CN115159458A - Natural gas hydrogen production system and hydrogen production method - Google Patents
Natural gas hydrogen production system and hydrogen production method Download PDFInfo
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- CN115159458A CN115159458A CN202210910236.3A CN202210910236A CN115159458A CN 115159458 A CN115159458 A CN 115159458A CN 202210910236 A CN202210910236 A CN 202210910236A CN 115159458 A CN115159458 A CN 115159458A
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 113
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 64
- 239000001257 hydrogen Substances 0.000 title claims abstract description 60
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 58
- 239000003345 natural gas Substances 0.000 title claims abstract description 41
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 35
- 239000007789 gas Substances 0.000 claims abstract description 78
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 59
- 238000001179 sorption measurement Methods 0.000 claims abstract description 45
- 238000006243 chemical reaction Methods 0.000 claims abstract description 29
- 238000000034 method Methods 0.000 claims abstract description 28
- 239000000446 fuel Substances 0.000 claims abstract description 11
- 230000008569 process Effects 0.000 claims description 22
- 239000002994 raw material Substances 0.000 claims description 11
- 239000003463 adsorbent Substances 0.000 claims description 9
- 239000002737 fuel gas Substances 0.000 claims description 9
- 230000008929 regeneration Effects 0.000 claims description 9
- 238000011069 regeneration method Methods 0.000 claims description 9
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 6
- 238000012545 processing Methods 0.000 claims description 6
- 229920006395 saturated elastomer Polymers 0.000 claims description 6
- 239000002918 waste heat Substances 0.000 claims description 6
- 239000006227 byproduct Substances 0.000 claims description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 3
- 239000001569 carbon dioxide Substances 0.000 claims description 3
- 239000003054 catalyst Substances 0.000 claims description 3
- 238000002485 combustion reaction Methods 0.000 claims description 3
- 238000003795 desorption Methods 0.000 claims description 3
- 238000006477 desulfuration reaction Methods 0.000 claims description 3
- 230000023556 desulfurization Effects 0.000 claims description 3
- 238000011010 flushing procedure Methods 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000012535 impurity Substances 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 238000000629 steam reforming Methods 0.000 claims description 3
- 229910052717 sulfur Inorganic materials 0.000 claims description 3
- 239000011593 sulfur Substances 0.000 claims description 3
- 230000009466 transformation Effects 0.000 claims description 3
- 229910019142 PO4 Inorganic materials 0.000 claims description 2
- 238000005260 corrosion Methods 0.000 claims description 2
- 230000007797 corrosion Effects 0.000 claims description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims description 2
- 239000010452 phosphate Substances 0.000 claims description 2
- 239000007787 solid Substances 0.000 claims description 2
- 230000000630 rising effect Effects 0.000 claims 2
- 238000010276 construction Methods 0.000 abstract description 5
- 238000003908 quality control method Methods 0.000 abstract description 5
- 238000009434 installation Methods 0.000 abstract description 3
- 230000008859 change Effects 0.000 abstract description 2
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 12
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 9
- 238000005336 cracking Methods 0.000 description 5
- 229910021529 ammonia Inorganic materials 0.000 description 4
- 230000001174 ascending effect Effects 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 4
- 238000013461 design Methods 0.000 description 4
- 238000007599 discharging Methods 0.000 description 4
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- 239000000047 product Substances 0.000 description 4
- 238000003786 synthesis reaction Methods 0.000 description 4
- 150000001875 compounds Chemical class 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
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- 238000000354 decomposition reaction Methods 0.000 description 2
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- 238000011049 filling Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 230000008094 contradictory effect Effects 0.000 description 1
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- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/042—Purification by adsorption on solids
- C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/047—Composition of the impurity the impurity being carbon monoxide
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
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- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/0495—Composition of the impurity the impurity being water
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- C01—INORGANIC CHEMISTRY
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- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
- C01B2203/0827—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel at least part of the fuel being a recycle stream
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- C01—INORGANIC CHEMISTRY
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- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
- C01B2203/1241—Natural gas or methane
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- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1288—Evaporation of one or more of the different feed components
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- General Health & Medical Sciences (AREA)
- Hydrogen, Water And Hydrids (AREA)
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Abstract
The invention discloses a natural gas hydrogen production system and a hydrogen production method, which change the traditional installation method, solve the quality control risk brought by the site construction of users and realize the whole-process quality control. It comprises a steam conversion device, a steam conversion device and an adsorption tower (8); the steam conversion device comprises a desulfurizer (1) and a converter (2), the converter (2) is connected with the steam conversion device, the steam conversion device comprises a boiler feed water preheater (4), a converted gas water cooler (5) and a converted gas-water separator (6), the converted gas-water separator (6) is connected with the converter (2) through an adsorption tower (8), a burner (3) is arranged at the bottom of the converter (2), and heat required by methane conversion is provided by burning fuel mixed gas through the burner (3) at the bottom. The invention realizes the standardized production of products, forms standard series products, is convenient for equipment management of users, has universal spare parts and reduces the running cost of the device.
