CN107099319B - It is a kind of to synchronize the device and method for producing methane rich synthesis gas and light tar - Google Patents
It is a kind of to synchronize the device and method for producing methane rich synthesis gas and light tar Download PDFInfo
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- 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
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- 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
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- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
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- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
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- 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
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- 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
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- 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
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- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
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- C10K1/00—Purifying combustible gases containing carbon monoxide
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Abstract
It is a kind of to synchronize the device and method for producing methane rich synthesis gas and light tar, the present invention can be by the mixed material that one or two kinds of carbon hydrogen element balance above according to reaction mass of biomass, low-rank coal, petroleum coke, oil shale etc. is constituted in specific proportions as charging, feed 0.1~1mm of particle size range, the produced methane rich synthesis gas group of device becomes CO 15~30vol%, H220~40vol%CH48~35vol%, CmHn0.1~0.2vol%CO28~12vol%, N22~4vol%.Most importantly, while producing methane rich synthesis gas, the high-quality middle coalite tar of 15wt%~20wt% can also be obtained, this part coal tar can be changed into the very high coal base fine chemical product of the higher high-grade fuel oil product of added value, aromatic hydrocarbons, a variety of added values after deep processing, substantially enhance the economic competitiveness of coal gas, on the basis of realizing efficient coal resources, step, comprehensive utilization, the coupling of natural gas from coal and coal base Fine Chemical Industry interchain is realized.
Description
Technical field
The present invention relates to the high-efficiency cleaning trans-utilization of carbon raw material, natural gas from coal technical fields, and in particular to a kind of
It is balanced by one or two kinds of carbon hydrogen element above according to reaction mass in biomass, low-rank coal, petroleum coke, oil shale
The mixing carbonaceous material mixed in specific proportions synchronizes the device and method for producing methane rich synthesis gas and light tar.
Background technology
The scattered burning of coal burning, especially colm is the main reason for causing the current coal-burning atmosphere pollution in China,
It is sulfate in haze, nitrate, PM2.5One of the important sources of equal pollutants.In the current Coal Consumption Structure in China,
About 20% dissipates burning for Industrial Boiler and 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.It solves caused by the current consumption of coal in China
Haze pollution problem, in addition to 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 other than management, should also reduce coal dispersion directly burning and be carried out using the industrially desulfurized of maturation, denitration, dedusting technology
The concentrated combustion and conversion of coal.Natural gas from coal is one of the path for belonging to coal and concentrating Efficient Conversion, and realizes coal
The important technology that fuel feedstocksization change gas with Industrial Boiler coal supports, and production process efficiency is higher than coal liquifaction, ammonia from coal, coal
The processes such as preparing dimethy ether.Natural gas from coal is to produce synthetic natural gas using gasification, purification and methanation technology using coal as raw material
Process, for occupy China's production of energy and main body of consumption coal low-carbon, clean using provide one effectively way
Diameter；It will be in coal the extensive intensive utilization of coal of project location by supplying clean natural gas to target market
Sulphur, nitrogen etc. cause the main matter of atmosphere pollution to trap and are converted into the products such as sulphur, ammonium hydroxide, 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, increasing
Substitute gas realizes that coal high-efficiency clean utilization, reduction environmental pollution are of great significance.
