CN1935951A - High temperature gasifying apparatus for solid carbon raw material - Google Patents
High temperature gasifying apparatus for solid carbon raw material Download PDFInfo
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- CN1935951A CN1935951A CN 200610124571 CN200610124571A CN1935951A CN 1935951 A CN1935951 A CN 1935951A CN 200610124571 CN200610124571 CN 200610124571 CN 200610124571 A CN200610124571 A CN 200610124571A CN 1935951 A CN1935951 A CN 1935951A
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 59
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 59
- 239000007787 solid Substances 0.000 title claims abstract description 24
- 239000002994 raw material Substances 0.000 title claims description 46
- 230000009467 reduction Effects 0.000 claims abstract description 95
- 238000002309 gasification Methods 0.000 claims abstract description 59
- 239000002893 slag Substances 0.000 claims abstract description 44
- 238000001816 cooling Methods 0.000 claims abstract description 27
- 238000002485 combustion reaction Methods 0.000 claims description 62
- 238000006243 chemical reaction Methods 0.000 claims description 34
- 239000000446 fuel Substances 0.000 claims description 27
- 238000004891 communication Methods 0.000 claims description 24
- 239000007921 spray Substances 0.000 claims description 17
- 239000003795 chemical substances by application Substances 0.000 claims description 8
- 239000002245 particle Substances 0.000 claims description 8
- 238000002347 injection Methods 0.000 claims description 5
- 239000007924 injection Substances 0.000 claims description 5
- 238000004804 winding Methods 0.000 claims description 5
- 239000007788 liquid Substances 0.000 abstract description 16
- 239000000463 material Substances 0.000 abstract description 11
- 239000000843 powder Substances 0.000 abstract description 7
- 230000004992 fission Effects 0.000 abstract 1
- 238000006722 reduction reaction Methods 0.000 description 84
- 239000002956 ash Substances 0.000 description 27
- 239000007789 gas Substances 0.000 description 23
- 239000000126 substance Substances 0.000 description 15
- 238000013461 design Methods 0.000 description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 11
- 238000000034 method Methods 0.000 description 10
- 230000004927 fusion Effects 0.000 description 8
- 230000004224 protection Effects 0.000 description 7
- 230000015572 biosynthetic process Effects 0.000 description 6
- 230000007774 longterm Effects 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- 238000012423 maintenance Methods 0.000 description 5
- 230000002829 reductive effect Effects 0.000 description 5
- 239000011819 refractory material Substances 0.000 description 5
- 238000003786 synthesis reaction Methods 0.000 description 5
- 230000009970 fire resistant effect Effects 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
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- 239000002737 fuel gas Substances 0.000 description 3
- 238000009434 installation Methods 0.000 description 3
- 238000002844 melting Methods 0.000 description 3
- 230000008018 melting Effects 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 239000002028 Biomass Substances 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 230000002950 deficient Effects 0.000 description 2
- 229910052500 inorganic mineral Inorganic materials 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000011707 mineral Substances 0.000 description 2
- 239000010813 municipal solid waste Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 208000035126 Facies Diseases 0.000 description 1
- 229910000805 Pig iron Inorganic materials 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003818 cinder Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 238000002513 implantation Methods 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
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- 230000003647 oxidation Effects 0.000 description 1
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- 238000012545 processing Methods 0.000 description 1
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- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur 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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- Processing Of Solid Wastes (AREA)
Abstract
The invention relates to high temperature gasification device for solid carbon containing material. It includes burning chamber, combined type burner, reduction chamber, and powder carbon containing material jet nozzle on the wall of the reduction chamber. The device adopts fission type structure to separate the reduction chamber from burning chamber. The bottom of the latter is set liquid state slag bath and hole. The bottom of the former is set accident slag bath and hole. And connecting channel is set between them, which is set crust blocks cooling control device. The former is also set diversion structure which adopts circularity and includes center vertical open-end tube, bell jar shape shell body, and circularity channel.
Description
Technical field
The present invention relates to a kind of high-temperature gasification device of solid carbon raw material, especially for the high-temperature gasification equipment of being made inflammable gas, synthesis gas and reducing gas by recyclable fuel, mineral fuel, biomass or rubbish etc.The present invention can use in power facility, chemical industry and metallurgy industry, to make inflammable gas, synthesis gas and reducing gas efficiently, is used for engine, building-up process, ore reduction and pig iron production etc.
Background technology
Have considerable gasification process at present, they can be divided into fixed bed gasification, fluidized-bed gasification and entrained flow gasification three major types basically.
In the moving-bed gasification stove, oxygenant is blown into the vapourizing furnace bottom, and the thick fuel gas of generation moves up by the fixed fuel bed, and with the feed consumption of implantation bottom, solid fuel moves down gradually.The qualification characteristic of moving-bed is countercurrent flow, when slightly fuel gas stream is through bed, and the feed cooling of being come in, and feed is dried and slough volatile matter.Therefore temperature is significantly different up and down in vapourizing furnace, and bottom temp is 1000 ℃ or higher, about 500 ℃ of head temperature.Fuel removes the fuel gas that volatile matter means output and contains a large amount of tar ingredients and methane in gasification, make follow-up treatment process complexity.
The important feature of fluidized-bed gasification furnace is to allow the raw material ash overheated, is bonded together the defluidization that causes fluidized-bed with the anti-gray fusing, generally uses air as oxygenant, keeps temperature to be lower than 1000 ℃, is applicable to the material gasification that ash fusion point is high.
The main characteristic of airflow bed gasification furnace is that temperature is very high, and evenly, the fuel stays time in the vapourizing furnace is very short, owing to this reason, the solid that feeds vapourizing furnace must be by segmentation and homogenizing, separate so generally carried out low-temperature pyrolysis before raw material enters reactor, the high temperature in the airflow bed gasification furnace makes the ash dissolving in the fuel, and discharges as molten molten slag.
Comprehensively described, the Working environment of moving-bed gasification stove and fluidized-bed gasification furnace is relative gentle, performance requriements to material is also lower, corresponding investment is also just low, but throughput and quality product are relatively poor, airflow bed gasification furnace has characteristics such as the big and synthetic gas quality height of wide, the single stove throughput of the fuel scope of application, but to the requirement height of material, investment is high.If overcome this shortcoming of airflow bed gasification furnace, will be the first-selection of gasifying process.
No matter be the burning or the gasification reduction reaction of carbonaceous particles, carrying out along with reaction, ash is more and more, speed of reaction is more and more lower, but under identical temperature, and combustionvelocity is than high many of gasification reduction rate, carry the high-carbon transformation efficiency, have several ways optional: the one, improve temperature of reaction, the 2nd, improve the residence time of raw material in stove, the 3rd, the carbon containing lime-ash that is not gasified totally reclaimed enter the combustion chamber and will remain carbon burning and fall.If improve the temperature of reaction; the life-span of refractory materials will be shortened greatly; not only increased maintenance cost; production can not long period be moved continuously; if adopt the method for water cooling tube dross protection; can improve equipment life; keep long-term operation; but have to aspect energy and the vaporized chemical demand side is made many compromises; because keep certain thickness solid-state slag blanket; water cooling tube will be taken away a lot of effective heat energy, must keep flowing of slag and discharge by additional heat simultaneously, and these measures cause a large amount of oxygen of needs; reduce the calorific value of gasifying gas; and thereby cause whole gasification exothermal efficiency low; for the low raw material of ash fusion point, this compromise is an acceptable, is beyond affordability for the high ash melting point raw material.Why present high-sulfur, high ash content, the high-ash-fusion coal of China is difficult to gasification, and reason just is this.
A common feature in above-mentioned each equipment for gasification is exactly that oxidation and reduction reaction are all carried out in same space, so, for the vapourizing furnace that adopts the refractory materials lining-up, the refractory materials of combustion zone and reduction zone bears almost same high temperature, and each maintenance almost will be changed all refractory materialss; For the vapourizing furnace that adopts the protection of water wall dross, temperature will guarantee the certain thickness of solid slag on each part water wall and the flowability of outer slag in the stove, wastes a lot of available energies, has reduced the calorific value of synthetic gas; Also be difficult in simultaneously and take to increase the raw material stroke on such vapourizing furnace, in whole space, make carbonaceous particles and the well-mixed effective measure of vaporized chemical.Even the vapourizing furnace that has is with combustion chamber and the separately design of reduction chamber, but it is not discrete fully, do not avoid above-mentioned defective, as Chinese patent 98810657.4, this patent and present the same can't really the accomplishing of air flow bed gasification burner with oxidizing reaction and reduction reaction difference temperature control, particularly the liquid slag of combustion chamber generation will be discharged through the reduction chamber, high velocity air must make the operative liquid slag spread in the reduction chamber, spray into the solid carbon powder raw material of reduction chamber inevitable with spread in the reduction chamber in liquid slag drip and mixing reunion and fall into following slag bath, the reduction efficiency of carbon conversion.Therefore, seeking a kind ofly neither increases maintenance cost, can keep long-term operation again, can improve the method and apparatus of efficiency of carbon conversion simultaneously again, makes this method and apparatus have wide the raw material scope of application and temperature range to become the task of top priority.
Summary of the invention
One of purpose of the high-temperature gasification device of solid carbon raw material of the present invention is to utilize airflow bed gasification furnace to have the big and high advantage of synthetic gas quality of wide, the single stove throughput of the fuel scope of application, overcome its requirement height to material, invest high shortcoming, and solve of the influence of the liquid slag of burning generation to reduction reaction, improve efficiency of carbon conversion; Two of purpose is increase raw material reaction strokes, makes carbonaceous particles and the well-mixed effecting reaction of vaporized chemical in whole space, improves efficiency of carbon conversion; Three of purpose is with combustion chamber and the fully separately design of reduction chamber, really accomplishes burning and reductive temperature are controlled respectively, reduces the available energy loss, improves the raw material scope of application and temperature range.
Technical scheme of the present invention: the high-temperature gasification device of solid carbon raw material of the present invention comprises that the combustion chamber reaches and its bonded cell burner, crust block cooling communication passage, reduction chamber, on the reduction locular wall powdery carbon raw material spray tube is arranged, this high-temperature gasification device adopts split-type structural, to reduce chamber and combustion chamber is divided into two independently bodies of heater, the bottom, combustion chamber is furnished with slag tap pond and slag notch, bottom, reduction chamber is furnished with accident slag bath and slag notch, is furnished with crust block cooling communication passage between combustion chamber and the reduction chamber.
The high-temperature gasification device of described solid carbon raw material, indoor being furnished with of reducing improved the flow-guiding structure that carbonaceous particles is reacted stroke and strengthened turbulence reaction intensity.
Described flow-guiding structure adopts the winding type flow-guiding structure: comprise the central vertical opening pipe that is communicated with the communication passage gasification agent inlet, diameter has the certain distance counterpart to cover on the opening top greater than the bell jar shape housing and the vertical opening tube opening of vertical opening pipe, and the chamber of reduction is separated into inside and outside multilayer circuitous channel.
Described flow-guiding structure adopts tangential rotation flow-guiding structure, promptly export and be arranged as and reduce the tangent inlet of chamber interior walls, simultaneously with pulverized fuel spray tube injection direction and the reverse layout of reduction chamber gas sense of rotation at the gasification agent inlet place of reduction chamber layout tangential flow guiding plate or with communication passage.
The high-temperature gasification device of described solid carbon raw material, the pulverized fuel spray tube on the reduction locular wall is distributed in around the wall, and spray tube can be arranged in the different positions up and down of reduction locular wall.
The high-temperature gasification device of described solid carbon raw material, the pulverized fuel spray tube outlet on the reduction locular wall are distributed in reduction indoor and outdoor multilayer circuitous channel.
The high-temperature gasification device of described solid carbon raw material, reduction exit, chamber is provided with poly-device for cooling.
The high-temperature gasification device of described solid carbon raw material, two combustion chambers of configuration, a reduction chamber.
The high-temperature gasification device of described solid carbon raw material, the communication passage between combustion chamber and the reduction chamber is from the horizontal by 5～20 ° of angles, and promptly combustor exit is lower than the reduction chamber inlet.
Advantage of the present invention:
The present invention is in line with not increasing maintenance cost, keep long-term operation, improve efficiency of carbon conversion, improving the principle of the raw material scope of application and temperature range, a kind of method and apparatus of simplification is proposed, overcome the defective of above-mentioned vapourizing furnace, especially significant to the gasification of high ash melting point carbon raw material:
1. the present invention separates combustion chamber and reduction chamber fully, by organizing strong swirling flow field to make most of liquid slag of combustion chamber generation be thrown to no longer process reduction chamber and directly discharge of the slag bath below the inflow combustion chamber on the combustion chamber wall, the liquid slag that the crust block pipe that is provided with on the communication passage further captures not burned chamber fully captures, avoid liquid slag that the combustion chamber produces to reducing the influence of indoor reduction reaction, improved efficiency of carbon conversion.
2. the present invention separates combustion chamber and reduction chamber fully, can be according to two reactions needs difference design temperature scope separately, make combustion chamber and reduction chamber respectively, the temperature of reduction chamber is regulated with the cooling control device on the passage by being arranged on connection, the environmental facies that make the reduction chamber are to gentleness, can adopt relatively inexpensive material manufacturing, help under the prerequisite that satisfies the working medium requirement, reducing equipment manufacturing cost, and the available energy loss is reduced greatly;
3. the present invention utilizes rate of combustion than the high a lot of principle of gasification rate, and designed combustion and reductive temperature environment guarantee that chamber temperature is higher than 100 ℃～200 ℃ of carbon raw material ash fusion point temperature, and the residue carbon that the reduction chamber can be reclaimed is all burnt;
4. the low material gasification of ash fusion point, combustion chamber adopt the protection of water wall dross, if the raw material type instability, it is low that ash fusion point has height to have, then adopt fire-resistant lining-up, the design philosophy that combustion chamber one is equipped with a usefulness has guaranteed system's long-term operation, and can use relatively inexpensive refractory materials;
5. set up the reduction chamber separately, can design winding type structure or cyclone structure, improve carbonaceous particles reaction stroke and strengthen turbulence reaction intensity, improved efficiency of carbon conversion;
6. the present invention has inherited that the conventional air bed gasifier fuel scope of application is wide, throughput is big and the high advantage of synthetic gas quality.
Description of drawings
Fig. 1 is a split type reaction unit structure iron of the present invention.
Fig. 2 is the A-A sectional view of reduction chamber flow-guiding structure and Fig. 1.
Fig. 3 is a reduction chamber cyclone structure synoptic diagram one.
Fig. 4 is a reduction chamber cyclone structure synoptic diagram two.
Fig. 5 is a combustion chamber the using and the reserved design diagram.
Fig. 6 is other way of realization of communication passage crust block cooling function.
Fig. 7 is an applicating flow chart of the present invention.
Embodiment
As Fig. 1: split type reaction unit of the present invention comprise combustion chamber 9 and with its bonded cell burner 1, separate with combustion chamber 9 reduction chamber 13, the spray tube 17,18,19 of multilayer pulverized fuel up and down distributes around the wall of reduction chamber 13.Between combustion chamber and the reduction chamber communication passage 25 of vaporized chemical being sent into the reduction chamber is arranged, crust block cooling control device 11 is arranged on the communication passage 25, slag bath 10 and slag notch 22, admission port 23 and spillway 24 are arranged at the bottom of combustion chamber, and there is accident slag bath 12 bottom of reduction chamber and removes cinder notch 22.1, admission port 23.1 and spillway 24.1.The reduction chamber exports 16 places and is provided with poly-device for cooling 15.Here use cell burner 1, fuel through port 4 enters the combustion chamber, and burning can enter the combustion chamber by air scoop 3 or oxygen port 7 with oxygenant, and carbon containing lime-ash and additive etc. enter from mouth 8, igniting enters from mouth 2,5 respectively with fuel and air, and 6 is flame monitor.The combination burner head adopts high temperature steel, and with cooling protections such as flow media such as air.In order to reduce thermosteresis, combustion chamber wall is provided with fire-resistant lining-up 21, also can establish water cooling tube 20, regulates chamber temperature, makes water vapour simultaneously.Combustion chamber and the communication passage 25 of reduction between the chamber are from the horizontal by angle a=5～20 °, and promptly combustor exit is lower than the reduction chamber inlet.
Reduce the indoor circuitous flow-guiding structure of guiding gas that has.
As Fig. 1, Fig. 2: flow-guiding structure comprises that the central vertical opening pipe 26 that is communicated with the communication passage gasification agent inlet and diameter have certain distance to face toward opening greater than the opening of the bell jar shape housing 14 of vertical opening pipe and vertical opening pipe 26, the coaxial opening that is covering vertical opening pipe 26 is separated into inside and outside multilayer with the chamber of reduction.Pulverized fuel spray tube outlet on the reduction locular wall is distributed in reduction indoor and outdoor multilayer space.Stain is represented air-flow to rising among Fig. 2, adds cross in the circle and represents that air-flow is circuitous downwards.
Fig. 3, Fig. 4 are the embodiment of reduction chamber cyclone structure: the cyclone structure of Fig. 3 is 25 tangentially to enter reduction chamber 13 and cause eddy flow, carbon containing powder raw material jet pipe 17 injection directions and the reverse layout of vaporized chemical eddy flow direction by entering the mouth.The cyclone structure of Fig. 4 is by adding flow deflector 30 at gasification agent inlet, making vaporized chemical tangentially enter reduction chamber 13 and cause eddy flow, carbon containing powder raw material jet pipe 17 injection directions and the reverse layout of vaporized chemical eddy flow direction.
The indoor purpose that flow-guiding structure or cyclone structure are set of reducing is to improve carbonaceous particles reaction stroke and strengthen turbulence reaction intensity, improves efficiency of carbon conversion.Therefore, for achieve the above object flow-guiding structure or cyclone structure can have a lot of forms, be not limited to the foregoing description.
Fig. 5 is a combustion chamber the using and the reserved design diagram: two combustion chambers 9,9.1,25th of 13 configurations, a reduction chamber, communication passage, the 31st, switching valve.
Fig. 6 is other way of realization synoptic diagram of communication passage cooling condensation function.
Fig. 7 is an applicating flow chart of the present invention:
Fuel and oxygenant are respectively from mouth 4,7 enter combustion chamber 9 internal combustion by burner 1, and to generate main component be the vaporized chemical of CO2 and H2O, and formation liquid slag, fall into bottom slag bath 10, vaporized chemical enters crust block cooling communication passage 25, further capture the liquid slag and the processing of lowering the temperature that catch fully not burned chamber, the lime-ash of condensing trapping is sent combustion chamber slag bath 10 back to, the vaporized chemical of slagging-off cooling enters reduction chamber 13 and carries out reduction reaction with the carbon containing powder raw material that spray tube 17 sprays into reduction chamber 13, CO2 is reduced to CO, aqueous vapour reducing is H2, synthetic gas carries the lime-ash that does not transform fully and leaves the outlet 16 of reactor reduction chamber through interchanger 29 coolings, in follow-up dust removal installation 27, capture, purification contain CO, the outlet output of the synthesis gas dust removal installation 27 of H2.
The carbon containing lime-ash of the isolated not complete reaction of fly-ash separator is sent combustion chamber 9 back to by pipeline 8 and will be remained carbon and burn, and under uniform temp and the same ash content, combustionvelocity is than big many of gasification rate, makes to burn residue carbon fast become possibility in the combustion chamber.
The burning room temp is controlled at 1300 ℃～1800 ℃; be higher than 100 ℃～200 ℃ of ash fusion point temperature; guarantee the residue carbon that reclaim the reduction chamber fully to be burnt and make the ash fusing; just because of carbonaceous particles is under uniform temp and identical ash content; combustionvelocity is than big many of gasification rate; just make us have an opportunity the residue carbon of reduction chamber is all burnt; the combustion chamber is to adopt fire-resistant lining-up or adopt the protection of water wall dross; then decide according to desired temperature and economic analysis; adopt the protection of water wall dross; guarantee long-term operation; but waste a lot of available energies, when temperature is too high, can make the very low of cold air efficiency change; but the vapourizing furnace that relative combustion and reduction are carried out at the same space, it is many that the available energy that slatterns will be lacked.As select fire-resistant lining-up for use, and can design two combustion chambers, one is equipped with a usefulness, can select the refractory materials of less expensive for use, but also will consider maintenance cost under the prerequisite of the long-term operation that guarantees total system.
Before sending into the reduction chamber, vaporized chemical, cools to 1100～1400 ℃ by crust block cooling degree control device 11 cooling that removes the gred.
Lower temperature range is selected in the reduction chamber, and reduction chamber medial temperature is controlled at 1000 ℃～1300 ℃, can guarantee under certain efficiency of carbon conversion prerequisite, makes the reduction chamber can adopt relatively inexpensive material, to save investment.The reduction chamber adopts anti-erosion heat-proof non-stick residue material to carry out winding type structure design or cyclone structure design, the carbon containing powder raw material is gradable to infeed, make full use of reduction space, chamber, it all is well-mixed making every partial reaction thing, makes reaction more abundant, and temperature distribution is relaxed more, in the reactor outlet bottom chilling apparatus 15 can be set, regulate the syngas outlet temperature, also can spray into the carbon containing powder raw material and come cooling syngas, and further produce partial synthesis gas in outer appropriate location.
Design philosophy of the present invention greatly expands the scope of application of fuel and temperature range, the Controllable Temperature of combustion chamber is built in 1300 ℃～1800 ℃, the medial temperature of reduction chamber can be controlled in 1000 ℃～1300 ℃, and ash fusion point all is suitable at 1000 ℃～1650 ℃ carbon raw material.
The present invention is directed to the high-temperature gasification reactor and proposed a kind of split type reaction unit, improved the raw material scope of application and temperature range, especially significant to the gasification of high ash melting point carbon raw material.Below enumerate embodiment and specify the present invention.
It is 1650 ℃ the recyclable fuel and the carbon raw material of making such as mineral fuel, biomass or rubbish that present embodiment adopts ash fusion point.Its embodiment is as shown in Figure 5:
Combustion gas and oxygenant enter in the independent combustion chamber through 4,7 mouthfuls respectively, burn being lower than under the situation of stoichiometric ratio, the carbon containing pulverized fuel that also burns simultaneously and reclaim from dust removal installation 27, it is complete to remain carbon burning, temperature of combustion is controlled at 1750 ℃～1800 ℃, guarantees that the ash fusing is formed liquid slag to get final product, if use higher temperature of combustion, to waste more available energies, reduce equipment life.Burner requires to have strong swirl-flow devices, liquid slag is thrown on the wall, and flows into the slag bath 10 of bottom, and the main component that burning generates is CO
2And H
2The vaporized chemical of O, vaporized chemical are through crust block communication passage 25, and crust block cooling control device 11 is caught the liquid slag condensation that not burned chamber captures fully and sent combustion chamber slag bath 10 back to, simultaneously gasification agent temperature is adjusted to about 1300 ℃.The vaporized chemical of slagging-off cooling is sent into reduction chamber 13, spray into reduction chamber carbon containing powder raw material with classification and carry out reduction reaction under 1100 ℃～1200 ℃ medial temperature, reduction generates the synthesis gas that contains CO, H2.In this temperature range, total generating rate of CO, H2 changes little, but the height of reduction temperature influences the ratio of CO and H2, so select which concrete reduction temperature, it is fixed to come according to the purposes of synthetic gas, and temperature is low more certainly, and equipment life is long more.Crust block cooling function for communication passage also can adopt other implementations, and as Fig. 6, the communication passage front portion is provided with condenser 11, and the slag of capture enters the slag bath 10 of combustion chamber, and the back is provided with aqueous vapor injection apparatus 32, further regulates gasification agent temperature.In a word, the crust block of communication passage cooling function has multiple way of realization, is not limited to the foregoing description.
Special structural design is adopted in reduction chamber 13: adopt anti-erosion, heat-proof non-stick residue material, the winding type structure is made in the chamber of reduction, fuel is gradable to infeed, the stroke that makes full use of reaction compartment and strengthen pulverized fuel improves efficiency of carbon conversion, synthetic gas carries lime-ash and flows together, exports 16 places in the reduction chamber chilling apparatus 15 is set, and temperature out is adjusted to 700 ℃～900 ℃, quenchant can be water vapor, cold synthetic gas, or even carbon containing pulverized fuel (but generating portion synthetic gas).Then, the synthetic band of gas the lime-ash that does not transform fully and is left reduction chamber 13, is admitted to hot precipitator 27, the synthetic gas that purifies enters next flow process from exporting 28, the lime-ash of collecting is sent into combustion chamber 9 by pipeline 8, will remain the intact portion of carbon and burn, and forms the slag bath 10 that liquid slag enters 9 bottoms, combustion chamber.
Core of the present invention is that reduction chamber and combustion chamber is discrete fully, the combustion chamber is communicated with communication passage between the chamber with reduction, the liquid slag that forms in the combustion chamber is directly discharged from the slag bath of combustion chamber without the reduction chamber, and according to burning and two reactions needs separately design temperature scope respectively of reducing.Therefore, every chamber and combustion chamber of will reducing is discrete, the liquid slag that forms in the combustion chamber is directly discharged from the slag bath of combustion chamber without the reduction chamber, and according to burning and two reactions needs separately design temperature scope respectively of reducing.All belong to protection scope of the present invention.
Claims (9)
1. the high-temperature gasification device of a solid carbon raw material, comprise that the combustion chamber reaches and its bonded cell burner, crust block cooling communication passage, reduction chamber, on the reduction locular wall powdery carbon raw material spray tube is arranged, it is characterized in that: this high-temperature gasification device adopts split-type structural, to reduce chamber and combustion chamber is divided into two independently bodies of heater, the bottom, combustion chamber is furnished with slag tap pond and slag notch, bottom, reduction chamber is furnished with accident slag bath and slag notch, is furnished with crust block cooling communication passage between combustion chamber and the reduction chamber.
2. the high-temperature gasification device of solid carbon raw material according to claim 1 is characterized in that: reduce the indoor flow-guiding structure that improves carbonaceous particles reaction stroke and strengthen turbulence reaction intensity that is furnished with.
3. the high-temperature gasification device of solid carbon raw material according to claim 2, it is characterized in that: flow-guiding structure adopts the winding type flow-guiding structure: comprise the central vertical opening pipe that is communicated with the communication passage gasification agent inlet, diameter has the certain distance counterpart to cover on the opening top greater than the bell jar shape housing and the vertical opening tube opening of vertical opening pipe, and the chamber of reduction is separated into inside and outside multilayer circuitous channel.
4. the high-temperature gasification device of solid carbon raw material according to claim 2, it is characterized in that: flow-guiding structure adopts tangential rotation flow-guiding structure, promptly export and be arranged as and reduce the tangent inlet of chamber interior walls, simultaneously with pulverized fuel spray tube injection direction and the reverse layout of reduction chamber gas sense of rotation at the gasification agent inlet place of reduction chamber layout tangential flow guiding plate or with communication passage.
5. the high-temperature gasification device of solid carbon raw material according to claim 1 and 2 is characterized in that: the pulverized fuel spray tube on the reduction locular wall is distributed in around the wall, and spray tube can be arranged in the different positions up and down of reduction locular wall.
6. the high-temperature gasification device of solid carbon raw material according to claim 3 is characterized in that: the pulverized fuel spray tube outlet on the reduction locular wall is distributed in reduction indoor and outdoor multilayer circuitous channel.
7. the high-temperature gasification device of solid carbon raw material according to claim 1 and 2 is characterized in that: reduction exit, chamber is provided with poly-device for cooling.
8. the high-temperature gasification device of solid carbon raw material according to claim 1 and 2 is characterized in that: two combustion chambers of configuration, a reduction chamber.
9. the high-temperature gasification device of solid carbon raw material according to claim 1 and 2 is characterized in that: the communication passage between combustion chamber and the reduction chamber is from the horizontal by 5～20 ° of angles, and promptly combustor exit is lower than the reduction chamber inlet.
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| Application Number | Priority Date | Filing Date | Title |
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| CN 200610124571 CN1935951B (en) | 2006-09-21 | 2006-09-21 | High temperature gasifying apparatus for solid carbon raw material |
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| CN 200610124571 CN1935951B (en) | 2006-09-21 | 2006-09-21 | High temperature gasifying apparatus for solid carbon raw material |
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| CN1935951A true CN1935951A (en) | 2007-03-28 |
| CN1935951B CN1935951B (en) | 2010-12-08 |
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| CN 200610124571 Expired - Fee Related CN1935951B (en) | 2006-09-21 | 2006-09-21 | High temperature gasifying apparatus for solid carbon raw material |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101671578B (en) * | 2009-09-22 | 2012-11-21 | 武汉凯迪控股投资有限公司 | Combustible material plasma high-temperature gasification technique and equipment thereof |
| CN102939361A (en) * | 2010-04-16 | 2013-02-20 | 新日铁住金工程技术株式会社 | Thermal decomposition coal gasification method and thermal decomposition coal gasification device |
| CN101671576B (en) * | 2009-09-22 | 2013-04-24 | 武汉凯迪控股投资有限公司 | Auxiliary gasification technique using synthesis gas to burnback and equipment thereof |
| CN106318465A (en) * | 2016-10-18 | 2017-01-11 | 复旦大学 | Kiln type gasifier for gasifying solid-state carbon-containing raw materials |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE19747324C2 (en) * | 1997-10-28 | 1999-11-04 | Bodo Wolf | Device for generating fuel, synthesis and reducing gas from renewable and fossil fuels, biomass, waste or sludge |
| AU2004320347B2 (en) * | 2004-06-01 | 2009-08-13 | Japan Science And Technology Agency | Solid-fuel gasification system |
-
2006
- 2006-09-21 CN CN 200610124571 patent/CN1935951B/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101671578B (en) * | 2009-09-22 | 2012-11-21 | 武汉凯迪控股投资有限公司 | Combustible material plasma high-temperature gasification technique and equipment thereof |
| CN101671576B (en) * | 2009-09-22 | 2013-04-24 | 武汉凯迪控股投资有限公司 | Auxiliary gasification technique using synthesis gas to burnback and equipment thereof |
| CN102939361A (en) * | 2010-04-16 | 2013-02-20 | 新日铁住金工程技术株式会社 | Thermal decomposition coal gasification method and thermal decomposition coal gasification device |
| CN106318465A (en) * | 2016-10-18 | 2017-01-11 | 复旦大学 | Kiln type gasifier for gasifying solid-state carbon-containing raw materials |
| CN106318465B (en) * | 2016-10-18 | 2023-06-27 | 复旦大学 | Kiln type gasifier for gasifying solid carbon-containing raw materials |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1935951B (en) | 2010-12-08 |
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