CN103087778B - Jet pipe, fluidized bed reactor with jet pipe and coal catalyzing and gasifying method - Google Patents
Jet pipe, fluidized bed reactor with jet pipe and coal catalyzing and gasifying method Download PDFInfo
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- CN103087778B CN103087778B CN201310032098.4A CN201310032098A CN103087778B CN 103087778 B CN103087778 B CN 103087778B CN 201310032098 A CN201310032098 A CN 201310032098A CN 103087778 B CN103087778 B CN 103087778B
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Abstract
The invention relates to a jet pipe, a fluidized bed reactor with the jet pipe and a coal catalyzing and gasifying method. A plurality of jet pipes which are in a bed-layer dispersing manner are adopted for feeding oxygen; the jet pipes are in a sleeve type structure; a central pipe is supplied with a mixture gas of oxygen and over-hot steam; the over-hot steam is supplied into annular spaces; the ratio of the oxygen to the over-hot steam is regulated to control the oxygen concentration to be within a certain range; the oxygen and a carbon material are mainly subjected to combustion strong exothermic reaction at a jet flow area; the released heat is used for providing heat for the gasification reaction in the reactor; the over-hot steam supplied into the annular spaces can intensity the internal circulation of carbon material granules, is subjected to heat exchange with a high-temperature gas at a central pipe area, and at the same time provide heat for the gasification heat absorption reaction in the annular spaces, so that partial high-temperature areas are prevented from happening through rapid heat exchange and gasification heat absorption reaction, and the happening rate that the jet pipe area has slag build-up is reduced.
Description
Technical field
The present invention relates to catalytic coal gasifaction technical field, relate in particular to a kind of jet pipe, fluidized-bed reactor and catalytic coal gasifaction method with this jet pipe.The present invention is not only applicable to catalytic coal gasifaction technique, is equally applicable to logical oxygen metallization processes and coal and the biomass gasifying process altogether of low ash smelting point, clinker(ing) coal.
Background technology
Along with developing rapidly and the increasingly stringent of environmental regulations of economy, in the following more than ten years, China will be explosive growth to the demand of this clean energy of Sweet natural gas, though and gas production has and increases far below demand, imbalance between supply and demand becomes increasingly conspicuous, and supply breach strengthens year by year.In view of the feature of China's Energy resources situation " rich coal, few oil, deficency "; long term maintenance can not change in a short time taking coal as main energy consumption structure; according to the development trend of the development trend of clean coal technology and world's low-carbon economy; coal is changed into top quality fuel-Sweet natural gas in fossil energy, is to be applicable to China's national situation, to dissolve energy dilemma and to ensure a shortcut of energy security.
Common Coal Gasification Technology, coal at high temperature with oxygen (or air) and/or water vapor (H
2o) vaporized chemical of composition carries out gasification reaction, generates and contains a small amount of methane (CH
4) synthetic gas (being mainly hydrogen, carbon monoxide and carbonic acid gas), carry out afterwards hydrosphere transformation and methanation operation, adopt two-step approach prepare methane.This Coal Gasification Technology has that the required temperature of gasification reaction is high, energy consumption is large, high to equipment requirements, and needs the shortcomings such as three reaction units, technique are more complicated.
Catalytic coal gasifaction technology is the clean efficient a kind of important way utilized of coal.Adopt catalytic coal gasifaction technology, coal at relatively low temperature with water vapor (H
2o), hydrogen (H
2), the vaporized chemical of carbon monoxide (CO) composition carries out gasification reaction under the katalysis of catalyzer, generates the methane (CH of high density
4).Catalytic coal gasifaction technology, compared with other Coal Gasification Technology, has the advantages such as methane content is high, gasification reaction is required temperature is low.
Existing catalysis gasification technique all adopts outer heat-supplying mode, U.S. EXXON, GPE company disclose this catalytic gasification technology, see patent US4318712, US2009246120A1, US2009165376A1, all need with a large amount of superheated vapours and cyclic part gas product carbon monoxide, hydrogen enters the heat release of vapourizing furnace generation methanation reaction that system institute heat requirement is provided, adopting low temperature separation process, gas product partial oxidation or setting up combustion oxygen vapourizing furnace provides superheated vapour and CO, H
2, the energy consumption of technique is all larger, and facility investment is high, technical process complexity, steam superheating system and heat exchange system load are higher, to sum up cause technique macroeconomic not good, and total efficiency is lower.