It is shown according to National Development and Reform Committee's latest data, China's whole year gas production is about 1371 billion cubic meters within 2016, together
Than increasing by 1.5%；720 billion cubic meter of Imported gas amount increases by 17.4%；2090 billion cubic meter of Natural Gas Consumption Using 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 more set coal gas industrial production devices in stable operation.Therefore development natural gas from coal industry is effective supplement China's stone
Oil, natural gas resource are insufficient, 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 as 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 that the higher the better for methane content in purified gas,
The operating load of second step methanation device can be both reduced in this way and also allows for unit scale and the throwing of control synthesis gas methanation
Cost is provided, ammonia from coal then requires methane in purified gas more lower better with synthesis ammonia.And the selection of coal gas front end gasification process
The economy such as investment intensity, operating cost to project entirety have great influence.Up to now, used by natural gas from coal
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 synthesis gas caused 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 that Lurgi crushed coal pressure gasifying technologies generate, BGL broken coals are molten
The raw gas methane content of slag gasification technology takes second place (6.2vol%).However Lurgi gasification technologies, BGL gasification technologies are applicable in
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 is adopted generated a large amount of fine coal resources in the process and 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 are only 0.6~0.8, and existing synthesis gas methanation
Reaction is required to H in unstripped gas2/ CO ratios be more than 2, need to by most of CO by reacting condition to adjust 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 excessively high, especially BGL techniques need a large amount of chilled water (chw), two kinds of gas also using slag tap
Chemical industry skill also will 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, there is an urgent need for methane concentration is high, coal feeding amount is big, waste water yield is small in a kind of synthesis gas of exploitation, raw material is suitable
H in Ying Xingqiang, synthesis gas2/ C ratios are big, and using fine coal as the dry cinder discharging gasification process of raw material.Patent of invention dry quenching co-production coal
The method (101747918 A of CN) of preparing natural gas discloses in a kind of process of coking absorbs high temperature with cold coal and its pyrolytic process
The coke cooling means of coke thermal energy provides 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 thermal energy, high-temperature coke is cooled down, by absorb thermal energy after high temperature heat-carrying gas and coal charge it is direct
Contact heat-exchanging rises mild pyrolysis with coal and recycles heat, by high-temperature coke quenching process and pyrolysis of coal PROCESS COUPLING, generates pyrolysis half
Burnt and pyrolysis coal gas further uses water vapour and oxygen gasified heat on the basis of above-mentioned dry coke quenching and the method for pyrolysis of coal
Solve semicoke generate gasification gas, then by gasification gas with pyrolysis coal gas gaseous mixture it is transformed and purification for methanation reaction life
At 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
It answers, but still has semicoke generation in technology, and belong to high temperature pyrolysis, heavy component is more in produced tar, has height
BTX and the PCX constituent content of added value are less.
Invention content
The purpose of the present invention is to provide one kind while fine coal pressurization fast pyrogenation produces high-quality middle coalite tar
It generates high concentration and is rich in methane synthesis gas, realize that the cascade utilization of coal resources, synchronizing for high-efficiency cleaning conversion produce methane rich
The device and method of synthesis gas and light tar.
In order to achieve the above objectives, the inventive system comprises carbonaceous material fast pyrolysis reaction system and with its entrance
Connected continuous pressure stable state feed system exports the purified synthesis gas being connected and particle separate system, purified synthesis gas with it
It is connected successively with light tar recovery system, methane-rich piece-rate system with the outlet of particle separate system；
The carbonaceous material fast pyrolysis reaction system includes two secondary fissure of circulating granular being sequentially connected from bottom to top
Solve hydrogen manufacturing subsystem, quickly mixing heating subsystem, carbonaceous material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis reaction subsystem
System；
The 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, the high-temperature dry isolated subsystem with
The syngas outlet that carbonaceous material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis reacts subsystem is connected, external particle cycle
The carbonaceous particles of system trapping are recycled back into circulating granular second pyrolysis hydrogen manufacturing subsystem；
The light tar recovery system includes oil gas adsorbing separation subsystem, the light oil separating-purifying being sequentially connected
Subsystem and light tar storage subsystem；
The methane-rich piece-rate system includes that methane separation purifies subsystem and methane boosting storage subsystem, described
Methane separation purification subsystem be connected with the syngas outlet of light oil separating-purifying subsystem.
The continuous pressure stable state feed system includes the raw material warehouse, controllable feed pulverizer, one being sequentially connected
Formula recycles gas dryer, feed surge device and mechanical strength manifold type fine coal charging gear, the mechanical strength manifold type powder
Coal charging gear is connected with the entrance of carbonaceous material fast pyrolysis reaction system.
