CN214327120U - Multi-component raw gas conversion hydrogen production device - Google Patents
Multi-component raw gas conversion hydrogen production device Download PDFInfo
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- CN214327120U CN214327120U CN202022403867.5U CN202022403867U CN214327120U CN 214327120 U CN214327120 U CN 214327120U CN 202022403867 U CN202022403867 U CN 202022403867U CN 214327120 U CN214327120 U CN 214327120U
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Abstract
The utility model relates to the technical field of hydrogen production, in particular to a multi-component raw gas conversion hydrogen production device, which is provided with a primary pipeline at the outlet end of a secondary pressurizing unit raw gas compressor, and the other end of the primary pipeline at the outlet end of the secondary pressurizing unit raw gas compressor is connected with the inlet of a variable-pressure adsorption decarbonization unit variable-gas liquid separation tank; a primary pipeline of a coarse desulfurization outlet is arranged, and a secondary pipeline of fuel gas of a coarse desulfurization return reforming furnace and a secondary pipeline of a coarse desulfurization outlet are arranged at the other end of the primary pipeline of the coarse desulfurization outlet; a primary pipeline at the outlet end of the start-up separator and a secondary pipeline at the outlet of the start-up separator are arranged; the utility model discloses simplify the flow, can reduce the start-stop cost with diffusing the feed gas recovery and recycling, the flexible operation is stable, and is dangerous little, the energy saving.
Description
Technical Field
The utility model relates to the technical field of hydrogen production, in particular to a multi-component raw material gas conversion hydrogen production device.
Background
At present, most hydrogen production devices adopted by domestic oil refineries produce hydrogen by a hydrocarbon steam conversion process, but hydrogen production raw materials are single media and can be generally divided into gaseous hydrocarbons and liquid hydrocarbons, and the gaseous hydrocarbons mainly comprise natural gas, oil field gas, methane, hydrogenation dry gas, reforming dry gas, catalysis dry gas, aromatization dry gas and the like; the liquid hydrocarbons mainly include straight-run naphtha, hydrogenated light naphtha, raffinate oil and topping oil produced by a reformer, saturated liquefied petroleum gas produced by a hydrogenation unit, and the like.
The hydrogen production is carried out by taking the mixed gas of the coke oven gas, the low-temperature dry distillation gas and the natural gas as the hydrogen production raw material or taking any single gas source of the natural gas and the coal gas as the hydrogen production raw material, which has obvious advantages compared with the prior art, however, the gases have obvious differences in the aspects of components, heat values, impurity contents and the like, and particularly have larger differences in the aspects of hydrocarbon composition and unsaturated hydrocarbon content, so that certain difficulty exists in practical use.
For example, in the process of hydrogen production by coke oven gas conversion, after secondary pressurization is completed, the coke oven gas enters a converter and a medium temperature conversion system, the process is complicated, the equipment operation cost is increased, and the operation difficulty and the danger degree are increased.
In the process of driving the hydrogen production device, a large amount of raw material gas is inevitably required to be diffused, and particularly in the process of driving the hydrogen production device, because each link needs to detect that the corresponding index is qualified, air can be introduced into the next flow, so that a large amount of raw material gas is continuously diffused for a long time.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a multi-component raw material gas conversion hydrogen production device, which solves the problems of complex process, high operation cost, high operation difficulty and high danger degree existing in the process of producing hydrogen by a converter and a medium temperature conversion system in the prior art by using coke oven gas; solves the problem that the crude desulfurization unit inevitably needs to diffuse a large amount of raw material gas in the process of driving in the prior art when hydrogen is produced.
