flow (19) therein the internal volume of mobile conduit produce Reduced pressure source (29).Also can pass through vacuum pump, Venturi tube or other device generation Reduced pressure source (29) that links to each other by fluidics device separated from the gas (27).Can (for example be lower than normal atmosphere) as required subsequently the surface-area (4) that increases in syrup is gone up the dividing potential drop gas that produces and regulate the speed that the gaseous mixture (3) that contains solute (5) with raising migrates out from syrup mixed flow (19).

For some specific embodiments, gas separator may further include safety valve (30) or further comprises signal generator (31), it links to each other with Reduced pressure source (29), can gather the gas in the gas separator (27) or dividing potential drop gas responds, or the rising of the reduction of the reduction of the minimizing of solute in the syrup (total soluble matter, some solute, solute concentration or some solute concentration), syrup acidity, syrup basicity, syrup pH value or other are represented that migrating out measuring of abundant solute from syrup (1) responds.

The present invention comprises that further this storage or transportation are avoided all or part of gaseous mixture is discharged in the atmosphere to containing storage or the transportation by the gaseous mixture (32) of the solute of removing in the syrup.In some embodiment of the present invention, the gaseous mixture that contains by the solute of removing in the syrup (for example containing carbonic acid gas) can be used for for example above-mentioned carbonation step.

The present invention can also be included in and add antifoams (33) in the syrup (1).Contain in the syrup and have the capillary material that surfactivity maybe can change water in a large number.Therefore, entrained air in the syrup or the solution gas transferred to the atmosphere from syrup know from experience to produce foam.There are many antifoams that can be used for reducing foam volume.Include but not limited to lipid acid, oils or similar substance.In order to be implemented in the middle injecting gas mixture (3) of syrup (1) as mentioned above or to shift the gaseous mixture (3) that contains some solutes (5) at least, can further need in syrup being exposed to required gaseous mixture (3) or in syrup, inject the step that simultaneously or almost simultaneously adds antifoams of this gaseous mixture.

In case from syrup (1), migrate out solute, volatile matter, gas dissolved, water-soluble acid or the similar substance of predetermined amount, just the syrup product that obtains can be transported in the existing sugar mill further to clarify or to purify.Perhaps, various embodiments of the present invention can be incorporated in the sugar mill to make the syrup that solute content reduces on the spot.

Referring now to Fig. 5, improve the sugaring system of pH value for the alkali that uses calcium oxide for example or calcium hydroxide and so on the iso-electric point that reaches the middle various materials of dissolved of syrup (1) at first, or as the sugaring system of the part of the traditional method of preliming syrup (33), its can with the cold ash (34) that adds, main add other step that ash (35) or centre add ash (36) and so on and separate or combination, these steps can be separated or combination with the first carbonation step (37) or the second carbonation step (38) of catching at least a portion non-sucrose in the syrup (1) with generation lime carbonate (39) throw out again, can filter (44) to clarification or the purification juice that obtains before at the water (45) of evaporation predetermined amount like this, the method and apparatus that the present invention relates to can be used for making the syrup product that solute content reduces or gas dissolved content reduces, these method and apparatus can be incorporated in one or more in these conventional procedures or all, perhaps through to a certain degree transformation with in the conventional procedures of benefiting from the syrup characteristic of handling according to the present invention.

Can recognize that the present invention reduces solute before being used in and adding any alkali.Because the present invention can fully improve the pH value of syrup or reduce the acidity of syrup, therefore can reduce traditional preliming or the main used alkali number of grey step that adds.Perhaps, use the underflow (for example used lime) of systems of processing to neutralize or be used for reducing in the system of processing of foaming, can before or after adopting the present invention, add underflow greater than a part of acid in the syrup at those.

Particularly, use the purify method of syrup of the present invention can comprise and from plant materials (2), obtain syrup (1), wherein contain sucrose, non-sucrose and water in the syrup as mentioned above.With shown in or described various embodiment use the present invention so that improve the pH value of syrup or the acidity of reduction syrup before syrup being carried out preliming (33).Syrup (1) is carried out cold master to be added ash (34) and/or the main process that adds ash (35) of heat and can combine with carbonating (37) (38) and carry out.In preliming (33) or main adding when using calcium oxide or calcium hydroxide as alkali (46) in ash (34) (35) step, the carbonation step (37) that is settled out lime carbonate (39) can be caught at least a portion non-sucrose in the syrup (1).These throw outs (39) can be by separating the non-sucrose of catching to remove with syrup (1) with throw out (39).In embodiments more of the present invention, can carry out the centre with the carbonation of appending (38) and add ash (36) step.Precipitated chalk (39) can be removed the non-sucrose of catching once more.Removing lime deposit (39) can obtain a kind ofly removing can produce the syrup (1) of required syrup (46) to aequum will containing the water yield (45).Perhaps, the sucrose that makes in the syrup to be contained carries out crystallization (47), can produce sugar product (48).

Now mainly with reference to Fig. 6, about adopting the sugaring system of the traditional lime carbonate purification step in the above-mentioned sugaring of ion-exchange (49) the replacement system, from United States Patent (USP) 3,785,863,4,331,483 or 4,140, can learn in No. 541 (being hereby incorporated by), for example can use that the alkali of lime and so on carries out pre-treatment to syrup so that make it in the easier before filtration of ion-exchange step (49), thereby make ion exchange material regeneration to produce calcium form, change the polarity load in the syrup (polar load) into calcium like this, or behind ion exchange process, reduce the acidity of syrup.

In the technology of these types, the present invention is used in before the syrup pre-treatment or with the syrup pre-treatment amount of solute or gas dissolved is reduced, or the acidity of syrup is reduced, or the polarity load of syrup is reduced, or the acidity of syrup is reduced.Can realize above-mentioned projects by process syrup according to the present invention.

Now mainly with reference to Fig. 7, about adopt filtering or ultrafiltration process replaces the sugaring system of the traditional lime carbonate purification step in the above-mentioned sugaring system, from United States Patent (USP) 4,432, can learn in No. 806 (being hereby incorporated by), for example can use the alkali of lime and so on that syrup is carried out pre-treatment and make its easier filtration (50).

In the technology of these types, the present invention is used in alkali and syrup is carried out pre-treatment so that non-sucrose reaches the amount minimizing that solute or gas dissolved are also assembled before or made simultaneously to its iso-electric point, or the acidity of syrup is reduced, perhaps otherwise produce the solia particle that can partly filter out from the remaining liq of syrup.Can realize above-mentioned projects by process syrup according to the present invention.

Mainly with reference to Fig. 8, the present invention can comprise that these equipment or method have utilized the pH in these liquid to reduce material than low solubility to containing liquid sucrose or leaching equipment or the method that syrup is processed now.When heating contains liquid sucrose, comprise CO ₂And SO ₂And so on gas can reduce in some interior solubility of substances.Therefore, even when these materials can not shift or can not further transfer in this dividing potential drop gas, also can on the interface between the mixture of these liquid and dividing potential drop gas, cause or promote the discharge of these materials from these liquid under lower fluid temperature.

Now mainly with reference to Fig. 9, it represents a specific embodiment of the present invention, wherein in the mixing tank that has travelling belt or other handling equipment usually (52), add sugar beet silk (51), perhaps can use pump (54) directly sugar beet silk (51) to be added in the cossettes extraction unit (53).In the specific embodiment of the present invention that sugar beet silk (51) is added in the mixing tank (52), sugar beet silk (51) can contact with part or all of leaching syrup or effluent (55) from cossettes extraction unit (53) in mixing tank (52) earlier before transporting to cossettes extraction unit (53) by pump.

In extraction unit (53), with hot water (59) (usually between 50 ℃ to 80 ℃) the sugar beet silk is handled, sometimes adopt convection type, so that sugar beet juice (can contain above-mentioned various other solubility and insoluble substance and material) is shifted out (remove) or shifts (transfer) in hot water (59) from sugar beet silk (51).Collecting the hot water (59) that contains the sugar beet juice that lixiviate goes out from sugar beet silk (51) (being called " leaching syrup " sometimes) now also is transported in the mixing tank (52) by the form of pump (60) with single current fluid stream or multithread fluid stream (55) (58).

Importantly, although the extraction unit technology has been used decades, do not know also that before the present invention extraction unit (53) itself can stop or reduce that the leaching syrup that contains a certain amount of some material that can be reduced according to the present invention or material or extraction unit migrate out some material with liquid or pH reduces material from being used for generating.The specific embodiment of the present invention has been utilized the temperature of employed rising in sugar beet silk leaching process, the temperature of this rising makes extraction unit liquid, beet pulp liquid, some solubility of substances that leaching syrup etc. contains reduces to remove, reduce or shift some material or material, for example alcohol, aldehyde, ketone, ester, nitrile, thioether, pyrazine, carbonic acid gas, carbonic acid, sulfurous gas, phosphoric acid, hydrochloric acid, sulfuric acid, sulfurous acid, citric acid, oxalic acid, succsinic acid, fumaric acid, lactic acid, oxyacetic acid, pyrrolidone-carboxylic acid, formic acid, acetate, butyric acid (butyric acid), toxilic acid, propionic acid, 3 Methylbutanoic acid, butyric acid (butanoic acid), valeric acid, the 5-methylhexanoic acid, caproic acid, enanthic acid or lactic acid.

In structure of the present invention (for example Fig. 1 to 7 and 11,12,13 and described herein those structure) in the comparatively high temps (pH reduce material than low solubility) that utilizes leach liquor or leach syrup to leaching monitoring, assessment and the control of syrup, beet pulp liquid or other leach liquor, can in extraction unit (53) itself or at all places shown in Figure 9 (200) (201) (202), locate to carry out, so that between extraction unit (53) and prelimer (57), the beet pulp pressed liquor is handled or handled to leaching syrup.Can connect and add well heater (T) (203) (204) and reach or remain on syrup temperature between about 60 ℃ to about 80 ℃ so that make syrup or leach syrup.Syrup is reached the various embodiment that has well heater of the present invention or to remain on about 60 ℃, about 61 ℃, about 62 ℃, about 63 ℃, about 64 ℃, about 65 ℃, about 66 ℃, about 67 ℃, about 68 ℃, about 69 ℃, about 70 ℃, about 71 ℃, about 72 ℃, about 73 ℃, about 74 ℃, about 75 ℃, about 76 ℃, about 77 ℃, about 78 ℃, about 79 ℃, about 80 ℃ or other temperature required.

Thus, there are many specific embodiment of the present invention, it demonstrates the structure of various use extraction units and sugar beet silk microwave leaching technology, in these structures some (demonstrate exemplary position (200) (201) (202) as shown in Figure 9, on these positions, lay of the present invention various structures shown in Figure 10 to 13 or hereinafter described), these structures provide abundant carrying out and have used the illustrated example of various embodiments of the present invention.These illustrated example are not considered as having limited various other embodiments that do not indicate.

Some embodiment of the present invention comprises the controlled exchange speed of atmosphere dividing potential drop, or the dividing potential drop gas in the maintenance extraction unit, and this dividing potential drop gas makes and additionally migrate out material or pH reduction material in extraction unit (53) from the leaching syrup (205) of heating.In embodiments more of the present invention, extraction unit (53) thereby can be transformed into is connected with the atmosphere fluid extraly can strengthen the exchange that the lip-deep atmosphere dividing potential drop of syrup is leached in heating.In other embodiments of the present invention, when the structure that can not transform extraction unit exchanges with the normal atmosphere in the enhancing extraction unit (53), flow generator (64) can be installed.The ventilation (63) that increases can be reached balance with the air-flow of formation in the extraction unit (53).Some material is transferred to assessment element (65) that the process the air-flow monitors from extraction unit with liquid can be provided about leaching extraction unit on the syrup interface with the information of the exchange of substance speed between liquid or the atmosphere dividing potential drop (or other selected gaseous mixture or dividing potential drop gas).

Now mainly with reference to Figure 10, other embodiments of the present invention comprise that utilizing pump (60) or other means of delivery will heat leaching syrup (66) transfers in the container (67), have increased the surface-area of heating leaching syrup (66) like this so that reduce the concentration of pH reduction material to a greater degree and (or have reached for example COA ₂Or SO ₂And so on pH reduce the predetermined amount of material) or make pH reduce material more promptly to leach the syrup and migrate out from heating.Heating leach surface-area (or required surface-area of variable adjustment) that syrup (66) increases can by inject required dividing potential drop gas (in order to carry out stripping) to leaching syrup with aforesaid variety of way obtain, quilt sprayed into container or is transported on the area substrate of increase.

