CN115888313A - Productivity adjusting process for producing fuel cell hydrogen and pipeline natural gas by coke oven gas - Google Patents
Productivity adjusting process for producing fuel cell hydrogen and pipeline natural gas by coke oven gas Download PDFInfo
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- 238000001179 sorption measurement Methods 0.000 claims abstract description 126
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- 238000011069 regeneration method Methods 0.000 claims abstract description 47
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- 230000006835 compression Effects 0.000 claims abstract description 39
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 56
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- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 2
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Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/50—Fuel cells
Abstract
The invention discloses a capacity adjusting process for preparing fuel cell hydrogen and pipeline natural gas from coke oven gas, which comprises a temperature swing adsorption unit (X3) connected from a compression and pretreatment unit (X1) or a conversion unit (X2) to remove heavy component impurities in the coke oven gas, a fine desulfurization unit (X4) connected from the temperature swing adsorption unit (X3) to remove inorganic sulfur and organic sulfur in the coke oven gas, and the like. The invention relates to a method for preparing natural gas by methanation synthesis, which comprises the steps of compressing and pretreating coke oven gas, performing bypass transformation, temperature swing adsorption and fine desulfurization on the coke oven gas, removing one part of the coke oven gas, performing pressure swing adsorption separation to obtain fuel hydrogen for proton exchange membrane fuel cell automobiles, mixing the other part of the coke oven gas with pressurized pressure swing adsorption desorption gas, performing methanation synthesis to obtain pipeline natural gas, and fully utilizing effective components of hydrogen and carbon in the coke oven gas by arranging a transformation bypass pipeline, changing a source of temperature swing adsorption regeneration gas and adjusting the flow rate of demethanization desorption gas to realize the flexible adjustment of the hydrogen and pipeline natural gas productivity of the fuel cells.
Description
Technical Field
The invention belongs to the technical field of new energy preparation, and particularly relates to a process for adjusting the capacity of hydrogen gas of a fuel cell and pipeline natural gas prepared from coke oven gas.
Background
In recent years, with the increasing attention on environmental protection in the world, energy systems mainly based on fossil fuels are gradually changed into diversified structures such as fossil fuels, renewable energy sources, nuclear energy and the like, and the energy structure in the world is developed toward lower carbon content. The hydrogen contains no carbon and is a clean energy source. The hydrogen fuel cell industry is one of the current new energy development directions, and is gradually accepted by the market due to the advantages of environmental protection, good low-temperature performance, long endurance, short filling time and the like.
Data show that the device for producing hydrogen by using fossil energy such as coal, natural gas, petroleum and the like as raw materials in China exceeds 70 percent, the carbon emission of hydrogen production by using the industrial raw materials is high, and the hydrogen production cost is 10-20 yuan/kg; the cost of large-scale hydrogen production is only 8-14 yuan/kg. Therefore, the hydrogen production by utilizing the industrial byproduct gas has great advantages in energy saving, carbon reduction and economic benefit.
The coke oven gas is a gas which is a byproduct generated in the coke production process by using coal as a raw material and contains effective components such as hydrogen, carbon monoxide, carbon dioxide and the like and impurities such as benzene, ammonia, sulfur and the like. The coke oven gas mainly comprises 55-60 percent of hydrogen and 23-27 percent of methane, and also comprises a small amount of carbon monoxide (5-8 percent) and C 2 And the unsaturated hydrocarbon (2 percent), carbon dioxide (1.5 to 3 percent), oxygen (0.3 to 0.8 percent) and nitrogen (3 to 7 percent). The coke oven gas is a high-quality hydrogen production raw material gas, wherein carbon monoxide and carbon dioxide can be converted into methane through hydrogenation, and a natural gas product is obtained through separation. Therefore, the coke oven gas is used for preparing the hydrogen of the fuel cell, and the pipeline natural gas is obtained by separation, so that the effective components in the coke oven gas can be utilized to the maximum extent.
Another problem with coke oven gas to fuel cell hydrogen is uncertainty in market demand. At present, the hydrogen industry of the fuel cell can be highly gathered, the scale of application and popularization is increased, and the supply cost is low in the cooperative development of the existing cities. The fuel cell hydrogen prepared in industrially developed areas has certain development advantages, and simultaneously faces the embarrassing situation that the number of hydrogen fuel cell vehicles is small, so that the hydrogen energy cannot be fully consumed, and the hydrogen capacity of the fuel cell needs to be reduced.
Disclosure of Invention
The invention provides a process for adjusting the productivity of hydrogen gas for fuel cells and pipeline natural gas prepared from coke oven gas, aiming at the defects of the prior art. In the device, by arranging the conversion bypass pipeline, changing the source of the temperature swing adsorption regenerated gas and adjusting the flow rate of the demethanization desorption gas, the effective components of hydrogen and carbon in the coke oven gas are fully utilized, and when the hydrogen demand of the fuel cell is insufficient, the natural gas capacity of the pipeline is improved, and the economic benefit is ensured.
In order to achieve the above purpose, the specific technical scheme of the invention is as follows:
the production capacity regulating process for producing fuel cell hydrogen and pipeline natural gas with coke oven gas includes the following steps:
the compression and pretreatment unit is connected with or not connected with the conversion unit and then enters the temperature swing adsorption unit; the device comprises a temperature swing adsorption unit, a fine desulfurization unit, a pressure swing adsorption unit, a desorption gas compression unit and a methanation and drying unit, wherein the temperature swing adsorption unit is connected from the compression and pretreatment unit or the transformation unit to remove heavy component impurities in the coke oven gas, the fine desulfurization unit is connected from the temperature swing adsorption unit to remove inorganic sulfur and organic sulfur in the coke oven gas, the pressure swing adsorption unit is connected from the fine desulfurization unit to prepare hydrogen of a fuel cell, the desorption gas compression unit is connected from the pressure swing adsorption unit to pressurize desorption gas, and the methanation and drying unit is connected from the desorption gas compression unit to convert carbon monoxide and carbon dioxide into methane after being mixed with gas in a fine purified gas conveying pipe. The coke oven gas conveying pipe is connected with the compression and pretreatment unit, the third desorption gas conveying pipe is connected with a fuel gas outer conveying pipe, the pressure swing adsorption unit is connected with a fuel cell hydrogen outer conveying pipe, and the methanation and drying unit is connected with a pipeline natural gas outer conveying pipe.
