CN214486811U - Heat exchange type ammonia decomposition reactor - Google Patents
Heat exchange type ammonia decomposition reactor Download PDFInfo
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- CN214486811U CN214486811U CN202023016856.8U CN202023016856U CN214486811U CN 214486811 U CN214486811 U CN 214486811U CN 202023016856 U CN202023016856 U CN 202023016856U CN 214486811 U CN214486811 U CN 214486811U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- 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
Abstract
The utility model discloses a heat exchange type ammonia decomposition reactor, which comprises a cover body and a cylinder body, wherein the cover body is connected with the cylinder body, the cover body comprises an upper sealing head, the upper sealing head is provided with a decomposition gas outlet pipe and a raw material gas inlet, the cylinder body is provided with a heat medium inlet pipe and a heat medium outlet pipe, a catalytic reaction loop part is arranged in the cylinder body, the catalytic reaction loop part divides the interior of the cylinder body into a catalytic reaction loop and a heat medium gas loop, the decomposition gas outlet pipe and the raw material gas inlet are both communicated with the catalytic reaction loop, and the heat medium inlet pipe and the heat medium outlet pipe are both communicated with the heat medium gas loop; the utility model discloses a waste gas, waste material, natural gas or fossil fuel provide hot medium through the burning, indirectly provide the heat source for the catalyst pipe, and the heat source is stable, decomposes thoroughly, and residual ammonia content is low in the decomposition gas, does benefit to the long period safe operation of device, does benefit to the device and enlarges, and single set hydrogen can reach 30 ten thousand tons of hydrogen production capacity per year, does benefit to various energy comprehensive recovery and utilizes, and the operation energy consumption is low.
Description
Technical Field
The utility model relates to an ammonia decomposition hydrogen production reactor technical field, concretely relates to heat transfer formula ammonia decomposition reactor.
Background
At present, hydrogen energy automobiles are widely popularized in China, because hydrogen escape amount is large in the process of storage and transportation, and long-distance transportation is difficult, the problem of hydrogen transportation is solved by storing and transporting hydrogen in the form of ammonia, and hydrogen production is carried out by arranging a hydrogen production device on site through a heat exchange type ammonia decomposition reactor.
The existing ammonia decomposition hydrogen production reactor is generally of a single tube or a plurality of tubes, a ring tube header structure is adopted between the upper part and the lower part of the multi-tube ammonia decomposition hydrogen production reactor, a large number of refractory bricks are arranged outside a catalyst heat exchange tube, an electric furnace is adopted to supply heat, and the production capacity is generally 1000-5000 Nm3Between the hour and the hour, only a small test device can be met, and the requirement of a large device cannot be met; the temperature of a bed layer needs to be maintained at 800 ℃, the temperature of a refractory brick needs to be above 850 ℃, heat is supplied by electric furnace heat radiation, heat supply is uneven, the temperature difference between two ends of a single tube bed layer of the catalyst reaches above 300 ℃, the catalyst cannot reach an optimal reaction temperature area, part of the catalyst does not play a role of catalysis, and the ammonia content in decomposed gas is more than or equal to 1000 PPm; the raw material gas can not be preheated, the waste heat of the decomposed gas can not be recovered, the operation energy consumption is high, the device is small, and the device can not operate because a heating element, namely an electric heater, is frequently blown.
In view of the above-mentioned drawbacks, the authors of the present invention have finally obtained the present invention through long-term research and practice.
SUMMERY OF THE UTILITY MODEL
For solving the technical defect, the utility model discloses a technical scheme lie in, provide a heat transfer formula ammonia decomposition reactor, including lid and barrel, the lid with the barrel is connected, the lid includes the upper cover, the upper cover is provided with decomposition gas outlet pipe and feed gas import, the barrel is provided with heat medium import pipe and heat medium outlet pipe, be provided with catalytic reaction return circuit portion in the barrel, catalytic reaction return circuit portion will separate for catalytic reaction return circuit and heat medium gas return circuit in the barrel, the decomposition gas outlet pipe with the feed gas import all with catalytic reaction return circuit intercommunication, heat medium import pipe with the heat medium outlet pipe all with heat medium gas return circuit intercommunication, be provided with the catalyst in the catalytic reaction return circuit portion.
