CN112811389A - Movable intensive type marine instant hydrogen production and hydrogenation integrated system - Google Patents
Movable intensive type marine instant hydrogen production and hydrogenation integrated system Download PDFInfo
- Publication number
- CN112811389A CN112811389A CN202110228512.3A CN202110228512A CN112811389A CN 112811389 A CN112811389 A CN 112811389A CN 202110228512 A CN202110228512 A CN 202110228512A CN 112811389 A CN112811389 A CN 112811389A
- Authority
- CN
- China
- Prior art keywords
- hydrogen
- pipeline
- discharge end
- feed end
- container
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000001257 hydrogen Substances 0.000 title claims abstract description 356
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 356
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 351
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 76
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 69
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 317
- 239000000446 fuel Substances 0.000 claims abstract description 67
- 238000006356 dehydrogenation reaction Methods 0.000 claims abstract description 63
- 238000011049 filling Methods 0.000 claims abstract description 51
- 238000000746 purification Methods 0.000 claims abstract description 38
- 238000010248 power generation Methods 0.000 claims abstract description 29
- 150000002431 hydrogen Chemical class 0.000 claims abstract description 12
- 238000003860 storage Methods 0.000 claims description 79
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 claims description 63
- 239000007789 gas Substances 0.000 claims description 63
- 238000003795 desorption Methods 0.000 claims description 31
- 239000007788 liquid Substances 0.000 claims description 26
- 239000002994 raw material Substances 0.000 claims description 16
- 230000003197 catalytic effect Effects 0.000 claims description 15
- 239000006200 vaporizer Substances 0.000 claims description 15
- 239000002608 ionic liquid Substances 0.000 claims description 14
- 238000001179 sorption measurement Methods 0.000 claims description 12
- 230000001105 regulatory effect Effects 0.000 claims description 11
- 238000011084 recovery Methods 0.000 claims description 6
- 235000019441 ethanol Nutrition 0.000 description 96
- 239000012071 phase Substances 0.000 description 25
- 239000007791 liquid phase Substances 0.000 description 11
- 239000000203 mixture Substances 0.000 description 11
- 239000000047 product Substances 0.000 description 11
- 238000000034 method Methods 0.000 description 10
- 239000003054 catalyst Substances 0.000 description 8
- 235000011054 acetic acid Nutrition 0.000 description 7
- 239000012535 impurity Substances 0.000 description 6
- 238000007084 catalytic combustion reaction Methods 0.000 description 5
- 238000001816 cooling Methods 0.000 description 5
- 239000002912 waste gas Substances 0.000 description 5
- 238000002485 combustion reaction Methods 0.000 description 4
- 230000001276 controlling effect Effects 0.000 description 4
- 238000011010 flushing procedure Methods 0.000 description 4
- 230000008016 vaporization Effects 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 238000005429 filling process Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 239000013589 supplement Substances 0.000 description 3
- 238000009834 vaporization Methods 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000005485 electric heating Methods 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 238000004146 energy storage Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 241001391944 Commicarpus scandens Species 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical group [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000003487 electrochemical reaction Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Images
Classifications
-
- 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
- C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63H—MARINE PROPULSION OR STEERING
- B63H21/00—Use of propulsion power plant or units on vessels
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D1/00—Pipe-line systems
- F17D1/02—Pipe-line systems for gases or vapours
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D1/00—Pipe-line systems
- F17D1/08—Pipe-line systems for liquids or viscous products
- F17D1/14—Conveying liquids or viscous products by pumping
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D3/00—Arrangements for supervising or controlling working operations
- F17D3/01—Arrangements for supervising or controlling working operations for controlling, signalling, or supervising the conveyance of a product
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63H—MARINE PROPULSION OR STEERING
- B63H21/00—Use of propulsion power plant or units on vessels
- B63H2021/003—Use of propulsion power plant or units on vessels the power plant using fuel cells for energy supply or accumulation, e.g. for buffering photovoltaic energy
-
- 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
- C01B2203/0266—Processes for making hydrogen or synthesis gas containing a decomposition step
- C01B2203/0277—Processes for making hydrogen or synthesis gas containing a decomposition step containing a catalytic decomposition step
-
- 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
-
- 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
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0833—Heating by indirect heat exchange with hot fluids, other than combustion gases, product gases or non-combustive exothermic reaction product gases
-
- 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
- C01B2203/12—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
- C01B2203/1217—Alcohols
- C01B2203/1229—Ethanol
-
- 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
- Y02E60/34—Hydrogen distribution
-
- 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
- Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
- Y02T70/00—Maritime or waterways transport
- Y02T70/50—Measures to reduce greenhouse gas emissions related to the propulsion system
-
- 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
- Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
- Y02T70/00—Maritime or waterways transport
- Y02T70/50—Measures to reduce greenhouse gas emissions related to the propulsion system
- Y02T70/5218—Less carbon-intensive fuels, e.g. natural gas, biofuels
- Y02T70/5236—Renewable or hybrid-electric solutions
-
- 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
- Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
- Y02T90/00—Enabling technologies or technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02T90/40—Application of hydrogen technology to transportation, e.g. using fuel cells
Abstract
The invention relates to the technical field of hydrogen fuel cell ships, in particular to a mobile intensive type marine instant hydrogen production and hydrogenation integrated system. The container comprises a container, wherein a first container compartment, a second container compartment, a third container compartment and a fourth container compartment are respectively arranged in the container, a photovoltaic power generation unit is arranged on the container, an ethanol dehydrogenation hydrogen production unit is arranged in the second container compartment, a hydrogen purification unit is arranged in the third container compartment, and a hydrogen filling unit is arranged in the fourth container compartment. The invention can realize the mobility supply of the hydrogen fuel cell ship by installing the movable intensive type marine instant hydrogen production and hydrogenation integrated system on the guarantee ship deck and utilizing the 'current production and use' of hydrogen, thereby avoiding the hydrogen fuel cell ship from frequently returning to and fixing a port base to supply hydrogen and improving the working efficiency of the hydrogen fuel cell ship.
Description
Technical Field
The invention relates to the technical field of hydrogen fuel cell ships, in particular to a mobile intensive type marine instant hydrogen production and hydrogenation integrated system.
Background
High emissions and oil leakage in the shipping industry have become one of the serious problems threatening the global ecology. In order to reduce global ship emission, a clean, efficient and sustainable new energy power propulsion technology needs to be researched, so that a novel green ship is developed to replace the existing fossil fuel ship.
The hydrogen energy is used as a clean and efficient secondary energy, has the characteristics of wide source, high combustion heat value, cleanness, no pollution, various utilization forms, energy storage and the like, and is considered to be one of ideal new energy sources for ships with the most development potential at the present stage.
The hydrogen fuel cell is used as a new green energy power device, hydrogen is used as fuel, chemical energy in the hydrogen fuel can be directly converted into electric energy through electrochemical reaction, and a reaction product is water.
Before the hydrogen is used up, the hydrogen fuel cell ship needs to return to a fixed port support base for hydrogen supply in order to prevent 'anchor drop' midway, and the shipping range is greatly limited. At the present stage, the problems of the lack of hydrogen storage and hydrogenation infrastructure matched with the hydrogen fuel cell for the ship, the storage and transportation safety of the hydrogen fuel for the ship, the supply convenience of the hydrogen fuel for the ship and the like become the bottleneck of the popularization and development of the hydrogen fuel cell ship.