Description
Technical Field
The invention relates to the technical field of hydrogen production, in particular to a natural gas hydrogen production system and a hydrogen production method.
Background
Hydrogen of the formula H 2 The molecular weight of the polymer is 2.01588,it is a very inflammable gas at normal temperature and pressure. Colorless and transparent, odorless and tasteless, and insoluble in water. Hydrogen is the least dense gas known in the world, and has a density of only 1/14 that of air, i.e., at 101.325 kPa (1 atm) and 0 ℃, and a density of 0.089g/L. Therefore, the hydrogen can be used as filling gas for the airship and the hydrogen balloon (because the hydrogen has flammability and low safety, the airship is filled with helium at present). Hydrogen is a substance with the minimum relative molecular mass, has strong reducibility and is often used as a reducing agent to participate in chemical reactions.
Industry typically produces hydrogen from natural gas or water gas without the use of energy intensive methods of water electrolysis. The prepared hydrogen is used for cracking reaction in the petrochemical industry and producing ammonia in a large quantity. Hydrogen molecules can enter crystal lattices of a plurality of metals to cause a hydrogen embrittlement phenomenon, so that special materials (such as Mongolian alloy) are required to be used for a storage tank and a pipeline of the hydrogen, and the design is more complicated.
The technologies generally adopted in the hydrogen production industry at present mainly comprise: water electrolysis, methanol cracking, natural gas cracking, ammonia decomposition, coal gasification hydrogen production, hydrogen-rich tail gas recovery and the like. At present, the main sources of hydrogen are divided into three main categories, namely traditional water electrolysis hydrogen production; purifying hydrogen by using industrial waste gas; thirdly, using fossil fuel, such as coal gas, natural gas, heavy oil and the like to make gas or propane, liquid ammonia, methanol and the like to obtain a hydrogen-containing gas source and then separating and purifying the hydrogen. Among the three types, the hydrogen production technology which can obtain high-purity hydrogen and is used for industry mainly comprises five types of water electrolysis, natural gas cracking, ammonia decomposition, coal gas production and methanol cracking.
China is rich in natural gas resources, most of which are mainly distributed in remote areas such as the west, the northwest and the like, so that the cost of compression, transportation, storage, utilization and the like is high. At present, in order to realize the economic utilization of natural gas, the natural gas is generally used as a primary raw material to be processed to produce compounds such as multi-carbon hydrocarbon and alcohol, and the processing is mainly completed in two steps of firstly converting methane into CO and H 2 (i.e., syngas), and then converting the syngas into multi-carbon hydrocarbons and alcohols, e.g., by F-T synthesis. Almost carbonaceous compounds can be used to produce synthesis gas, e.g. coal, naturalGas, etc., the cost of producing synthesis gas can vary, being mainly composed of H 2 the/C0 ratio, raw materials, preparation processes, scale, system integration level and other factors. The synthesis gas has wide application and can be used as an industrial raw material to produce ammonia, hydrogen, methanol and the like.
The main component of natural gas is methane (CH) 4 ) The hydrogen storage amount is 25 percent, and the mass ratio of hydrogen atoms in the compounds is the largest. Meanwhile, natural gas belongs to one of three fossil energy sources on the earth, and has a huge reserve (shale gas and natural ice which are prevalent recently are similar to the fossil energy sources), so that the natural gas is developed into the most mainstream hydrogen preparation technology in the industry for a long time and occupies an overwhelming dominance in many countries. Because of the stable chemical structure of methane, the industrial method usually adopts cheap and easily available steam and oxygen medium to react with methane to generate synthetic gas, and then prepares hydrogen through chemical conversion and separation.