Further, whether a conversion unit is arranged between the compression and pretreatment unit and the temperature swing adsorption unit is selected according to the situation; when the conversion unit is arranged, the air inlet and the air outlet of the conversion unit are both connected with a pre-purified gas bypass pipe, and the conversion unit converts carbon monoxide into hydrogen and carbon dioxide.
Furthermore, a pre-purification gas conveying pipe is connected between the compression unit and the temperature swing adsorption unit, the starting point of the first pre-purification gas bypass pipe is connected to the airflow starting end of the pre-purification gas conveying pipe, and the terminal point of the second pre-purification gas bypass pipe is connected to the airflow tail end of the pre-purification conveying pipe.
Preferably, along the air flow direction, air inlet valves are arranged on the pre-purified air delivery pipe behind the three-way connection and at the beginning of the first pre-purified air bypass pipe. When the hydrogen capacity of the fuel cell is pursued to be larger, the air inlet valve of the pre-purified gas conveying pipe is closed, and the air inlet valve of the first pre-purified gas bypass pipe is opened; and conversely, closing the air inlet valve of the first pre-purified gas bypass pipe and opening the air inlet valve of the pre-purified gas conveying pipe.
Further, a purified gas conveying pipe is connected between the temperature swing adsorption unit and the fine desulfurization unit, the temperature swing adsorption unit is provided with a regenerated gas conveying pipe and a regenerated gas output pipe, and the regenerated gas output pipe is connected to a fuel gas external conveying pipe.
Preferably, a self-purification gas conveying pipe is led out of the purification gas conveying pipe and connected to the regeneration gas conveying pipe, and whether the self-purification gas is used as the temperature swing adsorption regeneration gas or not is selected according to the capacity regulation requirement.
Furthermore, the fine desulfurization unit is connected with a fine purification gas conveying pipe, a first fine purification gas conveying pipe of the pressure swing adsorption unit and a second fine purification gas conveying pipe of the demethanization and drying unit are connected to the fine purification gas conveying pipe, and the air quantity of the second desorption gas conveying pipe, the first fine purification gas conveying pipe and the second fine purification gas conveying pipe is adjusted according to the capacity adjusting requirement.
Preferably, the purified gas in the fine desulfurization unit is sequentially subjected to prehydrogenation, primary hydrogenation, primary adsorption desulfurization, secondary hydrogenation, secondary adsorption desulfurization and copper-based fine desulfurization, so that the total sulfur in the fine purified gas after the fine desulfurization unit is not more than 0.02ppmv.
Furthermore, the pressure swing adsorption unit is connected with a hydrogen gas output pipe of the fuel cell and a first desorption gas delivery pipe.
Preferably, a hydrogen regeneration delivery pipe is led out from the fuel cell hydrogen gas delivery pipe, the hydrogen regeneration delivery pipe is connected to the regeneration gas delivery pipe and led out from the hydrogen fuel delivery pipe, the hydrogen fuel delivery pipe is connected to the fuel gas delivery pipe, and the fuel cell hydrogen is selected as the product gas or the fuel gas or the temperature swing adsorption regeneration gas according to the requirements of capacity regulation and hydrogen product filling.
Preferably, a second desorption gas conveying pipe and a third desorption gas conveying pipe are led out from the first desorption gas conveying pipe, the second desorption gas conveying pipe is connected to the desorption gas compression unit, a fuel gas outer conveying pipe and a regeneration desorption gas conveying pipe are led out from the third desorption gas conveying pipe, the regeneration desorption gas conveying pipe is connected to the regeneration gas conveying pipe, the desorption gas flow of the desorption gas compression unit in the second desorption gas conveying pipe is adjusted according to the capacity adjustment requirement, and meanwhile, desorption gas is selected as fuel gas or temperature swing adsorption regeneration gas.
Furthermore, the desorption gas compression unit is connected with a desorption gas conveying pipe, the desorption gas conveying pipe and the second fine purification gas conveying pipe are connected to a third fine purification gas conveying pipe, and the third fine purification gas conveying pipe is connected to the methanation and drying unit.
Preferably, the desorption gas compressor unit outlet pressure or the methanation unit operating pressure is determined according to the required pressure of the pipeline natural gas output pipeline.
Preferably, the third purified gas conveying pipe is provided with analysis point locations of the contents of hydrogen, carbon monoxide, carbon dioxide and low-carbon hydrocarbon, and the hydrogen-carbon ratio of the gas in the third purified gas conveying pipe is obtained according to the analysis result.
Preferably, the hydrogen-carbon ratio of the gas in the third purified gas delivery pipe is 3.0 to 3.3.
The invention relates to a method for preparing natural gas by methanation synthesis, which comprises the steps of compressing and pretreating coke oven gas, performing bypass transformation, temperature swing adsorption and fine desulfurization on the coke oven gas, removing one part of the coke oven gas, performing pressure swing adsorption separation to obtain fuel hydrogen for proton exchange membrane fuel cell automobiles, mixing the other part of the coke oven gas with pressurized pressure swing adsorption desorption gas, performing methanation synthesis to obtain pipeline natural gas, and fully utilizing effective components of hydrogen and carbon in the coke oven gas by arranging a transformation bypass pipeline, changing a source of temperature swing adsorption regeneration gas and adjusting the flow rate of demethanization desorption gas to realize the flexible adjustment of the hydrogen and pipeline natural gas productivity of the fuel cells.
Compared with the prior art, the invention has the positive effects that:
the method comprises the steps that a temperature swing adsorption unit is arranged to adsorb heavy component impurities of coke oven gas, and copper-based fine desulfurization is connected in series after hydrodesulfurization to ensure that the total sulfur of the purified coke oven gas is not more than 0.02ppmv, which is the key for successfully preparing the fuel cell hydrogen (the total sulfur of the fuel cell hydrogen is not more than 0.004 ppmv); the adoption of multiple temperature swing adsorption regeneration gas sources is the key for adjusting the productivity of the fuel cell hydrogen and the pipeline natural gas.
