CN109401792A - The combined fluidized bed reaction unit of catalytic gasification and reaction method - Google Patents
The combined fluidized bed reaction unit of catalytic gasification and reaction method Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- 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
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
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- C—CHEMISTRY; METALLURGY
- 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
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
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- C—CHEMISTRY; METALLURGY
- 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
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
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- C—CHEMISTRY; METALLURGY
- 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
- 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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- C—CHEMISTRY; METALLURGY
- 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
- 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
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- C—CHEMISTRY; METALLURGY
- 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
- 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
- C10J2300/0956—Air or oxygen enriched air
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- C—CHEMISTRY; METALLURGY
- 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
- 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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- C—CHEMISTRY; METALLURGY
- 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
- 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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- C—CHEMISTRY; METALLURGY
- 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
- 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
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- C—CHEMISTRY; METALLURGY
- 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
- 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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- C—CHEMISTRY; METALLURGY
- 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
- 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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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Abstract
The present invention relates to a kind of combined fluidized bed reaction unit of catalytic gasification and reaction method, mainly solve the problems, such as that efficiency of carbon con version existing in the prior art and the intensity of gasification are low, methane production is relatively low and gasifier operation stability is poor.The present invention passes through a kind of combined fluidized bed reaction unit of catalytic gasification and reaction method, catalyst is supported in carbon raw material, part burning and gasification reaction are carried out in thin reactor with higher linear speed and lower granule density simultaneously with gasifying agent and oxidant, the carbon-bearing particulate matter of the synthesis gas and unfinished reaction that then generate carries out the technical solution of further gasification reaction in the higher crude reaction device of granule density, above-mentioned technical problem is preferably resolved, can be applied in the industrial production of catalytic gasification richness methane phase.
Description
Technical field
The present invention relates to a kind of combined fluidized bed reaction unit of catalytic gasification and reaction methods.
Background technique
China is a coal big country, possesses coal resources abundant, with the rapid development of our country's economy, the life of coal
Yield and consumption figure climb up and up, and the coal production in China in 2014 reaches 38.7 hundred million tons, close to the half of world wide production.
China has become the maximum coal production state in the whole world and consumption of coal state.The directly burning of coal discharges a large amount of dirt in utilizing
Object is contaminated, causes many regional hazes in China to take place frequently, drastically influences environmental problem.Coal Gasification Technology be realize coal it is clean, efficiently,
The key technology of comprehensive utilization is important channel and the synthesis of chemicals, combined cycle generation and coal generation of coal conversion
With one of the key technology of natural gas.Currently, various kinds of coal gas technology successfully realizes industrial applications, it is all made of non-catalytic gas
Change technology improves efficiency of carbon con version by cost of high temperature and pressure, this just brings, and coal gas intensity of cooling is big, gas purification is difficult, energy
The problems such as consumption is high, harsh to equipment requirement.However, the catalytic gasification process of coal not only increases gasification reaction rate, while
Gasification reaction temperature is significantly reduced, the mild gasification of coal is achieved.Many synthesis processes can also be carried out simultaneously,
Under the effect of the catalyst, can while coal gasification the industrial chemicals such as synthesizing methane, methanol, ammonia, shorten process flow.Its
In the synthesis gas rich in methane directly produced by the method for catalytic coal gasifaction, be an important research side of catalytic coal gasifaction
To.
Patent US4318712 discloses a kind of technique of coal one-step method methane, will be passed through after catalyst and coal dust premix
In reactor, gasifying agent uses superheated steam, while also as the reaction temperature in heat source maintenance reactor.The temperature of superheated steam
Degree is 850 DEG C, and gasification reaction temperature is controlled at 700 DEG C or so.Coal carries out gasified reverse with superheated steam under the effect of the catalyst
It answers, while being passed through CO and H2Based on circulation synthesis gas, strengthen furnace in methanation reaction, directly obtain methane rich synthesis gas.
Patent CN201010279560.7 discloses a kind of multicompartment fluidized bed catalytic gasification methane technology, by gasification furnace point
Section, coal methanation section and synthesis gas methanation section are generated for synthesis gas.Make burning, gasification, methanation reaction and pyrolytic reaction point
Duan Jinhang, the extent of reaction and Temperature Distribution of each section of control, to improve methane production.However the pyrolysis section above gasification furnace
In, tiny fine coal is unreacted just to be run out of from gasification furnace, so that the carbon content of flying dust is higher, and the complete coal tar of unreacted
Back-mixing is directly discharged from gasification furnace to gasification furnace bottom cinder notch, causes the efficiency of carbon con version in reaction process lower.Coal in gasification furnace
When burnt particle residence time is 2~3h, efficiency of carbon con version is maintained essentially in the range of 60~90%.
In conclusion catalytic coal gasifaction technology is due to that need to consider methanation reaction, reaction temperature is lower, leads to reaction speed
Rate and efficiency of carbon con version reduce, the direct emission of the race leakage of carbon containing flying dust and the gasification thick slag of furnace bottom in synthesis gas, largely
On also affect the promotion of efficiency of carbon con version, for the utilization rate of energy, and when efficiency of carbon con version is lower, the calorific value of carbon residue is not complete
Complete utilization.Thus it is necessary to develop one kind can be improved efficiency of carbon con version and improve the intensity of gasification, methane production and gasification furnace fortune
The catalytic coal gasifaction method of row stability and high reliablity.
Summary of the invention
Present invention mainly solves the technical issues of first is that the efficiency of carbon con version existing in the prior art and intensity of gasification is low, first
Alkane yield is relatively low and gasifier operation stability and the problem of poor reliability, and it is combined fluidized bed to provide a kind of new catalytic gasification
Reaction unit and reaction method.In this method fluidized-bed reactor have efficiency of carbon con version is high, the intensity of gasification is high, methane production height with
And the feature that gasifier operation is stable, guarantee the efficient of reaction and stablizes.