Disclosure of Invention
The invention aims to provide a natural gas hydrogen production system and a hydrogen production method, which change the traditional installation method, solve the quality control risk brought by the site construction of a user and realize the whole-process quality control.
In order to realize the purpose, the invention provides the following technical scheme:
the invention provides a natural gas hydrogen production system which is characterized by comprising a steam conversion device, a steam conversion device and an adsorption tower; the steam conversion device comprises a desulfurizer and a converter, the converter is connected with the steam conversion device, the steam conversion device comprises a boiler feed water preheater, a converted gas water cooler and a converted gas-water separator, and the converted gas-water separator is connected with the adsorption tower.
Furthermore, a burner is arranged at the bottom of the converter, and the heat required by methane conversion is provided by burning fuel mixed gas through the burner at the bottom.
And further, the system also comprises a desalted water preheater, wherein desalted water enters the converter to be subjected to byproduct steam after being preheated by the desalted water preheater and the boiler water supply preheater.
Furthermore, 4-6 adsorption towers are provided, and 1 adsorption tower is in an adsorption state at any time.
The invention provides a natural gas hydrogen production system for a natural gas hydrogen production method, which is characterized by comprising the following steps:
step one, raw material pretreatment: pressurizing natural gas outside a battery compartment by a compressor, and heating by a feed gas preheater of a convection section of a steam reformer;
step two, steam reforming: the natural gas enters a desulfurizer for desulfurization treatment, the sulfur in the feed gas is reduced to be below 0.1PPM in the desulfurizer, the desulfurized feed gas and process steam enter an automatic value adjusting mixed gas preheater and are further preheated to be above 510 ℃, the feed gas and the process steam uniformly enter a converter from an upper gas collecting main pipe and an upper pig tail pipe, and methane and water steam react to generate CO and H in a catalyst layer 2 ；
Step three, transformation process: the reformed gas enters a boiler feed water preheater, a reformed gas water cooler and a reformed gas-water separator in sequence after the temperature of the reformed gas is raised and lowered, the condensate is separated to obtain process condensate, and the process gas is sent to pressure swing adsorption; mixing natural gas as fuel with desorption gas of pressure swing adsorption, adjusting the fuel gas amount entering a fuel gas preheater according to the temperature of gas at the outlet of the reformer, and enabling the fuel gas to enter a top burner for combustion after flow adjustment to provide heat for the reformer;
step four, adsorption process: the components such as methane, carbon dioxide and carbon monoxide in the converted gas are stopped on the surface of the adsorbent, hydrogen is collected from the top of the adsorption tower as a non-adsorption component and is sent to the outside, the adsorbent saturated by impurity components is desorbed from the adsorbent through a regeneration step, and is sent to the converter as fuel after being collected, and after the regeneration is finished, the adsorption tower has the capacity of processing the converted gas and producing hydrogen again.
Further, in the first step, the pressure of the natural gas is increased to 1.6MPa by a compressor, and the temperature of the feed gas is preheated to 370-390 ℃.
Further, in the second step, the desulfurized raw material gas and the process steam are mixed according to the content ratio of H2O/Sigma C = 3-4.
Furthermore, in the third step, the temperature of the converted gas discharged from the converter is 840-860 ℃, the high-temperature converted gas enters the tube pass of the waste heat boiler to generate 3.0MPa saturated steam, and the temperature of the converted gas discharged from the waste heat boiler is reduced to 290-310 ℃.
Further, in the fourth step, the regeneration step of the adsorption tower comprises the steps of uniform descending, forward discharging, reverse discharging, flushing, uniform ascending and final ascending.
Furthermore, phosphate solution and deoxidizer are added into the boiler device to improve the scaling condition and the corrosion condition of the boiler water, and the steam drum needs to continuously discharge part of the boiler water to control the total solid dissolving amount of the boiler water in the steam drum.
