CN103756731A - Interactive cyclic solid fuel gasification device with double fluidized beds and method - Google Patents
Interactive cyclic solid fuel gasification device with double fluidized beds and method Download PDFInfo
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Abstract
The invention relates to a mutually-cyclical solid fuel gasification device with double fluidized beds and a solid fuel gasification method. The method comprises the following steps: performing a pyrolysis gasification reaction between a solid fuel and a gas for fluidizations and reactions in a fluidized bed gasification reactor so as to generate a combustible gas, as well as solid coke and semicoke which are not subjected to incomplete pyrolysis gasification reaction, wherein the heat required by the pyrolysis reaction is obtained from high-temperature heat-carrying circulating bed materials; feeding the solid coke/the semicoke and the heat-carrying circulating bed materials with heat discharge into a pneumatic back-feeder through a cyclone separator or an overflow device according to a running state in the reactor; controllably sending the solid coke/the semicoke and the heat-carrying circulating bed materials into a combustion reactor; reheating the heat-carrying circulating bed materials due to the combustion of the solid coke/the semicoke in the combustion reactor; and refeeding the heated heat-carrying circulating bed materials into the gasification reactor through a back-feeding device so as to provide the heat for the pyrolysis gasification reaction. Thus, the device is gasified while the running parameters of the bubbling fluidization and the fast fluidization are adapted. As a result, the solid fuel gasification device provided by the invention has the good adaptability for various combustible solids; and the high running efficiency of the whole device is realized.
Description
Technical field
The present invention relates to a kind of mutual circulating double fluidized-bed apparatus for gasifying solid fuel, belong to solid fuel energy technology field.This mutual circulating double fluidized-bed apparatus for gasifying solid fuel is applicable to being applied to the many aspects such as gasification, gasifying biomass.
Background technology
Along with the rapid progress of society, evolution is followed and raw energy and environment problem highlights day by day with it, and these exploitation to the improvement of Energy production and consumption ways and new energy technology have produced reality and urgent need.
Specifically with regard to China's national situation, oil, natural gas reserves are relatively less, especially compare breach with output in domestic very large for petroleum demand, need to be from a large amount of imports of overseas each oil producing country, China's external oil interdependency is up to 60%, for ensureing national energy security and safeguarding that the stable life of the people is all an important hidden danger at present.With respect to the shortage of oil and gas resource, coal resources in China reserves are abundant and output is huge, and coal accounts for approximately seventy percent of China's total energy consumption at present.On the other hand, the flammable solid waste that comprises biomass is also very large in the output of China, particularly biomass resource is as one of clean reproducible energy, the application of this type of resource has vital role for making up energy demand breach and improving energy expenditure composition structure, for the realization of Sustainable development and the improvement of ecotope, also has important practical significance.
Solid fuel gasification is one of basic fundamental of future source of energy, fuel and industrial chemicals industry, is also one of effective technology of current solid fuel utilization.By gasification technology, utilize coal, biomass and all kinds of solid waste to transform and generate gas product or synthetic gas.Gas product after treatment both can be directly as fuel, also can as the substitute of Sweet natural gas, use by means production synthetic natural gases such as further refining and methanations.Synthetic gas can be widely used in all kinds of Chemical Manufacture the unstripped gas as chemosynthesis process, by synthetic each fuel oils that can produce multiple basic chemical raw materials and can be used for petroleum replacing product.
The research and development of gasification technology are the history in existing century more than one so far, has formed multiple different technology in its evolution.Current gasification technology mainly comprises fixed bed/moving bed technique, fluidization and air flow bed technology three classes, wherein fluidized-bed gasification technology has the advantages such as working temperature is moderate, throughput is stronger, but still has, the shortcoming such as gasification transformation efficiency not high, control difficulty, tar yield large and aerogenesis calorific value lower higher to ingredient requirement of fixed carbon.
Double-fluidized-bed gasification technology is a kind of special fluidisation bed gasification technology attracting people's attention gradually in recent years, by utilizing double-fluidized-bed special construction to realize, the decoupling zero of complex chemical reaction network in the gasification of flammable solid material is controlled, thereby the energy of output in gasification and material are efficiently utilized.Current design mainly comprises bubbling bed coupling bubbling bed, bubbling bed coupling cycle bed, circulation bed coupling cycle bed three classes for the double-fluidized-bed device of gasification technology, during design, adopt coupled gasification bed type-restriction raw material and the working parameter of double-fluidized-bed gasification installation, such device is relative poor to the variation adaptibility to response of material component and size, can not adapt to the practical application under multiple flammable solid raw material application background completely.
