CN220079106U - Device for preparing gas-based shaft furnace reducing gas by purifying biomass gas - Google Patents
Device for preparing gas-based shaft furnace reducing gas by purifying biomass gas Download PDFInfo
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- CN220079106U CN220079106U CN202220885261.6U CN202220885261U CN220079106U CN 220079106 U CN220079106 U CN 220079106U CN 202220885261 U CN202220885261 U CN 202220885261U CN 220079106 U CN220079106 U CN 220079106U
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- 150000002430 hydrocarbons Chemical class 0.000 claims description 36
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 33
- 239000003546 flue gas Substances 0.000 claims description 33
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 27
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 26
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 26
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 24
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 22
- 238000006477 desulfuration reaction Methods 0.000 claims description 21
- 230000023556 desulfurization Effects 0.000 claims description 21
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 17
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- 229910052760 oxygen Inorganic materials 0.000 claims description 14
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- 239000011593 sulfur Substances 0.000 claims description 11
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 abstract description 23
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 abstract description 14
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 22
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- 229910052742 iron Inorganic materials 0.000 description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
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- 229910000831 Steel Inorganic materials 0.000 description 2
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- 239000003245 coal Substances 0.000 description 2
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Abstract
A device for preparing gas-based shaft furnace reducing gas by purifying biomass gas relates to a device for preparing gas-based shaft furnace reducing gas. The utility model aims to solve the problems of high preparation cost and CO emission in the existing system for preparing the reducing gas by the tubular heating furnace 2 And other waste gases, causing problems of heat waste and air pollution. The utility model introduces the raw material gas containing biomass gas into a gas heating furnace for heating through a pipeline; the method comprises the steps of reforming gas in a gas heating furnace into first reducing gas, then entering the gas-based shaft furnace, reacting iron oxide with the reducing gas in the gas-based shaft furnace, directly reducing the iron oxide into reduced iron, discharging the directly reduced iron out of the furnace through the lower part of the gas-based shaft furnace, discharging crude gas generated by the reaction from the top of the shaft furnace, adding second reducing gas into the first reducing gas, adjusting the temperature, and then entering the gas-based shaft furnace. Solves the problems of external combustion heating and smoke emission of the tubular heating furnace, does not need intermediate medium heat exchange, and has high heat exchange efficiency. The method is used for preparing the reduced iron.
Description
Technical Field
The utility model relates to a device for preparing gas-based shaft furnace reducing gas, in particular to a device for preparing gas-based shaft furnace reducing gas by purifying biomass gas.
Background
The gas-based shaft furnace process is a clean iron-making technology and is an important technical means for realizing a double-carbon target in the steel industry in China. However, in the prior art, the main gas source of the gas-based shaft furnace is natural gas, and the current state of resources in China is more coal and less gas, so that in order to adapt to the domestic resource characteristics, it is becoming more and more important to develop a new gas source suitable for the gas-based shaft furnace and a technology thereof. Therefore, technicians at home and abroad research the gas-based shaft furnace technology of a non-natural gas source, the research direction is a coal gas process, coal is a non-renewable resource, and the development prospect is limited.
In addition, the existing gas-based shaft furnace technology adopts a tubular heating furnace to prepare raw material gas, for example, the utility model patent application number is 201710676084.4, and the name is: the patent of a preparation system and a preparation method of reducing gas of a gas-based shaft furnace provides that a plurality of catalyst tubes are arranged in parallel, and a heat recovery device is a heat exchanger; as another example, application number: 201910952204.8, the name is: a patent for a new reformer for producing a reducing gas proposes that the reformer comprises a radiant chamber housing, reformer tubes, a burner, a transition section and a convection section; the reforming furnace tubes are arranged in 2m rows in parallel in the radiation chamber box body. The preparation of the reducing gas by the tube furnace has the following problems:
(1) The raw material gas in the tube furnace is heated by adopting fuel combustion, and the raw material gas in the tube furnace is heated by the fuel combustion outside the tube, so that the diameter of the tube is limited, and the single tube furnace is small in volume and huge in quantity. The number of furnace tubes in the radiation chamber of a sleeve type heating furnace is hundreds, and the number of burners is tens; the transition section and convection section equipment for discharging flue gas and utilizing the flue gas waste heat are huge and have complex structures. All of these result in large investment in gas-based shaft furnace gas production systems;
(2) The process burns fuel to discharge CO 2 And other exhaust gases, heat is not effectively utilized, and air pollution is a problem;
(3) The catalyst for preparing the reducing gas is expensive, the usage amount is large, and the catalyst needs to be replaced periodically, so that the production and operation costs are high.
In summary, the existing system for preparing the reducing gas by the tubular heating furnace has the defects of high preparation cost and CO generation emission 2 And other waste gases, causing problems of heat waste and air pollution.
Disclosure of Invention
The utility model aims to solve the problems of high preparation cost and CO emission in the existing system for preparing the reducing gas by the tubular heating furnace 2 And other waste gases, causing problems of heat waste and air pollution. Further provides a device for purifying biomass gas to prepare gas-based shaft furnace reducing gas.
The utility model provides two technical schemes:
scheme one: a device for preparing gas-based shaft furnace reducing gas by purifying biomass gas comprises a gas-based shaft furnace, a gas-based shaft furnace top purified gas heating device, a biomass producer, a biomass gas ammonia water cooler, a biomass gas purification system, a non-catalytic partial oxidation reformer, a gas compressor, a gas-based shaft furnace top hot gas heat exchanger I, a gas-based shaft furnace top gas dust remover and a gas-based shaft furnace top gas CO removal device 2 The device comprises a component, a hydrocarbon-rich gas source, a pure oxygen source and a water vapor source; the biomass producer is sequentially connected with the biomass producer through a lifting pipelineThe biomass gas ammonia water cooler and the biomass gas purifying system are communicated, and biomass gas generated in the biomass generator flows through the biomass gas ammonia water cooler and the biomass gas purifying system, and the biomass gas purifying system is used for removing tar, naphthalene, sulfur, benzene and CO from the biomass gas 2 The gas compressor is communicated with a first gas-based shaft furnace top hot gas heat exchanger, the first gas-based shaft furnace top hot gas heat exchanger is communicated with a gas pipeline of a burner positioned on a non-catalytic partial oxidation reformer through the pipeline, an oxygen passage of the burner is communicated with a pure oxygen source through the pipeline, a steam passage of the burner is communicated with a steam source through the pipeline, so that partial oxidation combustion of pure oxygen and mixed gas in the non-catalytic partial oxidation reformer is realized, and the generated first reducing gas flows out through an outlet of the non-catalytic partial oxidation reformer; a part of the furnace hot gas of the gas-based furnace is divided into two gas flows after passing through a gas-based furnace top hot gas heat exchanger I and a gas-based furnace top gas dust remover, wherein a pipeline of the gas-based furnace top purified gas is communicated with an inlet of a gas-based furnace top purified gas heating device, and an outlet pipeline of the gas-based furnace top purified gas heating device is communicated with a pipeline flowing out of first reducing gas through an outlet of a non-catalytic partial oxidation reformer and then is connected with a gas-based furnace.