It is also equipped with trapping not on the carbonaceous material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis reaction subsystem
The built-in particle cycle subsystem of carbon containing inert particle, the built-in particle cycle subsystem pass through the inert particle of trapping more again
The built-in cycle revert system of access is recycled back into quickly mixing heating subsystem and circulating granular second pyrolysis hydrogen manufacturing subsystem respectively
It unites to regulate and control the total thermal capacitance of bed and bed material density of two subsystems.
The 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, the particle heat up region of activation respectively with external particle cycle subsystem and
Built-in particle cycle subsystem is connected.
The described quick mixing heating subsystem includes that the hydrogen-rich high temperature gas-solid fluid-mixing that sets gradually from bottom to top is whole
Flow area, vortex flow field transmission region, fluid-mixing temperature controlled region, the hydrogen-rich high temperature gas-solid fluid-mixing commutating zone and cycle
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.
The oil gas adsorbing separation subsystem is equipped with by high adsorption activity molecular sieve, modified graft polymer material, alkane
The adsorption stuffing bed that base benzene series copolymer fibre is formed.
The operating pressure of the carbonaceous material fast pyrolysis reaction system is 3.0~5.0MPa, reaction temperature 950
~1200 DEG C.
The quick mixing heating subsystem passes through local jet configuration and 50~300 high-temperature heat carrier circulating ratio institutes
The 10-20MJ/m of offer2The heat flux of s, 103~105DEG C/heating rate of s under, in 1~10ms that fresh feed is quick
It is heated to 500~700 DEG C of reaction temperature.
The methane separation purification subsystem uses CH4Concentration and separation material is with high intensity, high-throughput macromolecule sieve membrane
With flexible MOFs composites, porous active carbon fiber, activated alumina, carbon molecular sieve, the hollow fibre of high molecular polymer
One or two kinds of above classification enrichment membrane module assembled in dimension film.
The present invention synchronizes the method for producing methane rich synthesis gas and light tar and includes the following steps：
First, the feed coal in raw material warehouse is successively via controllable feed pulverizer, integrated circular gas dryer institute group
At stock preparation system prepare the drying coal dust that 10~1000 μm of particle size range and moisture content be 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 using mechanical strength manifold type fine coal charging gear
Quick mixing in cracking reaction system heats up subsystem, in quick mixing heating subsystem with self-loopa particle second pyrolysis
Hydrogen manufacturing subsystem and come high temperature gas-solid mixing heat carrier be under 50~300 times of Solids Circulation Rates 1-10ms when
It is interior instantaneously to be exchanged heat, pulverized coal particle be heated to after 500~700 DEG C of pyrolysis temperature be advanced into carbonaceous material constant temperature-plus
Pressure-catalytic hydrogenation fast pyrolysis reacts subsystem, later under 3.0~5.0MPa pressure conditions in completing quick fine coal in 2s
Fast pyrogenation reacts, CH containing high concentration caused by fast pyrogenation reaction4、CO、H2, tar steam, rich carbon particle, inert particle
Etc. the thermal decomposition products of components enter back into purified synthesis gas and particle separate system and carry out product cleanup and detach, carbonaceous material constant temperature-
Particle size range exists in gas-solid fluid-mixing caused by pulverized coal pyrolysis in pressurization-catalytic hydrogenation fast pyrolysis reaction subsystem
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 cycle revert system of multi-path is recycled back into quickly mixing heating subsystem and circulating granular second pyrolysis hydrogen manufacturing respectively
System is to the total thermal capacitance of bed and bed material density that regulate and control two subsystems；
Then, after preliminary purification i.e. 70~75wt% of fixation carbon content for escaping from built-in particle cycle subsystem and