Summary of the invention
Technical problem:
One of object of the present invention is to provide a kind of mutual circulating double fluidized-bed apparatus for gasifying solid fuel.This device has double-fluidized-bed mutual circulation loop, comprises fluidized-bed gasification furnace, vapourizing furnace cyclonic separator, the pneumatic material-returning device of vapourizing furnace, fluid-bed combustion furnace, roasting kiln cyclonic separator, the pneumatic material-returning device of roasting kiln.The entrance pipeline section of two material-returning devices is connected with cyclonic separator solid outlet and reactor flash pipe respectively.Thereby material-returning device is realized mutual circulation and the coupling between double-fluidized-bed reactor for a reactor is produced to controlled another reactor of sending into of solid materials.
One of object of the present invention is also to provide mutual circulating double fluidized-bed method for solid fuels gasification.Solid fuel carries out pyrolytic gasification at gasifying reactor and produces inflammable gas.Jiao/semicoke that reaction produces is admitted to combustion reactor by material-returning device, the heat release of burning in the situation that being mixed with thermal barrier particle.Thermal barrier after heating is got back in gasifying reactor and is provided gasification reaction required heat by circulation loop.By using the coupling between each reaction related in the design removing gasification process of mutual circulation double-reactor, making the interaction between each reaction distinguish to utilize becomes possibility, thereby improves the utilising efficiency of gasification institute's generate energy and material and promote combustible gas quality.
Technical scheme: for solving the problems of the technologies described above, the invention provides a kind of mutual circulating double fluidized-bed apparatus for gasifying solid fuel, this gasification installation comprises fluidized bed gasification reactor and fluidized-bed combustion reactor;
The outlet of fluidized bed gasification reactor top is connected with gasifying reactor cyclonic separator, and is connected with gasifying reactor material returning device top one side by returning charge downtake; Fluidized bed gasification reactor middle part is provided with overflow inclined tube and is connected with returning charge downtake; The pneumatic material returning device of gasifying reactor is connected with fluidized-bed combustion reactor by combustion reactor returning charge inclined tube;
The outlet of fluidized-bed combustion reactor top is connected with combustion reactor cyclonic separator, and is connected with combustion reactor material returning device top one side by returning charge downtake; Fluidized-bed combustion reactor middle part is provided with overflow inclined tube and is connected with returning charge downtake; The pneumatic material returning device of combustion reactor is connected with fluidized bed gasification reactor by gasifying reactor returning charge inclined tube.
Preferably, the superficial gas velocity of fluidized bed gasification reactor operation is 0.4～5m/s, and the superficial gas velocity of fluidized-bed combustion reactor operation is 0.4～5m/s; The temperature of fluidized bed gasification reactor operation is 700～900 ℃, and the temperature of fluidized bed gasification reactor operation is 800～1000 ℃.
The present invention also provides a kind of mutual circulating double fluidized-bed method for solid fuels gasification, and the method comprises the steps,
Solid fuel adds in fluidized bed gasification reactor by feeding screw entrance, and make this solid fuel by the fluidizing agent fluidisation being fed by this fluidized-bed reactor bottom fluidization gas inlet, the solid fuel being fluidized mixes and heats up with high temperature heat-carrying circulation bed material, first volatile matter in solid fuel separates out, there is pyrolytic gasification in remaining solid fuel subsequently in gasifying reactor, produce combustible gas and Jiao/semicoke, combustible gas is through the separated output of gasifying reactor cyclonic separator, comprising Jiao/semicoke has heat-carrying bed material by gasifying reactor cyclonic separator or gasifying reactor flash inclined tube, via returning charge downtake, to send into the pneumatic material returning device of gasifying reactor according to fluidization conditions difference in interior reaction remaining solid mixing of materials, via combustion reactor returning charge inclined tube, be admitted to combustion reactor subsequently, Jiao/semicoke as fuel in combustion reactor and by the fluidizing agent fluidisation being fed by combustion reactor bottom fluidization gas inlet, by utilizing the oxygen combustion containing in fluidizing agent, the heat that burning discharges is used to heat heat-carrying circulation bed material, and the flue gas that burning generates is discharged by combustion reactor cyclonic separator is separated, heat-carrying circulation bed material after intensification is sent into combustion reactor pneumatic material returning device by combustion reactor cyclonic separator or gasifying reactor flash inclined tube via returning charge downtake according to fluidization conditions difference, via gasifying reactor returning charge inclined tube, enter again gasifying reactor subsequently, and release of heat heat solid fuel makes its pyrolytic gasification, thereby form the mutual circulation between double-fluidized-bed reactor.