Further, a second heat exchanger of the furnace hot gas and a third heat exchanger of the furnace hot gas are sequentially communicated between the first heat exchanger of the furnace hot gas of the gas-based furnace and the dust remover of the furnace hot gas of the gas-based furnace.
Further, the gas-based shaft furnace top purified gas heating device is a biomass gas generator hot flue gas heat exchanger and/or a biomass gas rising pipe heat exchanger; a biomass gas rising pipe heat exchanger is arranged outside a rising pipe between the biomass generator and the biomass gas ammonia water cooler, and a biomass generator hot flue gas heat exchanger is arranged outside a hot flue gas pipeline of the biomass generator.
Further, the top gas of the gas-based shaft furnace is subjected to CO removal 2 AssemblyComprises a shaft furnace top gas compressor and a first desulfurization and CO2 removal device; the gas-based shaft furnace is sequentially connected with a shaft furnace hot gas heat exchanger I, a gas-based shaft furnace top gas dust remover, a shaft furnace top gas compressor, a first desulfurization and CO2 removal device and a biomass gas generator hot flue gas heat exchanger through pipelines and then is communicated with a first reduction pipeline at an outlet of the non-catalytic partial oxidation reformer, and shaft furnace hot gas generated by the gas-based shaft furnace sequentially passes through the shaft furnace hot gas heat exchanger I, the gas-based shaft furnace top gas dust remover, the shaft furnace top gas compressor, the first desulfurization and CO2 removal device and the CO removal device and is generated after the biomass gas generator hot flue gas heat exchanger 2 After being mixed with the first reducing gas, the furnace top purified gas is introduced into a shaft furnace tuyere of the gas-based shaft furnace.
Scheme II: a device for preparing gas-based shaft furnace reducing gas by purifying biomass gas comprises a gas-based shaft furnace, a gas-based shaft furnace top purified gas heating device, a biomass producer, a biomass gas ammonia water cooler, a biomass gas purification system, a non-catalytic partial oxidation reformer, a gas compressor, a gas-based shaft furnace top hot gas heat exchanger I, a gas-based shaft furnace top gas dust remover and a gas-based shaft furnace top gas CO removal device 2 The device comprises a component, a hydrogen-rich non-hydrocarbon gas source, a pure oxygen source and a water vapor source; the biomass producer is sequentially communicated with the biomass gas ammonia water cooler and the biomass gas purifying system through the ascending pipeline, and biomass gas generated in the biomass producer flows through the biomass gas ammonia water cooler and the biomass gas purifying system, and the biomass gas purifying system is used for removing tar, naphthalene, sulfur, benzene and CO from the biomass gas 2 The gas compressor is communicated with a first gas-based shaft furnace top hot gas heat exchanger, the first gas-based shaft furnace top hot gas heat exchanger is communicated with a gas pipeline of a burner positioned on the non-catalytic partial oxidation reformer through a pipeline, an oxygen passage of the burner is communicated with a pure oxygen source through the pipeline, a steam passage of the burner is communicated with a steam source through the pipeline, pure oxygen and mixed gas are partially oxidized and combusted in the non-catalytic partial oxidation reformer, and first reducing gas is generated and flows out from an outlet of the non-catalytic partial oxidation reformer; part of the furnace hot gas of the gas-based furnace passes through a gas-based furnace top hot gas heat exchanger I and a gas-based furnace top gas dust remover Dividing into two gas streams, wherein one gas stream is subjected to CO removal through the top gas of the gas-based shaft furnace 2 Component CO removal 2 Then is communicated with a hydrogen-rich non-hydrocarbon gas source and is mixed and preheated to become purified gas at the top of the gas-based shaft furnace, and the other gas does not remove CO 2 Is output as other uses; wherein, the purified gas at the top of the gas-based shaft furnace is heated by a purified gas heating device at the top of the gas-based shaft furnace, then mixed with the first reducing gas flowing out from an outlet of the non-catalytic partial oxidation reformer, and then enters the gas-based shaft furnace.
Compared with the prior art, the utility model has the following effects:
1. the utility model adopts a mode of converting the physical heat of hot coal gas in the ascending pipe of the biomass gas producer 9 and/or hot flue gas of the biomass gas producer into reducing gas through a heat exchanger to heat the reducing gas. The problem of the tubular heating furnace external combustion heating, the emission flue gas has been effectually solved, and then avoid the extravagant and the air pollution's of heat energy problem, does not still need intermediate medium heat transfer simultaneously, and heat exchange efficiency is high.
2. CO is not removed in the utility model 2 The top gas of the gas-based shaft furnace is used for fuel gas of other projects or used as chemical raw materials, and is not used as fuel gas of the gas-based shaft furnace any more, so that the problem of N2 enrichment caused by recycling of the top gas in the gas-based shaft furnace is solved.
3. The utility model realizes the preparation of the reducing gas of the gas-based shaft furnace by using the biomass gas through two modes of replacing the biomass gas with the same calorific value as the top gas of the gas-based shaft furnace and cross utilization of the heat energy of the gas-based shaft furnace and the biomass gas generator. By adopting different heating modes for the coal gas with different properties, no exhaust emission is realized in the whole process of preparing the reducing gas, and the purposes of full self-circulation recycling of the heat energy of the self-produced coal gas of the gas-based shaft furnace and no N2 enrichment are indirectly realized.
4. The utility model is characterized in that the water and CO of the furnace top purified gas 2 The content can be reduced to the design requirement through control, so that the effective components of the mixed reducing gas can be improved after the high-temperature reducing gas at the outlet of the non-catalytic partial oxidation furnace is mixed; the purified gas at the furnace top can be increased after being preheatedThe mixing amount of the top purified gas can further improve the effective components of the mixed reducing gas;
5. the internal combustion type non-catalytic partial oxidation technology is higher in heat efficiency and energy-saving than an external combustion type tubular heating furnace;
6. according to the utility model, a non-catalytic partial oxidation furnace with a refractory lining is used for replacing a heating furnace consisting of hundreds of heat-resistant steel pipes, so that the investment is further reduced;
7. The utility model uses renewable biomass gas as raw material gas of the gas-based shaft furnace for the first time, and provides a solution for distributing hydrocarbon-rich gas and/or hydrogen gas aiming at the problem that the biomass gas has high CO content and is not suitable for the gas-based shaft furnace: when the biomass gas and the hydrocarbon-rich gas are distributed, a scheme of firstly distributing the gas and then feeding the gas into an internal combustion heating furnace is adopted; when the biomass gas and the hydrogen-rich gas are distributed, an advanced internal combustion type heating furnace for biomass gas is adopted, and then a hydrogen distribution scheme is adopted. The ratio of H2/CO in the produced reducing gas reaches the gas requirement of the gas-based shaft furnace;
8. the utility model provides a reasonable distribution ratio of the distribution of the biomass and the coke oven gas, and ensures that the reducing gas prepared from the mixed gas of the biomass gas and the coke oven gas meets the gas requirement of the gas-based shaft furnace;
9. aiming at the problems that the content of unsaturated hydrocarbon in biomass gas is high, carbon is easy to accumulate in the reforming process, deep desulfurization, deep purification and the like are required for preventing catalyst poisoning, the utility model provides a mixed gas scheme for treating biomass gas and/or hydrocarbon-rich gas by adopting a non-catalytic partial oxidation process. The problem of easy carbon deposition is avoided, the catalyst is not needed, excessive deep purification is not needed, the process steps are simplified, and the investment and the operation cost are reduced.