Due to the special safety of hydrogen (flammability, explosiveness, easy leakage), the requirements for hydrogen fuel storage and transportation, filling and supply are particularly high. The hydrogen storage mode is various, and the commercialized popularization and application mainly include high-pressure gaseous hydrogen storage and liquid hydrogen storage.
The high-pressure gaseous hydrogen storage technology is a main hydrogen storage and supply mode of a commercial vehicle hydrogen supply station at the present stage, and particularly relates to a method for filling hydrogen into a fuel cell vehicle needing to be supplied by transporting a high-pressure large-capacity gaseous hydrogen storage cylinder group (20MP or 45MPa) as a hydrogen source through a long-tube trailer and performing secondary pressurization. At present, in the field of ships, a large-capacity high-pressure gaseous hydrogen storage cylinder group arranged on a ship is not directly adopted to store hydrogen and is used as a mobile marine supply hydrogen source to fill hydrogen into a hydrogen fuel cell ship.
The use of liquid hydrogen for shipping hydrogen (liquid hydrogen storage) is an effective way for shipping hydrogen fuel on a large scale worldwide, and has the advantages of large capacity, long-distance transportation and the like. However, liquid hydrogen needs to be stored at the temperature of-253 ℃, and the processes of liquefaction, vaporization and the like are needed during production and use, so that supporting facilities are complex, a large amount of energy is wasted, and the cost is high. Meanwhile, the requirement on liquid hydrogen heat insulation is high, the condition of-253 ℃ is always kept in the hydrogen storage tank in the transportation process, and the liquid hydrogen storage tank is easy to break under the continuous impact and swing environment when a ship runs, so that the liquid hydrogen is quickly evaporated, the hydrogen explosion danger exists, and the safety of crews and containers is endangered. Therefore, the safety design and manufacturing requirements for the liquid hydrogen transport ship are particularly high. If the liquid hydrogen transport ship is directly used as a mobile marine hydrogen supply source for hydrogen filling for the hydrogen fuel cell ship, the supporting facilities are complex, and the long-distance transportation safety is low.
Disclosure of Invention
The applicant provides a mobile intensive type marine instant hydrogen production and hydrogenation integrated system aiming at the defects in the prior art, and particularly, a photovoltaic power generation unit, an ethanol dehydrogenation hydrogen production unit, a hydrogen purification unit and a hydrogen filling unit are highly integrated and installed on a guarantee ship deck in a container to form a mobile marine hydrogen supply system, so that the 'current production and use' of hydrogen are realized, excessive transformation on the structure of the existing guarantee ship container and a power supply and distribution system is not needed, the photovoltaic power generation provides electric energy for the system, ethanol with high hydrogen storage capacity and safety and stability is used as a hydrogen source, and hydrogen filling and supply are carried out on a hydrogen fuel cell ship through the steps of ethanol dehydrogenation hydrogen production, purification, filling and the like; meanwhile, the ethyl acetate product after the hydrogen production by ethanol dehydrogenation is a high-economic-value chemical product and can be directly recycled; in addition, by means of heat recycling, waste gas catalytic combustion and the like, the energy utilization efficiency of the system can be improved, and meanwhile, no waste gas emission of the system can be realized.
The technical scheme adopted by the invention is as follows:
the integrated system comprises a container, wherein a first container compartment, a second container compartment, a third container compartment and a fourth container compartment are respectively arranged in the container, a photovoltaic power generation unit is arranged on the container and comprises a plurality of photovoltaic power generation devices arranged on the upper surface of the container, the photovoltaic power generation devices are electrically connected with a photovoltaic controller arranged in the first container compartment, and the photovoltaic controller is electrically connected with a storage battery arranged in the first container compartment; an ethanol dehydrogenation hydrogen production unit is arranged in the second container compartment, a hydrogen purification unit is arranged in the third container compartment, and a hydrogen filling unit is arranged in the fourth container compartment; the storage battery is respectively and electrically connected with the first controller, the second controller and the third controller, the first controller, the second controller and the third controller are respectively arranged in the second container compartment, the third container compartment and the fourth container compartment, the first controller is electrically connected with the ethanol dehydrogenation hydrogen production unit, the second controller is electrically connected with the hydrogen purification unit, and the third controller is electrically connected with the hydrogen filling unit;
the ethanol dehydrogenation hydrogen production unit comprises an ethanol raw material storage tank, wherein the discharge end of the ethanol raw material storage tank is connected with the feed end of a conveying pump through a pipeline, the feed end of the conveying pump is connected with the feed end of a preheater through a pipeline, the discharge end of the preheater is connected with the feed end of an ethanol vaporizer through a pipeline, the discharge end of the ethanol vaporizer is connected with the first feed end of a heat exchanger through a pipeline, the first discharge end of the heat exchanger is connected with the feed end of an ethanol dehydrogenation hydrogen production reactor through a pipeline, the discharge end of the ethanol dehydrogenation hydrogen production reactor is connected with the second feed end of the heat exchanger through a pipeline, the second discharge end of the heat exchanger is connected with the feed end of a cooler through a pipeline;
the hydrogen purification unit comprises a hydrogen purification module, the hydrogen purification module comprises a plurality of pressure swing adsorption towers which are connected in series, the hydrogen discharge end of the hydrogen purification module is connected with the feed end of a dryer through a pipeline, the discharge end of the dryer is connected with the feed end of a filter through a pipeline, the discharge end of the filter is connected with the feed end of a one-way valve through a pipeline, and the discharge end of the one-way valve is connected with the feed end of a hydrogen buffer tank through a pipeline;
the hydrogen filling unit comprises an ionic liquid compressor, the feed end of the ionic liquid compressor is connected with the discharge end of a check valve through a pipeline, the feed end of the check valve is connected with the discharge end of a hydrogen buffer tank through a pipeline, the discharge end of the ionic liquid compressor is connected with the feed end of a dryer through a pipeline, the discharge end of the dryer is connected with the feed end of a filter through a pipeline, the discharge end of the filter is connected with the feed end of a cooler through a pipeline, the discharge end of the cooler is connected with the feed end of a mass flow meter through a pipeline, the discharge end of the mass flow meter is connected with the feed end of a flow regulating valve through a pipeline.
Further, a flame detector and a hydrogen detector are arranged in the first container compartment, the second container compartment, the third container compartment and the fourth container compartment.
Further, the first discharge end of the gas-liquid separator is connected with the feed end of the ethyl acetate recovery tank through a pipeline.
Further, the desorption gas discharge end of the hydrogen purification module is connected with the desorption gas check valve feed end through a pipeline, the desorption gas check valve discharge end is connected with the desorption gas buffer tank feed end through a pipeline, the desorption gas buffer tank discharge end is connected with the desorption gas switch valve feed end through a pipeline, the desorption gas switch valve discharge end is connected with the first feed end of the hydrogen catalytic combustor through a pipeline, the first discharge end of the hydrogen catalytic combustor is connected with the second feed end of the ethanol dehydrogenation reactor through a pipeline, and the second feed end of the hydrogen catalytic combustor is connected with the air compressor discharge end through a pipeline.