The mode that development adopts outer heat supply to meet the required heat of gasification on a small scale still can, the mode that industrialization adopts outer heat supply to meet the required heat of gasification is invested huge, and in engineering, be difficult to realize, need to adopt fire coal to provide institute's heat requirement from heat-supplying mode for catalytic gasification reacts, maintain furnace temperature in certain temperature of reaction, without appending other equipment, technical process is simple, and Technical Economy is better.Adding of catalyzer can catalyst combustion reaction, improves carbonaceous material burning thermal discharge, and the base metal catalysts simultaneously adding may form low temperature fused matter with coal mineral under certain processing condition, reaction atmosphere, reduces the ash fusion point of coal; And catalysis gasification technique requires longer gas-solid contact time, bed is relatively high, the even flash heat transfer in full bed region difficulty relatively, in bed, local temperature is too high causes the coal ash particle slagging scorification that mutually bonds, cause fluidized state bad, deslagging difficulty when serious, defluidization etc. even, cause reactor to be difficult to continuous and steady operation.
Fluidized-bed reactor because its gas-solid mixing fully and the advantage such as transfer efficiency height and be widely used in gasification field.Industrialized U-gas vapourizing furnace, KRW and ash melt poly-vapourizing furnace and all adopt single efflux nozzle at present, i.e. one-jet fluidized-bed, and gas-solid contact efficiency is low, easily forms district of localized hyperthermia and causes slagging scorification.
CN1974733A discloses a kind of coal and biomass multiple fluid jet combined fluidized-bed gasifying device.Although it can provide higher gas-solid contact efficiency with respect to one-jet fluidized-bed, but for higher jet fluidized-bed of bed, because of solid particulate back-mixing less turbulence more slow, multiple efflux nozzles are distributed in the localized hyperthermia forming in same level and are difficult to be passed to fast full bed, are also easier to slagging scorification.
Current existing one-jet fluidized-bed and how jet fluidized-bed gasification installation, all exist gas-solid contact efficiency low, easily form the problem that district of localized hyperthermia causes slagging scorification, especially for higher jet fluidized-bed of bed, because of solid particulate back-mixing less turbulence more slow, multiple efflux nozzles are distributed in the localized hyperthermia forming in same level and are difficult to be passed to fast full bed, are also easier to slagging scorification.
Summary of the invention
The object of the invention is to for the existing jet fluidized-bed deficiency that is applied to gasification field, propose a kind of jet pipe, fluidized-bed reactor and catalytic coal gasifaction method with this jet pipe.
The present invention adopts and disperses oxygen supply that reaction institute heat requirement is provided, oxygen enters reactor by the multiple jet pipes of bed, ensures that oxygen is uniformly distributed, by regulating water vapour, oxygen blending ratio control oxygen concn in certain limit, avoid occurring district of bed localized hyperthermia, reduce slagging scorification probability.
For reaching this object, the present invention by the following technical solutions:
One of object of the present invention is to provide a kind of jet pipe, and described jet pipe is telescoping, comprises pipe core and the outer tube around pipe core; Between described pipe core and outer tube, form annular space.
Jet pipe of the present invention is formed by pipe core and outer tube suit, when application, in pipe core, pass into the gas mixture of oxygen and superheated vapour, described oxygen and the thermopositive reaction of carbonaceous material generation catalyticcombustion, for the gasification reaction in fluidized-bed reactor provides heat, realize coal-fired from heat supply; Because high calorie easily causes particles of carbonaceous material melting slagging scorification, therefore in annular space, pass into superheated vapour, strengthen the less turbulence in the pipe core region of jet pipe, thereby strengthen the heat exchange degree of pipe core region high-temperature medium, simultaneously the superheated vapour in annular space with carry out thermal exchange from the gas mixture of pipe core, the heat in time the pipe core exit region generation catalyticcombustion thermopositive reaction of jet pipe being produced changes away evacuation in time, reduces fluerics slagging scorification risk; Meanwhile, the superheated vapour in annular space can accelerate C and H after heat exchange improves temperature
2the speed of the thermo-negative reaction of O, further leads away heat, more reduces fluerics slagging scorification risk.
Described jet pipe is formed by connecting by horizontal section and vertical section; Preferably, the exit end of described outer tube is ejector nozzle shape.The exit end of outer tube is designed to ejector nozzle shape, can more effectively strengthens medium in annular space and, with the heat exchange of fluerics high-temperature gas, strengthen particles of carbonaceous material internal recycle, avoid the appearance in district of localized hyperthermia, solve better slagging scorification problem.
