CN107099319A - The device and method of methane rich synthesis gas and light tar is produced in a kind of synchronization - Google Patents

The device and method of methane rich synthesis gas and light tar is produced in a kind of synchronization Download PDF

Info

Publication number
CN107099319A
CN107099319A CN201710388522.7A CN201710388522A CN107099319A CN 107099319 A CN107099319 A CN 107099319A CN 201710388522 A CN201710388522 A CN 201710388522A CN 107099319 A CN107099319 A CN 107099319A
Authority
CN
China
Prior art keywords
subsystem
particle
gas
coal
synthesis gas
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
CN201710388522.7A
Other languages
Chinese (zh)
Other versions
CN107099319B (en
Inventor
李大鹏
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Individual
Original Assignee
Individual
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Individual filed Critical Individual
Priority to CN201710388522.7A priority Critical patent/CN107099319B/en
Publication of CN107099319A publication Critical patent/CN107099319A/en
Application granted granted Critical
Publication of CN107099319B publication Critical patent/CN107099319B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
    • B01D53/228—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion characterised by specific membranes
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C9/00—Aliphatic saturated hydrocarbons
    • C07C9/02—Aliphatic saturated hydrocarbons with one to four carbon atoms
    • C07C9/04—Methane
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
    • C10G1/086—Characterised by the catalyst used
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/32—Purifying combustible gases containing carbon monoxide with selectively adsorptive solids, e.g. active carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/702—Hydrocarbons
    • B01D2257/7022—Aliphatic hydrocarbons
    • B01D2257/7025—Methane
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1011—Biomass
    • 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
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/20—Capture or disposal of greenhouse gases of methane
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Combustion & Propulsion (AREA)
  • Materials Engineering (AREA)
  • Analytical Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The device and method of methane rich synthesis gas and light tar is produced in a kind of synchronization, the present invention can by biomass, low-rank coal, petroleum coke, oil shale etc. one or two kinds of above according to reaction mass the mixed material that constitutes in specific proportions of carbon hydrogen element balance as charging, feed 0.1~1mm of particle size range, the methane rich synthesis gas composition that device is produced is CO 15~30vol%, H220~40vol%CH48~35vol%, CmHn0.1~0.2vol%CO28~12vol%, N22~4vol%.Above all, while methane rich synthesis gas is produced, coalite tar in 15wt%~20wt% high-quality can also be obtained, this part coal tar can be changed into the higher high-grade fuel oil product of added value, aromatic hydrocarbons, a variety of added values very high coal base fine chemical product after deep processing, significantly strengthen the economic competitiveness of coal gas, on the basis of efficient coal resources, step, comprehensive utilization is realized, the coupling of natural gas from coal and coal base Fine Chemical Industry interchain is realized.