Based on the technical scheme, the embodiment of the invention can at least produce the following technical effects:
(1) The whole skid-mounted design changes the traditional field installation mode, and the production management and control of the whole processes of materials, flaw detection, pressure test and the like in a company are completely realized by processing, producing, tubing and prying in the company, so that the quality management and control risk brought by the field construction of a user is fundamentally solved, and the whole-process quality control is really realized.
(2) Products are all prized in a company, the idea of manufacturing a factory in the factory is adopted, after the verification in the factory is qualified, the products are disassembled and assembled according to a set disassembling and assembling scheme and sent to a user site for re-assembling, the site construction amount is small, and the construction period is short.
(3) The automation degree is very high, and full automatic monitoring and control can be carried out to the operational aspect of device through upper system to upload to cloud ware in real time to key data, carry out remote detection, realize on-the-spot unmanned management.
(4) The device has very strong mobility, can be used after being prized and installed again after being moved to a different place according to the specific conditions of a project, realizes the reutilization of equipment, and ensures the maximum benefit of the value of the equipment
(5) According to the demand of the hydrogen amount of the hydrogen filling station, standard process design is carried out, and the design principle of combining process modules is adopted, so that the standardized production of products is realized, the standard serialized products are formed, the equipment management of users is facilitated, spare parts are universal, and the operation cost of the device is reduced.
While the preferred embodiments of the present invention have been described in detail, the present invention is not limited to the above embodiments, and various changes can be made without departing from the spirit of the present invention within the knowledge of those skilled in the art.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
FIG. 1 is a schematic structural diagram of an embodiment of the present invention;
names of corresponding components represented by numerals or letters in the drawings:
1. a desulfurizer; 2. a converter; 3. burning a nozzle; 4. a boiler feed water preheater; 5. a reformed gas water cooler; 6. a reformed gas-water separator; 7. a desalted water preheater; 8. an adsorption tower.
Detailed Description
It should be understood that the specific embodiments described herein are merely illustrative of the invention and do not limit the invention.
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. 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 addition, the technical solutions in the embodiments may be combined with each other, but must be based on the realization of the technical solutions by those skilled in the art, and when the technical solutions are contradictory or cannot be realized, the technical solutions should be considered that the combination does not exist, and the technical solutions are not within the protection scope of the present invention.
A natural gas hydrogen production system comprises a steam conversion device, a steam conversion device and an adsorption tower 8; the steam conversion device comprises a desulfurizer 1 and a converter 2, the converter 2 is connected with the steam conversion device, the steam conversion device comprises a boiler feed water preheater 4, a converted gas water cooler 5 and a converted gas-water separator 6, and the converted gas-water separator 6 is connected with an adsorption tower 8. The bottom of the converter 2 is provided with a burner 3, and the heat required by the conversion of methane is provided by burning fuel mixed gas by the bottom burner 3. The device also comprises a desalted water preheater 7, and desalted water enters the converter 2 to be subjected to byproduct steam after being preheated by the desalted water preheater 7 and the boiler feed water preheater 4. 4-6 adsorption towers 8 are provided, and 1 adsorption tower is in an adsorption state at any time.
The purpose of the invention is realized by the following technical scheme, and the raw materials are shown in the following table 1:
table 1 raw material composition table
| Composition (I) | Content (%) |
| CH 4 | 92.887 |
| C 2 H 6 | 3.705 |
| C 3 H 8 | 0.679 |
| H 2 S | 0.002 |
| N 2 | 1.795 |
| CO 2 | 0.562 |
| Others are | 0.37 |
Step one, raw material pretreatment: pressurizing natural gas outside a battery compartment to 1.6MPa by a compressor, and heating to 380 ℃ by a feed gas preheater of a convection section of a steam reformer;
step two, steam reforming: the natural gas enters a desulfurizer 1 for desulfurization treatment, the sulfur in the feed gas is reduced to be below 0.1PPM in the desulfurizer 1, and the desulfurized feed gas and process steam (3.0 MPa) are mixed according to the H 2 The O/sigma C = 3-4 ratio enters an automatic value adjusting mixed gas preheater, is further preheated to more than 510 ℃, uniformly enters a converter 2 from an upper gas collecting header and an upper pigtail pipe, desalted water is preheated by a desalted water preheater 7 and a boiler feed water preheater 4 and enters the converter 2 to generate byproduct steam, and in a catalyst layer, methane reacts with steam to generate CO and H 2 The heat required by methane conversion is provided by burning fuel mixed gas by a bottom burner;
step three, transformation process: the temperature of the converted gas discharged from the converter is 850 ℃, the high-temperature converted gas enters the tube pass of the waste heat boiler 3 to generate saturated steam of 3.0MPa, the temperature of the converted gas discharged from the waste heat boiler 3 is reduced to 300 ℃, the converted gas sequentially enters the boiler feed water preheater 4, the converted gas water cooler 5 and the converted gas water separator 6, the condensate is separated to obtain process condensate, and the process gas is sent to pressure swing adsorption; the natural gas as fuel is mixed with the desorption gas of pressure swing adsorption, the fuel gas flow entering the fuel gas preheater is adjusted according to the temperature of the gas at the outlet of the reformer, and the fuel gas enters the top burner for combustion after flow adjustment, so that heat is provided for the reformer.
