CN112239196B - Multi-heat source complementary hydrogen production device based on high-temperature heat pipe heat collection - Google Patents
Multi-heat source complementary hydrogen production device based on high-temperature heat pipe heat collection Download PDFInfo
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- CN112239196B CN112239196B CN202011113326.7A CN202011113326A CN112239196B CN 112239196 B CN112239196 B CN 112239196B CN 202011113326 A CN202011113326 A CN 202011113326A CN 112239196 B CN112239196 B CN 112239196B
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- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 94
- 239000001257 hydrogen Substances 0.000 title claims abstract description 94
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 86
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 49
- 230000000295 complement effect Effects 0.000 title claims abstract description 22
- 239000012530 fluid Substances 0.000 claims abstract description 87
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 86
- 238000004891 communication Methods 0.000 claims abstract description 84
- 238000003860 storage Methods 0.000 claims abstract description 37
- 238000000746 purification Methods 0.000 claims abstract description 19
- 239000000376 reactant Substances 0.000 claims abstract description 11
- 239000007788 liquid Substances 0.000 claims description 232
- 239000007789 gas Substances 0.000 claims description 66
- 238000010521 absorption reaction Methods 0.000 claims description 62
- 238000006243 chemical reaction Methods 0.000 claims description 42
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 39
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 25
- 238000000926 separation method Methods 0.000 claims description 15
- 238000001179 sorption measurement Methods 0.000 claims description 15
- 239000012528 membrane Substances 0.000 claims description 13
- 229910052763 palladium Inorganic materials 0.000 claims description 13
- 229910001338 liquidmetal Inorganic materials 0.000 claims description 10
- 238000005555 metalworking Methods 0.000 claims description 10
- 230000015572 biosynthetic process Effects 0.000 claims description 9
- 238000003786 synthesis reaction Methods 0.000 claims description 9
- 239000002994 raw material Substances 0.000 claims description 7
- 238000007789 sealing Methods 0.000 claims description 6
- 238000011049 filling Methods 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 3
- 238000004134 energy conservation Methods 0.000 abstract description 2
- 238000005286 illumination Methods 0.000 abstract description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 14
- 150000002431 hydrogen Chemical class 0.000 description 8
- 238000005213 imbibition Methods 0.000 description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 7
- 229910002092 carbon dioxide Inorganic materials 0.000 description 7
- 239000001569 carbon dioxide Substances 0.000 description 7
- 229910002091 carbon monoxide Inorganic materials 0.000 description 7
- 229930195733 hydrocarbon Natural products 0.000 description 5
- 150000002430 hydrocarbons Chemical class 0.000 description 5
- 239000004215 Carbon black (E152) Substances 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000005381 potential energy Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- 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
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- C—CHEMISTRY; METALLURGY
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- 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
- C01B3/48—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 followed by reaction of water vapour with carbon monoxide
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D15/00—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies
- F28D15/02—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes
- F28D15/04—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes with tubes having a capillary structure
- F28D15/046—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes with tubes having a capillary structure characterised by the material or the construction of the capillary structure
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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
- C01B2203/0405—Purification by membrane separation
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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
- C01B2203/042—Purification by adsorption on solids
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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
- C01B2203/047—Composition of the impurity the impurity being carbon monoxide
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- C—CHEMISTRY; METALLURGY
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- 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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- C01B2203/04—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
- C01B2203/048—Composition of the impurity the impurity being an organic compound
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- 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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- C01B2203/062—Hydrocarbon production, e.g. Fischer-Tropsch process
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- 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
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- 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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- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The invention discloses a multi-heat-source complementary hydrogen production device based on high-temperature heat pipe heat collection, which comprises feeding and preheating equipment, thermochemical hydrogen production equipment, heat exchange equipment, purification equipment and hydrogen storage equipment or synthetic oil and oil storage equipment, wherein a discharge pipe of the feeding and preheating equipment is in fluid communication with a feed pipe of the thermochemical hydrogen production equipment, a discharge pipe of the thermochemical hydrogen production equipment is in fluid communication with a feed pipe of the heat exchange equipment, and a discharge pipe of the heat exchange equipment is in fluid communication with a feed pipe of the purification equipment. According to the invention, the high-temperature heat pipe reactor is arranged, so that the utilization rate of a heat source can be improved, the reactant can be conveniently heated, the high-temperature heat pipe reactor adopts the disc-type condenser to supply heat, the consumption of traditional energy sources can be reduced, the purposes of energy conservation and emission reduction are achieved, meanwhile, the high-temperature heat pipe can supply heat through the methane burner, the heat can be conveniently supplied when sunlight illumination is insufficient, and the hydrogen production can be realized by uninterrupted operation.
Description
Technical Field
The invention relates to the technical field of multi-heat source complementary hydrogen production devices. In particular to a multi-heat source complementary hydrogen production device based on high-temperature heat pipe heat collection.
Background
Hydrogen energy is widely concerned as a clean alternative energy source due to its high energy density and clean combustion products;
the existing hydrogen production process has the main defects of high energy consumption and low purity that the high energy consumption causes high carbon emission and environmental pollution, and the reaction heat source has low utilization rate during hydrogen production, thereby causing certain energy waste.
Disclosure of Invention
Therefore, the technical problem to be solved by the invention is to provide a multi-heat-source complementary hydrogen production device based on high-temperature heat pipe heat collection, which reduces the hydrogen production energy consumption and improves the hydrogen purity.
In order to solve the technical problems, the invention provides the following technical scheme: the multi-heat-source complementary hydrogen production device based on high-temperature heat pipe heat collection comprises feeding and preheating equipment, thermochemical hydrogen production equipment, heat exchange equipment, purification equipment and hydrogen storage equipment, wherein a discharge pipe of the feeding and preheating equipment is in fluid communication with a feed pipe of the thermochemical hydrogen production equipment, a discharge pipe of the thermochemical hydrogen production equipment is in fluid communication with a feed pipe of the heat exchange equipment, a discharge pipe of the heat exchange equipment is in fluid communication with a feed pipe of the purification equipment, and a hydrogen outlet of the purification equipment is in fluid communication with a hydrogen inlet of the hydrogen storage equipment.
