CN109401794A

CN109401794A - The combined fluidized bed reaction unit of staged conversion and reaction method

Info

Publication number: CN109401794A
Application number: CN201710704543.5A
Authority: CN
Inventors: 徐俊; 钟思青; 霍威; 屠功毅
Original assignee: China Petroleum and Chemical Corp; Sinopec Shanghai Research Institute of Petrochemical Technology
Current assignee: China Petroleum and Chemical Corp; Sinopec Shanghai Research Institute of Petrochemical Technology
Priority date: 2017-08-17
Filing date: 2017-08-17
Publication date: 2019-03-01
Anticipated expiration: 2037-08-17
Also published as: CN109401794B

Abstract

The present invention relates to a kind of combined fluidized bed reaction unit of staged conversion 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, treating capacity is little, deslagging is difficult to and fine coal utilization rate is lower.The present invention passes through a kind of combined fluidized bed reaction unit of staged conversion and reaction method, the carbon raw material of supported catalyst is pyrolyzed in pyrolysis oven, tar gas is collected after separation, the semicoke particle and gasifying agent and oxidant for being pyrolyzed back loading catalyst carry out part burning and gasification reaction in thin reactor, the carbonaceous particles of the synthesis gas and unfinished reaction that then generate carry out further gasification reaction in crude reaction device, carbonaceous particles and partial catalyst after reaction continue to return in pyrolysis oven, the lime-ash of bottom carries out the technical solution of deslagging in such a way that interval is classified deslagging, preferably resolve above-mentioned technical problem, it can be applied in the industrial production of coal staged conversion.

Description

The combined fluidized bed reaction unit of staged conversion and reaction method

Technical field

The present invention relates to a kind of combined fluidized bed reaction unit of staged conversion 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 is coal high-efficiency, the core technology of clean utilization, is Development of Coal base chemicals production, the combustion of coal base fluid body The basis of the process industrials such as material, synthetic natural gas (SNG), IGCC power generation, hydrogen manufacturing, industrial combustion gas and polygenerations systeme.China is Maximum Coal Gasification Technology application market in the world.Currently, various kinds of coal gas technology successfully realizes industrial applications, it is all made of Non-catalyzed gasification 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 The problems such as difficulty, energy consumption are high, harsh to equipment requirement.However, the catalytic gasification process of coal not only increases gasification reaction rate, It has been significantly reduced gasification reaction temperature simultaneously, has been achieved the mild gasification of coal.Many conjunctions can also be carried out simultaneously At process, under the effect of the catalyst, can while coal gasification the industrial chemicals such as synthesizing methane, methanol, ammonia, shorten technique Process.The synthesis gas rich in methane is directly wherein produced by the method for catalytic coal gasifaction, is that one of catalytic coal gasifaction is important Research direction.

In terms of the reactor of Coal Gasification Technology, currently relatively broad belongs to entrained flow bed gasification technology.But this skill Art must use the high-quality coal of low ash smelting point (1350 DEG C of <) and low ash content (< 10~15%), and solve high-ash-fusion coal Method is usually the fluxing agent for being added 10~30%, so that the ash of charging is higher, influences its operability and economy.Meanwhile The excessively high operation temperature of air flow bed slag gasification technology improves the investment, maintenance and operating cost of air flow bed.American Electric Power is ground The research report for studying carefully institute (EPRI) points out that existing industrial gas bed gasification furnace is not suitable for high ash, high ash melting point coal gasification, the world Need industrialized fluidized gasification technology.No matter fluidization, which burns or gasify to all have, adapts to high ash melting point, dirty coal Kind person's character, the circulating fluidized bed boiler burning gangue that succeeded is clear proof.

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%.

The method and device that patent CN101942344A discloses a kind of gasifying multi-segment staged converted fluidized bed is by standby Coal, gas supply, gasification, deslagging and fine powder conveying are formed, and multistage staged conversion fluidized gasification device is by melting poly- ash content from list Member, multistage staged fluidized bed pyrolytic gasification reactor, semicoke fine powder circulation conveying unit composition have gasification furnace volume utilization The characteristic high, treating capacity is big, total carbon utilisation rate is high is suitble to coal grading to convert integrated system, and the production that can be used alone is suitable for Extensive coal methylmethane synthesis and coal chemical industry coal gas.There is no fully utilize by being pyrolyzed out for the classification gasification of the technology Tar gas does not utilize the higher tar gas of added value more efficiently in terms of coal quality classified utilization；Still further aspect, the technology In melting after poly- grey Selective Separation of using of deslagging technique, dried slag removing, this technology have the prominent of matter compared with the technology of forefathers again It is broken, high stability, but due in reactor the process of slag making be unable to control position and the size of slagging, while deslagging mistake Cheng Zhong can not be completely separated semicoke and lime-ash due to the restriction of structure, therefore will cause that deslagging is inefficient, and carbon contains in slag Amount is not low, and overall carbon conversions are not high.

How to realize that gasified raw material localizes, develops the gasification furnace of suitable different types of coal characteristic, downstream product to China Development of Coal Chemical Industry it is most important.Existing gasification technology is promoted to a higher rank, and realizes the staged conversion of coal, by different technologies integrated optimization It is also an important trend of Coal Gasification Technology development.It is also required to develop simultaneously and is suitble to the carbonaceous solids substance in addition to coal Gasification technology, including biomass, liquefied residue, petroleum residue and carbonaceous solids waste etc..

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, and the direct emission for the thick slag of furnace bottom that gasifies largely also affects the promotion of efficiency of carbon con version, For the utilization rate of energy, the direct combustion gasification of tar causes energy and economic larger waste, and efficiency of carbon con version is lower When, the calorific value of carbon residue is not fully utilized.Thus it is necessary to develop one kind to can be improved efficiency of carbon con version and improve the intensity of gasification, first Alkane yield and the high coal grading method for transformation of fine coal utilization rate.