Two of object of the present invention is to provide a kind of how jet fluidized-bed reactor, and described reactor adopts at least one jet pipe as above as bed distribution device.Using above-mentioned jet pipe as bed distribution device, not only can realize coal-fired confession heat in fluidized-bed reactor, and can avoid slagging scorification problem.
Bed distribution device of the present invention is made up of multiple jet pipes.The distribution form of described multiple jet pipe in fluidized-bed there is no particular form, and those skilled in the art can carry out equidistantly or non-equidistance distribution according to practical situation.Same level gas passes into a mouthful number and can be one or radially multiple, and axial distribution device also can be set in bed, ensures that overall bed oxygen is uniformly dispersed.For example can adopt following two kinds of forms to arrange jet pipe:
(1) symmetrical two or more jet pipes in the interior same level of described reactor, the while arranges the jet pipe of multilayer symmetry arrangement vertically; Be described bed distribution device by multilayer vertically symmetrical multiple jet pipes form.
(2) multiple jet pipes are distributed in reactor vertically with asymmetrical form, and described bed distribution device is made up of multiple jet pipes of asymmetric distribution vertically.
The concrete structure of reactor of the present invention is as follows: described reactor comprises:
Reactor body, its inner chamber that forms;
Conical distribution plate, is positioned at described reactor body bottom, and forms air chamber between the wall of reactor body bottom;
Feeding line, runs through and is arranged at reactor body top, with described chamber in fluid communication, enters in described chamber for material carbon material;
Vaporized chemical pipeline, runs through and is arranged at reactor body bottom, is opened on air chamber, enters in described chamber by conical distribution plate for vaporized chemical;
Bed distribution device, runs through the sidewall that is arranged at reactor body, with described chamber in fluid communication;
Discharging pipeline, runs through and is arranged at reactor body top, with described chamber in fluid communication, discharges reactor for gaseous product.
Reactor body of the present invention has bearing capacity, can tolerate and maintain the temperature and pressure in respective inner space, is made up of pressure-resistant material.Described feeding line and vaporized chemical pipeline, for described material being introduced under certain pressure to inside reactor chamber, mix laggard row gasification reaction.Described discharging pipeline is discharged reactor for the gaseous product after gasification reaction.Those skilled in the art, according to practical condition, can determine the number that above-mentioned respective lines is required, better to realize function separately, realize object of the present invention.
In the present invention, vaporized chemical pipeline installing is in the bottom of reactor body, and gas-solid two-phase, in the indoor abundant contact of reactor cavity, is beneficial to and reaches fluidized state.In addition, vaporized chemical is simultaneously as fluidizing medium, and in reactor, gasification temperature is even.Vaporized chemical, from vaporized chemical pipeline enters, is uniformly distributed through conical distribution plate by air chamber, then enter reactor cavity indoor with carbonaceous material carry out gasification reaction, can make reaction in whole chamber, carry out simultaneously, raw material is made full use of.
Reactor of the present invention also comprises deslagging pipeline, runs through described reactor body and conical distribution plate, is opened on described chamber, discharges reactor for the remaining semicoke after gasification.In the present invention, carbonaceous material and vaporized chemical reactor cavity is indoor react after, gaseous product from discharging pipeline discharge reactor, gasification after produce semicoke product from deslagging pipeline discharge reactor.
Three of object of the present invention is to provide a kind of method of utilizing fluidized-bed reactor as above to carry out catalytic coal gasifaction:
Make carbonaceous material and vaporized chemical enter reactor cavity indoor, vaporized chemical reacts with carbonaceous material generating gasification;
To the gas mixture that passes into oxygen and superheated vapour in the pipe core of the jet pipe as bed distribution device; Described oxygen and the thermopositive reaction of carbonaceous material generation catalyticcombustion, for gasification reaction provides heat;
In annular space, pass into superheated vapour; Evacuate with the heat that catalyticcombustion thermopositive reaction is produced;
The gaseous product that gasification reaction is generated is discharged reactor from discharging pipeline; Remaining semicoke is discharged to reactor through deslagging pipeline.
The present invention is in the time of actually operating, and making to add the material carbon material of catalyzer and vaporized chemical, to enter reactor cavity indoor, and vaporized chemical reacts with carbonaceous material generating gasification under the effect of catalyzer.