Step four, adsorption process: the pressure swing adsorption consists of 5 adsorption towers 8, 1 adsorption tower is in an adsorption state at any time, components such as methane, carbon dioxide and carbon monoxide in converted gas are stopped on the surface of the adsorbent, hydrogen is collected from the top of the adsorption tower 8 as a non-adsorption component, the hydrogen is sent out of the adsorption tower, the adsorbent saturated by impurity components is desorbed from the adsorbent through a regeneration step and is sent to a conversion furnace as fuel after being collected, the regeneration step of the adsorption tower 8 consists of steps of uniform descending, forward discharging, reverse discharging, flushing, uniform ascending and final ascending, the regeneration is finished, the adsorption tower has the capacity of processing the converted gas and producing the hydrogen again, and the 5 adsorption tower flows through the steps in turn to ensure the continuous processing of the converted gas and the continuous production of the hydrogen at the same time.
The foregoing shows and describes the general principles and features of the present invention, together with the advantages thereof. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, which are described in the specification and illustrated only to illustrate the principle of the present invention, but that various changes and modifications may be made therein without departing from the spirit and scope of the present invention, which fall within the scope of the invention as claimed. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (10)
1. A natural gas hydrogen production system is characterized by comprising a steam conversion device, a steam conversion device and an adsorption tower (8); the steam conversion device comprises a desulfurizer (1) and a converter (2), the converter (2) is connected with the steam conversion device, the steam conversion device comprises a boiler feed water preheater (4), a converted gas water cooler (5) and a converted gas-water separator (6), and the converted gas-water separator (6) is connected with an adsorption tower (8).
2. The natural gas hydrogen production system according to claim 1, characterized in that: the bottom of the converter (2) is provided with a burner (3), and the heat required by methane conversion is provided by burning fuel mixed gas by the burner (3) at the bottom.
3. The natural gas hydrogen production system according to claim 1, characterized in that: the system also comprises a desalted water preheater (7), and desalted water enters the converter (2) to be subjected to byproduct steam after being preheated by the desalted water preheater (7) and the boiler feed water preheater (4).
4. The natural gas hydrogen production system according to claim 1, characterized in that: 4-6 adsorption towers (8) are arranged, and 1 adsorption tower is in an adsorption state at any time.
5. A method for producing hydrogen from natural gas is characterized by comprising the following steps:
step one, raw material pretreatment: pressurizing natural gas outside a battery compartment by a compressor, and heating by a feed gas preheater of a convection section of a steam reformer;
step two, steam reforming: natural gas enters a desulfurizer (1) for desulfurization treatment, the sulfur in the feed gas is removed to be below 0.1PPM in the desulfurizer (1), the desulfurized feed gas and process steam enter an automatic value adjusting mixed gas preheater and are further preheated to be above 510 ℃, the desulfurized feed gas and the process steam uniformly enter a converter (2) from an upper gas collecting main pipe and an upper pigtail pipe, and in a catalyst layer, methane and water steam react to generate CO and H 2 ；
Step three, transformation process: the reformed gas enters a boiler feed water preheater (4), a reformed gas water cooler (5) and a reformed gas water separator (6) in sequence after the temperature is raised and lowered, condensate is separated out to obtain process condensate, and the process gas is sent to pressure swing adsorption; mixing natural gas as fuel with desorption gas of pressure swing adsorption, adjusting the fuel gas amount entering a fuel gas preheater according to the temperature of gas at the outlet of the reformer, and enabling the fuel gas to enter a top burner for combustion after flow adjustment to provide heat for the reformer;
step four, adsorption process: methane, carbon dioxide and carbon monoxide in the converted gas are stopped on the surface of the adsorbent, hydrogen is collected from the top of the adsorption tower (8) as a non-adsorption component and is sent to the outside, the adsorbent saturated by impurity components is desorbed from the adsorbent through a regeneration step, and is sent to the converter as fuel after being collected, and after the regeneration is finished, the adsorption tower has the capacity of processing the converted gas and producing hydrogen again.