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 The problem that alkane yield is relatively low, treating capacity is little, deslagging low efficiency and fine coal utilization rate be not high provides a kind of new catalytic gasification Combined fluidized bed reaction unit and reaction method.Fluidized-bed reactor has efficiency of carbon con version height, intensity of gasification height, first in this method The feature that alkane yield is high, treating capacity is big, deslagging is controllable, stable and efficient and stable gasifier operation guarantees the efficient of reaction With stabilization.

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 staged conversion combination fluidisation Bed reaction device, capital equipment include: thin reactor 4, crude reaction device 5, pyrolysis oven 6 and classification slag-draining device 2, wherein thin anti- Answer 4 upper end of device it is expanding after be connected with 5 bottom of crude reaction device, crude reaction device 5 is connected with pyrolysis oven 6, pyrolysis oven 6 with carefully react Device 4 is connected by the first Loop Seal 9.

In above-mentioned technical proposal, the height of the thin reactor 4 is 2~8 times of 5 height of crude reaction device, the thin reaction The diameter of device 4 is 1.5~6 times of 5 diameter of crude reaction device.The slag-draining device 2 that is classified is by the deslagging of two sections difference barrel dliameter Device composition, the upper section slag-draining device diameter is 2~10 times of lower section slag-draining device diameter.In the classification slag-draining device 2 Equipped with classification baffle 3, the pattern of the classification baffle is perforated baffle, slanting baffle, grid baffle or ring core baffle.Above-mentioned technology In scheme, preferred technical solution is that classification baffle is ring core baffle.In above-mentioned technical proposal, preferred upper section slag-draining device is straight Diameter is 7~10 times of lower section slag-draining device diameter.

First Loop Seal 9 and the second Loop Seal 8 are loop seal, the loop seal type Formula is U valve, J valve, L valve or W valve.Preferred loop seal pattern is W valve in above-mentioned technical proposal.The W valve is by returning Expects pipe 12, resistance tube 13, inclined tube 14 and standpipe 15 form；12 bottom of refeed line is equipped with refeed line and inflates wind I；Resistance tube bottom Portion 13 is equipped with resistance tube and inflates wind H；The caliber of the refeed line 12, resistance tube 13 and inclined tube 14 is the 0.5~1 of standpipe caliber Times；The returning charge angle and resistance angle of the W valve are 45 °~75 °, and returning charge angle is greater than or equal to resistance angle.In above-mentioned technical proposal The returning charge angle and resistance angle of preferred W valve are 60 °~75 °, and the caliber of resistance tube 13 and inclined tube 14 is the 0.7~1 of standpipe caliber Times.In order to solve the above problem two, The technical solution adopted by the invention is as follows: a kind of combined fluidized bed reaction side of staged conversion Method comprises the following steps:

A, the carbon raw material E of supported catalyst, which enters in pyrolysis oven 6, is pyrolyzed rapidly, and the pyrolysis gas and semicoke after pyrolysis are in warm After being separated in solution furnace 6 and cyclone separator 7, coal tar D enters follow-up equipment and is purified and separated；

B, the semicoke after separation flows separately through the first Loop Seal 8 and the second Loop Seal 9, enters simultaneously with gasifying agent F It is mixed and is burnt, gasification reaction in thin reactor 4, the carbonaceous particles that the bulky grain slag after reaction does not react completely with part It controls and enters in classification slag-draining device 2 by valve, bulky grain is discharged by the bottom of classification slag-draining device 2 after gradation Slag, and the top that carbonaceous particles then pass through classification slag-draining device 2 flows into the upper end of thin reactor 4 and continues to participate in reaction；

C, the carbonaceous particles after reacting in thin reactor 4 enter further gasified reverse in crude reaction device 5 by gas lift It answers；Raw gas G after reaction purifies collection after separation, and the carbonaceous particles after separation enter pyrolysis oven 6 as heat carrier with slag In, heat is provided for the carbon raw material E pyrolysis of supported catalyst.

In above-mentioned technical proposal, the carbon raw material is selected from least one of coal, petroleum coke, biomass, the gasification Agent is selected from least one of oxygen, air, liquid water, vapor, carbon dioxide or hydrogen.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.The reaction item of the thin reactor 4 Part are as follows: 0~6.5MPa of reaction pressure, 800~1300 DEG C of reaction temperature, 2.0~15.0m/s of gas phase linear velocity, the thin reaction Fluidised form in device 4 is fast fluidization；The reaction condition of the crude reaction device 5 are as follows: 0~6.5MPa of reaction pressure, reaction temperature 600~1000 DEG C, 0.1~1.0m/s of gas phase linear velocity, the fluidised form in the crude reaction device 5 are turbulence fluidization or are bubbled fluidised form Change；Operation temperature in the pyrolysis oven 6 is 100-300 DEG C lower than the temperature in crude reaction device；Under in the classification slag-draining device 2 Gas phase linear velocity is 0.8~3m/s in section cylinder, and gas phase linear velocity is 0.1~0.3m/s in upper section cylinder；Returning charge in the W valve The blowing pressure that the refeed line inflation wind I and resistance bottom of the tube 13 of 12 bottom of pipe are equipped with resistance tube inflation wind H is less than or equal to vertical The pressure of bottom in pipe 15.

What is entered in thin reactor 4 in the present invention is the semicoke and gasifying agent after pyrolysis, in the reactor with combustion reaction, Based on gasification reaction and Partial Transformation reaction, methanation reaction.Since linear speed is higher in thin reactor, gas-solid ratio is relatively high, Steam/hydrocarbons ratio is also higher, and temperature controls within the scope of 800-1300 DEG C, is conducive to burning and gasification reaction.Carbon raw material and return Carbonaceous particles under the effect of the catalyst, due in reactor Gas-solid Two-phase Flow state be fast fluidization state, gas Content it is very high, gas-solid contact efficiency is also very high, thus combustion rate and gasification reaction rate is caused faster to improve The utilization rate of efficiency of carbon con version and carbon residue.The heat that combustion reaction generates is used to provide the consumption and heat of heat in gasification reaction area Damage, and necessary heat and gasifying agent are provided for gasification reaction.