Catalytic coal gasifaction method of the present invention is specific as follows:
The carbonaceous material of impregnated catalyst enters chamber of the reactor through feeding line, and vaporized chemical enters chamber of the reactor by air chamber through vaporized chemical pipeline after conical distribution plate gas distribution, and vaporized chemical reacts with material carbon material generating gasification under the effect of catalyzer;
The gas mixture that passes into oxygen and superheated vapour as the pipe core of the jet pipe of bed distribution device, passes into superheated vapour in annular space; Described oxygen and the heat release of carbonaceous material generation catalyticcombustion, for gasification reaction provides heat; Superheated vapour strengthening jet pipe turbulence heat exchange in annular space, the while is carried out thermal exchange with the high-temperature gas in pipe core, avoids the appearance in district of localized hyperthermia;
The gaseous product generating after gasification reaction is discharged reactor from discharging pipeline, and remaining semicoke is discharged reactor through deslagging pipeline.
Vaporized chemical of the present invention is superheated vapour, or O
2, CO or H
2in a kind of or at least two kinds with the mixed gas of superheated vapour.Typical but non-limiting example comprises superheated vapour, superheated vapour and O
2combination, the combination of superheated vapour and CO, superheated vapour and H
2combination, superheated vapour, CO and H
2combination, superheated vapour, O
2, CO and H
2combination etc., all can be used for implementing the present invention.
Preferably, the oxygen concentration in described vaporized chemical is 0 ~ 20mol%, for example 0.2 ~ 18.9mol%, 3 ~ 16mol%, 5.5 ~ 14.6mol%, 7 ~ 12mol%, 9mol% etc., more preferably 0 ~ 10mol%.
Preferably, the steam that described superheated vapour is produced by boiler and gaseous product carry out thermal exchange and obtain, and after heat exchange, temperature is 300 ~ 500 DEG C; Preferably, in described vaporized chemical, the water carbon mol ratio of superheated vapour and carbonaceous material is 0.5 ~ 3:1, for example 0.52 ~ 2.95:1,0.7 ~ 2.45:1,1.1 ~ 2.06:1,1.5 ~ 2:1,1.8:1 etc., preferably 1 ~ 2:1.
In the gas mixture that described pipe core passes into, oxygen concentration is by regulating the amount control of superheated vapour.Oxygen concentration≤30mol%, for example 0.1 ~ 29.6mol%, 0.75 ~ 26mol%, 1.2 ~ 24.3mol%, 4 ~ 21.7mol%, 8.6 ~ 18mol%, 10 ~ 16mol%, 13.4mol% etc., more preferably 5 ~ 20mol%.In the present invention, only need to control steam and oxygen proportion adjusting oxygen concentration, leading to how much oxygen and water vapour as for needs loses enthusiasm condition by fluidized-bed and determines, lose the hot more oxygen ability additional heat that needs to burn more, need to pass into more oxygen, some more jet pipes are set, but the water vapour of the vaporized chemical that the steam vapour amount totally passing into passes into respect to vaporized chemical pipeline is little.
Preferably, the superheat steam temperature passing in described annular space is 300 ~ 500 DEG C, for example 300.2 ~ 486 DEG C, and 316 ~ 470 DEG C, 330 ~ 453 DEG C, 356 ~ 435 DEG C, 370 ~ 413 DEG C, 386 DEG C etc.
Preferably, the service temperature of gasification reaction is 600 ~ 800 DEG C, for example 600.3 ~ 789.6 DEG C, and 625 ~ 770 DEG C, 645 ~ 748 DEG C, 680 ~ 720 DEG C, 695 ~ 703 DEG C etc., further preferably 750 DEG C.Working pressure is 0 ~ 5MPa, for example 0.1 ~ 4.99MPa, 0.2 ~ 4.5MPa, 0.5 ~ 3.5MPa etc., further preferred 0.3 ~ 4MPa.
The composition of described gaseous product is CH
4, CO, H
2, CO
2, a small amount of H
2s and NH
3and part entrained fines.In deslagging pipeline, pass into vaporized chemical, control bed drain purge by controlling tolerance size.
Under certain temperature, pressure condition, carbonaceous material with reactions such as vaporized chemical generating gasification, conversion, methanations, generates CH under the effect of catalyzer
4, CO, H
2deng available gas composition and CO
2, a small amount of H
2s and NH
3deng and part entrained fines discharge through discharging pipeline from reactor top outlet.In fluidized-bed reactor, principal reaction is as follows:
2C+2H
2O→2H
2+2CO（1）
CO+H
2O→CO
2+H
2（2）
3H
2+CO→CH
4+H
2O（3）
C+2H
2→CH
4（4）
2C+O
22CO（5）
C+O
2→CO
2（6）
Remaining semicoke after gasification is discharged reactor through deslagging pipeline, in deslagging pipeline, passes into the vaporized chemicals such as superheated vapour, carbon monoxide, hydrogen, and controls bed drain purge by the amount of controlling vaporized chemical.