Some embodiment of the present invention comprises the container (67) that has the top of fully opening wide, and the bottom of fully opening wide can further be provided, and (it can reduce opening size for simplicity so that the leaching syrup that will handle is transported in mixing tank, settling bowl (68) or pump (56) (54) or other transfer equipment.Add near can be from container (67) top from the heating syrup (66) of extraction unit, so that heating syrup (66) has the surface-area that increases to a great extent with respect to the atmosphere dividing potential drop in the container.As shown in figure 10, a specific embodiment of the present invention adds the heating syrup near container (67), make the heating syrup be distributed on the inwall and have enough strength so that descending to increase the residence time in container (67) to the inside turn of small part height at internal surface.

For embodiments more of the present invention, when container (67) only was used to hold leaching syrup with collection and treatment, the mode that adds the heating syrup in container (67) can be the method that increases heating syrup (66) surface-area.In these embodiments of the present invention, can be improved so that produce the extra surface-area that fluidics links to each other with atmosphere or required dividing potential drop gas that passes through the structure of liquid flow of heating syrup by stirring, pulse, be divided into many tributaries, spraying, formation drop or alternate manner.

Other embodiments of the present invention can utilize the structure of container (67) to make full use of the increase that syrup (66) surface-area is leached in heating.For example, container can have circle or tepee structure or or even the variable adjustment structure, this structure controllably increases or reduces the surface-area that adds the lip-deep heating syrup of container (67) and the residence time on vessel surface.For embodiments more of the present invention, this container can make the diameter of the conduit (69) that the conveying syrup that links to each other by fluidics and atmosphere dividing potential drop or required dividing potential drop gas (conduit reduces material with the pH to the leaching syrup of heating or unwanted stripping component is carried out stripping but this dividing potential drop gas can inject) uses increase.

In some embodiment of the present invention, with the contacted dividing potential drop gas of surface-area of heating syrup can be by finding time or the predetermined exchange of selected gaseous mixture is controlled, thereby the required dividing potential drop gas concentration that keeps constantly reducing leaches designated gas or the material that migrates out the syrup to increase from heating, comprises aforesaid stripping.

Now mainly with reference to Figure 11, another each embodiment of the present invention can comprise pump (70) and other liquid transfer element in case the injection port of gas syringe (71) reach enough production with liquid pressure (per square inch about 20 pounds to per square inch between about 25 pounds).As mentioned above, can with produce with liquid heat between about 50 ℃ to about 80 ℃ so that should produce and used in the liquid for example CO ₂, SO ₂And so on gas, the solubleness of producing with volatile organic compounds in the liquid or volatility mineral compound reduce.As required injection port (71) injects air or other dividing potential drop gas in producing usefulness liquid after, can transfer in the gas-liquid separator (72) with liquid producing, this separator is the centrifugal gas-liquid separator that can reach about 4 times of gravity in embodiments more of the present invention.Gas-liquid separator (72) makes to inject to produce with the dividing potential drop gas of liquid can transfer to gas dissolved, volatile organic compounds or volatility mineral compound atmosphere to reduce these materials in the concentration of producing with liquid.In embodiments more of the present invention, gas-liquid separator can be to hold the container of producing with liquid to increase atmosphere-production with the mode of liquid surface, and this makes material to transfer to the atmosphere with liquid from producing in the shorter time.When using centrifugal gas-liquid separator, to producing the centrifugal force that applies with liquid production is spread on the internal surface of cylindrical vessel (although also can use other structure) with liquid, centrifugal force is about 4 times of gravity in round shape embodiments more of the present invention.Production is spread over liquid on the internal surface of cylindrical vessel of centrifugal gas-liquid separator, can make the area increase of atmosphere (or other dividing potential drop gas)-productions usefulness liquid surface like this by the mode that keeps a gas column (produce and to transfer in this root gas column) at cylindrical center with the gas in the liquid.Gas is discharged system (73) can make dividing potential drop gas from producing with transferring in the atmosphere the liquid.In embodiments more of the present invention, can enter the preliming step of traditional sugaring system or enter aforesaid other procedure of processing with liquid with the production of liquid trap (72) from gas-production.

For other embodiments of the present invention, pump (74) or other are produced will produce with liquid with liquid transfer element and are transported in the liquid dispersion element (76) of nozzle and so on for example so that so that atmosphere (or other dividing potential drop gas)-productions with the mode of liquid surface area increase production is distributed with liquid.In some embodiments, liquid dispersion element (76) can produce drop or spraying.Gas distribution manifold (77) or other gas distribution elements air or other dividing potential drop gas are moved through produce with in the liquid dispersion so that gas is distributed producing with the gas dissolved in the liquid, volatile organic compounds or volatile acid or similar substance and the dividing potential drop inter gas by the gas distribution manifold adding.In some cases, this dividing potential drop gas stream that adds by gas distribution manifold (77) can form convection current with liquid with the dispersion production from liquid dispersion element (76) direction, thereby makes gas distribute (gas partitioning) or stripping process more effective.Can further add foam dispersion element (78) to break the foam that liquid generates in gas distribution or stripping process.Can use the sieve mesh or the sieve in aperture with suitable dimension.Liquid dispersion element (76), gas distribution manifold (77) and foam dispersion element (78) can be positioned at container (79) or gas partition column.Can determine the airshed of input gas distribution manifold (77) with gas delivery element (80).Can be based on the conditioned disjunction production in the container (79) being carried out separate analysis with the electrochemical conditions in the liquid or analysis-by-synthesis is regulated airshed.In embodiments more of the present invention, produce the preliming step that can enter traditional sugaring system with liquid, or enter aforesaid other procedure of processing.

Some embodiment of the present invention may further include can be to wherein importing the vacuum chamber of producing with liquid (84).Can be to the pressure adjustment in the vacuum chamber (84) or adjusting so that from through the production of this vacuum chamber (84) volatile matter (or reaching required pH value) with transfer aequum the liquid volume.Can by vacuum pump or in embodiments more of the present invention liquid movement by the delivery pipe system (88) (89) (90) that flows through produce vacuum in the vacuum chamber.The production that enters in the vacuum chamber (84) also can be regulated and can disperse to produce with liquid-gas interface area to increase through the second liquid dispersion element (82) with the amount of liquid by liquid control valve (81).To produce then with liquid and from vacuum chamber (84), transfer in the preliming step of traditional sugaring system, or enter aforesaid other procedure of processing.

The present invention further comprises the exhaust system (91) that is made of various assemblies (72) (79) (84) (90), transfer in the exhaust gas collection container (93) with liquid foam with liquid or production in order to the production that will overflow, can in this container, add antifoams by antifoams dispersive element (92).Then the production of collecting in the exhaust gas collection container (93) is transferred to the preliming step of traditional sugaring system from vacuum chamber (84) with liquid, or entered aforesaid other procedure of processing.

Now mainly with reference to Figure 12 and 13, a specific embodiment of the present invention can comprise the syrup treatment system of being furnished with syrup distributed component (300), and the non-limitative example of this distributed component can be full side's fog nozzle of BEX PSQ or the full side's fog nozzle of BEX PSWSQ wide-angle (300).Referring to embodiment.Syrup (301), no matter whether heat as mentioned above, can be distributed to have can make at least a material from described syrup is transferred to the gas (302) or gaseous mixture or dividing potential drop gas of the gas characteristic the described gas (for example atmospheric gas replenish or stripping to the atmospheric gas of required dividing potential drop).Variable adjustment flow generator (303) remains on described air-flow (302) to be enough to keep described at least a material is transferred under the state of gas characteristic the gas (302) (dividing potential drop gas, gas volume, gas residence time, gas velocity, or the like) from described syrup.Gaseous emission element (304) can make the gaseous emission that contains the material that migrates out from syrup in atmosphere or be brought to the desired position or be discharged in the required course of processing or enter in the required procedure of processing.Can form air-flow (302) by single gaseous emission position or a plurality of gaseous emissions position (305).In some embodiment of the present invention, gas at first enters in the gas distribution elements (310), gas distribution ring for example shown in Figure 13 (many perforates (313) are arranged in the ring).Gas distribution elements is used for producing the required convection current or the stream condition of other form at container (312).

For example, with about 60 to about 100 cubic feet/min (about 500 to 133 gallon per minute) dispersive syrup (301), leach syrup, the beet pulp syrup, extraction unit liquid, or syrup production with liquid dispersion in the air-flow that produces with the speed of about 450 to 850 cubic feet/min, some material is transferred to from syrup in the air-flow, and these materials are alcohol for example, aldehyde, ketone, ester, nitrile, thioether, pyrazine, carbonic acid gas, carbonic acid, sulfurous gas, phosphoric acid, hydrochloric acid, sulfuric acid, sulfurous acid, citric acid, oxalic acid, succsinic acid, fumaric acid, lactic acid, oxyacetic acid, pyrrolidone-carboxylic acid, formic acid, acetate, butanic acid (butyric acid), toxilic acid, propionic acid, 3 Methylbutanoic acid, butyric acid (butanoic acid), valeric acid, the 5-methylhexanoic acid, caproic acid, enanthic acid and lactic acid etc.For the specific embodiment of the invention of those structures shown in for example Figure 12 and 13, use air-flow (302) (unit is a cubic feet) that institute disperses four times of syrup (301) amounts with minimizing by the various amount of substances in the leaching syrup of sugar beet acquisition.Referring to embodiment 1 to 3.Similarly, can be similarly to handling by pulverizing the syrup that sugarcane obtains, and obtain similar result.Amount according to dispersion syrup and generation air-flow, correspondingly determine the size of this structure, and can serial or parallel connection use and comprise that a plurality of assembly of the present invention handles the syrup that typical sugar beet processing units (per minute leaches syrup for 1000 to 5000 gallons usually) is produced.

Some embodiment of the present invention further comprises the air-flow (307) that the flow generator (306) supplied is supplied with generation, and this air-flow can contain aerobic, ozone, some dividing potential drop gas has been carried out steam stripped air, primary alconol can have been changed into the aldehyde of response or the oxygenant of carboxylic acid.Perhaps, the specific embodiment of the present invention further comprises the oxygenant of supplying (308), and it can be distributed to by nozzle (311) and disperse in the syrup.

As mentioned above, when described syrup (301) be distributed to described have make at least a material when described syrup is transferred in the gas (302) of the gas characteristic the described gas, well heater (309) can make syrup reach or remain on and be selected under 60 ℃ to the 80 ℃ substantially invariable temperature in the scope.For different embodiments of the present invention, when described syrup (301) be distributed to described have make at least a material when described syrup is transferred in the gas (302) of the gas characteristic the described gas, syrup has and is selected from about 60 ℃, about 61 ℃, about 62 ℃, about 63 ℃, about 64 ℃, about 65 ℃, about 66 ℃, about 67 ℃, about 68 ℃, about 69 ℃, about 70 ℃, about 71 ℃, about 72 ℃, about 73 ℃, about 74 ℃, about 75 ℃, about 76 ℃, about 77 ℃, about 78 ℃, about 79 ℃ and about 80 ℃ temperature.

Embodiments more of the present invention may further include traverse baffle (311) so that disperseed syrup (301) and have make at least a material transfer to the gas of the gas characteristic the described gas from described syrup (interfacial area between 302 increases.

The syrup of carrying out is as mentioned above handled and can be carried out in first container (312) as shown in figure 13, the syrup that to handle is transferred to prelimer (57) or other procedure of processing from outlet (314) after this, maybe it can be transferred in second container (315).In those syrups that will handle are transferred to embodiment in second container, can syrup (301) be disperseed once more by at least one second dispersive element (316).Decompression producer (317) can make described second container (316) thus in pressure reduce and to make the partial pressure of at least a material that is shifted out by described syrup transfer reduce to lower partial pressure (318).

The decompression producer makes and reaches in second container (315) and keeps being enough to making dispersion syrup (102) ebullient lower pressure.Lower pressure (318) in second container (315) can be according to the difference of the temperature of disperseing syrup (301), composition and change or adjust (automatic or manual).Stripping gas flow-generator (319) desorb air-flow (320) can be added second container (315) thus in the substance transfer that volatilizes in atmosphere.Stripping gas (320) comprises air, atmospheric gas, nitrogen, oxygen, other designated gas.

Some embodiment of the present invention comprises that further an auxiliary gas reduces producer (gas reduction generation) (321) and makes dispersion syrup (301) boiling or keep boiling in second container (315) to help gas to reduce producer (317).

Be similar to first container (312), also can include traverse baffle (311) in second container (315) with the interfacial area between the gas (318) that increases syrup (301) and reduction dividing potential drop.

