CN114904359A - Device for selectively removing CO and using method thereof - Google Patents
Device for selectively removing CO and using method thereof Download PDFInfo
- Publication number
- CN114904359A CN114904359A CN202210480617.2A CN202210480617A CN114904359A CN 114904359 A CN114904359 A CN 114904359A CN 202210480617 A CN202210480617 A CN 202210480617A CN 114904359 A CN114904359 A CN 114904359A
- Authority
- CN
- China
- Prior art keywords
- cavity
- reaction
- hydrogen
- catalytic combustion
- main body
- 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
Images
Classifications
-
- 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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0407—Constructional details of adsorbing systems
- B01D53/0438—Cooling or heating systems
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/44—Details; Accessories
- F23G5/46—Recuperation of heat
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
- F23G7/07—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases in which combustion takes place in the presence of catalytic material
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
- H01M8/0662—Treatment of gaseous reactants or gaseous residues, e.g. cleaning
- H01M8/0668—Removal of carbon monoxide or carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
- B01D2259/40098—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating with other heating means
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/50—Fuel cells
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Organic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Electrochemistry (AREA)
- Sustainable Energy (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Sustainable Development (AREA)
- Life Sciences & Earth Sciences (AREA)
- Incineration Of Waste (AREA)
Abstract
The invention belongs to the technical field of energy environment, and discloses a device for selectively removing CO and a using method thereof. Two sets of symmetrical device main parts are arranged, when one set of device is saturated in adsorption, a desorption procedure is started, the other set of device is selected for further adsorption, and the treatment efficiency is improved. The desorption energy of CO is provided by a part of the catalytic combustion process of hydrogen-rich gas and air to be treated, and no additional heat source is needed. The desorbed CO is subjected to catalytic combustion reaction in the catalytic combustion cavity, the released energy further provides energy for desorption, and the product is CO 2 Without polluting the environmentAnd (6) dyeing. The air feeding cavity, the catalytic combustion cavity and the CO reaction cavity are arranged alternately, the structure is compact, and meanwhile, the exchange of gas and heat can be ensured to be more sufficient. The heat exchanger is arranged at a combustion tail gas outlet connected with the catalytic combustion cavity, so that the waste heat in the tail gas can be fully recovered, and the energy utilization rate is improved to the maximum extent.
Description
Technical Field
The invention belongs to the technical field of energy environment, and relates to a device for selectively removing CO and a using method thereof.
Background
The fuel cell is an important technology for efficiently converting chemical energy of fuel into electric energy, does not need Carnot to be circulated in the using process, and has high energy conversion rate. The raw materials are hydrogen and oxygen, the product is water, and the device does not pollute the environment and is an environment-friendly energy conversion device. The fuel cell technology is considered as one of the novel environment-friendly and efficient power generation technologies in the 21 st century, and is now applied to traffic power supplies, fixed power supplies, portable power supplies and the like.
Proton Exchange Membrane Fuel Cells (PEMFCs) are the fifth generation fuel cells which are rapidly developing after Alkaline Fuel Cells (AFCs), Phosphoric Acid Fuel Cells (PAFCs), Molten Carbonate Fuel Cells (MCFCs), and Solid Oxide Fuel Cells (SOFCs) and have the lowest operating temperature, the highest specific energy, the fastest start-up, the longest lifetime, and the widest application, and are listed as the first of ten scientific and technological new technologies in the 21 st century in the social investigation results of the U.S. journal.
However, CO has a poisoning effect on the electrode of PEMFC, and even if a very small amount of CO is contained in the raw material gas, it may have a fatal influence on the electrode of PEMFC. Although pure hydrogen is the most ideal raw material gas of the PEMFC, the preparation cost, the storage and transportation cost and the safety are poor, so that the scale use of the PEMFC is not facilitated. On-site hydrogen production is a more economical and feasible option for direct use with PEMFCs, but the product hydrogen requires deep removal of CO from the hydrogen-rich gas before entering the fuel cell.
CO selective oxidation is the current treatmentOne of the common methods for trace amounts of CO in hydrogen rich gas. The principle is that oxygen is introduced in the reforming process to convert CO into CO 2 . However, the oxygen-rich environment of the process results in some loss of hydrogen and requires an additional power or heat source. In addition, the process requires the participation of a catalyst to ensure that CO is oxidized preferentially to hydrogen. However, some impurity components in the hydrogen-rich gas can poison the catalyst, leading to deactivation of the catalyst over time; some noble metal catalysts are too costly to reuse; the thermal stability, catalytic activity and the like of the non-noble metal catalyst cannot meet the process requirements. CO can emit a large amount of heat in the oxidation process, if the materials are not uniformly distributed in the reaction process, local overheating is easily caused, and the requirements on the heat resistance of the device and the catalyst are high. At present, the technology is difficult to remove the trace CO in the hydrogen-rich gas to below 0.2 ppm.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention provides the device for selectively removing CO and the using method thereof.
The above purpose of the invention is realized by the following technical scheme:
a device for selectively removing CO comprises two reaction device main bodies, wherein each reaction device main body is a vertical device and is sequentially provided with an air feeding cavity, a catalytic combustion cavity and a CO reaction cavity from outside to inside; 0.5-3mm thin walls are arranged between the catalytic combustion cavity and the CO reaction cavity at intervals; the lower half part between the catalytic combustion cavity and the air feeding cavity is a thin-wall interval, and the upper half part is a thin-wall interval with non-uniformly distributed through holes; the CO reaction cavity is positioned at the central position of the reaction device main body, a hydrogen-rich gas inlet is arranged above the top of the reaction device main body, and the catalytic combustion cavity and the CO reaction cavity of each reaction device main body are respectively connected with the hydrogen-rich gas inlet through pipelines; and the pipeline is correspondingly and respectively provided with a hydrogen-rich gas inlet valve of the combustion cavity and a hydrogen-rich gas inlet valve of the CO reaction cavity; the top of the CO reaction cavity and the top of the catalytic combustion cavity are provided with connecting pipelines, and the pipelines are provided with CO reaction cavity desorption gas outlet valves; the side wall of the reaction device main body is provided with an air inlet, and the bottom of a catalytic combustion cavity in the reaction device main body is connected with a heat exchanger through a pipeline; the bottom of the CO reaction cavity is provided with a product gas outlet pipeline which is provided with a product gas outlet valve.
Furthermore, flowmeters are respectively arranged at the air inlet and the hydrogen-rich gas inlet; to provide effective control of the catalytic combustion reaction rate.
Furthermore, pressure sensors are respectively arranged at the air feeding cavity, the catalytic combustion cavity and the CO reaction cavity.
Furthermore, a CO concentration monitor is arranged at the connecting pipeline of the CO reaction cavity and the catalytic combustion cavity so as to monitor the desorption process of the CO reaction cavity.
Further, a CO selective adsorbent is arranged in the CO reaction cavity; the catalytic combustion cavity is filled with a catalytic combustion catalyst;
further, the catalytic combustion catalyst includes, but is not limited to, Pd-based, Pt-based, Rh-based, Ce-based, Zr-based, La-based catalysts; when the catalytic combustion catalyst is used, any one or more of the catalytic combustion catalysts is adopted;
furthermore, the upper half parts of the catalytic combustion cavity and the air feeding cavity are thin-walled intervals with non-uniform through holes; the aperture of the through hole is 1-5 mm.
Further, the heat exchanger is arranged at a tail gas outlet of the main body of the reaction device; so as to fully recycle the waste heat. The tail end of the heat exchanger is provided with a combustion tail gas outlet;
further, the two reaction device bodies are symmetrically arranged. The two reaction device main bodies are symmetrically distributed, when one reaction device main body adsorbs CO to reach saturation, the desorption process is started, the other reaction device main body is started to adsorb simultaneously, and the CO adsorption process can be continuously carried out.
Another purpose of the present invention is to claim a method for using the above device, which specifically comprises the following steps:
s1, checking the air tightness of a device, and starting a reaction device;
s2, the hydrogen-rich gas enters the CO reaction cavity of any reaction device main body from the hydrogen-rich gas inlet, at the moment, CO contained in the hydrogen-rich gas is efficiently adsorbed by the selective adsorbent in the adsorption cavity, and the product gas is discharged from the product gas outlet.
And S3, stopping air inlet to the CO reaction cavity of the main body of the reaction device when the main body of the reaction device is saturated in CO adsorption. Meanwhile, hydrogen-rich gas is introduced into the catalytic combustion chamber of the reaction device main body, and air is introduced into the air feeding chamber of the reaction device main body. Air diffuses to the catalytic combustion cavity through the through hole between the catalytic combustion cavity and the air feeding cavity, and at the moment, hydrogen-oxygen catalytic combustion reaction occurs in the catalytic combustion cavity under the action of the catalyst to supply heat for the CO reaction cavity. The CO reaction cavity generates a CO desorption process under the heating condition, and the separated CO is introduced into the catalytic combustion cavity to perform catalytic combustion reaction with air. And the combustion tail gas of the CO and the hydrogen is discharged through a combustion tail gas outlet, and the waste heat in the combustion process is recovered through a heat exchanger. And after the desorption process is finished, stopping introducing gas into the air feeding cavity and the catalytic combustion cavity, closing the combustion tail gas outlet, and waiting for the main body of the reaction device to cool. In synchronization with the process, the hydrogen-rich gas is introduced into the CO reaction chamber of the other reaction device main body, at the moment, the CO removal of the hydrogen-rich gas is carried out in the reaction device main body, and the product gas is discharged from the product gas outlet.
And S4, when the CO adsorption of the other reaction device main body is saturated, performing the desorption process of the reaction device main body and starting the adsorption process of the previous reaction device main body.
Further, the selective adsorbent includes, but is not limited to, copper-based adsorbents, molecular sieve-based adsorbents, zeolite-based adsorbents, activated nickel, porous carbon; when the selective adsorbent is used, any one or more of the selective adsorbents is adopted;
in the device provided by the invention, the physical adsorption means is selected for removing the trace CO in the hydrogen-rich gas, so that the loss of part of hydrogen in the selective catalytic combustion process is avoided. The absorption of CO can be carried out at normal temperature and normal pressure without additional heating or pressurizing conditions. Two sets of symmetrical device main parts are arranged, when one set of device is saturated in adsorption, a desorption procedure is started, the other set of device is selected for further adsorption, and the treatment efficiency is improved. CO removalThe additional energy is provided by a catalytic combustion process of a part of the hydrogen-rich gas and air (oxygen) to be treated, and no additional heat source is needed. The desorbed CO is subjected to catalytic combustion reaction in the catalytic combustion cavity, the released energy further provides energy for desorption, and the product is CO 2 And the environment is not polluted. The air feeding cavity, the catalytic combustion cavity and the CO reaction cavity are arranged alternately, the structure is compact, and meanwhile, the exchange of gas and heat can be ensured to be more sufficient. The air feeding cavity and the catalytic combustion cavity are separated by thin walls, and the thin walls of the upper half part are provided with non-uniformly distributed through holes of 1-5 mm. The design can ensure that hydrogen and air are in full contact reaction, improve the utilization rate of materials, ensure uniform mixing of the materials and avoid catalyst sintering inactivation caused by local overheating of a reaction device. The catalytic combustion process of air and hydrogen can be carried out at normal temperature and normal pressure without adding other conditions. The heat exchanger is arranged at a combustion tail gas outlet connected with the catalytic combustion cavity, so that the waste heat in the tail gas can be fully recovered, and the energy utilization rate is improved to the maximum extent.
Compared with the prior art, the invention has the beneficial effects that:
(1) the air feeding cavity, the catalytic combustion cavity and the CO reaction cavity are highly integrated, so that the reaction device has a compact structure, and the problems of poor integration level, large occupied area and the like of a common reaction device are solved;
(2) the heat exchange between two adjacent cavities of the catalytic combustion cavity and the CO reaction cavity is reasonably matched, the energy of the raw material gas is fully utilized to supply for the desorption process of CO, and meanwhile, a heat exchanger is arranged at the outlet of the catalytic combustion tail gas to fully recover the waste heat of the tail gas, so that the energy efficiency of the whole device is greatly improved;
(3) through the reasonable through-hole distribution that sets up between air feed chamber and the catalytic combustion chamber, improve the insufficient problem of material mixing in the reaction unit finite space, avoid local overheated emergence, improve raw materials utilization efficiency. The reaction device can remove the carbon monoxide in the feed gas containing 50-75% of hydrogen by volume concentration from 0.1-2.0% to below 1-0.2 ppm.