Compared with prior art scheme, the present invention has following beneficial effect:
Multiple jet pipes that the present invention adopts bed to disperse enter oxygen, and jet pipe structure is telescoping, and the gas mixture of the logical oxygen of pipe core and superheated vapour by hot steam, regulates oxygen and superheated vapour proportioning control oxygen concn in certain limit in annular space; Described oxygen and carbonaceous material be the main burning strong exothermal reaction that occurs in fluerics, and the heat of release provides heat for the gasification reaction in reactor; The superheated vapour passing in annular space, can strengthen the internal recycle of particles of carbonaceous material, and carry out thermal exchange with the high-temperature gas in pipe core region, simultaneously for the thermo-negative reaction of gasifying in annular space provides heat, through the appearance in district of localized hyperthermia, the Probability of reduction jet pipe region slagging scorification are avoided in heat exchange and gasification thermo-negative reaction fast.
The fire coal that the present invention adopts provides institute's heat requirement from heat-supplying mode for catalytic gasification reacts, and without appending other equipment, technical process is simple, and Technical Economy is better, and single stove is realized the coupling of heat material, and total efficiency is higher; And technique provided by the invention easily realizes in engineering, industrialization is amplified simple, and prospect is huge.
Brief description of the drawings
Fig. 1 is a kind of structural representation of how jet fluidized-bed reactor of the present invention;
Fig. 2 is the another kind of structural representation of how jet fluidized-bed reactor of the present invention;
Fig. 3 is a kind of structural representation of jet pipe of the present invention;
Fig. 4 is the another kind of structural representation of jet pipe of the present invention;
Fig. 5 is the slagging scorification situation map adopting in the fluidized-bed reactor of conventional one channel jet pipe.
Wherein, Fig. 1 is that from the difference of Fig. 2 the arrangement form of multiple jet pipes is different; The difference of Fig. 3 and Fig. 4 is that the outer tube exit end shape of jet pipe is different.
In figure: 1-pipe core; 2-outer tube; 3-annular space; 41-bed distribution device; 42-conical distribution plate; 43-feeding line; 44-air chamber; 45-deslagging pipeline; 46-vaporized chemical pipeline; 47-discharging pipeline.
The present invention is described in more detail below.But following example is only simple and easy example of the present invention, does not represent or limit the scope of the present invention, and protection scope of the present invention is as the criterion with claims.
Embodiment
For the present invention is described better, be convenient to understand technical scheme of the present invention, typical but non-limiting embodiment of the present invention is as follows:
Embodiment 1
As depicted in figs. 1 and 2, a kind of how jet fluidized-bed reactor, described reactor comprises:
Reactor body, its inner chamber that forms;
Conical distribution plate 42, is positioned at described reactor body bottom, and forms air chamber 44 between the wall of reactor body bottom;
Feeding line 43, runs through and is arranged at reactor body top, with described chamber in fluid communication, enters in described chamber for material carbon material;
Vaporized chemical pipeline 46, runs through and is arranged at reactor body bottom, is opened on air chamber 44, enters in described chamber by conical distribution plate 42 for vaporized chemical;
Bed distribution device 41, runs through the sidewall that is arranged at reactor body, with described chamber in fluid communication;
Discharging pipeline 47, runs through and is arranged at reactor body top, with described chamber in fluid communication, discharges reactor for gaseous product;
Deslagging pipeline 45, runs through described reactor body and conical distribution plate 42, is opened on described chamber, discharges reactor for the remaining semicoke after gasification.
Described bed distribution device 41 is made up of multiple jet pipes; Described multiple jet pipe is equidistant or unequal-interval distribution in reactor.
In Fig. 1, symmetrical two or more jet pipes in same level in described reactor, the while arranges multiple jet pipes of multilayer symmetry arrangement vertically, and in Fig. 2, multiple jet pipes are distributed in reactor vertically with asymmetrical form.
As shown in Figure 3 and Figure 4, described jet pipe is telescoping, comprises pipe core 1 and the outer tube 2 around pipe core 1; Between described pipe core 1 and outer tube 2, form annular space 3.Described jet pipe is formed by connecting by horizontal section and vertical section.In Fig. 3, the exit end of described outer tube 2 is straight tube shape.In Fig. 4, the exit end of described outer tube 2 is ejector nozzle shape.