Drawings
FIG. 1 is a system flow diagram of a first embodiment; fig. 2 is a system flow diagram of a second embodiment. FIG. 3 is a system flow diagram of a third embodiment; FIG. 4 is a system flow diagram of embodiment four; FIG. 5 is a system flow diagram of embodiment five; FIG. 6 is a system flow diagram of a sixth embodiment;
Detailed Description
The first embodiment is as follows: combining fig. 1, 2 and graph4 to 6 illustrate the present embodiment, which includes a gas-based shaft furnace 1, a gas-based shaft furnace top purified gas heating device, a biomass generator 9, a biomass gas ammonia water cooler 94, a biomass gas purification system 95, a non-catalytic partial oxidation reformer 2, a gas compressor 52, a gas-based shaft furnace top hot gas heat exchanger 13, a gas-based shaft furnace top gas dust remover 16, a gas-based shaft furnace top gas CO removal device 2 The assembly, a hydrocarbon-rich gas source 5, a pure oxygen source 4 and a water vapor source 7;
the biomass generator 9 is sequentially communicated with the biomass gas ammonia water cooler 94 and the biomass gas purifying system 95 through a rising pipeline, biomass gas 91 generated in the biomass generator 9 flows through the biomass gas ammonia water cooler 94 and the biomass gas purifying system 95, and the biomass gas purifying system 95 is used for removing tar, naphthalene, sulfur, benzene and CO from the biomass gas 91 2 Then, the gas compressor 52 is communicated with the first gas heat exchanger 13 of the gas-based shaft furnace top, the first gas heat exchanger 13 of the gas-based shaft furnace top is communicated with a gas pipeline of a burner 3 positioned on the non-catalytic partial oxidation reformer 2 through the pipeline, an oxygen passage of the burner 3 is communicated with a pure oxygen source 4 through the pipeline, a steam passage of the burner 3 is communicated with a steam source 7 through the pipeline, so that partial oxidation combustion of pure oxygen and the mixed gas 51 in the non-catalytic partial oxidation reformer 2 is realized, and the generated first reducing gas 21 flows out through an outlet of the non-catalytic partial oxidation reformer 2; a part of the furnace hot gas 12 of the gas-based furnace 1 is divided into two gas flows through a gas-based furnace top hot gas heat exchanger 13 and a gas-based furnace top gas dust remover 16, wherein a pipeline of the gas-based furnace top purified gas 121 is communicated with an inlet of a gas-based furnace top purified gas heating device, and an outlet pipeline of the gas-based furnace top purified gas heating device is communicated with a pipeline flowing out of the first reducing gas 21 through an outlet of the non-catalytic partial oxidation converter 2 and then is connected with the gas-based furnace 1.
The second embodiment is as follows: the description of the present embodiment is given with reference to fig. 1, 2, and 4 to 6, in which the first gas-based furnace top hot gas heat exchanger 13 and the second gas-based furnace top gas dust collector 16 of the present embodiment are further sequentially connected to each other by the second and third heat exchangers 14 and 15. Other compositions and communication relationships are the same as those of the first embodiment.
And a third specific embodiment: the gas-based shaft furnace top purified gas heating apparatus according to the present embodiment is a biomass gas producer hot flue gas heat exchanger 92 and/or a biomass gas riser heat exchanger 93, described with reference to fig. 1, 2, and 4 to 6; a biomass gas riser heat exchanger 93 is arranged outside a riser between the biomass generator 9 and the biomass gas ammonia water cooler 94, and a biomass generator hot flue gas heat exchanger 92 is arranged outside a biomass generator hot flue gas pipeline 81. The arrangement is convenient for selecting at least one heat exchange mode according to different use conditions. Other compositions and communication relationships are the same as those of the first or second embodiment.
The specific embodiment IV is as follows: the description of the present embodiment will be given with reference to fig. 1, 2, and 4 to 6, in which the top gas of the gas-based shaft furnace is CO-removed 2 The assembly comprises a shaft furnace top gas compressor 17 and a first desulphurisation, CO2 removal device 18;
the gas-based shaft furnace 1 is sequentially connected with a first shaft furnace hot gas heat exchanger 13, a gas-based shaft furnace top gas dust remover 16, a shaft furnace top gas compressor 17, a first desulfurization and CO2 removal device 18 and a biomass gas generator hot smoke heat exchanger 92 through pipelines, and then is communicated with a first reduction pipeline at the outlet of the non-catalytic partial oxidation reformer 2, and the shaft furnace hot gas 12 generated by the gas-based shaft furnace 1 sequentially passes through the first shaft furnace hot gas heat exchanger 13, the gas-based shaft furnace top gas dust remover 16, the shaft furnace top gas compressor 17, the first desulfurization and CO2 removal device 18 and CO removal generated after the biomass gas generator hot smoke heat exchanger 92 2 Is mixed with the first reducing gas 21 and is introduced into the shaft furnace tuyere of the gas-based shaft furnace 1. So arranged, the CO removal of the hot coal gas 12 of the shaft furnace is convenient 2 . Other compositions and communication relationships are the same as those of the first, second or third embodiments.
Fifth embodiment: the present embodiment will be described with reference to fig. 1, 2, and 4 to 6, in which water 71 in the present embodiment is connected to a biomass gas riser heat exchanger 93 through a pipe, and a steam gas source 7 after heat exchange is supplied to the burner 3. So arranged, the generated steam and oxygen are convenient to generate partial oxidation reaction. Other compositions and communication relationships are the same as those of the first, second, third or fourth embodiments.
Specific embodiment six: the present embodiment will be described with reference to fig. 5 to 6, and further includes a cooling gas heat exchanger 151, a cooling gas dust remover 161, and a second desulfurization/CO 2 removal device 181, wherein the cooling gas heat exchanger 151, the cooling gas dust remover 161, and the second desulfurization/CO 2 removal device 181 are connected in series with the gas-based shaft furnace 1 in this order, and one end of the cooling gas heat exchanger 151 is connected to the first shaft furnace hot gas heat exchanger 13 or the biomass gas riser heat exchanger 93 through a pipe, and the other end of the cooling gas heat exchanger 151 is connected to a pipe between the biomass gas generator hot flue gas heat exchanger 92 and the first desulfurization/CO 2 removal device 18, or to the burner 3. The arrangement is convenient for carrying out secondary desulfurization and CO2 removal on the hot coal gas 12 of the shaft furnace, and ensures the desulfurization and CO2 removal effect of the hot coal gas 12 of the shaft furnace. Other compositions and communication relationships are the same as those of the first, second, third, fourth or fifth embodiments.