Preferably, the decomposed gas outlet pipe is arranged on the axes of the cover body and the cylinder body, and the raw material gas inlet is arranged on one side of the cover body; the heat medium inlet pipe is arranged at one end, close to the cover body, of the cylinder body, and the heat medium outlet pipe is arranged at one end, far away from the cover body, of the cylinder body.
Preferably, the catalytic reaction loop part comprises an upper tube plate, a catalyst tube, a lower tube plate and a first end enclosure, the upper tube plate is hermetically connected with the inner wall of the cylinder body, so that an air inlet cavity is formed between the cover body and the upper tube plate, the lower tube plate is hermetically connected with the first end enclosure to form an air outlet cavity, the decomposed gas outlet tube is communicated with the air outlet cavity, and the raw material gas inlet is communicated with the air inlet cavity; the two ends of the catalyst tube are respectively connected with the upper tube plate and the lower tube plate in a sealing manner, the gas inlet cavity is communicated with the gas outlet cavity through the catalyst tube, and the catalyst is arranged in the catalyst tube.
Preferably, the catalyst pipe is provided with a plurality of catalyst pipes, and each catalyst pipe is annularly and uniformly distributed by taking the decomposed gas outlet pipe as a center.
Preferably, a baffle plate is further arranged between the upper tube plate and the lower tube plate, and the baffle plate is fixedly connected with the catalyst tubes.
Preferably, the baffle plate comprises a first baffle plate and a second baffle plate, the first baffle plate and the second baffle plate are arranged in parallel and in a staggered manner, and the diameter of the first baffle plate is larger than that of the second baffle plate;
the center of the first baffle plate is provided with a first through hole, the decomposed gas outlet pipe is arranged in the first through hole, and the diameter difference between the first through hole and the second baffle plate is 0 cm-10 cm; a first connection hole is annularly formed in the first baffle plate, the first connection hole is arranged corresponding to the catalyst tube, and the first connection hole is fixedly connected with the corresponding tube wall of the catalyst tube;
and a second through hole is formed in the center of the second baffle plate, the second through hole corresponds to the decomposed gas outlet pipe, and the second through hole is fixedly connected with the pipe wall of the decomposed gas outlet pipe. And a second connecting hole is annularly formed in the second baffle plate, the second connecting hole is arranged corresponding to the catalyst tube, and the second connecting hole is fixedly connected with the tube wall of the corresponding catalyst tube.
Preferably, an upper end socket heat insulation material layer is arranged on the inner wall of the upper end socket, and a barrel heat insulation material layer and a lower end socket heat insulation material layer are arranged on the inner wall of the barrel heat insulation material layer.
Preferably, the upper end socket is provided with a bed layer thermocouple, and the end part of the bed layer thermocouple is arranged in the catalyst pipe; the cylinder is provided with a thermal medium thermocouple, and the end part of the thermal medium thermocouple is arranged in the thermal medium gas loop.
Preferably, a tail pipe is arranged on the first seal head, the tail pipe is arranged at the position, away from the center of one side of the lower tube plate, of the first seal head, the end, away from the first seal head, of the tail pipe is provided with a second seal head, the cylinder body is provided with a short circuit, the tail pipe is arranged in the short circuit, the end, away from the cylinder body, of the short circuit is provided with a third seal head, and a gap is formed between the second seal head and the third seal head.
Preferably, the third end socket is connected with the short joint through a short joint flange.
Compared with the prior art, the beneficial effects of the utility model reside in that: the utility model discloses a waste gas, waste material, natural gas or fossil fuel provide hot medium through the burning, indirectly provide the heat source for the catalyst pipe, and the heat source is stable, decomposes thoroughly, and residual ammonia content is low in the decomposition gas, does benefit to the long period safe operation of device, does benefit to the device and enlarges, and single set hydrogen can reach 30 ten thousand tons of hydrogen production capacity per year, does benefit to various energy comprehensive recovery and utilizes, and the operation energy consumption is low.
Drawings
Fig. 1 is a structural view of the heat-exchange ammonia decomposition reactor.
The figures in the drawings represent:
1-bed layer thermocouple; 2-a decomposed gas outlet pipe; 3-a pipe expansion joint; 4, sealing the head; 5-raw material gas inlet; 6-cover body; 7-an upper end socket heat insulation material layer; 8-an upper tube plate; 9-housing flange; 10-an upper tube plate support ring; 11-heat medium inlet pipe; 12-a cylinder body; 13-a catalyst tube; 14-cylinder heat-insulating material layer; 15-a first baffle; 16-a second baffle plate; 17-thermal medium thermocouple; 18-a lower tube sheet; 19-a first elliptical head; 20-a lower end socket heat insulation material layer; 21-heat medium outlet pipe; 22-a tail pipe; 23-short circuit; 24-a shorting flange; 25-a second elliptical head; 26-third elliptical head.
