CN202829964U - Biomass fuel carbon dioxide cycle no-oxygen equipment - Google Patents

Biomass fuel carbon dioxide cycle no-oxygen equipment Download PDF

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Publication number
CN202829964U
CN202829964U CN2012203927006U CN201220392700U CN202829964U CN 202829964 U CN202829964 U CN 202829964U CN 2012203927006 U CN2012203927006 U CN 2012203927006U CN 201220392700 U CN201220392700 U CN 201220392700U CN 202829964 U CN202829964 U CN 202829964U
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tower
links
gas
import
carbon dioxide
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Expired - Fee Related
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CN2012203927006U
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张岩丰
张亮
夏明贵
刘文焱
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Wuhan Kaidi Engineering Technology Research Institute Co Ltd
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Wuhan Kaidi Engineering Technology Research Institute Co Ltd
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    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Abstract

The utility model discloses biomass fuel carbon dioxide cycle no-oxygen equipment which is mainly formed by sequential connection of a gasifier, a waste heat exchanger, a waste heat boiler, a cyclone dust collector, a scrubber tower, a shift reaction tower, a desulfurizing tower, a synthesis gas decarbonization tower, a catalyzed synthesis tower and an exhaust gas decarbonization tower. Only carbon dioxide is utilized to be used as a gasifying agent to gasify solid fuel gas such as biomass into high-quality synthesis gas and recycle carbon dioxide gas of the synthesis gas and the carbon dioxide gas generated by subsequent use processes of the synthesis gas to be gasified and circulated, thus the purpose of zero greenhouse gases carbon dioxide emissions of the whole system can be achieved. The biomass fuel carbon dioxide cycle no-oxygen equipment has the significant advantages of being no oxygen consumption, high in produced synthesis gas quality, high-efficient in refrigerated gas and simple in operation of a system. Moreover, the green house gases carbon dioxide emissions of the whole system is zero.