Seventh embodiment: the present embodiment will be described with reference to fig. 5 and 6, and further includes a cooling gas compressor 171, wherein one end of the cooling gas compressor 171 is in communication with the gas-based shaft furnace 1, and the other end of the cooling gas compressor 171 is in communication with a pipeline between the biomass gas purification system 95 and the biomass gas generator hot flue gas heat exchanger 92. The arrangement is convenient for compressing the hot coal gas 12 of the gas-based shaft furnace 1, and then further desulfurizing and CO2 removing treatment. Other compositions and communication relationships are the same as those in any one of the first to sixth embodiments.
Eighth embodiment: the present embodiment will be described with reference to fig. 1, 2, and 4 to 6, and further includes an air line 8 and a biomass gas producer hot flue gas line 81, where the air line 8 is connected to the biomass producer 9, and the biomass gas producer hot flue gas line 81 is connected to a biomass gas producer hot flue gas heat exchanger 92. So arranged, the biomass gas producer hot flue gas 81 is generated by burning residual carbon and air 8 after gas production in the producer. Other compositions and communication relationships are the same as those in any one of the first to seventh embodiments.
Detailed description nine: the present embodiment is described with reference to fig. 3, and includes a gas-based shaft furnace 1, a gas-based shaft furnace top purified gas heating device, a biomass generator 9, a biomass gas ammonia water cooler 94, a biomass gas purification system 95, a non-catalytic partial oxidation reformer 2, a gas compressor 52, a gas-based shaft furnace top hot gas heat exchanger 13, a gas-based shaft furnace top gas dust remover 16, and a gas-based shaft furnace top gas CO removal device 2 The assembly, a hydrogen-rich non-hydrocarbon gas source 6, a pure oxygen source 4 and a water vapor source 7;
the biomass generator 9 is sequentially communicated with the biomass gas ammonia water cooler 94 and the biomass gas purification system 95 through a rising pipeline, biomass gas 91 generated in the biomass generator 9 flows through the biomass gas ammonia water cooler 94 and the biomass gas purification system 95, the biomass gas purification system 95 is used for removing tar, naphthalene, sulfur, benzene and CO2 from the biomass gas 91, the gas compressor 52 is communicated with the first gas heat exchanger 13 at the top of the gas-based shaft furnace, the first gas heat exchanger 13 at the top of the gas-based shaft furnace is communicated with a gas pipeline of a burner 3 positioned on the non-catalytic partial oxidation reformer 2 through a pipeline, an oxygen pipeline of the burner 3 is communicated with a pure oxygen source 4 through a pipeline, a steam pipeline of the burner 3 is communicated with a steam gas source 7 through a pipeline, and pure oxygen and mixed gas 51 are partially oxidized and combusted in the non-catalytic partial oxidation reformer 2 to generate a first reducing gas 21 which flows out from an outlet of the non-catalytic partial oxidation reformer 2; a part of the furnace hot gas 12 of the gas-based furnace 1 is divided into two gas flows through a gas-based furnace top hot gas heat exchanger 13 and a gas-based furnace top gas dust remover 16, wherein one gas flow is subjected to CO removal through the gas-based furnace top gas 2 Component CO removal 2 Then is communicated with a hydrogen-rich non-hydrocarbon gas source 6 and is mixed and preheated to become gas-based shaft furnace top purified gas 121, and the other gas does not remove CO 2 Is output as other uses; wherein, the gas-based shaft furnace top purified gas 121 is heated by a gas-based shaft furnace top purified gas heating device, then mixed with the first reducing gas 21 flowing out from the outlet of the non-catalytic partial oxidation reformer 2, and then enters the gas-based shaft furnace 1.
Detailed description ten: the present embodiment will be described with reference to fig. 3, which further includes a cooling gas heat exchanger 151, a cooling gas dust collector 161, and a second desulfurization/CO 2 removal device 181, wherein the cooling gas heat exchanger 151, the cooling gas dust collector 161, and the second desulfurization/CO 2 removal device 181 are connected in series with the gas-based shaft furnace 1 in this order, and one end of the cooling gas heat exchanger 151 is connected to a drain pipe 711, and the other end of the cooling gas heat exchanger 151 is connected to the burner 3. The arrangement is convenient for carrying out secondary desulfurization and CO2 removal on the hot coal gas 12 of the shaft furnace, and ensures the desulfurization and CO2 removal effect of the hot coal gas 12 of the shaft furnace. Other compositions and communication relationships are the same as in any one of the first to ninth embodiments.
Embodiment one:
please refer to fig. 1: biomass gas 91 generated by the biomass gas producer 9 is cooled to about 500 ℃ through a biomass gas riser heat exchanger 93, enters a biomass gas ammonia water cooler 94 for further cooling, is separated from tar, naphthalene, sulfur and CO2 through a biomass gas purification system 95 according to the well-known treatment technology in the industry, is mixed with hydrocarbon-rich gas 5 (coke oven gas) to become mixed gas 51, the mixed gas 51 is pressurized through a compressor 52 (referred to as a gas compressor 52), hot gas 12 entering the top of the gas-based shaft furnace 1 is subjected to heat exchange to about 200 ℃ through a first heat exchanger 13 (referred to as a first shaft furnace hot gas heat exchanger), enters a gas channel of the non-catalytic partial oxidation furnace burner 3, pure oxygen 4 enters an oxygen channel of the non-catalytic partial oxidation furnace burner 3 after being subjected to heat exchange through a second heat exchanger 14 (referred to as a second shaft furnace hot gas heat exchanger), and water 71 enters a steam channel of the non-catalytic partial oxidation furnace burner through the heat exchanger 93 (referred to as a biomass gas riser heat exchanger 93). Pure oxygen and mixed gas 51 at the outlet of the burner 3 are subjected to anoxic combustion to generate first reducing gas with main components of H2, CO and H2O, wherein the ratio of the biomass gas to the hydrocarbon-rich gas is regulated to ensure that H2/CO is more than or equal to 1.6. At the outlet of the non-catalytic partial oxidation furnace 2, the first reducing gas 21 is about 1200 ℃.