Detailed Description
The above and further features and advantages of the present invention will be described in more detail below with reference to the accompanying drawings.
Example one
As shown in fig. 1, fig. 1 is a structural view of the heat-exchange ammonia decomposition reactor. Heat transfer formula ammonia decomposition reactor includes lid 6 and barrel 12, lid 6 with barrel 12 passes through casing flange 9 and connects, lid 6 includes upper cover 4, upper cover 4 is provided with decomposition gas outlet pipe 2 and feed gas import 5, barrel 12 is provided with heat medium import pipe 11 and heat medium outlet pipe 21, be provided with catalytic reaction return circuit portion in the barrel 12, catalytic reaction return circuit portion will separate into catalytic reaction return circuit and heat medium gas return circuit in the barrel 12, decomposition gas outlet pipe 2 with feed gas import 5 all with catalytic reaction return circuit intercommunication, heat medium import pipe 11 with heat medium outlet pipe 21 all with heat medium gas return circuit intercommunication. And a catalyst is arranged in the catalytic reaction loop part.
The heat medium flows out from the heat medium outlet pipe 21 through the heat medium inlet pipe 11 and the heat medium gas loop, the reaction gas flows out from the decomposition gas outlet pipe 2 through the raw material gas inlet 5 and the catalytic reaction loop, the reaction gas in the catalytic reaction loop exchanges heat with the heat medium in the heat medium gas loop, and the decomposition operation of the reaction gas is realized under the action of the catalyst.
Generally, the decomposition gas outlet pipe 2 is disposed on the axis of the lid 6 and the cylinder 12, and the raw material gas inlet 5 is disposed on one side of the lid 6; the heat medium inlet pipe 11 is provided at an end of the cylinder 12 close to the lid 6, and the heat medium outlet pipe 21 is provided at an end of the cylinder 12 remote from the lid 6.
The catalytic reaction loop part comprises an upper tube plate 8, a catalyst tube 13, a lower tube plate 18 and a first elliptical head 19, wherein the upper tube plate 8 is connected with the inner wall of the cylinder 12 in a sealing manner, so that a closed air inlet cavity is formed between the cover body 6 and the upper tube plate 8, the lower tube plate 18 is connected with the first elliptical head 19 in a sealing manner, a closed air outlet cavity is formed, the decomposed air outlet tube 2 is communicated with the air outlet cavity, and the raw material gas inlet 5 is communicated with the air inlet cavity. The two ends of the catalyst tube 13 are respectively connected with the upper tube plate 8 and the lower tube plate 18 in a sealing manner, the gas inlet cavity is communicated with the gas outlet cavity through the catalyst tube 13, and the catalyst is arranged in the catalyst tube 13.
The catalytic reaction loop is formed inside the catalyst tube 13, inside the gas outlet cavity and inside the decomposed gas outlet tube 2, and the heat medium gas loop is formed outside the catalyst tube 13, outside the gas outlet cavity and outside the decomposed gas outlet tube 2 in the closed space formed by the upper tube plate 8 and the cylinder 12.
Preferably, the catalyst pipe 13 is provided in plurality, and each catalyst pipe 13 is annularly and uniformly distributed around the decomposed gas outlet pipe 2. The catalyst pipe 13 is a seamless steel pipe having a standard of 10X 1 to 70X 4.
Generally, the cylinder 12 is fixedly connected with the upper tube plate 8 in a welding and sealing manner through the upper tube plate support ring 10.
And the decomposed gas outlet pipe 2 is provided with a pipeline expansion joint 3 for realizing sealing connection with an external pipeline.
Example two
Preferably, a baffle plate is further arranged between the upper tube plate 8 and the lower tube plate 18, the baffle plate is fixedly connected with the catalyst tube 13, the baffle plate realizes a turbulent flow effect on a heat medium in the heat medium gas loop, and the temperature in the heat medium gas loop is ensured to be uniform so as to realize a better heat exchange effect.