The sub-micron of 0.1~50 μ m of grain size, the synthesis gas of micron order richness carbon particle enter purified synthesis gas and particle separate system,
Pass sequentially through high-temperature dry isolated subsystem, synthesis gas deep purifying subsystem, particle screening subsystem, external particle cycle
Cross section of fluid channel gradual change type double-cyclone gas-solid separator of the system constructed by the coupled modes of aerodynamics and mechanical grading principle
Under the action of, it is efficiently separated with gas phase, and be recycled back into circulating granular second pyrolysis hydrogen manufacturing subsystem, passes sequentially through particle heating
Region of activation, primary pyrolysis reaction zone, deep pyrolytic reaction zone, it is final to generate hydrogen-rich crude synthesis gas, with react the high temperature of generation without
Machine particle constitutes high temperature, hydrogen-rich, gas-solid two-phase mixtures heat carrier together, is above advanced into quickly mixing heating subsystem, leads to successively
Hydrogen-rich high temperature gas-solid fluid-mixing commutating zone, vortex flow field transmission region, fluid-mixing temperature controlled region are crossed, instantaneously adds pulverized coal particle
Heat is 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 recycling gas phase,
Coalite tar enters light tar storage subsystem in final acquired liquid lightweight, recycles 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,
One or two kinds of carbon hydrogen element balance above according to reaction mass of petroleum coke, oil shale etc. constitutes mixed in specific proportions
Close material as charging, feed 0.1~1mm of particle size range, the produced methane rich synthesis gas group of device become CO 15~
30vol%, H220~40vol%CH48~35vol%, CmHn0.1~0.2vol%CO28~12vol%, N22~
4vol%.Most of all, while producing methane rich synthesis gas, the high-quality middle low temperature of 15wt%~20wt% can be also obtained
Coal tar, this part coal tar can be changed into the higher high-grade fuel oil product of added value, aromatic hydrocarbons, a variety of additional after deep processing
The very high coal base fine chemical product of value, substantially enhances 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 mating 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, realize synchronous production methane rich synthesis gas with it is high-quality
Middle coalite tar, methane concentration is up to 25~55vol% in the synthesis gas of generation, is higher than existing crushed coal pressure gasifying technology
Follow-up methanation device scale and investment is greatly reduced in methane concentration in generated crude synthesis gas；
2) H in crude synthesis gas caused by2/ C ratios are higher than 2.0, no longer need to improve H by transformationreation2/ C ratios；
3) yield of light tar is up to 15~20wt% in technology system disclosed in this invention, can be with downstream
Coal tar deep processing industrial chain be highly coupled integrated, greatly improve the macroeconomic competitiveness of process system；
4) dust concentration is extremely low in institute's production of synthetic gas, and total carbon high conversion rate, unit scale and operating flexibility are big, is convenient for engineering
Change application；
5) realize the diversification of device raw material, both can lower-grade metamorphic bituminous, lignite be raw material, can also biomass, low
One or two kinds of carbon hydrogen element balance above according to reaction mass of rank coal, petroleum coke, oil shale etc. is in specific proportions
The mixed material of composition, device charging are adaptable.
Description of the drawings
Fig. 1 is the device of the invention and flow diagram.
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. following
Ring particle second pyrolysis hydrogen manufacturing subsystem；Particle cycle subsystem built in 12.；13. quickly mixing heating subsystem；14. 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.
Specific implementation mode
In order to keep technical scheme of the present invention and advantage more clear apparent, with reference to the accompanying drawings and embodiments, to this hair
Bright device and method is further elaborated.