Conversion reaction and methanation reaction and partial gasification reaction are substantially carried out in the present invention in crude reaction device 5.By thin CO, H in the gas component flowed into reactor 4₂、CO₂、H₂O and CH₄It exists simultaneously, while being passed through and following in 5 bottom of crude reaction device Ring synthesis gas, circulation synthesis gas are by the gas of this system output, after purification and separation system, through CO₂Absorption plant removes Remove CO₂Synthesis gas after gas improves CO and H in crude reaction device 5₂Content, dilute CO₂Content, it is anti-to promote transformation The balance answered moves right, and improves H₂The ratio of/CO, and gas phase linear speed is lower in crude reaction device 5, gas-solid fluidised form be bubbled or Turbulent flow wants much lower in the thinner reactor 4 of gas-solid, and temperature control promotes methane within the scope of 600-1000 DEG C The movement for changing reaction balance improves outlet CH₄Yield.

6 selecting reactor of pyrolysis oven is bubbling fluidized bed or turbulent fluidized bed in the present invention, and the control of gas phase linear speed exists in bed 0.1-1m/s, heat source in furnace from by after gasification reaction high-temp solid heat carrier carbonaceous particles and lime-ash from crude reaction device Bring in 5, temperature control is 100-300 DEG C lower than the temperature in gasification reactor crude reaction device 5, under the effect of the catalyst The pyrolysis for carrying out the carbon raw material of high temperature, can be very easy to obtain conceivable tar product and coal gas product.This part Tar conventionally, as technology limitation, generally directly directly burnt up in gasification reactor；If not urging Under the action of agent, the particle heat that heat carrier particle is returned by gasification furnace is unable to reach the effect of high temperature pyrolysis, same to lose Larger amount of tar.And in the gasification reaction that lignite is raw material, the tar content of lignite is very high, if this part tar is not Extract and directly burn up, economic implication is very big, therefore the present invention pass through to lignite under the effect of the catalyst first High temperature pyrolysis extracts the tar of the overwhelming majority as product.The present invention under the effect of the catalyst, enhances carbon raw material and exists Rapid output tar and coal gas generate the pyrolytical condition of semicoke simultaneously under conditions of high temperature.In bubbling fluidized bed pyrolysis oven 6 Fluidized wind mostly come from gasification reaction by CO₂The CO that absorption plant absorbs₂Product is eliminated to be additionally required and be produced CO₂Funds.And it is preferred that bubbling fluidized bed or turbulent fluidized bed are as pyrolysis installation, heat transference efficiency is than traditional moving bed skill Art is much higher, and is not easy to plug agglomeration.

Pyrolysis oven 6 is preferably a kind of novel Cyclonic reactor in the present invention, is similar to cyclone separator, Cyclonic reactor Entrance can set 1-4, preferably 2.Cyclonic reactor inlet gas phase velocity is 15-30m/s.Heat source in furnace is from by gas High-temp solid heat carrier M carbonaceous particles and the lime-ash bring from crude reaction device 5 after changing reaction, temperature are controlled than gasified reverse It answers the temperature in device crude reaction device 5 100-300 DEG C low, carries out the pyrolysis of the carbon raw material of high temperature under the effect of the catalyst, It can be very easy to obtain conceivable tar product and coal gas product.The present invention under the effect of the catalyst, enhances carbon containing Raw material rapid output tar and coal gas under conditions of high temperature generate the pyrolytical condition of semicoke simultaneously.The Cyclonic reactor entrance Settable band is angled, can effectively reduce and enter riser by inlet direct short-circuit, improves the efficiency of cyclonic separation, simultaneously There is no back-mixing, reaction sequence carries out, and time of contact is short, advantageously forms semicoke and carries out next step gasification reaction.

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.First Loop Seal 9 and the second Loop Seal 8 are on-mechanical returning charge Mechanism, the loop seal pattern are U valve, J valve, L valve or W valve, it is not easy to leakage blocking.Overall structure is simple, if It is standby mature, it is not easy to abrasion and leakage occur.

Heretofore described first Loop Seal 9 and the second Loop Seal 8 are loop seal, and the on-mechanical returns Expect that mechanism form is preferably W valve.Granule organics in circulating fluidized bed system are to influence entire coal gasification treating capacity Key parameter, per area per time are directly related to the intensity and treating capacity of gasification by the semicoke particle of Loop Seal, Therefore it is met into outside the amount of the gasifying agent in reactor under an increased pressure, the semicoke that can orderly feed sufficient amount is skill Art difficult point and key.General non-mechanical valve is limited to the influence of pressure drop after and before the valve, while worrying that be passed through tolerance is easy too much The cyclone separator at standpipe and top is caused to collaborate, therefore the operation threshold of granule organics is relatively narrow.And W valve effectively increases The raising of grain cycle rate, while playing a reversed role for gas is avoided, it can play the role of stablizing high-throughput circulation.

The effect of heretofore described classification slag-draining device 2 is lime-ash controllable, orderly, being efficiently discharged in reactor. Now by deslagging technique, since the process of slag making is unable to control position and the size of slagging, while tapping process in reactor In, due to the restriction of structure, it can not be completely separated semicoke and lime-ash, therefore it is inefficient to will cause deslagging, carbon content in slag It is not low, so that overall carbon conversions are not high.Classification slag-draining device 2 of the invention is to pass through it using carbonaceous particles and lime-ash The difference of the fluidization characteristic of itself, in conjunction with baffle, reinforcing particle isolation classification.Slag-drip opening is according to differential pressure principle simultaneously, using class Like the technology of locking hopper, the very low lime-ash of phosphorus content is smoothly discharged.