And (II) a transformation bypass pipeline is arranged in the invention. When the hydrogen market demand of the fuel cell is small, the hydrogen does not pass through a conversion unit; and otherwise, the hydrogen enters the bypass conversion unit to obtain more hydrogen products of the fuel cell.
The regenerated gas of temperature swing adsorption of the invention is derived from self-purified gas, fuel cell hydrogen and pressure swing adsorption desorption gas, and can realize flexible adjustment of productivity. When the hydrogen market demand of the fuel cell is particularly small or the hydrogen product of the fuel cell is not filled, the hydrogen of the fuel cell is used as the temperature swing adsorption regeneration gas, and only the pipeline natural gas product is produced at the moment; when the demands of the fuel cell hydrogen market and the pipeline natural gas market are both small, the self-purification gas is adopted as the temperature swing adsorption regeneration gas, at the moment, the pipeline natural gas has high capacity, and the fuel cell hydrogen has low capacity; when the markets of the fuel cell hydrogen and the pipeline natural gas are good, the pressure swing adsorption desorption gas is used as the temperature swing adsorption regeneration gas, and the pipeline natural gas and the fuel cell hydrogen can reach high productivity.
Drawings
FIG. 1 is a block diagram of a process flow described in example 1 of the present invention.
FIG. 2 is a block diagram of the process flow described in example 2 of the present invention.
FIG. 3 is a block diagram of the process flow of example 3 of the present invention.
FIG. 4 is a block diagram of the process flow described in example 4 of the present invention.
Wherein, the names corresponding to the reference numbers are:
1-coke oven gas conveying pipe, 2-pre-purified gas conveying pipe, 3-first pre-purified gas by-pass pipe, 4-second pre-purified gas by-pass pipe, 5-purified gas conveying pipe, 6-self-purified gas conveying pipe, 7-purified gas conveying pipe, 8-first purified gas conveying pipe, 9-second purified gas conveying pipe, 10-fuel cell hydrogen gas external conveying pipe, 11-hydrogen regeneration conveying pipe, 12-first desorbed gas conveying pipe, 13-second desorbed gas conveying pipe, 14-third desorbed gas conveying pipe, 15-desorbed gas conveying pipe, 16-third purified gas conveying pipe, 17-pipeline natural gas external conveying pipe, 18-hydrogen fuel conveying pipe, 19-regenerated desorbed gas conveying pipe, 20-fuel gas external conveying pipe, 21-regenerated gas conveying pipe, X1-compression, pretreatment unit, X2-conversion unit, X3-temperature-changing adsorption unit, X4-fine desulfurization unit, X5-pressure changing adsorption unit, X6-desorbed gas compression unit, X7-methanation and drying unit.
Detailed Description
The device comprises a temperature swing adsorption unit X3 which is connected from a compression and pretreatment unit X1 or a conversion unit X2 (an air inlet and an air outlet of the conversion unit X2 are respectively connected with a first pre-purified gas bypass pipe 3 and a second pre-purified gas bypass pipe 4, the conversion unit X2 can convert carbon monoxide into hydrogen and carbon dioxide, whether the conversion unit X2 is arranged between the compression and pretreatment unit X1 and the temperature swing adsorption unit X3 is determined according to the situation or not) to remove heavy component impurities in coke oven gas, a fine desulfurization unit X4 which is connected from the temperature swing adsorption unit X3 to remove inorganic sulfur and organic sulfur in the coke oven gas, a pressure swing adsorption unit X5 which is connected from the fine desulfurization unit X4 to prepare hydrogen of a fuel cell, a desorption gas compression unit X6 which is connected from the pressure swing adsorption unit X5 to pressurize the coke oven gas, and a desorption gas delivery pipe 9 which is connected from the desorption compression unit X6 and is mixed with purified gas and then connected to a methanation and drying unit X7 to convert carbon monoxide and carbon dioxide into methane. The coke oven gas conveying pipe 1 is connected to a compression and pretreatment unit X1, a fuel gas external conveying pipe 20 is connected to a third desorption gas conveying pipe 14, a pressure swing adsorption unit X5 is connected to a fuel cell hydrogen external conveying pipe 10, and a methanation and drying unit X7 is connected to a pipeline natural gas external conveying pipe 17. A pre-purification gas conveying pipe 2 is connected between the compression and pretreatment unit X1 and the temperature swing adsorption unit X3, the starting point of a first pre-purification gas bypass pipe 3 is connected to the airflow starting end of the pre-purification gas conveying pipe 2, and the terminal point of a second pre-purification gas bypass pipe 4 is connected to the airflow tail end of the pre-purification conveying pipe 2. Preferably, along the air flow direction, the inlet valves are arranged on the back pre-purified air delivery pipe 2 of the three-way connection and the beginning of the first pre-purified air bypass pipe 3. When the hydrogen capacity of the fuel cell is pursued to be larger, the air inlet valve of the pre-purified gas delivery pipe 2 is closed, and the air inlet valve of the first pre-purified gas bypass pipe 3 is opened; on the contrary, the first pre-purified gas bypass pipe 3 intake valve is closed, and the pre-purified gas delivery pipe 2 intake valve is opened. A purified gas conveying pipe 5 is connected between the temperature swing adsorption unit X3 and the fine desulfurization unit X4, the temperature swing adsorption unit X3 is provided with a regenerated gas conveying pipe 21 and a regenerated gas output pipe 22, and the regenerated gas output pipe 22 is connected to a fuel gas external conveying pipe 20. A self-purification gas delivery pipe 6 is led out from the purification gas delivery pipe 5, the self-purification gas delivery pipe 6 is connected to a regeneration gas delivery pipe 21, and whether the self-purification gas is used as temperature swing adsorption regeneration gas or not is selected according to the capacity regulation requirement. The fine desulfurization unit X4 connects out fine purification gas conveyer pipe 7, is connected with the first fine purification gas conveyer pipe 8 that goes pressure swing adsorption unit X5 and the second fine purification gas conveyer pipe 9 that removes alkylation, drying unit X7 on the fine purification gas conveyer pipe 7, adjusts the tolerance of second desorption gas conveyer pipe 13, first fine purification gas conveyer pipe 8 and second fine purification gas conveyer pipe 9 according to the productivity regulation needs. Preferably, the purified gas in the fine desulfurization unit X4 is sequentially subjected to pre-hydrogenation, first-stage adsorption desulfurization, second-stage hydrogenation, second-stage adsorption desulfurization and copper-based fine desulfurization, so that the total sulfur in the fine purified gas after the fine desulfurization unit X4 is not more than 0.02ppmv.
