CN204714728U - Generate the equipment of water vapour, the equipment of heated air stream and the system for the preparation of aromatic dicarboxylic acid - Google Patents
Generate the equipment of water vapour, the equipment of heated air stream and the system for the preparation of aromatic dicarboxylic acid Download PDFInfo
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- CN204714728U CN204714728U CN201520108168.4U CN201520108168U CN204714728U CN 204714728 U CN204714728 U CN 204714728U CN 201520108168 U CN201520108168 U CN 201520108168U CN 204714728 U CN204714728 U CN 204714728U
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
- C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
- C07C51/255—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting
- C07C51/265—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting having alkyl side chains which are oxidised to carboxyl groups
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/487—Separation; Purification; Stabilisation; Use of additives by treatment giving rise to chemical modification
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Abstract
The disclosure provides a kind of equipment generating water vapour, and described equipment uses in for the preparation of the system of aromatic dicarboxylic acid, and described equipment comprises: the first slurries heat exchanger a) receiving thick aromatic dicarboxylic acid slurries; B) hydrogenation reactor from the thick aromatic dicarboxylic acid solution of described first slurries heat exchanger is received; C) a series of one or more crystallizer from the aromatic dicarboxylic acid solution of the purifying of described hydrogenation reactor is received; And d) heat is sent to current to generate the water vapour maker of water vapour from the crystallizer discharge stream of the one or more crystallizers from described series.
Description
Technical field
The disclosure relates to a kind of equipment generating water vapour, and described equipment uses in for the preparation of the system of aromatic dicarboxylic acid; An equipment for heated air stream, described equipment uses in for the preparation of the system of aromatic dicarboxylic acid; And a kind of system for the preparation of aromatic dicarboxylic acid.
Background technology
Aromatic dicarboxylic acid is usually by the catalyzed oxidation preparation in organic solvent of hydrocarbon precursor.Example is terephthalic acid (TA), and it is widely used in prepares polyester, as poly-(ethylene glycol terephthalate) (PET).Be called as " terephthalic acid of purifying " (PTA) as the TA needed for the reactant prepared for PET, and usually containing the terephthalic acid more than 99.97 % by weight, preferably more than 99.99 % by weight, and be less than 25ppm 4-carboxyl benzaldehyde (4-CBA).At industrial scale, the PTA being suitable for using in PET manufactures is prepared with two-phase method usually.First, by p-Xylol, under the existence of metal catalyst (such as, cobalt and/or manganese salt or compound), oxidation is (such as, use air) to provide " crude terephthalic acid " (CTA), as at such as US 2,833, described in 816.Then, by the CTA purifying prepared by this oxidizing reaction because its usually by impurity as 4-CBA, p-methylbenzoic acid, and give TA flaxen various foreign pigment and polluted.The purifying of CTA, outside at least one physical process of needs (such as, crystallization, washing etc.), also needs at least one chemical conversion (such as, hydrogenation) to produce PTA usually.
PTA is regarded as batch item of merchandise usually, and its annual production has millions of tons, and therefore manufacturers expects to reduce its cost with the economy making PTA manufacture and maximizing efficiency.This is by reducing cost of capital (such as, equipment cost) and variable cost (such as, to waste treatment, initial substance uses, organic solvent, heating fuel and deionized water are relevant cost) realizes.
Usually heat is introduced in aromatic dicarboxylic acid manufactory and also uses water vapour to make carrier transmission heat wherein.Particularly, by combustion heating fuel with heating water (such as in fossil-fuel boiler), the high-pressure steam that temperature is such as about 300 DEG C can be generated outside battery limits, then lead this high-pressure steam one or more heat exchanger, to transfer heat to the process flow with top temperature demand.The mesohigh water vapour (intermediate-pressure steam) that flash distillation with preparation temperature is such as about 220 DEG C can be carried out to the high pressure condensation product of gained, then this mesohigh water vapour can be used for heating process flow formation mesohigh condensation product (intermediate-pressure condensate) with lower heat demand, flash distillation can be carried out with setting-out steam in preparation, then and so forth until the depleted of energy of described water vapour to this mesohigh condensation product.
The heating fuel generated needed for high-pressure steam forms the remarkable variable cost of aromatic dicarboxylic acid manufacture method.Object of the present disclosure be to provide a kind of for the manufacture of aromatic dicarboxylic acid more economically and more effective method and apparatus and, particularly, the high-pressure steam demand being used for aromatic dicarboxylic acid manufacture method is minimized.Further object easily will be shown in from following specification sheets.
Utility model content
The disclosure provides a kind of equipment generating water vapour, and described equipment uses in for the preparation of the system of aromatic dicarboxylic acid, and described equipment comprises:
A) the first slurries heat exchanger of thick aromatic dicarboxylic acid slurries is received;
B) hydrogenation reactor from the thick aromatic dicarboxylic acid solution of described first slurries heat exchanger is received;
C) a series of one or more crystallizer from the aromatic dicarboxylic acid solution of the purifying of described hydrogenation reactor is received; And
D) heat is sent to current to generate the water vapour maker of water vapour from the crystallizer discharge stream of the one or more crystallizers from described series.
The disclosure also provides a kind of equipment of heated air stream, and described equipment uses in for the preparation of the system of aromatic dicarboxylic acid, and described equipment comprises:
A) according to the equipment for generating water vapour of the present disclosure; And
B) heat is sent to the first gaseous heat exchanger of described gas stream from described water vapour.
The disclosure also provides a kind of system for the preparation of aromatic dicarboxylic acid, and described system comprises according to equipment of the present disclosure.
The disclosure also provides a kind of system for the preparation of aromatic dicarboxylic acid, and described system comprises
Oxidation panel,
Crystallized region, described crystallized region comprises one or more crystallizer;
Process the distilling period from the emission gases of described oxidation panel;
Condensation segment, described condensation segment is connected to described distilling period;
To the pressurization washer that it processes before the overhead gas of self-condensation in future section is released into atmospheric environment; With
According to equipment of the present disclosure.
Object of the present disclosure can realize compared with the water vapour (such as mesohigh water vapour) of low pressure by generating in the process, instead of by directly obtaining these water vapour from high-pressure steam.Therefore first aspect of the present disclosure provides a kind of method for generating water vapour in the method preparing aromatic dicarboxylic acid, the described method preparing aromatic dicarboxylic acid comprises hydrocarbon precursor catalyzed oxidation in organic solvent, and the method for described generation water vapour comprises the following steps:
I) thick aromatic dicarboxylic acid slurries are heated to form thick aromatic dicarboxylic acid solution;
Ii) described thick aromatic dicarboxylic acid solution is sent to hydrogenation reactor;
Iii) the aromatic dicarboxylic acid solution of purifying is sent to a series of one or more crystallizer from described hydrogenation reactor; And
Iv) heat is sent to current water vapour maker to generate water vapour from the crystallizer discharge stream of the one or more crystallizers from described series.