The second technical problem to be solved by the present invention is to provide the corresponding reaction of one of one kind and solution technical problem
Method.
One of to solve above-mentioned technical problem, The technical solution adopted by the invention is as follows: a kind of catalytic gasification combination fluidisation
Bed reaction device, capital equipment includes: thin reactor 3, crude reaction device 4 and settler 6, wherein 3 upper end of thin reactor is expanding
It is connected afterwards with 4 bottom of crude reaction device, crude reaction device 4 is connected by separation equipment 7 with settler 6, and the bottom of settler 6 is logical
It crosses Loop Seal 8 to be connected with thin reactor 3, separation equipment 7 is located in 6 cylinder of settler.
In above-mentioned technical proposal, the height of the thin reactor 3 is 2-8 times of 4 height of crude reaction device, the crude reaction device
4 diameter is 1.5-6 times of thin 3 diameter of reactor, separation equipment 7 built in the settler 6, the separation equipment 7 by 2 groups and
2 groups or more of cyclone separator is composed.
Preferred technical solution, the height of the thin reactor 3 are 3-6 times of 4 height of crude reaction device, the crude reaction
The diameter of device 4 is 3-4.5 times of thin 3 diameter of reactor.
In order to solve the above problem two, The technical solution adopted by the invention is as follows: a kind of methanol with catalyst mixer
The method of alkene processed is comprised the following steps using above-mentioned reaction unit:
A, the carbon raw material E of supported catalyst is entered in settler 6 by feeding line 10, and is imported by Loop Seal 8,
With the gasifying agent A in gas line 2 simultaneously into being mixed in thin reactor 3 and gasification reaction, big after reaction
Grain slag is fallen in slag bath 1 by natural subsidence, and is isolated lime-ash G by catalyst reclaimer 11 and be catalyzed with slag bath recycling
Agent F；
B, the carbonaceous particles after reacting in thin reactor 3 enter in crude reaction device 4 by gas lift, net from gas
Change with further gasification reaction under the action of the circulation synthesis gas B of separation system 9, hydrogen and an oxygen in the circulation synthesis gas B
The volume ratio for changing carbon is 0.8-4.5, and gas after reaction and solid enter in separation equipment 7, and the solid contains fine ash, carbon containing
Particulate matter and slag, by separation after, gas be not discharged by isolated carbonaceous particles by whirlwind by isolated fine ash and after
Into Quick-gasifying reaction is carried out in flashing reactor 5, product gas then is extracted using gas purification and separation system 9, is gone out
The mouth fine ash C and catalyst D of fine ash recycling；
C, still further aspect, by separation equipment 7 separate after carbonaceous particles and slag settled in settler 6, and with come from
The catalyst D of fine ash recycling of feeding line 10, the carbon raw material E of supported catalyst, slag bath recycling catalyst F mixing, pass through
Loop Seal 8, which returns in thin reactor 3, continues gasification reaction.
In above-mentioned technical proposal, the carbon raw material includes coal, petroleum coke, biomass and its mixture, the gasifying agent
Including oxygen, air, liquid water, vapor, carbon dioxide or hydrogen and its mixture.The reaction condition of the thin reactor 3
Are as follows: reaction pressure 0-6.5MPa, 800-1600 DEG C of reaction temperature, gas phase linear velocity 2.0-15.0m/s, the stream in thin reactor 3
State is fast fluidization；The reaction condition of crude reaction device 4 are as follows: reaction pressure 0-6.5MPa, 600-1100 DEG C of reaction temperature, gas phase
Linear velocity 0.1-1.0m/s, the fluidised form in crude reaction device 4 are turbulence fluidization or bubbling fluidization.The catalyst is selected from alkali gold
At least one of category, alkaline-earth metal, transition metal；The catalyst is born in a manner of infusion process, dry pigmentation or ion-exchange
It is loaded on carbon raw material；The load capacity of the catalyst accounts for the 0.1~20% of raw coal quality.Water carbon in the thin reactor 3
The range of ratio is 0.5-4mol/mol, and the range of the steam/hydrocarbons ratio in the crude reaction device 4 is 2-20mol/mol.It is described quickly anti-
Answering device 5 is downflow fluidized bed, Cyclonic reactor, tubular reactor or fluidized-bed reactor.
In above-mentioned technical proposal, the circulation synthesis gas B is through CO2Absorption plant removes CO2It is passed through after gas thick anti-
Answer the synthesis gas in device 4.
In above-mentioned technical proposal, the settler 6 serves not only as the container of the sedimentation separation of product gas and particle, also makees
Play the role of premixing for feed end, the carbon raw material of supported catalyst is added after settler in settler and the heat of return
It carries particle and carries out contact heat transfer, ensure that carbon raw material has had certain uniform temperature before entering gasification reactor 3
Degree, facilitates the raising of reaction rate.Settler 6 has the function of pressure accumulation in the entire circulatory system simultaneously, passes through convenient for particle
It crosses Loop Seal 8 and can smoothly enter into and reacted in thin reactor 3.
What is entered in thin reactor 3 in the present invention is the carbon raw material and gasifying agent of supported catalyst, in the reactor with
Based on combustion reaction, gasification reaction and Partial Transformation reaction, methanation reaction.Since linear speed is higher in first reactor, gas
Gu steam/hydrocarbons ratio is also higher than relatively high, temperature is controlled within the scope of 900-1600 DEG C, is conducive to burning and gasification reaction.It is carbon containing
Raw material and the carbonaceous particles of return under the effect of the catalyst, due in reactor Gas-solid Two-phase Flow state be fast fluidization
State, the content of gas is very high, and gas-solid contact efficiency is also very high, thus leads to combustion rate and gasification reaction rate
Faster, the utilization rate of efficiency of carbon con version and carbon residue is improved.The heat that combustion reaction generates is used to provide heat in gasification reaction area
Consumption and heat waste, and provide necessary heat and gasifying agent for gasification reaction.