The invention relates to a fuel cell hydrogen gas external transmission pipe 10, wherein a hydrogen regeneration transmission pipe 11 is led out from the fuel cell hydrogen gas external transmission pipe 10, the hydrogen regeneration transmission pipe 11 is connected to a regeneration gas transmission pipe 21 and led out from a hydrogen fuel transmission pipe 18, the hydrogen fuel transmission pipe 18 is connected to a fuel gas external transmission pipe 20, and the fuel cell hydrogen gas is selected as a product gas or a fuel gas or a temperature swing adsorption regeneration gas according to the requirements of capacity adjustment and hydrogen product filling. Preferably, a second desorption gas conveying pipe 13 and a third desorption gas conveying pipe 14 are led out from the first desorption gas conveying pipe 12, the second desorption gas conveying pipe 13 is connected to a desorption gas compression unit X6, a fuel gas external conveying pipe 20 and a regeneration desorption gas conveying pipe 19 are led out from the third desorption gas conveying pipe 14, the regeneration desorption gas conveying pipe 19 is connected to a regeneration gas conveying pipe 21, the desorption gas flow rate of the desorption gas compression unit X6 in the second desorption gas conveying pipe 13 is adjusted according to the capacity adjustment requirement, and simultaneously, the desorption gas is selected as fuel gas or temperature swing adsorption regeneration gas.
A desorption gas conveying pipe 15 is connected to a desorption gas compression unit X6, the desorption gas conveying pipe 15 and a second fine purification gas conveying pipe 9 are connected to a third fine purification gas conveying pipe 16, and the third fine purification gas conveying pipe 16 is connected to a methanation and drying unit X7. Preferably, the desorption gas compressor unit X6 outlet pressure or the methanation unit X7 operating pressure is determined according to the required pressure of the pipeline natural gas export line 17. Preferably, the third purified gas delivery pipe 16 is provided with analysis points for the contents of hydrogen, carbon monoxide, carbon dioxide and low-carbon hydrocarbons, and the hydrogen-carbon ratio of the gas in the third purified gas delivery pipe 16 is obtained according to the analysis result. Preferably, the hydrogen-carbon ratio of the gas in the third purified gas delivery pipe 16 is 3.0 to 3.3.
The process method provided by the invention is used for regulating the productivity of fuel cell hydrogen and pipeline natural gas prepared from coke oven gas, the temperature swing adsorption unit is arranged for adsorbing heavy component impurities of the coke oven gas, the total sulfur of the purified coke oven gas is not more than 0.02ppmv by series copper-based fine desulfurization after hydrodesulfurization, and a plurality of temperature swing adsorption regenerated gas sources are adopted, which is the key for successfully preparing the fuel cell hydrogen and regulating the productivity of the fuel cell hydrogen and the pipeline natural gas.
The invention is provided with a conversion bypass pipeline. When the hydrogen market demand of the fuel cell is small, the hydrogen does not pass through a conversion unit; and on the contrary, the hydrogen enters the bypass conversion unit to obtain more hydrogen products of the fuel cell.
The regenerated gas of temperature swing adsorption of the invention is derived from self-purified gas, fuel cell hydrogen and pressure swing adsorption desorption gas, and can realize flexible adjustment of productivity. When the hydrogen market demand of the fuel cell is particularly small or the hydrogen product of the fuel cell is not filled, the hydrogen of the fuel cell is used as the temperature swing adsorption regeneration gas, and only the pipeline natural gas product is produced at the moment; when the demands of the fuel cell hydrogen market and the pipeline natural gas market are both small, the self-purification gas is adopted as the temperature swing adsorption regeneration gas, at the moment, the pipeline natural gas has high capacity, and the fuel cell hydrogen has low capacity; when the market demand of the fuel cell hydrogen is larger, the pressure swing adsorption desorption gas is adopted as the temperature swing adsorption regeneration gas, and the pipeline natural gas and the fuel cell hydrogen can achieve high productivity.
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is further described in detail below with reference to the accompanying drawings. It is to be understood that the described embodiments are merely exemplary of the invention, and not restrictive of the full scope of the invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplification of description, but do not indicate or imply that the device or element referred to must have a particular orientation or be constructed and operated in a particular orientation, and thus, they should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly and may be, for example, fixedly connected, detachably connected, or integrally connected; of course, mechanical connection and electrical connection are also possible; in addition, they may be directly connected, indirectly connected through an intermediary, or may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood according to specific situations by those of ordinary skill in the art.
As shown in the attached drawing of the abstract, the capacity adjusting process for preparing the fuel cell hydrogen from the coke oven gas and the pipeline natural gas makes full use of the effective components of hydrogen and carbon in the coke oven gas by arranging the conversion bypass pipeline, changing the source of the temperature swing adsorption regenerated gas and adjusting the flow rate of the demethanization desorption gas, improves the capacity of the pipeline natural gas when the hydrogen demand of the fuel cell is insufficient, and ensures the economic benefit.
Example 1:
the fuel cell hydrogen of the embodiment has no market, the fuel cell hydrogen is not filled, and the fuel cell hydrogen is used as the temperature swing adsorption regeneration gas, as shown in figure 1.
The coke oven gas after compression and pretreatment has the temperature of 40 ℃, the pressure of 1.6MPaG and the flow rate of 20029Nm 3 The molar composition of the catalyst is 60.69 percent of hydrogen, 10.46 percent of carbon monoxide, 2.82 percent of carbon dioxide, 19.40 percent of methane, 0.94 percent of ethylene, 0.94 percent of ethane, 3.86 percent of nitrogen, 0.42 percent of water and 0.46 percent of oxygen. Wherein each standard coke oven gas contains 6mg of tar and naphthalene, 20mg of hydrogen sulfide, 200mg of organic sulfur, 44mg of ammonia and 1200mg of benzene. The coke oven gas after pre-purification firstly enters a temperature swing adsorption unit X3 to remove tar and naphthalene to be not more than 1mg/Nm 3 And simultaneously removing heavy component impurities in the coke oven gas. And the regenerated gas of the temperature swing adsorption unit X3 is all fuel cell hydrogen prepared by the subsequent pressure swing adsorption unit X5 and is sent to a fuel pipe network after being regenerated.