In order to solve the technical problem, the utility model relates to a multi-component raw gas conversion hydrogen production device, which comprises a primary pressurizing unit, a temperature swing adsorption unit, a pressure swing adsorption coarse desorption unit, a secondary pressurizing unit, a pressure swing adsorption decarburization unit and a pressure swing adsorption purification unit, wherein the primary pressurizing unit comprises a gas compressor, the temperature swing adsorption unit comprises a temperature swing adsorption tower, the pressure swing adsorption coarse desorption unit comprises an adsorption tower and an iron system dry desulfurization tower, the secondary pressurizing unit comprises a raw gas compressor, a pressure swing adsorption decarburization unit comprises a pressure swing gas separating tank, the primary pressurizing unit is connected with the front end of the temperature swing adsorption unit through a pipeline, the temperature swing adsorption unit is connected with the front end of the pressure swing adsorption coarse desorption unit through a pipeline, the pressure swing adsorption coarse desorption unit is connected with the front end of the secondary pressurizing unit through a pipeline, the pressure swing adsorption decarburization unit is connected with the front end of the pressure swing adsorption purification unit through a pipeline, the outlet of the feed gas compressor of the secondary pressurizing unit is connected with a primary pipeline at the outlet end of the feed gas compressor of the secondary pressurizing unit, the other end of the primary pipeline at the outlet end of the feed gas compressor of the secondary pressurizing unit is connected with the inlet of a variable-pressure-adsorption decarbonizing unit variable-gas liquid separating tank, the variable-pressure-adsorption purifying unit is connected to the rear end of the variable-pressure-adsorption decarbonizing unit variable-gas liquid separating tank through a pipeline, and a pressure regulating facility IV is connected to the primary pipeline at the outlet end of the feed gas compressor of the secondary pressurizing unit.
The coke oven gas is firstly introduced into a primary pressurizing unit, a temperature swing adsorption unit, a pressure swing adsorption coarse desorption unit and a secondary pressurizing unit in sequence according to a conventional method, after the treated gas is compressed from a raw gas compressor, the treated gas is respectively collected into a pressure regulating facility IV through a primary pipeline at the outlet end of the raw gas compressor of the secondary pressurizing unit for pressure reduction, directly enters a gas separation tank at the inlet of the pressure swing adsorption decarburization unit without a fine desulfurization unit, a conversion furnace and a medium temperature conversion unit of a hydrogenation reactor, and continuously enters the pressure swing adsorption decarburization unit and the pressure swing adsorption purification unit, the prepared hydrogen is led out by a product hydrogen output device, and the operation is finished.
Compared with the prior art, the utility model discloses with the direct intercommunication of secondary pressurization unit and pressure swing adsorption decarbonization unit, because reborner and medium temperature transform system stop, only put into operation coal gas purification and pressure swing adsorption system, the flow is simplified greatly to limit, so can reduce the running cost, the operation degree of difficulty and the danger degree of device by a wide margin, device load lower limit is unrestricted moreover, flexible operation, stability.
The device is characterized by further comprising a reformer and a medium-temperature conversion unit, wherein the reformer comprises a furnace, a burner and a reformer tube, the medium-temperature conversion unit is connected to the rear end of the reformer through a pipeline, the pressure swing adsorption decarbonization unit is connected to the front end of the medium-temperature conversion unit through a pipeline, a primary rough desulfurization outlet pipeline is arranged on the pipeline at the rear end of the pressure swing adsorption coarse desulfurization unit, a secondary rough desulfurization return reformer fuel gas pipeline and a secondary rough desulfurization outlet pipeline are arranged at the other end of the primary rough desulfurization outlet pipeline, the other end of the secondary rough desulfurization return reformer fuel gas pipeline is connected to the inlet end of the reformer, a burner pressure regulating facility III is connected to the primary desulfurization return reformer fuel gas pipeline, the other end of the secondary rough desulfurization outlet pipeline is connected to the inlet of the primary pressurizing unit, and a pressure regulating facility V is connected to the secondary rough desulfurization outlet pipeline.
When the hydrogen is produced by using the coal gas or the mixed gas of the coal gas and the natural gas, the coal gas or the mixed gas of the coal gas and the natural gas is firstly introduced into a primary pressurizing unit, a temperature swing adsorption unit and a pressure swing adsorption rough-removing unit according to a conventional method in sequence, after the treated gas is output from the pressure swing adsorption rough-removing unit, one path of the treated gas is converged into a pressure regulating facility III for pressure reduction through a primary pipeline of a rough desulfurization outlet, and then the treated gas is returned to a secondary pipeline of a reformer fuel gas through rough desulfurization and is introduced into a reformer burner fuel gas inlet end to serve as a supplementary gas source of the reformer fuel gas, so that the operation is completed; and the other path of the gas is collected into a secondary pipeline of the coarse desulfurization outlet through a primary pipeline of the coarse desulfurization outlet, is decompressed by a pressure regulating facility V and then is introduced into a raw material gas inlet end of a primary pressurizing unit to serve as a hydrogen production raw material gas source, and the operation is finished.