Preferably, fluidized bed gasification reactor and fluidized-bed combustion reactor are all by making it the running status in bubbling fluidization or fast fluidization respectively to set valve switch on gasifying reactor flash inclined tube and combustion reactor flash inclined tube.
Beneficial effect: compared with prior art, the present invention has following characteristic and advantage:
(1) the present invention adopts the mutual circulating double fluidized-bed working method that fluidized bed gasification reactor combines with fluidized-bed combustion reactor, utilize solid heat-carrying bed material to realize the combination of high-temperature gasification and Jiao/coal-char combustion in solid fuel, the combustion reactions of the pyrolytic gasification reaction of heat absorption and heat release is placed in same device and completed, and that has realized energy and material combines output and utilization respectively;
(2) the solid-fuelled pyrolysis/gasification in the method for the invention and combustion processes are carried out respectively in two fluidized-beds, can realize respectively and controlling, and are easy to improve the operational efficiency of total system;
(3) gasification installation of the present invention, adopting double-fluidized-bed reactor, has the advantages such as fluidized-bed reactor is good to solid fuel kind adaptability, disposal of pollutants is low, simple to operate, treatment capacity is large.By particular design, make described device can adapt to respectively the operating requirement of bubbling fluidization and fast fluidization on this basis, make described gasification installation can tackle the complicated solid fuel that comprises coal, biomass etc., and the adjustment by operating parameter can improve burning and gasification efficiency to greatest extent, thereby realize the efficient utilization of material and energy;
(4) the present invention can further adopt multilayer feeding structure and multilayer flow structure, according to the variation of flammable solid kind and operating parameter, charging and flash position are adjusted, different types of flammable solid can be used simultaneously on described device, be conducive to the universal and development of solid fuel gasification technology.
Accompanying drawing explanation
Fig. 1 is the mutual circulating double fluidized bed gasifying apparatus principle schematic of the present invention;
Fig. 2 implements a kind of combination interchanger of the inventive method and the gasification installation structural representation of refining plant treating product gas and flue gas.
Wherein have: gasifying reactor spiral feed entrance 1, gasifying reactor fluidizing agent entrance 2, fluidized bed gasification reactor 3, gasifying reactor cyclonic separator 4, gasifying reactor flash inclined tube and by-pass valve control 5, the pneumatic material returning device 6 of gasifying reactor, combustion reactor returning charge inclined tube 7, combustion reactor spiral feed entrance 8, combustion reactor fluidizing agent entrance 9, combustion reactor 10, combustion reactor cyclonic separator 11, combustion reactor flash inclined tube and by-pass valve control 12, the pneumatic material returning device 13 of combustion reactor, gasifying reactor returning charge inclined tube 14, the pneumatic material returning device returning charge of gasifying reactor gas inlet 15, the pneumatic material returning device returning charge of combustion reactor gas inlet 16, gasifying reactor outlet 17, combustion reactor outlet 18, inflammable gas outlet 19, exhanst gas outlet 20, gasifying reactor cyclonic separator returning charge downtake 21, combustion reactor cyclonic separator returning charge downtake 22, combustible gas purifying device A, smoke eliminator B, combustible gas interchanger C, flue gas heat-exchange unit D.
Embodiment
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is further described.