Gasification reaction, conversion reaction and methanation reaction are substantially carried out in the present invention in crude reaction device 4.By thin reactor 3
CO, H in the gas component of middle inflow2、CO2、H2O and CH4It exists simultaneously, while being passed through circulation synthesis gas in 4 bottom of crude reaction device
B improves CO and H in crude reaction device 42Content, dilute CO2Content, the balance for promoting conversion reaction moves right,
Improve H2The ratio of/CO, and gas phase linear speed is lower in crude reaction device 4, gas-solid fluidised form is that bubbling or turbulent flow, gas-solid are compared
Want much lower in thin reactor 3, and temperature control promotes the movement of methanation reaction balance within the scope of 600-1100 DEG C,
Improve outlet CH4Yield.
The carbon containing object that flashing reactor 5 is directed to the part relatively fine particle separated by separation equipment 7 in the present invention carries out
Further gasification reaction, the not reacted carbon residue in this part by under the catalytic action for the catalyst being entrained in fine particle object with
Gas component with gasifying agent function carries out rapidly gasification reaction in flashing reactor 9, due to the gas in the reactor
Concentration of component is high, and the partial size of fine powder char particle object is smaller, and granule density is low, therefore can realize the gasified reverse of carbon residue quickly
It answers, to further increase the utilization rate of efficiency of carbon con version and carbon residue.
Main reactor and circulating system device in the present invention are mature circulating fluidized bed system, internal temperature control
It is easier to, gas-solid contact is high-efficient, and mass-and heat-transfer is strong.Loop Seal is on-mechanical returning charge equipment, it is not easy to leakage blocking.It is whole
Structure is simple, and equipment is mature, it is not easy to abrasion and leakage occurs, overall system architecture is much lower compared with the prior art.
Using technical solution of the present invention, increases, export than gasification outlet efficiency of carbon con version in prior art reactor
Methane content improves 31% in synthesis gas, and efficiency of carbon con version improves 97%, has efficiency of carbon con version height, intensity of gasification height, methane production
High and stable gasifier operation feature, guarantees the efficient of reaction and stablizes, and achieves preferable technical effect.
Detailed description of the invention
Fig. 1 is the flow diagram of the method for the invention:
In Fig. 1,1 is slag bath；2 be gas feed pipeline；3 be thin reactor；4 be crude reaction device；5 be flashing reactor；6
For settler；7 be separation equipment；8 be Loop Seal；9 be gas purification and separation system；10 for catalyst and carbon raw material into
Expects pipe line；11 be catalyst reclaimer；12 be circulation synthesis gas distributor.A is gasifying agent, including oxygen, air, liquid
Water, vapor, carbon dioxide or hydrogen and its mixture；B is circulation synthesis gas；C is outlet fine ash；D is fine ash recycling catalysis
Agent；E is the carbon raw material of supported catalyst；F is that slag bath recycles catalyst；G is lime-ash.
Catalyst and carbon raw material are entered in settler 6 by feeding line 10, are imported by Loop Seal 8 and are entered thin reactor
In 3, gasification reaction is carried out in thin reactor 3 after mixing with the vapor in gas line 2 with oxygen air, after reaction
Bulky grain slag fall in slag bath 1 by natural subsidence, and slag tap by the separation of catalyst reclaimer 11 and slag bath recycles
Catalyst.Carbonaceous particles after reacting in thin reactor 3 enter further gasification reaction in crude reaction device 4 by gas lift.
Gas and solid fine ash, carbon-bearing particulate matter and slag after reaction etc. enter in separation equipment 7, after separation, gas and part
Fine ash and carbonaceous particles enter after being discharged by whirlwind carries out Quick-gasifying reaction in flashing reactor 5, then using gas
Purification extracts product gas, fine ash and partially recycled catalyst with separation system 9；Still further aspect is separated by separation equipment 7
The carbonaceous particles and slag got off settle in settler 6, and urge with from catalyst and the fresh of carbon raw material feeding line
Agent, carbon raw material, fine ash recycling catalyst, slag bath recycling catalyst mixing, return in thin reactor 3 by Loop Seal 8
Continue gasification reaction.
The carbon raw material E of supported catalyst is entered in settler 6 by feeding line 10, and is imported by Loop Seal 8, with
Gasifying agent A in gas line 2 enters in thin reactor 3 simultaneously carries out mixing and gasification reaction, the bulky grain after reaction
Slag is fallen in slag bath 1 by natural subsidence, and isolates lime-ash G and slag bath recycling catalyst by catalyst reclaimer 11
F；Carbonaceous particles after reacting in thin reactor 3 enter in crude reaction device 4 by gas lift, from gas purification with separate
Further gasification reaction under the action of the circulation synthesis gas B of system 9, the body for recycling hydrogen and carbon monoxide in synthesis gas B
Than being 0.8-4.5, gas after reaction and solid enter in separation equipment 7 product, the solid contain fine ash, carbon-bearing particulate matter with
Slag, by separation after, gas be not discharged by isolated carbonaceous particles by whirlwind by isolated fine ash and after enter quickly
Quick-gasifying reaction is carried out in reactor 5, then using gas purification and separation system 9 extract product gas,OutletFine ash C with
And the catalyst D of fine ash recycling；Still further aspect, carbonaceous particles and slag after being separated by separation equipment 7 are sunk in settler 6
Drop, and catalyst is recycled with the catalyst D of fine ash recycling, the carbon raw material E of supported catalyst, slag bath from feeding line 10
F mixing, returns in thin reactor 3 by Loop Seal 8 and continues gasification reaction.
The present invention will be further described below by way of examples, but is not limited only to the present embodiment.
Specific embodiment
[embodiment 1]
Reaction process is as follows: catalyst and carbon raw material are entered in settler by feeding line, by Loop Seal import into
Enter in thin reactor, in gas line vapor and oxygen mix after gasification reaction is carried out in thin reactor, instead
Bulky grain slag after answering is fallen in slag bath by natural subsidence, and is slagged tap by the separation of catalyst reclaimer and recycled with slag bath
Catalyst.Carbonaceous particles after reacting in thin reactor enter further gasification reaction in crude reaction device by gas lift.Instead
Gas and solid fine ash, carbon-bearing particulate matter and slag after answering etc. enter in separation equipment, after separation, gas and part fine ash
And carbonaceous particles be discharged by whirlwind after enter flashing reactor in carry out Quick-gasifying reaction, then using gas purification with
Separation system extracts product gas, fine ash and partially recycled catalyst；Still further aspect is contained by what separation equipment separated
Carbon particle and slag settle in settler, and with the fresh catalyst, carbon containing from catalyst and carbon raw material feeding line
Raw material, fine ash recycling catalyst, slag bath recycling catalyst mixing, return in thin reactor by Loop Seal and continue gasified reverse
It answers.
Inner Mongol lignite is selected in experiment, is crushed 1mm or less processed and obtains fine coal and mix with 5% potassium carbonate catalyst.
Thin reactor diameter is 50mm, is highly 3000mm, linear speed 2m/s, steam/hydrocarbons ratio 1mol/mol, and reaction temperature is 800 DEG C,
Reaction pressure 2MPa；Crude reaction device diameter is 75mm, is highly 1500mm, and reaction temperature is 650 DEG C, reaction pressure 2MPa.It urges
The load capacity of agent accounts for the 5% of raw coal quality.Circulation synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, circulation
The ratio of hydrogen and carbon monoxide is 1 in synthesis gas.Since separative efficiency is higher, the particle for leaving separation equipment is considerably less, because
This flashing reactor selects tubular reactor, and operation temperature is 850 DEG C.Product gas is the synthesis gas rich in methane, outlet synthesis
CH in gas4Concentration 24.1%, outlet efficiency of carbon con version reach 96.6%.
[embodiment 2]
Reaction process is same as Example 1.Experiment select Inner Mongol lignite, be crushed 1mm or less processed obtain fine coal and with
5% potassium carbonate catalyst mixing.Thin reactor diameter is 50mm, is highly 3000mm, linear speed 2m/s, and steam/hydrocarbons ratio is
1mol/mol, reaction temperature are 800 DEG C, reaction pressure 2MPa；Crude reaction device diameter is 300mm, is highly 1500mm, reaction temperature
Degree is 650 DEG C, reaction pressure 2MPa.The load capacity of catalyst accounts for the 5% of raw coal quality.Circulation synthesis gas tolerance accounts for gasification installation
The 20% of exiting syngas total amount, recycling the ratio of hydrogen and carbon monoxide in synthesis gas is 1.Since separative efficiency is higher, from
The particle for opening separation equipment is considerably less, therefore flashing reactor selects tubular reactor, and operation temperature is 850 DEG C.Product gas is
Synthesis gas rich in methane, CH in exiting syngas4Concentration 24.8%, outlet efficiency of carbon con version reach 97.2%.
[embodiment 3]
Reaction process is same as Example 1.Experiment select Inner Mongol lignite, be crushed 1mm or less processed obtain fine coal and with
5% potassium carbonate catalyst mixing.Thin reactor diameter is 50mm, is highly 3000mm, linear speed 2m/s, and steam/hydrocarbons ratio is
1mol/mol, reaction temperature are 800 DEG C, reaction pressure 2MPa；Crude reaction device diameter is 150mm, is highly 1500mm, reaction temperature
Degree is 650 DEG C, reaction pressure 2MPa.The load capacity of catalyst accounts for the 5% of raw coal quality.Circulation synthesis gas tolerance accounts for gasification installation
The 20% of exiting syngas total amount, recycling the ratio of hydrogen and carbon monoxide in synthesis gas is 1.Since separative efficiency is higher, from
The particle for opening separation equipment is considerably less, therefore flashing reactor selects tubular reactor, and operation temperature is 850 DEG C.Product gas is
Synthesis gas rich in methane, CH in exiting syngas4Concentration 25%, outlet efficiency of carbon con version reach 97%.
[embodiment 4]
Reaction process is same as Example 1.Experiment select Inner Mongol lignite, be crushed 1mm or less processed obtain fine coal and with
5% potassium carbonate catalyst mixing.Thin reactor diameter is 50mm, is highly 3000mm, linear speed 2m/s, and steam/hydrocarbons ratio is
1mol/mol, reaction temperature are 800 DEG C, reaction pressure 2MPa；Crude reaction device diameter is 225mm, is highly 1500mm, reaction temperature
Degree is 650 DEG C, reaction pressure 2MPa.The load capacity of catalyst accounts for the 5% of raw coal quality.Circulation synthesis gas tolerance accounts for gasification installation
The 20% of exiting syngas total amount, recycling the ratio of hydrogen and carbon monoxide in synthesis gas is 1.Since separative efficiency is higher, from
The particle for opening separation equipment is considerably less, therefore flashing reactor selects tubular reactor, and operation temperature is 850 DEG C.Product gas is
Synthesis gas rich in methane, CH in exiting syngas4Concentration 25.4%, outlet efficiency of carbon con version reach 97.2%.
[embodiment 5] reaction process is same as Example 1.Inner Mongol lignite is selected in experiment, is crushed 1mm or less processed and obtained
Fine coal is simultaneously mixed with 5% potassium carbonate catalyst.Thin reactor diameter is 50mm, is highly 3000mm, linear speed 2m/s, water carbon
Than for 1mol/mol, reaction temperature is 800 DEG C, reaction pressure 2MPa；Crude reaction device diameter is 75mm, is highly 375mm, reaction
Temperature is 650 DEG C, reaction pressure 2MPa.The load capacity of catalyst accounts for the 5% of raw coal quality.Circulation synthesis gas tolerance accounts for gasification dress
The 20% of exiting syngas total amount is set, recycling the ratio of hydrogen and carbon monoxide in synthesis gas is 1.Since separative efficiency is higher,
The particle for leaving separation equipment is considerably less, therefore flashing reactor selects tubular reactor, and operation temperature is 850 DEG C.Product gas
For the synthesis gas rich in methane, CH in exiting syngas4Concentration 23.9%, outlet efficiency of carbon con version reach 95.5%.
[embodiment 6]
Reaction process is same as Example 1.Experiment select Inner Mongol lignite, be crushed 1mm or less processed obtain fine coal and with
5% potassium carbonate catalyst mixing.Thin reactor diameter is 50mm, is highly 3000mm, linear speed 2m/s, and steam/hydrocarbons ratio is
1mol/mol, reaction temperature are 800 DEG C, reaction pressure 2MPa；Crude reaction device diameter is 75mm, is highly 500mm, reaction temperature
It is 650 DEG C, reaction pressure 2MPa.The load capacity of catalyst accounts for the 5% of raw coal quality.Circulation synthesis gas tolerance accounts for gasification installation and goes out
The 20% of mouth synthesis gas total amount, recycling the ratio of hydrogen and carbon monoxide in synthesis gas is 1.Since separative efficiency is higher, leave
The particle of separation equipment is considerably less, therefore flashing reactor selects tubular reactor, and operation temperature is 850 DEG C.Product gas is richness
Synthesis gas containing methane, CH in exiting syngas4Concentration 24.6%, outlet efficiency of carbon con version reach 96.9%.
[embodiment 7]
Reaction process is same as Example 1.Experiment select Inner Mongol lignite, be crushed 1mm or less processed obtain fine coal and with
5% potassium carbonate catalyst mixing.Thin reactor diameter is 50mm, is highly 3000mm, linear speed 2m/s, and steam/hydrocarbons ratio is
1mol/mol, reaction temperature are 800 DEG C, reaction pressure 2MPa；Crude reaction device diameter is 75mm, is highly 1000mm, reaction temperature
Degree is 650 DEG C, reaction pressure 2MPa.The load capacity of catalyst accounts for the 5% of raw coal quality.Circulation synthesis gas tolerance accounts for gasification installation
The 20% of exiting syngas total amount, recycling the ratio of hydrogen and carbon monoxide in synthesis gas is 1.Since separative efficiency is higher, from
The particle for opening separation equipment is considerably less, therefore flashing reactor selects tubular reactor, and operation temperature is 850 DEG C.Product gas is
Synthesis gas rich in methane, CH in exiting syngas4Concentration 24.2%, outlet efficiency of carbon con version reach 96.5%.
[embodiment 8]
Reaction process is same as Example 1.Experiment select Inner Mongol lignite, be crushed 1mm or less processed obtain fine coal and with
5% potassium carbonate catalyst mixing.Thin reactor diameter is 50mm, is highly 3000mm, linear speed 15m/s, and steam/hydrocarbons ratio is
1mol/mol, reaction temperature are 800 DEG C, reaction pressure 2MPa；Crude reaction device diameter is 75mm, is highly 1500mm, reaction temperature
Degree is 650 DEG C, reaction pressure 2MPa.The load capacity of catalyst accounts for the 5% of raw coal quality.Circulation synthesis gas tolerance accounts for gasification installation
The 20% of exiting syngas total amount, recycling the ratio of hydrogen and carbon monoxide in synthesis gas is 1.Since separative efficiency is higher, from
The particle for opening separation equipment is considerably less, therefore flashing reactor selects tubular reactor, and operation temperature is 850 DEG C.Product gas is
Synthesis gas rich in methane, CH in exiting syngas4Concentration 30.3%, outlet efficiency of carbon con version reach 96.3%.
[embodiment 9]
Reaction process is same as Example 1.Experiment select Inner Mongol lignite, be crushed 1mm or less processed obtain fine coal and with
5% potassium carbonate catalyst mixing.Thin reactor diameter is 50mm, is highly 3000mm, linear speed 7m/s, and steam/hydrocarbons ratio is
1mol/mol, reaction temperature are 800 DEG C, reaction pressure 2MPa；Crude reaction device diameter is 75mm, is highly 1500mm, reaction temperature
Degree is 650 DEG C, reaction pressure 2MPa.The load capacity of catalyst accounts for the 5% of raw coal quality.Circulation synthesis gas tolerance accounts for gasification installation
The 20% of exiting syngas total amount, recycling the ratio of hydrogen and carbon monoxide in synthesis gas is 1.Since separative efficiency is higher, from
The particle for opening separation equipment is considerably less, therefore flashing reactor selects tubular reactor, and operation temperature is 850 DEG C.Product gas is
Synthesis gas rich in methane, CH in exiting syngas4Concentration 26.8%, outlet efficiency of carbon con version reach 96.9%.
[embodiment 10]
Reaction process is same as Example 1.Experiment select Inner Mongol lignite, be crushed 1mm or less processed obtain fine coal and with
5% potassium carbonate catalyst mixing.Thin reactor diameter is 50mm, is highly 3000mm, linear speed 2m/s, and steam/hydrocarbons ratio is
1mol/mol, reaction temperature are 800 DEG C, reaction pressure 0.1MPa；Crude reaction device diameter is 75mm, is highly 1500mm, reaction
Temperature is 650 DEG C, reaction pressure 2MPa.The load capacity of catalyst accounts for the 5% of raw coal quality.Circulation synthesis gas tolerance accounts for gasification dress
The 20% of exiting syngas total amount is set, recycling the ratio of hydrogen and carbon monoxide in synthesis gas is 1.Since separative efficiency is higher,
The particle for leaving separation equipment is considerably less, therefore flashing reactor selects tubular reactor, and operation temperature is 850 DEG C.Product gas
For the synthesis gas rich in methane, CH in exiting syngas4Concentration 22%, outlet efficiency of carbon con version reach 94.5%.
[embodiment 11]
Reaction process is same as Example 1.Experiment select Inner Mongol lignite, be crushed 1mm or less processed obtain fine coal and with
5% potassium carbonate catalyst mixing.Thin reactor diameter is 50mm, is highly 3000mm, linear speed 2m/s, and steam/hydrocarbons ratio is
1mol/mol, reaction temperature are 800 DEG C, reaction pressure 6.5MPa；Crude reaction device diameter is 75mm, is highly 1500mm, reaction
Temperature is 650 DEG C, reaction pressure 2MPa.The load capacity of catalyst accounts for the 5% of raw coal quality.Circulation synthesis gas tolerance accounts for gasification dress
The 20% of exiting syngas total amount is set, recycling the ratio of hydrogen and carbon monoxide in synthesis gas is 1.Since separative efficiency is higher,
The particle for leaving separation equipment is considerably less, therefore flashing reactor selects tubular reactor, and operation temperature is 850 DEG C.Product gas
For the synthesis gas rich in methane, CH in exiting syngas4Concentration 25.3%, outlet efficiency of carbon con version reach 97.2%.
[embodiment 12]
Reaction process is same as Example 1.Experiment select Inner Mongol lignite, be crushed 1mm or less processed obtain fine coal and with
5% potassium carbonate catalyst mixing.Thin reactor diameter is 50mm, is highly 3000mm, linear speed 2m/s, and steam/hydrocarbons ratio is
1mol/mol, reaction temperature are 1000 DEG C, reaction pressure 2MPa；Crude reaction device diameter is 75mm, is highly 1500mm, reaction temperature
Degree is 650 DEG C, reaction pressure 2MPa.The load capacity of catalyst accounts for the 5% of raw coal quality.Circulation synthesis gas tolerance accounts for gasification installation
The 20% of exiting syngas total amount, recycling the ratio of hydrogen and carbon monoxide in synthesis gas is 1.Since separative efficiency is higher, from
The particle for opening separation equipment is considerably less, therefore flashing reactor selects tubular reactor, and operation temperature is 850 DEG C.Product gas is
Synthesis gas rich in methane, CH in exiting syngas4Concentration 31.2%, outlet efficiency of carbon con version reach 98.7%.
[embodiment 13]
Reaction process is same as Example 1.Experiment select Inner Mongol lignite, be crushed 1mm or less processed obtain fine coal and with
5% potassium carbonate catalyst mixing.Thin reactor diameter is 50mm, is highly 3000mm, linear speed 2m/s, and steam/hydrocarbons ratio is
1mol/mol, reaction temperature are 800 DEG C, reaction pressure 2MPa；Crude reaction device diameter is 75mm, is highly 1500mm, reaction temperature
Degree is 650 DEG C, reaction pressure 2MPa.The load capacity of catalyst accounts for the 20% of raw coal quality.Circulation synthesis gas tolerance accounts for gasification dress
The 20% of exiting syngas total amount is set, recycling the ratio of hydrogen and carbon monoxide in synthesis gas is 1.Since separative efficiency is higher,
The particle for leaving separation equipment is considerably less, therefore flashing reactor selects tubular reactor, and operation temperature is 850 DEG C.Product gas
For the synthesis gas rich in methane, CH in exiting syngas4Concentration 27.5%, outlet efficiency of carbon con version reach 97.7%.
[embodiment 14]
Reaction process is same as Example 1.Experiment select Inner Mongol lignite, be crushed 1mm or less processed obtain fine coal and with
5% potassium carbonate catalyst mixing.Thin reactor diameter is 50mm, is highly 3000mm, linear speed 2m/s, and steam/hydrocarbons ratio is
1mol/mol, reaction temperature are 800 DEG C, reaction pressure 2MPa；Crude reaction device diameter is 75mm, is highly 1500mm, reaction temperature
Degree is 650 DEG C, reaction pressure 2MPa.The load capacity of catalyst accounts for the 1% of raw coal quality.Circulation synthesis gas tolerance accounts for gasification installation
The 20% of exiting syngas total amount, recycling the ratio of hydrogen and carbon monoxide in synthesis gas is 1.Since separative efficiency is higher, from
The particle for opening separation equipment is considerably less, therefore flashing reactor selects tubular reactor, and operation temperature is 850 DEG C.Product gas is
Synthesis gas rich in methane, CH in exiting syngas4Concentration 21.5%, outlet efficiency of carbon con version reach 96.5%.
[embodiment 15]
Reaction process is same as Example 1.Experiment select Inner Mongol lignite, be crushed 1mm or less processed obtain fine coal and with
5% potassium carbonate catalyst mixing.Thin reactor diameter is 50mm, is highly 3000mm, linear speed 2m/s, and steam/hydrocarbons ratio is
4mol/mol, reaction temperature are 800 DEG C, reaction pressure 2MPa；Crude reaction device diameter is 75mm, is highly 1500mm, reaction temperature
Degree is 650 DEG C, reaction pressure 2MPa.The load capacity of catalyst accounts for the 5% of raw coal quality.Circulation synthesis gas tolerance accounts for gasification installation
The 20% of exiting syngas total amount, recycling the ratio of hydrogen and carbon monoxide in synthesis gas is 1.Since separative efficiency is higher, from
The particle for opening separation equipment is considerably less, therefore flashing reactor selects tubular reactor, and operation temperature is 850 DEG C.Product gas is
Synthesis gas rich in methane, CH in exiting syngas4Concentration 22%, outlet efficiency of carbon con version reach 98.3%.
[embodiment 16]
Reaction process is same as Example 1.Experiment select Inner Mongol lignite, be crushed 1mm or less processed obtain fine coal and with
5% potassium carbonate catalyst mixing.Thin reactor diameter is 50mm, is highly 3000mm, linear speed 2m/s, and steam/hydrocarbons ratio is
0.2mol/mol, reaction temperature are 800 DEG C, reaction pressure 2MPa；Crude reaction device diameter is 75mm, is highly 1500mm, reaction
Temperature is 650 DEG C, reaction pressure 2MPa.The load capacity of catalyst accounts for the 5% of raw coal quality.Circulation synthesis gas tolerance accounts for gasification dress
The 20% of exiting syngas total amount is set, recycling the ratio of hydrogen and carbon monoxide in synthesis gas is 1.Since separative efficiency is higher,
The particle for leaving separation equipment is considerably less, therefore flashing reactor selects tubular reactor, and operation temperature is 850 DEG C.Product gas
For the synthesis gas rich in methane, CH in exiting syngas4Concentration 24%, outlet efficiency of carbon con version reach 94.2%.
[embodiment 17]
Reaction process is same as Example 1.Experiment select Inner Mongol lignite, be crushed 1mm or less processed obtain fine coal and with
5% potassium carbonate catalyst mixing.Thin reactor diameter is 50mm, is highly 3000mm, linear speed 2m/s, and steam/hydrocarbons ratio is
1mol/mol, reaction temperature are 800 DEG C, reaction pressure 2MPa；Crude reaction device diameter is 75mm, is highly 1500mm, reaction temperature
Degree is 650 DEG C, reaction pressure 2MPa.The load capacity of catalyst accounts for the 5% of raw coal quality.Circulation synthesis gas tolerance accounts for gasification installation
The 20% of exiting syngas total amount, recycling the ratio of hydrogen and carbon monoxide in synthesis gas is 4.5.Since separative efficiency is higher,
The particle for leaving separation equipment is considerably less, therefore flashing reactor selects tubular reactor, and operation temperature is 850 DEG C.Product gas
For the synthesis gas rich in methane, CH in exiting syngas4Concentration 29.2%, outlet efficiency of carbon con version reach 91.9%.
[embodiment 18]
Reaction process is same as Example 1.Experiment select Inner Mongol lignite, be crushed 1mm or less processed obtain fine coal and with
5% potassium carbonate catalyst mixing.Thin reactor diameter is 50mm, is highly 3000mm, linear speed 2m/s, and steam/hydrocarbons ratio is
1mol/mol, reaction temperature are 800 DEG C, reaction pressure 2MPa；Crude reaction device diameter is 75mm, is highly 1500mm, reaction temperature
Degree is 650 DEG C, reaction pressure 2MPa.The load capacity of catalyst accounts for the 5% of raw coal quality.Circulation synthesis gas tolerance accounts for gasification installation
The 20% of exiting syngas total amount, recycling the ratio of hydrogen and carbon monoxide in synthesis gas is 2.Since separative efficiency is higher, from
The particle for opening separation equipment is considerably less, therefore flashing reactor selects tubular reactor, and operation temperature is 850 DEG C.Product gas is
Synthesis gas rich in methane, CH in exiting syngas4Concentration 26.6%, outlet efficiency of carbon con version reach 93.9%.
[embodiment 19]
Reaction process is same as Example 1.Experiment select Inner Mongol lignite, be crushed 1mm or less processed obtain fine coal and with
5% potassium carbonate catalyst mixing.Thin reactor diameter is 50mm, is highly 3000mm, linear speed 2m/s, and steam/hydrocarbons ratio is
1mol/mol, reaction temperature are 800 DEG C, reaction pressure 2MPa；Crude reaction device diameter is 75mm, is highly 1500mm, reaction temperature
Degree is 650 DEG C, reaction pressure 2MPa.The load capacity of catalyst accounts for the 5% of raw coal quality.Circulation synthesis gas tolerance accounts for gasification installation
The 45% of exiting syngas total amount, recycling the ratio of hydrogen and carbon monoxide in synthesis gas is 1.Since separative efficiency is higher, from
The particle for opening separation equipment is considerably less, therefore flashing reactor selects tubular reactor, and operation temperature is 850 DEG C.Product gas is
Synthesis gas rich in methane, CH in exiting syngas4Concentration 27.8%, outlet efficiency of carbon con version reach 93.2%.
[embodiment 20]
Reaction process is same as Example 1.Experiment select Inner Mongol lignite, be crushed 1mm or less processed obtain fine coal and with
5% potassium carbonate catalyst mixing.Thin reactor diameter is 50mm, is highly 3000mm, linear speed 2m/s, and steam/hydrocarbons ratio is
1mol/mol, reaction temperature are 800 DEG C, reaction pressure 2MPa；Crude reaction device diameter is 75mm, is highly 1500mm, reaction temperature
Degree is 650 DEG C, reaction pressure 2MPa.The load capacity of catalyst accounts for the 5% of raw coal quality.Circulation synthesis gas tolerance accounts for gasification installation
The 10% of exiting syngas total amount, recycling the ratio of hydrogen and carbon monoxide in synthesis gas is 1.Since separative efficiency is higher, from
The particle for opening separation equipment is considerably less, therefore flashing reactor selects tubular reactor, and operation temperature is 850 DEG C.Product gas is
Synthesis gas rich in methane, CH in exiting syngas4Concentration 23.7%, outlet efficiency of carbon con version reach 97.4%.[comparative example 1]
Using the gasification reactor apparatus in the technique of multicompartment fluidized bed catalytic gasification methane-rich gas in the prior art, choosing
With Inner Mongol lignite, partial size is less than 1mm, the potassium carbonate that catalyst is 15%, operating pressure 2MPa, and 700 DEG C of operation temperature, gaseous line
Speed 1.2m/s.Test CO+H in obtained exit gas component2Content 60.2%, methane content 7.9%, efficiency of carbon con version
55%.
[comparative example 2]
Use in the prior art lurgi gasifier for coal gasification reaction device in preparing methane from coal technique, select Inner Mongol lignite, partial size
Less than 1mm, the potassium carbonate that catalyst is 15%, operating pressure 2MPa, 700 DEG C of operation temperature, gas phase linear velocity 1.2m/s.Experiment
CO+H in obtained exit gas component2Content 64%, methane content 14.1%, efficiency of carbon con version 91.7%.
