CN202688286U - Solid organic fuel pyrolysis and gasification device with two-stage serial fluidized bed - Google Patents
Solid organic fuel pyrolysis and gasification device with two-stage serial fluidized bed Download PDFInfo
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- CN202688286U CN202688286U CN 201220341206 CN201220341206U CN202688286U CN 202688286 U CN202688286 U CN 202688286U CN 201220341206 CN201220341206 CN 201220341206 CN 201220341206 U CN201220341206 U CN 201220341206U CN 202688286 U CN202688286 U CN 202688286U
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Abstract
The utility model discloses a solid organic fuel pyrolysis and gasification device with two-stage serial fluidized beds. The device comprises a primary fluidized bed reactor and a secondary fluidized bed reactor which are connected in series, a gas-solid separating device and a gas-liquid separating device. Organic solid fuels are processed by the two-stage serial fluidized beds, namely the organic solid fuels are first burnt or gasified in the primary fluidized bed reactor, and discharged high-temperature smoke or fuel gas is delivered to the secondary fluidized bed reactor to be gasified or pyrolyzed. Other heat does not need to be consumed in the pyrolysis reaction, the quality of the pyrolyzed gas can be improved, and high-quality solid fuels, fuel gas and tar products with high calorific value can be produced.
Description
Technical field
The present invention relates to the gasification of SOLID ORGANIC fuel thermal decomposition and produce oil, gas technical field.
Background technology
SOLID ORGANIC fuel refer to timber, agricultural stalk, municipal solid wastes (solid organic matters), mud etc. by thermal chemical reaction can release of heat organic solid.
Publication number is CN102191088A, open day is on September 21st, 2011, denomination of invention discloses the device and method that a kind of solid fuel double fluidized bed thermal pyrolysis grade transforms for the Chinese invention patent of " solid fuel double fluidized bed thermal pyrolysis grade transformation device and method ", this device is comprised of normal pressure or pressurised fluidized bed pyrolysis oven and fluidized-bed gasification furnace, and pressure is 1 ~ 5MPa during the pressurization operation.The method is first solid fuel to be carried out middle low temperature pyrogenation in the fluidized bed pyrolysis stove, form with tar and pyrolysis coal gas is extracted contained volatile matter in the solid fuel, the semicoke that again pyrolysis is produced is delivered to fluidized-bed gasification furnace, gasify take water vapour and oxygen as vaporized chemical, produce synthetic gas, produce simultaneously the high temperature circulation material, the high temperature circulation material is transported to pyrolysis oven as thermal barrier, for solid fuel pyrolysis provides required heat, thus the coproduction of realization tar, pyrolysis coal gas and synthetic gas.
Publication number is CN101220298, open day is on July 16th, 2008, denomination of invention discloses a kind of circulating fluidized bed pyrolysis gasification method and device for the Chinese invention patent of " circulating fluidized bed pyrolysis gasification method and device ", relate to Coal Gasification Technology, be used for pyrolysis or the gasification of coal, biomass and other multiple carbonaceous refuse.The method is: fuel carries out pyrolysis or gasification reaction in pyrolysis vaporizer, produces coal gas and semicoke; The semicoke high-temp circulating ash that produces that burns in the combustion chamber is sent into pyrolysis vaporizer, for the pyrolytic gasification reaction provides heat; The semicoke material returning device of the semicoke that pyrolysis vaporizer produces through being arranged at this bottom, chamber communicates.
Publication number is CN101624531, open day is on January 13rd, 2010, and denomination of invention discloses a kind of biomass spouted fluidized bed pyrolysis fractional condensation preparing bio-oil device for the Chinese invention patent of " biomass spouted fluidized bed pyrolysis fractional condensation preparing bio-oil device ".Wherein, the built-up type charging system can guarantee that biomass material is smooth and easy, stably enter reactor; Adopt spouted fluidized bed as pyrolysis reactor, can satisfy well the biomass fast pyrogenation technology to high heating rate, good heat-transfer effect and the mutually requirement of the residence time of losing heart; The system of fearing gas solid separation and charcoal can clean pyrolysis gas and collect the byproduct coke; Directly contact can realize separating of bio oil heavy component and light component with the condensed in two stages system that indirect heat exchange combines, not only can improve productive rate and the quality of bio oil, also preparing liquid fuel and extraction Chemicals are combined simultaneously, increase economy; Pyrolysis tail gas follow continuous supplying that system can guarantee the pyrolysis carrier gas to, reduced device running cost industry is amplified so that a whole set of pyrolysis installation is more convenient for.