Some embodiment of the present invention also comprises the 3rd container (322), wherein the pressure that can form as mentioned above or keep reducing.Syrup (301) can through outlet (323) from second container (315) transfer be shifted out and by to first and second containers similar syrup distribution member be distributed in the 3rd container.Perhaps, the syrup (301) of leaving second container (315) can directly be transferred in preliming step or filtration step or other step or the process as required.

The example of these embodiments of the present invention specifically is used to explain following universal: utilize the phenomenon of the syrup of heating to the solubleness reduction of some material, gas, volatile compound, acid or similar substance, by before the preliming step, controlling and/or make the surface-area increase that the heating syrup contacts with required dividing potential drop gas, definitely the concentration of these materials is monitored, assessed or controls heating the dividing potential drop gas that leaches the existence of syrup surface.Advantage of the present invention is considered to be to add a spot of alkali (for example lime) just can control foamed phenomenon in the course of processing of syrup before the preliming step.

Embodiment 1

Obtain syrup by the sugar beet silk being carried out traditional tower lixiviate.Form each by six parts of 500 milliliters of substantially the same control group and experimental group that leaching syrup aliquots containig is formed.Each part aliquots containig in control group and the experimental group is analyzed to determine its pH value.Leach the syrup aliquots containig for each part in the control group, its pH value is about 6.3.Just use the titration of 50%wt./vol. soda lye to the 11.2pH terminal point without further handling each part aliquots containig in the control group.According to the present invention each part aliquots containig in the experimental group is handled, is determined the pH value of each part aliquots containig subsequently, and with each part experiment aliquots containig usefulness 50%wt./vol. soda lye with control group mode titration much at one to the 11.2pH terminal point.

The result lists in following table 1.As can be seen from the table, the pH value of carrying out each part syrup aliquots containig before any processing is approximately 6.3.Experimental group after handling according to the present invention is compared with control group, and the pH value raises to some extent under the situation that does not add any alkali, and needs more a spot of caustic soda just can reach the 11.2pH terminal point.

Table 1

The pH value of the syrup that is untreated	Caustic alkali ML	The pH value of the syrup of handling	Caustic alkali mL	The % reduction of caustic alkali
The pH value of the syrup that is untreated	Caustic alkali ML	The pH value of the syrup of handling	Caustic alkali mL	The % reduction of caustic alkali	6.3	1.8	6.5	1.5	16.6
6.3	1.8	6.6	1.4	22.2	6.3	1.8	6.5	1.5	16.6
6.3	1.8	6.6	1.4	22.2	6.3	1.8	6.6	1.4	22.2
6.3	1.9	6.6	1.6	15.8	6.3	1.8	6.6	1.4	22.2
6.3	1.9	6.6	1.6	15.8	6.3	1.9	6.5	1.5	21.0
6.3	1.9	6.5	1.6	15.8	6.3	1.9	6.5	1.5	21.0

Compare with the syrup aliquots containig in the undressed control group, the syrup aliquots containig in the experimental group of handling according to the present invention reaches the required causticity alkali number of 11.2pH terminal point and has reduced about 15.8% to about 22.2%.

Embodiment 2

Obtain syrup by the sugar beet silk being carried out traditional tower lixiviate.Form control group and experimental group that each is made of 5 parts of 500 milliliters of substantially the same leach liquor aliquots containigs.Each part aliquots containig in control group and the experimental group is analyzed to determine the pH value.Leach the syrup aliquots containig for each part in the control group, its pH value is about 6.1.With each part aliquots containig in the control group without just further handling lime milk solution titration with 30 Brixs (brix) to the 11.2pH terminal point.According to the present invention each part aliquots containig in the experimental group is handled, is determined the pH value of each part aliquots containig subsequently, and with each part test aliquots containig with the lime milk solution of 30 Brixs with control group mode titration much at one to the 11.2pH terminal point.

The result lists in following table 2.As can be seen from the table, the pH that carries out each part syrup aliquots containig before any processing is approximately 6.1.Compare with control group according to the experimental group that the present invention handles, its pH value increases under the situation that does not add any alkali, and needs more a spot of milk of lime just can reach the 11.2pH terminal point.

Table 2

The pH of the syrup that is untreated	Milk of lime ml	The pH value of the syrup of handling	Milk of lime ml	The % reduction of milk of lime
The pH of the syrup that is untreated	Milk of lime ml	The pH value of the syrup of handling	Milk of lime ml	The % reduction of milk of lime	6.1	4.6	6.5	3.3	28.3
6.1	4.4	6.6	3.2	27.3	6.1	4.6	6.5	3.3	28.3
6.1	4.4	6.6	3.2	27.3	6.1	4.7	6.6	3.5	25.5
6.1	4.4	6.6	3.3	25.0	6.1	4.7	6.6	3.5	25.5
6.1	4.4	6.6	3.3	25.0	6.1	4.5	6.6	3.3	26.7

Compare with the syrup aliquots containig in the undressed control group, the amount that the syrup aliquots containig of the experimental group of handling according to the present invention reaches the required milk of lime of 11.2pH terminal point has reduced about 25.0% to about 28.3%.

Equally, institute's column data provides comparison to two kinds of dissimilar extraction equipments and leach extraction method in table 1 and the table 2.Importantly, data show that different extraction units or different leach extraction methods can produce the leaching syrup with visibly different pH value, even the pH value that every type microwave leaching technology produces can be inherent basically consistent.For example, the initial pH value of untreated leaching syrup is 6.1 in the table 2, and by comparison, the initial pH value of untreated leaching syrup is 6.3 in the table 1.

Embodiment 3

Obtain leaching syrup by the sugar beet silk being carried out traditional tower lixiviate, and, use the embodiment of the location between mixing tank and prelimer (location) shown in Figure 12 and 13 to handle according to the present invention.The leaching syrup that is distributed to (72 inches * 72 inches convection channel, wherein convection channel is high about 144 inches) in the big entraining air stream that produces with 400 cubic feet of speed of about per minute with the speed of 100 cubic feet of about per minutes makes multiple material shift from disperse syrup as the gas chromatography/mass spectrometry analysis as shown in following table 1 and 2 is indicated:

Table 1

The gas chromatographic analysis of table 1 expression sample SMBSC1 and SMBSC2 (by the enriched material that makes with the air-flow of syrup described herein after convective exchange), and the comparison carried out of the gas chromatographic analysis of the organic acid standard mixture sample that the chromatogram and the top 1-9 of those samples listed.As can be seen, the various organic acids that contained in the standard mixture of different quantities have been removed in the processing of syrup being carried out according to the present invention.

Table 2

The gas chromatography/mass spectrometry analysis of table 2 expression sample SMSBC5 D (by the enriched material that makes at the air-flow that does not use decompression and syrup temperature after carrying out convective exchange with syrup described herein under the situation between 60 ℃ to 70 ℃), the stratographic analysis of this sample shows that various volatile compounds are elevated to more than the baseline with the curvature that is occupied the majority by various alcohols.

Differentiate in these compounds each with GCMS, its kekule structures is in following table 3; List:

Table 3

Though have dissimilar extraction equipments and different leach extraction methods, but recognizing in the leaching process of the plant materials of sugar beet body or other type, those of ordinary skill in the art can not change or reduce the pH value, or do not recognize that different extraction equipments or diverse ways can generate syrup or the liquid with different pH values, or do not recognize the leaching syrup that can obtain to have low pH value than the extraction unit of novel type usually.Adopt identical microwave leaching technology or different microwave leaching technologies, microwave leaching technology generates the leaching syrup with different pH values, perhaps the improvement to microwave leaching technology has changed or has reduced the pH value that leaches syrup, thus, these the traditional method and instructions of the present invention of extracting syrup from plant materials greatly differ from each other as can be seen.

Be easy to find out from aforementioned content, can specifically implement key concept of the present invention in every way.The equipment that it comprises analytical technology and is used to finish suitable analysis.In this purposes, with the part of analytical technology as the result who obtains by described various device, or the inherent step is disclosed when using.It only is to use the natural result of predetermined or described equipment.In addition, though disclose some equipment, will be appreciated that these equipment not only realize some method, and can change in many ways.Importantly, for aforementioned all the elements, all these aspects all should be believed to comprise in its disclosed content.

The effect of basic explanation is played in the discussion that includes among the application.The reader should be clear, and all possible embodiment can not be clearly described in concrete discussion; Many alternative modes are implied with.It can not explain universal feature of the present invention fully, and can not show clearly each feature or key element are how reality is represented greater functionality or multiple alternative situation or equal key element.In addition, these are to imply in this disclosure.Describe when of the present invention when the terminology of determining with equipment, each parts of equipment all imply a kind of effect of playing.Not only comprise equipment claim, and comprise method or the process claim that indicates the present invention and each element role described equipment.Illustrate and terminology is not represented the restriction of claim scope that this paper is included.

Should also be understood that and under the situation that does not deviate from essence of the present invention, to carry out various changes.These changes also can lie in the specification sheets.It still falls within the scope of the invention.Contain embodiment clear and definite shown in comprising, various implicit alternative embodiment and the disclosure widely of main method or process etc. in the disclosure, and can rely on the support of the application's claim.It should be understood that and finished herein that any this language changes and claim widely.This complete patent application is used to support independently or contain as total system ground the patent of the numerous aspects of the present invention.

In addition, each key element of the present invention and claim also can realize with different methods.The disclosure should be understood to the change that comprises that each is such, as long as it is the embodiment change of any equipment embodiment, method or process embodiment or only is the change of these any key element.Especially, it should be understood that when the disclosure relates to each key element of the present invention, even the word of each key element can be expressed as suitable apparatus term or method term---have only function or come to the same thing.These are suitable, generalized or even more generally term should be considered as including in explanation to various key elements or effect.These terms can be substituted as required so that the general scope of authorizing right of the present invention is made clear.Take a single example, it should be understood that all effects can be expressed as equipment that causes this effect or the key element that causes this effect.Similarly, disclosed each physical element should be understood to and comprises disclosing effect that this physical element is facilitated.Consider this last aspect, take a single example, whether the disclosing of " syringe " should be understood to and comprise disclosing of " injection " effect---no matter clearly discussing---and conversely, and " injection " effectively openly should be understood to of acting on comprised " syringe " or or even the disclosing of " injection equipment ".This change and selectable term are considered to clearly include in this manual.

Any patent of mentioning in the present patent application, publication or other reference all are hereby incorporated by.In addition, as for employed each term, it should be understood that, unless its use in this application is inconsistent with interpreter, each term all includes general dictionary definition, and as all definition, alternative term and the synonym that are contained in Random House Webster ' s Unabridged Dictionary (the Random House Webster the does not have the abreviation voluminous dictionary) second edition all through being hereby incorporated by.Yet for above-mentioned every, information that these are incorporated herein by reference or statement can be inconsistent with patent content of the present invention, and thus, these statements obviously are not considered to be to be made by the applicant.

Therefore, the applicant requires following right at least: i) each syrup system of processing of disclosed herein and explanation, the methods involving of ii) open and explanation, iii) to each similar, suitable in these apparatus and method and even imply the change that has; Iv) realize as disclosed and described shown in the alternative design of each function; V) realize the alternative design and the method for each function that disclosed and described hint realizes; Vi) conduct separation and independently various features, component and the step shown in the invention; Vii) by disclosed various systems or component enhanced purposes; The viii) product that obtains by these systems or component; Ix) substantially as previously mentioned and with reference to the method and apparatus of any appended embodiment; X) the various combinations and the displacement of disclosed aforementioned each element; Xi) by means of computer or the above-mentioned the whole bag of tricks that carries out on computers; Xii) described programmable device as discussed above; (xiii) but carry out calculation of coding machine reading memory with the data that instruct the computer comprise equipment with described function as discussed above or element; Xiv) computer that is configured according to the open of this paper and explanation; Xv) as disclosed herein with the explanation independence or bonded sub-routine and program; Xvi) methods involving that discloses and illustrate; Xvii) to the similar, suitable of each system and method and even imply the change that has; Xviii) realize the alternative design of disclosed and described each function; Xix) realize realizing alternative design and the method shown in the disclosed and described function as hint; Xx) conduct separation and independently various device, component and the step shown in the invention; Xxi) above-mentioned every various combinations and displacement; And xxii) depends on the various possible dependent claims or the notion of listed every independent claim or notion.

It should be understood that the applicant just lists out at last has subordinative at first claim for the reason put into practice with for fear of adding possible hundreds of bar claim.It should be understood that,---include but not limited to EuropeanPatent Convention Article 123 (2) (European Patent Convention 124 articles the 2nd) and UnitedStates Patent Law (united states patent law) 35 U.S.C § 132 or other similar law---according to new things law (new matter laws) and have the support of required degree, promptly allow to be added in various appurtenants or other key element enumerated under independent claim or the notion, appurtenant or other key element under what its independent claim in office or the notion item also are like this.

