CN102079685A - Coal gasification process for methane preparation by two stage gasification stove - Google Patents
Coal gasification process for methane preparation by two stage gasification stove Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/08—Production of synthetic natural gas
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/463—Gasification of granular or pulverulent flues in suspension in stationary fluidised beds
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- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/466—Entrained flow processes
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- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
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- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
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- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0943—Coke
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- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0959—Oxygen
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- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0966—Hydrogen
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- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0969—Carbon dioxide
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
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- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0983—Additives
- C10J2300/0986—Catalysts
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- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
- C10J2300/1656—Conversion of synthesis gas to chemicals
- C10J2300/1662—Conversion of synthesis gas to chemicals to methane (SNG)
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Abstract
The invention relates to a coal gasification process for methane preparation, including the following steps that: a. coal is reacted with oxygen containing gas in a first stage gasification stove to produce coal-gasified gas products containing CO, CO2, H2 and H2O; b. a coolant is fed to the coal-gasified gas products for cooling, and a first stage gas product is obtained; and c. the first stage gas product is fed to a second stage gasification stove and reacted with coal and a catalyst to form a second stage gas product containing methane.
Description
Invention field
The method of the gasification system of the present invention relates to methane more specifically, the present invention relates to adopt the method for two-stage gasification furnace coal gasification system methane.
Background technology
Along with the exhausted day by day and human kind sustainable development of the world petroleum resource demand to environmental protection, the clean coal that turns to representative with coal gas utilizes technology will play irreplaceable effect in following fossil energy.Especially the rich coal of China is oil-poor, and the coal storage capacity accounts for the third place in the world, and coal resources areal distribution inequality, reasonable development and utilize Coal Gasification Technology that guarantee Chinese Energy Safety and Economic development are had long-range strategic importance.Characteristics such as compare with existing Sweet natural gas, synthesizing methane is low with its cost, and (coal) raw material sources are abundant cause the increasing industrialization concern of people.
Present methanation technology can be divided into two kinds of two-step approach (indirect method) and single stage method (direct method) substantially.Two-step approach is meant with existing mature technology (as moral formula air flow bed or lurgi gasifier technology) and with oxygenants such as air or oxygens coal or coal water slurry etc. is gasificated into H earlier
2With product such as CO, product gas through cooling, acid gas removal body (as H
2S etc.), remove purification process such as entrained particles after, adjust H/C ratio, synthesizing methane under Ni-based or other catalyst actions at last by water gas shift reaction.The advantage of two-step approach is gasification and methanation two step process separate operation, and technology is relatively ripe, as the synthesizing methane technology (SNG) of Great Plains.Shortcoming is that cost is than higher, and owing to introduce purified synthesis gas and water-gas shift device, the technology overall thermal efficiency is lower because synthetic gas need add costliness and complicated treating plant.The two-step approach that formally puts into production at present only has the technology of Great Plains, other all immature relatively.
Single stage method is that coal is gasificated into methane with the water vapour direct reaction under catalyzer (being generally base metal catalysts) effect.Exxon company has carried out the research work of a large amount of catalytic coal gasifactions at twentieth century 70 to the eighties under the subsidy of USDOE, the general flow of its technology is overheated steam to be carried out catalytic gasification with the coal that is mixed with catalyzer react direct synthesizing methane in fluidized-bed.Except that coal, the material that refinery coke etc. contain high fixed carbon also can adopt similar technology, has proposed a kind of technical process of catalytic gasification petroleum slag as US2007/0083072.Compare with two-step approach, it is simple that single stage method has technology, the thermo-efficiency advantages of higher.Shortcoming is that preparation high temperature (800-900 ℃) overheated steam equipment and attemperator need additionally be provided, the required heat of anaerobic gasification to be provided and to remedy the thermosteresis that system radiating causes.
It is little thermo-negative reaction that coal and water reaction generate methane, shown in reaction formula (1):
C+H
2O→CH
4+CO
2 5.4KJ/mol (1)
Only need add little heat in theory to keep the power loss that system radiating causes.But gasification is attended by water vapour and coal gasification reaction (reaction formula (2)) and water gas shift reaction parallel reactors such as (reaction formula (3)) simultaneously, wherein water vapour and coal gasification reaction (reaction formula (2)) is a strong endothermic reaction, and level of response is bigger, so actually operating needs more heat to keep the constant temperature gasification reaction.