According to the multi-heat-source complementary hydrogen production device based on high-temperature heat pipe heat collection, the feeding and preheating equipment comprises a steam generator, gas preheating equipment and a methane gas source, a steam outlet of the steam generator is in fluid communication with a discharge pipe of the gas preheating equipment, and a gas outlet of the methane gas source is in fluid communication with a preheated gas inlet of the gas preheating equipment; and the discharge pipe of the gas preheating device is in fluid communication with the feed pipe of the thermochemical hydrogen production device.
According to the multi-heat-source complementary hydrogen production device based on high-temperature heat pipe heat collection, the thermochemical hydrogen production equipment comprises a high-temperature heat pipe reactor, a disc type condenser and a methane burner, focal spots of the disc type condenser are located on the outer surface of the high-temperature heat pipe reactor, and the methane burner supplies heat to the high-temperature heat pipe reactor at night or in rainy days; the gas supply port of the methane gas source is in fluid communication with the gas inlet of the methane burner; the discharge pipe of the gas preheating device is in fluid communication with the reactant inlet of the high temperature thermal tube reactor.
According to the multi-heat-source complementary hydrogen production device based on high-temperature heat pipe heat collection, the heat exchange equipment comprises a high-temperature water-vapor conversion device, a heat exchanger and a low-temperature water-vapor conversion device, a discharge pipe of the high-temperature water-vapor conversion device is in fluid communication with a feed pipe of the heat exchanger, and a discharge hole of the heat exchanger is in fluid communication with a feed hole of the low-temperature water-vapor conversion device; and a reactant outlet of the high-temperature thermal tube reactor is in fluid communication with a feed inlet of the high-temperature water-vapor conversion device.
The purification equipment comprises a gas-liquid separator, a first compressor, a PSA pressure swing adsorption device and a palladium membrane separation device, wherein a discharge pipe of the gas-liquid separator is in fluid communication with a feed inlet of the first compressor, a discharge hole of the first compressor is in fluid communication with a feed inlet of the PSA pressure swing adsorption device, and a discharge pipe of the PSA pressure swing adsorption device is in fluid communication with a feed pipe of the palladium membrane separation device; the discharging pipe of the low-temperature water-vapor conversion device is in fluid communication with the feeding pipe of the gas-liquid separator, and the liquid outlet of the gas-liquid separator is in fluid communication with the feeding hole of the steam generator.
According to the multi-heat-source complementary hydrogen production device based on high-temperature heat pipe heat collection, the hydrogen storage equipment comprises a second compressor and a hydrogen storage tank, and a discharge pipe of the second compressor is communicated with a fluid at an air inlet of the hydrogen storage tank; and a discharge pipe of the palladium membrane separation device is in fluid communication with a feed pipe of the second compressor.
According to the multi-heat-source complementary hydrogen production device based on high-temperature heat pipe heat collection, the waste heat steam outlet pipe of the heat exchanger is communicated with the steam turbine, and the power output end of the steam turbine is electrically connected with the power input ends of the first compressor and the second compressor respectively.
The heat exchange device comprises a first heat exchanger and a gas-liquid separator, a first discharge pipe of the first heat exchanger is in fluid communication with a feed pipe of the gas-liquid separator, a first feed pipe of the first heat exchanger is in fluid communication with a discharge pipe of the thermochemical hydrogen production device, and a liquid outlet of the gas-liquid separator is in fluid communication with a feed inlet of a steam generator; the purification equipment comprises a PSA device, and a feed pipe of the PSA device is in fluid communication with a discharge pipe of the gas-liquid separator; a discharge pipe of the PSA device is in fluid communication with a second feed pipe of the first heat exchanger; the methane gas outlet of the PSA device is in fluid communication with the feed pipe of the gas preheating equipment; the synthetic oil and oil storage equipment comprises a Fischer-Tropsch synthesis reactor, a second heat exchanger and an oil storage tank, wherein a discharge pipe of the Fischer-Tropsch synthesis reactor is in fluid communication with a feed pipe of the second heat exchanger, and a discharge pipe of the second heat exchanger is in fluid communication with a feed pipe of the oil storage tank; and the feeding pipe of the Fischer-Tropsch reaction synthesizer is in fluid communication with the second discharging pipe of the first heat exchanger.
The high-temperature thermal pipe reactor comprises a circular pipe-shaped high-temperature thermal pipe, a circular pipe-shaped thermochemical reactor and a liquid metal working medium positioned between the inner wall of the circular pipe-shaped high-temperature thermal pipe and the outer wall of the circular pipe-shaped thermochemical reactor, a liquid absorption core is formed on the outer wall of the circular tubular thermochemical reactor, the liquid absorption core comprises two or more than two segmented capillary liquid absorption rings, the segmented capillary liquid absorption rings are in a circular truncated cone shape, a capillary liquid suction groove is arranged on the outer side wall of the segmented capillary liquid suction ring along the direction parallel to the bus, the capillary liquid absorption grooves extend from the upper bottom surface of the segmented capillary liquid absorption ring to the lower bottom surface of the segmented capillary liquid absorption ring, the outer side wall of the segmented capillary liquid absorption ring between the adjacent capillary liquid absorption grooves is provided with a first capillary liquid absorption hole, the first capillary liquid sucking hole extends downwards obliquely towards the axial direction of the segmented capillary liquid sucking ring; a second capillary liquid suction hole is formed in one longitudinal side wall of the capillary liquid suction groove, and a third capillary liquid suction hole is formed in the other longitudinal side wall of the capillary liquid suction groove; the first capillary liquid sucking hole, the second capillary liquid sucking hole and the third capillary liquid sucking hole on the segmented capillary liquid sucking ring between the adjacent capillary liquid sucking grooves form a Y-shaped capillary channel; the second capillary liquid absorbing hole and the third capillary liquid absorbing hole extend upwards from the capillary liquid absorbing groove towards one end, adjacent to the axis of the segmented capillary liquid absorbing ring, of the first capillary liquid absorbing hole in an inclined mode, the aperture of the second capillary liquid absorbing hole is equal to that of the third capillary liquid absorbing hole, the aperture of the third capillary liquid absorbing hole is larger than that of the first capillary liquid absorbing hole, the cross sectional area of the second capillary liquid absorbing hole is larger than that of the capillary liquid absorbing groove, and the cross sectional area of the first capillary liquid absorbing hole is equal to that of any two vertically adjacent segmented liquid absorbing rings: the diameter of the lower bottom surface of the segmented capillary liquid absorption ring on the upper layer is equal to the diameter of the upper bottom surface of the segmented capillary liquid absorption ring on the lower layer; the capillary liquid absorption grooves on the upper-layer segmented capillary liquid absorption ring correspond to the capillary liquid absorption grooves on the lower-layer segmented capillary liquid absorption ring one by one from top to bottom; in any two adjacent capillary liquid suction grooves up and down: the distance S1 between the groove bottom of the upper capillary imbibition groove and the axis of the segmented capillary imbibition ring is smaller than the distance S2 between the groove bottom of the lower capillary imbibition groove and the axis of the segmented capillary imbibition ring, and the cross-sectional area of the capillary imbibition groove on the segmented capillary imbibition ring at the lower layer is larger than that of the capillary imbibition groove on the segmented capillary imbibition ring at the upper layer.