And one part of the gas-based furnace top gas is subjected to heat exchange and dehydration through a first heat exchanger 13 and a second heat exchanger 14, is subjected to dust removal through a dust remover 16, is pressurized through a compressor 17 (referred to as a furnace top gas compressor 17), and is treated through a desulfurization and CO2 removal device 18 to form furnace top purified gas 121. The sum of water and CO2 content of the top purified gas 121 is controlled to be less than 10% through dehydration and CO2 removal, the top purified gas 121 enters a hot flue gas heat exchanger 92 (referred to as a biomass gas producer hot flue gas heat exchanger) of a biomass gas producer 9 to exchange heat, biomass gas producer hot flue gas 81 is generated by burning residual carbon after gas production in the producer with air 8, the top purified gas 121 after heat exchange is mixed with first reducing gas 21 at 1200 ℃ at the outlet of a non-catalytic partial oxidation furnace 2 to form mixed reducing gas, the temperature of the mixed reducing gas is about 850-950 ℃, and the mixed reducing gas enters the gas-based shaft furnace 1 through a tuyere 11. In the gas-based shaft furnace 1, iron oxide reacts with the reducing gas and is reduced into direct reduced iron, the direct reduced iron is discharged out of the furnace through the lower part of the gas-based shaft furnace 1, and crude gas generated by the reaction is discharged from the furnace top of the shaft furnace to become gas 12 of the gas-based shaft furnace.
The other part of the gas-based shaft furnace top gas 122 without CO2 is output as chemical raw material for preparing methanol, and the whole gas-based shaft furnace system has no gas emission.
Embodiment two:
please refer to fig. 2: the difference with fig. 1 is that the top purified gas 121 enters the biomass gas riser heat exchanger for heat exchange, and the water 71 flows through the hot flue gas heat exchanger 92 of the biomass gas generator 9 to generate steam 7, and other processes are the same.
Embodiment III:
please refer to fig. 3: the biomass gas 91 generated by the biomass gas producer 9 is cooled to about 500 ℃ by a biomass gas rising pipe heat exchanger 93, enters a biomass gas ammonia water cooler 94 for further cooling, and is subjected to tar, naphthalene, sulfur and CO removal by a purification system 95 according to the treatment technology known in the industry 2 Then, the biomass gas is divided into two branches, namely a biomass gas first branch 911 and a biomass gas second branch 912, the biomass gas second branch 912 is pressurized by the compressor 52, the top hot gas 12 entering the gas-based shaft furnace exchanges heat to about 300 ℃ in the first hot gas heat exchanger 13 of the shaft furnace, the gas enters a gas channel of the non-catalytic partial oxidation furnace burner 3, pure oxygen 4 enters an oxygen channel of the non-catalytic partial oxidation furnace burner 3 after exchanging heat in the second heat exchanger 14, and steam 7 generated by the heat exchanger 151 enters a steam channel of the non-catalytic partial oxidation furnace burner. Pure oxygen 4 and second are discharged from the burner 3The branched biomass gas 912 is subjected to anoxic combustion to generate first reducing gas with the main components of H2, CO and H2O. At the outlet of the non-catalytic partial oxidation furnace 2, the first reducing gas 21 is at about 1270 ℃.
The first branch biomass gas 911 is used as cooling gas of the reduced iron of the gas-based shaft furnace, enters from the bottom of the gas-based shaft furnace through a compressor 171 (referred to as a cooling gas compressor), is discharged from the upper part of the cooling section of the gas-based shaft furnace, is cooled and dehydrated through a heat exchanger 151, and is dedusted by a deduster 161, desulfurized and CO 2 After the device 181, it is mixed with the first branched biomass gas 911 to be used as a cooling gas for the reduced iron of the gas-based shaft furnace.
And a part of the gas-based furnace top gas is subjected to heat exchange and dehydration through a first furnace hot gas heat exchanger 13 and a second furnace hot gas heat exchanger 14, is subjected to dust removal through a dust remover 16, is pressurized through a compressor 17, and is treated through a desulfurization and CO2 removal device 18 to form furnace top purified gas 121. By dehydration and CO removal 2 Control of water and CO of top gas 121 2 The sum of the contents is less than 10%, after the top purified gas 121 is mixed into the hydrogen-rich non-hydrocarbon gas 6, the hydrogen-rich non-hydrocarbon gas is divided into two branches, the two branches respectively enter a hot flue gas heat exchanger 92 of a biomass gas producer 9 and a biomass gas riser heat exchanger 93 for heat exchange, the two branches after heat exchange are mixed into the top purified gas 121, the biomass gas producer hot flue gas 81 is generated by burning residual carbon after gas production in the producer with air 8, the top purified gas 121 after heat exchange is mixed with a first reducing gas 21 at 1270 ℃ at the outlet of a non-catalytic partial oxidation furnace 2 to form mixed reducing gas, the temperature of the mixed reducing gas is about 900-950 ℃, H2/CO is more than or equal to 1.6, and the mixed reducing gas enters the gas-based shaft furnace 1 through a tuyere 11. In the gas-based shaft furnace 1, iron oxide reacts with the reducing gas and is reduced into direct reduced iron, the direct reduced iron is discharged out of the furnace through the lower part of the gas-based shaft furnace 1, and crude gas generated by the reaction is discharged from the furnace top of the shaft furnace to become gas 12 of the gas-based shaft furnace.
Another part is not CO removed 2 The gas-based shaft furnace top gas 122 is output as chemical raw material for preparing urea, and the whole gas-based shaft furnace system has no gas emission.
Embodiment four:
please refer to fig. 4. The biomass gas 91 generated by the biomass gas generator 9 passes through the biomass gasThe temperature of the rising pipe heat exchanger 93 is reduced to about 500 ℃, the biomass gas ammonia water cooler 94 is further cooled, and tar, naphthalene, sulfur and CO are removed by a purification system 95 according to the treatment technology known in the industry 2 Then, the mixture is mixed with hydrocarbon-rich gas 5 (coke oven gas) to become mixed gas 51, the mixed gas 51 is pressurized by a compressor 52, enters a heat exchanger I13 of a top hot gas 12 of the gas-based shaft furnace, exchanges heat to about 200 ℃, enters a gas channel of a non-catalytic partial oxidation furnace burner 3, pure oxygen 4 enters an oxygen channel of the non-catalytic partial oxidation furnace burner 3 after exchanging heat in a heat exchanger II 14, and water enters a steam channel of the non-catalytic partial oxidation furnace burner through steam 7 generated by a heat exchanger III 15. Pure oxygen 4 and mixed gas 51 are subjected to anoxic combustion at the outlet of the burner 3 to generate first reducing gas with main components of H2, CO and H2O, wherein the ratio of the biomass gas to the hydrocarbon-rich gas is regulated to ensure that H2/CO is more than or equal to 1.8. At the outlet of the non-catalytic partial oxidation furnace 2, the first reducing gas 21 is at about 1250 ℃.