Referring to Fig. 1, the present invention include carbonaceous material fast pyrolysis reaction system 2 and be connected with its entrance continuous plus
Stable state feed system 1 is pressed, the purified synthesis gas being connected and particle separate system 3 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；
The carbonaceous material fast pyrolysis reaction system 2 includes two secondary fissure of circulating granular being sequentially connected from bottom to top
Solve hydrogen manufacturing subsystem 11, quickly mixing heating subsystem 13, the reaction of carbonaceous material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis
Subsystem 14；
The purified synthesis gas and particle separate system 3 include the high-temperature dry isolated subsystem 15 being sequentially connected, close
At gas deep purifying subsystem 16, particle screening subsystem 17 and external particle cycle subsystem 18, the 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 traps are recycled back into circulating granular second pyrolysis hydrogen manufacturing subsystem 11；
The light tar recovery system 4 includes the oil gas adsorbing separation subsystem 19 being sequentially connected, light oil separation
Purify subsystem 20 and light tar storage subsystem 21；
The methane-rich piece-rate system 5 includes methane separation purification subsystem 22 and methane boosting storage subsystem
23, methane separation purification subsystem 22 is connected with the syngas outlet of light oil separating-purifying subsystem 20.
The continuous pressure stable state feed system 1 includes raw material warehouse 6, the controllable feed pulverizer 7, one being sequentially connected
Body formula recycles gas dryer 8, feed surge device 9 and mechanical strength manifold type fine coal charging gear 10, the mechanical strength coupling
Box-like fine coal charging gear 10 is connected with the entrance of carbonaceous material fast pyrolysis reaction system 2.
It is also equipped with trapping on the 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 grain size of trapping~
The inert particle of 600 μm of grades is recycled back into quickly mixing heating subsystem 13 respectively by recycling revert system built in multi-path again
And circulating granular second pyrolysis hydrogen manufacturing subsystem 11 is regulating and controlling the total thermal capacitance of bed and bed material density of two subsystems.
The 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, the particle heat up region of activation 26 respectively with external particle
Cycle subsystem 18 and built-in particle cycle subsystem 12 are connected.
The 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, the 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, fluid-mixing temperature controlled region 27 with contain
Carbon material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis reaction subsystem 14 is connected.
The oil gas adsorbing separation subsystem 19 be equipped with by high adsorption activity molecular sieve, modified graft polymer material,
The adsorption stuffing bed that alkylbenzene system copolymer fibre is formed.
The operating pressure of the carbonaceous material fast pyrolysis reaction system 2 is 3.0~5.0MPa, and reaction temperature is
950~1200 DEG C.
The quick mixing heating subsystem 13 passes through local jet configuration and 50~300 high-temperature heat carrier circulating ratios
The 10-20MJ/m provided2The heat flux of s, 103~105DEG C/heating rate of s under, in 1~10ms that fresh feed is fast
Speed is heated to 500~700 DEG C of reaction temperature.
The methane separation purification subsystem 22 uses CH4Concentration and separation material is with high intensity, high-throughput macromolecule sieve
Film and flexibility MOFs composites, porous active carbon fiber, activated alumina, carbon molecular sieve, high molecular polymer are hollow
One or two kinds of above classification enrichment membrane module assembled in tunica fibrosa.