The water vapour generated is generally saturated steam.Preferably, at step I v) in generate water vapour be middle setting-out steam or mesohigh water vapour.More preferably, at step I v) in generate water vapour be mesohigh water vapour.
As used herein, the saturated steam of " high-pressure steam " to be finger pressure be about 50-150barA or about 75-125barA or about 100barA.Similarly, the condensation product of " high pressure condensation product " to be finger pressure be about 50-150barA or about 75-125barA or about 100barA.As used herein, the saturated steam of " mesohigh water vapour " to be finger pressure be about 10-50barA or about 12.5-40barA or about 15-35barA or about 17.5-30barA or about 20barA.As used herein, the saturated steam of " middle setting-out steam " to be finger pressure be about 5-10barA or about 6-9barA or about 8barA.As used herein, " Low pressure steam " is the saturated steam that finger pressure is less than about 5barA.
Thick aromatic dicarboxylic acid slurries can use high-pressure steam to heat.Therefore, step I) can step v be comprised): heat is sent to the thick aromatic dicarboxylic acid slurries the first slurries heat exchanger from high-pressure steam.High pressure condensation product can in step v) in generate.Under high pressure condensation product is in the temperature substantially the same with high-pressure steam usually, such as high pressure condensation product can be in lower than high-pressure steam 10 DEG C, or at the temperature of low 5 DEG C.Such as, if under high-pressure steam is in the temperature of 290-320 DEG C, then high pressure condensation product can be in 280-310 DEG C, or at the temperature of 285-315 DEG C.Therefore, step I) also can comprise step vi): in the second slurries heat exchanger, heat is sent to described thick aromatic dicarboxylic acid slurries from described high pressure condensation product, described second slurries heat exchanger is arranged in the upstream of described first slurries heat exchanger relative to the flow direction of described thick aromatic dicarboxylic acid slurries.In the upstream of the described second slurries heat exchanger of the flow direction relative to described thick aromatic dicarboxylic acid slurries, thick aromatic dicarboxylic acid slurries can be heated at least 250 DEG C, preferably, directly heat is not sent to described thick aromatic dicarboxylic acid slurries from described high-pressure steam or described high pressure condensation product.Therefore, before the heat from described high pressure condensation product and described high-pressure steam is applied to described thick aromatic dicarboxylic acid slurries, just described thick aromatic dicarboxylic acid slurries can be heated to high temperature.Then, before described stream arrives at described hydrogenation reactor, described high pressure condensation product and described high-pressure steam provide the last increase in required temperature.Therefore, compare with manufacture method before and manufactory, the disclosure with more economically, effective and favourable mode uses high-pressure steam.
This aspect of the present disclosure additionally provides a kind of equipment for generating water vapour in the method preparing aromatic dicarboxylic acid, and the described method preparing aromatic dicarboxylic acid comprises hydrocarbon precursor catalyzed oxidation in organic solvent, and described equipment comprises:
A) the first slurries heat exchanger, described first slurries heat exchanger arrangement is for receiving thick aromatic dicarboxylic acid slurries;
B) hydrogenation reactor, described hydrogenation reactor is configured to receive the thick aromatic dicarboxylic acid solution from described first slurries heat exchanger;
C) a series of one or more crystallizer, described one or more crystallizer is configured to receive the aromatic dicarboxylic acid solution from the purifying of described hydrogenation reactor; And
D) water vapour maker, described water vapour maker is configured to heat to be sent to current to generate water vapour from the crystallizer discharge stream of the one or more crystallizers from described series.
The water vapour generated is generally saturated steam.Preferably, by water vapour maker d) water vapour that generates is middle setting-out steam or mesohigh water vapour.More preferably, by water vapour maker d) water vapour that generates is mesohigh water vapour.
High-pressure steam can be used to heat thick aromatic dicarboxylic acid slurries.Therefore, the first slurries heat exchanger can be configured to heat to be sent to thick aromatic dicarboxylic acid slurries from high-pressure steam.Described equipment also can comprise e) the second slurries heat exchanger, described second slurries heat exchanger arrangement is that heat is sent to thick aromatic dicarboxylic acid slurries from the high pressure condensation product generated by high-pressure steam, and is arranged in the upstream of the first slurries heat exchanger relative to the flow direction of thick aromatic dicarboxylic acid slurries.Described equipment can be configured to, in the upstream of the described second slurries heat exchanger of the flow direction relative to thick aromatic dicarboxylic acid slurries, described thick aromatic dicarboxylic acid slurries are heated at least 250 DEG C, preferably, directly heat is not sent to thick aromatic dicarboxylic acid slurries from high-pressure steam or high pressure condensation product.Therefore, before the heat from high pressure condensation product and high-pressure steam is applied to thick aromatic dicarboxylic acid slurries, thick aromatic dicarboxylic acid slurries can be heated to high temperature.Then, before described stream arrives at hydrogenation reactor, high pressure condensation product and high-pressure steam provide temperature required last increase.
Contriver is surprised to find, the heat from crystallizer discharge stream can be used to generate water vapour (particularly mesohigh water vapour), and do not increase the high-pressure steam demand of elsewhere in the method, such as do not need other high-pressure steam (compared to wherein crystallizer discharge stream not for generating the method for water vapour) to heat thick aromatic dicarboxylic acid slurries.Therefore, present disclose provides new source of water vapor, mesohigh water vapour particularly, it can be used for substituting the water vapour deriving from high-pressure steam, therefore compared to previous manufacture method and equipment, the disclosure with a kind of more economically, effective and favourable mode uses high-pressure steam, and decreases the overall high-pressure steam demand of described method, this decreases demand for heat and then because this reducing variable cost.
Therefore, second aspect of the present disclosure provides a kind of method for heated air stream in the method preparing aromatic dicarboxylic acid, the described method preparing aromatic dicarboxylic acid comprises hydrocarbon precursor catalyzed oxidation in organic solvent, and the method for described heated air stream comprises the following steps:
I) water vapour is generated by the method according to first aspect of the present disclosure; And
II) heat is sent to the gas stream described first gaseous heat exchanger from described water vapour.
This aspect of the present disclosure additionally provides a kind of equipment for heated air stream in the method preparing aromatic dicarboxylic acid, and the described method preparing aromatic dicarboxylic acid comprises hydrocarbon precursor catalyzed oxidation in organic solvent, and described equipment comprises:
A) for generating the equipment of water vapour according to first aspect of the present disclosure; And
B) the first gaseous heat exchanger, described first gaseous heat exchanger is configured to heat to be sent to described gas stream from described water vapour.
Gas stream can be pressurization washer discharge gas stream.Be necessary that first heating this gas stream is sent in catalytic burner again, wherein removes organic compound from this gas stream.Therefore, present disclose provides and do not use high-pressure steam also not increase the high-pressure steam demand of elsewhere in described method to heat the method for this stream, thus decrease the overall high-pressure steam demand of described method.
Accompanying drawing explanation
Fig. 1 is the schematic diagram according to method and apparatus of the present disclosure.
