CN114832510A - Gas-liquid separator and water electrolysis hydrogen production system - Google Patents
Gas-liquid separator and water electrolysis hydrogen production system Download PDFInfo
- Publication number
- CN114832510A CN114832510A CN202210640014.4A CN202210640014A CN114832510A CN 114832510 A CN114832510 A CN 114832510A CN 202210640014 A CN202210640014 A CN 202210640014A CN 114832510 A CN114832510 A CN 114832510A
- Authority
- CN
- China
- Prior art keywords
- gas
- liquid separator
- catalyst
- liquid separation
- liquid
- 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.)
- Granted
Links
- 239000007788 liquid Substances 0.000 title claims abstract description 181
- 239000001257 hydrogen Substances 0.000 title claims abstract description 71
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 71
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 67
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 64
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 55
- 238000005868 electrolysis reaction Methods 0.000 title claims abstract description 22
- 239000007789 gas Substances 0.000 claims abstract description 158
- 238000000926 separation method Methods 0.000 claims abstract description 79
- 238000007872 degassing Methods 0.000 claims abstract description 58
- 239000012535 impurity Substances 0.000 claims abstract description 23
- 239000003054 catalyst Substances 0.000 claims description 108
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 19
- 239000001301 oxygen Substances 0.000 claims description 19
- 229910052760 oxygen Inorganic materials 0.000 claims description 19
- 238000010438 heat treatment Methods 0.000 claims description 16
- 238000001816 cooling Methods 0.000 claims description 9
- 238000006392 deoxygenation reaction Methods 0.000 claims description 9
- 238000007599 discharging Methods 0.000 claims description 9
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 238000004891 communication Methods 0.000 claims description 2
- 238000005192 partition Methods 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 19
- 230000008569 process Effects 0.000 abstract description 15
- 238000003795 desorption Methods 0.000 abstract description 10
- 238000009434 installation Methods 0.000 abstract description 8
- 230000009977 dual effect Effects 0.000 abstract description 3
- 239000012071 phase Substances 0.000 description 42
- 239000007791 liquid phase Substances 0.000 description 15
- 230000000694 effects Effects 0.000 description 8
- 230000005484 gravity Effects 0.000 description 8
- 238000006356 dehydrogenation reaction Methods 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 6
- 230000009471 action Effects 0.000 description 5
- 238000010586 diagram Methods 0.000 description 5
- 230000000630 rising effect Effects 0.000 description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 150000002431 hydrogen Chemical class 0.000 description 4
- 230000008859 change Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000000523 sample Substances 0.000 description 3
- 239000002826 coolant Substances 0.000 description 2
- 239000012809 cooling fluid Substances 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000006073 displacement reaction Methods 0.000 description 2
- 238000005485 electric heating Methods 0.000 description 2
- 239000012774 insulation material Substances 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000000712 assembly Effects 0.000 description 1
- 238000000429 assembly Methods 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 230000008602 contraction Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000014509 gene expression Effects 0.000 description 1
- 239000011810 insulating material Substances 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000000750 progressive effect Effects 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/02—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by utilising gravity
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
- C25B1/02—Hydrogen or oxygen
- C25B1/04—Hydrogen or oxygen by electrolysis of water
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
-
- 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
- Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Environmental & Geological Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Analytical Chemistry (AREA)
- Electrochemistry (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Inorganic Chemistry (AREA)
- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
Abstract
The invention discloses a gas-liquid separator and a water electrolysis hydrogen production system, which comprises a tank body, a gas-liquid separation part and a degassing part, wherein the tank body is provided with a crude gas inlet and a gas phase outlet which are sequentially arranged along the height direction; the gas-liquid separation part and the degassing part are arranged in the tank body and are positioned on a flowing path of the crude gas inlet and the gas phase outlet, the gas-liquid separation part is used for carrying out gas-liquid separation on the crude gas entering the tank body, and the degassing part is used for removing impurity gas in the crude gas. This vapour and liquid separator, when being applied to the corresponding system gas side of electrolytic water hydrogen production system, can carry out gas-liquid separation to the crude gas that gets into the jar internal through gas-liquid separation portion, simultaneously can desorption impurity gas in the crude gas through the degasification portion, make vapour and liquid separator integrated the gas-liquid separation and desorption impurity gas's in the crude gas dual function, reduced electrolytic water hydrogen production system's equipment quantity, the process flow of whole hydrogen production system has been shortened, consequently, the whole equipment cost and the installation space demand of electrolytic water hydrogen production system have been reduced.
Description
Technical Field
The invention relates to the technical field of gas-liquid separation, in particular to a gas-liquid separator and a water electrolysis hydrogen production system.
Background
In the existing technical scheme, in the hydrogen production process by water electrolysis, the gas-liquid separation and the deoxidation process are completed by two sets of devices which are completely and independently designed, and are respectively carried out in a gas-liquid separator and a deoxygenator, and equipment such as a cooler and the like is required to be arranged. The whole hydrogen production system has longer process flow, more equipment, high overall equipment cost and larger installation space requirement.
In conclusion, how to solve the problems of high overall equipment cost and large installation space requirement of the water electrolysis hydrogen production system becomes a problem to be solved urgently by the technical personnel in the field.
Disclosure of Invention
In view of this, the invention provides a gas-liquid separator and a water electrolysis hydrogen production system, so as to solve the problems of high overall equipment cost and large installation space requirement of the water electrolysis hydrogen production system.
In order to achieve the purpose, the invention provides the following technical scheme:
a gas-liquid separator for mounting to a corresponding gas generation side of an electrolyzed water hydrogen generation system comprising:
the tank body is provided with a crude gas inlet and a gas phase outlet which are sequentially arranged along the height direction;
a gas-liquid separation section and a degassing section which are provided in the tank body and are located on a flow path between the raw gas inlet and the gas phase outlet;
the gas-liquid separation part is used for carrying out gas-liquid separation on the crude gas entering the tank body; the degassing part is used for removing impurity gases in the crude gas.
Optionally, the gas-liquid separation portion includes a first gas-liquid separation part and a second gas-liquid separation part arranged in sequence from bottom to top, and the degassing portion is located between the first gas-liquid separation part and the second gas-liquid separation part.
Optionally, the degassing part is a degassing catalyst loaded between the first gas-liquid separator and the second gas-liquid separator, wherein the degassing catalyst is used for reacting with the impurity gas to generate water.