The utility model discloses during utilizing all the other unnecessary coal gases to introduce gas compressor raw gas pipeline, get into once more with the feed gas and utilize in the pressurization unit together to reach the purpose that will diffuse the feed gas recovery and recycle, realize reducing the cost of driving, the target of energy saving.
Further, the reactor comprises a hydrogenation reactor fine desulfurization unit, the hydrogenation reactor fine desulfurization unit comprises a hydrogenation reactor, a zinc oxide fine desulfurization tank, a start-up cooler and a start-up separator, the hydrogenation reactor fine desulfurization unit is connected between a secondary pressurization unit and a conversion furnace through a pipeline, a start-up separator outlet is provided with a start-up separator outlet primary pipeline and a start-up separator outlet secondary pipeline, the other end of the start-up separator outlet primary pipeline is connected to the inlet end of a burner, a pressure regulating facility II is connected to the start-up separator outlet primary pipeline, the other end of the start-up separator outlet secondary pipeline is connected to the inlet end of the secondary pressurization unit, and a pressure regulating facility I is connected to the start-up separator outlet secondary pipeline.
When any single gas source of coal gas and natural gas or mixed gas of the coal gas and the natural gas is used for producing hydrogen, raw material gas is firstly introduced into a primary pressurizing unit, a temperature swing adsorption unit, a pressure swing adsorption rough-removing unit, a secondary pressurizing unit and a hydrogenation reactor fine-desulfurizing unit according to a conventional method in sequence, after the treated gas is subjected to fine desulfurization, the treated gas enters a start-up separator, one path of an outlet of the start-up separator is converged into a pressure regulating facility II through a primary pipeline at an outlet end of the start-up separator for pressure reduction, and the gas after pressure reduction is introduced into a fuel gas inlet end of a burner of a reformer and serves as a supplementary gas source of fuel gas of the reformer, so that the operation is completed; and the other path of the gas is converged into a pressure regulating facility I for pressure reduction through a secondary pipeline at the outlet of the start-up separator, and the gas after pressure reduction is introduced into a raw material gas inlet end of the secondary pressurizing unit through the secondary pipeline at the outlet of the start-up separator to serve as a hydrogen production raw material gas source, so that the operation is completed.
The utility model discloses in utilizing unnecessary feed gas to introduce raw material compressor inlet line, get into secondary pressurization unit interior reuse together with the feed gas to reach the purpose that will diffuse the feed gas recovery and recycle, realize reducing and open the parking cost, the target of energy saving, especially when the hydrogen manufacturing of exclusive use natural gas, cost reduction range is great.
Further, the pressure regulating facility IV is a pressure reducing facility.
Further, the pressure regulating facility III is a pressure reducing facility; the pressure regulating facility V is a pressure reducing facility.
Further, the pressure regulating facility II is a pressure reducing facility, and the pressure regulating facility I is a pressure reducing facility.
The utility model has the advantages that:
1. the coke oven gas is used for hydrogen production, the secondary pressurizing unit is directly communicated with the pressure swing adsorption decarbonization unit, and because the converter and the medium temperature conversion system are shut down and only the gas purification and pressure swing adsorption system is put into operation, the flow is greatly simplified, the operation cost, the operation difficulty and the danger degree of the device can be greatly reduced, and the lower limit of the load of the device is not limited, and the operation is flexible and stable;
2. when the hydrogen is produced by using the coal gas or the mixed gas of the coal gas and the natural gas, the rest redundant coal gas is introduced into a raw material gas pipeline of the coal gas compressor and enters a primary pressurizing unit together with the raw material gas for reutilization, so that the aim of recycling the diffused raw material gas is fulfilled, and the aims of reducing the driving cost and saving energy are fulfilled;
3. when the hydrogen is produced by using any single gas source of the coal gas and the natural gas or the mixed gas of the coal gas and the natural gas, redundant raw material gas is introduced into an inlet pipeline of the raw material compressor and enters the secondary pressurizing unit together with the raw material gas for reuse, so that the aim of recycling the diffused raw material gas is fulfilled, the aims of reducing the starting and stopping cost and saving energy are fulfilled, and the cost is greatly reduced particularly when the natural gas is used alone for producing the hydrogen.
Drawings
Fig. 1 is a schematic view of the components and flow of the present invention.
In the figure: 1. a primary pipeline at a coarse desulfurization outlet; 2. a secondary pipeline at the outlet of the start-up separator; 3. a primary pipeline at the outlet end of the feed gas compressor of the secondary pressurizing unit; 4. a pressure regulating facility I; 5. a first-stage pipeline at the outlet end of the start-up separator; 6. a pressure regulating facility II; 7. the coarse desulfurization returns to a reformer fuel gas secondary pipeline; 8. a pressure regulating facility III; 9. a pressure regulating facility IV; 10. a coarse desulfurization outlet secondary pipeline; 11. and a pressure regulating facility V.
Detailed Description
As shown in figure 1, the utility model relates to a multi-component raw gas conversion hydrogen production device, which comprises a primary pressurizing unit, a temperature swing adsorption unit, a pressure swing adsorption coarse desorption unit, a secondary pressurizing unit, a pressure swing adsorption decarburization unit and a pressure swing adsorption purification unit, wherein the primary pressurizing unit comprises a gas compressor, the temperature swing adsorption unit comprises a temperature swing adsorption tower, the pressure swing adsorption coarse desorption unit comprises an adsorption tower and an iron system dry desulfurization tower, the secondary pressurizing unit comprises a raw gas compressor, the pressure swing adsorption decarburization unit comprises a pressure swing gas separating tank, the primary pressurizing unit is connected with the front end of the temperature swing adsorption unit through a pipeline, the temperature swing adsorption unit is connected with the front end of the pressure swing adsorption coarse desorption unit through a pipeline, the pressure swing adsorption coarse desorption unit is connected with the front end of the secondary pressurizing unit through a pipeline, the pressure swing adsorption decarburization unit is connected with the front end of the pressure swing adsorption purification unit through a pipeline, the outlet of the feed gas compressor of the secondary pressurizing unit is connected with a primary pipeline 3 at the outlet end of the feed gas compressor of the secondary pressurizing unit, the other end of the primary pipeline 3 at the outlet end of the feed gas compressor of the secondary pressurizing unit is connected with the inlet of a variable-pressure-adsorption decarbonizing unit variable-gas liquid separating tank, the variable-pressure-adsorption purifying unit is connected to the rear end of the variable-pressure-adsorption decarbonizing unit variable-gas liquid separating tank through a pipeline, and a pressure regulating facility IV 9 is connected to the primary pipeline 3 at the outlet end of the feed gas compressor of the secondary pressurizing unit.
The coke oven gas is firstly introduced into a primary pressurizing unit, a temperature swing adsorption unit, a pressure swing adsorption coarse desorption unit and a secondary pressurizing unit in sequence according to a conventional method, after the treated gas is compressed from a raw material gas compressor, the treated gas is respectively collected into a pressure regulating facility IV 9 through a primary pipeline 3 at the outlet end of the raw material gas compressor of the secondary pressurizing unit for pressure reduction, directly enters a gas separation tank at the inlet of the pressure swing adsorption decarburization unit without a fine desulfurization unit of a hydrogenation reactor, a conversion furnace and a medium temperature shift unit, and continuously enters the pressure swing adsorption decarburization unit and the pressure swing adsorption purification unit, the prepared hydrogen is guided out by a product hydrogen output device, and the operation is finished.
Compared with the prior art, the utility model discloses with the direct intercommunication of secondary pressurization unit and pressure swing adsorption decarbonization unit, because reborner and medium temperature transform system stop, only put into operation coal gas purification and pressure swing adsorption system, the flow is simplified greatly to limit, so can reduce the running cost, the operation degree of difficulty and the danger degree of device by a wide margin, device load lower limit is unrestricted moreover, flexible operation, stability.
Further, still including reborner and medium temperature transform unit, the reborner is including the stove, nozzle and reformer tube, medium temperature transform unit passes through the tube coupling at the reborner rear end, pressure swing adsorption decarbonization unit passes through the tube coupling at medium temperature transform unit front end, be equipped with coarse desulfurization export one-level pipeline 1 on the thick loose unit rear end pipeline of pressure swing adsorption, be equipped with coarse desulfurization on the coarse desulfurization export one-level pipeline 1 other end and return reborner fuel gas secondary line 7 and coarse desulfurization export secondary line 10, coarse desulfurization returns reborner fuel gas secondary line 7 other end and connects at the nozzle entry end, coarse desulfurization returns and is connected with pressure regulating facility III 8 on the reborner fuel gas secondary line 7, coarse desulfurization export secondary line 10 other end is connected at the unit import that once pressurizes, be connected with pressure regulating facility V11 on the coarse desulfurization export secondary line 10.
When the gas or the mixed gas of the gas and the natural gas is used for producing hydrogen, the gas or the mixed gas of the gas and the natural gas is firstly introduced into a primary pressurizing unit, a temperature swing adsorption unit and a pressure swing adsorption rough-removing unit in sequence according to a conventional method, after the treated gas is output from the pressure swing adsorption rough-removing unit, one path of the treated gas is converged into a pressure regulating facility III 8 for pressure reduction through a primary pipeline 1 at a rough desulfurization outlet, and then the treated gas is returned to a secondary pipeline 7 of reformer fuel gas through rough desulfurization and is introduced into a fuel gas inlet end of a reformer burner to serve as a supplementary gas source of the reformer fuel gas, so that the operation is completed; and the other path of the gas is collected into a secondary pipeline 10 of the coarse desulfurization outlet through a primary pipeline 1 of the coarse desulfurization outlet, is decompressed through a pressure regulating facility V11 and then is introduced into a raw material gas inlet end of a primary pressurizing unit to be used as a hydrogen production raw material gas source, and the operation is finished.
The utility model discloses during utilizing all the other unnecessary coal gases to introduce gas compressor raw gas pipeline, get into once more with the feed gas and utilize in the pressurization unit together to reach the purpose that will diffuse the feed gas recovery and recycle, realize reducing the cost of driving, the target of energy saving.
Further, still including hydrogenation ware fine desulphurization unit, hydrogenation ware fine desulphurization unit is including the hydrogenation ware, the zinc oxide fine desulphurization groove, start worker's cooler and start worker's separator, hydrogenation ware fine desulphurization unit passes through the tube coupling between secondary pressurization unit and reborner, the separator export of starting worker is equipped with start worker's separator exit end one-level pipeline 5 and start worker's separator export second grade pipeline 2, the 5 other ends of start worker's separator exit end one-level pipeline are connected at the nozzle entry end, be connected with pressure regulating facility II 6 on the separator exit end one-level pipeline 5 of starting worker, start worker's separator export second grade pipeline 2 other ends are connected at secondary pressurization unit entry end, be connected with pressure regulating facility I4 on the separator export second grade pipeline 2 of starting worker.
When the hydrogen is produced by using any single gas source of coal gas and natural gas or the mixed gas of the coal gas and the natural gas, the raw material gas is firstly introduced into a primary pressurizing unit, a temperature swing adsorption unit, a pressure swing adsorption rough-removing unit, a secondary pressurizing unit and a hydrogenation reactor fine-desulfurizing unit according to a conventional method in sequence, after the fine desulfurization of the treated gas is finished, the treated gas enters a start-up separator, one path of an outlet of the start-up separator is converged into a pressure regulating facility II 6 through a primary pipeline 5 at an outlet end of the start-up separator for pressure reduction, the gas after the pressure reduction is finished is introduced into a fuel gas inlet end of a reformer and serves as a supplementary gas source of the fuel gas of the reformer, and the operation is finished; and the other path of the gas is collected into a pressure regulating facility I4 for pressure reduction through a secondary pipeline 2 at the outlet of the start-up separator, and the gas after pressure reduction is introduced into a raw material gas inlet end of a secondary pressurizing unit through the secondary pipeline 2 at the outlet of the start-up separator to be used as a hydrogen production raw material gas source, so that the operation is completed.
The utility model discloses in utilizing unnecessary feed gas to introduce raw material compressor inlet line, get into secondary pressurization unit interior reuse together with the feed gas to reach the purpose that will diffuse the feed gas recovery and recycle, realize reducing and open the parking cost, the target of energy saving, especially when the hydrogen manufacturing of exclusive use natural gas, cost reduction range is great.
Further, the pressure regulating facility IV 9 is a pressure reducing facility.
Further, the pressure regulating facility III 8 is a pressure reducing facility; the pressure regulating facility V11 is a pressure reducing facility.
Further, the pressure regulating facility II 6 is a pressure reducing facility, and the pressure regulating facility I4 is a pressure reducing facility.
Claims (6)
1. A multi-component raw gas conversion hydrogen production device is characterized in that: the device comprises a primary pressurizing unit, a temperature swing adsorption unit, a pressure swing adsorption coarse-removing unit, a secondary pressurizing unit, a pressure swing adsorption decarburization unit and a pressure swing adsorption purification unit, wherein the primary pressurizing unit comprises a gas compressor, the temperature swing adsorption unit comprises a temperature swing adsorption tower, the pressure swing adsorption coarse-removing unit comprises an adsorption tower and an iron system dry desulfurization tower, the secondary pressurizing unit comprises a raw material gas compressor, a pressure swing adsorption decarburization unit comprises a variable gas separating tank, the primary pressurizing unit is connected with the front end of the temperature swing adsorption unit through a pipeline, the temperature swing adsorption unit is connected with the front end of the pressure swing adsorption coarse-removing unit through a pipeline, the pressure swing adsorption coarse-removing unit is connected with the front end of the secondary pressurizing unit through a pipeline, the pressure swing adsorption decarburization unit is connected with the front end of the pressure swing adsorption purification unit through a pipeline, the outlet of the raw material gas compressor of the secondary pressurizing unit is connected with a primary pipeline (3) at the outlet end of the raw material gas compressor of the secondary pressurizing unit, the other end of a primary pipeline (3) at the outlet end of the feed gas compressor of the secondary pressurizing unit is connected to the inlet of a variable-pressure adsorption decarburization unit variable-gas liquid separating tank, a variable-pressure adsorption purification unit is connected to the rear end of the variable-pressure adsorption decarburization unit variable-gas liquid separating tank through a pipeline, and a pressure regulating facility IV (9) is connected to the primary pipeline (3) at the outlet end of the feed gas compressor of the secondary pressurizing unit.
2. The apparatus for converting multicomponent raw gas into hydrogen production according to claim 1, wherein: also comprises a reformer and a medium temperature conversion unit, the reformer comprises a furnace, nozzle and reformer tube, the medium temperature transform unit passes through the tube coupling at the reformer rear end, pressure swing adsorption decarbonization unit passes through the tube coupling and is in medium temperature transform unit front end, be equipped with coarse desulfurization export one-level pipeline (1) on the thick off-line of pressure swing adsorption unit rear end pipeline, be equipped with on the thick desulfurization export one-level pipeline (1) other end that coarse desulfurization returns reformer fuel gas second grade pipeline (7) and coarse desulfurization export second grade pipeline (10), coarse desulfurization returns reformer fuel gas second grade pipeline (7) other end and connects at the nozzle entry end, coarse desulfurization returns and is connected with pressure regulating facility III (8) on reformer fuel gas second grade pipeline (7), coarse desulfurization export second grade pipeline (10) other end is connected at the unit import that once pressurizes, be connected with pressure regulating facility V (11) on coarse desulfurization export second grade pipeline (10).
3. The apparatus for converting multicomponent raw gas into hydrogen production according to claim 2, characterized in that: still including hydrogenation ware fine desulphurization unit, hydrogenation ware fine desulphurization unit is including the hydrogenation ware, zinc oxide fine desulphurization groove, the cooler of starting to work and the separator of starting to work, hydrogenation ware fine desulphurization unit passes through the tube coupling between secondary pressurization unit and reborner, the separator export of starting to work is equipped with separator export one-level pipeline of starting to work (5) and separator export second grade pipeline of starting to work (2), the separator export one-level pipeline of starting to work (5) other end is connected at the nozzle entry end, be connected with pressure regulating facility II (6) on separator export one-level pipeline of starting to work (5), separator export second grade pipeline of starting to work (2) other end is connected at secondary pressurization unit entry end, be connected with pressure regulating facility I (4) on separator export second grade pipeline of starting to work (2).
4. The apparatus for converting multicomponent raw gas into hydrogen production according to claim 1, wherein: and the pressure regulating facility IV (9) is a pressure reducing facility.
5. The apparatus for converting multicomponent raw gas into hydrogen production according to claim 2, characterized in that: the pressure regulating facility III (8) is a pressure reducing facility; the pressure regulating facility V (11) is a pressure reducing facility.
6. The apparatus for converting multicomponent raw gas into hydrogen production according to claim 3, wherein: the pressure regulating facility II (6) is a pressure reducing facility, and the pressure regulating facility I (4) is a pressure reducing facility.
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| CN113998672A (en) * | 2021-11-03 | 2022-02-01 | 上海浦江特种气体有限公司 | Hydrogen production device and method for urban wet garbage |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113998672A (en) * | 2021-11-03 | 2022-02-01 | 上海浦江特种气体有限公司 | Hydrogen production device and method for urban wet garbage |
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