6. The natural gas hydrogen production method according to claim 5, characterized in that: in the first step, the pressure of the natural gas is increased to 1.6MPa by a compressor, and the temperature of the raw material gas is increased to 370-390 ℃.
7. The natural gas hydrogen production method according to claim 5, characterized in that: in the second step, the desulfurized raw material gas and the process steam are mixed according to the ratio of H 2 Mixing at a content ratio of O/SIGMA C = 3-4.
8. The natural gas hydrogen production method according to claim 5, characterized in that: in the third step, the temperature of the converted gas discharged from the converter is 840-860 ℃, the high-temperature converted gas enters the tube pass of the waste heat boiler to generate 3.0MPa saturated steam, and the temperature of the converted gas discharged from the waste heat boiler is reduced to 290-310 ℃.
9. The natural gas hydrogen production method according to claim 5, characterized in that: in the fourth step, the regeneration step of the adsorption tower (8) comprises uniform reduction, forward release, reverse release, flushing, uniform rising and final rising.
10. The natural gas hydrogen production method according to claim 5, characterized in that: phosphate solution and deoxidizer are added into the boiler device to improve the scaling condition and the corrosion condition of the boiler water, and the steam drum needs to continuously discharge part of the boiler water to control the total solid dissolving amount of the boiler water in the steam drum.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106564861A (en) * | 2016-11-09 | 2017-04-19 | 华南理工大学 | Process for efficiently recovering reforming gas energy in hydrocarbon steam reforming hydrogen production process |
| CN207659077U (en) * | 2017-07-10 | 2018-07-27 | 杭州普菲科空分设备有限公司 | A kind of natural gas reforming hydrogen manufacturing device |
| CN213231512U (en) * | 2020-09-07 | 2021-05-18 | 重庆金苏化工有限公司 | Natural gas hydrogen production medium temperature shift system |
| CN113213425A (en) * | 2021-06-08 | 2021-08-06 | 金川集团股份有限公司 | System and method for preparing hydrogen by using natural gas |
| CN114014270A (en) * | 2021-12-10 | 2022-02-08 | 四川天采科技有限责任公司 | Modularized natural gas reforming hydrogen production machine and hydrogen production method thereof |
| CN218115020U (en) * | 2022-07-29 | 2022-12-23 | 四川金星清洁能源装备股份有限公司 | Natural gas hydrogen production system |
-
2022
- 2022-07-29 CN CN202210910236.3A patent/CN115159458B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106564861A (en) * | 2016-11-09 | 2017-04-19 | 华南理工大学 | Process for efficiently recovering reforming gas energy in hydrocarbon steam reforming hydrogen production process |
| CN207659077U (en) * | 2017-07-10 | 2018-07-27 | 杭州普菲科空分设备有限公司 | A kind of natural gas reforming hydrogen manufacturing device |
| CN213231512U (en) * | 2020-09-07 | 2021-05-18 | 重庆金苏化工有限公司 | Natural gas hydrogen production medium temperature shift system |
| CN113213425A (en) * | 2021-06-08 | 2021-08-06 | 金川集团股份有限公司 | System and method for preparing hydrogen by using natural gas |
| CN114014270A (en) * | 2021-12-10 | 2022-02-08 | 四川天采科技有限责任公司 | Modularized natural gas reforming hydrogen production machine and hydrogen production method thereof |
| CN218115020U (en) * | 2022-07-29 | 2022-12-23 | 四川金星清洁能源装备股份有限公司 | Natural gas hydrogen production system |
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