The particle screening subsystem 17 by pressure field constructed by inner flow passage configuration, the distribution of speed field gradient come
Realize the inert particle and the rich carbon particle of 60~80wt% of fixed carbon content, 50 μm of grain size ＜ of 50~600 μm of particle size range
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 7,8 institute of integrated circular gas dryer
The stock preparation system of composition prepares 10~1000 μm of particle size range and moisture content is less than the drying coal dust of 2.0wt%, prepares
It is fast into carbonaceous material using mechanical strength manifold type fine coal charging gear 10 that qualified fresh coal dust enters feed surge device 9
Quick mixing in speed heat cracking reaction system 2 heats up subsystem 13, in quick mixing heating subsystem 13 with self-loopa
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 the time of 1-10ms, 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, later in 2s under 3.0~5.0MPa pressure conditions
It is interior to complete quick fine coal fast pyrogenation reaction, the generated CH containing high concentration of 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 is detached with the progress product cleanup of particle separate system 3,
Carbonaceous material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis reacts gas-solid mixed flow caused by pulverized coal pyrolysis in subsystem 14
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 again by built in multi-path recycle revert system be recycled back into respectively quickly mixing heating subsystem 13 and cycle
Particle second pyrolysis hydrogen manufacturing subsystem 11 is regulating and controlling the total thermal capacitance of bed and bed material density of two subsystems；
Then, the 70~75wt% of fixation carbon content to escape from built-in particle cycle subsystem 12 after preliminary purification
And the sub-micron of 0.1~50 μ m of grain size, the synthesis gas of micron order richness carbon particle enter purified synthesis gas and particle shunting is
System 3 passes sequentially through high-temperature dry isolated subsystem 15, synthesis gas deep purifying subsystem 16, particle screening subsystem 17, external
Cross section of fluid channel gradual change type bispin of the particle cycle subsystem 18 constructed by the coupled modes of aerodynamics and mechanical grading principle
It under the action of gas solid separator, is efficiently separated with gas phase, and is recycled back into circulating granular second pyrolysis hydrogen manufacturing subsystem 11, according to
Secondary to be heated up region of activation 26, primary pyrolysis reaction zone 25, deep pyrolytic reaction zone 24 by particle, the final hydrogen-rich that generates slightly synthesizes
Gas constitutes high temperature, hydrogen-rich, gas-solid two-phase mixtures heat carrier together with the high temperature inorganic particle that reaction generates, and is above advanced into quickly
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
Pulverized coal particle is instantaneously heated to predetermined pyrolysis temperature by fluid temperature controlled region 27；
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 recycling gas phase of light oil separating-purifying subsystem 20
Oil ingredient, finally coalite tar enters light tar storage subsystem 21 in acquired liquid lightweight, after recycling 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 enters methane storage tank.
Claims (8)
1. a kind of synchronizing the device for producing methane rich synthesis gas and light tar, which is characterized 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 recycled 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；
The carbonaceous material fast pyrolysis reaction system (2) includes the circulating granular second pyrolysis being sequentially connected from bottom to top
Hydrogen manufacturing subsystem (11), quickly mixing heating subsystem (13), carbonaceous material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis are anti-
Answer subsystem (14)；
The operating pressure of the carbonaceous material fast pyrolysis reaction system (2) is 3.0~5.0MPa, reaction temperature 950
~1200 DEG C；
The described quick mixing heating subsystem (13) includes that the hydrogen-rich high temperature gas-solid fluid-mixing that sets gradually from bottom to top is whole
Area (29), vortex flow field transmission region (28), fluid-mixing temperature controlled region (27) are flowed, the hydrogen-rich high temperature gas-solid fluid-mixing is whole
Stream area (29) is connected with the deep pyrolytic reaction zone (24) of circulating granular second pyrolysis hydrogen manufacturing subsystem (11), mixed flow body temperature
Control area (27) reacts subsystem (14) with carbonaceous material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis and is connected；
The purified synthesis gas and particle separate system (3) include the high-temperature dry isolated subsystem (15) being sequentially connected, close
At gas deep purifying subsystem (16), particle screening subsystem (17) and external particle cycle subsystem (18), the 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)；
The light tar recovery system (4) includes the oil gas adsorbing separation subsystem (19) being sequentially connected, light oil separation
Purify subsystem (20) and light tar storage subsystem (21)；
The methane-rich piece-rate system (5) includes methane separation purification subsystem (22) and methane boosting storage subsystem
(23), methane separation purification subsystem (22) is connected with the syngas outlet of light oil separating-purifying subsystem (20).
2. according to claim 1 synchronize the device for producing methane rich synthesis gas and light tar, which is characterized 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
Recycle gas dryer (8), feed surge device (9) and mechanical strength manifold type fine coal charging gear (10), the mechanical strength
Manifold type fine coal charging gear (10) is connected with the entrance of carbonaceous material fast pyrolysis reaction system (2).