Description

The device and method of methane rich synthesis gas and light tar is produced in a kind of synchronization
Technical field
The present invention relates to the high-efficiency cleaning trans-utilization of carbon raw material, natural gas from coal technical field, and in particular to a kind of Carbon hydrogen element by the one or two kinds of in biomass, low-rank coal, petroleum coke, oil shale above according to reaction mass is balanced The mixing carbonaceous material mixed in specific proportions synchronously produces the device and method of methane rich synthesis gas and light tar.
Background technology
The scattered burning of coal burning, especially colm, is the main cause for causing the current coal-burning atmosphere pollution of China, It is sulfate, nitrate, PM in haze2.5One of important sources Deng pollutant.In the current Coal Consumption Structure of China, About 20% is used for Industrial Boiler and the scattered burning of life.The main body for dissipating coal consumption is small-sized cement factory, glass factory, steel mill and residential households Heating, these dissipate coal consumption and all do not install dedusting, desulphurization and denitration device substantially.Solve caused by the current consumption of coal of China Haze pollution problem, except depending on science and technology, Efficient Conversion and the clean utilization of coal are carried forward vigorously in innovation, are increased and are dissipated coal cleaning Change beyond management, should also reduce the scattered direct burning of coal, using the industrially desulfurized of maturation, denitration, dedusting technology, carry out The concentrated combustion and conversion of coal.Natural gas from coal is to belong to coal to concentrate one of path of Efficient Conversion, is also to realize coal The important technology that fuel feedstocksization change gas with Industrial Boiler coal is supported, and its production process efficiency is higher than coal liquifaction, ammonia from coal, coal The processes such as preparing dimethy ether.Natural gas from coal is, using coal as raw material, synthetic natural gas to be produced using gasification, purification and methanation technology Process, for the low-carbon of the coal that occupies China's production of energy and main body of consumption, clean using providing one effectively on the way Footpath；By supplying the natural gas of cleaning to target market, the extensive intensive utilization of coal of project location, by coal The products such as sulphur, nitrogen etc. cause the main matter of atmosphere pollution to trap and be converted into sulphur, ammoniacal liquor, realize recycling. Natural gas from coal can alleviate the atmosphere polluting problem in " haze besieged city " to a certain extent, to ensureing national energy security, increase Substitute gas, realize coal high-efficiency clean utilization, reduction environmental pollution it is significant.
Shown according to National Development and Reform Committee's latest data, the annual gas production of China in 2016 is about 1371 billion cubic meters, together Than increasing by 1.5%；The billion cubic meter of Imported gas amount 720, increases by 17.4%；The billion cubic meter of Natural Gas Consumption Using 2090, increases 6.6%.Natural gas external dependence degree is up to 34.44%, up to now, natural gas from coal industrial technology comparative maturity, the world On have many set coal gas industrial production devices in stable operation.Therefore development natural gas from coal industry is effective supplement China stone Oil, natural gas resource are not enough, ensure the important channel of national energy security, are beneficial to alleviate China's natural gas imbalance between supply and demand, Promote the balanced development of social economy.
The first step of conventional coal gas flow is identical with ammonia from coal and coal synthesis ammonia flow, is all first to carry out coal gasification Synthesis gas is produced, purified treatment is then carried out.Unlike, coal gas flow wishes in purified gas methane content, and the higher the better, It so can both reduce the operating load of second step methanation device and also allow for controlling unit scale and the throwing of synthesis gas methanation Cost is provided, ammonia from coal then requires that methane is more low better in purified gas with synthesis ammonia.And the selection of coal gas front end gasification process There is material impact to economy such as project overall investment intensity, operating costs.Up to now, natural gas from coal is used Gasification process is mostly crushed coal pressure gasifying technology, because compared with crushed coal pressure gasifying technology, conventional fine coal gasification process, Coal-water slurry gasification because in the synthesis gas produced by it methane content it is too low, as natural gas from coal gasification process simultaneously Without clear superiority.Typical crushed coal pressure gasifying is Lurgi crushed coal pressure gasifyings technology, BGL broken coal slag gasification technologies, Methane content highest (7vol%~12.5vol%) in the raw gas of Lurgi crushed coal pressure gasifyings technology generation, BGL broken coals melt The raw gas methane content of slag gasification technology takes second place (6.2vol%).But Lurgi gasification technologies, BGL gasification technologies are applicable Be all 5~50mm lump coal, and based on current machine excavating technology, directly as the feed coal accounting of above two gasification process Less than 30%, coal machine a large amount of fine coal resources produced during adopting can not be utilized.Therefore existing natural gas from coal gasification There is the short slab of coal blending in technique.In addition, in both technique institute production of synthetic gas CO volume fractions be 25vol%~ 56vol%, H2Volume fraction is 20vol%~35vol%, H2/ CO ratios only 0.6~0.8, and existing synthesis gas methanation Reaction is required to H in unstripped gas2/ CO ratios are more than 2, by reacting condition most of CO need to be adjusted into H2/ CO ratios.In addition, BGL Gasification technology, Lurgi crushed coal pressure gasifying technology list covering devices coal feeding amount only be respectively 950t/d, 1200t/d, unit scale compared with It is small, cause its specific investment intensity too high, especially BGL techniques also use slag tap, it is necessary to substantial amounts of chilled water (chw), two kinds of gas Chemical industry skill can also produce a large amount of very intractable waste water, and tail end wastewater intractability and cost are all very high.Therefore, for existing coal For process for producing natural, need that methane concentration in a kind of synthesis gas of exploitation is high, coal feeding amount is big, waste water yield is small, raw material is fitted badly H in Ying Xingqiang, synthesis gas2/ C ratios are big, and the dry cinder discharging gasification process by raw material of fine coal.Patent of invention dry quenching co-production coal The method (A of CN 101747918) of preparing natural gas is disclosed in a kind of process of coking with cold coal and its pyrolytic process absorption high temperature The coke cooling means of coke heat energy there is provided a kind of method of preparing natural gas by dry quenching co-production coal, using reducibility gas as Heat-carrying gas, absorb high-temperature coke heat energy, high-temperature coke are cooled down, and by absorbing, high temperature heat-carrying gas and coal charge after heat energy are direct Contact heat-exchanging, rises mild pyrolysis with coal and reclaims heat, by high-temperature coke quenching process and pyrolysis of coal PROCESS COUPLING, generation pyrolysis half Burnt and pyrolysis coal gas, on the basis of above-mentioned dry coke quenching and the method for pyrolysis of coal, further using water vapour and oxygen gasified heat Solve semicoke generation gasification gas, then by gasification gas with pyrolysis coal gas gaseous mixture it is transformed and purify for methanation reaction life Into natural gas.Although it is anti-that the process also carries out methanation with gasification gas gaseous mixture using pyrolysis coal gas as unstripped gas Should, but still have semicoke generation in technology, and belong to high temperature pyrolysis, produce heavy component in tar it is more, with height BTX and the PCX constituent content of added value are less.
The content of the invention
It is an object of the invention to provide one kind while coalite tar during fine coal pressurization fast pyrogenation produces high-quality Produce high concentration and be rich in methane synthesis gas, realize that the cascade utilization of coal resources, the synchronization of high-efficiency cleaning conversion produce methane rich The device and method of synthesis gas and light tar.
To reach above-mentioned purpose, the inventive system comprises carbonaceous material fast pyrolysis reaction system and with its entrance Connected continuous pressure stable state feed system, the purified synthesis gas and particle separate system, purified synthesis gas being connected are exported with it Outlet with particle separate system is connected with light tar recovery system, methane-rich piece-rate system successively；
Described carbonaceous material heat scission reaction system includes the circulating granular second pyrolysis system being sequentially connected from bottom to top Hydrogen subsystem, quick mixing heating subsystem, carbonaceous material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis reaction subsystem；
Described purified synthesis gas and particle separate system include high-temperature dry isolated subsystem, the synthesis gas being sequentially connected Deep purifying subsystem, particle screening subsystem and external particle cycle subsystem, described high-temperature dry isolated subsystem with The syngas outlet of carbonaceous material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis reaction subsystem is connected, external particle circulation The carbonaceous particles of system trapping are recycled back into circulating granular second pyrolysis hydrogen manufacturing subsystem；
Described light tar recovery system includes oil gas adsorbing separation subsystem, the light oil separating-purifying being sequentially connected Subsystem and light tar storage subsystem；
Described methane-rich piece-rate system includes methane separation and purifies subsystem and methane boosting storage subsystem, described Methane separation purification subsystem be connected with the syngas outlet of light oil separating-purifying subsystem.
Described continuous pressure stable state feed system includes the raw material warehouse, controllable feed pulverizer, one being sequentially connected Formula circulation gas dryer, feed surge device and mechanical strength manifold type fine coal charging gear, described mechanical strength manifold type powder Coal charging gear is connected with the entrance of carbonaceous material fast pyrolysis reaction system.
Trapping is also equipped with described carbonaceous material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis reaction subsystem not The built-in particle cycle subsystem of carbon containing inert particle, the built-in particle cycle subsystem is by the inert particle of trapping again by many The built-in circulation revert system of path is recycled back into quick mixing heating subsystem and circulating granular second pyrolysis hydrogen manufacturing subsystem respectively The total thermal capacitance of bed and bed density united to regulate and control two subsystems.
Described circulating granular second pyrolysis hydrogen manufacturing subsystem include set gradually from bottom to top particle heating region of activation, Primary pyrolysis reaction zone and deep pyrolytic reaction zone, described particle heating region of activation respectively with external particle cycle subsystem and Built-in particle cycle subsystem is connected.
The hydrogen-rich high temperature gas-solid fluid-mixing that described quick mixing heating subsystem includes setting gradually from bottom to top is whole Flow area, vortex flow field transmission region, fluid-mixing temperature controlled region, described hydrogen-rich high temperature gas-solid fluid-mixing commutating zone and circulation The deep pyrolytic reaction zone of grain second pyrolysis hydrogen manufacturing subsystem is connected, fluid-mixing temperature controlled region and carbonaceous material constant temperature-pressurization- Catalytic hydrogenation fast pyrolysis reaction subsystem is connected.
Described oil gas adsorbing separation subsystem is provided with by high adsorption activity molecular sieve, modified graft polymer material, alkane The adsorption stuffing bed that base benzene series copolymer fibre is constituted.