Referring to Fig. 1-2, mutual circulating double fluidized-bed apparatus for gasifying solid fuel provided by the invention, comprises fluidized bed gasification reactor 3 and fluidized-bed combustion reactor 10; Fluidized bed gasification reactor top outlet 17 is connected with gasifying reactor cyclonic separator 4, and is connected with gasifying reactor material returning device 6 top one sides by returning charge downtake 21; Fluidized bed gasification reactor middle part is provided with overflow inclined tube 5 and is connected with returning charge downtake 21; The pneumatic material returning device 6 of gasifying reactor is connected with fluidized-bed combustion reactor by combustion reactor returning charge inclined tube 7; Fluidized-bed combustion reactor top outlet 18 is connected with combustion reactor cyclonic separator 11, and is connected with combustion reactor material returning device 13 top one sides by returning charge downtake 22; Fluidized-bed combustion reactor middle part is provided with overflow inclined tube 12 and is connected with returning charge downtake 22; The pneumatic material returning device 13 of combustion reactor is connected with fluidized bed gasification reactor by gasifying reactor returning charge inclined tube 14.
Solid fuel adopts brown coal and biomass mixture material, by feeding screw entrance 1, add in fluidized bed gasification reactor 3, and make this solid fuel by the fluidizing agent fluidisation being fed by this fluidized-bed reactor bottom fluidization gas inlet 2, the solid fuel being fluidized mixes and heats up with high temperature heat-carrying circulation bed material, first volatile matter in solid fuel separates out, there is pyrolytic gasification in remaining solid fuel subsequently in gasifying reactor 3, produce combustible gas and solid Jiao/semicoke, combustible gas is through the separated output of gasifying reactor cyclonic separator 4, comprising Jiao/semicoke has heat-carrying bed material by gasifying reactor cyclonic separator 4 or gasifying reactor flash inclined tube 5, via returning charge downtake, to send into the pneumatic material returning device 6 of gasifying reactor according to fluidization conditions difference in interior reaction remaining solid mixing of materials, via combustion reactor returning charge inclined tube 7, be admitted to combustion reactor 10 subsequently.Jiao/semicoke as fuel in combustion reactor 10 and by the fluidizing agent fluidisation being fed by combustion reactor bottom fluidization gas inlet 9, by utilizing the oxygen combustion containing in fluidizing agent, the heat that burning discharges is used to heat heat-carrying circulation bed material, and the flue gas that burning generates is discharged by combustion reactor cyclonic separator 11 is separated.Heat-carrying circulation bed material after intensification is sent into combustion reactor pneumatic material returning device 13 by combustion reactor cyclonic separator 11 or gasifying reactor flash inclined tube 12 via returning charge downtake according to fluidization conditions difference, via gasifying reactor returning charge inclined tube 14, enter again gasifying reactor 3 subsequently, and release of heat heat solid fuel makes its pyrolytic gasification, thereby form the mutual circulation between double-fluidized-bed reactor.
Fluidized bed gasification reactor 3 and fluidized-bed combustion reactor 10 are all connected with combustion reactor cyclonic separator 11 with gasifying reactor cyclonic separator 4 respectively being provided with top outlet, all at fluidized-bed reactor middle part, be provided with can be by gasifying reactor returning charge inclined tube 5 and the combustion reactor returning charge inclined tube 12 of valve trip switch simultaneously, gasifying reactor returning charge inclined tube 5 passes into the pneumatic material returning device 6 of gasifying reactor after converging with gasifying reactor cyclonic separator returning charge downtake 21, combustion reactor returning charge inclined tube 12 passes into the pneumatic material returning device 13 of combustion reactor after converging with combustion reactor cyclonic separator returning charge downtake 22.
Fluidized bed gasification reactor 3 all can make it the running status in bubbling fluidization or fast fluidization respectively by the valve switch to set on gasifying reactor flash inclined tube 5 and combustion reactor flash inclined tube 12 with fluidized-bed combustion reactor 10.
The superficial gas velocity of fluidized bed gasification reactor 3 operations is 0.4～5m/s, and the superficial gas velocity of fluidized-bed combustion reactor 10 operations is 0.4～5m/s; The temperature of fluidized bed gasification reactor 3 operations is 700～900 ℃, and the temperature of fluidized bed gasification reactor 10 operations is 800～1000 ℃.
When the interior temperature of fluidized bed gasification reactor 3 is during lower than design requirements, can to fluidized-bed combustion reactor 10, add solid fuel or in fluidizing agent, sneak into inflammable gas by combustion reactor fluidizing agent entrance 9 by combustion reactor spiral feed entrance 8, in order to improve the interior intensity of combustion of combustion reactor 10, improve working temperature in reactor.
Combustion solid selects biomass and brown coal mixture as raw material, opening the valve arranging on the overflow inclined tube 5 of fluidized bed gasification reactor 3 makes it as bubbling fluidization bed operating, in gasifying reactor, superficial gas velocity is set as 0.35～0.45m/s, close the valve arranging on the overflow inclined tube 12 of combustion reactor 10 and make it as fast fluidization bed operating, in combustion reactor, superficial gas velocity is set as 3.5～4m/s.
Solid fuel is admitted to fluidized-bed combustion reactor 10 via roasting kiln feeding screw entrance 8, combustion reactor spiral input speed is set as 0.5m/s, by being arranged on the ignition device in combustion reactor, and control combustion reactor temperature is 900 ± 20 ℃.After temperature rises gradually and reaches in scope of design in gasifying reactor, by gasifying reactor feeding screw entrance 1, add solid fuel, in gasifying reactor, to control be 800 ± 20 ℃ to temperature.
Solid fuel adds the rear air being passed into by bottom fluidization gas inlet of gasifying fluidized bed 10 and water vapour mixed gas fluidisation, and to solid fuel, heating makes its pyrolytic gasification under this environment to high temperature heat-carrying circulation bed material.Solid fuel pyrolysis gasification rear portion conversion is combustible gas, and biomass and coal nubbin are converted into Jiao.High-temperature combustible gas is from gasifying reactor cyclonic separator outlet 19 outputs, first the air of inputting as first step preheating heating through combustible gas interchanger C, then after combustible gas purifying device A does further purifying treatment separating tar, obtain combustible gas product, as fuel or industrial raw material, use.Bed material after Jiao and heat exchange flows out and enters gasifying reactor material returning device 6 via gasifying reactor flash inclined tube 5 from overflow port, gasifying reactor material returning device is provided with fluidizing agent entrance 15, selects air to send into that gasifying reactor material returning device 6 reacts biomass Jiao of generating with coal and the bed material after heat exchange is sent into fluidized-bed combustion reactor 10 herein.
Air is sent into from fluidized-bed combustion reactor 10 base burning reactor stream oxidizing gases entrances 9 as fluidized wind, and auxiliary fuel enters from combustion reactor feeding screw entrance 8.Remaining Jiao of biomass and gasification and auxiliary fuel heat up heat-carrying circulation bed material in the interior burning of combustion reactor 10 release of heat.Heat-carrying circulation bed material after heating and high-temperature flue gas rise and enter combustion reactor cyclonic separator 11, high-temperature flue gas is exported by combustion reactor cyclonic separator outlet 20 after this is separated, for flue gas heat-exchange unit D, air is carried out to second stage preheating, and drain in environment after processing pollutent by smoke eliminator B.High temperature heat-carrying circulation bed material is separated by entering combustion reactor material returning device 13 by combustion reactor cyclonic separator returning charge downtake 22, returns in gasifying reactor 3 subsequently by gasifying reactor returning charge inclined tube 14.High temperature heat-carrying recycle stock and solid fuel carry out heat exchange by heat transfer types such as thermal convections, and high hotbed material plays katalysis simultaneously.
Material returning device is the double-chamber structure being interconnected, comprise pan feeding chamber and discharge chamber, can realize the controlled circulation of material between double-fluidized-bed reactor and effectively prevent that altering of gas in gasification installation is mixed, by passing into the flux that air flow quantity in material returning device can controlled circulation material.
Claims (4)
1. a mutual circulating double fluidized-bed apparatus for gasifying solid fuel, is characterized in that, this gasification installation comprises fluidized bed gasification reactor (3) and fluidized-bed combustion reactor (10);
Fluidized bed gasification reactor (3) top outlet (17) is connected with gasifying reactor cyclonic separator (4), and is connected with gasifying reactor material returning device (6) top one side by returning charge downtake (21); Fluidized bed gasification reactor middle part is provided with overflow inclined tube (5) and is connected with returning charge downtake (21); The pneumatic material returning device of gasifying reactor (6) is connected with fluidized-bed combustion reactor (10) by combustion reactor returning charge inclined tube (7);
Fluidized-bed combustion reactor (10) top outlet (18) is connected with combustion reactor cyclonic separator (11), and is connected with combustion reactor material returning device (13) top one side by returning charge downtake (22); Fluidized-bed combustion reactor middle part is provided with overflow inclined tube (12) and is connected with returning charge downtake (22); The pneumatic material returning device of combustion reactor (13) is connected with fluidized bed gasification reactor by gasifying reactor returning charge inclined tube (14).
2. mutual circulating double fluidized-bed apparatus for gasifying solid fuel according to claim 1, it is characterized in that, the superficial gas velocity of fluidized bed gasification reactor (3) operation is 0.4～5m/s, and the superficial gas velocity of fluidized-bed combustion reactor (10) operation is 0.4～5m/s; The temperature of fluidized bed gasification reactor (3) operation is 700～900 ℃, and the temperature of fluidized bed gasification reactor (10) operation is 800～1000 ℃.
3. a mutual circulating double fluidized-bed method for solid fuels gasification, is characterized in that, the method comprises the steps,
Solid fuel adds in fluidized bed gasification reactor (3) by feeding screw entrance (1), and make this solid fuel by the fluidizing agent fluidisation being fed by this fluidized-bed reactor bottom fluidization gas inlet (2), the solid fuel being fluidized mixes and heats up with high temperature heat-carrying circulation bed material, first volatile matter in solid fuel separates out, there is pyrolytic gasification in remaining solid fuel subsequently in gasifying reactor (3), produce combustible gas and Jiao/semicoke, combustible gas is through the separated output of gasifying reactor cyclonic separator (4), comprising Jiao/semicoke has heat-carrying bed material by gasifying reactor cyclonic separator (4) or gasifying reactor flash inclined tube (5), via returning charge downtake, to send into the pneumatic material returning device of gasifying reactor (6) according to fluidization conditions is different in interior reaction remaining solid mixing of materials, via combustion reactor returning charge inclined tube (7), be admitted to combustion reactor (10) subsequently, Jiao/semicoke as fuel in combustion reactor (10) and by the fluidizing agent fluidisation being fed by combustion reactor bottom fluidization gas inlet (9), by utilizing the oxygen combustion containing in fluidizing agent, the heat that burning discharges is used to heat heat-carrying circulation bed material, and the flue gas that burning generates is discharged by combustion reactor cyclonic separator (11) is separated, heat-carrying circulation bed material after intensification is sent into combustion reactor pneumatic material returning device (13) by combustion reactor cyclonic separator (11) or gasifying reactor flash inclined tube (12) via returning charge downtake according to fluidization conditions is different, via gasifying reactor returning charge inclined tube (14), enter again gasifying reactor (3) subsequently, and release of heat heat solid fuel makes its pyrolytic gasification, thereby form the mutual circulation between double-fluidized-bed reactor.
4. mutual circulating double fluidized-bed apparatus for gasifying solid fuel according to claim 3, it is characterized in that, fluidized bed gasification reactor (3) and fluidized-bed combustion reactor (10) are all by making it the running status in bubbling fluidization or fast fluidization respectively to gasifying reactor flash inclined tube (5) and the upper set valve switch of combustion reactor flash inclined tube (12).
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| CN108048138A (en) * | 2017-12-20 | 2018-05-18 | 武汉凯迪工程技术研究总院有限公司 | Based on the double-fluidized-bed biomass graded conversion of middle low temperature and coal-burning boiler coupled electricity-generation method and its system |
| CN108219848A (en) * | 2017-12-21 | 2018-06-29 | 北京交通大学 | A kind of four fluidized-bed gasification furnace reaction units |
| CN108795504A (en) * | 2018-04-23 | 2018-11-13 | 北京交通大学 | A kind of CO2Four fluidized-bed gasification furnace reaction unit of near-zero release and gasification process |
| CN109370649A (en) * | 2018-11-09 | 2019-02-22 | 江苏大学 | Biomass is from heat supply double-flow gasification system |
| CN110511787A (en) * | 2019-09-21 | 2019-11-29 | 贵州丝域环能科技有限公司 | A kind of novel double-fluidized-bed device of organic solid castoff hydrogen manufacturing |
| CN113265273A (en) * | 2021-05-19 | 2021-08-17 | 新奥科技发展有限公司 | Fluidized bed heat exchanger, double fluidized bed coal gasification system and control method thereof |
| CN113416583A (en) * | 2021-07-29 | 2021-09-21 | 北京工商大学 | Biomass in-situ nitrogen-control gasification co-production hot carbon device |
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