And the purified coke oven gas from the temperature swing adsorption unit X3 enters a fine desulfurization unit X4, and is sequentially subjected to pre-hydrogenation, primary adsorption desulfurization, secondary hydrogenation and secondary adsorption desulfurization, after the total sulfur in the coke oven gas is removed to be not more than 0.1ppmv, the coke oven gas is subjected to copper-based fine desulfurization to remove the total sulfur in the coke oven gas to be not more than 0.02ppmv, and the purification requirement of hydrogen for preparing a fuel cell by pressure swing adsorption is met.
The fuel cell of example 1 has no market for hydrogen, but still requires a portion of coke oven gas to remove excess hydrogen, depending on the hydrogen to carbon ratio requirements of the methanated pipeline natural gas.
The gas flow of the refined coke oven gas from the refined desulphurization unit X4 is 19717Nm 3 And h, dividing the mixture into two parts, namely a pressure swing adsorption unit X5 and a methanation and drying unit X7. According to the requirement of the subsequent methanation on the hydrogen-carbon ratio, the refined coke oven gas 14717Nm of the demethanization and drying unit X7 3 Perh, the coke oven gas is purified by 4955Nm after entering a pressure swing adsorption unit X5 for cooling and water distribution 3 H is the ratio of the total weight of the catalyst to the total weight of the catalyst. 2300Nm obtained by pressure swing adsorption unit X5 3 Hydrogen for fuel cell, having a molar purity of not less than 99.97%, total hydrocarbons (calculated as methane) of not more than 2ppmv, carbon monoxide of not more than 0.2ppmvTotal sulfur is not more than 0.004ppmv, formaldehyde is not more than 0.01ppmv, and total halogen compounds (calculated by halogen ions) are not more than 0.05ppmv, and all the components are used as regeneration gas for temperature swing adsorption of X3. The required pressure of the natural gas in the pipeline of the embodiment is 0.7MPaG, and the desorbed gas of the pressure swing adsorption unit X5 is 2655Nm 3 The mol composition of hydrogen is 25.88 percent, carbon monoxide is 20.02 percent, carbon dioxide is 5.39 percent, methane is 37.12 percent, ethane is 3.59 percent, nitrogen is 7.39 percent and water is 0.6 percent, the mixture is pressurized to 1.2MPaG through a desorption gas compression unit X6 and then is mixed with refined coke oven gas 14717Nm 3 The molar composition of the mixed gas/h is 54.57% of hydrogen, 12.07% of carbon monoxide, 3.25% of carbon dioxide, 22.37% of methane, 2.16% of ethane, 4.46% of nitrogen, 1.12% of water and 3.21% of hydrogen-carbon ratio, and the condition of preparing the pipeline natural gas through methanation is met.
8632Nm of natural gas in a pipeline from the methanation and drying unit X7 3 H, the molar composition of the catalyst is 6.49 percent of hydrogen, 84.54 percent of methane and 8.97 percent of nitrogen, and the high calorific value is 32.09MJ/m 3 And meets the requirements of the second class of natural gas in GB17820-2018 Natural gas.
Example 2
The fuel cell hydrogen market of this example is small, and the pipeline natural gas market is also common, and self-purified gas is used as the temperature swing adsorption regeneration gas, as shown in fig. 2.
The coke oven gas after compression and pretreatment has the temperature of 40 ℃, the pressure of 1.6MPaG and the flow rate of 20029Nm 3 The molar composition of the catalyst is 60.69 percent of hydrogen, 10.46 percent of carbon monoxide, 2.82 percent of carbon dioxide, 19.40 percent of methane, 0.94 percent of ethylene, 0.94 percent of ethane, 3.86 percent of nitrogen, 0.42 percent of water and 0.46 percent of oxygen. Wherein each standard coke oven gas contains 6mg of tar and naphthalene, 20mg of hydrogen sulfide, 200mg of organic sulfur, 44mg of ammonia and 1200mg of benzene. The coke oven gas after pre-purification firstly enters a temperature swing adsorption unit X3 to remove tar and naphthalene to be not more than 1mg/Nm 3 And simultaneously removing heavy component impurities in the coke oven gas. The regenerated gas of the temperature swing adsorption unit X3 adopts the purified coke oven gas with the gas quantity of 2000Nm after the temperature swing adsorption unit X3 3 And h, delivering the regenerated mixture to a fuel pipe network.
And (3) allowing the purified coke oven gas from the temperature swing adsorption unit X3 to enter a fine desulfurization unit X4, sequentially carrying out pre-hydrogenation, primary adsorption desulfurization, secondary hydrogenation and secondary adsorption desulfurization, removing the total sulfur in the coke oven gas to be not more than 0.1ppmv, and then allowing the coke oven gas to enter copper-based fine desulfurization to remove the total sulfur in the coke oven gas to be not more than 0.02ppmv, so that the purification requirement of hydrogen gas for fuel cell preparation by pressure swing adsorption is met.