Table 1
Continued 1
Continued 1
Claims (10)
1. a kind of combined fluidized bed reaction unit of catalytic gasification, capital equipment include: thin reactor (3), crude reaction device (4) and
Settler (6), which is characterized in that it is connected after thin reactor (3) upper end is expanding with crude reaction device (4) bottom, crude reaction device (4)
It is connected by separation equipment (7) with settler (6), the bottom of settler (6) passes through Loop Seal (8) and thin reactor (3)
It is connected, separation equipment (7) is located in settler (6) cylinder.
2. the combined fluidized bed reaction unit of catalytic gasification according to claim 1, it is characterised in that the thin reactor (3)
Height is 2-8 times of crude reaction device (4) height.
3. the combined fluidized bed reaction unit of catalytic gasification according to claim 1, it is characterised in that the crude reaction device (4)
Diameter is 1.5-6 times of thin reactor (3) diameter.
4. the combined fluidized bed reaction unit of catalytic gasification according to claim 1, it is characterised in that the settler (6) is built-in
Separation equipment (7), the separation equipment (7) are composed of 2 groups and 2 groups or more of cyclone separator.
5. a kind of combined fluidized bed reaction method of catalytic gasification is collaborated using any one catalytic gasification group of Claims 1 to 4
Fluidized bed reaction device comprises the following steps:
(a), the carbon raw material (E) of supported catalyst is entered in settler (6) by feeding line (10), and passes through Loop Seal
(8) it imports, with the gasifying agent (A) in gas line (2) simultaneously into being mixed in thin reactor (3) and gasified reverse
It answers, the bulky grain slag after reaction is fallen in slag bath (1) by natural subsidence, and is isolated by catalyst reclaimer (11)
Lime-ash (G) and slag bath recycling catalyst (F)；
(b), the carbonaceous particles in thin reactor (3) after reaction enter in crude reaction device (4) by gas lift, are coming from gas
Purification and further gasification reaction under the action of the circulation synthesis gas (B) of separation system (9), hydrogen in the circulation synthesis gas (B)
The volume ratio of gas and carbon monoxide is 0.8-4.5, and the gas and solid after reaction enter in separation equipment (7), and the solid contains
Have fine ash, carbon-bearing particulate matter and slag, after separation, gas with not by isolated fine ash and not by isolated carbonaceous particles by
Enter after whirlwind discharge and carry out Quick-gasifying reaction in flashing reactor (5), then using gas purification and separation system (9)
Extract the catalyst (D) of product gas, outlet fine ash (C) and fine ash recycling；
(c), still further aspect, by carbonaceous particles and the slag sedimentation in settler (6) after separation equipment (7) separation, and with
The carbon raw material (E) of the catalyst (D), supported catalyst that are recycled from the fine ash of feeding line (10), slag bath recycling catalyst (F)
Mixing returns by Loop Seal (8) and continues gasification reaction in thin reactor (3).
6. the combined fluidized bed reaction method of catalytic gasification according to claim 5, it is characterised in that the carbon raw material choosing
From coal, petroleum coke, biomass and its mixture, the gasifying agent be selected from oxygen, air, liquid water, vapor, carbon dioxide or
Hydrogen and its mixture.
7. the combined fluidized bed reaction method of catalytic gasification according to claim 5, it is characterised in that the thin reactor (3)
Reaction condition are as follows: reaction pressure 0-6.5MPa, 800-1600 DEG C of reaction temperature, gas phase linear velocity 2.0-15.0m/s, it is thin to react
Fluidised form in device (3) is fast fluidization；The reaction condition of crude reaction device (4) are as follows: reaction pressure 0-6.5MPa, reaction temperature
600-1100 DEG C, gas phase linear velocity 0.1-1.0m/s, the fluidised form in crude reaction device (4) are turbulence fluidization or bubbling fluidization.
8. the combined fluidized bed reaction method of catalytic gasification according to claim 5, it is characterised in that the catalyst is selected from
At least one of alkali metal, alkaline-earth metal, transition metal；The catalyst is with infusion process, dry pigmentation or ion-exchange side
Formula is supported on carbon raw material；The load capacity of the catalyst accounts for the 0.1~20% of raw coal quality.
9. the combined fluidized bed reaction method of catalytic gasification according to claim 5, it is characterised in that the thin reactor (3)
The range of interior steam/hydrocarbons ratio is 0.5-4mol/mol, and the range of the steam/hydrocarbons ratio in the crude reaction device (4) is 2-20mol/mol.
10. the combined fluidized bed reaction method of catalytic gasification according to claim 5, it is characterised in that the flashing reactor
It (5) is downflow fluidized bed, Cyclonic reactor, tubular reactor or fluidized-bed reactor.
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| EP2650347A1 (en) * | 2012-01-31 | 2013-10-16 | extech GmbH | Combined mixed gas system with gas purification and gas purification device |
| CN103450922A (en) * | 2012-05-28 | 2013-12-18 | 中国石油天然气股份有限公司 | Heavy oil thermal conversion and green coke gasification method and integrated device |
| CN106590761A (en) * | 2015-10-19 | 2017-04-26 | 中国石油化工股份有限公司 | Fluidized bed reaction device and reaction method for coal catalytic gasification for producing methane-rich synthetic gas |
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| CN101054536A (en) * | 2007-05-31 | 2007-10-17 | 宋建元 | Coal gasification device for circulating fluidized bed and manufacturing method thereof |
| EP2650347A1 (en) * | 2012-01-31 | 2013-10-16 | extech GmbH | Combined mixed gas system with gas purification and gas purification device |
| CN103450922A (en) * | 2012-05-28 | 2013-12-18 | 中国石油天然气股份有限公司 | Heavy oil thermal conversion and green coke gasification method and integrated device |
| CN106590761A (en) * | 2015-10-19 | 2017-04-26 | 中国石油化工股份有限公司 | Fluidized bed reaction device and reaction method for coal catalytic gasification for producing methane-rich synthetic gas |
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