Embodiment 2
A kind of method of utilizing how jet fluidized-bed reactor to carry out catalytic coal gasifaction, the carbonaceous material of impregnated catalyst is entered to chamber of the reactor through feeding line 43, vaporized chemical enters chamber of the reactor by air chamber 44 through vaporized chemical pipeline 46 after the even gas distribution of conical distribution plate 42, and vaporized chemical reacts with carbonaceous material generating gasification under the effect of catalyzer; Described vaporized chemical is superheated vapour and O
2mixed gas, oxygen concentration is wherein 5mol%, the water carbon mol ratio of vaporized chemical and carbonaceous material is 3.
The gas mixture that passes into oxygen and superheated vapour as the pipe core 1 of the jet pipe of bed distribution device 41, passes into superheated vapour in annular space 3; Described oxygen and the heat release of carbonaceous material generation catalyticcombustion, for gasification reaction provides heat; Superheated vapour strengthening jet pipe turbulence heat exchange in annular space 3, carries out thermal exchange with the high-temperature gas in pipe core 1 region simultaneously, avoids the appearance in district of localized hyperthermia.
Symmetrical two jet pipes in same level in described reactor, the while arranges the jet pipe of three layers of symmetry arrangement vertically, and oxygen can enter reactor by bed distribution device 41 from the multiple positions of bed, ensures that overall bed oxygen is uniformly dispersed.Oxygen concentration is by the control of steam regulation amount, and oxygen concentration is 25mol%, and oxygen total flux regulates according to equipment for gasification temperature requirement, and for catalytic gasification provides required heat, red-tape operati temperature is at 750 DEG C, and working pressure is at 2.5MPa.
Carbonaceous material with reactions such as vaporized chemical generating gasification, conversion, methanations, generates CH under the effect of catalyzer
4, CO, H
2deng available gas composition and CO
2, a small amount of H
2s and NH
3deng and part entrained fines discharge through discharging pipeline 47 from reactor top outlet.Remaining semicoke after gasification is discharged reactor through deslagging pipeline 45, and deslagging pipeline 45 can pass into vaporized chemical, controls bed drain purge by controlling tolerance size.
The steam that boiler produces and discharging pipeline expellant gas product carry out using as the superheated vapour in the present embodiment after thermal exchange in heat-exchange equipment, and after heat exchange, temperature is 400 DEG C.
Embodiment 3
A kind of method of utilizing how jet fluidized-bed reactor to carry out catalytic coal gasifaction, the carbonaceous material of impregnated catalyst is entered to chamber of the reactor through feeding line 43, vaporized chemical enters chamber of the reactor by air chamber 44 through vaporized chemical pipeline 46 after conical distribution plate 42 gas distributions, and vaporized chemical reacts with carbonaceous material generating gasification under the effect of catalyzer; Described vaporized chemical is superheated vapour, and controlling water carbon mol ratio is 2.5;
The gas mixture that passes into oxygen and superheated vapour as the pipe core 1 of the jet pipe of bed distribution device 41, passes into superheated vapour in annular space 3; Described oxygen and the heat release of carbonaceous material generation catalyticcombustion, for gasification reaction provides heat; Superheated vapour strengthening jet pipe turbulence heat exchange in annular space 3, carries out thermal exchange with the high-temperature gas in pipe core 1 region simultaneously, avoids the appearance in district of localized hyperthermia;
In described reactor, three jet pipes are distributed in reactor vertically with asymmetrical form, and oxygen can enter reactor by bed distribution device 41 from the multiple positions of bed, ensures that overall bed oxygen is uniformly dispersed.Oxygen concentration is by the control of steam regulation amount, and oxygen concentration is 20mol%, and oxygen total flux regulates according to equipment for gasification temperature requirement, and for catalytic gasification provides required heat, red-tape operati temperature is at 700 DEG C, and working pressure is at 3.5MPa.
Carbonaceous material with reactions such as vaporized chemical generating gasification, conversion, methanations, generates CH under the effect of catalyzer
4, CO, H
2deng available gas composition and CO
2, a small amount of H
2s and NH
3deng and part entrained fines discharge through discharging pipeline 47 from reactor top outlet.Remaining semicoke after gasification is discharged reactor through deslagging pipeline 45, and deslagging pipeline 45 agent of can ventilating is controlled bed drain purge by controlling tolerance size.
The steam that boiler produces and discharging pipeline expellant gas product carry out using as the superheated vapour of the present embodiment after thermal exchange in heat-exchange equipment, and after heat exchange, temperature is 450 DEG C.