The gas quantity of the refined coke oven gas discharged from the refined desulphurization unit X4 is 17745Nm 3 And h, dividing the mixture into two parts, namely a pressure swing adsorption unit X5 and a methanation and drying unit X7. The fuel cell of this example 2 has a very small hydrogen market, designed at 2000Nm 3 The filling amount per hour, and simultaneously considering the requirement of the subsequent methanation on the hydrogen-carbon ratio, the refined and purified coke oven gas 13397Nm of the demethanization and drying unit X7 3 Perh, the coke oven gas is subjected to fine purification 4309Nm after being cooled and water-separated in a pressure swing adsorption unit X5 3 H is used as the reference value. 2026Nm obtained by pressure swing adsorption Unit X5 3 Hydrogen of fuel cell, the molar purity of hydrogen is not less than 99.97%, total hydrocarbon (calculated by methane) is not more than 2ppmv, carbon monoxide is not more than 0.2ppmv, total sulfur is not more than 0.004ppmv, formaldehyde is not more than 0.01ppmv, total halogen compound (calculated by halogen ion) is not more than 0.05ppmv, and the hydrogen is charged for sale, and when the hydrogen is not charged, the hydrogen is sent to fuel pipe network. The pipeline natural gas of the embodiment requires 0.5MPaG of pressure and 2283Nm of desorbed gas of X5 pressure swing adsorption unit 3 The mol composition of the hydrogen gas is 25.04 percent, the carbon monoxide is 20.25 percent, the carbon dioxide is 5.45 percent, the methane is 37.54 percent, the ethane is 3.63 percent, the nitrogen gas is 7.48 percent and the water is 0.61 percent, the pressure is increased to 1.0MPaG through a desorption gas compression unit X6, and then the hydrogen gas and the refined purified coke oven gas are 13397Nm 3 The mol composition after mixing/h is 54.70 percent of hydrogen, 12.03 percent of carbon monoxide, 3.24 percent of carbon dioxide, 22.31 percent of methane, 2.16 percent of ethane, 4.44 percent of nitrogen, 1.13 percent of water and 3.23 percent of hydrogen-carbon ratio, thereby meeting the condition of preparing the pipeline natural gas through methanation.
7813Nm pipeline natural gas from methanation and drying unit X7 3 H, the molar composition of the hydrogen is 7.01 percent, the methane is 84.07 percent, the nitrogen is 8.92 percent, and the higher calorific value is 31.97MJ/m 3 And meets the requirements of the second class of natural gas in GB17820-2018 Natural gas.
Example 3
The fuel cell hydrogen market of this example is good, and pipeline natural gas market is general, adopts pressure swing adsorption stripping gas as temperature swing adsorption regeneration gas, as shown in fig. 3.
The temperature of the coke oven gas after compression and pretreatment is 40 ℃, the pressure is 2.0MPaG, and the flow is 20014Nm 3 The molar composition of the catalyst is 60.74 percent of hydrogen, 10.47 percent of carbon monoxide, 2.82 percent of carbon dioxide, 19.42 percent of methane, 0.94 percent of ethylene, 0.94 percent of ethane, 3.87 percent of nitrogen, 0.35 percent of water and 0.46 percent of oxygen. Wherein each standard coke oven gas contains 6mg of tar and naphthalene, 20mg of hydrogen sulfide, 200mg of organic sulfur, 44mg of ammonia and 1200mg of benzene. The coke oven gas after pre-purification firstly enters a temperature swing adsorption unit X3 to remove tar and naphthalene to be not more than 1mg/Nm 3 And simultaneously removing heavy component impurities in the coke oven gas. The regenerated gas of the temperature swing adsorption unit X3 adopts the pressure swing adsorption unit X5 to desorb gas with the gas quantity of 2000Nm 3 And h, delivering the regenerated mixture to a fuel pipe network.
And (3) allowing the purified coke oven gas from the temperature swing adsorption unit X3 to enter a fine desulfurization unit X4, sequentially carrying out pre-hydrogenation, primary adsorption desulfurization, secondary hydrogenation and secondary adsorption desulfurization, removing the total sulfur in the coke oven gas to be not more than 0.1ppmv, and then allowing the coke oven gas to enter copper-based fine desulfurization to remove the total sulfur in the coke oven gas to be not more than 0.02ppmv, so that the purification requirement of hydrogen gas for fuel cell preparation by pressure swing adsorption is met.
The gas flow of the refined coke oven gas from the refined desulphurization unit X4 is 19731Nm 3 And/h, dividing the mixture into two parts, namely a pressure swing adsorption unit X5 and a methanation and drying unit X7. Example 3 the fuel cell hydrogen production was designed to be about 6000Nm 3 The filling amount per hour, and simultaneously considering the requirement of the subsequent methanation on the hydrogen-carbon ratio, 6689Nm of the refined coke oven gas of the demethanization and drying unit X7 3 Perh, the coke oven gas is subjected to fine purification 12915Nm after the coke oven gas enters a pressure swing adsorption unit X5 for cooling and water distribution 3 H is the ratio of the total weight of the catalyst to the total weight of the catalyst. 6074Nm obtained by pressure swing adsorption Unit X5 3 Hydrogen of fuel cell, the molar purity of hydrogen is not less than 99.97%, total hydrocarbon (calculated by methane) is not more than 2ppmv, carbon monoxide is not more than 0.2ppmv, total sulfur is not more than 0.004ppmv, formaldehyde is not more than 0.01ppmv, total halide (calculated by halide ion) is not more than 0.05ppmv, and the hydrogen is charged for sale and sent to fuel pipe network when not charged. Example pipeNatural gas required pressure 1.0MPaG, and desorption gas 6846Nm of pressure swing adsorption unit X5 3 Per hour, molar composition of hydrogen 25.04%, carbon monoxide 20.25%, carbon dioxide 5.45%, methane 37.54%, ethane 3.63%, nitrogen 7.48%, water 0.61%, wherein 2000Nm 3 Use as X4 regeneration gas in a temperature swing adsorption Unit, 1841Nm 3 The hydrogen is removed from a fuel pipe network, and the rest is 1500Nm 3 The pressure of the coke oven gas is increased to 1.5MPaG through a desorption gas compression unit X6, and then the coke oven gas and the refined coke oven gas are 6689Nm 3 The mol composition after the mixing per hour is 53.51 percent of hydrogen, 12.34 percent of carbon monoxide, 3.32 percent of carbon dioxide, 22.89 percent of methane, 2.21 percent of ethane, 4.56 percent of nitrogen, 1.16 percent of water and 3.06 percent of hydrogen-carbon ratio, thereby meeting the condition of preparing the pipeline natural gas through methanation.
Pipeline natural gas 4082Nm from methanation and drying unit X7 3 H, the molar composition of the catalyst is 4.62 percent of hydrogen, 85.56 percent of methane, 0.67 percent of carbon dioxide, 9.15 percent of nitrogen and 32.24MJ/m of high calorific value 3 And meets the requirements of the second class of natural gas in GB17820-2018 Natural gas.