Summary of the invention
The object of the present invention is to provide a kind of pyrolysis gasifying device of new SOLID ORGANIC fuel, it can reach better heat energy utilization effect by the mode of two-stage series connection fluidized-bed, obtains multi-jointization product.
The present invention is achieved through the following technical solutions:
A kind of SOLID ORGANIC fuel two-stage series connection fluidized bed pyrolysis gasification installation, it comprises one-level fluidized-bed reactor and the secondary streams fluidized bed reactor that is connected in series, at least one-level gas-solid separating device and at least one-level gas-liquid separation device, the air outlet pipeline of one-level fluidized-bed reactor is connected in the inlet mouth of secondary streams fluidized bed reactor, the air outlet pipeline of secondary streams fluidized bed reactor is connected in the inlet mouth of gas-solid separating device, the air outlet pipeline of gas-solid separating device is connected in the inlet mouth of gas-liquid separation device, one-level fluidized-bed reactor and secondary streams fluidized bed reactor are respectively arranged with overflow port, and the discharge port of overflow port and gas-solid separating device compiles the feedback outlet that is connected to the one-level fluidized-bed reactor by pipeline.
Described one-level fluidized-bed reactor and secondary streams fluidized bed reactor inside comprise respectively concentrated phase reaction zone and the superposed dilute phase reaction zone that is positioned at the bottom, described overflow port is arranged at excessive section of the material concentrated phase on concentrated phase reaction zone top and dilute phase, and described feedback outlet is arranged at the concentrated phase reaction zone.
A kind of SOLID ORGANIC fuel two-stage series connection fluidized bed pyrolysis gasification installation, it comprises the one-level fluidized-bed reactor that is connected in series, the secondary streams fluidized bed reactor, at least one-level gas-solid separator, at least one-level fly-ash separator, at least one-level is used for refrigerating unit and the liquid phase tar recovery system of gas-liquid separation, one-level fluidized-bed reactor and secondary streams fluidized bed reactor inside comprise respectively concentrated phase reaction zone and the superposed dilute phase reaction zone that is positioned at the bottom, the discharge port pipeline that is positioned at the top of one-level fluidized-bed reactor is connected in the opening for feed that is positioned at the concentrated phase reaction zone of secondary streams fluidized bed reactor, the discharge port pipeline of secondary streams fluidized bed reactor is connected in the opening for feed of gas-solid separating device, the dilute phase reaction zone of one-level fluidized-bed reactor and secondary streams fluidized bed reactor is respectively arranged with overflow port, and the discharge port of described overflow port and gas-solid separating device compiles by pipeline and is connected to the feedback outlet of being located at one-level fluidized-bed reactor concentrated phase reaction zone.
Furthermore, described refrigerating unit for gas-liquid separation is indirect cooling device, have the heat-eliminating medium chamber that is cooled dielectric cavity and holds heat-eliminating medium that holds the medium that is cooled, described heat-eliminating medium chamber with the heat absorbing solid medium charge and with liquefied ammonia or water as mobile heat-eliminating medium.
The invention has the beneficial effects as follows: make organic solid fuel by the two-stage series connection fluidized-bed, elder generation burns in the one-level fluidized-bed reactor or gasifies, and gasification or pyrolysis in the secondary streams fluidized bed reactor are sent in the high-temperature flue gas of discharge or combustion gas.Do not need in the pyrolytic reaction to consume other heats and can improve the pyrolysis gas quality, can also produce solid fuel, combustion gas and the tar product of high-quality high heating value.Solid fuel (semicoke) can be used as the fuel of native system one-level fluidized-bed reactor, also can be transported to native system outer fuel or raw material as other equipment; It is outer as other industrial chemicals or fuel that tar product is transported to native system; Combustion gas is as the fuel of gas turbine power generation, is combined to form association circulating power generation system with the steam turbine generation of the waste heat boiler of native system, fills up the blank of the extensive generating of present biomass fuel.
Description of drawings
Fig. 1 is the two-stage series connection fluidized bed pyrolysis gasification system equipment flowsheet of embodiment 1.
Fig. 2 is the two-stage series connection fluidized bed pyrolysis gasification system equipment flowsheet of embodiment 2.
Fig. 3 is process flow sheet of the present invention.
Embodiment
In order to understand better the present invention, now the term among the present invention is defined.
The SOLID ORGANIC raw material refers to that timber, agricultural stalk, municipal solid wastes (solid organic matters), mud etc. can be by the organic solids of thermal chemical reaction energy release of heat.
Flue gas refers to that solid fuel and air or oxygen generation thermal chemical reaction generate the gaseous matter take nitrogen and carbonic acid gas as principal constituent.
Combustion gas refers to that it is the inflammable gas with heat of main component that solid fuel and air or oxygen generation thermal chemical reaction generate carbon monoxide, hydrogen, methane, carbonic acid gas.
The inflammable gas take methane, macromolecular compound, hydrogen, carbon monoxide as principal constituent that pyrolysis gas refers to that the volatile matter in the solid is separated out under the heat effect that the outer boundary of solid fuel gives.
Wooden Biomass refers to timber, wood chip, bark, branch, leaf, wood working scrap stock etc., and non-draft is biomass (such as stalks).
Fluidized-bed reactor refers to utilize reactant gases to make solid fuel particle be in the suspended motion state by the solid fuel layer, the reactor of the promoting the circulation of qi of going forward side by side, solid state reaction process.
This example be with the one-level fluidized-bed reactor as combustion reactor, the secondary fluidized-bed is as the Application Example of gasifying reactor.
As shown in Figure 1, SOLID ORGANIC fuel two-stage series connection fluidized bed pyrolysis gasification installation of the present invention is comprised of one-level fluidized-bed reactor 1, secondary streams fluidized bed reactor 2, gas-solid phase separator 3, fly-ash separator 4, water cooler 5 and liquid phase withdrawer 6.
One-level fluidized-bed reactor 1 inside comprises that the concentrated phase reaction zone 11 and the superposed dilute phase reaction zone 12 that are positioned at the bottom form.Reactor shell offers solid fuel import 1.1, steam spray nozzle 1.2, air or oxygen import 1.3 and feed back import 1.4 at the concentrated phase reaction zone, and the dilute phase reaction zone offers overflow port 1.5, and reactor head is provided with exhanst gas outlet 1.6.
Secondary streams fluidized bed reactor 2 comprises that the concentrated phase reaction zone 21 and the superposed dilute phase reaction zone 22 that are positioned at the bottom form.Reactor shell offers solid fuel import 2.1, steam spray nozzle 2.2, air or oxygen import 2.3, gas approach 2.4 at the concentrated phase reaction zone, and the dilute phase reaction zone offers overflow port 2.5, and exhanst gas outlet 2.6 is located at reactor head.
As shown in Figure 1, the discharge port of secondary streams fluidized bed reactor 2 is the opening for feed that exhanst gas outlet 2.6 pipelines are connected in gas-solid phase separator 3, the discharge port pipeline of gas-solid phase separator 3 is connected in the opening for feed of fly-ash separator 4, and the discharge port pipeline of fly-ash separator 4 is connected in water cooler 5.
Flow process as shown in Figure 3.
When if one-level fluidized-bed reactor heat only relies on the solids of feed back pipe 13 to be not enough to reach institute's heat requirement, its insufficient section heat adds one-level fluidized-bed reactor 1 by SOLID ORGANIC raw material or fossil solid fuel by solid fuel import 1.1.As roasting kiln, air or oxygen and water vapor are admitted in the one-level fluidized-bed reactor 1 simultaneously at the one-level fluidized-bed reactor, and generation is inferior partial oxidation combustion reactions take combustion reactions as main, gasification reaction in one-level fluidized-bed reactor 1.In this example, the water vapor that passes into is 382.8 ℃, 4.0MPa, and flow is 2050kg/h, and the air that passes into is 348 ℃, and 2.8MPa, flow are 16960kg/h.Control reaction pressure 1～5MPa, the interior temperature of bed are controlled at 870 ℃, N in the gaseous product in the one-level fluidized-bed reactor 1
2, CO
2And H
2The O component accounts for more than 90% the medium that carries as secondary fluidized-bed gasification reaction institute heat requirement, and flue gas is discharged by exhanst gas outlet 1.6, is transported to secondary streams fluidized bed reactor 2, directly as pyrolytic reaction thermal source and reaction medium in the secondary streams fluidized bed reactor.
The SOLID ORGANIC raw material adds secondary streams fluidized bed reactor 2 by solid fuel import 2.1, air or oxygen and water vapor also are admitted to secondary streams fluidized bed reactor 2 simultaneously, and the high-temperature flue gas that comes from one-level fluidized-bed reactor 1 enters secondary streams fluidized bed reactor 2 as the required heat of the gasification reaction of secondary streams fluidized bed reactor 2 by gas approach 2.4.Generating gasification reaction in the reactor 2, reaction conditions is 950 ℃ of pressure 1～5MPa, temperature, and in the gasification reaction process, Wooden Biomass and air are admitted in the secondary streams fluidized bed reactor 2, and the flue gas that obtains after the reaction or combustion gas are discharged by exhanst gas outlet 2.6.In example, the air that passes into is 348 ℃, and 2.8MPa, flow are 23300kg/h, and Wooden Biomass is 10420kg/h.Can see the following form from secondary streams fluidized bed reactor 2 exhaust gas components out:
Table 1 gaseous fraction
| CO | Vol.% | 23.88 |
| H 2 | Vol.% | 11.59 |
| CO 2 | Vol.% | 5.28 |
| H 2O | Vol.% | 3.93 |
| O 2 | Vol.% | 0.00 |
| N 2 | Vol.% | 54.33 |
| CH 4 | Vol.% | 0.85 |
| H 2S | ppmv | 910 |
| NH 3 | ppmv | 1200 |
The uncombusted thing flows out the feed back import 1.4 that is delivered to one-level fluidized-bed reactor 2 from overflow port 2.5 in the secondary streams fluidized bed reactor 2.Uncombusted thing herein is coke, and major ingredient is～86% fixed carbon and 14% ash content that its temperature is about 600 ℃.
Be sent to gas-solid phase separator 3 from secondary streams fluidized bed reactor 2 flue gas out and carry out gas, the solid separation, resulting gas is further delivered to fly-ash separator 4, and the solid that gas, solid separation obtain behind gas-solid phase separator 3 is sent in the one-level fluidized-bed reactor 1 by return line 13 and acts as a fuel.
Gas is further carried out gas, the solid separation in fly-ash separator 4, deliver to the power generation assemblys such as internal combustion turbine or oil engine after the gas of resulting separation is cleaned.Separating obtained solid is ash particle, and this ash particle is disposed by relevant regulations and standard.
The last products therefrom of native system technique be ~ 85% combustion gas (fuel gases calorific value :～12MJ/Nm3) and ~ 15% semicoke, combustion gas can be used as civilian or industrial combustion gas, also can be used as gas turbine power generation fuel; Semicoke is delivered to roasting kiln.
A reactor and second reactor and downstream process all arrange residual neat recovering system, reclaim heat by water, and water becomes steam, promote the steam turbine generating.
In this example, when the one-level fluidized-bed reactor moves as combustion reactor, produce high-temperature flue gas (CO
2, N
2, H
2O, a small amount of O
2Deng), as the thermal source of secondary streams fluidized bed reactor, at this moment, the secondary streams fluidized bed reactor moves as gasifying reactor.
This example for the one-level fluidized-bed reactor as the Application Example of gasifying reactor secondary streams fluidized bed reactor as pyrolysis reactor.
Be illustrated in figure 2 as this routine equipment flowsheet, its pipeline connecting mode is substantially the same manner as Example 1.
When if the A reactor heat only relies on the solids of feed back pipe 13 to be not enough to reach institute's heat requirement, its insufficient section heat adds one-level fluidized-bed reactor 1 by SOLID ORGANIC raw material or fossil solid fuel by solid fuel import 1.1.In the reaction process of one-level fluidized-bed reactor as vapourizing furnace, air or oxygen and water vapor are admitted in the one-level fluidized-bed reactor 1 simultaneously, occur in one-level fluidized-bed reactor 1 take gasification reaction as main reaction.In this example, the water vapor that passes into is 382.8 ℃, 4.0MPa, and flow is 885kg/h, and the air that passes into is 348 ℃, and 2.8MPa, flow are 10062kg/h, add simultaneously Wooden Biomass 4500kg/h.Control reaction pressure 1～5MPa, the interior temperature of bed are controlled at 870 ℃ in the one-level fluidized-bed reactor 1.The flue-gas temperature that obtains after the reaction consists of at 700 ~ 1000 ℃: 25.60% CO, 10.40% CO
2, 0.73% CH
4, 13.23% H
2, 2.15% H
2O, its calorific value reaches, and the combustion gas that obtains after the reaction is discharged by exhanst gas outlet 1.6, is transported to secondary streams fluidized bed reactor 2, directly as pyrolytic reaction thermal source and reaction medium in the secondary streams fluidized bed reactor.One-level fluidized-bed reactor exhaust gas components such as following table 2 out:
Table 2
| CO | Vol.% | 25.60 |
| H 2 | Vol.% | 13.23 |
| CO 2 | Vol.% | 10.40 |
| H 2O | Vol.% | 2.15 |
| O 2 | Vol.% | 0.00 |
| N 2 | Vol.% | 47.89 |
| CH 4 | Vol.% | 0.73 |
| H 2S | ppmv | 850 |
| NH 3 | ppmv | 1210 |
SOLID ORGANIC raw material or fossil solid fuel add secondary streams fluidized bed reactor 2 by solid fuel import 2.1, air or oxygen and water vapor also are admitted to secondary streams fluidized bed reactor 2 simultaneously, and the high-temperature flue gas that comes from one-level fluidized-bed reactor 1 enters secondary streams fluidized bed reactor 2 as the required heat of the pyrolytic reaction of secondary streams fluidized bed reactor 2 by gas approach 2.4.Service temperature general control in reactor 2 during gasification reaction is at 500 ~ 650 ℃, as about 600 ℃.Generating gasification reaction in the secondary streams fluidized bed reactor 2, pressure-controlling do not add oxygen or air etc. at 1～5MPa in the reaction whole process, pyrolytic reaction obtains～20% coke and～80% thermolysis gas (flue gas).The flue gas that obtains after the reaction or combustion gas are discharged by exhanst gas outlet 2.6.From the major ingredient of secondary streams fluidized bed reactor 2 flue gas out～combustion gas of 30% and～50% condensing liquid (wherein: tar ingredients～20% ,～moisture 30%).Wherein in the Gas Components, 34.2% CO, 4.19% CO
2, 5.6% CH
4, 20.3% H
2With 0.71% C
2H
4, C
2H
6Deng low-molecular-weight hydrocarbon; Gas Components specifically sees the following form 3:
Table 3
| CO | Vol.% | 34.20 |
| H 2 | Vol.% | 20.30 |
| CO 2 | Vol.% | 4.19 |
| H 2O | Vol.% | 5.30 |
| O 2 | Vol.% | 0.00 |
| N 2 | Vol.% | 30.41 |
| CH 4 | Vol.% | 5.60 |
| Calorific value | MJ/Nm 3 | 7.53 |
| Tar | Kg/h | 3000 |
The uncombusted thing flows out the feed back import 1.4 that is delivered to one-level fluidized-bed reactor 2 from overflow port 2.5 in the secondary streams fluidized bed reactor 2.Uncombusted thing (semicoke) also can be from overflow port in the secondary streams fluidized bed reactor 2, with the semicoke form, as gac raw material or alternative coal etc. as the solid fuel product.Uncombusted thing herein is coke, major ingredient is～70% fixed carbon ,～16% volatile matter and 14% ash content, its temperature～600 ℃ can be used as the main fuel of one-level fluidized-bed reactor or are sent to other places as combustion material, such as the semicoke of discharging as the gac raw material etc.
Be sent to gas-solid phase separator 3 from secondary streams fluidized bed reactor 2 flue gas out and carry out gas, the solid separation, resulting gas is further delivered to fly-ash separator 4, the solid that gas, solid separation obtain behind gas-solid phase separator 3 is sent in the one-level fluidized-bed reactor 1 by return line 13 and acts as a fuel, the gas major ingredient of gained is～80% thermolysis volatile matter, wherein the combustion gas of major ingredient～40% and～60% condensing liquid.
Gas is further carried out gas, the solid separation in fly-ash separator 4, the gas of resulting separation is sent to water cooler 5 and carries out gas, liquid separation, and separating obtained solid is ash particle, and this ash particle is disposed by relevant law, rules.Gas through supercooler 5 resulting separations is sent to the power generation assemblys such as internal combustion turbine or oil engine as fuel gas product.The liquid of resulting separation is tar, collects through liquid phase withdrawer 6, as liquid starting material or industrial chemicals.Water cooler 5 is indirect cooling device, has the heat-eliminating medium chamber that is cooled dielectric cavity and holds heat-eliminating medium that holds the medium that is cooled, described heat-eliminating medium chamber is filled with the heat absorbing solid medium, and with liquefied ammonia or water as mobile heat-eliminating medium, take out of outside the system as the heat portable object by sending into continuously the liquid such as liquefied ammonia or water.
The last products therefrom of native system technique be ~ 40% combustion gas (fuel gases calorific value :～12MJ/Nm3), ~ 30% semicoke and ~ 30% tar.Combustion gas can be used as civilian or industrial combustion gas, also can be used as gas turbine power generation fuel.The one-level fluidized-bed reactor mainly produces CO, H as gasification or partial gasification reactor when operation
2, N
2, a small amount of CO
2And CH
4Gas, as thermal source and the chemical reaction agent (also claiming vaporized chemical) of secondary streams fluidized bed reactor, at this moment, the secondary streams fluidized bed reactor moves as pyrolysis reactor.
Claims (4)
1. SOLID ORGANIC fuel two-stage series connection fluidized bed pyrolysis gasification installation, it is characterized in that: comprise the one-level fluidized-bed reactor and the secondary streams fluidized bed reactor that are connected in series, at least one-level gas-solid separating device and at least one-level gas-liquid separation device, the air outlet pipeline of one-level fluidized-bed reactor is connected in the inlet mouth of secondary streams fluidized bed reactor, the air outlet pipeline of secondary streams fluidized bed reactor is connected in the inlet mouth of gas-solid separating device, the air outlet pipeline of gas-solid separating device is connected in the inlet mouth of gas-liquid separation device, one-level fluidized-bed reactor and secondary streams fluidized bed reactor are respectively arranged with overflow port, and the discharge port of overflow port and gas-solid separating device compiles the feedback outlet that is connected to the one-level fluidized-bed reactor by pipeline.
2. SOLID ORGANIC fuel two-stage series connection fluidized bed pyrolysis gasification installation according to claim 1, it is characterized in that: described one-level fluidized-bed reactor and secondary streams fluidized bed reactor inside comprise respectively concentrated phase reaction zone and the superposed dilute phase reaction zone that is positioned at the bottom, described overflow port is arranged at excessive section of the material concentrated phase on concentrated phase reaction zone top and dilute phase, and described feedback outlet is arranged at the concentrated phase reaction zone.
3. SOLID ORGANIC fuel two-stage series connection fluidized bed pyrolysis gasification installation, it is characterized in that: comprise the one-level fluidized-bed reactor that is connected in series, the secondary streams fluidized bed reactor, at least one-level gas-solid separator, at least one-level fly-ash separator, at least one-level is used for refrigerating unit and the liquid phase tar recovery system of gas-liquid separation, one-level fluidized-bed reactor and secondary streams fluidized bed reactor inside comprise respectively concentrated phase reaction zone and the superposed dilute phase reaction zone that is positioned at the bottom, the discharge port pipeline that is positioned at the top of one-level fluidized-bed reactor is connected in the opening for feed that is positioned at the concentrated phase reaction zone of secondary streams fluidized bed reactor, the discharge port pipeline of secondary streams fluidized bed reactor is connected in the opening for feed of gas-solid separating device, the dilute phase reaction zone of one-level fluidized-bed reactor and secondary streams fluidized bed reactor is respectively arranged with overflow port, and the discharge port of described overflow port and gas-solid separating device compiles by pipeline and is connected to the feedback outlet of being located at one-level fluidized-bed reactor concentrated phase reaction zone.
4. SOLID ORGANIC fuel two-stage series connection fluidized bed pyrolysis gasification installation according to claim 3, it is characterized in that: described refrigerating unit for gas-liquid separation is indirect cooling device, have the heat-eliminating medium chamber that is cooled dielectric cavity and holds heat-eliminating medium that holds the medium that is cooled, described heat-eliminating medium chamber with the heat absorbing solid medium charge and with liquefied ammonia or water as mobile heat-eliminating medium.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102766480A (en) * | 2012-07-13 | 2012-11-07 | 韶关市海粤生物科技发展有限公司 | Device and method for pyrolyzing and gasifying solid organic fuel by two-stage serial fluidized bed |
| CN114263905A (en) * | 2021-12-23 | 2022-04-01 | 中国科学院工程热物理研究所 | Preheating fuel gasification nozzle |
-
2012
- 2012-07-13 CN CN 201220341206 patent/CN202688286U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102766480A (en) * | 2012-07-13 | 2012-11-07 | 韶关市海粤生物科技发展有限公司 | Device and method for pyrolyzing and gasifying solid organic fuel by two-stage serial fluidized bed |
| CN114263905A (en) * | 2021-12-23 | 2022-04-01 | 中国科学院工程热物理研究所 | Preheating fuel gasification nozzle |
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