Optionally, the outer side of the tank body is also provided with a catalyst filling opening and a catalyst discharging opening;
wherein the catalyst charging port is disposed near a lower surface of the second gas-liquid separating member, and the catalyst discharging port is disposed near an upper surface of the first gas-liquid separating member.
Optionally, an inner cylinder is arranged on the tank body, the bottom of the inner cylinder is communicated with a cavity where the gas-liquid separation part is located, a carrier cavity is formed by enclosing the inner walls of the inner cylinder and the tank body, a vent hole communicated with the carrier cavity is formed in the cylinder wall of the inner cylinder, and the gas phase outlet is communicated with the carrier cavity;
wherein the degassing section is loaded in the carrier chamber.
Optionally, an electric heater is arranged in the inner cylinder.
Optionally, the electric heater is equipped with a heating controller for adjusting a heating temperature of the electric heater.
Optionally, a support assembly is disposed in the carrier cavity, the support assembly divides the carrier cavity into a catalyst loading cavity and an exhaust cavity which are distributed from top to bottom, the degassing part is a degassed catalyst loaded in the catalyst loading cavity, and the gas phase outlet is communicated with the exhaust cavity.
Optionally, the outer side of the tank body is also provided with a catalyst filling opening and a catalyst discharging opening which are communicated with the catalyst loading cavity;
wherein the catalyst loading port is disposed proximate a top of the catalyst loading chamber and the catalyst discharge port is disposed proximate a bottom of the catalyst loading chamber.
Optionally, a cooler is further disposed in the exhaust cavity, the outer side of the tank body is provided with a liquid discharge port communicated with the exhaust cavity, the liquid discharge port is communicated with the bottom of the exhaust cavity and is arranged, and the arrangement position of the gas phase outlet on the exhaust cavity is higher than the liquid discharge port.
Optionally, the cooler is further equipped with a flow regulator for regulating the cooling amount of the cooler.
Optionally, the tank section corresponding to the gas-liquid separation part and the tank section corresponding to the deoxidation part are connected through an expansion joint.
Optionally, an insulating layer is further disposed on the outer side of the tank body.
Optionally, when the gas production side is a hydrogen production side, the raw gas is raw hydrogen, and the impurity gas is oxygen; when the gas production side is an oxygen production side, the crude gas is crude oxygen, and the impurity gas is hydrogen.
Compared with the introduction content of the background technology, the gas-liquid separator is used for being installed on the corresponding gas production side of the water electrolysis hydrogen production system and comprises a tank body, a gas-liquid separation part and a degassing part, wherein the tank body is provided with a coarse gas inlet and a gas phase outlet which are sequentially arranged along the height direction; the gas-liquid separation part and the degassing part are arranged in the tank body and are positioned on a flowing path of the crude gas inlet and the gas phase outlet, the gas-liquid separation part is used for carrying out gas-liquid separation on the crude gas entering the tank body, and the degassing part is used for removing impurity gas in the crude gas. This vapour and liquid separator, when being applied to the corresponding system gas side of electrolytic water hydrogen production system, can carry out gas-liquid separation to the crude gas that gets into the jar internal through gas-liquid separation portion, simultaneously can desorption impurity gas in the crude gas through the degasification portion, make vapour and liquid separator integrated the gas-liquid separation and desorption impurity gas's in the crude gas dual function, reduced electrolytic water hydrogen production system's equipment quantity, the process flow of whole hydrogen production system has been shortened, consequently, the whole equipment cost and the installation space demand of electrolytic water hydrogen production system have been reduced.
In addition, the invention also provides a system for producing hydrogen by electrolyzing water, which comprises a gas-liquid separator, wherein the gas-liquid separator is the gas-liquid separator described in any scheme. Because the gas-liquid separator has the technical effects, the hydrogen production system by electrolyzing water with the gas-liquid separator also has the corresponding technical effects.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
FIG. 1 is a first schematic structural view of a gas-liquid separator according to an embodiment of the present invention;
FIG. 2 is a schematic view of a second configuration of a gas-liquid separator according to an embodiment of the present invention;
FIG. 3 is a schematic view of a third structure of a gas-liquid separator according to an embodiment of the present invention;
fig. 4 is a schematic structural diagram of connection between a tank section corresponding to the gas-liquid separation portion and a tank section corresponding to the deoxidation portion, which is provided by an embodiment of the present invention, through an expansion joint.
Wherein, in fig. 1-4:
the device comprises a tank body 1, a crude gas inlet 11, a gas phase outlet 12, a liquid phase outlet 13, a catalyst filling port 14, a catalyst discharging port 15, a bent pipe 16, a liquid discharging port 17, a heat insulation layer 18, an outer cylinder body 18a, a heat insulation material 18b and a temperature measuring probe 19;
a gas-liquid separation part 2, a first gas-liquid separator 21, and a second gas-liquid separator 22;
a degassing section 3;
an inner cylinder 4, an electric heater 40, an electric heating tube 40a, a temperature detector 40b, and an air vent 41;
a carrier chamber 5, a catalyst loading chamber 5a, an exhaust chamber 5b, a degassing catalyst 51, a holder member 52;
a cooler 6, a coolant inlet 61, and a coolant outlet 62;
a mounting bracket 7;
an expansion joint 8.
Detailed Description
The core of the invention is to provide a gas-liquid separator and a water electrolysis hydrogen production system, so as to solve the problems of high overall equipment cost and large installation space requirement of the water electrolysis hydrogen production system.
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 to 4, fig. 1 is a first structural schematic diagram of a gas-liquid separator according to an embodiment of the present invention; FIG. 2 is a schematic view of a second configuration of a gas-liquid separator according to an embodiment of the present invention; FIG. 3 is a schematic view of a third structure of a gas-liquid separator according to an embodiment of the present invention; fig. 4 is a schematic structural diagram of connection between a tank section corresponding to the gas-liquid separation portion and a tank section corresponding to the deoxidation portion, which is provided by an embodiment of the present invention, through an expansion joint.
The embodiment of the invention provides a gas-liquid separator which is used for being installed on a corresponding gas making side of an electrolytic water hydrogen making system and comprises a tank body 1, a gas-liquid separation part 2 and a degassing part 3, wherein the tank body 1 is provided with a crude gas inlet 11 and a gas phase outlet 12 which are sequentially arranged along the height direction (for example, referring to fig. 1-3, the mode of sequentially arranging from bottom to top is adopted; or referring to fig. 4, the mode of sequentially arranging from top to bottom is adopted); the gas-liquid separation part 2 and the degassing part 3 are both arranged in the tank body 1 and are positioned on a flow path of the crude gas inlet 11 and the gas phase outlet 12; the gas-liquid separation part 2 is used for carrying out gas-liquid separation on the crude gas entering the tank body 1, and the degassing part 3 is used for removing impurity gas in the crude gas.