According to the multi-heat-source complementary hydrogen production device based on high-temperature heat pipe heat collection, the top and the bottom of the circular tubular thermochemical reactor are respectively welded with the upper end cover and the lower end cover, two ends of the circular tubular high-temperature pipe are respectively welded with the bottom of the upper end cover and the top of the lower end cover, the top of the circular tubular thermochemical reactor is communicated with the reactor inlet, the bottom of the circular tubular thermochemical reactor is communicated with the reactor outlet, and the top of the upper end cover is communicated with the liquid filling port; an upper sealing gasket is arranged between the inlet of the reactor and the upper end cover, a lower sealing gasket is arranged between the outlet of the reactor and the lower end cover, and a reaction zone is arranged inside the circular tubular thermochemical reactor.
The technical scheme of the invention achieves the following beneficial technical effects:
1. according to the invention, the high-temperature heat pipe reactor is arranged, so that the utilization rate of a heat source can be improved, the reactant can be conveniently heated, the high-temperature heat pipe reactor adopts the disc-type condenser to supply heat, the consumption of traditional energy sources can be reduced, the purposes of energy conservation and emission reduction are achieved, meanwhile, the high-temperature heat pipe can supply heat through the methane burner, the heat can be conveniently supplied when sunlight illumination is insufficient, and the hydrogen production can be realized by uninterrupted operation.
2. According to the invention, by arranging the PSA device and the palladium membrane separation device, impurities can be removed and purified from hydrogen, so that hydrogen with higher purity can be obtained, higher industrial standard can be reached, hydrocarbons can be synthesized, and fuel upgrading can be carried out.
3. According to the invention, by arranging the segmented capillary liquid absorption rings, and the bottom surfaces of the capillary liquid absorption channels on the upper and lower segmented capillary liquid absorption rings are not on the same surface, the capillary liquid absorption channels on each segmented capillary liquid absorption ring can independently play a capillary action, and can play a better capillary adsorption role on the liquid metal working medium condensed on the surface of the segmented capillary liquid absorption ring; the capillary liquid suction grooves are distributed from bottom to top in a step shape, so that the liquefaction center of the gaseous working medium can be greatly increased, the heat exchange efficiency is improved, and the secondary evaporation of the liquefied liquid metal working medium at the upper part can be reduced; the liquid suction core is formed by mutually matching a plurality of segmented capillary liquid suction rings, the formed capillary liquid suction channel is narrow at the top and wide at the bottom, after condensed working medium liquid drops are attached to the surface of the liquid suction core, the liquid metal working medium flows into the capillary liquid suction groove under the capillary action and flows downwards under the action of gravity.
4. According to the invention, through the Y-shaped channel formed by the first capillary liquid suction hole, the second capillary liquid suction hole and the third capillary liquid suction hole, liquid which is attached to the side surface of the liquid suction core and is relatively far away from the capillary liquid suction groove can be sucked into the first capillary liquid suction hole, and the liquid is guided into the capillary liquid suction groove through the flow guide of the second capillary liquid suction hole and the third capillary liquid suction hole, so that the liquid collecting and refluxing speed is effectively increased, and the heat exchange efficiency is improved; the cross sectional areas of the second capillary liquid suction hole and the third capillary liquid suction hole are larger than the cross sectional area of the capillary liquid suction groove, so that the liquid working medium in the capillary liquid suction groove is prevented from flowing back to the second capillary liquid suction hole and the third capillary liquid suction hole under the capillary action, and the temperature difference of reactants at the lower end and the upper end in the circular tubular thermochemical reactor is small by improving the liquid suction core structure on the outer wall of the circular tubular thermochemical reactor, thereby being beneficial to the full implementation of chemical reaction.
Drawings
FIG. 1 is a schematic diagram of a multi-source complementary hydrogen production system of the present invention;
FIG. 2 is a schematic structural diagram of a circular high-temperature heat pipe according to the present invention;
FIG. 3 is a schematic cross-sectional view of a wick according to the present invention;
FIG. 4 is a schematic perspective view of a segmented capillary wicking ring according to the present invention;
FIG. 5 is a schematic cross-sectional view of a segmented capillary wicking ring in accordance with the present invention;
FIG. 6 is a schematic diagram of a system for upgrading fuel by multi-source complementary hydrogen production according to the present invention.
The reference numbers in the figures denote: 1-a source of methane gas; 2-gas preheating equipment; 3-a steam generator; 4-a methane burner; 5-a dish concentrator; 6-high temperature thermal tube reactor; 7-high temperature water vapor conversion device; 8-a heat exchanger; 9-a steam turbine; 10-low temperature water vapor conversion device; 11-a gas-liquid separator; 12-a first compressor; 13-PSA pressure swing adsorption apparatus; 14-palladium membrane separation unit; 15-a second compressor; 16-a hydrogen storage tank; 17-reactor outlet; 18-a seal gasket; 19-a round tubular high-temperature heat pipe; 20-circular tubular thermochemical reactor; 21-liquid metal working medium; 22-a reaction zone; 23-upper end cap; 24-a liquid filling port; 25-lower end cap; 26-reactor inlet; 27-a wick; 28-segmented capillary wicking ring; 29-capillary pipette well; 30-a first capillary pipette well; 31-a second capillary pipette well; 32-a third capillary pipette well; 33-a first heat exchanger; 34-a fischer-tropsch synthesis reactor; 35-a second heat exchanger; 36-oil storage tank.
Detailed Description
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.
Referring to fig. 1, the present invention provides a technical solution: the multi-heat-source complementary hydrogen production device based on high-temperature heat pipe heat collection comprises feeding and preheating equipment, thermochemical hydrogen production equipment, heat exchange equipment, purification equipment and hydrogen storage equipment or synthetic oil and oil storage equipment, wherein a discharge pipe of the feeding and preheating equipment is in fluid communication with a feed pipe of the thermochemical hydrogen production equipment, a discharge pipe of the thermochemical hydrogen production equipment is in fluid communication with a feed pipe of the heat exchange equipment, a discharge pipe of the heat exchange equipment is in fluid communication with a feed pipe of the purification equipment, and a hydrogen outlet of the purification equipment is in fluid communication with a hydrogen inlet of the hydrogen storage equipment or a synthetic oil raw material gas inlet of the synthetic oil and oil storage equipment.
The feeding and preheating device comprises a steam generator 3, a gas preheating device 2 and a methane gas source 1, a steam outlet of the steam generator 3 is in fluid communication with a discharge pipe of the gas preheating device 2, and a gas outlet of the methane gas source 1 is in fluid communication with a preheating gas inlet of the gas preheating device 2; the discharge pipe of the gas preheating device 2 is in fluid communication with the feed pipe of the thermochemical hydrogen production device; the thermochemical hydrogen production equipment comprises a high-temperature thermal tube reactor 6, a disc type condenser 5 and a methane burner 4, wherein the focal spot of the disc type condenser 5 is positioned on the outer surface of the high-temperature thermal tube reactor 6, and the methane burner 4 supplies heat to the high-temperature thermal tube reactor 6 at night or in rainy days; the gas supply port of the methane gas source 1 is in fluid communication with the gas inlet of the methane burner 4; the discharge pipe of the gas preheating device 2 is in fluid communication with the reactant inlet of the high-temperature thermal tube reactor 6; the heat exchange equipment comprises a high-temperature water vapor conversion device 7, a heat exchanger 8 and a low-temperature water vapor conversion device 10, wherein a discharge pipe of the high-temperature water vapor conversion device 7 is in fluid communication with a feed pipe of the heat exchanger 8, and a discharge hole of the heat exchanger 8 is in fluid communication with a feed hole of the low-temperature water vapor conversion device 10; the reactant outlet of the high-temperature thermal tube reactor 6 is in fluid communication with the feed inlet of the high-temperature water-vapor conversion device 7; the purification equipment comprises a gas-liquid separator 11, a first compressor 12, a PSA (pressure swing adsorption) device 13 and a palladium membrane separation device, wherein a discharge pipe of the gas-liquid separator 11 is in fluid communication with a feed inlet of the first compressor 12, a discharge hole of the first compressor 12 is in fluid communication with a feed inlet of the PSA 13, and a discharge pipe of the PSA 13 is in fluid communication with a feed pipe of the palladium membrane separation device 14; the discharge pipe of the low-temperature water-vapor conversion device 10 is in fluid communication with the feed pipe of the gas-liquid separator 11, and the liquid outlet of the gas-liquid separator 11 is in fluid communication with the feed inlet of the steam generator 3; the hydrogen storage device comprises a second compressor 15 and a hydrogen storage tank 16, and discharge pipes of the second compressor are in fluid communication with an air inlet of the hydrogen storage tank 16; the discharge pipe of the palladium membrane separation device 14 is in fluid communication with the feed pipe of the second compressor 15; and a waste heat steam outlet pipe of the heat exchanger 8 is communicated with a steam turbine 9, and an electric power output end of the steam turbine 9 is electrically connected with electric power input ends of the first compressor 12 and the second compressor 15 respectively.
The heat exchange equipment comprises a first heat exchanger 33 and a gas-liquid separator 11, a first discharge pipe of the first heat exchanger 33 is in fluid communication with a feed pipe of the gas-liquid separator 11, a first feed pipe of the first heat exchanger 33 is in fluid communication with a discharge pipe of thermochemical hydrogen production equipment, and a liquid outlet of the gas-liquid separator 11 is in fluid communication with a feed inlet of a steam generator 3; the purification equipment comprises a PSA device 13, and a feed pipe of the PSA device 13 is in fluid communication with a discharge pipe of the gas-liquid separator 11; the discharge pipe of the PSA device 13 is in fluid communication with the second feed pipe of the first heat exchanger 33; the methane gas outlet of the PSA device 13 is in fluid communication with the feed pipe of the gas preheating device 2; the synthetic oil and oil storage equipment comprises a Fischer-Tropsch synthesis reactor 34, a second heat exchanger 35 and an oil storage tank 36, wherein a discharge pipe of the Fischer-Tropsch synthesis reactor 34 is in fluid communication with a feed pipe of the second heat exchanger 35, and a discharge pipe of the second heat exchanger 35 is in fluid communication with a feed pipe of the oil storage tank 36; the inlet pipe of ft reaction synthesizer and the second discharge tube fluid conduction of first heat exchanger 33, through setting up high temperature thermal tube reactor 6, can improve the utilization ratio to the heat source, be convenient for heat the reactant, high temperature thermal tube reactor 6 adopts dish formula spotlight ware 5 to supply heat, can reduce the consumption of traditional energy, reach energy saving and emission reduction's purpose, simultaneously, high temperature heat pipe can supply heat through methane burner 4, be convenient for supply heat when sunshine is not enough, realize incessant operation hydrogen manufacturing, through setting up PSA pressure swing adsorption equipment 13 and palladium membrane separator 14, can carry out edulcoration and purification to hydrogen, thereby obtain the higher hydrogen of purity, in order to reach higher industrial standard, and can carry out the synthetic hydrocarbon as shown in figure 6, carry out fuel upgrading.