The CO of exhaust gas is originally used in reaction unit system of the invention₂Product is fully used, the energy of pyrolysis Be by being passed in gasification reaction, due to the addition of catalyst so that the temperature of whole system is all in a lower level, Therefore the present invention increases than the prior art in terms of economy and safety.

Reaction unit and method of the invention is not limited only to be used in rich methane phase technique, may be also used in the combustion of fine coal system Expect in the techniques such as gas, fine coal hydrogen manufacturing.

Using technical solution of the present invention, compared with prior art, can orderly deslagging, deslagging is high-efficient, while having The feature that grain cycle rate is high, treating capacity is big, efficiency of carbon con version is high, methane production is high, volume increase tar and fine coal utilization rate are high, row Carbon content reduces 2% in lime-ash out, and granule organics improve 20%, guarantee reaction it is efficient with stablize, achieve compared with Good technical effect.

Detailed description of the invention

Fig. 1 is the flow diagram of the method for the invention；

Fig. 2 is the structural schematic diagram of W valve of the present invention；

Fig. 3 is the schematic diagram of ring core baffle of the present invention；

Fig. 4 is the schematic diagram of slanting baffle of the present invention；

Fig. 5 is the schematic diagram of grid baffle of the present invention；

Fig. 6 is the schematic diagram of macropore baffle of the present invention.

In Fig. 1,1 is locking hopper；2 be classification slag-draining device；3 be classification baffle；4 be thin reactor；5 be crude reaction Device；6 be pyrolysis oven；7 be cyclone separator；8 be the first Loop Seal；9 be the second Loop Seal.A is lime-ash；B is classification row The fluidized wind of slag device；C is circulation synthesis gas；D is coal tar；E is the carbon raw material of supported catalyst；F is gasifying agent, is selected from Oxygen, air, liquid water, vapor, carbon dioxide or hydrogen and its mixture；G is raw gas.

The carbon raw material E of supported catalyst, which enters in pyrolysis oven 6, to be pyrolyzed rapidly, and the pyrolysis gas and semicoke after pyrolysis are being pyrolyzed After being separated in furnace 6, coal tar D enters follow-up equipment and is purified and separated；Semicoke after separation flows separately through first and returns Expect mechanism 8 and the second Loop Seal 9, enters in thin reactor 4 simultaneously with gasifying agent F and mixed and burnt, gasification reaction, instead Bulky grain slag after answering enters in classification slag-draining device 3 with the carbonaceous particles that part is not reacted completely by valve control, passes through Bulky grain slag is discharged by the bottom of classification slag-draining device 3 after gradation, and carbonaceous particles then pass through the upper of classification slag-draining device 3 The upper end that portion flows into thin reactor 4 continues to participate in reaction；Carbonaceous particles after reacting in thin reactor 4 enter by gas lift Further gasification reaction in crude reaction device 5；Raw gas G after reaction purifies collection after separation, the carbonaceous particles after separation with Slag enters in pyrolysis oven 6 as heat carrier, provides heat for the carbon raw material E pyrolysis of supported catalyst.

In Fig. 2,4 be thin reactor；12 be refeed line；13 be resistance tube；14 be inclined tube；15 be standpipe.I is returning charge in figure Pipe inflates wind；H is that resistance tube inflates wind.α is returning charge angle；β is resistance angle.

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 pyrolysis oven by feeding line to be pyrolyzed, tar gas warp Collected after crossing separation, be pyrolyzed back loading catalyst semicoke particle and gasifying agent and oxidant simultaneously with higher linear speed with it is lower Granule density part burning and gasification reaction are carried out in thin reactor, the bulky grain slag after reaction with part do not react completely Carbonaceous particles by valve control enter classification slag-draining device in, after gradation by classification slag-draining device bottom arrange Bulky grain slag out, and the top that carbonaceous particles then pass through classification slag-draining device flows into the upper end of thin reactor and continues to participate in reaction. Carbonaceous particles after reacting in thin reactor enter further gasification reaction in crude reaction device by gas lift.It is thick after reaction Coal gas purifies collection after separation, and the carbonaceous particles after separation and slag enter in pyrolysis oven as heat carrier, is supported catalyst Carbon raw material pyrolysis provide heat.

Inner Mongol lignite is selected in experiment, is crushed 2mm 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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects bubbling fluidized bed, and reaction temperature is 600 DEG C.It is classified slag-draining device upper diameter and lower section diameter ratio is 7, Ring core baffle is equipped in device.Loop Seal uses U valve.Being classified carbon content in slag-draining device bottom discharge lime-ash is 1.1%, Grain cycle rate is 32kg/m²S exports CH₄Concentration 20.8%, outlet efficiency of carbon con version reach 97.8%, tar content 6.7%, As a result see Table 1 for details.

[embodiment 2]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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 300mm, is highly 1500mm.The load capacity of catalyst accounts for the 5% of raw coal quality. Circulation synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas It is 1.Pyrolysis oven selects bubbling fluidized bed, and reaction temperature is 600 DEG C.Slag-draining device upper diameter, which is classified, with lower section diameter ratio is 7, device is interior to be equipped with ring core baffle.Loop Seal uses U valve.Carbon content is in classification slag-draining device bottom discharge lime-ash 0.66%, granule organics 32kg/m²S exports CH₄Concentration 21.3%, outlet efficiency of carbon con version reach 98.2%, tar Content 6.5%.

[embodiment 3]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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 150mm, is highly 1500mm.The load capacity of catalyst accounts for the 5% of raw coal quality. Circulation synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas It is 1.Pyrolysis oven selects bubbling fluidized bed, and reaction temperature is 600 DEG C.Slag-draining device upper diameter, which is classified, with lower section diameter ratio is 7, device is interior to be equipped with ring core baffle.Loop Seal uses U valve.Carbon content is in classification slag-draining device bottom discharge lime-ash 0.65%, granule organics 32kg/m²S exports CH₄Concentration 21%, tar content 6.5%, outlet efficiency of carbon con version reach 98.1%.