3. according to claim 1 synchronize the device for producing methane rich synthesis gas and light tar, which is characterized in that institute
It is not carbon containing lazy it to be also equipped with trapping on 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) pass through the inert particle of trapping again
The built-in cycle revert system of multi-path is recycled back into quickly mixing heating subsystem (13) and circulating granular second pyrolysis system respectively
Hydrogen subsystem (11) is to the total thermal capacitance of bed and bed material density that regulate and control two subsystems.
4. according to claim 1 or 3 synchronize the device for producing methane rich synthesis gas and light tar, feature exists
In the 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), particle heating region of activation (26) respectively with outside
It sets particle cycle subsystem (18) and built-in particle cycle subsystem (12) is connected.
5. according to claim 1 synchronize the device for producing methane rich synthesis gas and light tar, which is characterized in that institute
The oil gas adsorbing separation subsystem (19) stated is equipped with by high adsorption activity molecular sieve, modified graft polymer material, alkyl benzene series
The adsorption stuffing bed that copolymer fibre is formed.
6. according to claim 1 synchronize the device for producing methane rich synthesis gas and light tar, which is characterized 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/m2The heat flux of s, 103~105DEG C/heating rate of s under, in fresh feed is quickly heated up in 1~10ms
500~700 DEG C of reaction temperature.
7. according to claim 1 synchronize the device for producing methane rich synthesis gas and light tar, which is characterized in that institute
The methane separation purification subsystem (22) stated uses CH4Concentration and separation material is with high intensity, high-throughput 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 above classification enrichment membrane module assembled.
8. a kind of synchronizing the method for producing methane rich synthesis gas and light tar, 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 formed prepares 10~1000 μm of particle size range and moisture content is less than the drying coal dust of 2.0wt%, system
It is carbon containing using the entrance of mechanical strength manifold type fine coal charging gear (10) that standby qualified fresh coal dust enters feed surge device (9)
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 the time of 1~10ms 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, later 3.0~
In completing quick fine coal fast pyrogenation reaction in 2s under 5.0MPa pressure conditions, contain high concentration caused by fast pyrogenation reaction
CH4、CO、H2, tar steam, rich carbon particle, inert particle component thermal decomposition product enter back into purified synthesis gas and particle shunting system
System (3) carries out product cleanup separation, and carbonaceous material constant temperature-pressurization-catalytic hydrogenation fast pyrolysis reacts powder in subsystem (14)
In gas-solid fluid-mixing caused by pyrolysis of coal particle size range in 50 μm~600 μm of not carbon containing inert particle in built-in particle
Cycle subsystem is captured in (12), and the inert particle of trapping is recycled back by recycling revert system built in multi-path respectively again
Heating subsystem (13) and circulating granular second pyrolysis hydrogen manufacturing subsystem (11) are quickly mixed to regulate and control the bed of two subsystems
The total thermal capacitance of layer and bed material density；
Then, after preliminary purification i.e. 70~75wt% of fixation carbon content for escaping from built-in particle cycle subsystem (12) and
The sub-micron of 0.1~50 μ m of grain size, the synthesis gas of micron order richness carbon particle enter purified synthesis gas and particle separate system
(3), high-temperature dry isolated subsystem (15), synthesis gas deep purifying subsystem (16), particle screening subsystem are passed sequentially through
(17), cross section of fluid channel of the external particle cycle subsystem (18) constructed by the coupled modes of aerodynamics and mechanical grading principle
It under the action of gradual change type double-cyclone gas-solid separator, is efficiently separated with gas phase, and is 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 generate hydrogen-rich crude synthesis gas, constitute high temperature, hydrogen-rich, gas-solid two-phase mixtures together with the high temperature inorganic particle that reaction generates
Heat carrier is above advanced into quickly 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 in oil gas adsorbing separation subsystem (19), light oil separating-purifying subsystem (20) recycling gas phase
Coal tar oil ingredient, finally coalite tar enters light tar storage subsystem (21) in acquired liquid lightweight, recycles
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.
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