As shown in fig. 2 to 5, the high-temperature thermal tube reactor 6 includes a circular tube-shaped high-temperature heat pipe 19, a circular tube-shaped thermal chemical reactor 20, and a liquid metal working medium 21 located between an inner wall of the circular tube-shaped high-temperature heat pipe 19 and an outer wall of the circular tube-shaped thermal chemical reactor 20, a liquid absorption core 27 is formed on the outer wall of the circular tube-shaped thermal chemical reactor 20, the liquid absorption core 27 includes two or more segmented capillary liquid absorption rings 28, and by providing the segmented capillary liquid absorption rings 28, bottom surfaces of capillary liquid absorption grooves 29 on the upper and lower segmented capillary liquid absorption rings 28 are not on the same surface, so that capillary liquid absorption grooves 29 on each segmented capillary liquid absorption ring 28 can independently perform a capillary action, and can perform a better capillary adsorption action on the liquid metal working medium 21 condensed on the surface of the segmented capillary liquid absorption rings 28; the capillary liquid suction grooves 29 are distributed from bottom to top in a step shape, so that the liquefaction center of the gaseous working medium can be greatly increased, the heat exchange efficiency is improved, and the secondary evaporation of the upper liquefied liquid metal working medium 21 can be reduced; the liquid absorption core 27 is formed by mutually matching a plurality of segmented capillary liquid absorption rings 28, the formed capillary liquid absorption groove 29 is narrow at the top and wide at the bottom, after condensed working medium liquid drops are attached to the surface of the liquid absorption core 27, the liquid metal working medium 21 flows into the capillary liquid absorption groove 29 under the capillary action and flows downwards under the action of gravity, the resistance of the liquid flowing downwards is small due to the narrow at the top and the wide at the bottom, the liquid amount is increased due to the continuous downward collection of the liquid, the falling gravitational potential energy is increased, and the influence of the rising working medium vapor on the backflow condensed liquid drops is reduced, the segmented capillary liquid absorption rings 28 are in a circular truncated cone shape, the capillary liquid absorption groove 29 is arranged on the outer side wall of the segmented capillary liquid absorption ring 28 along the direction parallel to a bus, the capillary liquid absorption groove 29 extends from the upper bottom surface of the segmented capillary liquid absorption ring 28 to the lower bottom surface of the segmented capillary liquid absorption ring 28, a first capillary liquid sucking hole 30 is formed in the outer side wall of the segmented capillary liquid sucking ring 28 between the adjacent capillary liquid sucking grooves 29, and the first capillary liquid sucking hole 30 extends downwards and slantways towards the axial direction of the segmented capillary liquid sucking ring 28; a second capillary liquid suction hole 31 is formed in one longitudinal side wall of the capillary liquid suction groove 29, and a third capillary liquid suction hole 32 is formed in the other longitudinal side wall; the first capillary liquid sucking hole 30, the second capillary liquid sucking hole 31 and the third capillary liquid sucking hole 32 on the segmented capillary liquid sucking ring 28 between the adjacent capillary liquid sucking grooves 29 form a Y-shaped capillary channel; the second capillary liquid-absorbing hole 31 and the third capillary liquid-absorbing hole 32 both extend from the capillary liquid-absorbing groove 29 to one end of the first capillary liquid-absorbing hole 30 adjacent to the axis of the segmented capillary liquid-absorbing ring 28 in an inclined manner, the aperture of the second capillary liquid-absorbing hole 31 and the aperture of the third capillary liquid-absorbing hole 32 are equal to and larger than that of the first capillary liquid-absorbing hole 30, the cross-sectional area of the second capillary liquid-absorbing hole 31 is larger than that of the capillary liquid-absorbing groove 29, the cross-sectional area of the first capillary liquid-absorbing hole 30 is equal to that of the capillary liquid-absorbing groove 29 in any two vertically adjacent segmented capillary liquid-absorbing rings 28, and liquid attached to the side surface of the liquid-absorbing groove 27 and relatively far from the capillary liquid-absorbing groove 29 can be absorbed into the first capillary liquid-absorbing hole 30 by arranging a Y-shaped channel composed of the first capillary liquid-absorbing hole 30, the second capillary liquid-absorbing hole 31 and the third capillary liquid-absorbing hole 32, the liquid is guided into the capillary liquid suction groove 29 by the guide of the second capillary liquid suction hole 31 and the third capillary liquid suction hole 32, so that the liquid collecting and refluxing speed is effectively improved, and the heat exchange efficiency is improved; the cross sectional areas of the second capillary liquid sucking hole 31 and the third capillary liquid sucking hole 32 are larger than the cross sectional area of the capillary liquid sucking groove 29, so that the liquid working medium in the capillary liquid sucking groove 29 is prevented from flowing back to the second capillary liquid sucking hole 31 and the third capillary liquid sucking hole 32 under the capillary action, and the temperature difference of reactants at the lower end and the upper end in the circular tubular thermochemical reactor 20 is smaller by improving the liquid sucking core 27 structure on the outer wall of the circular tubular thermochemical reactor 20, which is beneficial to the full implementation of chemical reaction: the diameter of the lower bottom surface of the segmented capillary liquid absorption ring 28 at the upper layer is equal to the diameter of the upper bottom surface of the segmented capillary liquid absorption ring 28 at the lower layer; the capillary liquid absorption grooves 29 on the upper-layer segmented capillary liquid absorption ring 28 correspond to the capillary liquid absorption grooves 29 on the lower-layer segmented capillary liquid absorption ring 28 one by one up and down; in any two of the capillary suction grooves 29 adjacent up and down: the distance S1 between the bottom of the upper capillary liquid sucking groove 29 and the axis of the segmented capillary liquid sucking ring 28 is smaller than the distance S2 between the bottom of the lower capillary liquid sucking groove 29 and the axis of the segmented capillary liquid sucking ring 28, and the cross-sectional area of the capillary liquid sucking groove 29 on the segmented capillary liquid sucking ring 28 is larger than that of the capillary liquid sucking groove 29 on the segmented capillary liquid sucking ring 28; the top and the bottom of the circular tubular thermochemical reactor 20 are respectively welded with an upper end cover 23 and a lower end cover 25, two ends of the circular tubular high-temperature tube are respectively welded with the bottom of the upper end cover 23 and the top of the lower end cover 25, the top of the circular tubular thermochemical reactor 20 is communicated with a reactor inlet 26, the bottom of the circular tubular thermochemical reactor 20 is communicated with a reactor outlet 17, and the top of the upper end cover 23 is communicated with a liquid filling port 24; an upper sealing gasket 18 is arranged between the reactor inlet 26 and the upper end cover 23, a lower sealing gasket 18 is arranged between the reactor outlet 17 and the lower end cover 25, and the reaction zone 22 is arranged inside the circular tubular thermochemical reactor 20.
The working principle is as follows: feeding and preheating: adjusting a steam flowmeter and a methane flowmeter, determining an optimal water-carbon ratio, introducing water into a steam generator 3, introducing methane of a methane gas source 1 into a gas preheating device 2, and merging the steam and the methane gas into the same pipeline at an outlet pipeline of the gas preheating device 2 to finish raw material preheating;
reaction: introducing a mixed raw material of methane and water vapor into the high-temperature thermal tube reactor 6, supplying heat for reaction by using the disc condenser 5 when the direct solar irradiance is sufficient, supplying heat for reaction by using the methane burner 4 at night or in rainy days, and after the reaction, allowing the reacted mixed gas to flow out from the outlet of the cylindrical high-temperature thermal tube reactor 6, wherein the main components of the gas are hydrogen, carbon monoxide, carbon dioxide, water vapor and methane;
heat exchange: the gas at the outlet 17 of the reactor is high-temperature gas with the temperature of more than 600 ℃, the high-temperature gas-water conversion device 7 is firstly introduced to further promote carbon monoxide and water vapor to be converted into carbon dioxide and hydrogen, the gas at the outlet of the high-temperature gas-water conversion device 7 enters a heat exchanger 8 to convert heat into water and generate water vapor, a steam turbine 9 is driven to generate electricity, electric quantity is used for the first compressor 12 and the second compressor 15 to work, the mixed gas after heat exchange is subjected to the low-temperature gas-water conversion device 10, and then the content of the hydrogen is further improved;
and (3) purification: the gas after the low-temperature water-vapor conversion device 10 mainly comprises hydrogen, carbon dioxide, water vapor, a small amount of methane and carbon monoxide, the gas is firstly introduced into a gas-liquid separator 11 to separate the water vapor from other gases, the water vapor is changed into liquid to flow into a steam generator 3 for recycling, the hydrogen, the carbon monoxide, the methane and the carbon dioxide enter a PSA (pressure swing adsorption) device 13 after passing through a first compressor 12, the purity of the hydrogen reaches 99.999 percent, and then the hydrogen enters a palladium membrane separation device 14, and high-purity hydrogen with the purity of 99.9999 percent can be generated after separation;
hydrogen storage: the pressure of the purified high-purity hydrogen is increased to 70MPa by the second compressor 15, and the purified high-purity hydrogen is injected into a hydrogen storage tank 16 or a seamless steel tube hydrogen storage bottle for storage.
In other embodiments, the apparatus and operation principle shown in fig. 6 may also be adopted:
feeding and preheating: firstly, adjusting a steam flowmeter and a methane flowmeter, determining an optimal water-carbon ratio, introducing water into a steam generator 3, introducing methane into a gas preheating device 2, and merging the steam and the methane gas into the same pipeline at an outlet pipeline of the gas preheating device 2 to finish raw material preheating;
reaction: introducing a mixed raw material of methane and water vapor into the cylindrical high-temperature thermal tube reactor 6, supplying heat for reaction by using the disc condenser 5 when the direct solar irradiance is sufficient, supplying heat for reaction by using the methane burner 4 at night or in rainy days, and after the reaction, allowing the reacted mixed gas to flow out from a discharge tube of the cylindrical high-temperature thermal tube reactor 6, wherein the main components of the gas are hydrogen, carbon monoxide, carbon dioxide, water vapor and methane;
gas separation and heat exchange: the mixed gas flowing out of the cylindrical high-temperature thermal tube reactor 6 enters a first heat exchanger 33, then flows into a gas-liquid separator 11, liquid after water vapor separation flows back to a steam generator 3 for recycling, hydrogen, carbon monoxide, carbon dioxide and methane enter a PSA pressure swing adsorption device 13, the separated methane flows back to a raw material preheating pipeline, the separated carbon dioxide is subjected to next industrial application, the separated carbon monoxide and hydrogen enter the first heat exchanger 33 for heating and then flow into a Fischer-Tropsch synthesis reactor 34 to generate a hydrocarbon mixture, the generated hydrocarbon mixture has the temperature of about 300 ℃, heat is converted into water through a second heat exchanger 35, the generated water vapor flows back to participate in the next reaction, and the hydrocarbon mixture after heat exchange enters an oil storage tank 36.
It should be understood that the above examples are only for clarity of illustration and are not intended to limit the embodiments. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. And obvious variations or modifications are possible which remain within the scope of the appended claims.
Claims (6)
1. The multi-heat-source complementary hydrogen production device based on high-temperature heat pipe heat collection comprises feeding and preheating equipment, thermochemical hydrogen production equipment, heat exchange equipment, purification equipment and hydrogen storage equipment or synthetic oil and oil storage equipment, and is characterized in that a discharge pipe of the feeding and preheating equipment is in fluid communication with a feed pipe of the thermochemical hydrogen production equipment, a discharge pipe of the thermochemical hydrogen production equipment is in fluid communication with a feed pipe of the heat exchange equipment, a discharge pipe of the heat exchange equipment is in fluid communication with a feed pipe of the purification equipment, and a hydrogen outlet of the purification equipment is in fluid communication with a hydrogen inlet of the hydrogen storage equipment or a synthetic oil raw material gas inlet of the synthetic oil and oil storage equipment;
the feeding and preheating device comprises a steam generator (3), a gas preheating device (2) and a methane gas source (1), wherein a steam outlet of the steam generator (3) is in fluid communication with a discharge pipe of the gas preheating device (2), and a gas outlet of the methane gas source (1) is in fluid communication with a preheating gas inlet of the gas preheating device (2); the discharge pipe of the gas preheating device (2) is in fluid communication with the feed pipe of the thermochemical hydrogen production device;
the thermochemical hydrogen production equipment comprises a high-temperature thermal tube reactor (6), a disc condenser (5) and a methane burner (4), wherein the focal spot of the disc condenser (5) is positioned on the outer surface of the high-temperature thermal tube reactor (6), and the methane burner (4) supplies heat to the high-temperature thermal tube reactor (6) at night or in rainy days; the gas supply port of the methane gas source (1) is in fluid communication with the gas inlet port of the methane burner (4); the discharge pipe of the gas preheating device (2) is in fluid communication with the reactant inlet of the high-temperature thermal tube reactor (6); the high-temperature thermal tube reactor (6) comprises a circular tube-shaped high-temperature heat pipe (19), a circular tube-shaped thermochemical reactor (20) and a liquid metal working medium (21) positioned between the inner wall of the circular tube-shaped high-temperature heat pipe (19) and the outer wall of the circular tube-shaped thermochemical reactor (20), wherein a liquid absorption core (27) is formed on the outer wall of the circular tube-shaped thermochemical reactor (20), the liquid absorption core (27) comprises two or more segmented capillary liquid absorption rings (28), the segmented capillary liquid absorption rings (28) are circular truncated cone-shaped in appearance, a capillary liquid absorption groove (29) is formed in the outer side wall of each segmented capillary liquid absorption ring (28) along the direction parallel to a bus, the capillary liquid absorption groove (29) extends from the upper bottom surface of each segmented capillary liquid absorption ring (28) to the lower bottom surface of each segmented capillary liquid absorption ring (28), and a first capillary liquid absorption hole (30) is formed in the outer side wall of each segmented capillary liquid absorption ring (28) between every two adjacent capillary liquid absorption grooves (29) ) The first capillary liquid sucking hole (30) extends obliquely downwards towards the axial direction of the segmented capillary liquid sucking ring (28); a second capillary liquid suction hole (31) is formed in one longitudinal side wall of the capillary liquid suction groove (29), and a third capillary liquid suction hole (32) is formed in the other longitudinal side wall; the first capillary liquid sucking hole (30), the second capillary liquid sucking hole (31) and the third capillary liquid sucking hole (32) on the segmented capillary liquid sucking ring (28) between the adjacent capillary liquid sucking grooves (29) form a Y-shaped capillary channel; the second capillary liquid sucking hole (31) and the third capillary liquid sucking hole (32) both extend from the capillary liquid sucking groove (29) to one end, adjacent to the axis of the segmented capillary liquid sucking ring (28), of the first capillary liquid sucking hole (30) in an inclined manner, the aperture of the second capillary liquid sucking hole (31) and the aperture of the third capillary liquid sucking hole (32) are equal to and larger than that of the first capillary liquid sucking hole (30), the cross-sectional area of the second capillary liquid sucking hole (31) is larger than that of the capillary liquid sucking groove (29), the cross-sectional area of the first capillary liquid sucking hole (30) is equal to that of the capillary liquid sucking groove (29), and in any two segmented capillary liquid sucking rings (28) adjacent up and down: the diameter of the lower bottom surface of the segmented capillary liquid absorption ring (28) on the upper layer is equal to the diameter of the upper bottom surface of the segmented capillary liquid absorption ring (28) on the lower layer; the capillary liquid suction grooves (29) on the upper-layer segmented capillary liquid suction ring (28) are in one-to-one correspondence with the capillary liquid suction grooves (29) on the lower-layer segmented capillary liquid suction ring (28) from top to bottom; in any two adjacent upper and lower capillary liquid suction grooves (29): the distance S1 between the bottom of the upper capillary liquid suction groove (29) and the axis of the segmented capillary liquid suction ring (28) is smaller than the distance S2 between the bottom of the lower capillary liquid suction groove (29) and the axis of the segmented capillary liquid suction ring (28), the cross-sectional area of the capillary liquid suction groove (29) on the segmented capillary liquid suction ring (28) on the lower layer is larger than that of the capillary liquid suction groove (29) on the segmented capillary liquid suction ring (28) on the upper layer, an upper end cover (23) and a lower end cover (25) are respectively welded at the top and the bottom of the circular tubular thermochemical reactor (20), two ends of the circular tubular high temperature heat pipe are respectively welded with the bottom of the upper end cover (23) and the top of the lower end cover (25), the top of the circular tubular thermochemical reactor (20) is communicated with a reactor inlet (26), the bottom of the circular tubular thermochemical reactor (20) is communicated with a reactor outlet (17), the top of the upper end cover (23) is communicated with a liquid filling opening (24); an upper sealing gasket (18) is arranged between the reactor inlet (26) and the upper end cover (23), a lower sealing gasket (18) is arranged between the reactor outlet (17) and the lower end cover (25), and a reaction zone (22) is arranged inside the circular tubular thermochemical reactor (20).
2. The high-temperature heat pipe heat collection-based multi-heat-source complementary hydrogen production device according to claim 1, wherein the heat exchange equipment comprises a high-temperature water-vapor conversion device (7), a heat exchanger (8) and a low-temperature water-vapor conversion device (10), a discharge pipe of the high-temperature water-vapor conversion device (7) is in fluid communication with a feed pipe of the heat exchanger (8), and a discharge hole of the heat exchanger (8) is in fluid communication with a feed hole of the low-temperature water-vapor conversion device (10); the reactant outlet of the high-temperature thermal tube reactor (6) is in fluid communication with the feed inlet of the high-temperature water-vapor conversion device (7).
3. The high-temperature heat pipe heat collection-based multi-heat-source complementary hydrogen production device according to claim 2, wherein the purification equipment comprises a gas-liquid separator (11), a first compressor (12), a PSA (pressure swing adsorption) device (13) and a palladium membrane separation device, wherein a discharge pipe of the gas-liquid separator (11) is in fluid communication with a feed inlet of the first compressor (12), a discharge pipe of the first compressor (12) is in fluid communication with a feed inlet of the PSA (pressure swing adsorption) device (13), and a discharge pipe of the PSA (pressure swing adsorption) device (13) is in fluid communication with a feed pipe of the palladium membrane separation device (14); the discharging pipe of the low-temperature water-vapor conversion device (10) is in fluid communication with the feeding pipe of the gas-liquid separator (11), and the liquid outlet of the gas-liquid separator (11) is in fluid communication with the feeding hole of the steam generator (3).
4. The high-temperature heat pipe heat collection-based multi-heat-source complementary hydrogen production device as claimed in claim 3, wherein the hydrogen storage equipment comprises a second compressor (15) and a hydrogen storage tank (16), and a discharge pipe of the second compressor is in fluid communication with an air inlet of the hydrogen storage tank (16); the discharge pipe of the palladium membrane separation device (14) is communicated with the feed pipe of the second compressor (15) in a fluid mode.
5. The high-temperature heat pipe heat collection-based multi-heat source complementary hydrogen production device as claimed in claim 2, wherein a residual heat steam outlet pipe of the heat exchanger (8) is communicated with a steam turbine (9), and an electric power output end of the steam turbine (9) is electrically connected with an electric power input end of the first compressor (12) and an electric power input end of the second compressor (15) respectively.
6. The high-temperature heat pipe heat collection-based multi-heat-source complementary hydrogen production device according to claim 1, wherein the heat exchange device comprises a first heat exchanger (33) and a gas-liquid separator (11), a first discharge pipe of the first heat exchanger (33) is in fluid communication with a feed pipe of the gas-liquid separator (11), a first feed pipe of the first heat exchanger (33) is in fluid communication with a discharge pipe of a thermochemical hydrogen production device, and a liquid outlet of the gas-liquid separator (11) is in fluid communication with a feed inlet of a steam generator (3);
the purification equipment comprises a PSA (pressure swing adsorption) device (13), and a feed pipe of the PSA device (13) is in fluid communication with a discharge pipe of the gas-liquid separator (11); a discharge pipe of the PSA device (13) is in fluid communication with a second feed pipe of the first heat exchanger (33); a methane gas outlet of the PSA (pressure swing adsorption) device (13) is in fluid communication with a feed pipe of the gas preheating equipment (2);
the synthetic oil and oil storage equipment comprises a Fischer-Tropsch synthesis reactor (34), a second heat exchanger (35) and an oil storage tank (36), wherein a discharge pipe of the Fischer-Tropsch synthesis reactor (34) is in fluid communication with a feed pipe of the second heat exchanger (35), and a discharge pipe of the second heat exchanger (35) is in fluid communication with a feed pipe of the oil storage tank (36); the feed pipe of the Fischer-Tropsch synthesis reactor is in fluid communication with the second discharge pipe of the first heat exchanger (33).
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102746870A (en) * | 2012-06-19 | 2012-10-24 | 中国石油化工股份有限公司 | FT synthesis technology |
| KR20130070796A (en) * | 2011-12-20 | 2013-06-28 | 한국에너지기술연구원 | Apparatus for simultaneous production of synthetic oil and electricity using fischer-tropsch synthesis reactor unit and fuel cell unit and method thereof |
| CN107596863A (en) * | 2017-08-18 | 2018-01-19 | 大连理工大学 | A kind of Photospot solar distributed heat hydrogen production system employing reforming technology based on cylindrical shape high-temperature heat pipe |
| CN109119660A (en) * | 2018-09-25 | 2019-01-01 | 北京市煤气热力工程设计院有限公司 | Thermoelectricity hydrogen polygenerations systeme based on city gas |
-
2020
- 2020-10-17 CN CN202011113326.7A patent/CN112239196B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20130070796A (en) * | 2011-12-20 | 2013-06-28 | 한국에너지기술연구원 | Apparatus for simultaneous production of synthetic oil and electricity using fischer-tropsch synthesis reactor unit and fuel cell unit and method thereof |
| CN102746870A (en) * | 2012-06-19 | 2012-10-24 | 中国石油化工股份有限公司 | FT synthesis technology |
| CN107596863A (en) * | 2017-08-18 | 2018-01-19 | 大连理工大学 | A kind of Photospot solar distributed heat hydrogen production system employing reforming technology based on cylindrical shape high-temperature heat pipe |
| CN109119660A (en) * | 2018-09-25 | 2019-01-01 | 北京市煤气热力工程设计院有限公司 | Thermoelectricity hydrogen polygenerations systeme based on city gas |
Non-Patent Citations (2)
| Title |
|---|
| 太阳能膜反应器燃料制取及联合循环效率分析;王宏圣等;《工程热物理学报》;20161231(第11期);3-10 * |
| 熔融盐作热载体太阳能甲烷蒸汽重整制氢过程的模拟研究;冯靓婧;《中国优秀硕士学位论文全文数据库》;20150415(第工程科技Ⅰ辑期);4-5,18-20,26-27 * |
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