Embodiment 4
A kind of method of utilizing how jet fluidized-bed reactor to carry out catalytic coal gasifaction, the carbonaceous material of impregnated catalyst is entered to chamber of the reactor through feeding line 43, vaporized chemical enters chamber of the reactor by air chamber 44 through vaporized chemical pipeline 46 after conical distribution plate 42 gas distributions, and vaporized chemical reacts with carbonaceous material generating gasification under the effect of catalyzer; Described vaporized chemical is superheated vapour, CO, H
2mixed gas, CO, H wherein
2mol ratio is 1:3, and both account for the 30mol% of vaporized chemical total amount, and the water carbon mol ratio of controlling vaporized chemical and carbonaceous material is 2;
The gas mixture that passes into oxygen and superheated vapour as the pipe core 1 of the jet pipe of bed distribution device 41, passes into superheated vapour in annular space 3; Described oxygen and the heat release of carbonaceous material generation catalyticcombustion, for gasification reaction provides heat; Superheated vapour strengthening jet pipe turbulence heat exchange in annular space 3, the while is carried out thermal exchange with the high-temperature gas in pipe core 1, avoids the appearance in district of localized hyperthermia;
Symmetrical two jet pipes in same level in described reactor, the while arranges the jet pipe of three layers of symmetry arrangement vertically, and oxygen can enter reactor by bed distribution device 41 from the multiple positions of bed, ensures that overall bed oxygen is uniformly dispersed.Oxygen concentration is by the control of steam regulation amount, and oxygen concentration is 15mol%, and oxygen total flux regulates according to equipment for gasification temperature requirement, and for catalytic gasification provides required heat, red-tape operati temperature is at 700 DEG C, and working pressure is at 3.5MPa.
Carbonaceous material with reactions such as vaporized chemical generating gasification, conversion, methanations, generates CH under the effect of catalyzer
4, CO, H
2deng available gas composition and CO
2, a small amount of H
2s and NH
3deng and part entrained fines discharge through discharging pipeline 47 from reactor top outlet.Remaining semicoke after gasification is discharged reactor through deslagging pipeline 45, and the deslagging pipeline agent of can ventilating is controlled bed drain purge by controlling tolerance size.
The steam that boiler produces and discharging pipeline expellant gas product carry out using as the superheated vapour of the present embodiment after thermal exchange in heat-exchange equipment, and after heat exchange, temperature is 500 DEG C.
Applicant's statement, the present invention illustrates detailed structure feature of the present invention and catalysis gasification method by above-described embodiment, but the present invention is not limited to above-mentioned detailed structure feature and catalysis gasification method, do not mean that the present invention must rely on above-mentioned detailed structure feature and catalysis gasification method could be implemented.Person of ordinary skill in the field should understand, any improvement in the present invention, and the selections of the equivalence replacement to the selected parts of the present invention and the increase of accessory, concrete mode etc., within all dropping on protection scope of the present invention and open scope.
The test raw material that the present invention adopts is not for connecting ditch bituminous coal (particle diameter is 20 ~ 80 orders), and its technical analysis and ultimate analysis are shown in Table 1:
Table 1 does not connect technical analysis and the ultimate analysis of ditch bituminous coal
In fluidized bed reaction, adopt respectively conventional one channel jet pipe and the present embodiment jet pipe to contrast, concrete technology condition and result are as shown in table 2:
Table 2 contrasts processing condition and result
Claims (20)
1. utilize fluidized-bed reactor to carry out a method for catalytic coal gasifaction, it is characterized in that, make carbonaceous material and vaporized chemical enter reactor cavity indoor, vaporized chemical reacts with carbonaceous material generating gasification;
To the gas mixture that passes into oxygen and superheated vapour in the pipe core (1) of the jet pipe as bed distribution device (41); Described oxygen and the thermopositive reaction of carbonaceous material generation catalyticcombustion, for gasification reaction provides heat;
In annular space (3), pass into superheated vapour; Evacuate with the heat that catalyticcombustion thermopositive reaction is produced;
The gaseous product that gasification reaction is generated is discharged reactor from discharging pipeline (47); Remaining semicoke is discharged to reactor through deslagging pipeline (45);
Oxygen concentration in described vaporized chemical is 0～20mol%;
Described reactor adopts at least one jet pipe as bed distribution device (41); Described jet pipe is telescoping, comprises pipe core (1) and the outer tube (2) around pipe core (1); Between described pipe core (1) and outer tube (2), form annular space (3); Described jet pipe is formed by connecting by horizontal section and vertical section;
Vaporized chemical pipeline (46), runs through and is arranged at reactor body bottom, is opened on air chamber (44), enters in described chamber by conical distribution plate (42) for vaporized chemical;
In the gas mixture that described pipe core (1) passes into, oxygen concentration is 5-30mol%.