Description

Biomass fuel carbonic acid gas circulation anaerobic equipment for gasification
Technical field
It is that the gasification of raw material utilizes the field that the utility model relates to biomass, refers to particularly a kind of biomass fuel carbonic acid gas circulation anaerobic equipment for gasification.
Background technology
Along with the growing interest of the public to global warming trend, reduction of greenhouse gas discharge more and more has been subject to the attention of countries in the world, has also proposed the concept of zero release energy resource system such as U.S. GE energy and environment research company, U.S. zero release alliance and Japanese new forms of energy comprehensive exploitation mechanism etc.
Current, the main technique method that solves the greenhouse gases zero release be with carbonic acid gas as reactant, be converted into by chemical reaction and contain carbon products, reach the purpose of zero release.Invention patent mandate notification number: CN102060662B, a kind of recoverable CO 2Chemical industry power Energy Polygeneration System and method, namely by reclaiming the CO in the chemical industry tail gas 2, a part of CO wherein 2Carry out aerobic gasification circulation and come producing synthesis gas, another part CO 2Carry out reforming reaction by adding Sweet natural gas, final preparation of dimethyl ether or methyl alcohol.This patent of invention can be recycled CO 2But this processing method needs oxygen gasified, thereby CO in the gasification 2Inversion quantity is limited, wherein most of CO 2Need react to transform by gas renormalizing, thereby have the shortcoming of aerobic consumption, need consumption Sweet natural gas and technical process complexity.
Summary of the invention
The purpose of this utility model is to propose a kind of biomass fuel carbonic acid gas circulation anaerobic equipment for gasification, and this equipment has fuel conversion height, anaerobic consumption, and the simple and whole system greenhouse gases CO2 emissions of technical process is the remarkable advantage such as zero.
For achieving the above object, the biomass fuel carbonic acid gas circulation anaerobic equipment for gasification that the utility model provides, comprise vapourizing furnace, afterheat heat exchanger, waste heat boiler, tornado dust collector, scrubber tower, transformationreation tower, thionizer, synthetic gas decarbonizing tower, catalyze and synthesize tower and tail gas decarbonizing tower, its special character is:
The syngas outlet of described vapourizing furnace links to each other with the thermal medium input terminus of afterheat heat exchanger, the thermal medium output terminal of described afterheat heat exchanger links to each other with the thermal source input terminus of waste heat boiler, the thermal source output terminal of described waste heat boiler links to each other with the inlet end of tornado dust collector, the outlet side of described tornado dust collector links to each other with the import of scrubber tower, the outlet of described scrubber tower links to each other by the inlet mouth of compressor with the transformationreation tower, and the steam output end of described waste heat boiler links to each other with the steam-in of transformationreation tower;
The air outlet of described transformationreation tower links to each other with the input terminus of thionizer, the output terminal of described thionizer links to each other with the input aperture of synthetic gas decarbonizing tower, the delivery port of described synthetic gas decarbonizing tower links to each other with the material inlet that catalyzes and synthesizes tower, the described by product outlet that catalyzes and synthesizes tower links to each other the CO of described tail gas decarbonizing tower and synthetic gas decarbonizing tower with the tail gas import of tail gas decarbonizing tower 2Outlet links to each other with the cold medium input terminus of afterheat heat exchanger simultaneously, and the cold medium output terminal of described afterheat heat exchanger links to each other with the vaporized chemical import of vapourizing furnace.
As preferred version, the CO of described tail gas decarbonizing tower and synthetic gas decarbonizing tower 2Outlet links to each other with the import of gas holder simultaneously, and the outlet of described gas holder links to each other with the cold medium input terminus of afterheat heat exchanger by gas blower.
Further, the import of described gas holder also with the CO that starts calcining furnace 2Delivery port links to each other.
Further, the inner chamber bottom of described vapourizing furnace is provided with air distribution plate, be provided with main vaporized chemical import on the furnace wall of described air distribution plate below, be provided with auxiliary vaporized chemical import on the furnace wall of described air distribution plate top, be provided with outside auxiliary energy entrance on the furnace wall of described auxiliary vaporized chemical import top, the cold medium output terminal of described afterheat heat exchanger is divided into two-way, and one the tunnel links to each other with main vaporized chemical import, and another road links to each other with auxiliary vaporized chemical import.
The utility model has the advantage of:
One adopts carbon dioxide as the whole system cycle fluid, has the advantage of whole plant zero greenhouse gas emission, zero oxygen consumption.
Its two, fully in conjunction with the biomass fuel self-characteristic, gasification unit only adopts carbonic acid gas as vaporized chemical, anaerobic gasification has not only replenished carbon source but also reduce the fuel combustion share, the unit of fuel transformation efficiency is high, available gas content is high.
Its three, raw material particle size without particular requirement, is only needed simple crushing, need not complex process, good economy performance.
Its four, adopt external heat source that auxiliary heat energy is provided, can fully in conjunction with the various forms energy, can realize comprehensive utilization of energy.
Description of drawings
Fig. 1 is the syndeton synoptic diagram of biomass fuel carbonic acid gas circulation anaerobic equipment for gasification of the present utility model.
Fig. 2 is the structural representation of vapourizing furnace among Fig. 1.
Fig. 3 is the A-A sectional structure synoptic diagram among Fig. 2.
Among the figure: vapourizing furnace 1, afterheat heat exchanger 2, waste heat boiler 3, tornado dust collector 4, scrubber tower 5, compressor 6, transformationreation tower 7, thionizer 8, synthetic gas decarbonizing tower 9 catalyzes and synthesizes tower 10, tail gas decarbonizing tower 11, gas holder 12, gas blower 13, fuel 14, outside auxiliary energy entrance 15, auxiliary vaporized chemical import 16, feed entrance 17, syngas outlet 18, air distribution plate 19, main vaporized chemical import 20, slag-drip opening 21, feeding device 22, slag cooler 23, steam 24, cold slag 25, flying dust 26, synthetic oil 27, synthesis tail gas 28, carbonic acid gas 29, synthetic gas 30, discharging gas 31 starts calcining furnace 32, Wingdale 33.
Embodiment
Below in conjunction with the drawings and specific embodiments the utility model is made further detailed description.
Biomass fuel carbonic acid gas circulation anaerobic equipment for gasification shown in the figure, mainly by vapourizing furnace 1, afterheat heat exchanger 2, waste heat boiler 3, tornado dust collector 4, scrubber tower 5, transformationreation tower 7, thionizer 8, synthetic gas decarbonizing tower 9, catalyze and synthesize tower 10 and tail gas decarbonizing tower 11 etc. and form.The top of vapourizing furnace 1 is provided with syngas outlet 18, and the bottom of vapourizing furnace 1 is provided with slag-drip opening 21, and the middle part outer wall of vapourizing furnace is provided with feed entrance 17, and feed entrance 17 links to each other with feeding device 22.The inner chamber bottom of vapourizing furnace 1 is provided with air distribution plate 19, be provided with main vaporized chemical import 20 on the furnace wall of air distribution plate 19 belows, be provided with auxiliary vaporized chemical import 16 on the furnace wall of air distribution plate 19 tops, be provided with outside auxiliary energy entrance 15 on the furnace wall of auxiliary vaporized chemical import 16 tops.
The syngas outlet 18 of vapourizing furnace 1 links to each other with the thermal medium input terminus of afterheat heat exchanger 2, the thermal medium output terminal of afterheat heat exchanger 2 links to each other with the thermal source input terminus of waste heat boiler 3, the thermal source output terminal of waste heat boiler 3 links to each other with the inlet end of tornado dust collector 4, the outlet side of tornado dust collector 4 links to each other with the import of scrubber tower 5, the outlet of scrubber tower 5 links to each other with the inlet mouth of transformationreation tower 7 by compressor 6, and the steam output end of waste heat boiler 3 links to each other with the steam-in of transformationreation tower 7.
The air outlet of transformationreation tower 7 links to each other with the input terminus of thionizer 8, the output terminal of thionizer 8 links to each other with the input aperture of synthetic gas decarbonizing tower 9, the delivery port of synthetic gas decarbonizing tower 9 links to each other with the material inlet that catalyzes and synthesizes tower 10, the by product outlet that catalyzes and synthesizes tower 10 links to each other the CO of tail gas decarbonizing tower 11 and synthetic gas decarbonizing tower 9 with the tail gas import of tail gas decarbonizing tower 11 2Outlet links to each other with the cold medium input terminus of afterheat heat exchanger 2 simultaneously, and the cold medium output terminal of afterheat heat exchanger 2 is divided into two-way, and one the tunnel links to each other with main vaporized chemical import 20, and another road links to each other with auxiliary vaporized chemical import 16.
The CO of tail gas decarbonizing tower 11 and synthetic gas decarbonizing tower 9 2Outlet links to each other with the import of gas holder 12 simultaneously, and the outlet of gas holder 12 links to each other with the cold medium input terminus of afterheat heat exchanger 2 by gas blower 13; The import of gas holder 12 also with the CO that starts calcining furnace 32 2Delivery port links to each other.
Among the present invention, the solid fuels such as biomass 14 are at first sent in the vapourizing furnace 1 by material inlet 17 by feeding device 22, the vaporized chemical CO of circulation 2Blast vaporized chemical CO by gas blower 13 2Be divided into two-way, the main vaporized chemical import 20 of leading up to is introduced, and enters in the vapourizing furnace 1 through air distribution plate 19; Another road enters in the vapourizing furnace 1 by auxiliary vaporized chemical import 16, simultaneously, introduces heat energy by outside auxiliary energy entrance 15, carries out pyroreaction in stove, carries out at first pyrolytic gasification, and main cracking generates CO, CO 2, CH 4, H 2And semicoke because the reaction in furnace temperature is controlled at 600 ~ 1600 ℃, under the high temperature mainly by semicoke material and CO 2Gas carries out gasification reaction, and gasification reaction speed is fast, and principal reaction is C+CO 2=2CO+Q.
With the test of biomass rice husk, with 1Nm 3Synthetic gas is benchmark, and the supplementary energy amount is 15 ~ 25% of entrance fuel total energy, and 800 ℃ of temperature of reaction need circulation CO 2Amount is 0.51Nm 3Need biological quality 0.48kg, outlet synthetic gas volume composition is: CO:50 ~ 55%, CO 2: 22 ~ 28%, H 2: 6 ~ 12%.
High-temperature synthesis gas 30 is drawn by the syngas outlet 18 of vapourizing furnace 1, and the cold slag 25 of fuel is discharged by slag-drip opening 21, drains into the slag field behind slag cooler 23.
Wherein, the vapourizing furnace reaction zone temperature is controlled at 600 ~ 1300 ℃, and 850 ~ 1250 ℃ is its optimum temps.The syngas outlet temperature is controlled in 800 ~ 1100 ℃ of scopes.Feed carrier gas in the gasification unit, technique purge the CO that usefulness gas all utilizes circulation 2Gas.Outside input energy sources accounts for processes 15 ~ 30% of raw material energy.The extra power pattern also comprises micro-wave energy, sun power, laser energy, inductance and should be able to wait other to can be exchanged into the energy pattern of heat energy except adopting plasma torch.Vaporized chemical CO 2Internal circulating load can suitably be regulated according to furnace temperature, fuel situation.Vaporized chemical air distribution plate spout flow velocity can rationally be controlled according to the fuel particle diameter in the vapourizing furnace, preferred embodiments be particle diameter in the following scope of 50mm, wind speed is 30 ~ 60m/s.When vapourizing furnace starts operation, adopt to start calcining furnace 32, utilize outer forged scoria lime stone 33, come high purity CO 2Gas is used gas as starting.In order to make this technique reach the best effort effect, satisfy the requirement of technique overall performance, key is the control bed temperature in the design, regulates in real time plasma power and carbonic acid gas feed rate.By the syngas outlet monitoring means being reached the control to above-mentioned key factor, also can realize chain control, carry out full-automatic operation, improve operation stability.
High-temperature synthesis gas 30 enters in the afterheat heat exchanger 2 subsequently, with the CO as vaporized chemical 2Gas 29 carries out heat exchange, plays the effect of preheating vaporized chemical, has improved the vapourizing furnace transformation efficiency.Then high-temperature synthesis gas after the one-level cooling enters and continues cooling in the waste heat boiler 3, and by-product water vapor 24, process tornado dust collector 4, scrubber tower 5 are further to synthetic gas cooling dedusting again for synthetic gas after the two-stage cooling, and the flying dust 26 that separates drains into the slag field after collecting, wherein preheating CO 2Temperature is 350 ~ 600 ℃.
Synthetic gas after the cooling washing boosts by compressor 6 subsequently, enter conversion tower 7 after boosting, synthetic gas is carried out modifier treatment in that conversion tower 7 is interior, principal reaction is water-gas reaction, wherein water vapor 24 derives from waste heat boiler 3, reaches like this purpose that the integrated artistic material rationally utilizes.
Synthetic gas after modified enters thionizer 8 subsequently, synthetic gas decarbonizing tower 9 carries out desulfurization decarbonization purification and processes.The Clean synthesis gas of drawing from synthetic gas decarbonizing tower 9 enters subsequently and catalyzes and synthesizes tower 10, the CO that separates from synthetic gas decarbonizing tower 9 2Gas 29 relies on overbottom pressure to be delivered to gas holder 12.
Synthetic gas enters and catalyzes and synthesizes in the tower 10,, also follows simultaneously to generate synthesis tail gas 28 with the synthetic chemical industry oil product 27 of synthetic gas by building-up reactions.
Synthesis tail gas 28 is sent in the tail gas decarbonizing tower 11 subsequently, isolates CO in tower 2Externally discharging after gas 29, residue are processed without the discharging gas 31 of greenhouse gases so realizes the discharging of integrated artistic zero greenhouse gases.
Synthetic gas decarbonizing tower 9 and tail gas decarbonizing tower 11 isolated CO 2Gas 29 enters gas holder 12 together, by main vaporized chemical import 20 and auxiliary vaporized chemical import 16 places that are delivered to vapourizing furnace 1 behind the gas blower 13, the circulation of so gasifying.