Embodiment
This document describes multiple embodiment of the present disclosure.Will be appreciated that, the feature of specifying in each embodiment can be combined to provide other embodiments with other specific characteristics.
Should be appreciated that the general operation for being prepared the method and apparatus of aromatic dicarboxylic acid by hydrocarbon precursor catalyzed oxidation is in organic solvent well-known.Such as, as mentioned above, the terephthalic acid (that is, the terephthalic acid of purifying) being suitable for using in PET preparation is prepared with two-phase method usually.First, by p-Xylol oxidation under the existence of metal catalyst (such as, cobalt and/or manganese salt or compound) (such as, using air) to provide crude terephthalic acid.Then, by the crude terephthalic acid purifying prepared by this oxidizing reaction to remove impurity, as 4-CBA and p-methylbenzoic acid, to generate the terephthalic acid of purifying.The purifying of crude terephthalic acid, outside at least one physical process of needs (such as, crystallization, washing etc.), also needs at least one chemical conversion (such as, hydrogenation) usually.
The preparation of aromatic dicarboxylic acid
The aromatic dicarboxylic acid prepared in method and apparatus of the present disclosure is preferably selected from terephthalic acid, phthalic acid and m-phthalic acid.Aromatic dicarboxylic acid is preferably terephthalic acid.Hydrocarbon precursor is the compound of oxidable formation aromatic dicarboxylic acid.Therefore, hydrocarbon precursor is generally the position quilt of the carboxylic acid substituent in required final product as C
1-6the benzene that alkyl, formyl radical or ethanoyl replace or naphthalene.Preferred hydrocarbon precursor is C
1-6the benzene that alkyl replaces particularly, is p-Xylol.Organic solvent is generally aliphatic carboxylic acid, as acetic acid, or the mixture of one or more these type of aliphatic carboxylic acids and water.Oxidizing reaction is carried out under can having any condition of oxygen wherein, and such as, this reaction can be carried out in atmosphere.Catalysts comprises cobalt and/or the manganese (such as, their acetate) of soluble form usually, uses bromine source (as hydrogen bromide) as promotor.The temperature of oxidizing reaction, usually in the scope of about 100-250 DEG C, is preferably about 150-220 DEG C.The pressure of any routine all can be used for this reaction, suitably to be kept in the liquid state by this reaction mixture.
Oxidation panel performs the function of hydrocarbon precursor catalyzed oxidation in organic solvent, thus forms product stream and emission gases.Product stream is sent to crystallized region usually to form the first slurries and the overhead vapours of thick aromatic dicarboxylic acid crystal.Usually the first slurries of thick aromatic dicarboxylic acid crystal are sent to segregation section, wherein mother liquor and thick aromatic dicarboxylic acid crystal are separated, then can mix with liquid, aqueous the second slurries forming thick aromatic dicarboxylic acid crystal.Usually the second slurries of this thick aromatic dicarboxylic acid crystal are sent to purification devices, heat and carry out hydrogenation, cooling the slurries of the aromatic dicarboxylic acid crystal forming purifying afterwards.
In distilling period, usually in the future the emission gases of autoxidation section is separated to the liquid stream that is rich in organic solvent and is rich in the steam stream of water.The liquid stream being rich in organic solvent from distilling period comprises the organic solvent of 80-95% w/w usually, and usually returns oxidation panel.The steam flow being rich in water from distilling period often comprises the organic solvent of 0.1-5.0% w/w, and usually in condensation segment condensation to form condensate flow and overhead gas.A part for condensate flow is typically used as the source of aqueous liquid of the second slurries for the formation of above-mentioned thick aromatic dicarboxylic acid crystal.A part for condensate flow also forms the scrub stream body source be used for from the aromatic dicarboxylic acid crystal of the purifying of purification devices usually.
Thick aromatic dicarboxylic acid slurries
As mentioned above, the slurries of the thick aromatic dicarboxylic acid crystal in liquid, aqueous are carried out to the purification section of typical aromatic dicarboxylic acid manufacture method.Therefore, in these class methods, the second slurries of above-mentioned thick aromatic dicarboxylic acid crystal form the thick aromatic dicarboxylic acid slurries used in the disclosure.This slurries, except comprising aromatic dicarboxylic acid, also comprise byproduct of reaction (p-methylbenzoic acid, phenylformic acid and 4-CBA in such as TA preparation) and organic solvent derivative and (such as from the methyl acetate of acetic acid) and a small amount of catalysts usually.Heat thick aromatic dicarboxylic acid slurries to form thick aromatic dicarboxylic acid solution, in hydrogenation reactor, hydrogenation is carried out to this solution, usually on carbon the palladium of load fixed bed catalyst on, some impurity conversion are become the easier form (such as 4-CBA being converted into p-methylbenzoic acid) removed from the aromatic dicarboxylic acid crystal of purifying under high temperature (such as 275-290 DEG C) with high pressure (such as 70-90barA).
Heated slurry
Usually, before the hydrogenation of the thick aromatic dicarboxylic acid solution of gained, first thick aromatic dicarboxylic acid slurries are heated with solubilizing reaction by product, be usually up to about 280 DEG C or higher temperature.This can be realized by the slurries delivered to a series of heat exchanger (as shell and-tube heat exchanger) that spread heat raised gradually from series of temperature.Therefore, along with the stream heating raised gradually by this series of temperatures by thick aromatic dicarboxylic acid slurries, the dissolution of solid in thick aromatic dicarboxylic acid slurries, makes finally to form thick aromatic dicarboxylic acid solution.First heat exchanger (counting backward from hydrogenation reactor) applies final heating step before the hydrogenation, and this is generally used in the high-pressure steam source generated outside battery limits and carries out, and the temperature in this high-pressure steam source is such as about 300 DEG C.Therefore, heat is sent to the thick aromatic dicarboxylic acid slurries the first slurries heat exchanger from high-pressure steam.Because the generation of this high-pressure steam forms the significant variable cost of aromatic dicarboxylic acid manufacture method, therefore wish farthest to reduce the high-pressure steam demand of the method and farthest utilize the heat energy from this water vapour.Therefore, the high pressure condensation product generated in this first hot transfer step can be sent to the second heat exchanger (being arranged in the upstream of the first slurries heat exchanger relative to the flow direction of thick aromatic dicarboxylic acid slurries), in the second heat exchanger, heat be sent to thick aromatic dicarboxylic acid slurries from high pressure condensation product.