[embodiment 4]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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 375mm.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects bubbling fluidized bed, and reaction temperature is 600 DEG C.It is classified slag-draining device upper diameter and lower section diameter ratio is 7, Ring core baffle is equipped in device.Loop Seal uses U valve.Being classified carbon content in slag-draining device bottom discharge lime-ash is 1.3%, Grain cycle rate is 32kg/m²S exports CH₄Concentration 20.1%, tar content 6.6%, outlet efficiency of carbon con version reach 97.3%.

[embodiment 5]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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 1000mm.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects bubbling fluidized bed, and reaction temperature is 600 DEG C.It is classified slag-draining device upper diameter and lower section diameter ratio is 7, Ring core baffle is equipped in device.Loop Seal uses U valve.Being classified carbon content in slag-draining device bottom discharge lime-ash is 0.98%, Granule organics are 32kg/m²S exports CH₄Concentration 20.2%, tar content 6.6%, outlet efficiency of carbon con version reach 97.8%.

[embodiment 6]

Inner Mongol lignite is selected in experiment, is crushed 2mm or less processed and obtains fine coal and mix with 5% potassium carbonate catalyst. Thin reactor diameter is 50mm, is highly 3000mm, linear speed 15m/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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects bubbling fluidized bed, and reaction temperature is 600 DEG C.It is classified slag-draining device upper diameter and lower section diameter ratio is 7, Ring core baffle is equipped in device.Loop Seal uses U valve.Being classified carbon content in slag-draining device bottom discharge lime-ash is 1.2%, Grain cycle rate is 32kg/m²S exports CH₄Concentration 23.4%, outlet efficiency of carbon con version reach 97.6%, tar content 6.3%.

[embodiment 7]

Inner Mongol lignite is selected in experiment, is crushed 2mm or less processed and obtains fine coal and mix with 5% potassium carbonate catalyst. Thin reactor diameter is 50mm, is highly 3000mm, linear speed 7m/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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects bubbling fluidized bed, and reaction temperature is 600 DEG C.It is classified slag-draining device upper diameter and lower section diameter ratio is 7, Ring core baffle is equipped in device.Loop Seal uses U valve.Being classified carbon content in slag-draining device bottom discharge lime-ash is 0.6%, Grain cycle rate is 32kg/m²S exports CH₄Concentration 22.5%, outlet efficiency of carbon con version reach 98.5%, tar content 6.6%.

[embodiment 8]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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 0.1MPa；Crude reaction device diameter is 75mm, is highly 1500mm.The load capacity of catalyst accounts for the 5% of raw coal quality. Circulation synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas It is 1.Pyrolysis oven selects bubbling fluidized bed, and reaction temperature is 600 DEG C.Slag-draining device upper diameter, which is classified, with lower section diameter ratio is 7, device is interior to be equipped with ring core baffle.Loop Seal uses U valve.Being classified carbon content in slag-draining device bottom discharge lime-ash is 2.8%, Granule organics are 32kg/m²S exports CH₄Concentration 18.9%, outlet efficiency of carbon con version reach 96.1%, tar content 6.7%.

[embodiment 9]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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 6.5MPa；Crude reaction device diameter is 75mm, is highly 1500mm.The load capacity of catalyst accounts for the 5% of raw coal quality. Circulation synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas It is 1.Pyrolysis oven selects bubbling fluidized bed, and reaction temperature is 600 DEG C.Slag-draining device upper diameter, which is classified, with lower section diameter ratio is 7, device is interior to be equipped with ring core baffle.Loop Seal uses U valve.Carbon content is in classification slag-draining device bottom discharge lime-ash 0.32%, granule organics 32kg/m²S exports CH₄Concentration 22.2%, outlet efficiency of carbon con version reach 98.6%, tar Content 6.5%, as a result see Table 2 for details.

[embodiment 10]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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 1500 DEG C, Reaction pressure 2MPa；Crude reaction device diameter is 75mm, is highly 1500mm.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects bubbling fluidized bed, and reaction temperature is 600 DEG C.It is classified slag-draining device upper diameter and lower section diameter ratio is 7, Ring core baffle is equipped in device.Loop Seal uses U valve.Being classified carbon content in slag-draining device bottom discharge lime-ash is 0.14%, Granule organics are 32kg/m²S exports CH₄Concentration 28.9%, outlet efficiency of carbon con version reach 99%, tar content 6.3%.

[embodiment 11]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 4.5.Pyrolysis oven selects bubbling fluidized bed, and reaction temperature is 600 DEG C.Slag-draining device upper diameter, which is classified, with lower section diameter ratio is 7, device is interior to be equipped with ring core baffle.Loop Seal uses U valve.Being classified carbon content in slag-draining device bottom discharge lime-ash is 3.8%, Granule organics are 32kg/m²S exports CH₄Concentration 27.7%, outlet efficiency of carbon con version reach 95.1%, tar content 6.8%.

[embodiment 12]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 2.Pyrolysis oven selects bubbling fluidized bed, and reaction temperature is 600 DEG C.It is classified slag-draining device upper diameter and lower section diameter ratio is 7, Ring core baffle is equipped in device.Loop Seal uses U valve.Being classified carbon content in slag-draining device bottom discharge lime-ash is 2.5%, Grain cycle rate is 32kg/m²S exports CH₄Concentration 24.2%, outlet efficiency of carbon con version reach 96.5%, tar content 6.6%.

[embodiment 13]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects bubbling fluidized bed, and reaction temperature is 700 DEG C.It is classified slag-draining device upper diameter and lower section diameter ratio is 7, Ring core baffle is equipped in device.Loop Seal uses U valve.Being classified carbon content in slag-draining device bottom discharge lime-ash is 0.71%, Granule organics are 32kg/m²S exports CH₄Concentration 21.1%, outlet efficiency of carbon con version reach 98.1%, tar content 6.3%.