Specifically, the baffle plate comprises a first baffle plate 15 and a second baffle plate 16, the first baffle plate 15 and the second baffle plate 16 are arranged in parallel and in a staggered manner, and the diameter of the first baffle plate 15 is larger than that of the second baffle plate 16.
Generally, the first baffle plate 15 is centrally provided with a first through hole in which the decomposed gas outlet pipe 2 and a part of the catalyst pipe 13 are disposed, and the diameter of the first through hole is different from the diameter of the second baffle plate 16 by 0cm to 10 cm. A first connection hole is annularly arranged on the first baffle 15, the first connection hole is arranged corresponding to the catalyst tube 13, and the first connection hole is fixedly connected with the tube wall of the corresponding catalyst tube 13.
The second baffle 16 is provided with a second through hole at the center, the second through hole is arranged corresponding to the decomposed gas outlet pipe 2, and the second through hole is fixedly connected with the pipe wall of the decomposed gas outlet pipe 2. A second connection hole is annularly formed in the second baffle 16, the second connection hole is arranged corresponding to the catalyst tube 13, and the second connection hole is fixedly connected with the tube wall of the corresponding catalyst tube 13.
Through the gap between the outer edge of the second baffle plate 16 and the inner wall of the cylinder 12, the gap between the outer edge of the first baffle plate 15 and the inner wall of the cylinder 12 and the gap in the first through hole, a variable flow channel is formed, and the turbulent flow effect of the heat medium is realized.
Preferably, an upper end enclosure heat-insulating material layer 7 is arranged on the inner wall of the upper end enclosure 4, and a cylinder heat-insulating material layer 14 and a lower end enclosure heat-insulating material layer 20 are arranged on the inner wall of the cylinder heat-insulating material layer 14, so that the heat-insulating effect of the heat-exchange ammonia decomposition reactor is improved. Generally, the upper end socket heat insulation material layer 7 and the lower end socket heat insulation material layer 20 are both spherical, and the cylinder heat insulation material layer 14 is circular.
Preferably, the upper end socket 4 is provided with a bed layer thermocouple 1, and the end part of the bed layer thermocouple 1 is arranged in the catalyst pipe 13 and used for detecting the temperature in the catalytic reaction loop; the cylinder 12 is provided with a thermal medium thermocouple 17, and the end of the thermal medium thermocouple 17 is arranged in the thermal medium gas loop and used for detecting the temperature in the thermal medium gas loop.
Preferably, a tail pipe 22 is arranged on the first elliptical head 19, the tail pipe 22 is arranged at the center position of one side of the first elliptical head 19 far away from the lower tube plate 18, and a second elliptical head 25 is arranged at the end part of the tail pipe 22 far away from the first elliptical head 19. Correspondingly, the barrel 12 is provided with a short circuit 23, the tail pipe 22 is arranged in the short circuit 23, the short circuit 23 is far away from the end part of the barrel 12 and is provided with a third elliptical seal head 26, and a gap is formed between the second elliptical seal head 25 and the third elliptical seal head 26. Preferably, the third elliptical head 26 is connected with the short joint 23 through a short joint flange 24, so that the short joint 23 can enter the inside of the cylinder 12 to perform corresponding operations such as maintenance.
And enough gap height exists between the second elliptical seal head 25 and the third elliptical seal head 26, so that the downward expansion of the whole structure is ensured, and the thermal stress is completely eliminated. The short joint 23 is connected with the third elliptical seal head 26 through the short joint flange 24, and after the short joint flange 24 is opened, the tail pipe 22 can be separated from the second elliptical seal head 25, so that the self-discharging of the catalyst can be realized.
The pipeline expansion joint 3, the upper end socket 4, the feed gas inlet 5 and the upper end socket heat-insulating material layer 7 are combined with the cover body 6 convenient for hoisting, so that the upper tube plate 8 and the upper port of the catalyst tube 13 can be completely exposed in the visual field, and the filling and the maintenance of the catalyst are facilitated.
The decomposed gas outlet pipe 2, the upper tube plate 8, the catalyst pipe 13, the first baffle plate 15, the second baffle plate 16, the lower tube plate 18, the first elliptical head 19, the tail pipe 22 and the second elliptical head 25 are combined into a catalytic reaction loop assembly which can be lifted independently.
The shell flange 9, the heat medium inlet pipe 11, the cylinder 12, the cylinder heat-insulating material layer 14, the lower end socket heat-insulating material layer 20, the heat medium outlet pipe 21, the short joint 23, the short joint flange 24 and the third elliptical end socket 26 are combined into a heat medium gas closed space, and heat is transferred to a catalyst bed layer in the catalyst pipe 13 by the heat medium through the pipe wall of the catalyst pipe 13.
Generally, the catalyst tube 13 is filled with a ruthenium (Ru) catalyst, and has good low-temperature activity.
The temperature of the catalyst pipe 13 is maintained at 450-550 ℃, and the temperature of the heat medium is 550-650 ℃.
The heat medium for supplying heat to the catalyst tubes 13 may be provided by combustion using exhaust gas, waste material, natural gas, or fossil fuel.
The utility model discloses a waste gas, waste material, natural gas or fossil fuel provide hot medium through the burning, indirectly provide the heat source for the catalyst pipe, and the heat source is stable, decomposes thoroughly, and residual ammonia content is low in the decomposition gas, does benefit to the long period safe operation of device, does benefit to the device and enlarges, and single set hydrogen can reach 30 ten thousand tons of hydrogen production capacity per year, does benefit to various energy comprehensive recovery and utilizes, and the operation energy consumption is low.
The foregoing is only a preferred embodiment of the present invention, which is illustrative, not limiting. Those skilled in the art will appreciate that many variations, modifications, and equivalents may be made thereto without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (9)
1. A heat exchange type ammonia decomposition reactor is characterized by comprising a cover body and a cylinder body, wherein the cover body is connected with the cylinder body, the cover body comprises an upper end enclosure, the upper end enclosure is provided with a decomposition gas outlet pipe and a raw material gas inlet, the cylinder body is provided with a heat medium inlet pipe and a heat medium outlet pipe, a catalytic reaction loop part is arranged in the cylinder body, the catalytic reaction loop part divides the inside of the cylinder body into a catalytic reaction loop and a heat medium gas loop, the decomposition gas outlet pipe and the raw material gas inlet are both communicated with the catalytic reaction loop, the heat medium inlet pipe and the heat medium outlet pipe are both communicated with the heat medium gas loop, and a catalyst is arranged in the catalytic reaction loop part;
the catalytic reaction loop part comprises an upper tube plate, a catalyst tube, a lower tube plate and a first seal head, the upper tube plate is hermetically connected with the inner wall of the cylinder body, so that an air inlet cavity is formed between the cover body and the upper tube plate, the lower tube plate is hermetically connected with the first seal head to form an air outlet cavity, the decomposed gas outlet tube is communicated with the air outlet cavity, and the raw material gas inlet is communicated with the air inlet cavity; the two ends of the catalyst tube are respectively connected with the upper tube plate and the lower tube plate in a sealing manner, the gas inlet cavity is communicated with the gas outlet cavity through the catalyst tube, and the catalyst is arranged in the catalyst tube.
2. The heat exchange ammonia decomposition reactor of claim 1, wherein the decomposition gas outlet pipe is disposed on an axis of the cover and the cylinder, and the feed gas inlet is disposed at one side of the cover; the heat medium inlet pipe is arranged at one end, close to the cover body, of the cylinder body, and the heat medium outlet pipe is arranged at one end, far away from the cover body, of the cylinder body.
3. The heat-exchange ammonia decomposition reactor according to claim 1, wherein the catalyst tube is provided in plurality, and each of the catalyst tubes is annularly and uniformly distributed centering on the decomposed gas outlet pipe.
4. The heat-exchange ammonia decomposition reactor of claim 1 further comprising a baffle plate disposed between the upper tube plate and the lower tube plate, the baffle plate being fixedly attached to the catalyst tubes.
5. The heat-exchange ammonia decomposition reactor of claim 4, wherein the baffles comprise a first baffle and a second baffle, the first baffle and the second baffle being arranged in parallel and staggered, and the first baffle having a diameter greater than the diameter of the second baffle;
the center of the first baffle plate is provided with a first through hole, the decomposed gas outlet pipe is arranged in the first through hole, and the diameter difference between the first through hole and the second baffle plate is 0 cm-10 cm; a first connection hole is annularly formed in the first baffle plate, the first connection hole is arranged corresponding to the catalyst tube, and the first connection hole is fixedly connected with the corresponding tube wall of the catalyst tube;
the center of the second baffle plate is provided with a second through hole, the second through hole corresponds to the decomposed gas outlet pipe, the second through hole is fixedly connected with the pipe wall of the decomposed gas outlet pipe, a second connecting hole is annularly arranged on the second baffle plate and corresponds to the catalyst pipe, and the second connecting hole is fixedly connected with the pipe wall of the corresponding catalyst pipe.
6. The heat-exchange ammonia decomposition reactor according to claim 1, wherein an upper head thermal insulation material layer is disposed on an inner wall of the upper head, and a cylinder thermal insulation material layer and a lower head thermal insulation material layer are disposed on an inner wall of the cylinder thermal insulation material layer.
7. The heat-exchange ammonia decomposition reactor of claim 1, wherein the top head is provided with a bed thermocouple, the end of the bed thermocouple being disposed within the catalyst tube; the cylinder is provided with a thermal medium thermocouple, and the end part of the thermal medium thermocouple is arranged in the thermal medium gas loop.
8. The heat-exchange ammonia decomposition reactor according to claim 1, wherein a tail pipe is disposed on the first head, the tail pipe is disposed at a central position of a side of the first head away from the lower tube plate, a second head is disposed at an end of the tail pipe away from the first head, the cylinder is provided with a short joint, the tail pipe is disposed in the short joint, a third head is disposed at an end of the short joint away from the cylinder, and a gap is disposed between the second head and the third head.
9. The heat-exchange ammonia decomposition reactor of claim 8, wherein the third head and the short joint are connected by a short joint flange.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202023016856.8U CN214486811U (en) | 2020-12-14 | 2020-12-14 | Heat exchange type ammonia decomposition reactor |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202023016856.8U CN214486811U (en) | 2020-12-14 | 2020-12-14 | Heat exchange type ammonia decomposition reactor |
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| CN214486811U true CN214486811U (en) | 2021-10-26 |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US11697108B2 (en) | 2021-06-11 | 2023-07-11 | Amogy Inc. | Systems and methods for processing ammonia |
| US11724245B2 (en) | 2021-08-13 | 2023-08-15 | Amogy Inc. | Integrated heat exchanger reactors for renewable fuel delivery systems |
| US11764381B2 (en) | 2021-08-17 | 2023-09-19 | Amogy Inc. | Systems and methods for processing hydrogen |
| US11795055B1 (en) | 2022-10-21 | 2023-10-24 | Amogy Inc. | Systems and methods for processing ammonia |
| US11834334B1 (en) | 2022-10-06 | 2023-12-05 | Amogy Inc. | Systems and methods of processing ammonia |
| US11834985B2 (en) | 2021-05-14 | 2023-12-05 | Amogy Inc. | Systems and methods for processing ammonia |
| US11866328B1 (en) | 2022-10-21 | 2024-01-09 | Amogy Inc. | Systems and methods for processing ammonia |
-
2020
- 2020-12-14 CN CN202023016856.8U patent/CN214486811U/en active Active
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US11834985B2 (en) | 2021-05-14 | 2023-12-05 | Amogy Inc. | Systems and methods for processing ammonia |
| US11697108B2 (en) | 2021-06-11 | 2023-07-11 | Amogy Inc. | Systems and methods for processing ammonia |
| US11724245B2 (en) | 2021-08-13 | 2023-08-15 | Amogy Inc. | Integrated heat exchanger reactors for renewable fuel delivery systems |
| US11764381B2 (en) | 2021-08-17 | 2023-09-19 | Amogy Inc. | Systems and methods for processing hydrogen |
| US11769893B2 (en) | 2021-08-17 | 2023-09-26 | Amogy Inc. | Systems and methods for processing hydrogen |
| US11843149B2 (en) | 2021-08-17 | 2023-12-12 | Amogy Inc. | Systems and methods for processing hydrogen |
| US11834334B1 (en) | 2022-10-06 | 2023-12-05 | Amogy Inc. | Systems and methods of processing ammonia |
| US11840447B1 (en) | 2022-10-06 | 2023-12-12 | Amogy Inc. | Systems and methods of processing ammonia |
| US11912574B1 (en) | 2022-10-06 | 2024-02-27 | Amogy Inc. | Methods for reforming ammonia |
| US11795055B1 (en) | 2022-10-21 | 2023-10-24 | Amogy Inc. | Systems and methods for processing ammonia |
| US11866328B1 (en) | 2022-10-21 | 2024-01-09 | Amogy Inc. | Systems and methods for processing ammonia |
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