In addition,, explain, use transitional term " to comprise " claim that maintenance " can be expanded " according to traditional claim if when using or using.Therefore, unless requirement is arranged in the literary composition in addition, being to be understood that term " comprises " (comprise) or for example " comprising " (comprises) or " comprising " mutation (comprising) and so on, is to infer to comprise described key element or step or key element group or step group but do not get rid of other any key element or step or key element group or step group.These terms should be understood so that give the applicant lawful covering scope the most widely with generalized form.

Claim listed in this specification sheets is quoted a part that becomes this specification sheets of the present invention through this; and the applicant clearly keeps and uses all or part of content that is contained in these claims that illustrate as a supplement to support any one or whole rights of claim or its any key element or component; the applicant further clearly keeps as required the arbitrary portion that these claims contained or full content or its any key element or component are moved on to (vice versa) in claims from specification sheets right; so that define the application or its any application case fully continuously; sub-application case or partial continuous application case scope required for protection; perhaps so that obtain patent law according to any country or treaty; the interests of rule or regulations reduction expense, and the content of these introducings should be present in the application and (comprises any application case fully continuously; cut apart application case or partial continuous application case or any rearrangement or expansion to it) phase whole co-pending in.

Claims

1. the method that the syrup that is obtained by plant materials is purified comprises the following steps:

A) obtain plant materials;

B) shift out syrup from the described plant materials of at least a portion, wherein said syrup contains sucrose, non-sucrose and water, and wherein a certain amount of described non-sucrose comprises solute;

C) described syrup is exposed in the gaseous mixture;

D) before adding alkali, the described solute of a part is transferred to the described gaseous mixture from described syrup;

E) between described syrup and described gaseous mixture, produce the interfacial surface area that increases;

F) improve the transfer rate of described solute from described syrup to described gaseous mixture; And

G) the described solute in the described syrup of minimizing.

2. the method that the syrup that is obtained by plant materials is purified as claimed in claim 1, the wherein said step that shifts out syrup from the described plant materials of at least a portion comprises carries out lixiviate to obtain described syrup to described plant materials.

3. the method that the syrup that is obtained by plant materials is purified as claimed in claim 1, the wherein said step that shifts out syrup from the described plant materials of at least a portion comprises mills to obtain described syrup to described plant materials.

4. the method that the syrup that is obtained by plant materials is purified as claimed in claim 1, wherein said plant materials is selected from sugarcane, sugar beet and sweet sorghum.

5. the method that the syrup that is obtained by plant materials is purified as claimed in claim 1, wherein said non-sucrose comprises at least a insoluble plant body, solubility plant materials, grogs, fertilizer, the carbohydrate except that sucrose, organic non-sugar, inorganic non-sugar, gas dissolved, organic acid, mineral acid, protein, phosphoric acid salt, carbanion, bicarbonate ion, metal ion, pectin, tinting material, Saponin/TSM, wax, fat and the gummy material of being selected from.

6. the method that the syrup that is obtained by plant materials is purified as claimed in claim 1, the described solute of at least a portion in the wherein said syrup comprises volatile matter.

7. the method that the syrup that is obtained by plant materials is purified as claimed in claim 1, the described solute in the wherein said syrup comprises gas dissolved.

8. the method that the syrup that is obtained by plant materials is purified as claimed in claim 7, the described gas dissolved in the wherein said syrup is selected from carbonic acid gas and sulfurous gas.

9. the method that the syrup that is obtained by plant materials is purified as claimed in claim 7, the gas dissolved in the wherein said syrup comprises the carbonic acid gas that exists with the form that is selected from carbon dioxide, carbanion, bicarbonate ion and carbonic acid.

10. the method that the syrup that is obtained by plant materials is purified as claimed in claim 7, the gas dissolved in the wherein said syrup comprises the sulfurous gas that exists with the form that is selected from sulfur dioxide gas, sulfuric acid and sulfurous acid.

11. the method that the syrup that is obtained by plant materials is purified as claimed in claim 1, wherein solute comprises water-soluble acid.

12. the method that the syrup that is obtained by plant materials is purified as claimed in claim 11, wherein said water-soluble acid is selected from phosphoric acid, hydrochloric acid, sulfuric acid, citric acid, oxalic acid, succsinic acid, fumaric acid, lactic acid, oxyacetic acid, pyrrolidone-carboxylic acid, formic acid, acetate, butyric acid, toxilic acid and lactic acid.

13. the method that the syrup that is obtained by plant materials is purified as claimed in claim 1, wherein said gaseous mixture are selected from atmospheric gas, filter atmospheric gas, air and filtrated air.

14. the method that the syrup that is obtained by plant materials is purified as claimed in claim 1, the wherein said step that interfacial surface area between described syrup and the described gaseous mixture is increased comprise described syrup is stirred.

15. the method that the syrup that is obtained by plant materials is purified as claimed in claim 1, the wherein said step that interfacial surface area between described syrup and the described gaseous mixture is increased comprises sprays to described syrup.

16. the method that the syrup that is obtained by plant materials is purified as claimed in claim 1, the wherein said step that interfacial surface area between described syrup and the described gaseous mixture is increased comprise described gaseous mixture is blasted in the described syrup.

17. the method that the syrup that is obtained by plant materials is purified as claimed in claim 1, the wherein said step that interfacial surface area between described syrup and the described gaseous mixture is increased comprises injects described syrup with described gaseous mixture.

18. the method that the syrup that is obtained by plant materials is purified as claimed in claim 1, the wherein said step that interfacial surface area between described syrup and the described gaseous mixture is increased comprises with described gaseous mixture carries out stripping to described syrup.

19. the method that the syrup that is obtained by plant materials is purified as claimed in claim 1, wherein:

A) described syrup is exposed in the gaseous mixture;

B) before adding alkali, the described solute of a part is transferred to the described gaseous mixture from described syrup;

C) interfacial surface area between described syrup and the described gaseous mixture is increased;

D) transfer rate of described solute from described syrup to described gaseous mixture improved; And

E) solute in the described syrup of minimizing.

The described step of above content that comprises comprises that described gaseous mixture is injected syrup to flow to form the mixed flow of described syrup and described gaseous mixture, and the described solute of at least a portion moves on to the described injecting gas mixture from described syrup circulation thus.

20. the method that the syrup that is obtained by plant materials is purified as claimed in claim 19, wherein said syrup stream comprises the Continuous Flow of syrup.

21. the method that the syrup that is obtained by plant materials is purified as claimed in claim 20, wherein said mixed flow comprises the successive mixed flow.

22. the method that the syrup that is obtained by plant materials is purified as claimed in claim 21, it further is included in the step that produces decompression on the described mixed flow.

23. the method that the syrup that is obtained by plant materials is purified as claimed in claim 22, it further comprises described syrup stream is disposed so that produce the step of described decompression on described mixed flow.

24. the method that the syrup that is obtained by plant materials is purified as claimed in claim 19, it further comprises described solute and the described mixed flow separation steps that will transfer in the described gaseous mixture.

25. the method that the syrup that is obtained by plant materials is purified as claimed in claim 24, it further comprises the step of response Reduced pressure source with the air-flow that produces the described gaseous mixture of separating from described mixing supply flow.

26. as claim 19, the 23 or 25 described methods that the syrup that is obtained by plant materials is purified, it further comprises the pressure on the described interface surface between described syrup and the described gaseous mixture is reduced to subatmospheric step.

27. the method that the syrup that is obtained by plant materials is purified as claimed in claim 1, the wherein said described step that described solute in the described syrup is reduced comprises that the concentration that makes oxonium ion in the described syrup reduces.

28. the method that the syrup that is obtained by plant materials is purified as claimed in claim 1, the wherein said step that described solute in the described syrup is reduced comprise that the ability that makes described syrup produce oxonium ion reduces.

29. the method that the syrup that is obtained by plant materials is purified as claimed in claim 1, the wherein said step that described solute in the described syrup is reduced comprises that the pH value with described syrup improves the amount that is selected from 0.1pH, 0.2pH, 0.3pH, 0.4pH, 0.5pH, 0.6pH, 0.7pH, 0.8pH, 0.9pH, 1.0pH, 1.1pH, 1.2pH, 1.3pH, 1.4pH, 1.5pH, 1.6pH, 1.7pH, 1.8pH, 1.9pH, 2.0pH.

30. the method that the syrup that is obtained by plant materials is purified as claimed in claim 29, it further may further comprise the steps: the alkali number in the syrup that the wherein said solute content that joins certain volume reduces is reduced, so that be based upon the initial pH value between about 11.0 and about 12.0.

31. the method that the syrup that is obtained by plant materials is purified as claimed in claim 29, it further may further comprise the steps: the alkali number in the syrup that joins a certain amount of wherein said solute content reduction is reduced, so that be based upon the initial pH value between about 11.5 and about 12.5.

32. the method that the syrup that is obtained by plant materials is purified as claimed in claim 29, it further may further comprise the steps: the alkali number in the syrup that joins a certain amount of wherein said solute content reduction is reduced, so that the corresponding pH value of iso-electric point of the described non-sucrose of at least a portion in foundation and the described syrup.

33. the method that the syrup that is obtained by plant materials is purified as claimed in claim 1, the described step that the described solute in the described syrup is reduced comprise the water-soluble acid that is produced by gas dissolved in the described syrup is reduced.

34. the method that the syrup that is obtained by plant materials is purified as claimed in claim 1, it further is included in and described syrup is exposed to before the described step in the gaseous mixture step of removing at least a portion insolubles from described syrup.

35. the method that the syrup that is obtained by plant materials is purified as claimed in claim 1, it further is included in and described syrup is exposed to after the described step in the gaseous mixture step of removing at least a portion insolubles from described syrup.

36. the method that the syrup that is obtained by plant materials is purified as claimed in claim 1, it further is included in after the described step that makes the described solute minimizing in the described syrup, adds the alkali of first quantity in described syrup.

37. the method that the syrup that is obtained by plant materials is purified as claimed in claim 36, the described step that wherein adds the alkali of first quantity after the described step that the described solute in making described syrup reduces in described syrup comprises the step of described syrup being carried out preliming.

38. the method that the syrup that is obtained by plant materials is purified as claimed in claim 36, the described step that wherein adds the alkali of first quantity after the described step that the described solute in making described syrup reduces in described syrup comprises carries out the cold step that adds ash to described syrup.

39. the method that the syrup that is obtained by plant materials is purified as claimed in claim 36, the described step that wherein adds the alkali of first quantity after the described step that the described solute in making described syrup reduces in described syrup comprises carries out the step that heat adds ash to described syrup.

40. the method that the syrup that is obtained by plant materials is purified as claimed in claim 36 wherein after the described step that reduces of the described solute in making described syrup joins the alkali of first quantity described step in the described syrup and comprises based on the minimizing of solute described in the described syrup add more a spot of alkali in described syrup.

41. the method that the syrup that is obtained by plant materials is purified as claimed in claim 36, it further is included in the described step that the described solute in the described syrup is reduced adds the alkali of second quantity afterwards in described syrup step, and this step comprises carries out the step that cold master adds ash to described syrup.

42. the method that the syrup that is obtained by plant materials is purified as claimed in claim 41, the described step that wherein adds the alkali of second quantity after the described step that the described solute in making described syrup reduces in described syrup comprises carries out the main step that adds ash of heat to described syrup.

43. comprising based on the minimizing of solute described in the described syrup, the method that the syrup that is obtained by plant materials is purified as claimed in claim 41, the described step that wherein adds the alkali of first quantity after the described step that the described solute in making described syrup reduces in described syrup in described syrup, add more a spot of alkali.

44. the method that the syrup that is obtained by plant materials is purified as claimed in claim 41, it further is included in the described step that the described solute in the described syrup is reduced adds the alkali of the 3rd quantity afterwards in described syrup step, and this step comprises carries out the main step that adds ash of heat to described syrup.

45. the method that the syrup that is obtained by plant materials is purified as claimed in claim 44, wherein in described syrup, add the described step of the alkali of the 3rd quantity after the described step that the described solute in making described syrup reduces, comprise described syrup is carried out the middle step that adds ash.

46. the method that the syrup that is obtained by plant materials is purified as claimed in claim 44 further is included in after the described step that makes the described solute minimizing in the described syrup, adds the alkali of the 4th quantity in described syrup.

47. as claim 36,41, the 44 or 46 described methods that the syrup that is obtained by plant materials is purified, wherein said alkali is selected from calcium oxide, calcium hydroxide and milk of lime.

48., further comprise the step that makes described syrup carbonation with the gas of first quantity as claim 36 or the 41 described methods that the syrup that is obtained by plant materials is purified.

49. the method that the syrup that is obtained by plant materials is purified as claimed in claim 48, the gas of wherein said first quantity is selected from atmospheric gas, air and carbonic acid gas.

50. the method that the syrup that is obtained by plant materials is purified as claimed in claim 48 comprises that further the gas by described alkali and described first quantity generates sedimentary step.

51., further comprise the step that makes described syrup carbonation with the gas of second quantity as claim 41 or the 44 described methods that the syrup that is obtained by plant materials is purified.

52. the method that the syrup that is obtained by plant materials is purified as claimed in claim 51, wherein said gas is selected from atmospheric gas, air and carbonic acid gas.

53. the method that the syrup that is obtained by plant materials is purified as claimed in claim 51 comprises that further the gas by described alkali and described second quantity generates sedimentary step.

54., further comprise the step that makes described syrup carbonation with the gas of the 3rd quantity as claim 44 or the 46 described methods that the syrup that is obtained by plant materials is purified.

55. the method that the syrup that is obtained by plant materials is purified as claimed in claim 54, wherein said gas is selected from atmospheric gas, air and carbonic acid gas.

56. the method that the syrup that is obtained by plant materials is purified as claimed in claim 54 comprises that further the gas by described alkali and described the 3rd quantity generates sedimentary step.

57. the method that the syrup that is obtained by plant materials is purified as claimed in claim 50 further comprises with described precipitation and catches the described non-sucrose of at least a portion in the described syrup.

58. the method that the syrup that is obtained by plant materials is purified as claimed in claim 53 further comprises with described precipitation and catches the described non-sucrose of at least a portion in the described syrup.

59. the method that the syrup that is obtained by plant materials is purified as claimed in claim 56 further comprises with described precipitation and catches the described non-sucrose of at least a portion in the described syrup.

60. the method that the syrup that is obtained by plant materials is purified as claimed in claim 57 further comprises described precipitation and described syrup of having caught described non-sucrose is carried out separation steps.

61. the method that the syrup that is obtained by plant materials is purified as claimed in claim 58 further comprises described precipitation and described syrup of having caught described non-sucrose is carried out separation steps.

62. the method that the syrup that is obtained by plant materials is purified as claimed in claim 59 further comprises described precipitation and described syrup of having caught described non-sucrose is carried out separation steps.

63. the method that the syrup that is obtained by plant materials is purified as claimed in claim 60 further comprises the step that the water yield that makes in the described syrup reduces.

64. the method that the syrup that is obtained by plant materials is purified as claimed in claim 61 further comprises the step that the water yield that makes in the described syrup reduces.

65. the method that the syrup that is obtained by plant materials is purified as claimed in claim 62 further comprises the step that the water yield that makes in the described syrup reduces.

66., comprise that further the sucrose that makes in the described syrup carries out the crystalline step as the described method that the syrup that is obtained by plant materials is purified of claim 63.

67., comprise that further the sucrose that makes in the described syrup carries out the crystalline step as the described method that the syrup that is obtained by plant materials is purified of claim 64.

68., comprise that further the sucrose that makes in the described syrup carries out the crystalline step as the described method that the syrup that is obtained by plant materials is purified of claim 65.

69. sugar according to the described method preparation of claim 66.

70. sugar according to the described method preparation of claim 67.

71. sugar according to the described method preparation of claim 68.

72. make the syrup of solute content minimizing according to claim 1,2,3,4,6,7,11,17,19,27 or 29 described methods.

73. make the syrup of water-soluble acid content minimizing according to claim 5,11,12 or 33 described methods.

75. the syrup that volatile matter content is reduced.

75. make the syrup of gas dissolved content minimizing according to claim 7,8 or 9 described methods.

76. the method that the syrup that is obtained by plant materials is purified comprises:

A) obtain syrup from plant materials, contain sucrose, non-sucrose and water in the wherein said syrup;

B) gas dissolved in the described syrup is reduced;

C) described syrup is carried out preliming;

D) described syrup is carried out cold master and add ash;

E) carry out the main ash that adds of heat;

F) carbonic acid gas of adding first quantity in described syrup;

G) make the precipitation of calcium carbonate of first quantity;

H) catch the described non-sucrose of first part with described lime carbonate;

I) the described non-sucrose of described first part is removed from described syrup with described lime carbonate;

J) described syrup is carried out the centre and add ash;

K) carbonic acid gas of adding second quantity in described syrup;

L) lime carbonate of second quantity is precipitated from described syrup;

M) catch the described non-sucrose of second section with described lime carbonate;

N) the described non-sucrose of described second section is removed from described syrup with described lime carbonate; And

O) make described crystallization of sucrose.

77., the described step that gas dissolved reduces in the described syrup is comprised the following steps: as the method for the described purification syrup of claim 76

A) stream of the described syrup of generation;

B) injecting gas mixture in the described stream of described syrup forms the mixed flow that comprises described syrup and described gaseous mixture; And

C) the described gas dissolved of a part is transferred to the described gaseous mixture from described syrup.

78. as the method for the described purification syrup of claim 77, wherein said syrup stream comprises the Continuous Flow of syrup.

79. as the method for the described purification syrup of claim 77, wherein said mixed flow comprises the successive mixed flow.

80., further be included in the step that produces decompression on the described mixed flow as the method for the described purification syrup of claim 79.

81., further comprise described syrup stream disposed so that produce the step of decompression on described mixed flow as the method for the described purification syrup of claim 80.

82., comprise that further the described gaseous mixture to contain the described gas dissolved that shifts from described syrup carries out separation steps as the method for claim 77 or 78 described purification syrups.

83., comprise that further the response Reduced pressure source contains the step of air-flow of the described gaseous mixture of the described gas dissolved that shifts with generation from described syrup as the method for the described purification syrup of claim 82.

84. as the method for the described purification syrup of claim 76, the wherein said step that gas dissolved in the described syrup is reduced comprises the steps:

A) generate the stream of described syrup, its interfacial surface area contacts with described gaseous mixture in the container by fluidics;

B) make the described interfacial surface area increase that is connected to the described syrup of described gaseous mixture by fluidics;

C) pressure in the described container is reduced; And

D) the described gas dissolved of at least a portion is transferred to the described gaseous mixture from described syrup.

85. as the method for the described purification syrup of claim 84, the wherein said step of the interfacial surface area increase of described syrup that makes comprises the drop that generates described syrup.

86. as the method for the described purification syrup of claim 76, the wherein said step of gas dissolved minimizing in the described syrup that makes comprises the steps:

A) described syrup is flowed first end of introducing container;

B) described syrup is spread on the distribution media in the described container;

C) described gaseous mixture is introduced second end of described container;

D) form convection current described spreading between described syrup on the described distribution media and the described gaseous mixture.

87. as the method for the described purification syrup of claim 76, wherein said plant materials is selected from sugarcane, sugar beet and sweet sorghum.

88. as the method for claim 76,77,84 or 86 described purification syrups, the described gas dissolved in the wherein said syrup is selected from carbonic acid gas and sulfurous gas.

89. as the method for claim 76,77,84 or 86 described purification syrups, the wherein said step that gas dissolved in the described syrup is reduced further comprises the step that the acid that makes in the described syrup reduces.

90. as the method for the described purification syrup of claim 89, wherein said acid is selected from carbonic acid, phosphoric acid, hydrochloric acid, sulfuric acid, citric acid, oxalic acid, succsinic acid, fumaric acid, lactic acid, oxyacetic acid, pyrrolidone-carboxylic acid, formic acid, acetate, butyric acid, toxilic acid and lactic acid.

91. the method that the syrup that is obtained by plant materials is purified comprises the following steps:

A) obtain plant materials;

B) shift out syrup from the described plant materials of at least a portion, wherein said syrup contains sucrose, non-sucrose and water, and wherein comprises solute to the described non-sucrose of small part;

C) described syrup is exposed in the gaseous mixture;

D) the described solute of a part is transferred to the described gaseous mixture from described syrup;

F) transfer rate of described solute from described syrup to described gaseous mixture improved;

G) amount of solute in the described syrup is reduced; And

H) the described gaseous mixture that contains by the described solute that shifts in the described syrup is separated.

92. the method that the syrup that is obtained by plant materials is purified comprises the following steps:

A) obtain plant materials;

B) shift out syrup from the described plant materials of at least a portion, wherein said syrup contains sucrose, non-sucrose and water, and wherein comprises volatile matter to the described non-sucrose of small part;

C) described syrup is exposed in the gaseous mixture;

D) the described volatile matter of a part is transferred to the described gaseous mixture from described syrup;

F) transfer rate of described volatile matter from described syrup to described gaseous mixture improved;

G) amount of volatile matter in the described syrup is reduced; And

H) the described gaseous mixture that contains the described volatile matter that is shifted by described syrup is separated.

93. a syrup purification system comprises:

A) syrup that obtains by plant materials, wherein said syrup contains sucrose, non-sucrose and water, and wherein said non-sucrose comprises at least a solute that makes the pH reduction of described syrup;

B) the lower gas of dividing potential drop of the described at least a solute of at least a intrinsic standoff ratio;

C) be used for described at least a gas and described syrup blended gas syringe mutually;

D) interface, here the described at least a solute of at least a portion is transferred to the described at least a gas from described syrup;

E) atmosphere that is connected with described interfacial phase by fluidics,

The described solute of at least a portion is transferred in the described at least a gas thus, so that the pH of described syrup raises.

94. as the described syrup purification system of claim 93, wherein said syrup comprises the syrup that is obtained by the plant materials that is selected from sugarcane, sugar beet and sweet sorghum.

95. as the described syrup purification system of claim 93, wherein said syrup comprises the liquid that is obtained by plant materials with the method that is selected from stripping and rolls,

96. as the described syrup purification system of claim 93, wherein solute comprises the carbonic acid gas that exists with the form that is selected from carbon dioxide, carbanion, bicarbonate ion and carbonic acid.

97. as the described syrup purification system of claim 93, wherein solute comprises the sulfurous gas that exists with the form that is selected from sulfur dioxide gas, sulfuric acid and sulfurous acid.

98. as the described syrup purification system of claim 93, wherein solute comprises water-soluble acid.

99. as the described syrup purification system of claim 98, wherein water-soluble acid comprises the water-soluble acid that is selected from phosphoric acid, hydrochloric acid, sulfuric acid, citric acid, oxalic acid, succsinic acid, fumaric acid, lactic acid, oxyacetic acid, pyrrolidone-carboxylic acid, formic acid, acetate, butyric acid, toxilic acid and lactic acid.

100. as the described syrup purification system of claim 93, the lower gas of dividing potential drop of the described at least a solute of wherein said at least a intrinsic standoff ratio is selected from atmospheric gas, filters atmospheric gas, washed atmospheric gas and Purge gas.

101. as the described syrup purification system of claim 93, the raising of wherein said pH is to take place under the situation that does not add alkali.

102. as the described syrup purification system of claim 101, wherein said alkali is selected from calcium oxide, calcium hydroxide and milk of lime.

103. as the described syrup purification system of claim 93, wherein said gas syringe has described at least a gas and described syrup stream blended structure.

104. as the described syrup purification system of claim 93, wherein said gas syringe has following structure: it comprises and has perforate so that with the gas delivery conduit of described at least a gas delivery in the described stream of described syrup.

105. as the described syrup purification system of claim 104, the described stream of wherein said syrup comprises, the Continuous Flow of the described syrup that described gas syringe is responded by fluidics.

106. as the described syrup purification system of claim 105, the described Continuous Flow of wherein said syrup has the flow velocity of variable adjustment.

107. as the described syrup purification system of claim 106, the flow velocity of wherein said variable adjustment responds to the described at least a concentration of the solute of described syrup pH reduction that makes.

108. as the described syrup purification system of claim 104, the stream of wherein said syrup comprises the intermittent flow of described syrup.

109. as the described syrup purification system of claim 93, wherein said at least a gas syringe can be to the dividing potential drop of the described at least a solute of at least a intrinsic standoff ratio the flow velocity of lower gas make variable adjustment.

110. as the described syrup purification system of claim 93, it further comprises the interfacial surface area of increase.

111. as the described syrup purification system of claim 93, it further comprises a gas distribution elements, so that described at least a gas is sneaked in almost whole volumes of described syrup.

112. as the described syrup purification system of claim 111, wherein said gas distribution elements comprises the impeller of pump.

113. as the described syrup purification system of claim 111, wherein said gas distribution elements comprises that reducing described syrup flows the size of mobile conduit therein.