Furthermore, an emptying valve and a vacuum pump are arranged on a pipeline between the mass flow meter and the flow regulating valve.
Further, the container is arranged on the ship.
Further, the container is arranged on the port wharf.
Furthermore, the discharge end of the hydrogen filling unit is connected with the feed end of the hydrogen fuel storage device through a pipeline, and the discharge end of the hydrogen fuel storage device is connected with the ground hydrogenation gun through a pipeline.
Further, hydrogen fuel storage device includes hydrogen fuel storage module, and hydrogen fuel storage module includes a plurality of series connection's high-pressure storage tank, and hydrogen fuel storage module discharge end passes through pipe connection ground hydrogenation rifle, and hydrogen fuel storage module feed end passes through the pipe connection check valve discharge end, and the check valve feed end passes through the pipe connection bypass valve discharge end, and the bypass valve feed end passes through the discharge end of pipe connection hydrogen filling unit.
The invention has the following beneficial effects:
1. the invention provides a system for supplying hydrogen fuel to a hydrogen fuel cell ship, which can realize the mobility supply of the hydrogen fuel cell ship by installing a mobile intensive type marine instant hydrogen production and hydrogenation integrated system on a guarantee ship deck and utilizing the 'current production and use' of hydrogen, thereby avoiding the hydrogen fuel cell ship from frequently returning to and fixing a port base for hydrogen supply and improving the working efficiency of the hydrogen fuel cell ship;
2. according to the invention, the photovoltaic power generation unit, the ethanol dehydrogenation hydrogen production unit, the hydrogen purification unit, the hydrogen filling unit and other equipment are highly integrated on the container, and the power generation, energy storage, hydrogen production, hydrogen storage and hydrogenation are integrated to form a movable intensive marine hydrogen supply system. Meanwhile, the system is arranged on a guarantee ship deck, so that an open space is ensured in the hydrogen filling process, and the safety is improved;
3. the photovoltaic power generation unit is arranged at the outer top of the container to provide energy for a hydrogen supply system, excessive electric energy is stored by utilizing the storage battery pack, the self-production and self-utilization of the electric energy are realized, and the power supply and distribution system of the existing support ship does not need to be modified. Meanwhile, the rich hydrogen desorption gas generated in the hydrogen adsorption and purification process is recovered by a catalytic combustion method, and the generated heat is directly supplied to the ethanol dehydrogenation hydrogen production reactor, so that the whole system is free of waste gas emission and is green and environment-friendly; the heat generated in the dehydrogenation reaction in the ethanol dehydrogenation hydrogen production reactor is recovered, so that the high-efficiency utilization of the energy of the whole system is realized;
4. the invention adopts absolute ethyl alcohol with higher hydrogen storage density as a hydrogen supply source on the sea or in the inland river, the hydrogen storage quantity is large, and the purity of the prepared hydrogen is high after purification; in a non-working state, the ethanol is stably and safely stored in a raw material storage tank on a ship in a liquid state for a long time, so that safe storage and transportation under the environments of sea surface (water surface) swing and impact of the ship can be ensured; under the working state, the hydrogen is prepared on line. In addition, after the absolute ethyl alcohol is used, the absolute ethyl alcohol is convenient for operators to quickly fill and supply, and the hydrogen storage and transportation cost is reduced; meanwhile, the product ethyl acetate after hydrogen production by ethanol dehydrogenation is a high-economic-value chemical product, can be directly recycled, and is economical and economical;
5. the invention can be installed on a support ship, sea islands, port shore bases and land hydrogenation stations to form a water-land multipurpose hydrogen energy supply network.
Drawings
FIG. 1 is a schematic view of the structure of the present invention.
FIG. 2 is a diagram of the structure of a photovoltaic power generation unit and an ethanol dehydrogenation hydrogen production unit.
Fig. 3 is a structural view of a hydrogen purification unit and a hydrogen filling unit of the present invention.
FIG. 4 is a block diagram of an embodiment of the present invention.
FIG. 5 is a diagram of a second embodiment of the present invention.
Wherein: 1. a container; 101. a first container compartment; 102. a second container compartment; 103. a third container compartment; 104. a fourth container compartment; 105. a flame detector; 106. a hydrogen gas detector; 2. a photovoltaic power generation unit; 201. a photovoltaic power generation device; 202. a photovoltaic controller; 203. a storage battery; 3. an ethanol dehydrogenation hydrogen production unit; 301. an ethanol raw material storage tank; 302. a delivery pump; 303. a preheater; 304. an ethanol vaporizer; 305. a heat exchanger; 306. an ethanol dehydrogenation hydrogen production reactor; 307. a cooler; 308. a gas-liquid separator; 309. an ethyl acetate recovery tank; 310. a first controller; 4. a hydrogen purification unit; 401. a pressure swing adsorption tower; 402. a dryer; 403. a filter; 404. a one-way valve; 405. a hydrogen buffer tank; 406. a desorption gas check valve; 407. a desorption gas buffer tank; 408. a desorption gas switch valve; 409. a hydrogen catalytic burner; 410. an air compressor; 411. a second controller; 5. a hydrogen filling unit; 501. a check valve; 502. an ionic liquid compressor; 503. a dryer; 504. a filter; 505. a cooler; 506. a mass flow meter; 507. a flow regulating valve; 508. a hydrogenation gun; 509. an atmospheric valve; 510. a vacuum pump; 511. a third controller; 6. a hydrogen fuel storage device; 601. a bypass valve; 602. a check valve; 603. a high pressure storage tank; 7. a ground hydrogenation gun; A. a vessel; B. a hydrogen-fueled marine vessel; C. a hydrogen-fueled vehicle.
Detailed Description
The following describes embodiments of the present invention with reference to the drawings.
As shown in fig. 1, the mobile intensive marine immediate hydrogen production and hydrogenation integrated system of the present invention mainly comprises a container 1, wherein a first container compartment 101, a second container compartment 102, a third container compartment 103 and a fourth container compartment 104 are respectively arranged in the container 1, and a flame detector 105 and a hydrogen detector 106 are respectively arranged in the first container compartment 101, the second container compartment 102, the third container compartment 103 and the fourth container compartment 104.
As shown in fig. 1 and 2, a photovoltaic power generation unit 2 is disposed on a container 1, the photovoltaic power generation unit 2 includes a plurality of photovoltaic power generation devices 201 disposed on an upper surface of the container 1, the plurality of photovoltaic power generation devices 201 are electrically connected to a photovoltaic controller 202 disposed in a first container compartment 101, and the photovoltaic controller 202 is electrically connected to a storage battery 203 disposed in the first container compartment 101. The photovoltaic power generation device 201 is used for converting solar energy into electric energy, and the photovoltaic controller 202 is used for transmitting the electric energy generated by the photovoltaic power generation device 201 to the storage battery 203 for storage, and meanwhile supplying power to an inverter load of the photovoltaic power generation device 201.
As shown in fig. 1, an ethanol dehydrogenation hydrogen production unit 3 is disposed in the second container compartment 102, a hydrogen purification unit 4 is disposed in the third container compartment 103, and a hydrogen filling unit 5 is disposed in the fourth container compartment 104.
As shown in fig. 1 to 3, the storage battery 203 is electrically connected to the first controller 310, the second controller 411 and the third controller 511, the first controller 310, the second controller 411 and the third controller 511 are respectively disposed in the second container compartment 102, the third container compartment 103 and the fourth container compartment 104, the first controller 310 is electrically connected to the ethanol dehydrogenation hydrogen production unit 3, the second controller 411 is electrically connected to the hydrogen purification unit 4, and the third controller 511 is electrically connected to the hydrogen filling unit 5.
As shown in fig. 2, the ethanol dehydrogenation hydrogen production unit 3 includes an ethanol raw material storage tank 301, a discharge end of the ethanol raw material storage tank 301 is connected to a feed end of a transfer pump 302 through a pipeline, a discharge end of the transfer pump 302 is connected to a feed end of a preheater 303 through a pipeline, a discharge end of the preheater 303 is connected to a feed end of an ethanol vaporizer 304 through a pipeline, a discharge end of the ethanol vaporizer 304 is connected to a first feed end of a heat exchanger 305 through a pipeline, a first discharge end of the heat exchanger 305 is connected to a feed end of an ethanol dehydrogenation hydrogen production reactor 306 through a pipeline, a discharge end of the ethanol dehydrogenation hydrogen production reactor 306 is connected to a second feed end of the heat exchanger 305 through a pipeline, a second discharge end of the heat exchanger 305 is connected to a feed end of a cooler 307 through a pipeline, a discharge end of the cooler 307 is connected to a feed end of a gas-liquid separator 308 through a pipeline, a first discharge end of the gas-liquid separator.
The ethanol raw material storage tank 301 stores liquid phase ethanol, the ethanol raw material storage tank 301 is provided with a liquid supplementing port, so that an operator can conveniently supplement absolute ethanol, and the ethanol raw material can be 95% ethanol or absolute ethanol. The preheater 303 includes an electric tracing device capable of preheating the liquid phase ethanol transferred from the ethanol raw material storage tank 301. The ethanol vaporizer 304 is used for vaporizing the vapor-liquid phase mixture ethanol delivered by the preheater 303 to form ethanol vapor. The heat exchanger 305 is used to recover heat from the product in the hydrogen purification unit 4 and reheat the steam generated from the ethanol vaporizer 304 to form superheated ethanol vapor. The ethanol dehydrogenation reactor 306 contains a catalyst reaction bed inside, the catalyst reaction bed is filled with a catalyst, and the catalyst is a copper-based catalyst. Under the high-temperature condition (220-300 ℃), the gas-phase ethanol is subjected to catalytic cracking by using a catalyst, an ethanol dehydrogenation reaction is carried out, a gas-phase mixture of hydrogen and ethyl acetate is generated, and the resultant directly enters a heat exchanger 305 for heat exchange. The heat required for the dehydrogenation reaction of ethanol is partly derived from the reactor body and partly derived from the hydrogen purification unit 4. The cooler 307 is used for further cooling the gas phase mixture of hydrogen and ethyl acetate after heat exchange in the heat exchanger 305. The gas-liquid separator 308 is configured to perform gas-liquid separation on the cooled mixture of hydrogen and ethyl acetate, to separate the mixture into gas-phase hydrogen and liquid-phase ethyl acetate, the gas-phase hydrogen in the gas-liquid separator 308 enters the hydrogen purification unit 4 through a pipeline, and the liquid-phase ethyl acetate in the gas-liquid separator 308 enters the ethyl acetate recovery tank 309 through a pipeline for storage.
As shown in fig. 3, the hydrogen purification unit 4 includes a hydrogen purification module, the hydrogen purification module includes a plurality of pressure swing adsorption towers 401 connected in series, the hydrogen discharge end of the hydrogen purification module is connected to the feed end of a dryer 402 through a pipeline, the discharge end of the dryer 402 is connected to the feed end of a filter 403 through a pipeline, the discharge end of the filter 403 is connected to the feed end of a check valve 404 through a pipeline, the discharge end of the check valve 404 is connected to the feed end of a hydrogen buffer tank 405 through a pipeline, and the discharge end of the hydrogen buffer tank 405 is connected to the hydrogen filling unit 5 through a pipeline. The desorption gas discharge end of the hydrogen purification module is connected with the feed end of a desorption gas check valve 406 through a pipeline, the discharge end of the desorption gas check valve 406 is connected with the feed end of a desorption gas buffer tank 407 through a pipeline, the discharge end of the desorption gas buffer tank 407 is connected with the feed end of a desorption gas switch valve 408 through a pipeline, the discharge end of the desorption gas switch valve 408 is connected with the first feed end of a hydrogen catalytic combustor 409 through a pipeline, and the first discharge end of the hydrogen catalytic combustor 409 is connected with the second feed end of the ethanol dehydrogenation reactor 306 through a pipeline. The second feeding end of the hydrogen catalytic burner 409 is connected with the discharging end of the air compressor 410 through a pipeline.
The pressure swing adsorption tower 401 is used for purifying gas-phase hydrogen, separating impurities contained in the hydrogen, separating the gas-phase hydrogen generated in the ethanol dehydrogenation hydrogen production unit 3 into hydrogen and desorbed gas (hydrogen-rich gas), discharging the impurities and the desorbed gas together, and purifying the hydrogen by the pressure swing adsorption tower 401 to obtain the hydrogen with the purity of more than or equal to 99.99%. The dryer 402 is used to dry the purified hydrogen gas, and the filter 403 is used to filter the dried hydrogen gas. The hydrogen buffer tank 405 is used to buffer and store the purified hydrogen. When the system stops working, the desorption gas check valve 406 can prevent desorption gas from flowing backwards under the back pressure. The desorption gas buffer tank 407 is used for buffering and storing desorption gas. The desorption gas switch valve 408 is used for controlling the on-off of the desorption gas conveying pipeline. The hydrogen catalytic combustor 409 mixes and combusts the desorbed gas delivered from the desorbed gas buffer tank 407 and the air delivered from the air compressor 410 through catalytic combustion, and the heat generated by combustion is recycled to the ethanol dehydrogenation reactor 306.
As shown in fig. 3, the hydrogen filling unit 5 includes an ionic liquid compressor 502, a feed end of the ionic liquid compressor 502 is connected to a discharge end of the check valve 501 through a pipeline, and a feed end of the check valve 501 is connected to a discharge end of the hydrogen buffer tank 405 through a pipeline. The discharge end of the ionic liquid compressor 502 is connected with the feed end of the dryer 503 through a pipeline, the discharge end of the dryer 503 is connected with the feed end of the filter 504 through a pipeline, the discharge end of the filter 504 is connected with the feed end of the cooler 505 through a pipeline, the discharge end of the cooler 505 is connected with the feed end of the mass flow meter 506 through a pipeline, the discharge end of the mass flow meter 506 is connected with the feed end of the flow regulating valve 507 through a pipeline, and the discharge end of the flow regulating valve 507 is connected with the hydrogenation gun 508 through a. An air release valve 509 and a vacuum pump 510 are arranged on a pipeline between the mass flow meter 506 and the flow regulating valve 507.
The ionic liquid compressor 502 is used to pressurize the hydrogen gas exiting the hydrogen buffer tank 405. The dryer 503 and the filter 504 respectively dry and filter the pressurized hydrogen gas, and the cooler 505 is used for cooling the high-pressure hydrogen to below-20 ℃. The mass flow meter 506 is used for metering the amount of the supplied hydrogen, and the flow regulating valve 507 is used for controlling the hydrogen flow and the hydrogenation speed. The hydrogenation lance 508 is used to connect to the hydrogen fuel cell marine hydrogenation port to be replenished. The emptying valve 509 is used for emptying and emptying the hydrogenation pipeline, so that the safety of the hydrogenation pipeline is protected. The vacuum pump 510 is used to evacuate the hydrogen fill line.
An application example of the mobile intensive marine instant hydrogen production and hydrogenation integrated system is shown in fig. 4, wherein a container 1 of the mobile intensive marine instant hydrogen production and hydrogenation integrated system is arranged on a ship a to serve as a mobile marine hydrogenation station, a hydrogen fuel ship B needing hydrogen fuel supplement is driven to the side of the ship a, and then a hydrogenation gun 508 of the mobile intensive marine instant hydrogen production and hydrogenation integrated system is inserted into a hydrogenation port of the hydrogen fuel ship B to perform hydrogen fuel supplement.
When a mobile marine hydrogenation station is adopted for hydrogenation, the whole using process is as follows:
(1) and (3) installation: the container 1 is directly placed on a deck A of the security ship by hoisting, and a connecting piece at the bottom of the container can be directly and fixedly connected with a connecting piece pre-embedded in the deck A of the security ship;
(2) and power generation: the photovoltaic power generation device 201 arranged on the outer top of the container 1 comprises a plurality of groups of array photovoltaic panels and is used for converting solar energy into electric energy, the electricity generated by the photovoltaic power generation device 201 is transmitted to the storage battery 203 through the photovoltaic controller 202 to be stored, and the electric energy is provided for the ethanol dehydrogenation hydrogen production unit module 3, the hydrogen purification unit 4 and the hydrogen filling unit 5;
(3) and vacuumizing: in order to ensure the safety of hydrogen filling, the hydrogen filling unit 5 and the hydrogen buffer tank 405 should be evacuated before the system is started, and air and gas impurities in the pipeline and the hydrogen buffer tank are removed. And closing the check valve 404 and the emptying valve C, sequentially opening the check valve 501, finally opening the vacuum pump 14, extracting impurities in the pipeline, and indicating that the vacuum degree in the pipeline of the hydrogen filling unit 5 and the hydrogen buffer tank 405 reaches-0.1 MPa when the reading of a pressure sensor of the outlet pipeline of the vacuum pump shows-0.1 MPa. The vacuum pump 510 is closed, the one-way valves 404 are opened in sequence, and the vacuumizing is finished;
(4) and a hydrogenation gun is connected: a hydrogenation gun 508 outside the container is connected with a hydrogenation port of a fuel cell ship B to be supplied with hydrogen through a metal hose to prepare for hydrogen filling;
(5) and starting the system: starting a system, wherein a liquid phase raw material ethanol flows into a preheater 303 from an output port of a raw material storage tank 301 for storing ethanol through a pipeline by the operation of a delivery pump 302, forms an ethanol gas-liquid mixture through electric heating, flows into an ethanol vaporizer 304 through the pipeline for further vaporization to form gas phase ethanol, and enters an ethanol dehydrogenation hydrogen production reactor 306;
a heat exchanger 305 is arranged between the ethanol dehydrogenation hydrogen production reactor 306 and the ethanol vaporizer 304, the heat conducting medium flowing in the heat exchanger 305 is gas phase ethanol flowing out of the ethanol vaporizer 304, and the heat conducting medium is a mixture of product high temperature gas phase hydrogen and ethyl acetate flowing out of the ethanol dehydrogenation hydrogen production reactor 306. Specifically, a high-temperature outlet of the heat exchanger 305 is connected with an inlet of the ethanol dehydrogenation hydrogen production reactor 306 through a pipeline, a high-temperature inlet of the heat exchanger 305 is connected with an outlet of the ethanol dehydrogenation hydrogen production reactor 306 through a pipeline, and a low-temperature outlet of the heat exchanger 305 is connected with a cooler 307 through a pipeline;
the gas phase ethanol entering the ethanol dehydrogenation hydrogen production reactor 306 is catalytically decomposed under the condition of a high-temperature catalyst, and the product is a mixture of high-temperature gas phase hydrogen and ethyl acetate. The product is cooled by heat exchange in a heat exchanger 305 and cooled in a cooler 307, and then sent to a gas-liquid separator 308 to be separated into gas-phase hydrogen and liquid-phase ethyl acetate, and the liquid-phase ethyl acetate is sent back to a storage ethyl acetate recovery tank 309. The gas-phase hydrogen is sent to the hydrogen purification unit 4;
the method comprises the following steps that the ethanol dehydrogenation reactor 306 can maintain gas phase ethanol for dehydrogenation reaction at 220-300 ℃, so that part of heat of the ethanol dehydrogenation reactor 306 is removed from heat conveyed by a hydrogen catalytic combustor 409 in a burning manner, and a heating device is arranged outside the ethanol dehydrogenation reactor 306 and is an electric heater;
the gas-phase hydrogen delivered from the gas-liquid separator 308 enters a pressure swing adsorption tower 401, and is subjected to adsorption, pressure equalization, reverse discharge, forward discharge, flushing, pressure boosting and other steps to generate hydrogen with the purity of more than or equal to 99.99%, and then the hydrogen is dried by a dryer 402, filtered by a filter 403 and delivered to a hydrogen buffer tank 405 through a one-way valve 404;
hydrogen-rich desorbed gas generated in the reverse release and flushing processes flows into a desorbed gas buffer tank 407 through a desorbed gas check valve 406, after the gas is stabilized, a desorbed gas switch valve 408 is opened, the hydrogen-rich desorbed gas is conveyed to a hydrogen catalytic combustor 409 to be mixed with air from an air compressor 410 to generate catalytic combustion, and heat generated by combustion is recycled to the ethanol dehydrogenation hydrogen production reactor 306, so that no waste gas is discharged in the whole ethanol dehydrogenation hydrogen production process;
(6) and hydrogen filling: compressing and pressurizing high-quality hydrogen in a hydrogen buffer tank 405 by an ionic liquid compressor 502, drying by a dryer 503, filtering by a filter 504, cooling to the temperature below-20 ℃ by a cooler 505, adjusting a flow regulating valve 507, controlling the hydrogenation speed, opening a hydrogenation gun 508, and filling the hydrogen to be supplemented to a hydrogen fuel cell ship B by the hydrogenation gun 508;
(7) and closing the system: during the hydrogen filling process, the total hydrogen filling amount is monitored and measured by the mass flow meter 506, and whether the hydrogen filling process is completed or not is judged. After the required total hydrogen filling amount is reached, a breaking valve in the hydrogenation gun 508 is opened, the hydrogenation gun is closed, and the hydrogen filling unit 5, the ethanol dehydrogenation hydrogen production unit 4 and the hydrogen purification unit 3 are closed in sequence.
(8) And leaving the support ship: the whole hydrogen filling work is completed, and the hydrogen fuel cell ship B leaves the guarantee ship A.
Fig. 5 shows an application example of the mobile intensive marine instant hydrogen production and hydrogenation integrated system, wherein a container 1 of the mobile intensive marine instant hydrogen production and hydrogenation integrated system is arranged on a port wharf and used as a fixed hydrogenation station for hydrogenation.
In order to store and fill hydrogen fuel in a port and a wharf conveniently, the discharge end of a hydrogen filling unit 5 of the intensive marine instant hydrogen production and hydrogenation integrated system is connected with the feed end of a hydrogen fuel storage device 6 through a pipeline, the discharge end of the hydrogen fuel storage device 6 is connected with a ground hydrogenation gun 7 through a pipeline, and the intensive marine instant hydrogen production and hydrogenation integrated system can fill hydrogen gas into a hydrogen fuel vehicle C on the land or a hydrogen fuel ship B on the sea through the ground hydrogenation gun 7 and can also directly fill hydrogen gas into the hydrogen fuel vehicle C on the land or the hydrogen fuel ship B on the sea through a hydrogenation gun 508 of the hydrogen filling unit 5.
As shown in fig. 5, the hydrogen fuel storage device 6 includes a hydrogen fuel storage module, the hydrogen fuel storage module includes a plurality of high-pressure storage tanks 603 connected in series, the discharge end of the hydrogen fuel storage module is connected to the ground hydrogenation gun 7 through a pipeline, the feed end of the hydrogen fuel storage module is connected to the discharge end of the check valve 602 through a pipeline, the feed end of the check valve 602 is connected to the discharge end of the bypass valve 601 through a pipeline, and the feed end of the bypass valve 601 is connected to the discharge end of the hydrogen filling unit 5 through a pipeline.
When a fixed hydrogenation station is adopted for hydrogenation, the whole using process is as follows:
(1) and (3) installation: the container 1 is placed in the fixed hydrogenation station A of the port base by hoisting, and the bottom connecting piece of the container can be directly and fixedly connected with the connecting piece of the fixed hydrogenation station B of the port base.
(2) And power generation: the photovoltaic power generation device 201 arranged on the outer top of the container 1 comprises a plurality of groups of array photovoltaic panels and is used for converting solar energy into electric energy, the electricity generated by the photovoltaic power generation device 201 is transmitted to the storage battery 203 for storage through the photovoltaic controller 202, and the electric energy is provided for the ethanol dehydrogenation hydrogen production unit module 3, the hydrogen adsorption and purification unit module 4 and the hydrogen filling unit module 5;
(3) and vacuumizing: in order to ensure the safety of hydrogen filling, the hydrogen filling unit 5 and the hydrogen buffer tank 405 should be evacuated before the system is started, and air and gas impurities in the pipeline and the hydrogen buffer tank are removed. And closing the check valve 404 and the emptying valve C, sequentially opening the check valve 501, finally opening the vacuum pump 14, extracting impurities in the pipeline, and indicating that the vacuum degree in the pipeline of the hydrogen filling unit 5 and the hydrogen buffer tank 405 reaches-0.1 MPa when the reading of a pressure sensor of the outlet pipeline of the vacuum pump shows-0.1 MPa. The vacuum pump 510 is closed, the one-way valves 404 are opened in sequence, and the vacuumizing is finished;
(4) and a hydrogenation gun is connected: a hydrogenation gun 508 outside the container is connected with a hydrogenation port of a ship B to be supplied with hydrogen fuel through a metal hose to prepare for hydrogen filling;
(5) and starting the system: starting a system, wherein a liquid phase raw material ethanol flows into a preheater 303 from an output port of a raw material storage tank 301 for storing ethanol through a pipeline by the operation of a delivery pump 302, forms an ethanol gas-liquid mixture through electric heating, flows into an ethanol vaporizer 304 through the pipeline for further vaporization to form gas phase ethanol, and enters an ethanol dehydrogenation hydrogen production reactor 306;
a heat exchanger 305 is arranged between the ethanol dehydrogenation hydrogen production reactor 306 and the ethanol vaporizer 304, the heat conducting medium flowing in the heat exchanger 305 is gas phase ethanol flowing out of the ethanol vaporizer 304, and the heat conducting medium is a mixture of product high temperature gas phase hydrogen and ethyl acetate flowing out of the ethanol dehydrogenation hydrogen production reactor 306. Specifically, a high-temperature outlet of the heat exchanger 305 is connected with an inlet of the ethanol dehydrogenation hydrogen production reactor 306 through a pipeline, a high-temperature inlet of the heat exchanger 305 is connected with an outlet of the ethanol dehydrogenation hydrogen production reactor 306 through a pipeline, and a low-temperature outlet of the heat exchanger 305 is connected with a cooler 307 through a pipeline;
the gas phase ethanol entering the ethanol dehydrogenation hydrogen production reactor 306 is catalytically decomposed under the condition of a high-temperature catalyst, and the product is a mixture of high-temperature gas phase hydrogen and ethyl acetate. The product is cooled by heat exchange in a heat exchanger 305 and cooled in a cooler 307, and then sent to a gas-liquid separator 308 to be separated into gas-phase hydrogen and liquid-phase ethyl acetate, and the liquid-phase ethyl acetate is sent back to a storage ethyl acetate recovery tank 309. The gas-phase hydrogen is sent to the hydrogen purification unit 4;
the method comprises the following steps that the ethanol dehydrogenation reactor 306 can maintain gas phase ethanol for dehydrogenation reaction at 220-300 ℃, so that part of heat of the ethanol dehydrogenation reactor 306 is removed from heat conveyed by a hydrogen catalytic combustor 409 in a burning manner, and a heating device is arranged outside the ethanol dehydrogenation reactor 306 and is an electric heater;
the gas-phase hydrogen delivered from the gas-liquid separator 308 enters a pressure swing adsorption tower 401, and is subjected to adsorption, pressure equalization, reverse discharge, forward discharge, flushing, pressure boosting and other steps to generate hydrogen with the purity of more than or equal to 99.99%, and then the hydrogen is dried by a dryer 402, filtered by a filter 403 and delivered to a hydrogen buffer tank 405 through a one-way valve 404;
hydrogen-rich desorbed gas generated in the reverse release and flushing processes flows into a desorbed gas buffer tank 407 through a desorbed gas check valve 406, after the gas is stabilized, a desorbed gas switch valve 408 is opened, the hydrogen-rich desorbed gas is conveyed to a hydrogen catalytic combustor 409 to be mixed with air from an air compressor 410 to generate catalytic combustion, and heat generated by combustion is recycled to the ethanol dehydrogenation hydrogen production reactor 306, so that no waste gas is discharged in the whole ethanol dehydrogenation hydrogen production process;
(6) and filling the hydrogen into the high-pressure hydrogen storage tank of the fixed hydrogen filling station:
when hydrogen is not required to be directly filled into a hydrogen fuel ship or a fuel cell automobile, the bypass valve 601 and the check valve 602 are opened, high-quality hydrogen in the hydrogen buffer tank 405 is compressed and pressurized by the ionic liquid compressor 502, dried by the dryer 503 and filtered by the filter 504, cooled to below 20 ℃ below zero by the cooler 505, and directly conveyed to the high-pressure storage tank 603 of the fixed hydrogenation station for storage.
Step (7), hydrogen filling hydrogen fuel cell ship or automobile
And (3) driving the ship or the automobile with the hydrogen fuel cell to be replenished to a port, connecting a hydrogen filling port with a hydrogenation gun 508, compressing and pressurizing the high-quality hydrogen in the hydrogen buffer tank 405 in the step (5) by using an ionic liquid compressor 502, drying by using a dryer 503, cooling by using a filter 504, cooling to the temperature below minus 20 ℃ by using a cooler 505, adjusting a flow regulating valve 507, controlling the hydrogenation speed, and opening the hydrogenation gun 508 to fill the ship or the automobile with the hydrogen fuel cell to be replenished by using the hydrogenation gun 508. In addition, the hydrogen can be directly filled through the high-pressure hydrogen storage tank 603 of the fixed hydrogenation station.
(8) System shutdown
After the hydrogen filling of the high-pressure storage tank 603 of the fixed type hydrogen filling station is finished, the hydrogen filling unit 5, the ethanol dehydrogenation hydrogen production unit 4 and the hydrogen purification unit 3 are closed in sequence.
(9) Support ship leaving port base
The whole hydrogen filling work is completed, and the hydrogen fuel cell ship or the fuel cell automobile leaves the port base.
The above description is intended to be illustrative and not restrictive, and the scope of the invention is defined by the appended claims, which may be modified in any manner within the scope of the invention.
Claims (9)
1. The utility model provides a remove intensive marine instant hydrogen production hydrogenation integrated system, includes container (1), its characterized in that: a first container compartment (101), a second container compartment (102), a third container compartment (103) and a fourth container compartment (104) are respectively arranged in the container (1), a photovoltaic power generation unit (2) is arranged on the container (1), the photovoltaic power generation unit (2) comprises a plurality of photovoltaic power generation devices (201) arranged on the upper surface of the container (1), the photovoltaic power generation devices (201) are electrically connected with a photovoltaic controller (202) arranged in the first container compartment (101), and the photovoltaic controller (202) is electrically connected with a storage battery (203) arranged in the first container compartment (101); an ethanol dehydrogenation hydrogen production unit (3) is arranged in the second container compartment (102), a hydrogen purification unit (4) is arranged in the third container compartment (103), and a hydrogen filling unit (5) is arranged in the fourth container compartment (104); the storage battery (203) is electrically connected with the first controller (310), the second controller (411) and the third controller (511) respectively, the first controller (310), the second controller (411) and the third controller (511) are arranged in the second container compartment (102), the third container compartment (103) and the fourth container compartment (104) respectively, the first controller (310) is electrically connected with the ethanol dehydrogenation hydrogen production unit (3), the second controller (411) is electrically connected with the hydrogen purification unit (4), and the third controller (511) is electrically connected with the hydrogen filling unit (5);
the ethanol dehydrogenation hydrogen production unit (3) comprises an ethanol raw material storage tank (301), the discharge end of the ethanol raw material storage tank (301) is connected with the feed end of a conveying pump (302) through a pipeline, the discharge end of the conveying pump (302) is connected with the feed end of a preheater (303) through a pipeline, the discharge end of the preheater (303) is connected with the feed end of an ethanol vaporizer (304) through a pipeline, the discharge end of the ethanol vaporizer (304) is connected with the first feed end of a heat exchanger (305) through a pipeline, the first discharge end of the heat exchanger (305) is connected with the feed end of an ethanol dehydrogenation hydrogen production reactor (306) through a pipeline, the discharge end of the ethanol dehydrogenation hydrogen production reactor (306) is connected with the second feed end of the heat exchanger (305) through a pipeline, the second discharge end of the heat exchanger (305) is connected with the feed end of a cooler (307) through a pipeline, and the discharge end of the;
the hydrogen purification unit (4) comprises a hydrogen purification module, the hydrogen purification module comprises a plurality of pressure swing adsorption towers (401) which are connected in series, the hydrogen discharge end of the hydrogen purification module is connected with the feed end of a dryer (402) through a pipeline, the discharge end of the dryer (402) is connected with the feed end of a filter (403) through a pipeline, the discharge end of the filter (403) is connected with the feed end of a one-way valve (404) through a pipeline, and the discharge end of the one-way valve (404) is connected with the feed end of a hydrogen buffer tank (405) through a pipeline;
the hydrogen filling unit (5) comprises an ionic liquid compressor (502), the feed end of the ionic liquid compressor (502) is connected with the discharge end of a check valve (501) through a pipeline, the feed end of the check valve (501) is connected with the discharge end of a hydrogen buffer tank (405) through a pipeline, the discharge end of the ionic liquid compressor (502) is connected with the feed end of a dryer (503) through a pipeline, the discharge end of the dryer (503) is connected with the feed end of a filter (504) through a pipeline, the discharge end of the filter (504) is connected with the feed end of a cooler (505) through a pipeline, the discharge end of the cooler (505) is connected with the feed end of a mass flow meter (506) through a pipeline, the discharge end of the mass flow meter (506) is connected with the feed end of a flow regulating valve (507) through a pipeline, and the discharge end.
2. The mobile intensive marine immediate hydrogen production and hydrogenation integrated system of claim 1, wherein: a flame detector (105) and a hydrogen detector (106) are arranged in the first container compartment (101), the second container compartment (102), the third container compartment (103) and the fourth container compartment (104).
3. The mobile intensive marine immediate hydrogen production and hydrogenation integrated system of claim 1, wherein: the first discharge end of the gas-liquid separator (308) is connected with the feed end of the ethyl acetate recovery tank (309) through a pipeline.
4. The mobile intensive marine immediate hydrogen production and hydrogenation integrated system of claim 1, wherein: the desorption gas discharge end of the hydrogen purification module is connected with the feed end of a desorption gas check valve (406) through a pipeline, the discharge end of the desorption gas check valve (406) is connected with the feed end of a desorption gas buffer tank (407) through a pipeline, the discharge end of the desorption gas buffer tank (407) is connected with the feed end of a desorption gas switch valve (408) through a pipeline, the discharge end of the desorption gas switch valve (408) is connected with the first feed end of a hydrogen catalytic combustor (409) through a pipeline, the first discharge end of the hydrogen catalytic combustor (409) is connected with the second feed end of an ethanol dehydrogenation reactor (306) through a pipeline, and the second feed end of the hydrogen catalytic combustor (409) is connected with the discharge end of an air compressor (410) through a pipeline.
5. The mobile intensive marine immediate hydrogen production and hydrogenation integrated system of claim 1, wherein: and an air release valve (509) and a vacuum pump (510) are arranged on a pipeline between the mass flow meter (506) and the flow regulating valve (507).
6. The integrated system for instantly producing hydrogen and hydrogenating mobile intensive ships according to any one of claims 1 to 5, wherein the integrated system comprises: the container (1) is arranged on a ship.
7. The integrated system for instantly producing hydrogen and hydrogenating mobile intensive ships according to any one of claims 1 to 5, wherein the integrated system comprises: the container (1) is arranged on a port wharf.
8. The mobile intensive marine immediate hydrogen production and hydrogenation integrated system of claim 7, wherein: the discharge end of the hydrogen filling unit (5) is connected with the feed end of the hydrogen fuel storage device (6) through a pipeline, and the discharge end of the hydrogen fuel storage device (6) is connected with the ground hydrogenation gun (7) through a pipeline.
9. The mobile intensive marine immediate hydrogen production and hydrogenation integrated system of claim 8, wherein: the hydrogen fuel storage device (6) comprises a hydrogen fuel storage module, the hydrogen fuel storage module comprises a plurality of high-pressure storage tanks (603) connected in series, the discharge end of the hydrogen fuel storage module is connected with a ground hydrogenation gun (7) through a pipeline, the feed end of the hydrogen fuel storage module is connected with the discharge end of a check valve (602) through a pipeline, the feed end of the check valve (602) is connected with the discharge end of a bypass valve (601) through a pipeline, and the feed end of the bypass valve (601) is connected with the discharge end of a hydrogen filling unit (5) through a pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110228512.3A CN112811389A (en) | 2021-03-02 | 2021-03-02 | Movable intensive type marine instant hydrogen production and hydrogenation integrated system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110228512.3A CN112811389A (en) | 2021-03-02 | 2021-03-02 | Movable intensive type marine instant hydrogen production and hydrogenation integrated system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112811389A true CN112811389A (en) | 2021-05-18 |
Family
ID=75862713
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110228512.3A Pending CN112811389A (en) | 2021-03-02 | 2021-03-02 | Movable intensive type marine instant hydrogen production and hydrogenation integrated system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112811389A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115991455A (en) * | 2023-02-08 | 2023-04-21 | 杭州普菲科空分设备有限公司 | Multi-tower multi-section low-energy-consumption hydrogen production device and control system thereof |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20120325290A1 (en) * | 2011-06-27 | 2012-12-27 | Integrated Power Technology Corporation | Solar cogeneration vessel |
| CN107785596A (en) * | 2016-08-31 | 2018-03-09 | 北京亿华通科技股份有限公司 | Removable hydrogenation plant |
| CN108940150A (en) * | 2018-08-21 | 2018-12-07 | 北京国能中林科技开发有限公司 | A kind of self-heating dehydrogenation reactor system suitable for liquid hydrogen source material |
| CN109149744A (en) * | 2018-08-21 | 2019-01-04 | 北京国能中林科技开发有限公司 | A kind of hydrogen source material energy storage peak shaving system suitable for wind-force and photovoltaic power generation |
| CN110171804A (en) * | 2019-04-29 | 2019-08-27 | 上海电气集团股份有限公司 | A kind of hydrogen manufacturing purification integrated apparatus and application method |
| CN110654520A (en) * | 2019-09-26 | 2020-01-07 | 哈尔滨工程大学 | Ship direct-current networking system adopting fuel cell and ship applying same |
| CN210885288U (en) * | 2019-05-20 | 2020-06-30 | 广东国能中林实业有限公司 | Hydrogen oil filling system |
| CN111536418A (en) * | 2020-05-09 | 2020-08-14 | 中国船舶科学研究中心 | Heat self-recycling offshore alloy hydrogen storage replenishing system and method |
-
2021
- 2021-03-02 CN CN202110228512.3A patent/CN112811389A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20120325290A1 (en) * | 2011-06-27 | 2012-12-27 | Integrated Power Technology Corporation | Solar cogeneration vessel |
| CN107785596A (en) * | 2016-08-31 | 2018-03-09 | 北京亿华通科技股份有限公司 | Removable hydrogenation plant |
| CN108940150A (en) * | 2018-08-21 | 2018-12-07 | 北京国能中林科技开发有限公司 | A kind of self-heating dehydrogenation reactor system suitable for liquid hydrogen source material |
| CN109149744A (en) * | 2018-08-21 | 2019-01-04 | 北京国能中林科技开发有限公司 | A kind of hydrogen source material energy storage peak shaving system suitable for wind-force and photovoltaic power generation |
| CN110171804A (en) * | 2019-04-29 | 2019-08-27 | 上海电气集团股份有限公司 | A kind of hydrogen manufacturing purification integrated apparatus and application method |
| CN210885288U (en) * | 2019-05-20 | 2020-06-30 | 广东国能中林实业有限公司 | Hydrogen oil filling system |
| CN110654520A (en) * | 2019-09-26 | 2020-01-07 | 哈尔滨工程大学 | Ship direct-current networking system adopting fuel cell and ship applying same |
| CN111536418A (en) * | 2020-05-09 | 2020-08-14 | 中国船舶科学研究中心 | Heat self-recycling offshore alloy hydrogen storage replenishing system and method |
Non-Patent Citations (1)
| Title |
|---|
| 蒋玉岭等: "制氢系统解吸气回收利用探讨", 《冶金动力》 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115991455A (en) * | 2023-02-08 | 2023-04-21 | 杭州普菲科空分设备有限公司 | Multi-tower multi-section low-energy-consumption hydrogen production device and control system thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US11929530B2 (en) | Hydrated magnesium hydride energy system | |
| CN111170273B (en) | Combined cooling, heating and power supply system and power supply method based on ammonia energy ship | |
| JP6243357B2 (en) | Methods and systems for energy conversion and generation | |
| US6918430B2 (en) | Onboard hydrogen storage unit with heat transfer system for use in a hydrogen powered vehicle | |
| JP6506468B2 (en) | Dehydrogenation reaction system of liquid hydrogen source material | |
| CN101538010B (en) | System for decomposing ammonia to prepare hydrogen on the basis of after heat of heat engine gas exhaust | |
| WO2019204857A1 (en) | Offshore energy generation system | |
| US20030121481A1 (en) | Fuel system | |
| CN104265512A (en) | High-pressure/low-pressure gas supply system of ship power plant | |
| CN212356521U (en) | Combined cooling heating and power system based on ammonia energy ship | |
| JP2003040601A (en) | Method for supplying hydrogen | |
| US20070289882A1 (en) | Apparatus for refueling on-board metal hydride hydrogen storage tank | |
| CN204060975U (en) | A kind of high voltage/low voltage fuel gas supply system of Ship Power Equipment | |
| CN113224357A (en) | Hydrogen reaction system is stored in circulation | |
| CN104803351A (en) | Hydrogen production device and process for hydrogen refueling station | |
| CN112811389A (en) | Movable intensive type marine instant hydrogen production and hydrogenation integrated system | |
| CN202812779U (en) | CNG (Compressed Natural Gas) pipe-bundle container | |
| CN112349926A (en) | Vehicle-mounted fuel cell system capable of being started quickly | |
| US20200182405A1 (en) | Refueling station for supplying energy carriers to vehicles | |
| RU2388118C1 (en) | Installation for electric energy generation from raw hydrocarbons | |
| CN113386936A (en) | Modularized hydrogen energy ship electric transmission power system and method | |
| CN112786934A (en) | Phosphoric acid fuel cell power system taking methanol as raw material and power generation method thereof | |
| US20110064647A1 (en) | Method for storage and transportation of hydrogen | |
| CN219713069U (en) | Hydrogenation ship | |
| CN214753863U (en) | Hydrogen reaction system is stored in circulation |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20210518 |
|
| RJ01 | Rejection of invention patent application after publication |