Before thick aromatic dicarboxylic acid slurries arrive at the second heat exchanger, by the preheating of described thick aromatic dicarboxylic acid slurries partly being reduced the high-pressure steam demand of described heating steps.Therefore, in the upstream of the second slurries heat exchanger of the flow direction relative to described thick aromatic dicarboxylic acid slurries, thick aromatic dicarboxylic acid slurries can be heated at least 220 DEG C or at least 230 DEG C or at least 240 DEG C, or preferably at least 250 DEG C, preferably, directly heat is not sent to thick aromatic dicarboxylic acid slurries from high-pressure steam or high pressure condensation product.This preheating can be carried out by thick aromatic dicarboxylic acid slurries heat be sent to one or more other heat exchanger from one or more crystallizer discharge stream of the one or more crystallizers from this series.Therefore, the step heating thick aromatic dicarboxylic acid slurries can also comprise thick aromatic dicarboxylic acid slurries heat be sent to from the crystallizer discharge stream of the one or more crystallizers from this series the 3rd slurries heat exchanger, and described 3rd slurries heat exchanger is arranged in the upstream of the second slurries heat exchanger relative to the flow direction of thick aromatic dicarboxylic acid slurries.
The disclosure can comprise the aromatic dicarboxylic acid solution of purifying is sent to a series of two or more crystallizer or a series of more than three crystallizers or a series of more than four crystallizers or a series of more than five crystallizers from hydrogenation reactor.
" first " crystallizer in a series of is receive the crystallizer from the aromatic dicarboxylic acid solution of the purifying of hydrogenation reactor.Therefore, can by heat from the thick aromatic dicarboxylic acid slurries be sent to from the crystallizer discharge stream of the first crystallizer this series in the 3rd slurries heat exchanger.Alternatively or additionally, heat can be sent to the thick aromatic dicarboxylic acid slurries in the 3rd slurries heat exchanger from the crystallizer discharge stream from the second crystallizer this series.The step heating thick aromatic dicarboxylic acid slurries can also comprise thick aromatic dicarboxylic acid slurries heat be sent to from the crystallizer discharge stream of the one or more crystallizers from this series the 4th slurries heat exchanger, and described 4th slurries heat exchanger is arranged in the upstream of the 3rd slurries heat exchanger relative to the flow direction of thick aromatic dicarboxylic acid slurries.Particularly, can by heat from the thick aromatic dicarboxylic acid slurries be sent to from the crystallizer discharge stream of the second crystallizer this series in the 4th slurries heat exchanger.
Can from each of above-mentioned crystallizer, obtain single discharge stream and be sent to above-mentioned heat exchanger.Alternatively, multiple discharge stream can be obtained (by using the crystallizer with multiple venting hole from each of above-mentioned crystallizer, or by the stream of segmentation from the single venting hole in each crystallizer), then in multiple discharge stream is sent to above-mentioned heat exchanger, and by other one or more elsewheres (such as, being used for generating water vapour) being used in described method.
Water vapour maker
Water vapour maker is heat exchanger, preferred shell-and-tube exchanger (such as autoclave heat exchanger), wherein heat is sent to current (such as, boiler feed water stream) to generate water vapour from crystallizer discharge stream, preferred mesohigh water vapour.Usually current are pumped to water vapour maker under stress, and can by its preheating before current are sent to water vapour maker.
Although the heat of the crystallizer discharge stream from the first crystallizer in this series can be sent to the current in water vapour maker, but this crystallizer discharge stream is usually than being used for generating the required hotter of mesohigh water vapour, and it is more effective for therefore utilizing this crystallizer discharge stream to heat thick aromatic dicarboxylic acid slurries.Therefore, preferably heat is sent to current in water vapour maker to generate water vapour from the crystallizer discharge stream from the second crystallizer this series or the later crystallization device in this series.Particularly, preferably by heat from the current be sent to from the crystallizer discharge stream of the second crystallizer this series in water vapour maker to generate water vapour.Although than colder from the crystallizer discharge stream of the first crystallizer in this series, under being in from the crystallizer discharge stream of the second crystallizer the high temperature being enough to generate mesohigh water vapour.Further preferably, if heat to be sent to the thick aromatic dicarboxylic acid slurries in the 4th slurries heat exchanger from the crystallizer discharge stream from the second crystallizer this series, and heat is sent to current in water vapour maker to generate water vapour from the crystallizer discharge stream from the second crystallizer this series.This can be used for guaranteeing that the generation of water vapour does not comprise the heating of thick aromatic dicarboxylic acid slurries, and namely the generation of water vapour can not cause needs other high-pressure steam to heat thick aromatic dicarboxylic acid slurries.
Heated air stream
The water vapour (such as mesohigh water vapour) generated in first aspect of the present disclosure can be used for heating other streams for the preparation of in the method and apparatus of aromatic dicarboxylic acid, thus reduce other water vapour, the particularly use of valuable high-pressure steam.Therefore, second aspect of the present disclosure is by using this water vapour by heat from the described water vapour gas stream be sent to the first gaseous heat exchanger.
Described water vapour, particularly mesohigh water vapour, be found particularly useful to heating and pressurizing washer discharge gas stream.Pressurization washer is one in a series of segments, and these sections processed it before being released into atmospheric environment at the overhead gas of self-condensation in future section.This equipment first uses organic solvent (such as acetic acid) then to wash overhead gas with water, thus reduces material in the described gas level as unreacted hydrocarbon precursor (such as p-Xylol) and organic solvent derivative (such as methyl acetate).Then can be further processed pressurization washer discharge gas stream.Such as, this gas stream can be processed to remove the organic constituent of carbon monoxide and any remnants in catalytic burner, in off gas scrubber, then can process the catalytic burner exit gas of gained further, then be discharged in atmospheric environment.
Wish before it is further processed, first heating and pressurizing washer discharge gas stream, as catalyticcombustion, to increase the efficiency of these process.Can by pressurization washer discharge gas stream preheating in the second gaseous heat exchanger (such as by the heat from Low pressure steam or middle setting-out steam is sent to the second gaseous heat exchanger), described second gaseous heat exchanger is arranged in the upstream of the first gaseous heat exchanger relative to the flow direction of pressurization washer discharge gas stream.Alternatively or additionally, can heat it by heat being sent to pressurization washer discharge gas stream in the 3rd gaseous heat exchanger, described 3rd gaseous heat exchanger is arranged in the downstream of the first gaseous heat exchanger relative to the flow direction of pressurization washer discharge gas stream.Therefore, pressurization washer discharge gas stream can be sent to the 3rd gaseous heat exchanger from the first gaseous heat exchanger, then can be sent to catalytic burner from the 3rd gaseous heat exchanger.Can in the future spread and deliver to the 3rd gaseous heat exchanger by the catalytic burner exit gas of autocatalysis burner, deliver to pressurization washer discharge gas stream to make heat spread from catalytic burner exit gas.
The disclosure is further described with reference to accompanying drawing.
Fig. 1 is the schematic diagram of the method and apparatus according to preferred embodiment of the present disclosure.Heating zone 10 comprises the first heat exchanger 12, second heat exchanger 14, the 3rd heat exchanger 16 and the 4th heat exchanger 18.First heat exchanger 12 is supplied with the high-pressure steam charging 12a that pressure is about 100barA, and this charging generates, to heat thick aromatic dicarboxylic acid (preferred terephthalic acid) slurry stream 14a in the boiler burning fossil oil.High pressure condensate flow 12b is sent to the second heat exchanger 14 to heat thick aromatic dicarboxylic acid slurry stream 16a.Crystallizer discharge stream 30a from the first crystallizer 30 is fed to the 3rd heat exchanger 16 to heat thick aromatic dicarboxylic acid slurry stream 18a.Crystallizer discharge stream 40a from the second crystallizer 40 is fed to the 4th heat exchanger 18 to heat thick aromatic dicarboxylic acid slurry stream 10a.Therefore, thick aromatic dicarboxylic acid slurry stream 10a is fed to heating zone 10, and these slurries is heated to dissolve its solid ingredient successively in the 4th heat exchanger 18, the 3rd heat exchanger 16, second heat exchanger 14 and the first heat exchanger 12 thus forms thick aromatic dicarboxylic acid solution stream 10b.Heating should make thick aromatic dicarboxylic acid slurry stream 16a temperature when arrival the second heat exchanger 14 be at least 250 DEG C.
Thick aromatic dicarboxylic acid solution stream 10b is fed to hydrogenation reactor 20, in this reactor on carbon the palladium of load fixed bed catalyst on, under the pressure of the temperature of 275-290 DEG C and 70-90barA, hydrogenation is carried out to thick aromatic dicarboxylic acid solution stream 10b.The aromatic dicarboxylic acid solution stream 20a of purifying is fed to the first crystallizer 30 to form the aromatic dicarboxylic acid slurry stream 30b of purifying, this slurry stream is fed to the second crystallizer 40.Removing purifying aromatic dicarboxylic acid slurry stream 40b for further process, to reclaim the aromatic dicarboxylic acid crystal of purifying.
Crystallizer from the second crystallizer 40 is discharged water vapour 40c and is fed to water vapour maker 50 with heating boiler feed water stream 50a.Be that the mesohigh water vapour charging 50b of about 22barA is fed to the first gaseous heat exchanger 60 with heating and pressurizing washer discharge gas stream 70d by pressure.By Low pressure steam charging 70b heating and pressurizing washer discharge gas stream 70a in the second gaseous heat exchanger 70, and pressurization washer discharge gas stream 70d is sent to the first gaseous heat exchanger 60.Pressurization washer discharge gas stream 60a is fed to the 3rd gaseous heat exchanger 80.Pressurization washer discharge gas stream 80a is fed to catalytic burner 90 to prepare catalytic burner exit gas stream 90a, this gas stream charging is back to the 3rd gaseous heat exchanger 80, with heating and pressurizing washer discharge gas stream 60a.By catalytic burner exit gas stream 80b by being used for the exhaust gas expander of Power Recovery (power recovery), being then first disposed to off gas scrubber and being released into again in atmospheric environment.
Collect waste water steam 16b, 18b and 50c and looped back treatment facility.Waste water steam/condensation product 14b, 60b and 70c is fed to water vapour recovery system for future use.
According to embodiment of the present disclosure, provide following equipment scheme.
Equipment scheme 1
Generate an equipment for water vapour, described equipment uses in for the preparation of the system of aromatic dicarboxylic acid, and described equipment comprises:
A) the first slurries heat exchanger of thick aromatic dicarboxylic acid slurries is received;
B) hydrogenation reactor from the thick aromatic dicarboxylic acid solution of described first slurries heat exchanger is received;
C) a series of one or more crystallizer from the aromatic dicarboxylic acid solution of the purifying of described hydrogenation reactor is received; And
D) heat is sent to current to generate the water vapour maker of water vapour from the crystallizer discharge stream of the one or more crystallizers from described series.
Equipment scheme 2
Equipment according to equipment scheme 1, wherein said first slurries heat exchanger is connected to high-pressure steam source.
Equipment scheme 3
Equipment according to equipment scheme 1, described equipment also comprises
E) heat is sent to the second slurries heat exchanger of described thick aromatic dicarboxylic acid slurries from the high pressure condensation product generated by described high-pressure steam, and described second slurries heat exchanger is arranged in the upstream of described first slurries heat exchanger relative to the flow direction of described thick aromatic dicarboxylic acid slurries.
Equipment scheme 4
Equipment according to equipment scheme 1, described equipment also comprises
F) heat is sent to the 3rd slurries heat exchanger of described thick aromatic dicarboxylic acid slurries from the crystallizer discharge stream of the one or more crystallizers from described series, and described 3rd slurries heat exchanger is arranged in the upstream of described second slurries heat exchanger relative to the flow direction of described thick aromatic dicarboxylic acid slurries.
Equipment scheme 5
Equipment according to equipment scheme 4, wherein said equipment comprises a series of plural crystallizer.
Equipment scheme 6
Equipment according to equipment scheme 5, wherein said 3rd slurries heat exchanger is connected to the discharge outlet of the first crystallizer in described series.
Equipment scheme 7
Equipment according to equipment scheme 6, wherein said water vapour maker is connected to the discharge outlet of the later crystallization device in the discharge outlet of the second crystallizer in described series or described series.
Equipment scheme 8
Equipment according to equipment scheme 7, wherein water vapour maker is connected to the discharge outlet of the second crystallizer in described series.
Equipment scheme 9
Equipment according to equipment scheme 8, described equipment comprises
G) heat is sent to the 4th slurries heat exchanger of described thick aromatic dicarboxylic acid slurries from the crystallizer discharge stream from the second crystallizer described series, and described 4th slurries heat exchanger is arranged in the upstream of described 3rd slurries heat exchanger relative to the flow direction of described thick aromatic dicarboxylic acid slurries.
Equipment scheme 10
An equipment for heated air stream, described equipment uses in for the preparation of the system of aromatic dicarboxylic acid, and described equipment comprises:
A) equipment for generating water vapour according to any one in equipment scheme 1-9; And
B) heat is sent to the first gaseous heat exchanger of described gas stream from described water vapour.
Equipment scheme 11
Equipment according to equipment scheme 10, described equipment also comprises
C) heat is sent to the second gaseous heat exchanger of described gas stream, and described second gaseous heat exchanger is arranged in the upstream of described first gaseous heat exchanger relative to the flow direction of described gas stream.
Equipment scheme 12
Equipment according to equipment scheme 11, described equipment also comprises the pressurization washer processing described gas stream.
Equipment scheme 13
Equipment according to equipment scheme 12, wherein said pressurization washer is connected to described second gaseous heat exchanger.
Equipment scheme 14
Equipment according to equipment scheme 13, described equipment also comprises
D) the 3rd gaseous heat exchanger from the pressurization washer discharge gas stream of described first gaseous heat exchanger is received; And
E) catalytic burner from the pressurization washer discharge gas stream of described 3rd gaseous heat exchanger is received,
Wherein said 3rd gaseous heat exchanger also receives catalytic burner exit gas stream.
Equipment scheme 15
Equipment according to equipment scheme 1, wherein said water vapour maker is shell-and-tube exchanger.
Equipment scheme 16
For the preparation of a system for aromatic dicarboxylic acid, described system comprises the equipment according to any one in equipment scheme 1 to 15.
Equipment scheme 17
For the preparation of a system for aromatic dicarboxylic acid, described system comprises
Oxidation panel,
Crystallized region, described crystallized region comprises one or more crystallizer;
Process the distilling period from the emission gases of described oxidation panel;
Condensation segment, described condensation segment is connected to described distilling period;
To the pressurization washer that it processes before the overhead gas of self-condensation in future section is released into atmospheric environment; With
Equipment according to any one in equipment scheme 1 to 15.
In addition, in some embodiments, the disclosure also comprises following additional aspects.
Additional aspects 1
For generating a method for water vapour in the method preparing aromatic dicarboxylic acid, the described method preparing aromatic dicarboxylic acid comprises hydrocarbon precursor catalyzed oxidation in organic solvent, and the method for described generation water vapour comprises the following steps:
I) thick aromatic dicarboxylic acid slurries are heated to form thick aromatic dicarboxylic acid solution;
Ii) described thick aromatic dicarboxylic acid solution is sent to hydrogenation reactor;
Iii) the aromatic dicarboxylic acid solution of purifying is sent to a series of one or more crystallizer from described hydrogenation reactor; And
Iv) heat is sent to current water vapour maker to generate water vapour from the crystallizer discharge stream of the one or more crystallizers from described series.
Additional aspects 2
Method according to additional aspects 1, wherein at step I v) in generate water vapour be middle setting-out steam or mesohigh water vapour.
Additional aspects 3
Method according to additional aspects 2, wherein at step I v) in generate water vapour be mesohigh water vapour.
Additional aspects 4
Method according to additional aspects 2 or additional aspects 3, the pressure of wherein said mesohigh water vapour is about 10-50BarA or about 12.5-40barA or about 15-35BarA or about 17.5-30barA or about 20BarA.
Additional aspects 5
Method according to any one in additional aspects 1-4, wherein step I) comprise the following steps:
V) heat is sent to the described thick aromatic dicarboxylic acid slurries the first slurries heat exchanger from high-pressure steam.
Additional aspects 6
Method according to additional aspects 5, the pressure of wherein said high-pressure steam is about 50-150BarA or about 75-125BarA or about 100BarA.
Additional aspects 7
Method according to additional aspects 5 or additional aspects 6, its mesohigh condensation product is in step v) in produce and wherein step I) further comprising the steps of:
Vi) heat is sent to the described thick aromatic dicarboxylic acid slurries the second slurries heat exchanger from described high pressure condensation product, described second slurries heat exchanger is arranged in the upstream of described first slurries heat exchanger relative to the flow direction of described thick aromatic dicarboxylic acid slurries.
Additional aspects 8
Described thick aromatic dicarboxylic acid slurries, wherein in the upstream of the described second slurries heat exchanger of the flow direction relative to described thick aromatic dicarboxylic acid slurries, are heated at least 250 DEG C by the method according to additional aspects 7.
Additional aspects 9
Method according to additional aspects 8, wherein in the upstream of the described second slurries heat exchanger of the flow direction relative to described thick aromatic dicarboxylic acid slurries, described thick aromatic dicarboxylic acid slurries are heated at least 250 DEG C, and directly heat are not sent to described thick aromatic dicarboxylic acid slurries from high-pressure steam or high pressure condensation product.
Additional aspects 10
Method according to any one in additional aspects 7-9, wherein step I) further comprising the steps of:
Vii) heat is sent to the described thick aromatic dicarboxylic acid slurries the 3rd slurries heat exchanger from the crystallizer discharge stream of the one or more crystallizers from described series, described 3rd slurries heat exchanger is arranged in the upstream of described second slurries heat exchanger relative to the flow direction of described thick aromatic dicarboxylic acid slurries.
Additional aspects 11
Method according to additional aspects 10, wherein step I ii) comprise the aromatic dicarboxylic acid solution of the described purifying from described hydrogenation reactor is sent to two or more crystallizers a series of.
Additional aspects 12
Method according to additional aspects 11, wherein step vii) comprise described thick aromatic dicarboxylic acid slurries heat be sent to from the crystallizer discharge stream from the first crystallizer described series in described 3rd slurries heat exchanger.
Additional aspects 13
Method according to additional aspects 12, wherein step I v) comprise heat is sent to current in described water vapour maker to generate water vapour from the crystallizer discharge stream from the second crystallizer described series or the later crystallization device in described series.
Additional aspects 14
Method according to additional aspects 13, wherein step I v) comprise heat is sent to current in described water vapour maker to generate water vapour from the crystallizer discharge stream from the second crystallizer described series.
Additional aspects 15
Method according to additional aspects 14, wherein step I) further comprising the steps of:
Viii) heat is sent to the described thick aromatic dicarboxylic acid slurries in the 4th slurries heat exchanger from the crystallizer discharge stream from the second crystallizer described series, described 4th slurries heat exchanger is arranged in the upstream of described 3rd slurries heat exchanger relative to the flow direction of described thick aromatic dicarboxylic acid slurries.
Additional aspects 16
For a method for heated air stream in the method preparing aromatic dicarboxylic acid, the described method preparing aromatic dicarboxylic acid comprises hydrocarbon precursor catalyzed oxidation in organic solvent, and the method for described heated air stream comprises the following steps:
I) water vapour is generated by the method according to any one in additional aspects 1-15; And
II) in the first gaseous heat exchanger, heat is sent to described gas stream from described water vapour.
Additional aspects 17
Method according to additional aspects 16, wherein said gas stream is pressurization washer discharge gas stream.
Additional aspects 18
Method according to additional aspects 17, described method is further comprising the steps of:
III) heat is sent to the described pressurization washer discharge gas stream in the second gaseous heat exchanger, described second gaseous heat exchanger is arranged in the upstream of described first gaseous heat exchanger relative to the flow direction of described pressurization washer discharge gas stream.
Additional aspects 19
Method according to additional aspects 18, described method is further comprising the steps of:
IV) the described pressurization washer discharge gas stream from described first gaseous heat exchanger is sent to the 3rd gaseous heat exchanger;
V) the described pressurization washer discharge gas stream from described 3rd gaseous heat exchanger is sent to catalytic burner; And
VI) catalytic burner exit gas is spread deliver to described 3rd gaseous heat exchanger, make heat spread from described catalytic burner exit gas to deliver to described pressurization washer discharge gas stream.
Additional aspects 20
Method according to any one in aforementioned additional aspects, wherein said aromatic dicarboxylic acid is terephthalic acid.
Additional aspects 21
For generating an equipment for water vapour in the method preparing aromatic dicarboxylic acid, the described method preparing aromatic dicarboxylic acid comprises hydrocarbon precursor catalyzed oxidation in organic solvent, and described equipment comprises:
A) the first slurries heat exchanger, described first slurries heat exchanger arrangement is for receiving thick aromatic dicarboxylic acid slurries;
B) hydrogenation reactor, described hydrogenation reactor is configured to receive the thick aromatic dicarboxylic acid solution from described first slurries heat exchanger;
C) a series of one or more crystallizer, described one or more crystallizer is configured to receive the aromatic dicarboxylic acid solution from the purifying of described hydrogenation reactor; And
D) water vapour maker, described water vapour maker is configured to heat to be sent to current to generate water vapour from the crystallizer discharge stream of the one or more crystallizers from described series.
Additional aspects 22
Equipment according to additional aspects 21, wherein by water vapour maker d) the described water vapour that generates is middle setting-out steam or mesohigh water vapour.
Additional aspects 23
Equipment according to additional aspects 22, wherein by water vapour maker d) the described water vapour that generates is mesohigh water vapour.
Additional aspects 24
Equipment according to additional aspects 22 or additional aspects 23, the pressure of wherein said mesohigh water vapour is about 10-50BarA or about 12.5-40barA or about 15-35BarA or about 17.5-30barA or about 20BarA.
Additional aspects 25
Equipment according to any one in additional aspects 21-24, wherein said first slurries heat exchanger arrangement is for be sent to described thick aromatic dicarboxylic acid slurries by heat from high-pressure steam.
Additional aspects 26
Equipment according to additional aspects 25, the pressure of wherein said high-pressure steam is about 50-150BarA or about 75-125BarA or about 100BarA.
Additional aspects 27
Equipment according to additional aspects 25 or additional aspects 26, described equipment also comprises:
E) the second slurries heat exchanger, described second slurries heat exchanger arrangement is that heat is sent to described thick aromatic dicarboxylic acid slurries from the high pressure condensation product generated by described high-pressure steam, and is arranged in the upstream of described first slurries heat exchanger relative to the flow direction of described thick aromatic dicarboxylic acid slurries.
Additional aspects 28
Equipment according to additional aspects 26, wherein said Equipments Setting is the upstream of the described second slurries heat exchanger in the flow direction relative to described thick aromatic dicarboxylic acid slurries, and described thick aromatic dicarboxylic acid slurries are heated at least 250 DEG C.
Additional aspects 29
Equipment according to additional aspects 28, wherein said Equipments Setting is the upstream of the described second slurries heat exchanger in the flow direction relative to described thick aromatic dicarboxylic acid slurries, described thick aromatic dicarboxylic acid slurries are heated at least 250 DEG C, and directly heat are not sent to described thick aromatic dicarboxylic acid slurries from high-pressure steam or high pressure condensation product.
Additional aspects 30
Equipment according to any one in additional aspects 27-29, described equipment also comprises:
F) the 3rd slurries heat exchanger, described 3rd slurries heat exchanger arrangement is that heat is sent to described thick aromatic dicarboxylic acid slurries from the crystallizer discharge stream of the one or more crystallizers from described series, and it is arranged in the upstream of described second slurries heat exchanger relative to the flow direction of described thick aromatic dicarboxylic acid slurries.
Additional aspects 31
Equipment according to additional aspects 30, wherein said equipment comprises a series of plural crystallizer.
Additional aspects 32
Equipment according to additional aspects 31, wherein said 3rd slurries heat exchanger arrangement is that heat is sent to described thick aromatic dicarboxylic acid slurries from the crystallizer discharge stream from the first crystallizer described series.
Additional aspects 33
Equipment according to additional aspects 32, wherein said water vapour maker is configured to heat to be sent to described current to generate water vapour from the crystallizer discharge stream from the second crystallizer described series or the later crystallization device in described series.
Additional aspects 34
Equipment according to additional aspects 33, wherein said water vapour maker is configured to heat to be sent to described current to generate water vapour from the crystallizer discharge stream from the second crystallizer described series.
Additional aspects 35
Equipment according to additional aspects 34, described equipment also comprises:
G) the 4th slurries heat exchanger, described 4th slurries heat exchanger arrangement is that heat is sent to described thick aromatic dicarboxylic acid slurries from the crystallizer discharge stream from the second crystallizer described series, and it is arranged in the upstream of described 3rd slurries heat exchanger relative to the flow direction of described thick aromatic dicarboxylic acid slurries.
Additional aspects 36
For an equipment for heated air stream in the method preparing aromatic dicarboxylic acid, the described method preparing aromatic dicarboxylic acid comprises hydrocarbon precursor catalyzed oxidation in organic solvent, and described equipment comprises:
A) equipment for generating water vapour according to any one in additional aspects 21-35; And
B) the first gaseous heat exchanger, described first gaseous heat exchanger is configured to heat to be sent to described gas stream from described water vapour.
Additional aspects 37
Equipment according to additional aspects 36, wherein said gas stream is pressurization washer discharge gas stream.
Additional aspects 38
Equipment according to additional aspects 37, described equipment also comprises:
C) the second gaseous heat exchanger, described second gaseous heat exchanger is configured to heat to be sent to described gas stream, and described second gaseous heat exchanger is arranged in the upstream of described first gaseous heat exchanger relative to the flow direction of described gas stream.
Additional aspects 39
Equipment according to additional aspects 38, described equipment also comprises:
D) the 3rd gaseous heat exchanger, described 3rd gaseous heat exchanger is configured to receive the described pressurization washer discharge gas stream from described first gaseous heat exchanger; And
E) catalytic burner, described catalytic burner is configured to receive the described pressurization washer discharge gas stream from described 3rd gaseous heat exchanger,
Wherein said 3rd gaseous heat exchanger is also configured to receive catalytic burner exit gas stream and heat spread from described catalytic burner exit gas deliver to described pressurization washer discharge gas stream.
Additional aspects 40
Equipment according to any one in additional aspects 21-39, wherein said aromatic dicarboxylic acid is terephthalic acid.
Additional aspects 41
For the preparation of a method for aromatic dicarboxylic acid, the described method preparing aromatic dicarboxylic acid comprises hydrocarbon precursor catalyzed oxidation in organic solvent, and the described method preparing aromatic dicarboxylic acid comprises the following steps:
I) described hydrocarbon precursor is oxidized in organic solvent under the existence of metal catalyst provide thick aromatic dicarboxylic acid slurries;
Wherein said method is further comprising the steps of:
Ii) described thick aromatic dicarboxylic acid slurries are heated to form thick aromatic dicarboxylic acid solution;
Iii) described thick aromatic dicarboxylic acid solution is sent to hydrogenation reactor;
Iv) the aromatic dicarboxylic acid solution of purifying is sent to a series of one or more crystallizer from described hydrogenation reactor; With
V) heat is sent to current water vapour maker to generate water vapour from the crystallizer discharge stream of the one or more crystallizers from described series.
Additional aspects 42
Method according to additional aspects 41, said method comprising the steps of:
Heat is sent to the gas stream the first gaseous heat exchanger from described water vapour.
Claims (17)
1. generate an equipment for water vapour, described equipment uses in for the preparation of the system of aromatic dicarboxylic acid, and described equipment comprises:
A) the first slurries heat exchanger of thick aromatic dicarboxylic acid slurries is received;
B) hydrogenation reactor from the thick aromatic dicarboxylic acid solution of described first slurries heat exchanger is received;
C) a series of one or more crystallizer from the aromatic dicarboxylic acid solution of the purifying of described hydrogenation reactor is received; And
D) heat is sent to current to generate the water vapour maker of water vapour from the crystallizer discharge stream of the one or more crystallizers from described series.
2. equipment according to claim 1, wherein said first slurries heat exchanger is connected to high-pressure steam source.
3. equipment according to claim 2, described equipment also comprises
E) heat is sent to the second slurries heat exchanger of described thick aromatic dicarboxylic acid slurries from the high pressure condensation product generated by described high-pressure steam, and described second slurries heat exchanger is arranged in the upstream of described first slurries heat exchanger relative to the flow direction of described thick aromatic dicarboxylic acid slurries.
4. equipment according to claim 3, described equipment also comprises
F) heat is sent to the 3rd slurries heat exchanger of described thick aromatic dicarboxylic acid slurries from the crystallizer discharge stream of the one or more crystallizers from described series, and described 3rd slurries heat exchanger is arranged in the upstream of described second slurries heat exchanger relative to the flow direction of described thick aromatic dicarboxylic acid slurries.
5. equipment according to claim 4, wherein said equipment comprises a series of plural crystallizer.
6. equipment according to claim 5, wherein said 3rd slurries heat exchanger is connected to the discharge outlet of the first crystallizer in described series.
7. equipment according to claim 6, wherein said water vapour maker is connected to the discharge outlet of the later crystallization device in the discharge outlet of the second crystallizer in described series or described series.
8. equipment according to claim 7, wherein water vapour maker is connected to the discharge outlet of the second crystallizer in described series.
9. equipment according to claim 8, described equipment comprises
G) heat is sent to the 4th slurries heat exchanger of described thick aromatic dicarboxylic acid slurries from the crystallizer discharge stream from the second crystallizer described series, and described 4th slurries heat exchanger is arranged in the upstream of described 3rd slurries heat exchanger relative to the flow direction of described thick aromatic dicarboxylic acid slurries.
10. equipment according to claim 1, wherein said water vapour maker is shell-and-tube exchanger.
The equipment of 11. 1 kinds of heated air streams, described equipment uses in for the preparation of the system of aromatic dicarboxylic acid, and described equipment comprises:
A) equipment for generating water vapour according to any one in claim 1-10; And
B) heat is sent to the first gaseous heat exchanger of described gas stream from described water vapour.
12. equipment according to claim 11, described equipment also comprises
C) heat is sent to the second gaseous heat exchanger of described gas stream, and described second gaseous heat exchanger is arranged in the upstream of described first gaseous heat exchanger relative to the flow direction of described gas stream.
13. equipment according to claim 12, described equipment also comprises the pressurization washer processing described gas stream.
14. equipment according to claim 13, wherein said pressurization washer is connected to described second gaseous heat exchanger.
15. equipment according to claim 14, described equipment also comprises
D) the 3rd gaseous heat exchanger from the pressurization washer discharge gas stream of described first gaseous heat exchanger is received; And
E) catalytic burner from the pressurization washer discharge gas stream of described 3rd gaseous heat exchanger is received,
Wherein said 3rd gaseous heat exchanger also receives catalytic burner exit gas stream.
16. 1 kinds of systems for the preparation of aromatic dicarboxylic acid, described system comprises the equipment according to any one in claim 1 to 15.
17. 1 kinds of systems for the preparation of aromatic dicarboxylic acid, described system comprises
Oxidation panel,
Crystallized region, described crystallized region comprises one or more crystallizer;
Process the distilling period from the emission gases of described oxidation panel;
Condensation segment, described condensation segment is connected to described distilling period;
To the pressurization washer that it processes before the overhead gas of self-condensation in future section is released into atmospheric environment; With
Equipment according to any one in claim 1 to 15.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB1417636.6 | 2014-10-06 | ||
| GBGB1417636.6A GB201417636D0 (en) | 2014-10-06 | 2014-10-06 | Production of an aromatic dicarboxylic acid |
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| Publication Number | Publication Date |
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| CN204714728U true CN204714728U (en) | 2015-10-21 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520108168.4U Active CN204714728U (en) | 2014-10-06 | 2015-02-13 | Generate the equipment of water vapour, the equipment of heated air stream and the system for the preparation of aromatic dicarboxylic acid |
| CN202110202650.4A Pending CN112979460A (en) | 2014-10-06 | 2015-02-13 | Preparation of aromatic dicarboxylic acids |
| CN201510079766.8A Pending CN105985237A (en) | 2014-10-06 | 2015-02-13 | Production of an aromatic dicarboxylic acid |
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| CN202110202650.4A Pending CN112979460A (en) | 2014-10-06 | 2015-02-13 | Preparation of aromatic dicarboxylic acids |
| CN201510079766.8A Pending CN105985237A (en) | 2014-10-06 | 2015-02-13 | Production of an aromatic dicarboxylic acid |
Country Status (3)
| Country | Link |
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| CN (3) | CN204714728U (en) |
| GB (1) | GB201417636D0 (en) |
| WO (1) | WO2016055456A2 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| GB201417636D0 (en) * | 2014-10-06 | 2014-11-19 | Invista Tech Sarl | Production of an aromatic dicarboxylic acid |
| WO2019028097A1 (en) * | 2017-08-01 | 2019-02-07 | Bp Corporation North America Inc. | Process for pre-heating boiler feed water in the manufacture of purified aromatic carboxylic acids |
| CN112341325A (en) * | 2020-12-02 | 2021-02-09 | 台化兴业(宁波)有限公司 | Energy recovery device and method for aromatic dicarboxylic acid production process |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| DD289891A7 (en) * | 1989-03-22 | 1991-05-16 | Petrolchemie Und Kraftstoffe Ag,De | PROCESS FOR CLEANING TEREPHTHALIC ACID |
| JP4869758B2 (en) * | 2006-03-27 | 2012-02-08 | 三井化学株式会社 | Method for producing high purity terephthalic acid |
| CN101637699B (en) * | 2008-08-02 | 2012-01-25 | 中国石油化工股份有限公司 | Method for purifying waste gas of pure terephthalic acid producing device |
| GB201417636D0 (en) * | 2014-10-06 | 2014-11-19 | Invista Tech Sarl | Production of an aromatic dicarboxylic acid |
-
2014
- 2014-10-06 GB GBGB1417636.6A patent/GB201417636D0/en not_active Ceased
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- 2015-02-13 CN CN201520108168.4U patent/CN204714728U/en active Active
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Also Published As
| Publication number | Publication date |
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| CN112979460A (en) | 2021-06-18 |
| WO2016055456A3 (en) | 2016-06-02 |
| WO2016055456A2 (en) | 2016-04-14 |
| GB201417636D0 (en) | 2014-11-19 |
| CN105985237A (en) | 2016-10-05 |
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