114., further comprise the Reduced pressure source that described at least a gas and described syrup are responded as the described syrup purification system of claim 93.

115. as the described syrup purification system of claim 93, further comprise a gas separator that described at least a gas is responded, wherein said at least a gas further comprises from the next described at least a solute of part of described syrup transfer.

116. as the described syrup purification system of claim 93, further comprise the Reduced pressure source that described at least a gas is responded, wherein said at least a gas further comprises from the next described at least a solute of a part of described syrup transfer.

117. as the described syrup purification system of claim 116, wherein said Reduced pressure source comprises normal atmosphere.

118. as the described syrup purification system of claim 117, wherein said Reduced pressure source comprises vacuum pump.

119. a syrup purification system comprises:

A) contain the syrup of a certain amount of carbonic acid gas;

B) at least a gas that the interface of described syrup is responded, the dividing potential drop of wherein said at least a gas makes the carbonic acid gas of a part of described amount transfer to the described described at least a gas at the interface from described syrup;

C) at least one gas syringe, it is configured to the described at least a gas that described interface is responded is mixed mutually with described syrup;

D) gas separator that is connected with described at least a gas by fluidics, wherein said at least a gas further comprise the described part that shifts the carbonic acid gas of the described amount of coming from described liquid.

120. as the described syrup purification system of claim 119, wherein said syrup comprises the syrup that is obtained by the plant materials that is selected from sugarcane, sugar beet and sweet sorghum.

121. as the described syrup purification system of claim 119, wherein said syrup comprises the liquid that obtains from plant materials with the method that is selected from lixiviate and rolls.

122. as the described syrup purification system of claim 119, wherein said solute comprises the carbonic acid gas that exists with the form that is selected from carbon dioxide, carbanion, bicarbonate ion and carbonic acid.

123. as the described syrup purification system of claim 119, the wherein said at least a gas that interface with described syrup is responded, the dividing potential drop of wherein said at least a gas make the carbonic acid gas of a part of described amount transfer to the described described at least a gas that is selected from atmospheric gas, filtration atmospheric gas, washed atmospheric gas and Purge gas at the interface from described syrup.

124. as the described syrup purification system of claim 119, wherein said syrup has certain pH value, wherein under the situation that does not add alkali, along with the described part of the carbonic acid gas of described amount is transferred in the described at least a gas, the described pH value of described syrup raises.

125. as the described syrup purification system of claim 119, wherein said alkali is selected from calcium oxide, calcium hydroxide and milk of lime.

126. as the described syrup purification system of claim 119, wherein saidly be configured to make described at least a gas that described interface is responded and described syrup at least a gas syringe of blended mutually, comprise the gas delivery conduit that has the perforate that is connected with described syrup by fluidics.

127. as the described syrup purification system of claim 126, the described stream of wherein said syrup comprises the Continuous Flow of described syrup.

128. as the described syrup purification system of claim 127, the described Continuous Flow of wherein said syrup further comprises the flow velocity of variable adjustment.

129. as the described syrup purification system of claim 128, the flow velocity of wherein said variable adjustment responds to the carbonic acid gas of the described amount that contains in the described syrup.

130. as the described syrup purification system of claim 126, the described stream of wherein said syrup comprises the intermittent flow of described syrup.

131. as the described syrup purification system of claim 130, wherein intermittent flow responds to the carbonic acid gas of the described amount that contains in the described syrup.

132. as the described syrup purification system of claim 126, wherein said at least a gas syringe has the flow velocity of variable adjustment.

133. as the described syrup purification system of claim 119, the surface-area that wherein has variable adjustment with the described interface of described syrup.

134. as the described syrup purification system of claim 133, further comprise gas distribution elements, so that make described at least a gas distribution in almost whole volumes of described syrup.

135. as the described syrup purification system of claim 134, wherein said gas distribution elements comprises the impeller of pump.

136. as the described syrup purification system of claim 134, wherein said gas distribution elements comprises that reducing described syrup flows the size of mobile conduit therein.

137., further comprise the Reduced pressure source on the described syrup stream as the described syrup purification system of claim 119.

138. as the described syrup purification system of claim 137, wherein said Reduced pressure source comprises the normal atmosphere that is connected with the described interfacial phase of described syrup by fluidics.

139. as the described syrup purification system of claim 137, wherein said Reduced pressure source comprises the vacuum pump that is connected with the described interfacial phase of described syrup by fluidics.

140. the method that the syrup that is obtained by plant materials is handled may further comprise the steps:

A) obtain syrup from plant materials;

B) syrup is exposed to have at least a material is transferred in the gas of the characteristic the described gas from described syrup;

C) gas characteristic that at least a material will be transferred to the described gas from described syrup keeps one section to be enough to make the time that at least a amount of substance reduces described in the described syrup.

141. as the described method that the syrup that is obtained by plant materials is handled of claim 140, wherein said plant materials is selected from sugarcane, sugar beet and sweet sorghum.

142. as the described method that the syrup that is obtained by plant materials is handled of claim 140, the described step of wherein obtaining syrup from described plant materials comprises carries out lixiviate to obtain described syrup to described plant materials.

143. as the described method that the syrup that is obtained by plant materials is handled of claim 140, the described step of wherein obtaining syrup from described plant materials comprises mills to obtain described syrup to described plant materials.

144. as the described method that the syrup that is obtained by plant materials is handled of claim 140, wherein said at least a material is selected from gas, acid, volatile organic compounds, alcohol, aldehyde, ketone, ester, nitrile, thioether, pyrazine, carbonic acid gas, carbonic acid, sulfurous gas, phosphoric acid, hydrochloric acid, sulfuric acid, sulfurous acid, citric acid, oxalic acid, succsinic acid, fumaric acid, lactic acid, oxyacetic acid, pyrrolidone-carboxylic acid, formic acid, acetate, butanic acid, toxilic acid, propionic acid, 3 Methylbutanoic acid, butyric acid, valeric acid, 5-methylhexanoic acid, caproic acid, enanthic acid and lactic acid.

145. as the described method that the syrup that is obtained by plant materials is handled of claim 140, wherein said gas with gas characteristic is selected from gaseous mixture, air, filtrated air, oxygen and ozone.

146., further be included in described syrup is exposed to have and make at least a material transfer to the temperature that makes described syrup when described step in the described gas of the gas characteristic the described gas begins to reach step between 60 ℃ to 80 ℃ from described syrup as the described method that the syrup that is obtained by plant materials is handled of claim 140.

147., further be included in described syrup is exposed to have and at least a material transferred to from described syrup make described syrup remain on the step of the substantially constant temperature in the scope that is selected from 60 ℃ to 80 ℃ when described step in the described gas of the gas characteristic the described gas begins as the described method that the syrup that is obtained by plant materials is handled of claim 140.

148. as the described method that the syrup that is obtained by plant materials is handled of claim 140, wherein have when making at least a material transfer to described step in the described gas of the gas characteristic the described gas from described syrup to begin in that described syrup is exposed to, described syrup has and is selected from about 60 ℃, about 61 ℃, about 62 ℃, about 63 ℃, about 64 ℃, about 65 ℃, about 66 ℃, about 67 ℃, about 68 ℃, about 69 ℃, about 70 ℃, about 71 ℃, about 72 ℃, about 73 ℃, about 74 ℃, about 75 ℃, about 76 ℃, about 77 ℃, about 78 ℃, about 79 ℃ and about 80 ℃ temperature.

149. as the described method that the syrup that is obtained by plant materials is handled of claim 140, further be included in described syrup is exposed to and have the described step that at least a material is transferred in the described gas of the gas characteristic the described gas from described syrup and carry out in the process, described syrup is remained on be selected from the step of 60 ℃ to the 80 ℃ substantially constant temperature in the scope.

150. as the described method that the syrup that is obtained by plant materials is handled of claim 140, wherein have the described step that at least a material is transferred to from described syrup in the described gas of the gas characteristic the described gas and carry out in the process in that described syrup is exposed to, described syrup has and is selected from about 60 ℃, about 61 ℃, about 62 ℃, about 63 ℃, about 64 ℃, about 65 ℃, about 66 ℃, about 67 ℃, about 68 ℃, about 69 ℃, about 70 ℃, about 71 ℃, about 72 ℃, about 73 ℃, about 74 ℃, about 75 ℃, about 76 ℃, about 77 ℃, about 78 ℃, about 79 ℃ and about 80 ℃ temperature.

151., further comprise syrup is exposed to and reduce having of pressure and make at least a material transfer to step in the described gas of the gas characteristic the described gas from described syrup as the described method that the syrup that is obtained by plant materials is handled of claim 140.

152. as the described method that the syrup that is obtained by plant materials is handled of claim 151, wherein said reduction pressure comprises pressure below atmospheric pressure.

153. as the described method that the syrup that is obtained by plant materials is handled of claim 152, further be included in described syrup is exposed to and reduce having of pressure and make at least a material when described syrup is transferred to described step in the described gas of the gas characteristic the described gas and begun, make the temperature of described syrup reach step between 60 ℃ to 80 ℃.

154. as the described method that the syrup that is obtained by plant materials is handled of claim 140, further be included in described syrup is exposed to and reduce having of pressure and make at least a material when described syrup is transferred to described step in the described gas of the gas characteristic the described gas and begun, make described syrup keep being selected from the step of 60 ℃ to the 80 ℃ substantially constant temperature in the scope.

155. as the described method that the syrup that is obtained by plant materials is handled of claim 154, wherein reduce having of pressure when making at least a material transfer to described step in the described gas of the gas characteristic the described gas from described syrup to begin in that syrup is exposed to, described syrup has and is selected from about 60 ℃, about 61 ℃, about 62 ℃, about 63 ℃, about 64 ℃, about 65 ℃, about 66 ℃, about 67 ℃, about 68 ℃, about 69 ℃, about 70 ℃, about 71 ℃, about 72 ℃, about 73 ℃, about 74 ℃, about 75 ℃, about 76 ℃, about 77 ℃, about 78 ℃, about 79 ℃ and about 80 ℃ temperature.

156., further be included in syrup is exposed to and reduce the described step that having of pressure make at least a material transfer in the described gas of the gas characteristic the described gas from described syrup and carry out making in the process described syrup to remain on the step that is selected from 60 ℃ to the 80 ℃ substantially constant temperature in the scope as the described method that the syrup that is obtained by plant materials is handled of claim 152.

157. as the described method that the syrup that is obtained by plant materials is handled of claim 152, wherein carry out in the process syrup being exposed to the described step that at least a material is transferred to from described syrup in the described gas of the gas characteristic the described gas that has that reduces pressure, described syrup has and is selected from about 60 ℃, about 61 ℃, about 62 ℃, about 63 ℃, about 64 ℃, about 65 ℃, about 66 ℃, about 67 ℃, about 68 ℃, about 69 ℃, about 70 ℃, about 71 ℃, about 72 ℃, about 73 ℃, about 74 ℃, about 75 ℃, about 76 ℃, about 77 ℃, about 78 ℃, about 79 ℃ and about 80 ℃ temperature.

158., further comprise making described syrup and having making at least a material transfer to the step that the interfacial area of the described inter gas of the gas characteristic the described gas increases from described syrup as the described method that the syrup that is obtained by plant materials is handled of claim 140.

159., wherein make described syrup and have to make at least a material transfer to described step that the interfacial area of the described inter gas of the gas characteristic the described gas increases to comprise described syrup is distributed in the described gas from described syrup as the described method that the syrup that is obtained by plant materials is handled of claim 158.

160., wherein make described syrup and have to make at least a material transfer to step that the interfacial area of the described inter gas of the gas characteristic the described gas increases to comprise described syrup is sprayed in the described gas from described syrup as the described method that the syrup that is obtained by plant materials is handled of claim 158.

161. as the described method that the syrup that is obtained by plant materials is handled of claim 158, wherein make described syrup and have make at least a material from described syrup transfer to described step that the interfacial area of the described inter gas of the gas characteristic the described gas increases comprise make described syrup spread over material surface long-pending on.

162. as the described method that the syrup that is obtained by plant materials is handled of claim 140, the gas characteristic that described at least a material will be transferred to the described gas from described syrup keeps one section described step that is enough to make the time that at least a amount of substance reduces described in the described syrup, comprises that the gas characteristic that will described at least a material be transferred to the described gas from described syrup keeps one section to be enough to make the time that oxonium ion concentration reduces in the described syrup.

163. as the described method that the syrup that is obtained by plant materials is handled of claim 140, the gas characteristic that described at least a material will be transferred to the described gas from described syrup keeps one section described step that is enough to make the time that at least a amount of substance reduces described in the described syrup, comprises making described at least a material transfer to the time that gas characteristic the described gas keeps one section amount of substance that is enough to make described at least a generation oxonium ion to reduce from described syrup.

164. as the described method that the syrup that is obtained by plant materials is handled of claim 140, the gas characteristic that at least a material will be transferred to the described gas from described syrup keeps one section described step that is enough to make the time that at least a amount of substance reduces described in the described syrup, makes the pH value of described syrup improve the amount that is selected from 0.1pH, 0.2pH, 0.3pH, 0.4pH, 0.5pH, 0.6pH, 0.7pH, 0.8pH, 0.9pH, 1.0pH, 1.1pH, 1.2, pH1.3, pH1.4, pH1.5, pH1.6, pH1.7, pH1.8, pH1.9,2.0pH.

165. as the described method that the syrup that is obtained by plant materials is handled of claim 140, the gas characteristic that described at least a material will be transferred to the described gas from described syrup keeps one section described step that is enough to make the time that at least a amount of substance reduces described in the described syrup, makes to join in the described syrup and reduces to some extent with the required alkali number of initial pH value that is based upon between about 11.0 to about 12.0.

166. as the described method that the syrup that is obtained by plant materials is handled of claim 140, the gas characteristic that described at least a material will be transferred to the described gas from described syrup keeps one section described step that is enough to make the time that at least a amount of substance reduces described in the described syrup, makes to join in the described syrup and reduces to some extent with the required alkali number of initial pH value that is based upon between about 11.5 to about 12.5.

167. as the described method that the syrup that is obtained by plant materials is handled of claim 140, the gas characteristic that described at least a material will be transferred to the described gas from described syrup keeps one section described step that is enough to make the time that at least a amount of substance reduces described in the described syrup, make in the described syrup that joins certain volume with set up with described syrup in the required alkali number of the corresponding pH value of iso-electric point of at least a material reduce to some extent.

168. as claim 165, the 166 or 167 described methods that the syrup that is obtained by plant materials is handled, wherein said alkali is selected from calcium oxide, calcium hydroxide and milk of lime.

169. the syrup of handling according to claim 140,141,142,143,145,146,147,151,152,153,154,158 or 159 described methods.

170. the method that the syrup that is obtained by plant materials is handled comprises the following steps:

A) obtain plant materials;

B) plant materials is carried out lixiviate to obtain the leaching syrup;

C) the plant waste silk is transferred in the squeezing machine;

D) described plant waste silk is squeezed to obtain waste silk squeezing syrup;

E) waste silk being squeezed syrup is exposed to have at least a material is transferred in the gas of the gas characteristic the described gas from described syrup;

F) gas characteristic that described at least a material will be transferred to the described gas from described waste silk squeezing syrup keeps one section to be enough to make the time that at least a amount of substance reduces described in the described waste silk squeezing syrup.

171., comprise that further the waste silk squeezing syrup that described at least a substances content is reduced sends back in the extraction unit as the described method that the syrup that is obtained by plant materials is handled of claim 170.

172., wherein saidly plant materials carried out lixiviate comprise that with the step of obtaining syrup the waste silk that reduces with described at least a substances content squeezes syrup plant materials is carried out lixiviate as the described method that the syrup that is obtained by plant materials is handled of claim 170.

173. the waste silk of handling according to claim 170,171 or 172 described methods squeezes syrup.

174. the method that the syrup that is obtained by plant materials is handled may further comprise the steps:

A) obtain plant materials;

B) plant materials is carried out lixiviate to obtain the leaching syrup;

C) will leach syrup is exposed to have at least a material is transferred in the gas of the gas characteristic the described gas from described syrup;

D) gas characteristic that described at least a material will be transferred to the described gas from described leaching syrup keeps one section to be enough to make the time that at least a amount of substance reduces described in the described leaching syrup.

175., further comprise described leaching syrup and described plant materials blended step that wherein said at least a substances content is reduced as the described method that the syrup that is obtained by plant materials is handled of claim 174.

176., further comprise described leaching syrup and described plant materials separation steps with the content reduction of wherein said at least a material as the described method that the syrup that is obtained by plant materials is handled of claim 175.

177. as the described method that the syrup that is obtained by plant materials is handled of claim 176, further comprise the described leaching syrup that will reduce with wherein said at least a substances content mutually the described plant materials of blended be transported to step in the extraction unit.

178., comprise that further the described leaching syrup that wherein said at least a substances content is reduced is transported to the step in the preliming groove as the described method that the syrup that is obtained by plant materials is handled of claim 177.

179., further be included in described leaching syrup to be exposed to have and make described at least a material transfer to the temperature that makes described syrup when described step in the described gas of the gas characteristic the described gas begins to reach step between 60 ℃ to 80 ℃ from described syrup as the described method that the syrup that is obtained by plant materials is handled of claim 174.

180. as the described method that the syrup that is obtained by plant materials is handled of claim 174, further be included in described syrup to be exposed to have and make described at least a material when described syrup is transferred to described step in the described gas of the gas characteristic the described gas and begun, make described leaching syrup remain on the step that is selected from 60 ℃ to the 80 ℃ substantially constant temperature in the scope.

181. as the described method that the syrup that is obtained by plant materials is handled of claim 174, wherein described syrup is exposed to have when making described at least a material transfer to described step in the described gas of the gas characteristic the described gas from described syrup to begin, described leaching syrup has and is selected from about 60 ℃, about 61 ℃, about 62 ℃, about 63 ℃, about 64 ℃, about 65 ℃, about 66 ℃, about 67 ℃, about 68 ℃, about 69 ℃, about 70 ℃, about 71 ℃, about 72 ℃, about 73 ℃, about 74 ℃, about 75 ℃, about 76 ℃, about 77 ℃, about 78 ℃, about 79 ℃ and about 80 ℃ temperature.

182., further comprise being exposed to and reducing having of pressure and make at least a material transfer to step in the described gas of the gas characteristic the described gas from described syrup with leaching syrup as the described method that the syrup that is obtained by plant materials is handled of claim 174.

183. as the described method that the syrup that is obtained by plant materials is handled of claim 182, wherein said reduction pressure comprises pressure below atmospheric pressure.

184. as the described method that the syrup that is obtained by plant materials is handled of claim 183, further be included in to make and leach syrup and be exposed to and reduce having of pressure and make at least a material when described syrup is transferred to described step in the described gas of the gas characteristic the described gas and begun, make the temperature of described syrup reach step between 60 ℃ to 80 ℃.

185. as the described method that the syrup that is obtained by plant materials is handled of claim 183, further be included in to make and leach syrup and be exposed to and reduce having of pressure and make at least a material when described syrup is transferred to described step in the described gas of the gas characteristic the described gas and begun, make described leaching syrup remain on the step that is selected from 60 ℃ to the 80 ℃ substantially constant temperature in the scope.

186. as the described method that the syrup that is obtained by plant materials is handled of claim 183, wherein leach syrup and be exposed to and reduce having of pressure when making at least a material transfer to described step in the described gas of the gas characteristic the described gas from described syrup to begin making, described syrup has and is selected from about 60 ℃, about 61 ℃, about 62 ℃, about 63 ℃, about 64 ℃, about 65 ℃, about 66 ℃, about 67 ℃, about 68 ℃, about 69 ℃, about 70 ℃, about 71 ℃, about 72 ℃, about 73 ℃, about 74 ℃, about 75 ℃, about 76 ℃, about 77 ℃, about 78 ℃, about 79 ℃ and about 80 ℃ temperature.

187., further be included in to make and leach syrup and be exposed to and reduce the described step that having of pressure make at least a material transfer in the described gas of the gas characteristic the described gas from described syrup and carry out making in the process described leaching syrup to remain on the step that is selected from 60 ℃ to the 80 ℃ substantially constant temperature in the scope as the described method that the syrup that is obtained by plant materials is handled of claim 183.

188. as the described method that the syrup that is obtained by plant materials is handled of claim 183, wherein leach syrup and be exposed to the described step that at least a material is transferred to from described syrup in the described gas of the gas characteristic the described gas that has that reduces pressure and carry out in the process making, described leaching syrup has and is selected from about 60 ℃, about 61 ℃, about 62 ℃, about 63 ℃, about 64 ℃, about 65 ℃, about 66 ℃, about 67 ℃, about 68 ℃, about 69 ℃, about 70 ℃, about 71 ℃, about 72 ℃, about 73 ℃, about 74 ℃, about 75 ℃, about 76 ℃, about 77 ℃, about 78 ℃, about 79 ℃ and about 80 ℃ temperature.

189. the leaching syrup of handling according to claim 174,175,176,177,178,179,182,183 or 183 described methods.

190. the method that the syrup that is obtained by plant materials is handled comprises the following steps:

A) obtain plant materials;

B) plant materials is carried out lixiviate to obtain the leaching syrup;

C) the leaching syrup that described at least a substances content is reduced is mixed with described plant materials;

D) described plant materials is separated with described leaching syrup;

E) making the leaching syrup be exposed to have makes described at least a material transfer in the gas of the gas characteristic the described gas from described leaching syrup;

F) gas characteristic that described at least a material will be transferred to the described gas from described leaching syrup keeps one section to be enough to make the time that at least a amount of substance reduces described in the described leaching syrup.

191., comprise that further described leaching syrup and described plant materials that wherein said at least a substances content is reduced carry out separation steps as the described method that the syrup that is obtained by plant materials is handled of claim 190.

192. as the described method that the syrup that is obtained by plant materials is handled of claim 191, further comprise the described leaching syrup that will reduce with wherein said at least a substances content mutually the described plant materials of blended be transported to step in the extraction unit.

193., comprise that further the described leaching syrup that wherein said at least a substances content is reduced is transported to the step in the preliming groove as the described method that the syrup that is obtained by plant materials is handled of claim 191.

194., further be included in described leaching syrup to be exposed to have and make described at least a material transfer to the temperature that makes described syrup when described step in the described gas of the gas characteristic the described gas begins to reach step between 60 ℃ to 80 ℃ from described syrup as the described method that the syrup that is obtained by plant materials is handled of claim 190.

195. as the described method that the syrup that is obtained by plant materials is handled of claim 190, further be included in described leaching syrup to be exposed to have and make described at least a material when described syrup is transferred to described step in the described gas of the gas characteristic the described gas and begun, make described leaching syrup keep being selected from the step of 60 ℃ to the 80 ℃ substantially constant temperature in the scope.

196. as the described method that the syrup that is obtained by plant materials is handled of claim 190, wherein described leaching syrup is exposed to have when making described at least a material transfer to described step in the described gas of the gas characteristic the described gas from described syrup to begin, described leaching syrup has and is selected from about 60 ℃, about 61 ℃, about 62 ℃, about 63 ℃, about 64 ℃, about 65 ℃, about 66 ℃, about 67 ℃, about 68 ℃, about 69 ℃, about 70 ℃, about 71 ℃, about 72 ℃, about 73 ℃, about 74 ℃, about 75 ℃, about 76 ℃, about 77 ℃, about 78 ℃, about 79 ℃ and about 80 ℃ temperature.

197., further comprise described leaching syrup being exposed to have making at least a material transfer to step in the described gas of the gas characteristic the described gas from described syrup as the described method that the syrup that is obtained by plant materials is handled of claim 190.

198. as the described method that the syrup that is obtained by plant materials is handled of claim 197, wherein said reduction pressure comprises pressure below atmospheric pressure.

199. as the described method that the syrup that is obtained by plant materials is handled of claim 198, further be included in described leaching syrup to be exposed to have and make at least a material when described syrup is transferred to described step in the described gas of the gas characteristic the described gas and begun, make the temperature of described syrup reach step between 60 ℃ to 80 ℃.

200. as the described method that the syrup that is obtained by plant materials is handled of claim 190, further be included in described leaching syrup to be exposed to have and make at least a material when described syrup is transferred to described step in the described gas of the gas characteristic the described gas and begun, make described leaching syrup keep being selected from the step of 60 ℃ to the 80 ℃ substantially constant temperature in the scope.

201. as the described method that the syrup that is obtained by plant materials is handled of claim 198, wherein described leaching syrup is exposed to have when making at least a material transfer to described step in the described gas of the gas characteristic the described gas from described syrup to begin, described syrup has and is selected from about 60 ℃, about 61 ℃, about 62 ℃, about 63 ℃, about 64 ℃, about 65 ℃, about 66 ℃, about 67 ℃, about 68 ℃, about 69 ℃, about 70 ℃, about 71 ℃, about 72 ℃, about 73 ℃, about 74 ℃, about 75 ℃, about 76 ℃, about 77 ℃, about 78 ℃, about 79 ℃ and about 80 ℃ temperature.