Example 4
In the fuel cell hydrogen market of the present example, the pipeline natural gas market is common, and the shift unit X2 is arranged to convert carbon monoxide into hydrogen, and meanwhile, the pressure swing adsorption desorption gas is used as the temperature swing adsorption regeneration gas, as shown in fig. 3.
The temperature of the coke oven gas after compression and pretreatment is 40 ℃, the pressure is 2.0MPaG, and the flow is 20014Nm 3 The molar composition of the catalyst is 60.74 percent of hydrogen, 10.47 percent of carbon monoxide, 2.82 percent of carbon dioxide, 19.42 percent of methane, 0.94 percent of ethylene, 0.94 percent of ethane, 3.87 percent of nitrogen, 0.35 percent of water and 0.46 percent of oxygen. Wherein each standard coke oven gas contains 6mg of tar and naphthalene, 20mg of hydrogen sulfide, 200mg of organic sulfur, 44mg of ammonia and 1200mg of benzene. Entering a conversion unit X2, simultaneously supplementing water vapor, converting carbon monoxide into hydrogen and carbon dioxide, wherein the flow rate of the coke oven gas after conversion, cooling and water diversion is 21548Nm 3 The molar composition of the catalyst is 63.93 percent of hydrogen, 0.49 percent of carbon monoxide, 11.86 percent of carbon dioxide, 18.03 percent of methane, 1.74 percent of ethane, 3.59 percent of nitrogen and 0.36 percent of water. The coke oven gas after pre-purification firstly enters a temperature swing adsorption unit X3 to remove tar and naphthalene to a small extentAt 1mg/Nm 3 And simultaneously removing heavy component impurities in the coke oven gas. The regenerated gas of the temperature swing adsorption unit X3 adopts the pressure swing adsorption unit X6 to desorb gas with the gas quantity of 2000Nm 3 And h, delivering the regenerated mixture to a fuel pipe network.
And (3) allowing the purified coke oven gas from the temperature swing adsorption unit X3 to enter a fine desulfurization unit X4, sequentially carrying out pre-hydrogenation, primary adsorption desulfurization, secondary hydrogenation and secondary adsorption desulfurization, removing the total sulfur in the coke oven gas to be not more than 0.1ppmv, and then allowing the coke oven gas to enter copper-based fine desulfurization to remove the total sulfur in the coke oven gas to be not more than 0.02ppmv, so that the purification requirement of hydrogen gas for fuel cell preparation by pressure swing adsorption is met.
The gas quantity of the refined coke oven gas discharged from the refined desulphurization unit X4 is 21545Nm 3 And/h, dividing the mixture into two parts, namely a pressure swing adsorption unit X5 and a methanation and drying unit X7. This example 4 fuel cell hydrogen production was designed to be about 6000Nm 3 The charging amount per hour, and simultaneously considering the requirement of the subsequent methanation on the hydrogen-carbon ratio, 8503Nm of refined coke oven gas of a demethanization and drying unit X7 3 13058Nm of the refined purified coke oven gas enters a pressure swing adsorption unit X5 for cooling and water separation 3 H is used as the reference value. 6503Nm obtained by pressure swing adsorption unit X5 3 Hydrogen of fuel cell, the molar purity of hydrogen is not less than 99.97%, total hydrocarbon (calculated by methane) is not more than 2ppmv, carbon monoxide is not more than 0.2ppmv, total sulfur is not more than 0.004ppmv, formaldehyde is not more than 0.01ppmv, total halide (calculated by halide ion) is not more than 0.05ppmv, and the hydrogen is charged for sale and sent to fuel pipe network when not charged. The required pressure of the natural gas of the pipeline of the embodiment is 1.0MPaG, and the desorbed gas 6556Nm of the pressure swing adsorption unit X5 3 H, molar composition of hydrogen 25.04%, carbon monoxide 20.25%, carbon dioxide 5.45%, methane 37.54%, ethane 3.63%, nitrogen 7.48%, water 0.61%, 2000Nm 3 Use as X4 regeneration gas in a temperature swing adsorption Unit, 2806Nm 3 Perh go to fuel pipe network, remaining 1750Nm 3 The pressure of the coke oven gas is increased to 1.5MPaG through a desorption gas compression unit X6, and then the coke oven gas is mixed with 8503Nm of the purified coke oven gas 3 The mol composition after mixing is 57.43 percent of hydrogen, 3.82 percent of carbon monoxide, 10.76 percent of carbon dioxide, 21.29 percent of methane, 2.06 percent of ethane, 4.24 percent of nitrogen and 0.4 percent of water, and the hydrogen-carbon ratio3.06, the condition for preparing the pipeline natural gas by methanation is met.
Pipeline natural gas 4758Nm from methanation and drying unit X7 3 H, the molar composition of the catalyst is 4.69 percent of hydrogen, 85.48 percent of methane, 0.70 percent of carbon dioxide, 9.14 percent of nitrogen and 32.22MJ/m of high calorific value 3 And meets the requirements of the second class of natural gas in GB17820-2018 Natural gas.
Finally, it should be noted that: the above embodiments are only preferred embodiments of the present invention to illustrate the technical solutions of the present invention, but not to limit the technical solutions, and certainly not to limit the patent scope of the present invention; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; the modifications or the substitutions do not cause the essence of the corresponding technical solutions to depart from the scope of the technical solutions of the embodiments of the present invention; that is, the technical problems to be solved by the present invention, which are not substantially changed or supplemented by the spirit and the concept of the main body of the present invention, are still consistent with the present invention and shall be included in the scope of the present invention; in addition, the technical scheme of the invention is directly or indirectly applied to other related technical fields, and the technical scheme is included in the patent protection scope of the invention.