The operating pressure of described carbonaceous material fast pyrolysis reaction system is 3.0~5.0MPa, and reaction temperature is 950 ~1200 DEG C.
Described quick mixing heating subsystem passes through local jet configuration and 50~300 high-temperature heat carrier circulating ratio institutes The 10-20MJ/m of offer2S heat flux, 103~105DEG C/s heating rate under, in 1~10ms that fresh feed is quick It is heated to 500~700 DEG C of reaction temperature.
Described methane separation purification subsystem uses CH4Concentration and separation material is with high intensity, high flux macromolecule sieve membrane With flexible MOFs composites, porous active carbon fiber, activated alumina, carbon molecular sieve, the hollow fibre of high molecular polymer The classification enrichment the membrane module more than one or two kinds of in dimension film assembled.
The present invention synchronously produces methane rich synthesis gas and the method for light tar comprises the following steps：
First, the feed coal in raw material warehouse is successively via controllable feed pulverizer, integrated circular gas dryer institute group Into stock preparation system prepare the drying coal dust that 10~1000 μm of particle size range and moisture content are less than 2.0wt%, prepare and close The fresh coal dust of lattice enters feed surge device and enters the fast speed heat of carbonaceous material by mechanical strength manifold type fine coal charging gear again Quick mixing heating subsystem in cracking reaction system, with self-loopa particle second pyrolysis in quick mixing heating subsystem Hydrogen manufacturing subsystem and come high temperature gas-solid mixing heat carrier be under 50~300 times of Solids Circulation Rates 1-10ms when In instantaneously exchanged heat, pulverized coal particle be heated to after 500~700 DEG C of pyrolysis temperature be advanced into carbonaceous material constant temperature-add Pressure-catalytic hydrogenation fast pyrolysis reaction subsystem, afterwards under 3.0~5.0MPa pressure conditions in completing quick fine coal in 2s Fast pyrogenation reacts, the CH containing high concentration produced by fast pyrogenation reaction4、CO、H2, tar steam, rich carbon particle, inert particle Thermal decomposition product etc. component enters back into purified synthesis gas and particle separate system and carries out product cleanup and separates, and carbonaceous material constant temperature- Particle size range exists in gas-solid fluid-mixing in pressurization-catalytic hydrogenation fast pyrolysis reaction subsystem produced by pulverized coal pyrolysis 50 μm~600 μm of not carbon containing inert particle is captured in built-in particle cycle subsystem, and the inert particle of trapping passes through again The built-in circulation revert system of multi-path is recycled back into quick mixing heating subsystem and circulating granular second pyrolysis hydrogen manufacturing respectively System is to the total thermal capacitance of bed and bed density that regulate and control two subsystems；
Then, after preliminary purification i.e. from built-in particle cycle subsystem escape 70~75wt% of fixation carbon content and The synthesis gas of the rich carbon particle of the sub-micron of the μ m of particle diameter 0.1~50, micron order enters purified synthesis gas and particle shunting is System, passes sequentially through high-temperature dry isolated subsystem, synthesis gas deep purifying subsystem, particle screening subsystem, external particle and follows Cross section of fluid channel gradual change type double-cyclone gas-solid point constructed by coupled modes of the loop subsystems in aerodynamics and mechanical grading principle In the presence of device, efficiently separated with gas phase, and be recycled back into circulating granular second pyrolysis hydrogen manufacturing subsystem, pass sequentially through particle Heat up region of activation, primary pyrolysis reaction zone, deep pyrolytic reaction zone, final to produce hydrogen-rich crude synthesis gas, the height produced with reaction Warm inorganic particle constitutes high temperature, hydrogen-rich, gas-solid two-phase mixtures heat carrier together, is above advanced into quick mixing heating subsystem, according to It is secondary by hydrogen-rich high temperature gas-solid fluid-mixing commutating zone, vortex flow field transmission region, fluid-mixing temperature controlled region, instantaneously by fine coal Grain is heated to predetermined pyrolysis temperature；
Finally, purified synthesis gas enters back into the light tar in downstream with the decontaminating syngas that particle separate system is exported Recovery system, passes sequentially through the coal tar oil ingredient in oil gas adsorbing separation subsystem, light oil separating-purifying subsystem recovery gas phase, Coalite tar enters light tar storage subsystem in final acquired liquid lightweight, reclaims the purification of gained after oil product Methane rich synthesis gas enters back into methane-rich piece-rate system, passes sequentially through methane separation purification subsystem, methane boosting storage System, finally enters methane storage tank.
Compared with the gasification process that existing natural gas from coal technique matches, the present invention can by biomass, low-rank coal, The one or two kinds of of petroleum coke, oil shale etc. is above according to mixing that the carbon hydrogen element balance of reaction mass is constituted in specific proportions Compound material feeds 0.1~1mm of particle size range as charging, the methane rich synthesis gas composition that device is produced for CO 15~ 30vol%, H220~40vol%CH48~35vol%, CmHn0.1~0.2vol%CO28~12vol%, N22~ 4vol%.Most of all, while methane rich synthesis gas is produced, can also obtain low temperature in 15wt%~20wt% high-quality Coal tar, this part coal tar can be changed into the higher high-grade fuel oil product of added value after deep processing, aromatic hydrocarbons, a variety of additional Value very high coal base fine chemical product, significantly strengthens the economic competitiveness of coal gas, realize coal resources efficiently, step, On the basis of comprehensive utilization, the coupling of natural gas from coal and coal base Fine Chemical Industry interchain is realized.
Compared with the supporting gasification process of existing natural gas from coal, the present invention has following advantage：