And a part of the gas-based shaft furnace top gas is subjected to heat exchange and dehydration through heat exchangers 13 and 14, is subjected to dust removal through a dust remover 16 (referred to as a gas-based shaft furnace top gas dust remover 16), is pressurized through a compressor 17, is treated through a desulfurization and CO2 removal device 18, and becomes furnace top purified gas 121 (the flow rate is about 750M 3/t.iron), and the sum of the water content and the CO2 content of the furnace top purified gas 121 is controlled to be less than 9% through dehydration and CO2 removal. The furnace top purified gas 121 is divided into two branches, the two branches enter a hot flue gas heat exchanger 92 and a biomass gas rising pipe heat exchanger 93 of a biomass gas producer 9 respectively for heat exchange, the two branches after heat exchange are mixed into the furnace top purified gas 121, at the moment, the temperature of the furnace top purified gas 121 reaches about 660 ℃, the biomass gas producer hot flue gas 81 is generated by burning residual carbon after gas production in the producer and air 8, the furnace top purified gas 121 after heat exchange is mixed with 1250 ℃ first reducing gas 21 (with the flow of about 1000M 3/t.iron) at the outlet of a non-catalytic partial oxidation furnace 2 to form mixed reducing gas, the temperature of the mixed reducing gas is about 1000 ℃, the mixed reducing gas enters the gas-based shaft furnace 1 through a tuyere 11, and the water content of the reducing gas 21 generated by the non-catalytic partial oxidation furnace in the mixed reducing gas is reduced by adding the furnace top purified gas 121, and the effective components of the mixed reducing gas entering the gas-based shaft furnace are improved. As the preheating temperature of the top purified gas 121 is further increased, the mixing amount of the top purified gas 121 is increased, the water content of the mixed reducing gas entering the gas-based shaft furnace is further reduced, and the effective components of the mixed reducing gas entering the gas-based shaft furnace are improved. In the gas-based shaft furnace 1, iron oxide reacts with the reducing gas and is reduced into direct reduced iron, the direct reduced iron is discharged out of the furnace through the lower part of the gas-based shaft furnace 1, and crude gas generated by the reaction is discharged from the furnace top of the shaft furnace to become gas 12 of the gas-based shaft furnace.
Residual unde CO 2 The gas-based shaft furnace top gas 122 with the flow rate of about 470M 3/t-iron (the heat value of about 2000 kcal/M3), the equivalent heat value of the replaced biomass gas 91, the flow rate of about 235M 3/t-iron (the heat value of the biomass gas of about 4000 kcal/M3), the replaced biomass gas 91 (the flow rate of 235M 3/t-iron) and the newly-supplemented biomass gas 9 (the flow rate of about 130M 3/t-iron) are mixed into mixed gas with the flow rate of about 660M 3/t-iron by the aid of the hydrocarbon-rich gas 5 (the flow rate of about 295M 3/t-iron) in the coke oven gas, the top gas 122 of the gas-based shaft furnace 1 without CO2 removal replaces the biomass gas 8 to serve other purposes, the purpose of the gas-based self-produced gas heat energy self-circulation shaft furnace is indirectly realized through a gradient utilization mode of different types of gas, the whole gas-based shaft furnace system does not need external combustion of reducing gas in a heating pipe, exhaust emission generated by external combustion is avoided, nitrogen is not enriched in the gas-based shaft furnace, and normal operation and production efficiency is not influenced.
Fifth embodiment:
referring to fig. 5, the difference between the flow of fig. 5 and the flow of fig. 4 is that: the mixed gas 51 firstly enters the top hot gas 12 of the gas-based shaft furnace to exchange heat in the first heat exchanger 13, then enters the heat exchanger of the hot recycle gas discharged from the cooling section of the gas-based shaft furnace to exchange heat for the second time, and then enters the gas channel of the non-catalytic partial oxidation furnace burner 3.
Example six:
please refer to fig. 6. Fig. 6 differs from the flow of fig. 4 in that: the top purified gas 121 is divided into three branches, and the three branches enter a hot flue gas heat exchanger 92, a biomass gas rising pipe heat exchanger 93 and a hot recycle gas heat exchanger discharged from a cooling section of the gas-based shaft furnace of the biomass gas generator 9 respectively for heat exchange, the three branches after heat exchange are mixed into the top purified gas 121, and the mixed top purified gas 121 is mixed with the 1250 ℃ first reducing gas 21 at the outlet of the non-catalytic partial oxidation furnace 2.
In addition, the device for purifying the biomass gas to prepare the gas-based shaft furnace reducing gas is adopted to realize the principle of preparing the gas-based shaft furnace reducing gas from the biomass gas:
introducing a raw material gas containing biomass gas into a gas heating furnace through a pipeline for heating; the method comprises the steps of reforming gas in a gas heating furnace into first reducing gas, then entering the gas-based shaft furnace, reacting iron oxide with the reducing gas in the gas-based shaft furnace, directly reducing the iron oxide into reduced iron, discharging the directly reduced iron out of the furnace through the lower part of the gas-based shaft furnace, discharging crude gas generated by the reaction from the top of the shaft furnace, adding second reducing gas into the first reducing gas, adjusting the temperature, and then entering the gas-based shaft furnace.
The hot gas generated by the biomass gas producer is mixed with hydrocarbon-rich gas after passing through a heat exchanger, an ammonia water cooler and a gas purifying system, the components are regulated to form mixed gas, and then the mixed gas enters an internal combustion type heating furnace after passing through a pressurizing device and a preheating device, is combusted with oxygen in the internal combustion type heating furnace, and undergoes partial oxidation reaction to generate first reducing gas with the main components of H2, CO and H2O.
The hot coal gas generated by the biomass gas generator can also enter the internal combustion heating furnace after passing through the heat exchanger, the ammonia water cooler, the coal gas purifying system, the pressurizing device and the preheating device, and is combusted with oxygen in the internal combustion heating furnace to generate a first reducing gas with main components of H2, CO and H2O by partial oxidation reaction, and then a second reducing gas regulating component which is rich in hydrogen and non-hydrocarbon is added.
The two schemes are preferably used for removing CO by a gas purifying system 2 And (3) gas.
The hot gas heat exchanger is arranged around the biomass gas ascending pipe, and the second reducing gas of the gas-based shaft furnace is added into the first reducing gas of the gas-based shaft furnace after heat exchange of the biomass gas ascending pipe heat exchanger and/or the biomass gas generator hot flue gas heat exchanger. The main component of the second reducing gas is H2 and/or CO, and H2+CO accounts for more than 90% of the total gas amount.
Preferably the second reducing gas is a gas-based shaft furnace top clean gas. Furnace roofThe purified gas comes from heat exchange, dehydration, dust removal, desulfurization and CO removal of a part of crude gas at the top of the gas-based shaft furnace 2 And (3) treating, namely, carrying out heat exchange, dehydration and dust removal treatment on the other part of the raw gas at the top of the gas-based shaft furnace to obtain the gas at the top of the gas-based shaft furnace. When the internal combustion heating furnace only heats biomass gas, the top purified gas also needs to be added with hydrogen-rich non-hydrocarbon gas.