This vapour and liquid separator, when being applied to the corresponding system gas side of electrolytic water hydrogen production system, can carry out gas-liquid separation to the coarse gas that gets into jar body 1 through gas-liquid separation portion 2, the impure gas in the coarse gas can be got rid of through degasification portion 3 simultaneously, make vapour and liquid separator integrated the gaseous dual function of the impure gas in gas-liquid separation and the desorption coarse gas, the equipment quantity of electrolytic water hydrogen production system has been reduced, the process flow of whole hydrogen production system has been shortened, therefore, the whole equipment cost and the installation space demand of electrolytic water hydrogen production system have been reduced.
It should be noted that, as will be understood by those skilled in the art, for the gas-liquid separator, the bottom of the tank 1 should be provided with a liquid phase outlet 13, so that the liquid phase after gas-liquid separation flows away, and generally flows into the electrolytic tank or the water collector of the water electrolysis hydrogen production system. The specific structural form of the gas-liquid separation part is not limited, and the working principle of the gas-liquid separation part is to remove trace moisture contained in the crude gas (crude hydrogen or crude hydrogen) and separate the crude gas and the crude hydrogen by depending on the gravity difference of gas phase and liquid phase, so that gas phase with low liquid content is obtained. For example, the gas-liquid separation part may specifically be configured to cool the raw gas by a cooling mechanism, and then condense the trace moisture in the raw gas into liquid to be removed; for another example, the components such as the liquid drop catching component, the wire mesh defoaming component and the baffle plate are used for realizing gas-liquid separation, and in the practical application process, the components can be selectively arranged according to the practical requirements.
In addition, the gas-liquid separator can be specifically applied to the hydrogen production side of the water electrolysis hydrogen production system, and can also be applied to the oxygen production side. When the gas-liquid separator is applied to the hydrogen production side (that is, the gas production side is the hydrogen production side), the crude gas is crude hydrogen, the impurity gas is oxygen, and the degassing operation is deoxidation; when the gas-liquid separator is applied to the oxygen generation side (i.e., the oxygen generation side is the gas generation side), the crude gas is crude oxygen, the impurity gas is hydrogen, and the degassing operation is dehydrogenation. Wherein, the deoxidation refers to that a small amount of oxygen in the crude hydrogen reacts under the action of a deoxidation catalyst to generate moisture, so that the small amount of oxygen contained in the crude hydrogen is removed; the dehydrogenation refers to the reaction of a small amount of hydrogen in crude oxygen under the action of a dehydrogenation catalyst to generate water, so that a small amount of hydrogen contained in the crude oxygen is removed.
In some specific embodiments, referring to fig. 1, a first structural schematic diagram of a gas-liquid separator according to an embodiment of the present invention, the gas-liquid separation section 2 may specifically include a first gas-liquid separation member 21 and a second gas-liquid separation member 22 arranged in sequence from bottom to top, and the degassing section 3 is located between the first gas-liquid separation member 21 and the second gas-liquid separation member 22. This first structural style mainly relies on normal atmospheric temperature desorption impure gas, specifically, inside the crude gas raw materials passes through crude gas entry 11 and gets into vapour and liquid separator, then passes through first gas-liquid separation spare 21, degasification portion 3 and second gas-liquid separation spare 22 in proper order to can accomplish gas-liquid separation-desorption impure gas-the processing procedure of gas-liquid separation again in proper order, produced water when so can making crude gas desorption impure gas obtains further desorption, in order to guarantee the purity of the gas of being derived by gas phase outlet 12.
The first gas-liquid separator 21 and the second gas-liquid separator 22 in the gas-liquid separation section 2 may specifically adopt a wire mesh demister structure, or may adopt other structures that can realize gas-liquid separation, which are commonly used by those skilled in the art, and are not limited to the specific embodiments.
In a further embodiment, the degassing part 3 may be specifically designed as a degassing catalyst loaded between the first gas-liquid separating member 21 and the second gas-liquid separating member 22, wherein the degassing catalyst is used to react with the impurity gas to generate water, specifically, when the impurity gas is hydrogen, the degassing catalyst is a dehydrogenation catalyst, and when the impurity gas is oxygen, the degassing catalyst is a deoxidation catalyst. Get rid of impure gas through the mode of degasification catalyst and can satisfy high-efficient desorption impure gas to it is more convenient to change the maintenance, only needs to change new degasification catalyst can.
In the specific technical scheme, in order to conveniently replace the degassed catalyst, a catalyst filling opening 14 and a catalyst discharging opening 15 can be further arranged on the outer side of the tank body 1; wherein the catalyst charging port 14 is disposed near the lower surface of the second gas-liquid separating member 22, and the catalyst discharging port 15 is disposed near the upper surface of the first gas-liquid separating member 21. Old degassed catalyst can be unloaded through the catalyst discharge opening 15 and is arranged close to the upper surface of the first gas-liquid separating member 21, so that the old degassed catalyst can be unloaded cleanly; the catalyst filling port 14 can be filled with a new degassed catalyst and is disposed near the lower surface of the second gas-liquid separator 22, so that the space between the first gas-liquid separator 21 and the second gas-liquid separator 22 can be filled with the catalyst.
It is understood that the method of removing impurity gas by using a degassing catalyst is merely an example of the embodiment of the present invention, and other degassing materials commonly used by those skilled in the art may be used in the practical application, and are not limited in any way.
In order to better understand the gas-liquid separator of the first structure provided by the present invention, the operation of the gas-liquid separator of the first structure is briefly described below with reference to fig. 1 by taking the application of the gas-liquid separator to the hydrogen production side by electrolyzing water as an example:
raw crude hydrogen enters from a crude gas inlet 11, is primarily separated into gas-liquid two phases in the bottom space of the tank body 1 under the action of gravity, the liquid phase enters the bottommost part of the tank body 1 and flows out of a liquid phase outlet 13 of the tank body 1, the gas-liquid is further separated when the rising gas phase passes through a first gas-liquid separating member 21 (such as a wire mesh demister), the separated liquid phase enters the bottom of the tank body 1 and flows out from the liquid phase outlet 13, the gas phase continuously rises to a degassing part 3 (namely a deoxygenation catalyst), deoxygenation reaction occurs, a gas-water mixture obtained after the reaction enters a second gas-liquid separating member 22 at the upper part, the liquid phase is further separated, the obtained gas phase flows out from a gas phase outlet 12 of the tank body 1, and the separated liquid phase flows downwards to the bottom of the tank body 1 and flows out of the tank body 1 from the liquid phase outlet 13.