Drawings
FIG. 1 is a schematic diagram of a selective CO removal apparatus according to the present invention;
FIG. 2 is a plan view of a main body a of the reaction apparatus of the present invention;
FIG. 3 is a schematic view of the configuration of the wall between the air feed chamber and the catalytic combustion chamber of the present invention;
in the figure: 1. the device comprises combustion chamber hydrogen-rich gas inlet valves a, 2, CO reaction chamber hydrogen-rich gas inlet valves a, 3, CO reaction chamber desorption gas outlet valves a, 4, air feeding chambers a, 5, catalytic combustion chambers a, 6, CO reaction chambers a, 7, product gas outlet valves a, 8, hydrogen-rich gas inlets 9, combustion tail gas outlets a, 10, heat exchangers a, 11, combustion chamber hydrogen-rich gas inlet valves b, 12, air inlets a, 13, CO reaction chamber desorption gas outlet valves b, 14, CO reaction chamber hydrogen-rich gas inlet valves b, 15, heat exchangers b, 16, air feeding chambers b, 17, catalytic combustion chambers b, 18, CO reaction chambers b, 19, product gas outlet valves b, 20, combustion tail gas outlets b, 21, air inlets b, 22, reaction device bodies a, 23 and reaction device bodies b.
Detailed Description
While the invention will be described in connection with certain embodiments and examples, which are set forth below, it is intended that the present invention shall be illustrative, but not limiting, and that various other modifications and equivalents may be made thereto without departing from the spirit and scope of the invention as set forth in the claims. The combustion chamber hydrogen-rich gas inlet valve a, the CO reaction chamber desorption gas outlet valve a, the product gas outlet valve a, the heat exchanger a, the combustion chamber hydrogen-rich gas inlet valve b, the CO reaction chamber desorption gas outlet valve b, the CO reaction chamber hydrogen-rich gas inlet valve b, the heat exchanger b, the product gas outlet valve b, the flowmeter, the pressure sensor and the CO concentration monitor which are connected with the PLC system in the embodiment do not limit a specific model, and the working function of the system is realized.
Example 1
A device for selectively removing CO, as shown in fig. 1-3, comprises two reaction device bodies: a reaction device main body a 22 and a reaction device main body b23, wherein both the reaction device main bodies are vertical devices,
the reaction device main body a 22 comprises an air feeding cavity a 4, a catalytic combustion cavity a5 and a CO reaction cavity a6 which are arranged from outside to inside in sequence; a thin wall interval of 0.5-3mm is arranged between the catalytic combustion cavity a5 and the CO reaction cavity a 6; the lower half part between the catalytic combustion cavity a5 and the air feeding cavity a 4 is a thin-wall interval, and the upper half part is a thin-wall interval with non-uniform through holes; the CO reaction cavity a6 is positioned at the central position of the reaction device main body a 22, a hydrogen-rich gas inlet 8 is arranged above the top of the reaction device main body a 22, and the catalytic combustion cavity a5 and the CO reaction cavity a6 are respectively connected with the hydrogen-rich gas inlet 8 through pipelines; and the pipeline is correspondingly and respectively provided with a combustion chamber hydrogen-rich gas inlet valve a1 and a CO reaction chamber hydrogen-rich gas inlet valve a 2; the top of the CO reaction cavity a6 and the top of the catalytic combustion cavity a5 are provided with connecting pipelines, and the pipelines are provided with CO reaction cavity desorption gas outlet valves a 3; the side wall of the reaction device main body a 22 is provided with an air inlet a 12, and the bottom of a catalytic combustion chamber a5 in the reaction device main body a 22 is connected with a heat exchanger a10 through a pipeline; a product gas outlet pipeline is arranged at the bottom of the CO reaction cavity a6, and a product gas outlet valve a 7 is arranged on the pipeline;
the reaction device main body b23 comprises an air feeding cavity b 16, a catalytic combustion cavity b 17 and a CO reaction cavity b 18 which are arranged from outside to inside in sequence; a thin wall interval of 0.5-3mm is arranged between the catalytic combustion cavity b 17 and the CO reaction cavity b 18; the lower half part between the catalytic combustion cavity b 17 and the air feeding cavity b 16 is a thin-wall interval, and the upper half part is a thin-wall interval with non-uniform through holes; the CO reaction cavity b 18 is positioned at the central position of the reaction device main body b23, a hydrogen-rich gas inlet 8 is arranged above the top of the reaction device main body b23, and the catalytic combustion cavity b 17 and the CO reaction cavity b 18 are respectively connected with the hydrogen-rich gas inlet 8 through pipelines; and the pipeline is correspondingly and respectively provided with a combustion chamber hydrogen-rich gas inlet valve b 11 and a CO reaction chamber hydrogen-rich gas inlet valve b 14; the top of the CO reaction chamber b 18 and the top of the catalytic combustion chamber b 17 are provided with connecting pipelines, and the pipelines are provided with CO reaction chamber desorption gas outlet valves b 13; the side wall of the reaction device main body b23 is provided with an air inlet b 21, and the bottom of a catalytic combustion cavity b 17 in the reaction device main body b23 is connected with a heat exchanger b 15 through a pipeline; a product gas outlet pipeline is arranged at the bottom of the CO reaction cavity b 18, and a product gas outlet valve b 19 is arranged on the pipeline;
further, flow meters are respectively arranged at the air inlet a 12, the air inlet b 21 and the hydrogen-rich gas inlet 8; to provide effective control of the catalytic combustion reaction rate.
Further, pressure sensors are respectively arranged at the air feeding cavity a 4, the catalytic combustion cavity a5, the CO reaction cavity a6, the air feeding cavity b 16, the catalytic combustion cavity b 17 and the CO reaction cavity b 18.
Further, a CO concentration monitor is respectively arranged at the connecting pipeline between the CO reaction cavity a6 and the catalytic combustion cavity a5 and the connecting pipeline between the CO reaction cavity b 18 and the catalytic combustion cavity b 17 so as to monitor the desorption process of the CO reaction cavity.
Further, CO selective adsorbents are filled in the CO reaction cavity a6 and the CO reaction cavity b 18; pd-based catalysts for catalytic combustion are filled in the catalytic combustion chamber a5 and the catalytic combustion chamber b 17;
further, the heat exchanger a10 is arranged at the tail gas outlet of the main body a 22 of the reaction device; the heat exchanger b 15 is arranged at a tail gas outlet of the main body b23 of the reaction device; so as to fully recycle the waste heat. The tail end of the heat exchanger a10 is provided with a combustion tail gas outlet a 9; the tail end of the heat exchanger b 15 is provided with a combustion tail gas outlet b 20.
The combustion chamber hydrogen-rich gas inlet valve a1, the CO reaction chamber hydrogen-rich gas inlet valve a 2, the CO reaction chamber desorption gas outlet valve a 3, the product gas outlet valve a 7, the heat exchanger a10, the combustion chamber hydrogen-rich gas inlet valve b 11, the CO reaction chamber desorption gas outlet valve b 13, the CO reaction chamber hydrogen-rich gas inlet valve b 14, the heat exchanger b 15, the product gas outlet valve b 19, the flowmeter, the pressure sensor and the CO concentration monitor are respectively connected with the PLC system.
The main body of the reaction device is two sets of vertical devices which are symmetrically arranged. Each set of the device is provided with three different functional cavities, namely an air feeding cavity, a catalytic combustion cavity and a CO reaction cavity, which are arranged in sequence. The top of the reaction device main body is provided with a hydrogen-rich gas inlet 8, the gas input of the catalytic combustion chamber in the CO desorption stage is controlled by a combustion chamber hydrogen-rich gas inlet valve, the input of the hydrogen-rich gas in the CO adsorption stage is controlled by a CO reaction chamber hydrogen-rich gas inlet valve, and the emission of the CO gas to the catalytic combustion chamber in the CO desorption stage is controlled by a CO reaction chamber desorption gas outlet valve. One side of the reaction device main body is provided with an air inlet. The bottom of the reaction device is provided with a combustion tail gas outlet and a heat exchanger so as to fully utilize the waste heat of the combustion tail gas, and meanwhile, a product gas outlet valve is arranged so as to fully control the discharge of the product gas. And a CO selective adsorbent is filled in the CO reaction cavity. The CO reaction cavity and the catalytic combustion cavity are separated by a thin wall, the lower half part of the catalytic combustion cavity and the air feeding cavity are separated by a thin wall, and the thin wall of the upper half part is provided with non-uniformly distributed through holes so as to ensure that hydrogen and air are in full contact reaction, and the utilization rate of materials is improved. Meanwhile, the uniform mixing of materials can be ensured, and the sintering and inactivation of the catalyst caused by local overheating of the main body of the reaction device are avoided.
The use method of the device for removing trace CO in the hydrogen-rich gas specifically comprises the following steps:
s1, before starting the reaction device, the air tightness of the whole device is checked firstly because the experimental process of the whole device relates to toxic or flammable and explosive gases such as carbon monoxide, hydrogen and the like. The specific operation is as follows: closing a combustion tail gas outlet a 9, a combustion tail gas outlet b 20, a product gas outlet valve a 7, a product gas outlet valve b 19, a hydrogen-rich gas inlet 8, a combustion chamber hydrogen-rich gas inlet valve a1, a CO reaction chamber hydrogen-rich gas inlet valve a 2, a CO reaction chamber desorption gas outlet valve a 3, a combustion chamber hydrogen-rich gas inlet valve b 11, a CO reaction chamber desorption gas outlet valve b 13 and a CO reaction chamber hydrogen-rich gas inlet valve b 14. Air is introduced into the reaction device main body a 22 and the reaction device main body b23 from the air inlet a 12 and the air inlet b 21, when the pressure in the air feeding cavity or the catalytic combustion cavity reaches 0.2MPa, the introduction of the air is stopped, and when the pressure is kept unchanged, the air tightness of the part is good. And (3) closing the air inlet a 12 and the air inlet b 21, opening the hydrogen-rich gas inlet 8, the hydrogen-rich gas inlet valve a 2 of the CO reaction cavity and the hydrogen-rich gas inlet valve b 14 of the CO reaction cavity, introducing air into the reaction device main body a 22 and the reaction device main body b23 through the hydrogen-rich gas inlet 8, stopping introducing the air when the pressure in the CO reaction cavity reaches 0.2MPa, and starting the device when the pressure is kept unchanged and the air tightness is good.
S2, opening a hydrogen-rich gas inlet 8, a hydrogen-rich gas inlet valve a 2 and a product gas outlet valve a 7 of the CO reaction chamber, and keeping other gas inlets, outlets and valves closed. And introducing the hydrogen-rich gas to be treated into the hydrogen-rich gas inlet 8, so that trace CO in the hydrogen-rich gas is fully adsorbed by the CO selective adsorbent filled in the CO reaction cavity a6, and discharging the gas reaching the standard through a product gas outlet valve a 7.
S3, when the main body a 22 of the reaction device reaches CO adsorption saturation, closing a hydrogen-rich gas inlet valve a 2 and a product gas outlet valve a 7 of the CO reaction cavity, stopping gas inflow to a CO adsorption cavity a6 of the main body a 22 of the reaction device, and simultaneously starting a CO desorption program of the reaction device, wherein the specific operations are as follows: and opening a hydrogen-rich gas inlet valve a1, an air inlet a 12, a CO reaction chamber desorption gas outlet valve a 3 and a combustion tail gas outlet a 9 of the combustion chamber. Air is introduced into the air inlet chamber a 4, and the air is diffused into the catalytic combustion chamber a5 through the small holes between the catalytic combustion chamber a5 and the wall surface of the air inlet chamber a 4. The hydrogen-rich gas and the air generate hydrogen-oxygen catalytic combustion reaction under the action of the catalytic combustion catalyst filled in the catalytic combustion cavity a5, and heat is transferred through the wall surface between the catalytic combustion cavity a5 and the CO reaction cavity a 6. The CO selective adsorbent in the CO reaction cavity a6 is subjected to CO desorption process under a heated condition, and the separated CO flows into the catalytic combustion cavity a5 from the CO reaction cavity desorption gas outlet valve a 3 to perform catalytic combustion reaction with air. Combustion exhaust gas (main component is CO) of the catalytic combustion chamber a5 2 And H 2 O) is discharged through a combustion tail gas outlet a 9, and the waste heat in the combustion process is recovered through a heat exchanger a 10. And a CO concentration detection device is arranged at the CO reaction cavity desorption gas outlet valve a 3, when the desorption process is detected to be finished, air is stopped to be introduced into the air inlet a 12, the combustion cavity hydrogen-rich gas inlet valve a1, the CO reaction cavity desorption gas outlet valve a 3 and the combustion tail gas outlet a 9 are closed, and the reaction device is waited for cooling. Meanwhile, the adsorption process of the other reaction device main body b23 is started, and the specific operations are as follows: and opening a hydrogen-rich gas inlet valve b 14 and a product gas outlet valve b 19 of the CO reaction chamber, and keeping a hydrogen-rich gas inlet valve b 11 of the combustion chamber and a desorption gas outlet valve b 13 of the CO reaction chamber closed. The hydrogen-rich gas to be treated is introduced into the CO reaction chamber b 18Wherein, the trace CO is fully absorbed by the CO selective absorbent filled in the CO reaction cavity b 18, and the gas reaching the standard is discharged through a product gas outlet valve b 19.
S4, when the main body b23 of the reaction device reaches CO adsorption saturation, closing a hydrogen-rich gas inlet valve b 14 and a product gas outlet valve b 19 of the CO reaction cavity, stopping gas inlet to a CO adsorption cavity b 18 of the main body b23 of the reaction device, and simultaneously starting a CO desorption program of the reaction device, wherein the specific operation is as follows: and opening a hydrogen-rich gas inlet valve b 11, an air inlet b 21, a CO reaction chamber desorption gas outlet valve b 13 and a combustion tail gas outlet b 20 of the combustion chamber. Air is introduced into the air inlet chamber b 16, and the air is diffused into the catalytic combustion chamber b 17 through the small holes formed between the catalytic combustion chamber b 17 and the wall surface of the air inlet chamber b 16. The hydrogen-rich gas and the air generate hydrogen-oxygen catalytic combustion reaction under the action of the catalytic combustion catalyst filled in the catalytic combustion cavity b 17, and heat is transferred through the wall surface between the catalytic combustion cavity b 17 and the CO reaction cavity b 18. The CO selective adsorbent in the CO reaction cavity b 18 is subjected to a CO desorption process under a heated condition, and the separated CO flows into the catalytic combustion cavity b 17 from the CO reaction cavity desorption gas outlet valve b 13 to perform catalytic combustion reaction with air. The combustion tail gas of the catalytic combustion cavity b 17 is discharged through a combustion tail gas outlet b 20, and the waste heat in the combustion process is recovered through a heat exchanger b 15. And a CO concentration detection device is arranged at the CO reaction cavity desorption gas outlet valve b 13, when the desorption process is detected to be finished, air is stopped to be introduced into the air inlet b 21, the combustion cavity hydrogen-rich gas inlet valve b 11, the CO reaction cavity desorption gas outlet valve b 13 and the combustion tail gas outlet b 20 are closed, and the reaction device is waited to be cooled. At this time, the other reaction device main body a 22 finishes the desorption of CO and the temperature reduction, and the adsorption process of the reaction device main body a 22 is started, the specific operation is the same as step S2.
The reaction device main body a 22 and the reaction device main body b23 can respectively carry out the adsorption and desorption processes of CO, and the continuity of the whole CO desorption process is ensured.
After the reaction is stable, the composition of the product gas is periodically sampled and detected at a product gas outlet so as to judge whether the reaction device provided by the invention operates normally.
The above description is only for the purpose of creating a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art can substitute or change the technical solution and the inventive concept of the present invention within the technical scope of the present invention.
Claims (8)
1. A device for selectively removing CO is characterized by comprising two reaction device main bodies, wherein each reaction device main body is a vertical device and is sequentially provided with an air feeding cavity, a catalytic combustion cavity and a CO reaction cavity from outside to inside; 0.5-3mm thin walls are arranged between the catalytic combustion cavity and the CO reaction cavity at intervals; the lower half part between the catalytic combustion cavity and the air feeding cavity is a thin-wall interval, and the upper half part is a thin-wall interval with non-uniformly distributed through holes; the CO reaction cavity is positioned at the central position of the reaction device main body, a hydrogen-rich gas inlet (8) is arranged above the top of the reaction device main body, and the catalytic combustion cavity and the CO reaction cavity of each reaction device main body are respectively connected with the hydrogen-rich gas inlet (8) through pipelines; and the pipeline is correspondingly and respectively provided with a hydrogen-rich gas inlet valve of the combustion cavity and a hydrogen-rich gas inlet valve of the CO reaction cavity; the top of the CO reaction cavity and the top of the catalytic combustion cavity are provided with connecting pipelines, and the pipelines are provided with CO reaction cavity desorption gas outlet valves; the side wall of the reaction device main body is provided with an air inlet, and the bottom of a catalytic combustion cavity in the reaction device main body is connected with a heat exchanger through a pipeline; the bottom of the CO reaction cavity is provided with a product gas outlet pipeline which is provided with a product gas outlet valve.
2. The apparatus for selectively removing CO according to claim 1, wherein the air inlet and the hydrogen-rich gas inlet (8) are respectively provided with a flow meter; and pressure sensors are respectively arranged at the air feeding cavity, the catalytic combustion cavity and the CO reaction cavity.
3. The apparatus for selectively removing CO as claimed in claim 2, wherein a CO concentration monitor is provided at a connection pipe of the CO reaction chamber and the catalytic combustion chamber.
4. The apparatus for selectively removing CO according to claim 3, wherein the CO reaction chamber is internally provided with a CO selective adsorbent; the catalytic combustion chamber is filled with a catalytic combustion catalyst.
5. The apparatus for selectively removing CO according to claim 4, wherein the heat exchanger is arranged at a tail gas outlet of the main body of the reaction apparatus; the tail end of the heat exchanger is provided with a combustion tail gas outlet.
6. The apparatus for selective removal of CO of claim 1, comprising two reaction apparatus bodies: a reaction device main body a (22) and a reaction device main body b (23), wherein the two reaction device main bodies are vertical devices,
the reaction device main body a (22) comprises an air feeding cavity a (4), a catalytic combustion cavity a (5) and a CO reaction cavity a (6) which are arranged from outside to inside in sequence; 0.5-3mm thin-wall intervals are arranged between the catalytic combustion cavity a (5) and the CO reaction cavity a (6); the lower half part between the catalytic combustion cavity a (5) and the air feeding cavity a (4) is a thin-wall interval, and the upper half part is a thin-wall interval with non-uniform through holes; the CO reaction cavity a (6) is positioned at the center of the reaction device main body a (22), a hydrogen-rich gas inlet (8) is formed above the top of the reaction device main body a (22), and the catalytic combustion cavity a (5) and the CO reaction cavity a (6) are respectively connected with the hydrogen-rich gas inlet (8) through pipelines; and the pipeline is correspondingly and respectively provided with a combustion chamber hydrogen-rich gas inlet valve a (1) and a CO reaction chamber hydrogen-rich gas inlet valve a (2); the top of the CO reaction cavity a (6) and the top of the catalytic combustion cavity a (5) are provided with connecting pipelines, and the pipelines are provided with CO reaction cavity desorption gas outlet valves a (3); the side wall of the reaction device main body a (22) is provided with an air inlet a (12), and the bottom of a catalytic combustion cavity a (5) in the reaction device main body a (22) is connected with a heat exchanger a (10) through a pipeline; a product gas outlet pipeline is arranged at the bottom of the CO reaction cavity a (6), and a product gas outlet valve a (7) is arranged on the pipeline;
the reaction device main body b (23) comprises an air feeding cavity b (16), a catalytic combustion cavity b (17) and a CO reaction cavity b (18) which are arranged from outside to inside in sequence; 0.5-3mm thin-wall intervals are arranged between the catalytic combustion cavity b (17) and the CO reaction cavity b (18); the lower half part between the catalytic combustion cavity b (17) and the air feeding cavity b (16) is a thin-wall interval, and the upper half part is a thin-wall interval with non-uniform through holes; the CO reaction cavity b (18) is positioned in the center of the reaction device main body b (23), a hydrogen-rich gas inlet (8) is formed above the top of the reaction device main body b (23), and the catalytic combustion cavity b (17) and the CO reaction cavity b (18) are respectively connected with the hydrogen-rich gas inlet (8) through pipelines; and the pipeline is correspondingly and respectively provided with a combustion chamber hydrogen-rich gas inlet valve b (11) and a CO reaction chamber hydrogen-rich gas inlet valve b (14); the top of the CO reaction cavity b (18) and the top of the catalytic combustion cavity b (17) are provided with connecting pipelines, and the pipelines are provided with CO reaction cavity desorption gas outlet valves b (13); the side wall of the reaction device main body b (23) is provided with an air inlet b (21), and the bottom of a catalytic combustion cavity b (17) in the reaction device main body b (23) is connected with a heat exchanger b (15) through a pipeline; a product gas outlet pipeline is arranged at the bottom of the CO reaction cavity b (18), and a product gas outlet valve b (19) is arranged on the pipeline; flowmeters are respectively arranged at the air inlet a (12), the air inlet b (21) and the hydrogen-rich gas inlet (8);
pressure sensors are respectively arranged at the air feeding cavity a (4), the catalytic combustion cavity a (5), the CO reaction cavity a (6), the air feeding cavity b (16), the catalytic combustion cavity b (17) and the CO reaction cavity b (18);
CO concentration monitors are respectively arranged at the connecting pipeline of the CO reaction cavity a (6) and the catalytic combustion cavity a (5) and the connecting pipeline of the CO reaction cavity b (18) and the catalytic combustion cavity b (17);
CO selective adsorbents are filled in the CO reaction cavity a (6) and the CO reaction cavity b (18); catalytic combustion catalysts are filled in the catalytic combustion cavity a (5) and the catalytic combustion cavity b (17);
the heat exchanger a (10) is arranged at a tail gas outlet of the main body a (22) of the reaction device; the heat exchanger b (15) is arranged at a tail gas outlet of the main body b (23) of the reaction device;
the tail end of the heat exchanger a (10) is provided with a combustion tail gas outlet a (9); the tail end of the heat exchanger b (15) is provided with a combustion tail gas outlet b (20).
7. The use of the apparatus for selective CO removal according to claim 5, wherein,
s1, checking the air tightness of a device, and starting a reaction device;
s2, allowing the hydrogen-rich gas to enter a CO reaction cavity of any reaction device main body from a hydrogen-rich gas inlet (8), wherein CO contained in the hydrogen-rich gas is efficiently adsorbed by a selective adsorbent in an adsorption cavity, and the product gas is discharged from a product gas outlet;
s3, stopping gas inlet to the CO reaction cavity of the reaction device main body when the CO adsorption of the reaction device main body is saturated; meanwhile, hydrogen-rich gas is introduced into a catalytic combustion cavity of the main body of the reaction device, and air is introduced into an air feeding cavity of the main body of the reaction device; air diffuses to the catalytic combustion cavity through a through hole between the catalytic combustion cavity and the air feeding cavity, and at the moment, hydrogen-oxygen catalytic combustion reaction occurs in the catalytic combustion cavity under the action of a catalyst to supply heat to the CO reaction cavity; the CO reaction cavity generates a CO desorption process under the heating condition, and the separated CO is introduced into the catalytic combustion cavity to perform catalytic combustion reaction with air; the combustion tail gas of CO and hydrogen is discharged through a combustion tail gas outlet, and the waste heat in the combustion process is recovered through a heat exchanger; after the desorption process is finished, stopping introducing gas into the air feeding cavity and the catalytic combustion cavity, closing a combustion tail gas outlet, and waiting for the temperature of the reaction device main body to be reduced; synchronously with the process, introducing the hydrogen-rich gas into a CO reaction cavity of the other reaction device main body, removing CO of the hydrogen-rich gas in the reaction device main body, and discharging the product gas from a product gas outlet;
and S4, when the CO adsorption of the other reaction device main body is saturated, performing the desorption process of the reaction device main body and starting the adsorption process of the previous reaction device main body.
8. The use method of the device for selectively removing CO according to claim 6 is characterized by comprising the following steps:
s1, before starting a reaction device, the air tightness of the whole device is checked firstly because the experimental process of the whole device relates to toxic or flammable and explosive gases such as carbon monoxide, hydrogen and the like; the specific operation is as follows: closing a combustion tail gas outlet a (9), a combustion tail gas outlet b (20), a product gas outlet valve a (7), a product gas outlet valve b (19), a hydrogen-rich gas inlet (8), a combustion chamber hydrogen-rich gas inlet valve a (1), a CO reaction chamber hydrogen-rich gas inlet valve a (2), a CO reaction chamber desorption gas outlet valve a (3), a combustion chamber hydrogen-rich gas inlet valve b (11), a CO reaction chamber desorption gas outlet valve b (13) and a CO reaction chamber hydrogen-rich gas inlet valve b (14); air is introduced into the reaction device main body a (22) and the reaction device main body b (23) from the air inlet a (12) and the air inlet b (21), when the pressure in the air feeding cavity or the catalytic combustion cavity reaches 0.2MPa, the introduction of the air is stopped, and when the pressure is kept unchanged, the air tightness of the part is good; closing an air inlet a (12) and an air inlet b (21), opening a hydrogen-rich gas inlet (8), a hydrogen-rich gas inlet valve a (2) of a CO reaction cavity and a hydrogen-rich gas inlet valve b (14) of the CO reaction cavity, introducing air into a reaction device main body a (22) and a reaction device main body b (23) through the hydrogen-rich gas inlet (8), stopping introducing the air when the pressure in the CO reaction cavity reaches 0.2MPa, and starting the device when the pressure is kept unchanged and the air tightness is good;
s2, opening a hydrogen-rich gas inlet (8), a hydrogen-rich gas inlet valve a (2) of the CO reaction chamber and a product gas outlet valve a (7) and keeping other gas inlets, outlets and valves closed; introducing the hydrogen-rich gas to be treated into the hydrogen-rich gas inlet (8), so that trace CO in the hydrogen-rich gas is fully adsorbed by the CO selective adsorbent filled in the CO reaction cavity a (6), and discharging the gas up to the standard through a product gas outlet valve a (7);
s3, when the main body a (22) of the reaction device reaches CO adsorption saturation, closing a hydrogen-rich gas inlet valve a (2) and a product gas outlet valve a (7) of the CO reaction cavity, stopping air inlet to the CO adsorption cavity a (6) of the main body a (22) of the reaction device, and simultaneously starting a CO desorption program of the reaction device, wherein the specific operation is as follows: opening a hydrogen-rich gas inlet valve a (1), an air inlet a (12), a CO reaction chamber desorption gas outlet valve a (3) and a combustion tail gas outlet a (9) of the combustion chamber; introducing air into the air feeding cavity a (4), wherein the air diffuses into the catalytic combustion cavity a (5) through small holes between the catalytic combustion cavity a (5) and the wall surface of the air feeding cavity a (4); hydrogen-rich gas and air generate hydrogen-oxygen catalytic combustion reaction under the action of a catalytic combustion catalyst filled in the catalytic combustion cavity a (5), and heat is transferred through the wall surface between the catalytic combustion cavity a (5) and the CO reaction cavity a (6); CO selective adsorbent in the CO reaction cavity a (6) is subjected to CO desorption process under heated condition, and separated CO flows into the catalytic combustion cavity a (5) from the CO reaction cavity desorption gas outlet valve a (3) to perform catalytic combustion reaction with air; the combustion tail gas of the catalytic combustion cavity a (5) is discharged through a combustion tail gas outlet a (9), and the waste heat in the combustion process is recovered through a heat exchanger a (10); a CO concentration detection device is arranged at the desorption gas outlet valve a (3) of the CO reaction chamber, when the desorption process is detected to be finished, air is stopped to be introduced into the air inlet a (12), the hydrogen-rich gas inlet valve a (1) of the combustion chamber, the desorption gas outlet valve a (3) of the CO reaction chamber and the combustion tail gas outlet a (9) are closed, and the reaction device is waited for cooling; meanwhile, the adsorption process of the other reaction device main body b (23) is started, and the specific operation is as follows: opening a hydrogen-rich gas inlet valve b (14) and a product gas outlet valve b (19) of the CO reaction chamber, and keeping a hydrogen-rich gas inlet valve b (11) and a desorption gas outlet valve b (13) of the combustion chamber closed; introducing the hydrogen-rich gas to be treated into a CO reaction chamber b (18), wherein trace CO is fully adsorbed by a CO selective adsorbent filled in the CO reaction chamber b (18), and discharging the gas reaching the standard through a product gas outlet valve b (19);
s4, when the main body b (23) of the reaction device reaches CO adsorption saturation, closing a hydrogen-rich gas inlet valve b (14) and a product gas outlet valve b (19) of the CO reaction cavity, stopping air inlet to the CO adsorption cavity b (18) of the main body b (23) of the reaction device, and simultaneously starting a CO desorption program of the reaction device, wherein the specific operation is as follows: opening a hydrogen-rich gas inlet valve b (11), an air inlet b (21), a CO reaction chamber desorption gas outlet valve b (13) and a combustion tail gas outlet b (20) of the combustion chamber; introducing air into the air feeding cavity b (16), wherein the air diffuses into the catalytic combustion cavity b (17) through small holes between the catalytic combustion cavity b (17) and the wall surface of the air feeding cavity b (16); hydrogen-rich gas and air generate hydrogen-oxygen catalytic combustion reaction under the action of a catalytic combustion catalyst filled in the catalytic combustion cavity b (17), and heat is transferred through the wall surface between the catalytic combustion cavity b (17) and the CO reaction cavity b (18); CO selective adsorbent in the CO reaction cavity b (18) is subjected to a CO desorption process under a heated condition, and the separated CO flows into the catalytic combustion cavity b (17) from the CO reaction cavity desorption gas outlet valve b (13) to perform catalytic combustion reaction with air; the combustion tail gas of the catalytic combustion cavity b (17) is discharged through a combustion tail gas outlet b (20), and the waste heat in the combustion process is recovered through a heat exchanger b (15); a CO concentration detection device is arranged at the desorption gas outlet valve b (13) of the CO reaction chamber, when the desorption process is detected to be finished, air is stopped to be introduced into the air inlet b (21), the hydrogen-rich gas inlet valve b (11) of the combustion chamber, the desorption gas outlet valve b (13) of the CO reaction chamber and the combustion tail gas outlet b (20) are closed, and the temperature of the reaction device is waited to be reduced; at this time, after the other reaction device main body a (22) has completed the desorption of CO and completed the temperature reduction, the adsorption process of the reaction device main body a (22) is started, and the specific operation is the same as step S2;
the reaction device main body a (22) and the reaction device main body b (23) can respectively carry out the adsorption and desorption processes of CO, and the continuity of the whole CO desorption process is ensured.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210480617.2A CN114904359B (en) | 2022-05-05 | 2022-05-05 | Device for selectively removing CO and application method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210480617.2A CN114904359B (en) | 2022-05-05 | 2022-05-05 | Device for selectively removing CO and application method thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN114904359A true CN114904359A (en) | 2022-08-16 |
| CN114904359B CN114904359B (en) | 2023-06-27 |
Family
ID=82766680
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210480617.2A Active CN114904359B (en) | 2022-05-05 | 2022-05-05 | Device for selectively removing CO and application method thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114904359B (en) |
Citations (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001090931A (en) * | 1999-09-22 | 2001-04-03 | Babcock Hitachi Kk | Deodorizing device |
| JP2002100386A (en) * | 2000-09-25 | 2002-04-05 | Sanyo Electric Co Ltd | Fuel cell system and starting method |
| CA2324699A1 (en) * | 2000-10-27 | 2002-04-27 | Questair Technologies Inc. | Carbon monoxide removal from hydrogen feed to fuel cell |
| US20020110504A1 (en) * | 2001-02-09 | 2002-08-15 | Gittleman Craig S. | Carbon monoxide adsorption for carbon monoxide clean-up in a fuel cell system |
| JP2007042371A (en) * | 2005-08-02 | 2007-02-15 | Toyota Motor Corp | Fuel cell system |
| JP2010101303A (en) * | 2008-09-25 | 2010-05-06 | Toyota Motor Corp | Exhaust emission control device of internal combustion engine |
| CN107233779A (en) * | 2017-08-04 | 2017-10-10 | 青岛蓝皑环保节能有限公司 | A kind of organic exhaust gas desorption catalyzing burning all-in-one |
| CN107973271A (en) * | 2017-12-04 | 2018-05-01 | 大连大学 | The reaction unit and application method of micro CO in a kind of removing hydrogen-rich gas |
| CN208237892U (en) * | 2018-04-04 | 2018-12-14 | 河北宏顺旺吉环保科技有限公司 | The system of catalysis burning processing VOCs exhaust gas |
| CN208372756U (en) * | 2018-01-25 | 2019-01-15 | 杭州润信科技有限公司 | Container-type organic exhaust gas adsorption purification-catalytic combustion regenerative skid-mounted device |
| CN109499261A (en) * | 2018-12-03 | 2019-03-22 | 四川天科技股份有限公司 | The removing system and method for CO in a kind of used in proton exchange membrane fuel cell hydrogen |
| CN109833726A (en) * | 2019-03-06 | 2019-06-04 | 苏州弘维环境科技有限公司 | A kind of dedicated molecular sieve used zeolite concentration CO desorption apparatus of exhaust-gas treatment |
| CN212855120U (en) * | 2020-05-14 | 2021-04-02 | 领跃电子科技（珠海）有限公司 | Emission device for purifying volatile organic compounds |
-
2022
- 2022-05-05 CN CN202210480617.2A patent/CN114904359B/en active Active
Patent Citations (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001090931A (en) * | 1999-09-22 | 2001-04-03 | Babcock Hitachi Kk | Deodorizing device |
| JP2002100386A (en) * | 2000-09-25 | 2002-04-05 | Sanyo Electric Co Ltd | Fuel cell system and starting method |
| CA2324699A1 (en) * | 2000-10-27 | 2002-04-27 | Questair Technologies Inc. | Carbon monoxide removal from hydrogen feed to fuel cell |
| US20020110504A1 (en) * | 2001-02-09 | 2002-08-15 | Gittleman Craig S. | Carbon monoxide adsorption for carbon monoxide clean-up in a fuel cell system |
| JP2007042371A (en) * | 2005-08-02 | 2007-02-15 | Toyota Motor Corp | Fuel cell system |
| JP2010101303A (en) * | 2008-09-25 | 2010-05-06 | Toyota Motor Corp | Exhaust emission control device of internal combustion engine |
| CN107233779A (en) * | 2017-08-04 | 2017-10-10 | 青岛蓝皑环保节能有限公司 | A kind of organic exhaust gas desorption catalyzing burning all-in-one |
| CN107973271A (en) * | 2017-12-04 | 2018-05-01 | 大连大学 | The reaction unit and application method of micro CO in a kind of removing hydrogen-rich gas |
| CN208372756U (en) * | 2018-01-25 | 2019-01-15 | 杭州润信科技有限公司 | Container-type organic exhaust gas adsorption purification-catalytic combustion regenerative skid-mounted device |
| CN208237892U (en) * | 2018-04-04 | 2018-12-14 | 河北宏顺旺吉环保科技有限公司 | The system of catalysis burning processing VOCs exhaust gas |
| CN109499261A (en) * | 2018-12-03 | 2019-03-22 | 四川天科技股份有限公司 | The removing system and method for CO in a kind of used in proton exchange membrane fuel cell hydrogen |
| CN109833726A (en) * | 2019-03-06 | 2019-06-04 | 苏州弘维环境科技有限公司 | A kind of dedicated molecular sieve used zeolite concentration CO desorption apparatus of exhaust-gas treatment |
| CN212855120U (en) * | 2020-05-14 | 2021-04-02 | 领跃电子科技（珠海）有限公司 | Emission device for purifying volatile organic compounds |
Non-Patent Citations (1)
| Title |
|---|
| 巩远辉;王燕;蔡旺锋;陈益清;: "吸附浓缩-蓄热催化燃烧工艺过程研究", 现代化工, no. 05, pages 208 - 212 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN114904359B (en) | 2023-06-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP5065605B2 (en) | Hydrogen production apparatus, fuel cell system and operation method thereof | |
| US6376114B1 (en) | Reformate fuel treatment system for a fuel cell power plant | |
| CN111483978B (en) | Reforming hydrogen production device and reforming hydrogen production method | |
| CN109713342B (en) | Electrochemical ammonia reforming hydrogen production device and method | |
| US7611793B2 (en) | Fuel cell system, hydrogen gas supply unit, and method of controlling fuel cell system | |
| US6309768B1 (en) | Process for regenerating a carbon monoxide oxidation reactor | |
| JP2004284875A (en) | Hydrogen production system, and fuel cell system | |
| US6387555B1 (en) | Selective oxidizer in cell stack manifold | |
| JP2000178007A (en) | Hydrogen purifier | |
| CN114904359B (en) | Device for selectively removing CO and application method thereof | |
| JP2008308351A (en) | Pretreatment method and airtightness testing method for fuel reforming apparatus, operation pretreatment method for fuel cell power generation system | |
| JPH08138703A (en) | Fuel cell power generating system | |
| WO2023212843A1 (en) | Device for selectively removing co and use method therefor | |
| JPH03208801A (en) | Method for removing carbon monoxide in reformed gas as raw material for hydrogen | |
| JP4143028B2 (en) | Fuel cell system and operation method thereof | |
| CN114976155A (en) | Hydrogen fuel cell system combining methanol reforming and solid oxide | |
| JP2002280038A (en) | Fuel cell electric power generating system | |
| JP4455040B2 (en) | Fuel cell system and operation method thereof | |
| CN111085194A (en) | Regeneration process of nuclear power plant passive spherical dehydrogenation catalyst | |
| JP2009087726A (en) | Fuel cell system | |
| CN205933211U (en) | Selective oxidation purifies CO's methanol reforming reactor | |
| CN217881590U (en) | Hydrogen fuel cell system combining methanol reforming and solid oxide | |
| CN114477086B (en) | Methanol steam reforming hydrogen production device and starting method thereof | |
| JP4550385B2 (en) | Hydrogen production apparatus and fuel cell system | |
| JP2000021431A (en) | Method of stopping reforming equipment for fuel cell |
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 |