202. as the described method that the syrup that is obtained by plant materials is handled of claim 198, further be included in and described leaching syrup be exposed to have the described step that at least a material is transferred in the described gas of the gas characteristic the described gas from described syrup to be carried out in the process, make described leaching syrup keep being selected from the step of 60 ℃ to the 80 ℃ substantially constant temperature in the scope.

203. as the described method that the syrup that is obtained by plant materials is handled of claim 198, wherein carry out in the process described leaching syrup being exposed to have the described step that at least a material is transferred to from described syrup in the described gas of the gas characteristic the described gas, described leaching syrup has and is selected from about 60 ℃, about 61 ℃, about 62 ℃, about 63 ℃, about 64 ℃, about 65 ℃, about 66 ℃, about 67 ℃, about 68 ℃, about 69 ℃, about 70 ℃, about 71 ℃, about 72 ℃, about 73 ℃, about 74 ℃, about 75 ℃, about 76 ℃, about 77 ℃, about 78 ℃, about 79 ℃ and about 80 ℃ temperature.

204. the leaching syrup of handling according to claim 190,191,192,193,194,197,198 or 199 method.

205. the method that the syrup that is obtained by plant materials is handled may further comprise the steps:

A) obtain plant materials;

B) to the described plant materials of small part, shifting out syrup;

C) make described syrup reach constant temperature between 60 ℃ to 80 ℃;

D) described syrup is exposed in the gaseous mixture under constant temperature;

E) the described solute of at least a portion is transferred to the described gaseous mixture from described syrup;

F) the described solute in the described syrup of minimizing.

206. as the described method that the syrup that is obtained by plant materials is handled of claim 205, wherein said plant materials comprises sugar beet, and wherein said syrup comprises the leaching syrup that is obtained by described sugar beet, and wherein said constant temperature comprises the constant temperature that is selected between about 65 ℃ and about 75 ℃.

207. as the described method that the syrup that is obtained by plant materials is handled of claim 205, wherein said plant materials comprises sugar beet, wherein said syrup comprises the leaching syrup that is obtained by described sugar beet, and wherein said constant temperature comprises the constant temperature that is selected between about 68 ℃ and about 72 ℃.

208. as the described method that the syrup that is obtained by plant materials is handled of claim 205, wherein said gaseous mixture comprises atmospheric gas.

209. the method that the syrup that is obtained by plant materials is handled may further comprise the steps:

A) by obtaining syrup in the plant materials;

B) make described syrup reach temperature between 60 ℃ to 80 ℃;

C) described syrup is exposed in the gaseous mixture under described temperature;

D) the described solute of at least a portion is transferred to the described gaseous mixture from described syrup;

E) will have described in the described syrup the described gaseous mixture that the described at least a material of part is transferred into and remove, the content of at least a material described in the syrup reduces thus.

210. the method that the syrup that is obtained by plant materials is handled may further comprise the steps:

A) by obtaining syrup in the plant materials;

B) syrup is exposed to have at least a material is transferred in the gas of the dividing potential drop the described gas from described syrup;

C) the described dividing potential drop that described at least a material will be shifted out from described syrup transfer keeps one section to be enough to make the time that at least a amount of substance reduces described in the described syrup.

211. a syrup treatment system comprises:

A) syrup dispersive element;

B) syrup is distributed to gas wherein, and wherein said gas has makes at least a material transfer to gas characteristic the described gas from described syrup;

C) variable adjustment flow generator, it makes described gas stream be enough to keep to make at least a material to transfer to described gas characteristic the described gas from described syrup;

D) gaseous emission element discharges the described stream of described gas by it.

212. as the described syrup treatment system of claim 211, wherein said syrup is to be obtained by the plant materials that is selected from sugarcane, sugar beet and sweet sorghum.

213. as the described syrup treatment system of claim 211, further comprise extraction unit, and wherein said syrup comprises that sugar beet leaches syrup.

214., further comprise runner milling, and wherein said syrup comprises the sugar cane juice that grinds as the described syrup treatment system of claim 212.

215. as the described syrup treatment system of claim 211, wherein said at least a material is selected from gas, acid, volatile organic compounds, alcohol, aldehyde, ketone, ester, nitrile, thioether, pyrazine, carbonic acid gas, carbonic acid, sulfurous gas, phosphoric acid, hydrochloric acid, sulfuric acid, sulfurous acid, citric acid, oxalic acid, succsinic acid, fumaric acid, lactic acid, oxyacetic acid, pyrrolidone-carboxylic acid, formic acid, acetate, butanic acid, toxilic acid, propionic acid, 3 Methylbutanoic acid, butyric acid, valeric acid, 5-methylhexanoic acid, caproic acid, enanthic acid and lactic acid.

216. as the described syrup treatment system of claim 211, wherein said gas with gas characteristic is selected from gaseous mixture, air, filtrated air, oxygen and ozone.

217. as the described syrup treatment system of claim 211, further comprise well heater so that be distributed in described syrup and have when making described at least a material transfer in the described gas of the gas characteristic the described gas from described syrup, the temperature of described syrup is reached be selected from 60 ℃ to the 80 ℃ substantially invariable temperature in the scope.

218. as the described syrup treatment system of claim 211, wherein be distributed in described syrup and have when making described at least a material transfer in the described gas of the gas characteristic the described gas from described syrup, described syrup has and is selected from about 60 ℃, about 61 ℃, about 62 ℃, about 63 ℃, about 64 ℃, about 65 ℃, about 66 ℃, about 67 ℃, about 68 ℃, about 69 ℃, about 70 ℃, about 71 ℃, about 72 ℃, about 73 ℃, about 74 ℃, about 75 ℃, about 76 ℃, about 77 ℃, about 78 ℃, about 79 ℃ and about 80 ℃ temperature.

219., comprise that further decompression producer so that make has the pressure that makes at least a material transfer to the described gas of the gas characteristic the described gas from described syrup and reduces as the described syrup treatment system of claim 211.

220. as the described method that the syrup that is obtained by plant materials is handled of claim 219, the described reduction pressure of wherein said gas comprises pressure below atmospheric pressure.

221. as the described syrup treatment system of claim 219, further comprise secondary heater so that be distributed to having of described reduction pressure when making at least a material transfer in the described gas of the gas characteristic the described gas from described syrup, make the temperature of described syrup reach 60 ℃ to the 80 ℃ substantially invariable temperature in the scope in described syrup.

222. as the described syrup treatment system of claim 219, wherein be distributed to having of described reduction pressure when making at least a material transfer in the described gas of the gas characteristic the described gas from described syrup in described syrup, described syrup has and is selected from about 60 ℃, about 61 ℃, about 62 ℃, about 63 ℃, about 64 ℃, about 65 ℃, about 66 ℃, about 67 ℃, about 68 ℃, about 69 ℃, about 70 ℃, about 71 ℃, about 72 ℃, about 73 ℃, about 74 ℃, about 75 ℃, about 76 ℃, about 77 ℃, about 78 ℃, about 79 ℃ and about 80 ℃ temperature.

223. as the described syrup treatment system of claim 211, wherein said syrup is distributed to have by the first syrup dispersive element in first container described at least a material is transferred in the described gas of the gas characteristic the described gas from described syrup.

224. as the described syrup treatment system of claim 219, wherein said syrup is distributed to having of described reduction pressure by the second syrup dispersive element in second container makes described at least a material transfer in the described gas of the gas characteristic the described gas from described syrup.

225. as the described syrup treatment system of claim 223, in described first container, further comprise traverse baffle so that described syrup with have the interfacial area that makes described at least a material transfer to the described inter gas of the gas characteristic the described gas and increase from described syrup.

226. as the described syrup treatment system of claim 224, in described second container, further comprise traverse baffle so that described syrup with have the interfacial area that makes described at least a material transfer to the described inter gas of the gas characteristic the described gas and increase from described syrup.

227. as claim 223 or 224 described syrup treatment systems, wherein said syrup dispersive element comprises nozzle.

228. a syrup treatment system comprises:

A) syrup dispersive element;

B) syrup is distributed to the gas of reduction pressure wherein, and the gas of wherein said reduction pressure has makes at least a material transfer to gas characteristic the described gas from described syrup; With

C) variable adjustment flow generator, it makes described gas remain on the pressure of described reduction down so that described at least a material is transferred to the described gas from described syrup.

229. as the described syrup treatment system of claim 228, wherein said syrup is to be obtained by the plant materials that is selected from sugarcane, sugar beet and sweet sorghum.

230. as the described syrup treatment system of claim 229, further comprise extraction unit, and wherein said syrup comprises that sugar beet leaches syrup.

231., further comprise runner milling, and wherein said syrup comprises the sugar cane juice that grinds as the described syrup treatment system of claim 229.

232. as the described syrup treatment system of claim 228, wherein said at least a material is selected from gas, acid, volatile organic compounds, alcohol, aldehyde, ketone, ester, nitrile, thioether, pyrazine, carbonic acid gas, carbonic acid, sulfurous gas, phosphoric acid, hydrochloric acid, sulfuric acid, sulfurous acid, citric acid, oxalic acid, succsinic acid, fumaric acid, lactic acid, oxyacetic acid, pyrrolidone-carboxylic acid, formic acid, acetate, butanic acid, toxilic acid, propionic acid, 3 Methylbutanoic acid, butyric acid, valeric acid, 5-methylhexanoic acid, caproic acid, enanthic acid and lactic acid.

233. as the described syrup treatment system of claim 228, the gas of wherein said reduction pressure is selected from gaseous mixture, air, filtrated air, oxygen and ozone.

234. as the described syrup treatment system of claim 228, further comprise a well heater so that when described syrup is distributed in the described gas with described reduction pressure, described syrup is reached be selected from 60 ℃ to the 80 ℃ substantially invariable temperature in the scope, wherein said gas allows described at least a material to transfer to the described gas from described syrup.

235. as the described syrup treatment system of claim 228, wherein when described syrup is distributed in the described gas with described reduction pressure, described syrup has and is selected from about 60 ℃, about 61 ℃, about 62 ℃, about 63 ℃, about 64 ℃, about 65 ℃, about 66 ℃, about 67 ℃, about 68 ℃, about 69 ℃, about 70 ℃, about 71 ℃, about 72 ℃, about 73 ℃, about 74 ℃, about 75 ℃, about 76 ℃, about 77 ℃, about 78 ℃, about 79 ℃ and about 80 ℃ temperature, wherein said gas allows described at least a material to transfer to the described gas from described syrup.

236., comprise further that flow generator has with generation to make at least a material transfer to the air-flow of the gas characteristic the described gas from described syrup as the described syrup treatment system of claim 228.

237. as the described method that the syrup that is obtained by plant materials is handled of claim 236, wherein said gas with gas characteristic is selected from gaseous mixture, air, filtrated air, oxygen and ozone.

238. as the described syrup treatment system of claim 228, further comprise secondary heater so that be distributed in described syrup and have when making at least a material transfer in the described gas of the gas characteristic the described gas from described syrup, make described syrup reach about 60 ℃ of substantially invariable temperature to about 80 ℃ of scopes.

239. as the described syrup treatment system of claim 238, wherein be distributed in described syrup and have when making described at least a material transfer in the described gas of the gas characteristic the described gas from described syrup, described syrup has and is selected from about 60 ℃, about 61 ℃, about 62 ℃, about 63 ℃, about 64 ℃, about 65 ℃, about 66 ℃, about 67 ℃, about 68 ℃, about 69 ℃, about 70 ℃, about 71 ℃, about 72 ℃, about 73 ℃, about 74 ℃, about 75 ℃, about 76 ℃, about 77 ℃, about 78 ℃, about 79 ℃ and about 80 ℃ temperature.

240. as the described syrup treatment system of claim 228, wherein said syrup is distributed to have by the first syrup dispersive element in first container and makes described at least a material transfer to the gas characteristic the described gas and have in the described gas that reduces pressure from described syrup.

241. as the described syrup treatment system of claim 236, wherein said syrup is distributed to have by the second syrup dispersive element in second container described at least a material is transferred in the described gas stream of the gas characteristic the described gas from described syrup.

242. as the described syrup treatment system of claim 240, in described first container, further comprise traverse baffle so that described syrup with have the interfacial area that makes described at least a material transfer to the described inter gas of the gas characteristic the described gas and increase from described syrup.

243. as the described syrup treatment system of claim 241, in described second container, further comprise traverse baffle so that described syrup with have the interfacial area that makes described at least a material transfer to the described inter gas of the gas characteristic the described gas and increase from described syrup.

244. as the described syrup treatment system of claim 241, wherein said syrup dispersive element comprises nozzle.