2. the method for claim 1, is characterized in that, the exit end of described outer tube (2) is ejector nozzle shape.
3. the method for claim 1, is characterized in that, described bed distribution device (41) is made up of multiple jet pipes; Described multiple jet pipe is equidistantly in reactor or non-equidistance distributes.
4. method as claimed in claim 3, is characterized in that, described bed distribution device (41) by multilayer vertically symmetrical multiple jet pipes form;
Or described bed distribution device (41) is made up of multiple jet pipes of asymmetric distribution vertically.
5. the method as described in claim 3 or 4, is characterized in that, described reactor comprises:
Reactor body, its inner chamber that forms;
Conical distribution plate (42), is positioned at described reactor body bottom, and forms air chamber (44) between the wall of reactor body bottom;
Feeding line (43), runs through and is arranged at reactor body top, with described chamber in fluid communication, enters in described chamber for raw material;
Vaporized chemical pipeline (46), runs through and is arranged at reactor body bottom, is opened on air chamber (44), enters in described chamber by conical distribution plate (42) for vaporized chemical;
Bed distribution device (41), runs through the sidewall that is arranged at reactor body, with described chamber in fluid communication;
Discharging pipeline (47), runs through and is arranged at reactor body top, with described chamber in fluid communication, discharges reactor for gaseous product.
6. method as claimed in claim 5, it is characterized in that, described reactor also comprises deslagging pipeline (45), runs through described reactor body and conical distribution plate (42), be opened on described chamber, discharge reactor for the remaining semicoke after gasification.
7. the method for claim 1, is characterized in that, described vaporized chemical is superheated vapour, or O
2, CO or H
2in a kind of or at least two kinds with the mixed gas of superheated vapour.
8. the method for claim 1, is characterized in that, the oxygen concentration in described vaporized chemical is 0～10mol%.
9. the method for claim 1, is characterized in that, the steam that described superheated vapour is produced by boiler and gaseous product carry out thermal exchange and obtain, and after heat exchange, temperature is 300～500 DEG C.
10. the method for claim 1, is characterized in that, the water carbon mol ratio of described vaporized chemical and carbonaceous material is 0.5～3:1.
11. methods as claimed in claim 10, is characterized in that, the water carbon mol ratio of described vaporized chemical and carbonaceous material is 1～2:1.
12. the method for claim 1, is characterized in that, in the gas mixture that described pipe core (1) passes into, oxygen concentration is by regulating the amount control of superheated vapour.
13. methods as claimed in claim 12, is characterized in that, in the gas mixture that described pipe core (1) passes into, oxygen concentration is 5～20mol%.
14. methods as claimed in claim 12, is characterized in that, the superheat steam temperature passing in described annular space is 300～500 DEG C.
15. methods as claimed in claim 12, is characterized in that, the service temperature of gasification reaction is 600～800 DEG C.
16. methods as claimed in claim 15, is characterized in that, the service temperature of gasification reaction is 750 DEG C.
17. methods as claimed in claim 12, is characterized in that, working pressure is 0～5MPa.
18. methods as claimed in claim 17, is characterized in that, working pressure is 0.3～4MPa.
19. the method for claim 1, is characterized in that, the composition of described gaseous product is CH
4, CO, H
2, CO
2, a small amount of H
2s and NH
3and part entrained fines.
20. methods as claimed in claim 19, is characterized in that, in deslagging pipeline (45), pass into vaporized chemical, and control bed drain purge by the amount that control passes into vaporized chemical.
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| CN103992820B (en) * | 2014-05-16 | 2017-01-11 | 新奥科技发展有限公司 | Comprehensive utilization method of coal gangue |
| CN103992821B (en) * | 2014-05-16 | 2017-01-11 | 新奥科技发展有限公司 | Coal gasification method |
| CN104178224B (en) * | 2014-08-07 | 2017-04-05 | 新奥科技发展有限公司 | A kind of gas distributor, gasification furnace and carbonaceous material gasification process |
| CN104178223B (en) * | 2014-08-12 | 2017-05-31 | 新奥科技发展有限公司 | A kind of catalytic coal gasifaction method |
| CN106010665B (en) * | 2016-07-21 | 2019-04-05 | 新奥科技发展有限公司 | A kind of fluidized bed coal gasification device and method |
| CN107177384B (en) * | 2017-07-11 | 2020-06-19 | 新奥科技发展有限公司 | Catalytic gasification device, system and method |
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