Claims (10)
1. The production capacity regulating process for preparing fuel cell hydrogen and pipeline natural gas by coke oven gas is characterized by comprising the following steps: the compression and pretreatment unit (X1) is connected or not connected with the conversion unit (X2) and then enters a temperature swing adsorption unit (X3);
a temperature swing adsorption unit (X3) which is connected out from the compression and pretreatment unit (X1) or the conversion unit (X2) to remove heavy component impurities in the coke oven gas, a fine desulfurization unit (X4) which is connected out from the temperature swing adsorption unit (X3) to remove inorganic sulfur and organic sulfur in the coke oven gas, a pressure swing adsorption unit (X5) which is connected out from the fine desulfurization unit (X4) to prepare hydrogen of the fuel cell, a desorption gas compression unit (X6) which is connected out from the pressure swing adsorption unit (X5) to pressurize desorption gas, and a methanation and drying unit (X7) which is connected out from the desorption gas compression unit (X6) and connected to convert carbon monoxide and carbon dioxide into methane after being mixed with gas of a fine gas purification pipe (9);
the conversion unit (X2) is a unit which is connected with a first pre-purified gas bypass pipe (3) and a second pre-purified gas bypass pipe (4) and is used for converting carbon monoxide into hydrogen and carbon dioxide;
the coke oven gas conveying pipe (1) is connected with a compression and pretreatment unit (X1), a fuel gas external conveying pipe (20) is connected to the third desorption gas conveying pipe (14), a pressure swing adsorption unit (X5) is connected with a fuel cell hydrogen external conveying pipe (10), and a methanation and drying unit (X7) is connected with a pipeline natural gas external conveying pipe (17).
2. The process for capacity adjustment according to claim 1, wherein a pre-clean gas transfer line (2) is connected between the compression and pre-treatment unit (X1) and the temperature swing adsorption unit (X3), wherein a first pre-clean gas bypass line (3) is connected to the pre-clean gas transfer line (2) at the beginning of the gas flow, and a second pre-clean gas bypass line (4) is connected to the pre-clean gas transfer line (2) at the end of the gas flow.
3. The capacity adjustment process according to claim 2, wherein an air inlet valve is arranged on the pre-purified air delivery pipe (2) and at the beginning of the first pre-purified air bypass pipe (3) in the air flow direction; when the hydrogen capacity of the fuel cell is pursued to be larger, the air inlet valve of the pre-purified gas delivery pipe (2) is closed, and the air inlet valve of the first pre-purified gas bypass pipe (3) is opened; on the contrary, the air inlet valve of the first pre-purified air bypass pipe (3) is closed, and the air inlet valve of the pre-purified air delivery pipe (2) is opened.
4. The capacity modulation process according to claim 1, wherein a purified gas delivery pipe (5) is connected between the temperature swing adsorption unit (X3) and the fine desulfurization unit (X4), the temperature swing adsorption unit (X3) is provided with a regenerated gas delivery pipe (21) and a regenerated gas output pipe (22), and the regenerated gas output pipe (22) is connected to the fuel gas output pipe (20); a self-purification gas delivery pipe (6) is led out from the purification gas delivery pipe (5), the self-purification gas delivery pipe (6) is connected to a regeneration gas delivery pipe (21), and whether the self-purification gas is used as temperature swing adsorption regeneration gas or not is selected according to the capacity regulation requirement.
5. The capacity adjustment process according to claim 1, wherein the fine desulfurization unit (X4) is connected to a fine purification gas delivery pipe (7), the fine purification gas delivery pipe (7) is connected to a first fine purification gas delivery pipe (8) of the pressure swing adsorption unit (X5) and a second fine purification gas delivery pipe (9) of the demethanization and drying unit (X7), and the amounts of the second desorption gas delivery pipe (13), the first fine purification gas delivery pipe (8) and the second fine purification gas delivery pipe (9) are adjusted according to the capacity adjustment requirement; the purified gas in the fine desulfurization unit (X4) is sequentially subjected to pre-hydrogenation, first-stage adsorption desulfurization, second-stage hydrogenation, second-stage adsorption desulfurization and copper-based fine desulfurization, so that the total sulfur in the fine purified gas after the fine desulfurization unit (X4) is not more than 0.02ppmv.
6. The capacity-adjusting process according to claim 1, wherein the pressure swing adsorption unit (X5) is connected to the fuel cell hydrogen gas delivery pipe (10) and the first desorption gas delivery pipe (12).
7. The process for regulating the energy production according to claim 6, wherein a hydrogen regeneration delivery pipe (11) is led out from the fuel cell hydrogen gas delivery pipe (10), the hydrogen regeneration delivery pipe (11) is connected to a regeneration gas delivery pipe (21) and led out from a hydrogen fuel delivery pipe (18), the hydrogen fuel delivery pipe (18) is connected to a fuel gas delivery pipe (20), and the fuel cell hydrogen gas is selected as a product gas or a fuel gas or a temperature swing adsorption regeneration gas according to the requirements of energy production regulation and hydrogen product filling.
8. The productivity adjustment process according to claim 6 or 7, wherein: a second desorption gas conveying pipe (13) and a third desorption gas conveying pipe (14) are led out from the first desorption gas conveying pipe (12), the second desorption gas conveying pipe (13) is connected to a desorption gas compression unit (X6), a fuel gas outward conveying pipe (20) and a regeneration desorption gas conveying pipe (19) are led out from the third desorption gas conveying pipe (14), the regeneration desorption gas conveying pipe (19) is connected to a regeneration gas conveying pipe (21), the desorption gas flow rate of the desorption gas compression unit (X6) in the second desorption gas conveying pipe (13) is adjusted according to the capacity adjusting requirement, and simultaneously desorption gas is selected as fuel gas or temperature swing adsorption regeneration gas.
9. The capacity adjustment process according to claim 1, wherein the desorption gas compression unit (X6) is connected with a desorption gas conveying pipe (15), the desorption gas conveying pipe (15) and the second purified gas conveying pipe (9) are connected with a third purified gas conveying pipe (16), and the third purified gas conveying pipe (16) is connected with the methanation and drying unit (X7); and determining the outlet pressure of the desorption gas compressor unit (X6) or the operation pressure of the methanation unit (X7) according to the pressure required by the pipeline natural gas output pipe (17).
10. The capacity adjusting process according to claim 9, wherein the third purified gas delivery pipe (16) is provided with analysis points for the contents of hydrogen, carbon monoxide, carbon dioxide and lower hydrocarbons, and the hydrogen-carbon ratio of the gas in the third purified gas delivery pipe (16) is obtained according to the analysis result; the hydrogen-carbon ratio of the gas in the third purified gas conveying pipe (16) is 3.0-3.3.
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