C+H
2O→H
2+CO 131KJ/mol (2)
CO+H
2O→CO
2+H
2 -41KJ/mol (3)
Traditional method of keeping suitable catalytic gasification temperature (～700 ℃) is to adopt the inlet air temperature of higher water vapour (800～900 ℃), catalytic coal gasifaction technology as Exxon, for example referring to H.A.Marshall and F.C.R.M.Smits, " Exxon catalytic coalgasification coal gasification process and large pilot plantdevelopment program; " Pittsburgh, PA, USA, 1982, the 357-377 page or leaf.The overheated steam for preparing 800～900 ℃ needs sectionalized superheater and superpower boiler usually, causes system's total energy consumption higher.In addition, the temperature-rise period of water vapour, there is the etching problem of material under the High Temperature High Pressure, therefore to producing and carrying the material of the equipment of overheated steam to have higher requirement from saturated steam to overheated steam.Use the method for the patent US4292048 proposition of single stage method, promptly CH with methane reforming
4And H
2CO and H that the O reaction generates
2And from isolated CO of vapourizing furnace and H
2Feed vapourizing furnace, react near pining for property to improve the methane yield and to make, thereby reduce the needed heat of thermo-negative reaction (being mainly reaction formula (2)).The shortcoming of this method is required CO and H
2Internal circulating load is bigger, has increased system energy consumption and equipment size.
Summary of the invention
The invention provides the method that a kind of gasification generates methane, may further comprise the steps:
Coal and oxygen-containing gas are reacted in the one-level vapourizing furnace, and generation comprises CO, CO
2, H
2, H
2The gasification gaseous product of O;
B. in described gasification gaseous product, feed refrigerant and lower the temperature, obtain the one-level gaseous product;
C. described one-level gaseous product is fed in the secondary vapourizing furnace and with coal and catalyst reaction, obtain comprising the secondary gas product of methane.
The accompanying drawing summary
Fig. 1 is the schema of an embodiment of method of the present invention.
Fig. 2 is the synoptic diagram of the one-level vapourizing furnace that uses in the method for the present invention.
Fig. 3 is the synoptic diagram of the secondary vapourizing furnace that uses in the method for the present invention, and wherein Fig. 3 A is the front view of this stove, and Fig. 3 B is the vertical view of this furnace interior.
These figure only are illustrative, the scope that does not limit the present invention in any way.
Detailed Description Of The Invention
Method of the present invention is carried out in the two-stage vapourizing furnace that is connected in series.Elaborate the present invention below in conjunction with Fig. 1.
In step a of the present invention, coal and oxygen-containing gas are reacted in the one-level vapourizing furnace, generation comprises CO, CO
2, H
2, H
2The gasification gaseous product of O.Wherein coal can feed in the one-level vapourizing furnace with the form of coal water slurry or dry coal dust, and apparatus for feeding is that the slurry feed equipment of this area routine such as high pressure water coal slurry transferpump (as surge pump) and coal-water slurry nozzle or feeding-in solid body equipment such as lock hopper charging and pressurization blow equipment.Simultaneously, from feed oxygen-containing gas to the one-level vapourizing furnace, described oxygen-containing gas can be air, oxygen-rich air or purity oxygen.Coal and oxygen are in 900-1600 ℃ temperature of one-level vapourizing furnace and the pressure of 20-70atm (referring to absolute pressure, down together) generating gasification reaction down, and generation comprises CO, CO
2, H
2, H
2The gasification gaseous product of O, if use air or oxygen-rich air, then this gasification gaseous product also comprises nitrogen and rare gas element.The gasification reaction of coal and oxygen is emitted a large amount of heats, and this heat part is used to keep the high temperature of one-level vapourizing furnace, and another part is then contained in the gasification gaseous product for future use.The gasification gaseous product moves upward along the one-level vapourizing furnace, and the lime-ash that the gasification back produces is then discharged from one-level vapourizing furnace bottom.
In step b of the present invention, in described gasification gaseous product, feed refrigerant and lower the temperature, obtain the one-level gaseous product.The purpose that feeds the refrigerant cooling is the temperature that the temperature regulation of gas extremely is fit to the performance katalysis a little more than the catalyzer of secondary vapourizing furnace.Wherein refrigerant is that liquid water or temperature are that 200～350 ℃ water vapour or the gas separating technology after two-stage vapourizing furnace technology of the present invention are separated and the CO and the H of recirculation
2, or their mixture.In the embodiment that the mixture that uses them is operated, refrigerant is based on water or water vapour, the CO of recirculation and H
2Play auxiliary cooling effect, circulation CO and H
2Main purpose be the CH that improves in the secondary vapourizing furnace
4Yield.As its name suggests, the temperature of these refrigerants should be lower than the temperature of gasification gaseous product.When refrigerant was liquid water or water at low temperature steam, because the existence of water gas shift reaction (see before and state equation 3), the gas phase composition of gasification gaseous product can change; When refrigerant is the CO and the H of recirculation
2The time, the gas phase of gasification gaseous product is formed also and can therefore be changed.To make the gaseous product after the gas phase composition changes be called the one-level gaseous product because of mixing coolant cools.Wherein refrigerant can feed to any position between the outlet of one-level vapourizing furnace at the middle part of one-level vapourizing furnace, for example feeds in the one-level vapourizing furnace by preferably being the nozzle that contraposition lays at the middle part of one-level vapourizing furnace between the outlet of one-level vapourizing furnace at least one pair of.Perhaps, refrigerant also can be passed in the connecting tube between one-level vapourizing furnace and the secondary vapourizing furnace.Or, can come performing step b by all feeding refrigerant in any position between exporting at middle part to one-level vapourizing furnace and the connecting tube between one-level vapourizing furnace and secondary vapourizing furnace at the one-level vapourizing furnace.The temperature of the one-level gaseous product that the cooling back forms is 800-900 ℃.
In step c of the present invention, described one-level gaseous product fed in the secondary vapourizing furnace and with coal and catalyst reaction, obtain comprising the secondary gas product of methane.Wherein, the temperature in the secondary vapourizing furnace is 650-750 ℃, and pressure is 20-40atm, and the required heat of keeping in the secondary vapourizing furnace of temperature can completely or partially be provided by the one-level gaseous product.Employed catalyzer is selected from alkaline carbonate or alkali metal hydroxide or their mixture among this step c.Coal and catalyzer can feed respectively in the secondary vapourizing furnace or feed in the secondary vapourizing furnace with the form of mixture, preferably the form with mixture feeds in the secondary vapourizing furnace, wherein coal and aqueous catalyst solution are mixed, obtain coal and mixture of catalysts after the drying by this area conventional means.The apparatus for feeding that is adopted also is the conventional apparatus for feeding of this area, for example lock hopper feeding unit etc.Requirement according to the required water coal ratio of fluidization and catalytic gasification reaction in the secondary vapourizing furnace can preferably additionally feed overheated steam in the secondary vapourizing furnace, be used for the auxiliary transformation efficiency of keeping fluidized state and improving gasification.The temperature of described overheated steam is 800～900 ℃, pressure is 20～40atm, it can directly feed in the secondary vapourizing furnace or feed in the connecting tube between one-level vapourizing furnace and the secondary vapourizing furnace, preferred directly the feeding in the secondary vapourizing furnace for example enters the secondary vapourizing furnace by the conical distribution plate that is arranged in secondary vapourizing furnace bottom.Reaction shown in following equation takes place with the one-level gaseous product in coal dust under the effect of catalyzer, generation comprises the secondary gas product of methane, this secondary gas product leaves the secondary vapourizing furnace, enter follow-up gas delivery operation, the lime-ash that produces in the secondary vapourizing furnace is then discharged from secondary vapourizing furnace bottom.
C+H
2O→H
2+CO (4)
CO+H
2O→CO
2+H
2 (3)
3H
2+CO→CH
4+H
2O (5)
The secondary gas product adopts the conventional separation means in this area to isolate CO, H in follow-up gas delivery operation
2, CO
2Deng, finally obtaining highly purified methane gas, these separation means are that the technician is known, do not repeat them here.CO that in separation circuit, separates and H
2Can be Deng gas separately as refrigerant, perhaps, as the fill-in of other refrigerant such as liquid water or water at low temperature steam, with implementation step b.
From the lime-ash that the secondary vapourizing furnace is discharged, contain materials such as semicoke, lime-ash and catalyzer.Can pass through therefrom Separation and Recovery catalyzer of the conventional separation means in this area, and the catalyst recirculation that reclaims is used, these all are that the technician is known, repeat no more.
The one-level vapourizing furnace that adopts in the method for the present invention can be air flow bed, fluidized-bed or carry bed.The example of air flow bed can be the several types such as egas air flow bed of Shell, GE or ConocoPhilips company; The example of fluidized-bed can be the ugas fluidized-bed, also can be that KRW is gray melting poly-fluid bed; Carrying the example of bed is the conveying vapourizing furnace of KBR, or the like.When these vapourizing furnaces of direct use do not carry out any transformation to it, then need in the connecting tube between one-level vapourizing furnace and the secondary vapourizing furnace, feed refrigerant.As the preferred embodiments of the invention, can transform above-mentioned various vapourizing furnaces, described transformation was meant before the outlet of these vapourizing furnaces sets up coolant jet, preferably set up at least one pair of and be the nozzle that contraposition is laid, by these nozzles refrigerant is fed in the one-level vapourizing furnace, be used for the gasification gaseous product is carried out chilling.Wherein without the concrete structure of the egas air flow bed of the Shell, the GE that transform or ConocoPhilips respectively referring to below with reference to document:
Schuurman, the United States Patent (USP) 4202672 that is entitled as " Apparatus for gasification of finelydivided fuel " of P.J;
Schlinger, W.G. " Coal gasification development andcommercialization of the Texaco coal gasification process ", International Journal of Energy Research, 2007, vol 4 (2), 127-136; With
Rotter, the United States Patent (USP) 4306506 that is entitled as " Gasification apparatus " of Franz;
Carry the example of bed to see below with reference to document:
Brandon?M.Davis，Roxann?Leonard，P.Vimalchand，Guohai?Liu，Peter?V.Smith，Ron?Breault，“Operation?of?the?PSDF?transportgasifier”，Twenty-second?Annual?Pittsburgh?Coal?Conference，Pittsburgh，PA，September?12-15，2005。
Gray melting poly-fluid bed about ugas fluidized-bed and KRW, referring to below with reference to document:
Jequier, J., Longchambon, L., and Van De Putte, G., " Thegasification of coal fines ", J.Inst.Fuel, 1960,33 584-591 and
Hartman，H.F.，Belk，J.P.，Reagan，E.E.，Low?Btu?coalgasification?processes，vol?2，Selected?Process?Descriptions，1978，11，A-139-151；
Incorporate the content of these patents or paper into this paper by reference.
Fig. 2 has provided the example of improved egas air flow bed as the one-level vapourizing furnace, has only provided the charging situation of each material among Fig. 2, and has omitted concrete vapourizing furnace internal structure.Enter the bottom of one-level vapourizing furnace after coal water slurry and the oxygen mix, in the generating gasification reaction of high temperature (1400-1500 ℃) district of one-level vapourizing furnace bottom.Different with the coal water slurry swirling flow feeding manner at original egas two fragment position places, any position before the outlet of one-level vapourizing furnace, be provided with at least one pair of and be the nozzle that contraposition is laid, by this nozzle refrigerant is fed in the one-level vapourizing furnace, the mode that this contraposition is laid has been strengthened mixing of gasification gaseous product and refrigerant, thereby has realized rapid cooling.
The secondary vapourizing furnace that adopts in the method for the present invention can be jet bed or circulating fluidized bed, but preferred jet bed.Because gasification gaseous product and one-level gaseous product are all without dust removal process, so enter and usually carry coal ash or unreacted coal tar particle completely in the one-level gaseous product of secondary vapourizing furnace secretly, be the gas distribution grid of the particle plugging secondary vapourizing furnace that prevents to carry secretly, the secondary vapourizing furnace preferably adopts the operating method of jet bed.The jet bed is named jet fluidized-bedly again, is to spray into the bed type that fluidized-bed constituted of a finite space by (vertical, level or inclination) jet at a high speed.In the practical application, commonly flat spout or the insertion nozzle of high speed vertical fluid fluid by bottom conical distribution plate or flat grid distributor center enters bed and forms jet and the coexistent two kinds of flow states of fluidisation.About the structure and the operating method of jet bed, can be referring to following two reference:
Jequier, J., Longchambon, L., and Van De Putte, G., " Thegasification of coal fines ", J.Inst.Fuel, 1960,33 584-591 and
Hartman，H.F.，Belk，J.P.，Reagan，E.E.，Low?Btu?coalgasification?processes，vol?2，Selected?Process?Descriptions，1978，11，A-139-151；
Incorporate the full text of these reference into this paper by reference.Fig. 3 has provided a kind of diagram of jet bed: the one-level gaseous product injects bed from jet bed pipe core, not only avoided entrained particles to stop up gas distribution grid, and can be by adjusting the caliber and the charge flow rate of pipe core, realize separating of the different ash of density and Jiao.Fluidisation then feeds from the bottom with water vapour, and coal and catalyzer feed from certain position, secondary vapourizing furnace middle part.
It will be appreciated by those skilled in the art that the present invention is applicable to coal incessantly, but can expand to multiple carbonaceous material, for example refinery coke etc.Wherein refinery coke be meant crude oil through distillation with lightweight oil with after mink cell focus separates, the product that mink cell focus changes into through the process of hot tearing again, its main component is a carbon, occupies more than the 80wt%, remaining is hydrogen, oxygen, nitrogen, sulphur and metallic element.
Advantage of the present invention is as follows:
(1) high-temperature gas that the one-level gasification furnace produces in this technology can be directly used in the secondary gasification furnace after by adjustment, for the secondary gasification furnace provides reaction required reaction heat, alleviated the load of secondary catalytic gasification overheated steam boiler, overall thermal efficiency is higher than conventional two-step methane technology method processed.
(2) gas need not to add independent cleaning equipment to remove CO before entering the secondary gasification furnace2、H
2S or entrained particles have reduced equipment investment.
(3) the one-level gasification furnace produces is rich in CO and H2The synthesis gas of (60-80 volume %) can improve the methane yield of secondary gasification furnace catalytic gasification effectively, has relatively alleviated CO and H with a ground beetle alkylation process2Internal circulating load, thus energy consumption reduced.
Claims (21)
1. a gasification generates the method for methane, may further comprise the steps:
Coal and oxygen-containing gas are reacted in the one-level vapourizing furnace, and generation comprises CO, CO
2, H
2, H
2The gasification gaseous product of O;
B. in described gasification gaseous product, feed refrigerant and lower the temperature, obtain the one-level gaseous product;
C. described one-level gaseous product is fed in the secondary vapourizing furnace and with coal and catalyst reaction, obtain comprising the secondary gas product of methane.
2. the process of claim 1 wherein that described oxygen-containing gas is air, oxygen-rich air or purity oxygen.
3. the process of claim 1 wherein that the temperature in the one-level vapourizing furnace is 900-1600 ℃, pressure is 20-70atm.
4. the process of claim 1 wherein that the coal among the step a feeds in the one-level vapourizing furnace with the form of coal water slurry or dry coal dust.
5. the process of claim 1 wherein that feeding described refrigerant by the middle part at the one-level vapourizing furnace to any position between the outlet of one-level vapourizing furnace comes performing step b.
6. the method for claim 5 wherein feeds refrigerant in the one-level vapourizing furnace by the nozzle of laying at least one pair of contraposition between the outlet of one-level vapourizing furnace at the middle part of one-level vapourizing furnace.
7. the process of claim 1 wherein and come performing step b by feeding described refrigerant in the connecting tube between one-level vapourizing furnace and secondary vapourizing furnace.
8. the process of claim 1 wherein and come performing step b by all feeding refrigerant in any position between exporting at middle part to one-level vapourizing furnace and the connecting tube between one-level vapourizing furnace and secondary vapourizing furnace at the one-level vapourizing furnace.
9. the process of claim 1 wherein that described refrigerant is that liquid water or temperature are 200～350 ℃ the water vapour or the CO and the H of recirculation
2Or their mixture.
10. the process of claim 1 wherein that the temperature of described one-level gaseous product is 800-900 ℃.
11. the process of claim 1 wherein that the temperature in the secondary vapourizing furnace is 650～750 ℃, pressure is 20-40atm.
12. the process of claim 1 wherein that the catalyzer among the step c is selected from alkaline carbonate or alkali metal hydroxide or their mixture.
13. the process of claim 1 wherein that coal among the step c and catalyzer feed respectively in the secondary vapourizing furnace or feed in the secondary vapourizing furnace with the form of mixture.
14. the process of claim 1 wherein and also in the secondary vapourizing furnace, feed overheated steam extraly among the step c.
15. the method for claim 14, the temperature of wherein said overheated steam are 800～900 ℃, pressure is 20～40atm.
16. the method for claim 13, wherein said overheated steam directly feed in the secondary vapourizing furnace or feed in the connecting tube between one-level vapourizing furnace and the secondary vapourizing furnace.
17. the method for claim 5, wherein said one-level vapourizing furnace are air flow bed, fluidized-bed or carry bed, wherein set up coolant jet before the outlet of this one-level vapourizing furnace.
18. the method for claim 7, wherein said one-level vapourizing furnace are air flow bed, fluidized-bed or carry bed, randomly set up coolant jet before the outlet of this one-level vapourizing furnace.
19. the process of claim 1 wherein that described secondary vapourizing furnace is the jet bed.
20. the method for claim 1 also comprises described secondary gas product is carried out gas delivery to obtain the step of methane.
21. the method for each of aforementioned claim wherein replaces coal with refinery coke.
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| CN200910224298.3A CN102079685B (en) | 2009-11-26 | 2009-11-26 | Coal gasification process for methane preparation by two stage gasification stove |
| PCT/CN2010/001890 WO2011063608A1 (en) | 2009-11-26 | 2010-11-25 | Process for producing methane by gasification of coal with two-stage gasifier |
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| CN200910224298.3A CN102079685B (en) | 2009-11-26 | 2009-11-26 | Coal gasification process for methane preparation by two stage gasification stove |
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| WO2011063608A1 (en) | 2011-06-03 |
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