[embodiment 14]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects bubbling fluidized bed, and reaction temperature is 500 DEG C.It is classified slag-draining device upper diameter and lower section diameter ratio is 7, Ring core baffle is equipped in device.Loop Seal uses U valve.Being classified carbon content in slag-draining device bottom discharge lime-ash is 1.2%, Grain cycle rate is 32kg/m²S exports CH₄Concentration 20.3%, outlet efficiency of carbon con version reach 97.6%, tar content 6.6%.

[embodiment 15]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 10% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects bubbling fluidized bed, and reaction temperature is 600 DEG C.It is classified slag-draining device upper diameter and lower section diameter ratio is 7, Ring core baffle is equipped in device.Loop Seal uses U valve.Being classified carbon content in slag-draining device bottom discharge lime-ash is 0.37%, Granule organics are 32kg/m²S exports CH₄Concentration 19.9%, outlet efficiency of carbon con version reach 98.5%, tar content 6.6%.

[embodiment 16]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 45% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects bubbling fluidized bed, and reaction temperature is 600 DEG C.It is classified slag-draining device upper diameter and lower section diameter ratio is 7, Ring core baffle is equipped in device.Loop Seal uses U valve.Being classified carbon content in slag-draining device bottom discharge lime-ash is 3.4%, Grain cycle rate is 32kg/m²S exports CH₄Concentration 24.2%, outlet efficiency of carbon con version reach 95.4%, tar content 6.7%.

[embodiment 17]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects Cyclonic reactor, 1 entrance, and inlet angle is 5 °, and reaction temperature is 600 DEG C.It is classified slag-draining device upper section Diameter and lower section diameter ratio are 7, are equipped with ring core baffle in device.Loop Seal uses U valve.It is classified the discharge of slag-draining device bottom Carbon content is 0.53% in lime-ash, granule organics 32kg/m²S exports CH₄Concentration 21.8%, outlet efficiency of carbon con version reach To 98.3%, tar content 6.8%, as a result see Table 3 for details.

[embodiment 18]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects Cyclonic reactor, 1 entrance, and inlet angle is 5 °, and reaction temperature is 600 DEG C.It is classified slag-draining device upper section Diameter and lower section diameter ratio are 7, are equipped with grid baffle in device.Loop Seal uses U valve.It is classified the discharge of slag-draining device bottom Carbon content is 0.7% in lime-ash, granule organics 32kg/m²S exports CH₄Concentration 21.7%, outlet efficiency of carbon con version reach To 98.2%, tar content 6.8%.

[embodiment 19]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects Cyclonic reactor, 1 entrance, and inlet angle is 5 °, and reaction temperature is 600 DEG C.It is classified slag-draining device upper section Diameter and lower section diameter ratio are 7, are equipped with slanting baffle in device.Loop Seal uses U valve.It is classified slag-draining device bottom discharge ash Carbon content is 0.65% in slag, granule organics 32kg/m²S exports CH₄Concentration 21.7%, outlet efficiency of carbon con version reach 98.2%, tar content 6.8%.

[embodiment 20]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects Cyclonic reactor, 1 entrance, and inlet angle is 5 °, and reaction temperature is 600 DEG C.It is classified slag-draining device upper section Diameter and lower section diameter ratio are 7, are equipped with ring core baffle in device.Loop Seal uses U valve.It is classified the discharge of slag-draining device bottom Carbon content is 0.91% in lime-ash, granule organics 32kg/m²S exports CH₄Concentration 21.8%, outlet efficiency of carbon con version reach To 97.9%, tar content 6.5%.

[embodiment 21]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects Cyclonic reactor, 1 entrance, and inlet angle is 5 °, and reaction temperature is 600 DEG C.It is classified slag-draining device upper section Diameter and lower section diameter ratio are 2, are equipped with ring core baffle in device.Loop Seal uses U valve.It is classified the discharge of slag-draining device bottom Carbon content is 0.8% in lime-ash, granule organics 32kg/m²S exports CH₄Concentration 21.8%, outlet efficiency of carbon con version reach To 98%, tar content 6.8%.

[embodiment 22]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects Cyclonic reactor, 1 entrance, and inlet angle is 5 °, and reaction temperature is 600 DEG C.It is classified slag-draining device upper section Diameter and lower section diameter ratio are 10, are equipped with ring core baffle in device.Loop Seal uses U valve.It is classified slag-draining device bottom row Carbon content is 0.55% in lime-ash out, granule organics 32kg/m²S exports CH₄Concentration 21.8% exports efficiency of carbon con version Reach 98.3%, tar content 6.8%.

[embodiment 23]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects Cyclonic reactor, 1 entrance, and inlet angle is 5 °, and reaction temperature is 600 DEG C.It is classified slag-draining device upper section Diameter and lower section diameter ratio are 7, are equipped with ring core baffle in device.Loop Seal uses W valve, the refeed line of W valve, resistance tube with The ratio between caliber and standpipe caliber of inclined tube are 1, and returning charge angle and resistance angle angle are 60 °, and refeed line inflates wind and resistance tube is inflated The ratio between pressure of bottom is less than 1 in the blowing pressure and standpipe of wind.Carbon content is in classification slag-draining device bottom discharge lime-ash 0.55%, granule organics 39kg/m²S exports CH₄Concentration 22.6%, outlet efficiency of carbon con version reach 98.7%, tar Content 7%, as a result see Table 4 for details.

[embodiment 24]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects Cyclonic reactor, 1 entrance, and inlet angle is 5 °, and reaction temperature is 600 DEG C.It is classified slag-draining device upper section Diameter and lower section diameter ratio are 7, are equipped with ring core baffle in device.Loop Seal uses W valve, the refeed line of W valve, resistance tube with The ratio between caliber and standpipe caliber of inclined tube are 0.7, and returning charge angle and resistance angle angle are 60 °, and refeed line inflation wind is filled with resistance tube The ratio between pressure of bottom is less than 1 in the blowing pressure and standpipe of gas wind.Carbon content is in classification slag-draining device bottom discharge lime-ash 0.55%, granule organics 38kg/m²S exports CH₄Concentration 22.4%, outlet efficiency of carbon con version reach 98.6%, tar Content 7%.