In some more specific embodiments, referring to fig. 2, a second schematic structural diagram of the gas-liquid separator provided in the embodiment of the present invention, an inner cylinder 4 may be specifically disposed on the tank 1, the inner cylinder 4 is at least partially located inside the tank 1 and above the gas-liquid separation portion 2, a carrier cavity 5 is defined by the inner cylinder 4 and the inner wall of the tank 1, an electric heater 40 is disposed in the inner cylinder 4, the bottom of the inner cylinder 4 is communicated with the cavity where the gas-liquid separation portion 2 is located, an air vent 41 communicated with the carrier cavity 5 is disposed on the cylinder wall of the inner cylinder 4, and the gas phase outlet 12 is communicated with the carrier cavity 5; the degassing part 3 is loaded in the carrier chamber 5, and the degassing part 3 may be a degassing catalyst 51 for reacting with the impurity gas to generate water. The specific working process is as follows: the raw material of the crude gas enters the tank body 1 through the crude gas inlet 11, then passes through the gas-liquid separation part 2, enters the carrier cavity 5 through the vent hole 41 on the inner cylinder 4, reacts with the degassing catalyst 51 in the carrier cavity 5 to remove impurity gas, and finally the purified gas is output through the gas phase outlet 12. By designing the tank body 1 in this second structural form, the inner cylinder 4 can make the arrangement positions of the gas-liquid separation section 2 and the degassing section 3 in the tank body 1 not interfere with each other and not affect each other, which is more convenient when the operation of unloading and filling the degassing catalyst 51 is performed. And by arranging the electric heater 40, the working environment of the gas-liquid separator is made to be a high temperature environment, i.e., the temperature is above the dew point temperature of moisture at the working pressure. The electric heater 40 may specifically include an electric heating tube 40a and a temperature detector 40b (e.g., a thermocouple), and the air flowing through the inner cylinder 4 is heated by the electric heater 40.
In a further embodiment, the electric heater 40 may be further equipped with a heating controller for adjusting the heating temperature of the electric heater 40. In a specific adjusting mode, for example, in a water electrolysis hydrogen production system, the problem of unstable gas production is easily caused due to the characteristic of variable power/power fluctuation in the working process of the water electrolysis hydrogen production system. Therefore, by configuring the heating controller, when the water electrolysis hydrogen production system is in low power or the gas production amount is small (the specific numerical value can be set according to the actual working condition requirement), the temperature of the heater is reduced by the heating controller, so that the requirement of deoxidation on the hydrogen production side (dehydrogenation on the oxygen production side) is met; when the water electrolysis hydrogen production system is in high power or the gas production amount is large (specific numerical value can be set according to actual working condition requirements), the heating temperature of the electric heater is increased through the heating controller, and therefore the deoxidation effect of the hydrogen production side or the dehydrogenation effect of the oxygen production side can be increased. It should be noted that, the heating controller may be manually operated by a user, or may be automatically controlled, and is not limited to this.
In a further embodiment, a support member 52 is disposed in the carrier chamber 5, the support member 52 divides the carrier chamber 5 into a catalyst loading chamber 5a and a gas discharge chamber 5b distributed from top to bottom, the degassing part 3 is a degassing catalyst 51 loaded in the catalyst loading chamber 5a, and the gas phase outlet 12 is communicated with the gas discharge chamber 5 b. The arrangement of the exhaust-related devices is made more convenient by providing the holder member 52 to divide the carrier chamber 5 into the catalyst loading chamber 5a and the exhaust chamber 5b, because there is no interference between the exhaust chamber 5b and the catalyst loading chamber 5 a. It should be noted that the holder member 52 should have gas permeability (e.g., a support layer having a porous structure) to allow pure gas for removing impurity gases to enter the exhaust chamber 5b from the catalyst-loading chamber 5 a.
In addition, in order to conveniently load and unload the degassed catalyst in the catalyst loading cavity 5a, a catalyst loading port 14 and a catalyst unloading port 15 which are communicated with the catalyst loading cavity 5a can be arranged on the outer side of the tank body 1; wherein the catalyst filling port 14 is disposed near the top of the catalyst loading chamber 5a and the catalyst discharge port 15 is disposed near the bottom of the catalyst loading chamber 5 a. Old degassed catalyst can be unloaded through the catalyst discharge opening 15 and is arranged close to the bottom of the catalyst loading chamber 5a, facilitating the unloading of old degassed catalyst clean; the space of the catalyst loading chamber 5a can be filled with new degassed catalyst by the catalyst filling port 14 and disposed near the top of the catalyst loading chamber 5a, which can be easily filled with the catalyst.
In order to better understand the gas-liquid separator of the second structure provided by the present invention, the following takes the application of the gas-liquid separator to the hydrogen production side of the water electrolysis hydrogen production system as an example, and the specific operation process of the gas-liquid separator is briefly described with reference to fig. 2:
the specific separation and deoxidation process is as follows: crude hydrogen firstly enters a separation space at the lower end of a tank body 1 from a crude gas inlet 11 of the tank body 1, gas-liquid two phases are subjected to primary separation in a bottom space of the tank body 1 due to gravity difference, the gas carrying a trace amount of moisture further separates the gas-liquid two phases in a gas-liquid separation part 2 (such as a wire mesh demister), all separated liquid phases fall to the bottommost part of the tank body 1 through gravity and flow out of the tank body 1 from a liquid phase outlet 13, the rising gas phase enters the bottom of an inner cylinder 4 of an electric heater 40, the rising gas phase temperature is continuously increased under the heating of the electric heater 40 and enters a catalyst loading cavity 5a from a vent 41 of the inner cylinder 4, and the gas phase flows from top to bottom through a deoxygenation catalyst loaded in the catalyst loading cavity 5a to generate deoxygenation reaction on the deoxygenation catalyst and leaves the tank body 1 from a gas phase outlet 12.
In some specific embodiments, referring to fig. 3, the exhaust chamber 5b may further include a cooler 6, and the outside of the tank body is provided with a drain 17 communicated with the exhaust chamber 5b, the drain 17 is communicated with the bottom of the exhaust chamber 5b, and the gas phase outlet 12 is disposed at a position higher than the drain 17 on the exhaust chamber 5 b. Through arranging cooler 6 in exhaust cavity 5b, can cool off the moisture that the gas-water mixture after degasification makes the gas phase through cooler 6 and cool off and separate out, the moisture that separates out flows to exhaust cavity 5 b's bottom because of the action of gravity, finally is discharged away by leakage fluid dram 17, through design cooler 6, makes vapour and liquid separator have the cooling function, also makes the combustion gas purer simultaneously. The cooler may specifically adopt a heat exchange structure in the form of a coil, a tube, or the like, so as to sufficiently cool the degassed gas phase and separate water therefrom. Specifically, the cooler 6 generally has a cooling fluid inlet 61 and a cooler outlet 62 extending to the outside of the tank 1, and the arrangement of the cooling fluid inlet 61 and the cooler outlet 62 is preferably designed in a bottom-up manner, which is more favorable for sufficient heat exchange cooling.
In a further embodiment, the above-described cooler 6 may also be equipped with a flow regulator, by which the cooling amount of the cooler 6 can be regulated. Specifically, the flow rate of the cooler 6 can be adjusted according to the hydrogen production (oxygen production) power of the water electrolysis hydrogen production system, thereby improving the cooling and gas-liquid separation effects. For example, when the water electrolysis hydrogen production system is in low power/low gas production (the specific value can be set according to the actual requirement), the cooling amount can be reduced through the flow regulator; when the water electrolysis hydrogen production system is at high power/high gas production (the specific value can be set according to the actual requirement), the cooling capacity can be increased through the flow regulator.
Generally, the degassing part 3 performs a degassing reaction (a catalyst deoxidation reaction or a catalyst dehydrogenation reaction), which generates relatively high heat, and the temperature of the operating environment of the gas-liquid separation part 2 is relatively low, so that, in order to improve the stability of the entire tank and avoid the problem that the tank may be damaged due to hard connection, referring to fig. 4, a tank section corresponding to the gas-liquid separation part 2 (i.e., a tank wall of the tank 1 for enclosing the gas-liquid separation part 2) and a tank section corresponding to the deoxidation part 3 (i.e., a tank wall of the tank 1 for enclosing the deoxidation part 3) may be connected by an expansion joint 8. Wherein, the coarse gas inlet 11 and the gas phase outlet 12 may be arranged from top to bottom, or from bottom to top, and are not limited herein. Through design expansion joint 8, can absorb the jar section that gas-liquid separation portion 2 corresponds and the jar section that deoxidation portion 3 corresponds because the displacement volume that expend with heat and contract with cold produced, avoided the hard joint to lead to the easy problem of damaging of jar body, promoted the stability of whole jar of body.
It should be noted that, when the tank 1 has a vertically arranged inner cylinder 4, the inner cylinder 4 is at least partially located inside the tank 1 and above the gas-liquid separation part 2, the inner cylinder 4 and the inner wall of the tank 1 are surrounded to form a carrier chamber 5, a support member 52 is arranged in the carrier chamber 5, the support member 52 divides the carrier chamber 5 into a catalyst loading chamber 5a and an exhaust chamber 5b which are distributed from top to bottom, the degassing part 3 is a degassing catalyst 51 loaded in the catalyst loading chamber 5a, the gas phase outlet 12 is communicated with the exhaust chamber 5b, a cooler 6 can be arranged in the exhaust chamber 5b, a liquid discharge port 17 communicated with the exhaust chamber 5b is arranged outside the tank, the liquid discharge port 17 is arranged in communication with the bottom of the exhaust chamber 5b, and the arrangement position of the gas phase outlet 12 on the exhaust chamber 5b is higher than the liquid discharge port 17, that the tank section corresponding to the exhaust chamber 5b (the tank wall of the tank 1 for surrounding the exhaust chamber 5b) corresponds to the catalyst loading chamber 5a Preferably, the inner cylinder section corresponding to the exhaust cavity 5b (i.e. the cylinder wall of the inner cylinder 18a enclosing the exhaust cavity 5b) and the inner cylinder section corresponding to the catalyst loading cavity 5a (i.e. the cylinder wall of the inner cylinder 18a enclosing the catalyst loading cavity 5a) are connected by expansion joints. Because the temperature of the catalyst loading cavity 5a is relatively high when the catalyst loading cavity 5a performs degassing reaction (such as deoxidation reaction), and the temperature of the exhaust cavity 5b is relatively low due to the arrangement of the cooler 6 in the exhaust cavity 5b, the displacement generated by thermal expansion and cold contraction between the inner cavity wall and the outer cavity wall of the exhaust cavity 5b and the inner cavity wall and the outer cavity wall of the catalyst loading cavity 5a can be absorbed by designing the expansion joint, so that the problem that the tank body is easily damaged due to hard connection is avoided, and the stability of the whole tank body is improved.
In addition, in order to prevent gas in the external environment from entering the tank body during the liquid discharge process of the liquid discharge port 17, the bottom of the exhaust cavity 5b is connected with the liquid discharge port 17 through a bent pipe 16.
In order to better understand the gas-liquid separator of the third structural form provided by the present invention, the following description will take the gas-liquid separator as an example, which is installed on the hydrogen production side of the hydrogen production system by electrolyzing water, and refer to fig. 3 to describe the specific operation process of the gas-liquid separator:
crude hydrogen raw material enters a separation space at the lower end of a tank body 1 from a crude gas inlet 11 of the tank body, gas-liquid two phases are subjected to primary separation in a bottom space of the tank body 1 due to gravity difference, the gas carrying a trace amount of moisture further separates the gas-liquid two phases in a gas-liquid separation part 2 (such as a wire mesh demister), all separated liquid phases fall to the bottommost part of the tank body 1 through gravity and flow out of the tank body 1 from a liquid phase outlet 13, the rising gas phase enters the bottom of an inner cylinder 4 of an electric heater 40, the rising gas phase temperature is continuously raised under the heating of the electric heater 40, after reaching a preset temperature, high-temperature gas leaves from a gas phase outlet 41 of the inner cylinder 4 and enters a catalyst loading cavity 5a of a carrier cavity 5, the gas phase flows from top to bottom and passes through a deoxygenation catalyst in the catalyst loading cavity 5a continuously, and deoxygenation reaction is carried out on the deoxygenation catalyst, a small amount of water diversion is generated after deoxidation, at the moment, the water in the gas phase is cooled and separated out by the deoxidized gas-water mixture through the cooler 6, the separated water enters the bent pipe 16 (such as a U-shaped bend) under the action of gravity and finally leaves the tank body 1 through the water outlet 17, so that the gas-water separation effect after deoxidation is realized, and the cooled gas phase leaves the equipment from the gas phase outlet 12.
In a further embodiment, referring to fig. 3, in order to avoid heat loss of the electric heater 40, the outer side of the tank 1 may be further provided with an insulating layer 18. The specific structural form of the insulating layer 18 may include an outer cylinder 18a sleeved outside the tank 1, and an enclosed space between the outer cylinder 18a and the outer wall of the tank 1 is filled with an insulating material 18 b. The outer cylinder 18a may be a sheet iron barrel wrapped outside the tank 1, and a thermal insulation material 18b is filled between the outer cylinder and the sheet iron barrel to reduce heat loss generated by the electric heater. It should be noted that, when the tank section corresponding to the exhaust cavity 5b (i.e., the tank wall of the tank body 1 for enclosing the exhaust cavity 5b) and the tank section corresponding to the catalyst loading cavity 5a (i.e., the tank wall of the tank body 1 for enclosing the catalyst loading cavity 5a) and the inner cylinder section corresponding to the exhaust cavity 5b (i.e., the cylinder wall of the inner cylinder 18a for enclosing the exhaust cavity 5b) and the inner cylinder section corresponding to the catalyst loading cavity 5a (i.e., the cylinder wall of the inner cylinder 18a for enclosing the catalyst loading cavity 5a) are connected by the expansion joint, the corresponding relative position of the insulating layer 18 should also have the expansion joint to ensure that the whole tank body is stably connected with the insulating layer.
In addition, when the electric heater 40 starts heating, in order to monitor the heating temperature of the gas and control the heating power of the electric heater, a temperature probe 19 extending into the catalyst loading chamber 5a may be provided on the wall of the tank body corresponding to the carrier chamber 5, and is preferably designed to be two, upper and lower, so as to detect the gas temperature change more accurately. In practical application, a metal sleeve can be specifically arranged so as to facilitate the installation of the temperature measuring probe 19.
In addition, the invention also provides a system for producing hydrogen by electrolyzing water, which comprises a gas-liquid separator, wherein the gas-liquid separator is the gas-liquid separator described in any scheme. Because the gas-liquid separator has the technical effects, the hydrogen production system by electrolyzing water with the gas-liquid separator also has the corresponding technical effects.
It should be noted that, in the present specification, the embodiments are all described in a progressive manner, each embodiment focuses on differences from other embodiments, and the same and similar parts among the embodiments may be referred to each other.
It should be understood that the use of "system," "device," "unit," and/or "module" herein is merely one way to distinguish between different components, elements, components, parts, or assemblies of different levels. However, other words may be substituted by other expressions if they accomplish the same purpose.
As used in this application and in the claims, the terms "a," "an," "the," and/or "the" are not intended to be inclusive in the singular, but rather are intended to include the plural, unless the context clearly dictates otherwise. In general, the terms "comprises" and "comprising" merely indicate that steps and elements are included which are explicitly identified, that the steps and elements do not form an exclusive list, and that a method or apparatus may include other steps or elements. An element defined by the phrase "comprising an … …" does not exclude the presence of other identical elements in the process, method, article, or apparatus that comprises the element.
In the description of the embodiments herein, "/" means "or" unless otherwise specified, for example, a/B may mean a or B; "and/or" herein is merely an association describing an associated object, and means that there may be three relationships, e.g., a and/or B, which may mean: a exists alone, A and B exist simultaneously, and B exists alone. In addition, in the description of the embodiments of the present application, "a plurality" means two or more than two.
In the following, the terms "first", "second" are used for descriptive purposes only and are not to be understood as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature.
If used in this application, the flowcharts are intended to illustrate operations performed by the system according to embodiments of the present application. It should be understood that the preceding or following operations are not necessarily performed in the exact order in which they are performed. Rather, the various steps may be processed in reverse order or simultaneously. Meanwhile, other operations may be added to the processes, or a certain step or several steps of operations may be removed from the processes.
The principles and embodiments of the present invention are explained herein using specific examples, which are presented only to assist in understanding the core concepts of the present invention. It should be noted that, for those skilled in the art, it is possible to make various improvements and modifications to the present invention without departing from the principle of the present invention, and those improvements and modifications also fall within the scope of the claims of the present invention.
Claims (15)
1. A gas-liquid separator for mounting to a corresponding gas generation side of an electrolyzed water hydrogen generation system, comprising:
the tank body (1) is provided with a crude gas inlet (11) and a gas phase outlet (12) which are sequentially arranged along the height direction;
a gas-liquid separation section (2) and a degassing section (3) which are provided in the tank body (1) and are located on a flow path between the raw gas inlet (11) and the gas phase outlet (12);
the gas-liquid separation part (2) is used for carrying out gas-liquid separation on the crude gas entering the tank body (1); the degassing part (3) is used for removing impurity gases in the crude gas.
2. The gas-liquid separator according to claim 1, wherein the gas-liquid separation section (2) comprises a first gas-liquid separation member (21) and a second gas-liquid separation member (22) arranged in this order from bottom to top, and the degassing section (3) is located between the first gas-liquid separation member (21) and the second gas-liquid separation member (22).
3. The gas-liquid separator according to claim 2, wherein the degassing section (3) is a degassing catalyst loaded between the first gas-liquid separator (21) and the second gas-liquid separator (22).
4. The gas-liquid separator according to claim 3, wherein the tank (1) is further provided with a catalyst filling port (14) and a catalyst discharge port (15) on the outside;
wherein the catalyst charging port (14) is disposed near a lower surface of the second gas-liquid separating member (22), and the catalyst discharging port (15) is disposed near an upper surface of the first gas-liquid separating member (21).
5. The gas-liquid separator according to claim 1, wherein an inner cylinder (4) is provided on the tank (1), the bottom of the inner cylinder (4) is communicated with the cavity where the gas-liquid separation part (2) is located, a carrier cavity (5) is formed by the inner cylinder (4) and the inner wall of the tank (1), an air vent (41) communicated with the carrier cavity (5) is provided on the cylinder wall of the inner cylinder (4), and the gas phase outlet (12) is communicated with the carrier cavity (5);
wherein the degassing section (3) is loaded into the carrier chamber (5).
6. The gas-liquid separator according to claim 5, wherein an electric heater (40) is provided in the inner cylinder (4).
7. The gas-liquid separator according to claim 6, wherein the electric heater (40) is equipped with a heating controller for adjusting a heating temperature of the electric heater (40).
8. The gas-liquid separator according to claim 5, wherein a holder member (52) is provided in the carrier chamber (5), the holder member (52) partitions the carrier chamber (5) into a catalyst loading chamber (5a) and a gas discharge chamber (5b) which are arranged from top to bottom, the degassing section (3) is a degassing catalyst (51) loaded in the catalyst loading chamber (5a), and the gas phase outlet (12) communicates with the gas discharge chamber (5 b).
9. The gas-liquid separator according to claim 8, wherein the tank (1) is further provided at an outer side thereof with a catalyst charging port (14) and a catalyst discharging port (15) communicating with the catalyst loading chamber (5 a);
wherein the catalyst loading port (14) is disposed proximate to a top of the catalyst loading chamber (5a) and the catalyst discharge port (15) is disposed proximate to a bottom of the catalyst loading chamber (5 a).
10. The gas-liquid separator according to claim 8, wherein a cooler (6) is further provided in the gas discharge chamber (5b), and the outside of the tank body is provided with the drain port (17) communicating with the gas discharge chamber (5b), the drain port (17) is disposed in communication with the bottom of the gas discharge chamber (5b), and the gas phase outlet (12) is disposed higher than the drain port (17) on the gas discharge chamber (5 b).
11. The gas-liquid separator according to claim 10, wherein the cooler is further equipped with a flow regulator for regulating a cooling amount of the cooler.
12. The gas-liquid separator according to claim 1, wherein the tank section corresponding to the gas-liquid separation portion (2) and the tank section corresponding to the deoxygenation portion (3) are connected by an expansion joint (8).
13. The gas-liquid separator according to any one of claims 1-12, characterized in that the tank (1) is also provided with an insulating layer (18) on its outer side.
14. The gas-liquid separator of any one of claims 1-12, wherein when the gas generation side is a hydrogen generation side, the raw gas is raw hydrogen and the impurity gas is oxygen; when the gas production side is an oxygen production side, the crude gas is crude oxygen, and the impurity gas is hydrogen.
15. A water electrolysis hydrogen production system comprising a gas-liquid separator, wherein the gas-liquid separator is according to any one of claims 1 to 14.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210640014.4A CN114832510B (en) | 2022-06-08 | 2022-06-08 | Gas-liquid separator and electrolytic water hydrogen production system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210640014.4A CN114832510B (en) | 2022-06-08 | 2022-06-08 | Gas-liquid separator and electrolytic water hydrogen production system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN114832510A true CN114832510A (en) | 2022-08-02 |
| CN114832510B CN114832510B (en) | 2024-05-14 |
Family
ID=82574495
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210640014.4A Active CN114832510B (en) | 2022-06-08 | 2022-06-08 | Gas-liquid separator and electrolytic water hydrogen production system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114832510B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114000171A (en) * | 2021-10-21 | 2022-02-01 | 中国华能集团清洁能源技术研究院有限公司 | Electrolytic hydrogen production system and method with hydrogen-oxygen recombination reactor |
Citations (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH05269305A (en) * | 1992-03-24 | 1993-10-19 | Kurita Water Ind Ltd | Deoxygenation method and device |
| JP2003267725A (en) * | 2002-03-15 | 2003-09-25 | Hitachi Zosen Corp | Method of manufacturing ammonia, its apparatus and flue gas denitrification using the manufactured ammonia |
| JP2005335962A (en) * | 2004-05-24 | 2005-12-08 | Matsushita Electric Works Ltd | Hydrogen production apparatus |
| JP2006170567A (en) * | 2004-12-17 | 2006-06-29 | Jipangu Energy:Kk | Clean steam producing method and producing system |
| CN1903703A (en) * | 2006-08-04 | 2007-01-31 | 四川亚联高科技有限责任公司 | Technological method of purifying hydrogen of hydrogen enriched gas source |
| CN103834433A (en) * | 2012-11-21 | 2014-06-04 | 中国石油化工集团公司 | Upstroke reaction separator and hydrogenation method |
| CN204494430U (en) * | 2015-03-16 | 2015-07-22 | 天津滨海新区大港汇丰汽车装饰有限公司 | A kind of vulcanization of rubber smoke catalytic incinerator |
| CN105001930A (en) * | 2015-08-12 | 2015-10-28 | 苏州苏净保护气氛有限公司 | Methane purification deoxidization system and methane purification deoxidization method |
| WO2018025282A1 (en) * | 2016-08-01 | 2018-02-08 | Luigi Patron | Hydroconversion system and method for heavy oils using a dispersed catalyst reactor in a single reaction stage with recycling, with double extraction of reaction liquid from the reactor |
| CN110540173A (en) * | 2018-05-28 | 2019-12-06 | 上海米素环保科技有限公司 | method and device suitable for purifying reformed hydrogen |
| CN111717891A (en) * | 2020-06-23 | 2020-09-29 | 广东鑫国源能源有限公司 | Novel hydrogen deoxygenator |
| WO2020241059A1 (en) * | 2019-05-24 | 2020-12-03 | 株式会社辰巳菱機 | Dehydrogenation system and catalyst-holding device |
| CN212492844U (en) * | 2020-05-06 | 2021-02-09 | 杭州快凯高效节能新技术有限公司 | Multi-section heat exchanger de-hydrocarbon comprehensive tower |
| CN112961712A (en) * | 2021-02-08 | 2021-06-15 | 赛鼎工程有限公司 | System and method for preparing LNG (liquefied Natural gas) and hydrogen by deeply purifying coke oven gas |
| CN113479905A (en) * | 2021-06-29 | 2021-10-08 | 福州大学化肥催化剂国家工程研究中心 | Self-deoxidization ammonia synthesis tower and renewable energy source ammonia synthesis system |
| CN114000171A (en) * | 2021-10-21 | 2022-02-01 | 中国华能集团清洁能源技术研究院有限公司 | Electrolytic hydrogen production system and method with hydrogen-oxygen recombination reactor |
| CN114180521A (en) * | 2022-01-04 | 2022-03-15 | 西安交通大学 | Biomass hydrogen production system and method |
| CN114345123A (en) * | 2022-01-10 | 2022-04-15 | 中国华能集团清洁能源技术研究院有限公司 | Hydrogen deoxidation and drying integrated tower and control method |
| CN114534418A (en) * | 2022-02-18 | 2022-05-27 | 阳光氢能科技有限公司 | Gas-liquid separator and hydrogen production system |
| CN114592199A (en) * | 2022-03-03 | 2022-06-07 | 上海丹通新材料有限公司 | System for preparing high-purity hydrogen by adopting pressure swing adsorption |
-
2022
- 2022-06-08 CN CN202210640014.4A patent/CN114832510B/en active Active
Patent Citations (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH05269305A (en) * | 1992-03-24 | 1993-10-19 | Kurita Water Ind Ltd | Deoxygenation method and device |
| JP2003267725A (en) * | 2002-03-15 | 2003-09-25 | Hitachi Zosen Corp | Method of manufacturing ammonia, its apparatus and flue gas denitrification using the manufactured ammonia |
| JP2005335962A (en) * | 2004-05-24 | 2005-12-08 | Matsushita Electric Works Ltd | Hydrogen production apparatus |
| JP2006170567A (en) * | 2004-12-17 | 2006-06-29 | Jipangu Energy:Kk | Clean steam producing method and producing system |
| CN1903703A (en) * | 2006-08-04 | 2007-01-31 | 四川亚联高科技有限责任公司 | Technological method of purifying hydrogen of hydrogen enriched gas source |
| CN103834433A (en) * | 2012-11-21 | 2014-06-04 | 中国石油化工集团公司 | Upstroke reaction separator and hydrogenation method |
| CN204494430U (en) * | 2015-03-16 | 2015-07-22 | 天津滨海新区大港汇丰汽车装饰有限公司 | A kind of vulcanization of rubber smoke catalytic incinerator |
| CN105001930A (en) * | 2015-08-12 | 2015-10-28 | 苏州苏净保护气氛有限公司 | Methane purification deoxidization system and methane purification deoxidization method |
| WO2018025282A1 (en) * | 2016-08-01 | 2018-02-08 | Luigi Patron | Hydroconversion system and method for heavy oils using a dispersed catalyst reactor in a single reaction stage with recycling, with double extraction of reaction liquid from the reactor |
| CN110540173A (en) * | 2018-05-28 | 2019-12-06 | 上海米素环保科技有限公司 | method and device suitable for purifying reformed hydrogen |
| WO2020241059A1 (en) * | 2019-05-24 | 2020-12-03 | 株式会社辰巳菱機 | Dehydrogenation system and catalyst-holding device |
| CN212492844U (en) * | 2020-05-06 | 2021-02-09 | 杭州快凯高效节能新技术有限公司 | Multi-section heat exchanger de-hydrocarbon comprehensive tower |
| CN111717891A (en) * | 2020-06-23 | 2020-09-29 | 广东鑫国源能源有限公司 | Novel hydrogen deoxygenator |
| CN112961712A (en) * | 2021-02-08 | 2021-06-15 | 赛鼎工程有限公司 | System and method for preparing LNG (liquefied Natural gas) and hydrogen by deeply purifying coke oven gas |
| CN113479905A (en) * | 2021-06-29 | 2021-10-08 | 福州大学化肥催化剂国家工程研究中心 | Self-deoxidization ammonia synthesis tower and renewable energy source ammonia synthesis system |
| CN114000171A (en) * | 2021-10-21 | 2022-02-01 | 中国华能集团清洁能源技术研究院有限公司 | Electrolytic hydrogen production system and method with hydrogen-oxygen recombination reactor |
| CN114180521A (en) * | 2022-01-04 | 2022-03-15 | 西安交通大学 | Biomass hydrogen production system and method |
| CN114345123A (en) * | 2022-01-10 | 2022-04-15 | 中国华能集团清洁能源技术研究院有限公司 | Hydrogen deoxidation and drying integrated tower and control method |
| CN114534418A (en) * | 2022-02-18 | 2022-05-27 | 阳光氢能科技有限公司 | Gas-liquid separator and hydrogen production system |
| CN114592199A (en) * | 2022-03-03 | 2022-06-07 | 上海丹通新材料有限公司 | System for preparing high-purity hydrogen by adopting pressure swing adsorption |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114000171A (en) * | 2021-10-21 | 2022-02-01 | 中国华能集团清洁能源技术研究院有限公司 | Electrolytic hydrogen production system and method with hydrogen-oxygen recombination reactor |
Also Published As
| Publication number | Publication date |
|---|---|
| CN114832510B (en) | 2024-05-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US9789433B2 (en) | Apparatus for in-situ production of low dissolved hydrogen sulfide, degassed, sulfur from Claus sulfur recovery | |
| CN111334672B (en) | Energy-saving magnesium purification device and purification process thereof | |
| CN114832510A (en) | Gas-liquid separator and water electrolysis hydrogen production system | |
| JP2011256099A (en) | Apparatus for producing polycrystalline silicon | |
| US6579438B1 (en) | Molten salt electrolytic cell having metal reservoir | |
| CN203687669U (en) | Acid gas condenser | |
| JP2001009265A (en) | Catalytic device for methanol synthesis and method for synthesizing methanol | |
| CN211999864U (en) | Energy-saving magnesium purification device | |
| CN219002011U (en) | Triethylene glycol reflux control equipment | |
| CN217179726U (en) | Calibration device of liquid level sensor | |
| CN213159445U (en) | Sulfur hexafluoride and hexafluoroethane rectification control system | |
| CN116966616A (en) | Reaction rectifying tower, device and method for co-producing methyl ethyl carbonate and diethyl carbonate | |
| CN211799799U (en) | Laboratory biochemical gas separation and purification device | |
| CN110553474B (en) | Horizontal supercritical drying device and horizontal supercritical reaction system | |
| CN218465958U (en) | Alkaline water electrolysis hydrogen production waste heat utilization equipment | |
| CN221131682U (en) | Reaction adsorption tower and desorption system with same | |
| CN206444581U (en) | A kind of methyl alcohol synthetic reactor | |
| CN217887440U (en) | Novel adsorption column | |
| CN215085051U (en) | Continuous phase splitting tank for normal temperature condensation material | |
| CN215209286U (en) | Novel liquefied gas separation device | |
| CN212769860U (en) | Mixed gas separation device | |
| CN212504658U (en) | Stabilizer system in benzene hydrogenation process | |
| CN215506256U (en) | Integrated washing tower for cold hydrogenation | |
| CN215939020U (en) | Rectifying column reboiler heating device based on sodium methoxide production technology | |
| CN219023842U (en) | Electronic hydrochloric acid absorption system |
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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |