CN101671578B - Combustible material plasma high-temperature gasification technique and equipment thereof - Google Patents
Combustible material plasma high-temperature gasification technique and equipment thereof Download PDFInfo
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- CN101671578B CN101671578B CN 200910272197 CN200910272197A CN101671578B CN 101671578 B CN101671578 B CN 101671578B CN 200910272197 CN200910272197 CN 200910272197 CN 200910272197 A CN200910272197 A CN 200910272197A CN 101671578 B CN101671578 B CN 101671578B
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- 239000000463 material Substances 0.000 title claims abstract description 77
- 238000002309 gasification Methods 0.000 title claims abstract description 71
- 238000000034 method Methods 0.000 title claims abstract description 43
- 239000000571 coke Substances 0.000 claims abstract description 69
- 239000000446 fuel Substances 0.000 claims abstract description 44
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 29
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 27
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 26
- 239000007787 solid Substances 0.000 claims abstract description 18
- 239000002893 slag Substances 0.000 claims abstract description 17
- 239000007789 gas Substances 0.000 claims description 79
- 230000003647 oxidation Effects 0.000 claims description 28
- 238000007254 oxidation reaction Methods 0.000 claims description 28
- 230000008569 process Effects 0.000 claims description 28
- 238000006243 chemical reaction Methods 0.000 claims description 21
- 238000000926 separation method Methods 0.000 claims description 17
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 14
- 229910052760 oxygen Inorganic materials 0.000 claims description 14
- 239000001301 oxygen Substances 0.000 claims description 14
- 238000005516 engineering process Methods 0.000 claims description 13
- 239000000203 mixture Substances 0.000 claims description 13
- 238000002844 melting Methods 0.000 claims description 12
- 230000008018 melting Effects 0.000 claims description 12
- 239000008187 granular material Substances 0.000 claims description 11
- 238000005507 spraying Methods 0.000 claims description 11
- 239000002028 Biomass Substances 0.000 claims description 10
- 238000010504 bond cleavage reaction Methods 0.000 claims description 10
- 239000002245 particle Substances 0.000 claims description 10
- 230000007017 scission Effects 0.000 claims description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 238000010891 electric arc Methods 0.000 claims description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 5
- 239000003546 flue gas Substances 0.000 claims description 5
- 238000010438 heat treatment Methods 0.000 claims description 5
- 230000008676 import Effects 0.000 claims description 3
- 238000002347 injection Methods 0.000 claims description 3
- 239000007924 injection Substances 0.000 claims description 3
- 239000011236 particulate material Substances 0.000 claims description 3
- 239000010802 sludge Substances 0.000 claims description 3
- 238000005336 cracking Methods 0.000 abstract description 6
- 230000004927 fusion Effects 0.000 abstract description 6
- 239000012535 impurity Substances 0.000 abstract description 4
- 238000007599 discharging Methods 0.000 abstract description 2
- 239000007800 oxidant agent Substances 0.000 abstract 2
- 239000004480 active ingredient Substances 0.000 abstract 1
- 239000011269 tar Substances 0.000 description 29
- 229910052799 carbon Inorganic materials 0.000 description 10
- 239000003245 coal Substances 0.000 description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 9
- 238000011161 development Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 239000011280 coal tar Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 238000011160 research Methods 0.000 description 3
- 230000009466 transformation Effects 0.000 description 3
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 239000003034 coal gas Substances 0.000 description 2
- 239000004615 ingredient Substances 0.000 description 2
- 239000003380 propellant Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000007233 catalytic pyrolysis Methods 0.000 description 1
- 239000011285 coke tar Substances 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000001627 detrimental effect Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000012840 feeding operation Methods 0.000 description 1
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- 230000010354 integration Effects 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- -1 moisture content Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000010902 straw Substances 0.000 description 1
- 230000004083 survival effect Effects 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
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Abstract
The invention relates to a combustible material plasma high-temperature gasification technique and equipment thereof. The technique comprises the following steps: firstly, laying a coke bed layer at the bottom part of a gasification furnace; secondly, putting the combustible material, a fluxing agent and an extra coke on the coke bed layer continuously to form a fuel bed layer; then injecting a primary oxidizing agent, starting a first-stage plasma torch to generate high temperature and high heat, forming a fusing zone at the joint of the coke bed layer and the fuel bed layer, forming a gasifying zone above the fusion zone, gasifying the combustible material to generate crude synthesis gas, and discharging the generated fused slag from the bottom part of the gasification furnace; then introducing the crude synthesis gas into a gas-solid separator for removing impurities to obtain purified synthesis gas; and finally introducing the purified synthesis gas into a detarrer, injecting a secondary oxidizing agent, starting a second-stage plasma torch to generate high temperature and high heat, cracking residual tar therein to obtain fined synthesis gas. The equipment mainly comprises three parts, namely the gasification furnace, the gas-solid separator and the detarrer. The fuel has good adaptability, high gasification efficiency, few tar content in the synthesis gas and high active ingredient.
Description
Technical field
The present invention relates to combustible material is carried out the high-temperature gasification Treatment Technology, refer to a kind of combustible material plasma high-temperature gasification technique and equipment thereof particularly.
Technical background
Along with the natural increase and the sustainable development of economy of population, but promptly reducing, cause the China and even the world all to have long-term and huge energy demand and supply pressure as the conventional high-quality fossil oil in main energy sources source.In the face of the megatrend of global integration, the economy of China's highly energy-consuming, low efficiency will face the baptism of how in international competition, to try to achieve survival and development.Utilizing on the problem of fire coal, biomass, MSW flammable raw materials such as (MSW), energy-saving and cost-reducing having become promotes the most important of national economy, social sustainable development and the most effective one of means.
Obtain this rudimentary form of utilizing that falls behind relatively of the energy with the combustible material burning and compare, the synthetic gas that the combustible material gasification is obtained has higher value, and its purposes is also more extensive.In the combustible material gasification technology; The coal-fired gasification technology of high heating value has just realized suitability for industrialized production abroad as far back as nineteen fifties; So far successfully developed wide to the coal suitability, vapor pressure is high, gasification efficiency is high, pollute few various coal gasifying process, wherein representative have fixed bed gasification technology, fluidized bed gasifying process and an entrained flow gasification technology etc.The gas-solid counter current contact mode of fixed bed gasification process using, fuel adds from top of gasification furnace, and vaporized chemical gets into from the vapourizing furnace bottom, and the coal gas of generation is drawn from furnace roof, and solid-state or liquid lime-ash is then discharged from furnace bottom.Fluidized bed gasifying process adopts the gas-solid mixed flow way of contact; Fuel feeds from the vapourizing furnace bottom; Vaporized chemical adds from vapourizing furnace bottom and bottom, and the first coal gas of generation is introduced gas-solid separator separates by vapourizing furnace top, and the lime-ash of generation is then discharged by the hearth deslagging pipe.The gas-solid following current way of contact of entrained flow gasification process using, vaporized chemical and fuel are sent into vapourizing furnace simultaneously and are reacted, and the first synthetic gas and the lime-ash of generation are discharged vapourizing furnace simultaneously.Practice for many years confirms that these gasifying process have good effect to the gasification of fire coal; But because characteristics such as its moisture content to fuel, ash, fugitive constituent and ash fusion point are very sensitive; Mostly can only adapt to the very close fuel of a kind of fuel or physicochemical property with a kind of gasifying process, so its application has received very big restriction.
The gasification technology of biomass and MSW low calorie fuelss such as (MSW) then is a kind of new energy technology that occurs this century; Development has faster also been arranged so far; Especially a large amount of research has been carried out to the gasifying biomass generation technology in Europe and America, and has obtained suitable achievement.In recent years, domestic a lot of institution of higher learning and scientific research institute have also dropped into a large amount of energy to this, and adopt fixed bed or fluidized bed gasifying process that low calorie fuelss such as biomass have been carried out a large amount of gasification tests.Yet test-results is unsatisfactory, and its efficiency of carbon conversion is low, gasification efficiency is low, synthetic gas effective ingredient (CO+H
2) the defective that ratio is low, the synthetic gas calorific value is low and unstable, tar content is high very outstanding.
Studying carefully its cause, is because foregoing existing fixed bed or fluidized-bed gasification furnace can only adapt to a kind of fuel to relatively poor, a kind of vapourizing furnace of the flexibility of fuel on the one hand, causes the less stable of its operation, and efficiency of carbon conversion is lower.Be on the other hand because the composition of biomass and MSW (MSW) etc. and calorific value along with the variation of natural causes such as collection channel, season, weather instability extremely; Control to parameters in the gasifying process requires also very high; And the gasification temperature of existing fixed bed or fluidized-bed gasification furnace is generally between 800～1200 ℃; Generally between 500～800 ℃, the highest temperature out can not surpass 1000 ℃ to the temperature out of synthetic gas yet, and the low calorie fuels in this temperature range will produce tar in a large number; This is one of the most difficult product that purifies of gasifying process; Tar too much can cause line clogging and equipment contaminate, causes equipment to be difficult to the continous-stable operation, brings great difficulty for the follow-up industrial utilization of synthetic gas.Simultaneously, because deslagging temperature is low, can only adopt dry ash extraction, the efficiency of carbon conversion of vapourizing furnace is also lower.So the gasification for biomass and MSW (MSW), municipal sludge, low grade coal etc. does not still have the gasification use of the achievement, particularly biomass fuel of successful commercial exploitation still to be in the research trial stage both at home and abroad at present.
Summary of the invention
The object of the invention is exactly that combustible material plasma high-temperature gasification technique and the equipment thereof that a kind of fuel tolerance is good, gasification efficiency is high, the coal-tar middle oil composition of synthetic gas is few, effective ingredient is high will be provided.
Be to realize above-mentioned purpose, guiding theory of the present invention organically combines a plurality of process steps and is one, and each process step is cooperated each other, realizes the gasification of fuel by different level, and to impel the tar class impurity conversion in the synthetic gas be the available energy.The combustible material plasma high-temperature gasification technique that the present invention designed; Be in vapourizing furnace, utilize plasmatorch to various fire coals, biomass, MSW, municipal sludge or other combustible materials carry out high-temperature heating treatment, will be wherein organism gasification changing into synthetic gas, with the process that the ash fusing that is produced is discharged, its concrete technological process comprises the steps:
The coke granule that 1) will have high-temperature stability and a porous crack characteristic is routed to the bottom of vapourizing furnace, forms coke bed;
2) mixture of combustible material, fusing assistant and additional coke is put on the coke bed continuously, formed the fuel bed;
3) the once oxidation agent is ejected in the vapourizing furnace; The one-level plasmatorch that starts on the vapourizing furnace produces high-temperature plasma electric arc, makes the burning of part of coke and combustible material, forms melting zone in the junction of coke bed and fuel bed; The high-temperature flue gas that burning is generated is up; High-temperature gasification is carried out to the fuel bed in gasification zone on melting zone top, and making organism Pintsch process wherein is CO and H2, and the crude synthesis gas that is obtained is outlet output from vapourizing furnace top; Inorganics ash is wherein then formed slag by high temperature melting, and flows to the discharge of vapourizing furnace bottom through the hole of coke bed;
4) crude synthesis gas that obtained is imported in the gas-solid separator, wherein macrobead ash and coke granule are separated, and the gasification zone of sending back in the vapourizing furnace circulates again, obtain clean synthetic gas simultaneously;
5) the clean synthetic gas that is obtained is introduced except that in the tar device; And injection secondary oxidation agent in removing the tar device; Start the secondary plasmatorch that removes on the tar device simultaneously and produce high-temperature plasma electric arc, make a small amount of coke granule residual in the clean synthetic gas and tar class material Pintsch process be converted into CO, H
2, CH
4And CO
2, finally obtain smart synthetic gas.
Above-mentioned steps 1) in, the particle diameter of coke is 120～180mm, and this particle diameter can guarantee the ventilation property of coke bed, makes it be not easy to harden.And the coke carbon content in this particle size range is high, porosity is big; Can discharge lot of energy when at high temperature burning; Help the stable of coke bed temperature, the high-temperature liquid state slag can flow out through the hole of coke smoothly, and the carbon granule of combustible material but can not pass through coke bed; Thereby, improved the transformation efficiency of carbon by high-temperature gasification.The Thickness Design of coke bed is 800～1500mm, and this thickness can guarantee the stable and filtering feature of coke bed, and can adapt to the variation of combustible material characteristic better.
Above-mentioned steps 2) in, the particle diameter of combustible material, fusing assistant and additional coke is less than or equal to 150mm, and is corresponding with the particle diameter of coke bed.The addition of solubility promoter accounts for 1～3% of combustible material weight; This weight percent is to confirm according to the ash characteristics of gasification combustible material; When adopting the combustible material of gasification ash fusion point height, the mobile difference of lime-ash,, can reach the ash fusion point that reduces combustible material through in vapourizing furnace, adding the solubility promoter that accounts for combustible material weight 1～3%; Improve the mobile effect of molten ash, thereby the assurance molten slag can be discharged vapourizing furnace smoothly.Solubility promoter can be selected Wingdale for use.Because the coke in the coke bed is constantly consumed in gasification; In order to keep the stable of coke bed; Need constantly in vapourizing furnace, to replenish coke, the addition that replenishes coke accounts for 3～5% of combustible material weight, and the thickness of fuel bed is 2500～3000mm; Can guarantee the continous-stable of gasification like this, improve the flexibility that vapourizing furnace changes combustible material moisture content, ash.
Above-mentioned steps 3) in; The temperature of melting zone is preferably at 3000～5000 ℃; This temperature can guarantee to melt the HMP ash in the combustible material; And the high-temperature flue gas that melting zone produces can be strengthened the heat transfer to the fuel bed, reaches the combustible material rapid heating, be rapidly heated, cracked effect fast.The temperature of gasification zone to satisfy the hot environment of organism gasification reaction, improves gasification reaction speed preferably at 1700～2000 ℃, reduces the generation of coal-tar middle oil type of material of gasification.
Above-mentioned steps 3) in, the temperature of crude synthesis gas in the exit, top of vapourizing furnace is controlled at 1000～1250 ℃, to guarantee the abundant cracking of tar class material, reduces the content of coal-tar middle oil type of material of crude synthesis gas.Slag is controlled at 1650～1700 ℃ at the deslagging temperature of vapourizing furnace bottom, so that slag is in molten state, guarantees that molten slag has reasonable flowability, guarantees that the vapourizing furnace deslagging is smooth and easy.
Above-mentioned steps 3) in, the lift velocity of crude synthesis gas is controlled at 0.8～1.0m/s, and the residence time of crude synthesis gas in vapourizing furnace is controlled at 10～15s, and the lower lift velocity and the long residence time can guarantee the cracking of trying one's best of the tar in the crude synthesis gas.Simultaneously, the high-carbon transformation efficiency can be significantly carried in the minimizing of coke granule and ash granule content in the crude synthesis gas, but also helps the purification of follow-up crude synthesis gas.
Above-mentioned steps 3) and in the step 5), oxygen, oxygen-rich air, air, water vapor or its combination are selected in once oxidation agent and secondary oxidation agent; The spraying pressure of selected oxygen, oxygen-rich air, air is 33000～36000Pa; Selected water vapor is 250～350 ℃ a superheated vapour, and spraying pressure is 0.4～0.5Mpa.Control above-mentioned spraying pressure, can make oxygenant overcome the resistance of oxidize nozzle, the while also can overcome the resistance of fuel bed, guarantees that oxygenant penetrates combustible material, contacts well with material, guarantees all even stable of temperature field in furnace, airflow field that gasify.
Above-mentioned steps 5) in, will be heated to 1200～1400 ℃ except that the clean synthetic gas in the tar device, it is that 0.5Mpa, temperature are 350 ℃ superheated vapour that spraying pressure is selected in the secondary oxidation agent.This spraying pressure has guaranteed that the secondary oxidation agent that sprays into can mix with clean synthetic gas fully, adds strong disturbance, can reduce the cracked caloric receptivity simultaneously.In the cracking process of tar, superheated vapour can with the rapid reaction of tar composition, generate CO, H
2, CH
4, CO
2Deng gas, can effectively reduce sooty like this and produce, can tar be converted into inflammable gas again, improve the output of synthetic gas.For example, reactions takes place in the naphthalene in the tar when 1200～1400 ℃ of catalytic pyrolysiss:
C
10H
8+10H
2O→10CO+14H
2
C
10H
8+20H
2O→10CO
2+24H
2
C
10H
8+10H
2O→2CO+4CO
2+6H
2+4CH
4
Can know that by above-mentioned chemical reaction superheated vapour is very beneficial for the generation of coke tar cracking and inflammable gas, thereby improve gasification efficiency.
For realizing the custom-designed combustible material plasma high-temperature gasification equipment of above-mentioned technology, mainly by vapourizing furnace, gas-solid separator with remove tar device three parts and constitute.Wherein:
Said vapourizing furnace has a vapourizing furnace housing, and the top or the upper portion side wall of vapourizing furnace housing are provided with feeding device, through feeding device can lay coke bed in the bottom of vapourizing furnace housing, laying fuel bed on coke bed; Vapourizing furnace lower part of frame sidewall is provided with one-level plasmatorch and once oxidation agent nozzle, and the one-level plasmatorch is positioned at the junction of coke bed and fuel bed, and once oxidation agent nozzle is positioned at the top of one-level plasmatorch; Also be provided with the synthetic gas output channel on the top of vapourizing furnace housing or the upper portion side wall; The bottom of vapourizing furnace housing is provided with the slag discharger.
Said gas-solid separator has a cyclonic separation cylindrical shell, and the upper gas import of cyclonic separation cylindrical shell links to each other with the synthetic gas output channel, and the bottom particulate material outlet of cyclonic separation cylindrical shell links to each other with vapourizing furnace lower part of frame returning charge mouth through the feed back pipe.
The said tar utensil that removes has a scission reaction housing, and the shell wall of scission reaction housing is provided with secondary plasmatorch and secondary oxidation agent nozzle, and the inlet end of scission reaction housing links to each other with the upper gas outlet of cyclonic separation cylindrical shell.
Compared with prior art, the present invention has following advantage:
One of which, the present invention makes gasification efficiency and efficiency of carbon conversion significantly improve, synthetic gas available gas (CO+H at vapourizing furnace with except that adopting plasmatorch to provide gasification required high temperature in the tar device
2) the composition ratio obviously improves, thereby make synthetic gas be suitable for generating and the synthetic application of chemical industry;
Its two, the vapourizing furnace that gasifying process of the present invention adopts adopts atmospheric operation, feeding device and slag discharging device are simple in structure, easily realization;
Its three, the gasifying process that the present invention adopts is good to the flexibility of fuel, the fuel pre-treatment is simple, the feed of wide-size distribution, combustible materials such as gasifiable all kinds of fire coals, biomass, MSW and mud, and the above-mentioned multiple propellant combination that can gasify simultaneously;
Its four, gasifying process of the present invention adopts high-temperature gasification, through gas-solid separation with after removing tar and handling, the ash content of coal is low in the smart synthetic gas of preparation, its ash content of coal is less than 3～5g/Nm
3, smart synthetic gas does not contain tar class detrimental impurity.
Its five, gasifying process of the present invention adopts high-temperature gasification, through gas-solid separation with after removing tar and handling, efficiency of carbon conversion is high, generally can reach more than 99.5%.
Its six, gasifying process of the present invention adopts the high-temperature liquid state deslagging, but the lime-ash vitrifying handle, realize cindery harmless comprehensive utilization.
They are seven years old; Gasifying process of the present invention is provided with coke bed in vapourizing furnace; Apply the plasma arc of adjustable power in coke bed and fuel bed junction; Thereby make vapourizing furnace good to the flexibility of characteristic variations such as fuel composition, moisture content, ash and calorific value, when the characteristic of fuel changes when influencing gasification result, intake that can be through the adjustment plasmatorch and add or reduce the steady running that the quantity of replenishing coke guarantees vapourizing furnace.
In sum; The present invention has little, the characteristics such as technology is simple, efficiency of carbon conversion is high, synthetic gas available gas composition ratio height, equipment serviceability height of investment; The present invention can adapt to various dissimilar combustible materials; And realized cindery harmless treatment, the tar class impurity in the clean synthetic gas that after gas-solid the separation, generates further is cracked into available gas, has greatly improved the transformation efficiency of combustible material; Thereby effectively prevented because the technical problem that the gasifying process that tar pickup blocking pipe and equipment cause can not carry out has continuously improved the economic benefit of power plant.
Description of drawings
Accompanying drawing is a kind of structural representation of combustible material plasma high-temperature gasification equipment.
Embodiment
Below in conjunction with accompanying drawing and specific embodiment equipment of the present invention and technology are done further to specify:
Combustible material plasma high-temperature gasification equipment shown in the figure is mainly by vapourizing furnace, gas-solid separator with remove tar device three parts and constitute.Wherein, vapourizing furnace has a vapourizing furnace housing 3, and the top of vapourizing furnace housing 3 is provided with feeding device 4, and the length that feeding device 4 stretches in the vapourizing furnace can be adjusted according to the capacity of actual vapourizing furnace.Can lay coke bed 12, laying fuel bed 13 on coke bed 12 in the bottom of vapourizing furnace housing 3 through feeding device 4.
The lower sides of vapourizing furnace housing 3 is provided with one-level plasmatorch 1 and once oxidation agent nozzle 2.In order to guarantee the even of temperature field, this one-level plasmatorch 1 is provided with 2～6, and along circumferentially being distributed on the lower sides of vapourizing furnace housing 3, the workplace of this one-level plasmatorch 1 is corresponding to the junction of coke bed 12 with fuel bed 13 through flange.Vapourizing furnace in use can be adjusted the input electric power of one-level plasmatorch 1 according to the characteristic variations of combustible material.In general, the total energy of plasmatorch is about 0.8～5% of combustible material total energy, and for the combustible material of low moisture content, low ash, high heating value, the power of plasmatorch can be less, otherwise can be bigger.
Once oxidation agent nozzle 2 is positioned at the top of one-level plasmatorch 1.This once oxidation agent nozzle 2 can be provided with 2～4 layers, and every layer of a plurality of nozzle are along circumferentially being distributed on the lower sides of vapourizing furnace housing 3, to guarantee that injection evenly.Vapourizing furnace in use can be controlled the crude synthesis gas temperature of vapourizing furnace outlet through the amount of feeding of oxygenant in the adjustment once oxidation agent nozzle 2.The composition of oxygenant can be used according to downstream industry the requirement of synthetic pneumatolytic part is prepared, and generally adopts oxygen, oxygen-rich air, air and water vapor etc., also can be several kinds and be used.The top of vapourizing furnace housing 3 is provided with synthetic gas output channel 5.The bottom of vapourizing furnace housing 3 is provided with slag discharger 11.
Gas-solid separator has a cyclonic separation cylindrical shell 9, and the upper gas import of cyclonic separation cylindrical shell 9 links to each other with synthetic gas output channel 5, and the bottom particulate material outlet of cyclonic separation cylindrical shell 9 links to each other with the bottom returning charge mouth of vapourizing furnace housing 3 through feed back pipe 10.
Removing the tar utensil has a scission reaction housing 6, and the shell wall of scission reaction housing 6 is provided with secondary plasmatorch 7 and secondary oxidation agent nozzle 8, and the inlet end of scission reaction housing 6 links to each other with the upper gas outlet of cyclonic separation cylindrical shell 9.The oxygenant that high temperature that provides through secondary plasmatorch 7 and secondary oxidation agent nozzle 8 provide; Can further handle the clean synthetic gas that comes out from cyclonic separation cylindrical shell 9; Make tar class material cracking wherein be converted into available gas, thereby obtain smart synthetic gas.
The technological process of above-mentioned combustible material plasma high-temperature gasification equipment is such:
At first, be the industrial coke of 120～180mm or the bottom that the metallurgical coke particle is routed to vapourizing furnace with particle diameter, forming thickness is the coke bed 12 of 800～1500mm.When gasifier operation, should confirm the thickness of coke bed 12 according to the characteristic of combustible material, simultaneously also should according to the factors such as quality of synthetic gas at any time the thickness of STRENGTH ON COKE bed 12 adjust.
Then, the mixture of combustible material, fusing assistant and additional coke is put on the coke bed 12 continuously, forming thickness is the fuel bed 13 of 2500～3000mm.The thickness of this fuel bed 13 should be adjusted according to the characteristic of combustible material when gasifier operation, also should adjust the thickness of fuel bed 13 at any time according to the factors such as quality of synthetic gas simultaneously.The particle diameter of above-mentioned combustible material, fusing assistant and additional coke should be less than or equal to 150mm; The addition of solubility promoter accounts for 1～3% of combustible material weight; Concrete addition is adjusted according to the ash characteristics and the grey deal of combustible material; Can discharge vapourizing furnace smoothly with the assurance slag, the addition that replenishes coke accounts for 3～5% of combustible material weight.In concrete feeding operation; Can select furnace roof feed (like present embodiment); Also can be employed in the mode that the vapourizing furnace upper side feeds; But no matter which kind of feed-type all should guarantee the continuity of feed and the homogeneity that the interior combustible material of stove distributes, and reduces because of the disturbance of feed to the inner flue gas of the stove flow field.During gasifier operation, continuously add combustible material through feeding device 4, the mixture of fusing assistant and additional coke is kept the stable of fuel bed 13 height.The combustible material that adds can be single fuel, also can be the propellant combination of various materials different in kind, as being single coal, agricultural crop straw, municipal wastes, also can be the mixture of these fuel.
Secondly; To be ejected in the vapourizing furnace by the once oxidation agent of oxygen, oxygen-rich air, air, water vapor or combinations thereof; The one-level plasmatorch 1 that starts on the vapourizing furnace produces high-temperature plasma electric arc; Making the burning of part of coke and combustible material, is 3000～5000 ℃ melting zone in the junction formation temperature of coke bed 12 and fuel bed 13, and the high-temperature flue gas that burning is generated is up; High-temperature gasification is carried out to fuel bed 13 in the gasification zone that at the melting zone upper temp is 1700～2000 ℃, and making organism Pintsch process wherein is CO and H
2, the crude synthesis gas that is obtained is outlet output from vapourizing furnace top, and its exit temperature is 1000～1250 ℃.The ash content of coal is 30～50g/Nm in this crude synthesis gas
3, tar content is also higher.Inorganics ash in the combustible material is then formed slag by high temperature melting, and flows to the discharge of vapourizing furnace bottom through the hole of coke bed 12, and its deslagging temperature is 1650～1700 ℃.Than higher combustible material, reduce cindery temperature of fusion for ash fusion point, the flowability of adjustment slag through in combustible material, adding solubility promoter (being generally Wingdale).Discharge the water quenched slag vitrifying of vapourizing furnace, realize innoxious and fully utilize.In the present embodiment, select for use the spraying pressure of oxygen, oxygen-rich air, air to be controlled at 33000～36000Pa; Adopt 250～350 ℃ superheated vapour when selecting water vapor for use, spraying pressure is controlled at 0.4～0.5Mpa, is evenly distributed to guarantee the oxygenant that gets into vapourizing furnace housing 3.For combustible material is fully gasified, the lift velocity of crude synthesis gas is controlled between 0.8～1.0m/s, and the residence time of crude synthesis gas in vapourizing furnace is controlled between 10～15s.
Once more; The crude synthesis gas that obtained is imported in the cyclonic separation cylindrical shell 9 of gas-solid separator, wherein macrobead ash and coke granule are separated, and circulate again in the gasification zone of sending vapourizing furnace housing 3 back to; Obtain clean synthetic gas simultaneously, the gas the ash content of coal in this clean synthetic gas is 3～5g/Nm
3
At last, the clean synthetic gas that is obtained is introduced except that in the scission reaction housing 6 of tar device, and in it, sprayed the secondary oxidation agent through secondary oxidation agent nozzle 8, the secondary oxidation agent is 350 ℃ superheated vapour preferably, and spraying pressure is 0.5Mpa.Start secondary plasmatorch 7 simultaneously and produce high-temperature plasma electric arc; Clean synthetic gas is heated to 1200～1400 ℃; And the speed of controlling clean synthetic gas makes it stop 2～15 seconds in the high-temperature zone, makes a small amount of coke granule residual in the clean synthetic gas and tar class material Pintsch process be converted into CO, H
2, CH
4And CO
2, finally obtain smart synthetic gas.
Claims (9)
1. combustible material plasma high-temperature gasification technique; Be in vapourizing furnace, utilize plasmatorch to various fire coals, biomass, MSW, municipal sludge or other combustible materials carry out high-temperature heating treatment, will be wherein organism gasification changing into synthetic gas, with the process that the ash fusing that is produced is discharged, it is characterized in that: this technology comprises the steps:
The coke granule that 1) will have high-temperature stability and a porous crack characteristic is routed to the bottom of vapourizing furnace, forms coke bed;
2) mixture of combustible material, fusing assistant and additional coke is put on the coke bed continuously, formed the fuel bed;
3) the once oxidation agent is ejected in the vapourizing furnace; The one-level plasmatorch that starts on the vapourizing furnace produces high-temperature plasma electric arc; Make the burning of part of coke and combustible material, form melting zone in the junction of coke bed and fuel bed, the high-temperature flue gas that burning is generated is up; High-temperature gasification is carried out to the fuel bed in gasification zone on melting zone top, and making organism Pintsch process wherein is CO and H
2, the crude synthesis gas that is obtained is outlet output from vapourizing furnace top; Inorganics ash is wherein then formed molten slag by high temperature melting, and flows to the discharge of vapourizing furnace bottom through the hole of coke bed; Wherein, the temperature of melting zone is 3000～5000 ℃, and the temperature of gasification zone is 1700～2000 ℃, and the temperature of crude synthesis gas in the exit, top of vapourizing furnace is 1000～1250 ℃, and slag is 1650～1700 ℃ at the deslagging temperature of vapourizing furnace bottom;
4) crude synthesis gas that obtained is imported in the gas-solid separator, wherein macrobead ash and coke granule are separated, and the gasification zone of sending back in the vapourizing furnace circulates again, obtain clean synthetic gas simultaneously;
5) the clean synthetic gas that is obtained is introduced except that in the tar device; And injection secondary oxidation agent in removing the tar device; Start the secondary plasmatorch that removes on the tar device simultaneously and produce high-temperature plasma electric arc, make a small amount of coke granule residual in the clean synthetic gas and tar class material Pintsch process be converted into CO, H
2, CH
4And CO
2, finally obtain smart synthetic gas.
2. combustible material plasma high-temperature gasification technique according to claim 1 is characterized in that: in the said step 1), the particle diameter of coke is 120～180mm, and the thickness of coke bed is 800～1500mm.
3. combustible material plasma high-temperature gasification technique according to claim 1; It is characterized in that: said step 2); The particle diameter of combustible material, fusing assistant and additional coke is less than or equal to 150mm; The addition of solubility promoter accounts for 1～3% of combustible material weight, and the addition that replenishes coke accounts for 3～5% of combustible material weight, and the thickness of fuel bed is 2500～3000mm.
4. according to claim 1 or 2 or 3 described combustible material plasma high-temperature gasification techniques, it is characterized in that: in the said step 3), the lift velocity of crude synthesis gas is 0.8～1.0m/s, and the residence time of crude synthesis gas in vapourizing furnace is 10～15s.
5. according to claim 1 or 2 or 3 described combustible material plasma high-temperature gasification techniques, it is characterized in that: in said step 3) and the step 5), oxygen, oxygen-rich air, air, water vapor or its combination are selected in once oxidation agent and secondary oxidation agent; The spraying pressure of selected oxygen, oxygen-rich air, air is 33000～36000Pa; Selected water vapor is 250～350 ℃ a superheated vapour, and spraying pressure is 0.4～0.5Mpa.
6. according to claim 1 or 2 or 3 described combustible material plasma high-temperature gasification techniques; It is characterized in that: in the said step 5); To be heated to 1200～1400 ℃ except that the clean synthetic gas in the tar device, it is that 0.5Mpa, temperature are 350 ℃ superheated vapour that spraying pressure is selected in the secondary oxidation agent.
7. combustible material plasma high-temperature gasification equipment that is used to realize the said technology of claim 1 mainly by vapourizing furnace, gas-solid separator with remove tar device three parts and constitute, is characterized in that:
Said vapourizing furnace has a vapourizing furnace housing (3); The top of vapourizing furnace housing (3) or upper portion side wall are provided with feeding device (4), through feeding device (4) can lay coke bed (12) in the bottom of vapourizing furnace housing (3), laying fuel bed (13) on coke bed (12); The lower sides of vapourizing furnace housing (3) is provided with one-level plasmatorch (1) and once oxidation agent nozzle (2); One-level plasmatorch (1) is positioned at the junction of coke bed (12) and fuel bed (13), and once oxidation agent nozzle (2) is positioned at the top of one-level plasmatorch (1); Also be provided with synthetic gas output channel (5) on the top of vapourizing furnace housing (3) or the upper portion side wall; The bottom of vapourizing furnace housing (3) is provided with slag discharger (11);
Said gas-solid separator has a cyclonic separation cylindrical shell (9); The upper gas import of cyclonic separation cylindrical shell (9) links to each other with synthetic gas output channel (5), and the bottom particulate material outlet of cyclonic separation cylindrical shell (9) links to each other with the bottom returning charge mouth of vapourizing furnace housing (3) through feed back pipe (10);
The said tar utensil that removes has a scission reaction housing (6); The shell wall of scission reaction housing (6) is provided with secondary plasmatorch (7) and secondary oxidation agent nozzle (8), and the inlet end of scission reaction housing (6) links to each other with the upper gas outlet of cyclonic separation cylindrical shell (9).
8. combustible material plasma high-temperature gasification equipment according to claim 7 is characterized in that: said one-level plasmatorch (1) is provided with 2～6, along circumferentially being distributed on the lower sides of vapourizing furnace housing (3).
9. according to claim 7 or 8 described combustible material plasma high-temperature gasification equipment, it is characterized in that: said once oxidation agent nozzle (2) is provided with 2～4 layers, and every layer of a plurality of nozzle are along circumferentially being distributed on the lower sides of vapourizing furnace housing (3).
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