[embodiment 25]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects Cyclonic reactor, 1 entrance, and inlet angle is 5 °, and reaction temperature is 600 DEG C.It is classified slag-draining device upper section Diameter and lower section diameter ratio are 7, are equipped with ring core baffle in device.Loop Seal uses W valve, the refeed line of W valve, resistance tube with The ratio between caliber and standpipe caliber of inclined tube are 0.5, and returning charge angle and resistance angle angle are 60 °, and refeed line inflation wind is filled with resistance tube The ratio between pressure of bottom is less than 1 in the blowing pressure and standpipe of gas wind.Carbon content is in classification slag-draining device bottom discharge lime-ash 0.55%, granule organics 36kg/m²S exports CH₄Concentration 22.3%, outlet efficiency of carbon con version reach 98.5%, tar Content 7%.

[embodiment 26]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects Cyclonic reactor, 1 entrance, and inlet angle is 5 °, and reaction temperature is 600 DEG C.It is classified slag-draining device upper section Diameter and lower section diameter ratio are 7, are equipped with ring core baffle in device.Loop Seal uses W valve, the refeed line of W valve, resistance tube with The ratio between caliber and standpipe caliber of inclined tube are 1, and returning charge angle and resistance angle angle are 75 °, and refeed line inflates wind and resistance tube is inflated The ratio between pressure of bottom is less than 1 in the blowing pressure and standpipe of wind.Carbon content is in classification slag-draining device bottom discharge lime-ash 0.55%, granule organics 36kg/m²S exports CH₄Concentration 22.3%, outlet efficiency of carbon con version reach 98.5%, tar Content 7%.

[embodiment 27]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects Cyclonic reactor, 1 entrance, and inlet angle is 5 °, and reaction temperature is 600 DEG C.It is classified slag-draining device upper section Diameter and lower section diameter ratio are 7, are equipped with ring core baffle in device.Loop Seal uses W valve, the refeed line of W valve, resistance tube with The ratio between caliber and standpipe caliber of inclined tube are 1, and returning charge angle and resistance angle angle are 45 °, and refeed line inflates wind and resistance tube is inflated The ratio between pressure of bottom is less than 1 in the blowing pressure and standpipe of wind.Carbon content is in classification slag-draining device bottom discharge lime-ash 0.55%, granule organics 35kg/m²S exports CH₄Concentration 22.1%, outlet efficiency of carbon con version reach 98.5%, tar Content 7%.

[embodiment 28]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects Cyclonic reactor, 1 entrance, and inlet angle is 5 °, and reaction temperature is 600 DEG C.It is classified slag-draining device upper section Diameter and lower section diameter ratio are 7, are equipped with ring core baffle in device.Loop Seal uses W valve, the refeed line of W valve, resistance tube with The ratio between caliber and standpipe caliber of inclined tube are 1, and returning charge angle angle is 60 °, and resistance angle angle is 75 °, and refeed line inflates wind and resistance The ratio between pressure of bottom is less than 1 in the blowing pressure and standpipe of solenoid inflation wind.It is classified carbon in slag-draining device bottom discharge lime-ash Content is 0.55%, granule organics 33kg/m²S exports CH₄Concentration 21.8%, outlet efficiency of carbon con version reach 98.3%, tar content 7%.

[embodiment 29]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects Cyclonic reactor, 1 entrance, and inlet angle is 5 °, and reaction temperature is 600 DEG C.It is classified slag-draining device upper section Diameter and lower section diameter ratio are 7, are equipped with ring core baffle in device.Loop Seal uses W valve, the refeed line of W valve, resistance tube with The ratio between caliber and standpipe caliber of inclined tube are 1, and returning charge angle and resistance angle angle are 60 °, and refeed line inflates wind and resistance tube is inflated The ratio between pressure of bottom is equal to 1 in the blowing pressure and standpipe of wind.Carbon content is in classification slag-draining device bottom discharge lime-ash 0.55%, granule organics 33kg/m²S exports CH₄Concentration 21.9%, outlet efficiency of carbon con version reach 98.3%, tar Content 7%.

[comparative example 1]

Reaction process is as follows: catalyst and carbon raw material are entered in pyrolysis oven by feeding line to be pyrolyzed, tar gas warp Collected after crossing separation, be pyrolyzed back loading catalyst semicoke particle and gasifying agent and oxidant simultaneously with higher linear speed with it is lower Granule density part burning and gasification reaction are carried out in thin reactor.Carbonaceous particles after reacting in thin reactor pass through gas Body is lifted into further gasification reaction in crude reaction device.Raw gas after reaction purifies collection after separation, containing after separation Carbon particle and slag enter in pyrolysis oven as heat carrier, provide heat for the carbon raw material pyrolysis of supported catalyst.

Inner Mongol lignite is selected in experiment, is crushed 2mm 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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects Cyclonic reactor, 1 entrance, and inlet angle is 5 °, and reaction temperature is 600 DEG C.Poly- technology row is melted using ash Slag.Loop Seal uses U valve.It is 2.7% that ash, which melts carbon content in poly- bottom discharge lime-ash, granule organics 30kg/m²· S exports CH₄Concentration 20.5%, outlet efficiency of carbon con version reach 93.2%, and tar content 6.8%, as a result see Table 5 for details.