The biomass gas is replaced by the gas-based shaft furnace top gas with equal heating value; the replaced biomass gas and the newly-supplemented biomass gas enter a heating furnace together for heating, wherein the heating furnace adopts an internal combustion type heating furnace which is a non-catalytic partial oxidation furnace; the biomass gas is replaced by the gas-based shaft furnace top gas and other heat values, so that the hydrocarbon-rich biomass gas is heated in the internal combustion type non-catalytic partial oxidation furnace, the requirement on biomass gas purification is reduced, the purification process flow is simplified, the investment is reduced, the problem of carbon deposition of the tubular heating furnace is avoided, and the fact that waste gas is not discharged in the heating process of the first reducing gas is realized. The top gas of the gas-based shaft furnace for replacement is used for other purposes.
Through the heat energy cross utilization of the gas-based shaft furnace and the biomass gas generator, the reducing gas heating of the biomass gas system for the gas-based shaft furnace system is realized, namely, the biomass gas in the biomass gas ascending pipe and/or the hot flue gas of the biomass gas generator are/is directly used for heat exchange to supply the second reducing gas to the gas-based shaft furnace, and no waste gas emission in the heating process of the second reducing gas is realized.
The biomass gas is prepared into the gas-based shaft furnace reducing gas by the two modes of replacing biomass gas with the gas-based shaft furnace top gas and the like in a heat value and cross utilization of the gas-based shaft furnace and the biomass gas generator heat energy. By adopting different heating modes for the coal gas with different properties, the whole process of preparing the reducing gas has no exhaust emission, and the aim of recycling the heat energy of the self-produced coal gas of the gas-based shaft furnace is indirectly realized.
The replaced biomass gas and the newly-supplemented biomass gas are pressurized to 0.15-1Mpa and then enter a gas channel of the non-catalytic partial oxidation furnace burner, and preheated pure oxygen and steam enter respective channels of the non-catalytic partial oxidation furnace burner respectively. Pure oxygen and mixed gas are subjected to anoxic combustion at the outlet of the burner to generate high-temperature reducing gas taking CO, H2 and H2O as main components, and the high-temperature reducing gas reaches 1100-1350 ℃ at the outlet of the non-catalytic partial oxidation furnace.
The second reducing gas is preheated and then mixed with high-temperature reducing gas at the outlet of the non-catalytic partial oxidation furnace to form mixed reducing gas, the temperature of the mixed reducing gas is 850-1100 ℃, and the mixed reducing gas enters the gas-based shaft furnace through the tuyere.
The preheating of the pure oxygen and the generation of the steam are realized in the following way, and the waste heat of the hot gas of the top of the gas-based shaft furnace and/or the hot gas of the biomass gas rising pipe is utilized.
The raw material gas containing biomass gas can be single biomass gas or mixed gas of biomass gas and hydrocarbon-rich gas.
The apparatus reduction method for preparing a gas-based shaft furnace reduction gas by purifying biomass gas according to the present utility model will be described with reference to fig. 1 to 6:
a method for preparing gas-based shaft furnace reducing gas from biomass gas comprises the following steps: introducing raw material gas into a gas heating furnace through a pipeline for heating, reforming the gas in the heating furnace into first reducing gas, then entering a gas-based shaft furnace, and discharging raw gas generated by the reaction in the gas-based shaft furnace from the top of the shaft furnace;
Step two: the raw material gas comprises biomass gas and hydrocarbon-rich gas, or biomass gas and hydrogen-rich non-hydrocarbon gas;
s1: when the feed gas is a biomass gas and a hydrocarbon-rich gas: the biomass gas is purified to remove tar, naphthalene, sulfur, ammonia, benzene and CO in the biomass gas 2 Then mixing the mixture with hydrocarbon-rich gas, then entering an internal combustion heating furnace, combusting with oxygen, generating partial oxidation reaction to generate first reducing gas with the main components of H2 and CO, adding second reducing gas into the first reducing gas, and then entering a gas-based shaft furnace;
s2: when the feed gas is a biomass gas and a hydrogen-rich non-hydrocarbon gas: the biomass gas enters an internal combustion heating furnace, burns with oxygen and generates partial oxidation reaction to generate first reducing gas with the main components of H2 and CO, hydrogen-rich non-hydrocarbon gas or hydrogen-rich non-hydrocarbon gas and second reducing gas are added into the first reducing gas, and then the first reducing gas enters a gas-based shaft furnace, wherein the main components of the second reducing gas are H2 and CO.
Further, the biomass gas in the S1 of the second step is firstly mixed with hydrocarbon-rich gas and then purified to remove tar, naphthalene, sulfur, ammonia, benzene and CO in the biomass gas 2 。
Further, the internal combustion heating furnace in the step S1 and the step S2 is a non-catalytic partial oxidation furnace, and the biomass gas or the biomass gas and the hydrocarbon-rich gas are preheated by adopting a gas-based shaft furnace top hot gas heat exchanger and then are added into the non-catalytic partial oxidation furnace.
Further, the hydrogen-rich non-hydrocarbon gas and/or the second reducing gas in the second step is preheated by a biomass gas in a rising pipe heat exchanger and/or a biomass generating furnace high-temperature flue gas heat exchanger and/or a thermal cycle gas heat exchanger discharged by a gas-based shaft furnace cooling section, and then added into the first reducing gas.
Further, the second reducing gas in the S2 of the second step is gas-based shaft furnace top purified gas, and the top purified gas is part of gas-based shaft furnace top hot gas which is cooled, dedusted, desulfurized and removed from CO 2 And (5) the gas after the reaction.
Further, after biomass gas or biomass gas and hydrocarbon-rich gas in the second step are preheated by adopting a gas-based shaft furnace top hot gas heat exchanger, the biomass gas or the biomass gas and the hydrocarbon-rich gas are added into a non-catalytic partial oxidation furnace after being preheated and warmed by a thermal cycle gas heat exchanger discharged from a gas-based shaft furnace cooling section.
Further, another part of the second step is not CO stripped 2 The heat value of the top gas of the gas-based shaft furnace is used for replacing biomass gas, the replaced biomass gas and the newly-supplemented biomass gas are used for other purposes, the biomass gas and the newly-supplemented biomass gas enter a gas heating furnace for heating, and the self-circulation recycling of the gas energy of the gas-based shaft furnace is indirectly realized through the gradient utilization mode of different types of gas.
While only the preferred embodiments of the present utility model have been described, the present utility model is not limited to the above-described embodiments, and various modifications and equivalent substitutions for the features and embodiments of the present utility model may be made by those skilled in the art without departing from the spirit of the utility model and the scope of the appended claims without departing from the spirit of the utility model.