Claims (4)

1. biomass fuel carbonic acid gas circulation anaerobic equipment for gasification, comprise vapourizing furnace (1), afterheat heat exchanger (2), waste heat boiler (3), tornado dust collector (4), scrubber tower (5), transformationreation tower (7), thionizer (8), synthetic gas decarbonizing tower (9), catalyze and synthesize tower (10) and tail gas decarbonizing tower (11), it is characterized in that:
The syngas outlet (18) of described vapourizing furnace (1) links to each other with the thermal medium input terminus of afterheat heat exchanger (2), the thermal medium output terminal of described afterheat heat exchanger (2) links to each other with the thermal source input terminus of waste heat boiler (3), the thermal source output terminal of described waste heat boiler (3) links to each other with the inlet end of tornado dust collector (4), the outlet side of described tornado dust collector (4) links to each other with the import of scrubber tower (5), the outlet of described scrubber tower (5) links to each other with the inlet mouth of transformationreation tower (7) by compressor (6), and the steam output end of described waste heat boiler (3) links to each other with the steam-in of transformationreation tower (7);
The air outlet of described transformationreation tower (7) links to each other with the input terminus of thionizer (8), the output terminal of described thionizer (8) links to each other with the input aperture of synthetic gas decarbonizing tower (9), the delivery port of described synthetic gas decarbonizing tower (9) links to each other with the material inlet that catalyzes and synthesizes tower (10), the described by product outlet that catalyzes and synthesizes tower (10) links to each other the CO of described tail gas decarbonizing tower (11) and synthetic gas decarbonizing tower (9) with the tail gas import of tail gas decarbonizing tower (11) 2Outlet links to each other with the cold medium input terminus of afterheat heat exchanger (2) simultaneously, and the cold medium output terminal of described afterheat heat exchanger (2) links to each other with the vaporized chemical import of vapourizing furnace (1).
2. biomass fuel carbonic acid gas circulation anaerobic equipment for gasification according to claim 1 is characterized in that: the CO of described tail gas decarbonizing tower (11) and synthetic gas decarbonizing tower (9) 2Outlet links to each other with the import of gas holder (12) simultaneously, and the outlet of described gas holder (12) links to each other with the cold medium input terminus of afterheat heat exchanger (2) by gas blower (13).
3. biomass fuel carbonic acid gas circulation anaerobic equipment for gasification according to claim 2 is characterized in that: the import of described gas holder (12) also with the CO that starts calcining furnace (32) 2Delivery port links to each other.
4. according to claim 1 and 2 or 3 described biomass fuel carbonic acid gas circulation anaerobic equipment for gasification, it is characterized in that: the inner chamber bottom of described vapourizing furnace (1) is provided with air distribution plate (19), be provided with main vaporized chemical import (20) on the furnace wall of described air distribution plate (19) below, be provided with auxiliary vaporized chemical import (16) on the furnace wall of described air distribution plate (19) top, be provided with outside auxiliary energy entrance (15) on the furnace wall of described auxiliary vaporized chemical import (16) top, the cold medium output terminal of described afterheat heat exchanger (2) is divided into two-way, one the tunnel links to each other with main vaporized chemical import (20), and another road links to each other with auxiliary vaporized chemical import (16).
CN2012203927006U 2012-08-09 2012-08-09 Biomass fuel carbon dioxide cycle no-oxygen equipment Expired - Fee Related CN202829964U (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2014023149A1 (en) * 2012-08-09 2014-02-13 武汉凯迪工程技术研究总院有限公司 Method and device for biomass gasification by cycling of carbon dioxide without oxygen

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2014023149A1 (en) * 2012-08-09 2014-02-13 武汉凯迪工程技术研究总院有限公司 Method and device for biomass gasification by cycling of carbon dioxide without oxygen

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Granted publication date: 20130327

Termination date: 20210809