[comparative example 2]

Inner Mongol lignite is selected in experiment, is crushed 2mm 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.The load capacity of catalyst accounts for the 5% of raw coal quality.It follows Ring synthesis gas tolerance accounts for the 20% of gasification installation exiting syngas total amount, recycles the ratio of hydrogen and carbon monoxide in synthesis gas and is 1.Pyrolysis oven selects Cyclonic reactor, 1 entrance, and inlet angle is 5 °, and reaction temperature is 600 DEG C.Using boiler dry type solid-state Deslagging technique deslagging.Loop Seal uses U valve.It is 7.8% that carbon content in lime-ash, which is discharged, in bottom, granule organics 32kg/ m²S exports CH₄Concentration 21.1%, outlet efficiency of carbon con version reach 89.7%, tar content 6.8%.

[comparative example 3]

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 2.5MPa, and 700 DEG C of operation temperature, gas phase Linear velocity 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 4]

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 2.5MPa, 700 DEG C of operation temperature, gas phase linear velocity 1.2m/s.It is real CO+H in the exit gas component tested₂Content 64%, methane content 14.1%, efficiency of carbon con version 91.7%.

Table 1

Table 2

Table 3

Table 4

Table 5

Claims

1. a kind of combined fluidized bed reaction unit of staged conversion, capital equipment includes: thin reactor (4), crude reaction device (5), heat Furnace (6) and classification slag-draining device (2) are solved, wherein be connected after thin reactor (4) upper end is expanding with crude reaction device (5) bottom, Crude reaction device (5) is connected with pyrolysis oven (6), and pyrolysis oven (6) is connected with thin reactor (4) by the first Loop Seal (9).

2. the combined fluidized bed reaction unit of staged conversion according to claim 1, it is characterised in that the thin reactor (4) Height is 2~8 times of crude reaction device (5) height, and the diameter of the thin reactor (4) is the 1.5~6 of crude reaction device (5) diameter Times.

3. the combined fluidized bed reaction unit of staged conversion according to claim 1, it is characterised in that the classification slag-draining device (2) it is made of the slag-draining device of two sections difference barrel dliameter, the upper section slag-draining device diameter is the 2 of lower section slag-draining device diameter ~10 times.

4. the combined fluidized bed reaction unit of staged conversion according to claim 1, it is characterised in that the classification slag-draining device (2) classification baffle (3) is equipped in, the pattern of classification baffle (3) is perforated baffle, slanting baffle, grid baffle or ring core gear Plate.

5. the combined fluidized bed reaction unit of staged conversion according to claim 1, it is characterised in that first Loop Seal It (9) is loop seal with the second Loop Seal (8), the loop seal pattern is U valve, J valve, L valve or W Valve.

6. the combined fluidized bed reaction unit of staged conversion according to claim 5, it is characterised in that the W valve is by refeed line (12), resistance tube (13), inclined tube (14) and standpipe (15) form；Refeed line (12) bottom is equipped with refeed line inflation wind (I)； Resistance bottom of the tube (13) is equipped with resistance tube inflation wind (H)；The refeed line (12), resistance tube (13) and the caliber of inclined tube (14) are 0.5~1 times of standpipe caliber；The returning charge angle and resistance angle of the W valve are 45 °~75 °, and returning charge angle is greater than or equal to resistance Angle.

7. a kind of combined fluidized bed reaction method of staged conversion is combined using staged conversion any in claim 1~6 and is fluidized Bed reaction device comprises the following steps:

(a), the carbon raw material (E) of supported catalyst enters in pyrolysis oven (6) and is pyrolyzed rapidly, and the pyrolysis gas and semicoke after pyrolysis exist After being separated in pyrolysis oven (6) and cyclone separator (7), coal tar (D) enters follow-up equipment and is purified and separated；

(b), the semicoke after separating flows separately through the first Loop Seal (8) and the second Loop Seal (9), simultaneously with gasifying agent (F) It is mixed and is burnt, gasification reaction into thin reactor (4), the bulky grain slag after reaction contains with what part was not reacted completely Carbon particle enters in classification slag-draining device (2) by valve control, by the bottom of classification slag-draining device (2) after gradation Bulky grain slag is discharged, and the upper end that carbonaceous particles then pass through the thin reactor (4) of top inflow of classification slag-draining device (2) continues to join With react；

(c), the carbonaceous particles in thin reactor (4) after reaction enter in crude reaction device (5) by gas lift and further gasify Reaction；Raw gas (G) after reaction purifies collection after separation, and the carbonaceous particles after separation enter pyrolysis as heat carrier with slag In furnace (6), heat is provided for carbon raw material (E) pyrolysis of supported catalyst.

8. the combined fluidized bed reaction method of staged conversion according to claim 7, it is characterised in that the carbon raw material choosing From at least one of coal, petroleum coke, biomass, the gasifying agent is selected from oxygen, air, liquid water, vapor, carbon dioxide Or at least one of hydrogen.

9. the combined fluidized bed reaction method of staged conversion according to claim 7, 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.

10. the combined fluidized bed reaction method of staged conversion according to claim 7, it is characterised in that the thin reactor (4) reaction condition are as follows: 0~6.5MPa of reaction pressure, 800~1300 DEG C of reaction temperature, gas phase 2.0~15.0m/s of linear velocity, Fluidised form in the thin reactor (4) is fast fluidization；The reaction condition of the crude reaction device (5) are as follows: reaction pressure 0~ 6.5MPa, 600~1000 DEG C of reaction temperature, 0.1~1.0m/s of gas phase linear velocity, the fluidised form in the crude reaction device (5) are rapids Dynamic fluidization or bubbling fluidization；Operation temperature in the pyrolysis oven (6) is 100-300 DEG C lower than the temperature in crude reaction device； Gas phase linear velocity is 0.8~3m/s in the interior lower section cylinder of classification slag-draining device (2), and gas phase linear velocity is in upper section cylinder 0.1~0.3m/s；Refeed line inflation wind (I) of refeed line (12) bottom and resistance tube (13) bottom are equipped with resistance in the W valve The blowing pressure that pipe inflates wind (H) is less than or equal to the pressure of standpipe (15) interior bottom.