1) using fine coal as raw material, by the Fast retrieval of fine coal, synchronous production methane rich synthesis gas and high-quality are realized Methane concentration is up to 25~55vol% in middle coalite tar, the synthesis gas of generation, higher than existing crushed coal pressure gasifying technology Methane concentration in produced crude synthesis gas, is greatly reduced follow-up methanation device scale and investment；
2) H in the crude synthesis gas produced by2/ C ratios are higher than 2.0, without improving H by transformationreation again2/ C ratios；
3) high income of light tar, can be with downstream up to 15~20wt% in technology system disclosed in this invention Coal tar deep processing industrial chain height coupling integration, greatly improve the macroeconomic competitiveness of process system；
4) dust concentration is extremely low in institute's production of synthetic gas, total carbon high conversion rate, and unit scale and operating flexibility are big, are easy to engineering Change application；
5) diversification of device raw material is realized, both can be using lower-grade metamorphic bituminous, lignite as raw material, can also biomass, low The one or two kinds of of rank coal, petroleum coke, oil shale etc. is balanced in specific proportions above according to the carbon hydrogen element of reaction mass The mixed material of composition, device charging strong adaptability.
Brief description of the drawings
Fig. 1 is device and schematic flow sheet of the invention.
In figure：1. continuous pressure stable state feed system；2. carbonaceous material fast pyrolysis reaction system；3. purified synthesis gas With particle separate system；4. light tar recovery system；5. methane-rich piece-rate system；6. raw material warehouse；7. controllable charging Grinder；8. integrated circular gas dryer；9. feed surge device；10. mechanical strength manifold type fine coal charging gear；11. follow Ring particle second pyrolysis hydrogen manufacturing subsystem；12. built in particle cycle subsystem；13. quick mixing heating subsystem；14. it is carbon containing Material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis reacts subsystem；15. high-temperature dry isolated subsystem；16. synthesis gas is deep Spend purifying subsystem；17. particle screening subsystem；18. external particle cycle subsystem；19. oil gas adsorbing separation subsystem； 20. light oil separating-purifying subsystem；21. light tar storage subsystem；22. methane separation purifies subsystem；23. methane liter Press storage subsystem；24. deep pyrolytic reaction zone；25. primary pyrolysis reaction zone；The region of activation 26. particle heats up；27. mixed flow Body temperature controlled region；28. vortex flow field transmission region；29. hydrogen-rich high temperature gas-solid fluid-mixing commutating zone.
Embodiment
In order that technical scheme and advantage are more clear apparent, below in conjunction with the accompanying drawings and embodiment, to this hair Bright device and method is further elaborated.
Referring to Fig. 1, the present invention includes carbonaceous material fast pyrolysis reaction system 2 and continuous adding of being connected with its entrance Stable state feed system 1 is pressed, the purified synthesis gas and particle separate system 3 being connected are exported with it, purified synthesis gas is shunted with particle The outlet of system 3 is connected with light tar recovery system 4, methane-rich piece-rate system 5 successively；
Described carbonaceous material heat scission reaction system 2 includes the circulating granular second pyrolysis system being sequentially connected from bottom to top Hydrogen subsystem 11, quick mixing heating subsystem 13, carbonaceous material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis reaction subsystem System 14；
Described purified synthesis gas and particle separate system 3 include high-temperature dry isolated subsystem 15, the conjunction being sequentially connected Into gas deep purifying subsystem 16, particle screening subsystem 17 and external particle cycle subsystem 18, described high-temperature dry point The syngas outlet that ion system 15 reacts subsystem 14 with carbonaceous material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis is connected, The carbonaceous particles that external particle cycle subsystem 18 is trapped are recycled back into circulating granular second pyrolysis hydrogen manufacturing subsystem 11；
Described light tar recovery system 4 includes oil gas adsorbing separation subsystem 19, the light oil separation being sequentially connected Purify subsystem 20 and light tar storage subsystem 21；
Described methane-rich piece-rate system 5 includes methane separation and purifies subsystem 22 and methane boosting storage subsystem 23, described methane separation purification subsystem 22 is connected with the syngas outlet of light oil separating-purifying subsystem 20.
Described continuous pressure stable state feed system 1 includes raw material warehouse 6, the controllable feed pulverizer 7, one being sequentially connected Body formula circulation gas dryer 8, feed surge device 9 and mechanical strength manifold type fine coal charging gear 10, described mechanical strength coupling Box-like fine coal charging gear 10 is connected with the entrance of carbonaceous material fast pyrolysis reaction system 2.
Trapping is also equipped with described carbonaceous material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis reaction subsystem 14 The built-in particle cycle subsystem 12 of not carbon containing inert particle, the built-in particle cycle subsystem 12 by 50 μm of the particle diameter of trapping~ The inert particle of 600 μm of levels is recycled back into quick mixing heating subsystem 13 respectively by circulating revert system built in multi-path again And bed total thermal capacitance and bed density of the circulating granular second pyrolysis hydrogen manufacturing subsystem 11 to regulate and control two subsystems.
Described circulating granular second pyrolysis hydrogen manufacturing subsystem 11 includes the particle heating activation set gradually from bottom to top Area 26, primary pyrolysis reaction zone 25 and deep pyrolytic reaction zone 24, described particle heating region of activation 26 respectively with external particle Cycle subsystem 18 and built-in particle cycle subsystem 12 are connected.