Claims (5)
1. The device for preparing gas-based shaft furnace reducing gas by purifying biomass gas is characterized in that: the device comprises a gas-based shaft furnace (1), a gas-based shaft furnace top purified gas heating device, a biomass producer (9), a biomass gas ammonia water cooler (94), a biomass gas purifying system (95), a non-catalytic partial oxidation reformer (2), a gas compressor (52), a gas-based shaft furnace top hot gas heat exchanger I (13), a gas-based shaft furnace top gas dust remover (16) and a gas-based shaft furnace top gas CO removal device 2 The device comprises a component, a hydrocarbon-rich gas source (5), a pure oxygen source (4) and a water vapor source (7);
the biomass generator (9) is sequentially communicated with the biomass gas ammonia water cooler (94) and the biomass gas purifying system (95) through a rising pipeline, biomass gas (91) generated in the biomass generator (9) flows through the biomass gas ammonia water cooler (94) and the biomass gas purifying system (95), and the biomass gas purifying system (95) is used for removing tar, naphthalene, sulfur, benzene and CO from the biomass gas (91) 2 Then, the gas compressor (52) is communicated with the first gas heat exchanger (13) of the gas-based shaft furnace, the first gas heat exchanger (13) of the gas-based shaft furnace is communicated with a gas pipeline of a burner (3) positioned on a non-catalytic partial oxidation reformer (2) through the pipeline, an oxygen channel of the burner (3) is communicated with a pure oxygen source (4) through the pipeline, a steam channel of the burner (3) is communicated with a steam source (7) through the pipeline, so that partial oxidation combustion of pure oxygen and mixed gas (51) in the non-catalytic partial oxidation reformer (2) is realized, and the generated first reducing gas (21) flows out through an outlet of the non-catalytic partial oxidation reformer (2); a part of the hot gas (12) of the gas-based shaft furnace (1) is divided into two gas flows through a first gas-based shaft furnace top hot gas heat exchanger (13) and a gas-based shaft furnace top gas dust remover (16), wherein a pipeline for purifying the gas (121) at the gas-based shaft furnace top and the gas-based shaft furnaceThe inlet of the top purified gas heating device is communicated, and the outlet pipeline of the top purified gas heating device of the gas-based shaft furnace is communicated with a pipeline flowing out of the first reducing gas (21) through the outlet of the non-catalytic partial oxidation converter (2) and then is connected with the inlet gas-based shaft furnace (1).
2. The apparatus for purifying biomass gas to produce gas-based shaft furnace reducing gas according to claim 1, wherein: the first gas-based furnace top hot gas heat exchanger (13) and the second gas-based furnace top gas dust remover (16) are also sequentially communicated with the second gas-based furnace top hot gas heat exchanger (14) and the third gas-based furnace top hot gas heat exchanger (15).
3. The apparatus for purifying biomass gas to produce gas-based shaft furnace reducing gas according to claim 2, wherein: the gas-based shaft furnace top purified gas heating device is a biomass gas generator hot flue gas heat exchanger (92) and/or a biomass gas rising pipe heat exchanger (93); a biomass gas rising pipe heat exchanger (93) is arranged outside a rising pipe between the biomass generator (9) and the biomass gas ammonia water cooler (94), and a biomass generator hot flue gas heat exchanger (92) is arranged outside a biomass generator hot flue gas pipeline (81).
4. A device for purifying biomass gas to produce a gas-based shaft furnace reducing gas according to claim 1 or 3, characterized in that: CO removal from top gas of gas-based shaft furnace 2 The assembly comprises a shaft furnace top gas compressor (17) and a first desulphurisation, CO2 removal device (18);
the gas-based shaft furnace (1) is sequentially connected with a first shaft furnace hot gas heat exchanger (13), a gas-based shaft furnace top gas dust remover (16), a shaft furnace top gas compressor (17), a first desulfurization and CO2 removal device (18) and a biomass gas producer hot gas heat exchanger (92) through pipelines and then communicated with a first reduction gas pipeline at an outlet of a non-catalytic partial oxidation reformer (2), and shaft furnace hot gas (12) generated by the gas-based shaft furnace (1) sequentially passes through the first shaft furnace hot gas heat exchanger (13), the gas-based shaft furnace top gas dust remover (16), the shaft furnace top gas compressor (17), the first desulfurization and CO2 removal device (18) and the biomass gas producer hot gas heat exchanger (92) Post-produced CO removal 2 The top purified gas (121) of (2) is mixed with the first reducing gas (21) and then introduced into the shaft furnace tuyere of the gas-based shaft furnace (1).
5. The device for preparing gas-based shaft furnace reducing gas by purifying biomass gas is characterized in that: comprises a gas-based vertical furnace (1), a gas-based vertical furnace top purified gas heating device, a biomass producer (9), a biomass gas ammonia water cooler (94), a biomass gas purifying system (95), a non-catalytic partial oxidation reformer (2), a gas compressor (52), a gas-based vertical furnace top hot gas heat exchanger I (13), a gas-based vertical furnace top gas dust remover (16) and a gas-based vertical furnace top gas CO removal device 2 The device comprises a component, a hydrogen-rich non-hydrocarbon gas source (6), a pure oxygen source (4) and a water vapor source (7);
the biomass generator (9) is sequentially communicated with the biomass gas ammonia water cooler (94) and the biomass gas purifying system (95) through a rising pipeline, biomass gas (91) generated in the biomass generator (9) flows through the biomass gas ammonia water cooler (94) and the biomass gas purifying system (95), and the biomass gas purifying system (95) is used for removing tar, naphthalene, sulfur, benzene and CO from the biomass gas (91) 2 The gas compressor (52) is communicated with the first gas heat exchanger (13) of the top of the gas-based shaft furnace, the first gas heat exchanger (13) of the top of the gas-based shaft furnace is communicated with a gas pipeline of a burner (3) positioned on the non-catalytic partial oxidation reformer (2) through a pipeline, an oxygen passage of the burner (3) is communicated with a pure oxygen source (4) through the pipeline, a steam passage of the burner (3) is communicated with a steam source (7) through the pipeline, pure oxygen and mixed gas (51) are partially oxidized and combusted in the non-catalytic partial oxidation reformer (2), and a first reducing gas (21) is generated and flows out from an outlet of the non-catalytic partial oxidation reformer (2); a part of the hot gas (12) of the gas-based shaft furnace (1) is divided into two gas flows through a first gas heat exchanger (13) of the gas-based shaft furnace top, and a gas flow is separated into two gas flows through a gas-based shaft furnace top gas dust remover (16), wherein one gas flow is subjected to CO removal through the gas-based shaft furnace top gas 2 Component CO removal 2 Then is communicated with a hydrogen-rich non-hydrocarbon gas source (6) and is mixed and preheated to become gas-based shaft furnace top purified gas (121), and the other gas does not remove CO 2 Is output as other uses; wherein the top of the gas-based shaft furnace is used for purifying gas (121 After being heated by a gas-based shaft furnace top purified gas heating device, the gas is mixed with first reducing gas (21) flowing out from an outlet of a non-catalytic partial oxidation converter (2) and then enters the gas-based shaft furnace (1).
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