Described quick mixing heating subsystem 13 includes the hydrogen-rich high temperature gas-solid fluid-mixing set gradually from bottom to top Commutating zone 29, vortex flow field transmission region 28, fluid-mixing temperature controlled region 27, described hydrogen-rich high temperature gas-solid fluid-mixing commutating zone 29 are connected with the deep pyrolytic reaction zone 24 of circulating granular second pyrolysis hydrogen manufacturing subsystem 11, and fluid-mixing temperature controlled region 27 is with containing Carbon material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis reaction subsystem 14 is connected.
Described oil gas adsorbing separation subsystem 19 be provided with by high adsorption activity molecular sieve, modified graft polymer material, The adsorption stuffing bed that alkylbenzene system copolymer fibre is constituted.
The operating pressure of described carbonaceous material fast pyrolysis reaction system 2 is 3.0~5.0MPa, and reaction temperature is 950~1200 DEG C.
Described quick mixing heating subsystem 13 passes through local jet configuration and 50~300 high-temperature heat carrier circulating ratios The 10-20MJ/m provided2S heat flux, 103~105DEG C/s heating rate under, in 1~10ms that fresh feed is fast Speed is heated to 500~700 DEG C of reaction temperature.
Described methane separation purification subsystem 22 uses CH4Concentration and separation material is sieved with high intensity, high flux macromolecule Film and flexibility MOFs composites, porous active carbon fiber, activated alumina, carbon molecular sieve, high molecular polymer are hollow The classification enrichment the membrane module more than one or two kinds of in tunica fibrosa assembled.
Described particle screening subsystem 17 by the pressure field constructed by inner flow passage configuration, speed field gradient distribution come Realize the inert particle of 50~600 μm of particle size range and 60~80wt% of fixed carbon content, 50 μm of particle diameter ＜ rich carbon particle Classification, segmentation, classification loop returning charge.
The method of the present invention is as follows:
First, the feed coal in raw material warehouse 6 is successively via controllable feed pulverizer 7, the institute of integrated circular gas dryer 8 The stock preparation system of composition prepares 10~1000 μm of particle size range and moisture content is less than 2.0wt% drying coal dust, prepares It is fast into carbonaceous material by mechanical strength manifold type fine coal charging gear 10 again that qualified fresh coal dust enters feed surge device 9 Quick mixing heating subsystem 13 in speed heat cracking reaction system 2, with self-loopa in quick mixing heating subsystem 13 Grain second pyrolysis hydrogen manufacturing subsystem 11 and the high temperature gas-solid mixing heat carrier that comes under 50~300 times of Solids Circulation Rates In instantaneously being exchanged heat in 1-10ms time, pulverized coal particle be heated to after 500~700 DEG C of pyrolysis temperature be advanced into it is carbon containing Material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis reacts subsystem 14, afterwards in 2s under 3.0~5.0MPa pressure conditions It is interior to complete quick fine coal fast pyrogenation reaction, the CH containing high concentration produced by fast pyrogenation reaction4、CO、H2, tar steam, rich carbon The thermal decomposition product of the components such as particle, inert particle enters back into purified synthesis gas and separated with the progress product cleanup of particle separate system 3, Gas-solid mixed flow in carbonaceous material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis reaction subsystem 14 produced by pulverized coal pyrolysis Particle size range is captured in 50 μm~600 μm of not carbon containing inert particle in built-in particle cycle subsystem 12 in body, trapping Inert particle be recycled back into quick mixing heating subsystem 13 and circulation respectively by circulating revert system built in multi-path again Bed total thermal capacitance and bed density of the particle second pyrolysis hydrogen manufacturing subsystem 11 to regulate and control two subsystems；
Then, the 70~75wt% of fixation carbon content escaped after preliminary purification from built-in particle cycle subsystem 12 And the synthesis gas of the rich carbon particle of the sub-micron of the μ m of particle diameter 0.1~50, micron order enters purified synthesis gas and particle shunting System 3, passes sequentially through high-temperature dry isolated subsystem 15, synthesis gas deep purifying subsystem 16, particle screening subsystem 17, outer The cross section of fluid channel gradual change type put constructed by coupled modes of the particle cycle subsystem 18 in aerodynamics and mechanical grading principle is double In the presence of eddy flow gas-solid separator, efficiently separated with gas phase, and be recycled back into circulating granular second pyrolysis hydrogen manufacturing subsystem 11, Particle heating region of activation 26, primary pyrolysis reaction zone 25, deep pyrolytic reaction zone 24 are passed sequentially through, the final hydrogen-rich that produces slightly is synthesized Gas, high temperature, hydrogen-rich, gas-solid two-phase mixtures heat carrier are constituted together with the high temperature inorganic particle that reaction is produced, and are above advanced into quick Mixing heating subsystem 13, passes sequentially through hydrogen-rich high temperature gas-solid fluid-mixing commutating zone 29, vortex flow field transmission region 28, mixing Fluid temperature controlled region 27, is instantaneously heated to predetermined pyrolysis temperature by pulverized coal particle；
Finally, purified synthesis gas enters back into the lightweight coal tar in downstream with the decontaminating syngas that particle separate system 3 is exported Oil recovery system 4, passes sequentially through the coal tar in oil gas adsorbing separation subsystem 19, the recovery gas phase of light oil separating-purifying subsystem 20 Coalite tar enters light tar storage subsystem 21 in oil ingredient, final acquired liquid lightweight, reclaims after oil product The purification methane rich synthesis gas of gained enters back into methane-rich piece-rate system 5, passes sequentially through methane separation purification subsystem 22, first Alkane boosting storage subsystem (23, finally enter methane storage tank.

Claims (10)

1. the device of methane rich synthesis gas and light tar is produced in a kind of synchronization, it is characterised in that quick including carbonaceous material Heat scission reaction system (2) and the continuous pressure stable state feed system (1) being connected with its entrance, the synthesis being connected is exported with it Gas is purified to be reclaimed with light tar successively with particle separate system (3), the outlet of purified synthesis gas and particle separate system (3) System (4), methane-rich piece-rate system (5) are connected；
Described carbonaceous material heat scission reaction system (2) includes the circulating granular second pyrolysis hydrogen manufacturing being sequentially connected from bottom to top Subsystem (11), quick mixing heating subsystem (13), carbonaceous material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis reaction System (14)；
Described purified synthesis gas and particle separate system (3) include high-temperature dry isolated subsystem (15), the conjunction being sequentially connected Into gas deep purifying subsystem (16), particle screening subsystem (17) and external particle cycle subsystem (18), described high temperature Dry method isolated subsystem (15) reacts the synthesis of subsystem (14) with carbonaceous material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis Gas outlet is connected, and the carbonaceous particles of external particle cycle subsystem (18) trapping are recycled back into circulating granular second pyrolysis hydrogen manufacturing System (11)；
Described light tar recovery system (4) includes oil gas adsorbing separation subsystem (19), the light oil separation being sequentially connected Purify subsystem (20) and light tar storage subsystem (21)；
Described methane-rich piece-rate system (5) includes methane separation purification subsystem (22) and methane boosting storage subsystem (23), described methane separation purification subsystem (22) is connected with the syngas outlet of light oil separating-purifying subsystem (20).
2. the device of methane rich synthesis gas and light tar is produced in synchronization according to claim 1, it is characterised in that institute The continuous pressure stable state feed system (1) stated includes the raw material warehouse (6), controllable feed pulverizer (7), integral type being sequentially connected Circulate gas dryer (8), feed surge device (9) and mechanical strength manifold type fine coal charging gear (10), described mechanical strength Manifold type fine coal charging gear (10) is connected with the entrance of carbonaceous material fast pyrolysis reaction system (2).
3. the device of methane rich synthesis gas and light tar is produced in synchronization according to claim 1, it is characterised in that institute It is not carbon containing lazy that trapping is also equipped with the carbonaceous material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis reaction subsystem (14) stated The built-in particle cycle subsystem (12) of property particle, the built-in particle cycle subsystem (12) passes through the inert particle of trapping again The built-in circulation revert system of multi-path is recycled back into quick mixing heating subsystem (13) and circulating granular second pyrolysis system respectively Hydrogen subsystem (11) is to the total thermal capacitance of bed and bed density that regulate and control two subsystems.
4. the device of methane rich synthesis gas and light tar is produced in the synchronization according to claim 1 or 3, its feature exists In described circulating granular second pyrolysis hydrogen manufacturing subsystem (11) includes the particle heating region of activation set gradually from bottom to top (26), primary pyrolysis reaction zone (25) and deep pyrolytic reaction zone (24), described particle heat up region of activation (26) respectively with outside Put particle cycle subsystem (18) and built-in particle cycle subsystem (12) is connected.
5. the device of methane rich synthesis gas and light tar is produced in synchronization according to claim 1, it is characterised in that institute The quick mixing heating subsystem (13) stated includes the hydrogen-rich high temperature gas-solid fluid-mixing commutating zone set gradually from bottom to top (29), vortex flow field transmission region (28), fluid-mixing temperature controlled region (27), described hydrogen-rich high temperature gas-solid fluid-mixing commutating zone (29) it is connected with the deep pyrolytic reaction zone (24) of circulating granular second pyrolysis hydrogen manufacturing subsystem (11), fluid-mixing temperature controlled region (27) it is connected with carbonaceous material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis reaction subsystem (14).
6. the device of methane rich synthesis gas and light tar is produced in synchronization according to claim 1, it is characterised in that institute The oil gas adsorbing separation subsystem (19) stated is provided with by high adsorption activity molecular sieve, modified graft polymer material, alkyl benzene series The adsorption stuffing bed that copolymer fibre is constituted.
7. the device of methane rich synthesis gas and light tar is produced in synchronization according to claim 1, it is characterised in that institute The operating pressure for the carbonaceous material fast pyrolysis reaction system (2) stated is 3.0~5.0MPa, and reaction temperature is 950~1200 ℃。
8. the device of methane rich synthesis gas and light tar is produced in synchronization according to claim 1, it is characterised in that institute What the quick mixing heating subsystem (13) stated was provided by local jet configuration and 50~300 high-temperature heat carrier circulating ratios 10-20MJ/m2S heat flux, 103~105DEG C/s heating rate under, in fresh feed is quickly heated up in 1~10ms 500~700 DEG C of reaction temperature.
9. the device of methane rich synthesis gas and light tar is produced in synchronization according to claim 1, it is characterised in that institute The methane separation purification subsystem (22) stated uses CH4Concentration and separation material is with high intensity, high flux macromolecule sieve membrane and flexibility In MOFs composites, porous active carbon fiber, activated alumina, carbon molecular sieve, high molecular polymer hollow-fibre membrane One or two kinds of more than assembled classification enrichment membrane module.
10. a kind of method that methane rich synthesis gas and light tar are produced in synchronization, it is characterised in that：
First, the feed coal in raw material warehouse (6) is successively via controllable feed pulverizer (7), integrated circular gas dryer (8) The stock preparation system constituted prepares 10~1000 μm of particle size range and moisture content is less than 2.0wt% drying coal dust, system Standby qualified fresh coal dust enters feed surge device (9) and enters carbon containing by mechanical strength manifold type fine coal charging gear (10) again Quick mixing heating subsystem (13) in material fast pyrolysis reaction system (2), in quick mixing heating subsystem (13) In with self-loopa particle second pyrolysis hydrogen manufacturing subsystem (11) and of the high temperature gas-solid mixing heat carrier at 50~300 times that comes It is instantaneously to be exchanged heat in 1~10ms time under grain circulating ratio, pulverized coal particle is heated to pyrolysis temperature 500~700 Carbonaceous material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis reaction subsystem (14) is advanced on after DEG C, afterwards 3.0~ In completing quick fine coal fast pyrogenation reaction in 2s under 5.0MPa pressure conditions, contain high concentration produced by fast pyrogenation reaction CH4、CO、H2, tar steam, rich carbon particle, the thermal decomposition product of the component such as inert particle enter back into purified synthesis gas and particle shunting System (3) is carried out in product cleanup separation, carbonaceous material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis reaction subsystem (14) In gas-solid fluid-mixing produced by pulverized coal pyrolysis particle size range in 50 μm~600 μm of not carbon containing inert particle at built-in It is captured in grain cycle subsystem (12), the inert particle of trapping is circulated respectively by circulation revert system built in multi-path again to be returned Quick mixing heating subsystem (13) and circulating granular second pyrolysis hydrogen manufacturing subsystem (11) are returned to regulate and control two subsystems The total thermal capacitance of bed and bed density；
Then, after preliminary purification i.e. from built-in particle cycle subsystem (12) escape 70~75wt% of fixation carbon content and The synthesis gas of the rich carbon particle of the sub-micron of the μ m of particle diameter 0.1~50, micron order enters purified synthesis gas and particle shunting is Unite (3), pass sequentially through high-temperature dry isolated subsystem (15), synthesis gas deep purifying subsystem (16), particle screening subsystem (17), the cross section of fluid channel constructed by coupled modes of the external particle cycle subsystem (18) in aerodynamics and mechanical grading principle In the presence of gradual change type double-cyclone gas-solid separator, efficiently separated with gas phase, and be recycled back into circulating granular second pyrolysis hydrogen manufacturing Subsystem (11), passes sequentially through particle heating region of activation (26), primary pyrolysis reaction zone (25), deep pyrolytic reaction zone (24), It is final to produce hydrogen-rich crude synthesis gas, constitute high temperature, hydrogen-rich, gas-solid two-phase mixtures together with the high temperature inorganic particle that reaction is produced Heat carrier, is above advanced into quick mixing heating subsystem (13), passes sequentially through hydrogen-rich high temperature gas-solid fluid-mixing commutating zone (29), vortex flow field transmission region (28), fluid-mixing temperature controlled region (27), are instantaneously heated to predetermined pyrolysis temperature by pulverized coal particle；
Finally, purified synthesis gas enters back into the light tar in downstream with the decontaminating syngas that particle separate system (3) is exported Recovery system (4), passes sequentially through oil gas adsorbing separation subsystem (19), light oil separating-purifying subsystem (20) and reclaims in gas phase Coalite tar enters light tar storage subsystem (21) in coal tar oil ingredient, final acquired liquid lightweight, reclaims The purification methane rich synthesis gas of gained enters back into methane-rich piece-rate system (5) after oil product, passes sequentially through methane separation purification System (22), methane boosting storage subsystem (23), finally enter methane storage tank.
CN201710388522.7A 2017-05-27 2017-05-27 It is a kind of to synchronize the device and method for producing methane rich synthesis gas and light tar Active CN107099319B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201710388522.7A CN107099319B (en) 2017-05-27 2017-05-27 It is a kind of to synchronize the device and method for producing methane rich synthesis gas and light tar

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201710388522.7A CN107099319B (en) 2017-05-27 2017-05-27 It is a kind of to synchronize the device and method for producing methane rich synthesis gas and light tar

Publications (2)

Publication Number Publication Date
CN107099319A true CN107099319A (en) 2017-08-29
CN107099319B CN107099319B (en) 2018-09-28

Family

ID=59659176

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201710388522.7A Active CN107099319B (en) 2017-05-27 2017-05-27 It is a kind of to synchronize the device and method for producing methane rich synthesis gas and light tar

Country Status (1)

Country Link
CN (1) CN107099319B (en)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110386589A (en) * 2019-08-06 2019-10-29 强伟氢能科技有限公司 A kind of high throughput methanol-water reformation hydrogen production micro passage reaction
CN110628445A (en) * 2019-10-30 2019-12-31 浙江科技学院 Biomass gas-carbon co-production reactor and reaction method thereof
CN110857391A (en) * 2018-08-24 2020-03-03 李大鹏 Self-adaptive three-cycle pressurized carbon-containing material step conversion system and method
CN113845951A (en) * 2020-06-28 2021-12-28 中国石油化工股份有限公司 Device and method for preparing methane by coal one-step method
CN113926379A (en) * 2021-12-15 2022-01-14 太原理工大学 Hydrogen production method by supercritical water oxygen oil production by long-distance multi-stage heating of pilot-scale organic rock
CN113926380A (en) * 2021-12-16 2022-01-14 太原理工大学 System for preparing oil and hydrogen by supercritical water oxygen through long-distance multi-stage heating of pilot-scale organic rock

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4594140A (en) * 1984-04-04 1986-06-10 Cheng Shang I Integrated coal liquefaction, gasification and electricity production process
CN105238447A (en) * 2015-09-18 2016-01-13 李大鹏 Apparatus and method for preparing natural gas and light oil from coal
CN207175870U (en) * 2017-05-27 2018-04-03 李大鹏 A kind of device for synchronously producing methane rich synthesis gas and light tar

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4594140A (en) * 1984-04-04 1986-06-10 Cheng Shang I Integrated coal liquefaction, gasification and electricity production process
CN105238447A (en) * 2015-09-18 2016-01-13 李大鹏 Apparatus and method for preparing natural gas and light oil from coal
CN207175870U (en) * 2017-05-27 2018-04-03 李大鹏 A kind of device for synchronously producing methane rich synthesis gas and light tar

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110857391A (en) * 2018-08-24 2020-03-03 李大鹏 Self-adaptive three-cycle pressurized carbon-containing material step conversion system and method
CN110386589A (en) * 2019-08-06 2019-10-29 强伟氢能科技有限公司 A kind of high throughput methanol-water reformation hydrogen production micro passage reaction
CN110386589B (en) * 2019-08-06 2023-06-27 广东能创科技有限公司 High flux methanol-water reforming hydrogen production micro-channel reactor
CN110628445A (en) * 2019-10-30 2019-12-31 浙江科技学院 Biomass gas-carbon co-production reactor and reaction method thereof
US10889760B2 (en) 2019-10-30 2021-01-12 Zhejiang University Of Science & Technoiogy Biomass gas-carbon co-production reactor and reaction method thereof
CN113845951A (en) * 2020-06-28 2021-12-28 中国石油化工股份有限公司 Device and method for preparing methane by coal one-step method
CN113926379A (en) * 2021-12-15 2022-01-14 太原理工大学 Hydrogen production method by supercritical water oxygen oil production by long-distance multi-stage heating of pilot-scale organic rock
CN113926379B (en) * 2021-12-15 2022-02-18 太原理工大学 Hydrogen production method by supercritical water oxygen oil production by long-distance multi-stage heating of pilot-scale organic rock
CN113926380A (en) * 2021-12-16 2022-01-14 太原理工大学 System for preparing oil and hydrogen by supercritical water oxygen through long-distance multi-stage heating of pilot-scale organic rock
CN113926380B (en) * 2021-12-16 2022-02-18 太原理工大学 System for preparing oil and hydrogen by supercritical water oxygen through long-distance multi-stage heating of pilot-scale organic rock

Also Published As

Publication number Publication date
CN107099319B (en) 2018-09-28

Similar Documents

Publication Publication Date Title
CN107099319B (en) It is a kind of to synchronize the device and method for producing methane rich synthesis gas and light tar
US10113125B2 (en) Method and system for cogenerating gas-steam based on gasification and methanation of biomass
CN104789245B (en) A kind of pyrolysis gasifying device and technique
RU2459857C2 (en) Method and apparatus for producing biofuel from solid biomass
CN104531186B (en) Method for producing tar and hydrocarbon fuel products with coal
CN109609198B (en) Biomass circulating fluidized bed grading pyrolysis gasification and high-temperature tar and dust removal integrated process
CN105154121A (en) Low-rank coal gradation usage poly-generation system and method
CN108026459A (en) Full steam gasification with carbon trapping
CN109652103B (en) Down bed-fixed bed pyrolysis-gasification integrated method and device
CN105462638A (en) Method and apparatus for producing natural gas through combination of crushed coal pressurization gasification and coal water slurry gasification
CN108795505B (en) Coal powder hydro-gasification method and system
CN107474859B (en) Coal pyrolysis gasification process coupling device and method thereof
CN102010738A (en) Coal or biomass medium low temperature pyrolysis quality improving system and method for producing quality improved coal, high calorific value pyrolysis gas and tar or liquefied synthetic oil by utilizing same
CN107760384A (en) The devices and methods therefor of efficient catalytic coal gasifaction methane rich synthesis gas
JP3231040B2 (en) Method for converting carbonaceous material into granular carbon and methanol
CN103214334A (en) Thermoelectricity combined production method and apparatus for preparing alkene and by coal and natural gas
CN205133505U (en) Low order coal grading utilizes many cogeneration system
CN113025388B (en) Method for co-resource utilization of urban solid waste and carbon dioxide
CN207175870U (en) A kind of device for synchronously producing methane rich synthesis gas and light tar
CN102559310A (en) Method for preparing natural gas and other hydrocarbons by using coke-oven gas and other industrial exhaust gases to carry out coal hydrogasification
CN109401794B (en) Staged conversion combined fluidized bed reaction device and reaction method
CN107916141B (en) Biomass and low-rank coal gasification-flash pyrolysis staged utilization method
CN112280580A (en) Method for increasing oil and improving quality of pulverized coal pyrolysis for fluidized bed
CN109652147B (en) Circulating fluidized bed pyrolysis-gasification device and method
CN104053754A (en) Biomethane Production Method

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant