CN216654502U - Radial isothermal ammonia synthesis reactor - Google Patents
Radial isothermal ammonia synthesis reactor Download PDFInfo
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- CN216654502U CN216654502U CN202123195280.0U CN202123195280U CN216654502U CN 216654502 U CN216654502 U CN 216654502U CN 202123195280 U CN202123195280 U CN 202123195280U CN 216654502 U CN216654502 U CN 216654502U
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Abstract
The utility model discloses a radial isothermal ammonia synthesis reactor, which comprises a pressure-bearing shell, a gas collecting cylinder, a catalyst frame and a partition part, wherein the catalyst frame is arranged in the pressure-bearing shell, the gas collecting cylinder is arranged in the catalyst frame, a plurality of gas collecting holes are formed in the gas collecting cylinder, the interior of the catalyst frame is communicated with the interior of the gas collecting cylinder through the gas collecting holes, distribution holes are formed in the catalyst frame, the interior of the pressure-bearing shell is communicated with the interior of the catalyst frame through the distribution holes, a catalyst is filled in a catalytic reaction cavity, a heat exchange assembly is arranged in the catalytic reaction cavity, a water distribution assembly is arranged in the gas collecting chamber, and the water distribution assembly is communicated with the heat exchange assembly; according to the utility model, the caecum heat exchange tube is embedded into the catalyst bed layer, so that the catalyst bed layer is ensured to carry out synthetic ammonia reaction under the isothermal condition of 340 ℃, and the content of outlet ammonia can reach 41.56%, which is about 2 times of the synthesis rate of the existing multistage heat-insulating synthetic ammonia.
Description
Technical Field
The utility model relates to the technical field of chemical equipment, in particular to a radial isothermal ammonia synthesis reactor.
Background
At present, large-scale low-pressure (15.0MPa) ammonia synthesis reactors existing in domestic and foreign ammonia synthesis technology suppliers are all three-stage heat-insulating catalyst beds, interlayer gas-gas heat exchangers are adopted between the two-stage heat-insulating beds and between the two-stage heat-insulating beds to remove heat at an outlet of a heat-insulating section, the temperature of gas at the inlet of the next-stage heat-insulating catalyst bed is ensured to be less than or equal to 380 ℃, high-temperature synthesis gas at the outlet of the three-stage heat-insulating catalyst bed directly enters a direct-connected waste heat boiler, and 3.8MPa saturated steam is a byproduct.
Under the best operation parameters, the ammonia net value of the existing ammonia synthesis reactor is only 20.7 percent, the main task of completing the ammonia synthesis reaction is a first-stage adiabatic catalyst bed layer and a second-stage adiabatic catalyst bed layer, the net value of three-stage (final-stage) ammonia is only 3.53 percent, the catalyst loading accounts for more than 50 percent of the total loading, and only 3.53/20.07 of the synthetic ammonia yield is completed to 17.59 percent. The three-stage (final stage) has low synthetic ammonia yield mainly because the three-stage (final stage) is an adiabatic catalyst bed, the reaction 'equilibrium temperature span' at 426 ℃ of the outlet is 10 ℃, and the ammonia synthesis reaction equilibrium temperature span is too small, so that the synthesis rate of ammonia is inhibited.
The existing ammonia synthesis reactor adopts a direct connection mode of a waste heat boiler and gas at an outlet of a three-stage bed layer of the ammonia synthesis reactor, and the structure corresponding to an adiabatic catalyst bed layer can not ensure that the catalyst bed layer carries out ammonia synthesis reaction under an isothermal condition.
In view of the drawbacks, the inventors have finally obtained the present invention through long-term research and practice.
SUMMERY OF THE UTILITY MODEL
In order to solve the technical defects, the utility model adopts the technical scheme that a radial isothermal ammonia synthesis reactor is provided, which comprises a pressure-bearing shell, a gas collecting cylinder, a catalyst frame and a separating part, wherein the catalyst frame is arranged in the pressure-bearing shell, the gas collecting cylinder is arranged in the catalyst frame, a plurality of gas collecting holes are arranged on the gas collecting cylinder, the inside of the catalyst frame is communicated with the inside of the gas collecting cylinder through the gas collecting holes, the catalyst frame is provided with distribution holes, the inside of the pressure-bearing shell is communicated with the inside of the catalyst frame through the distribution holes, the catalyst frame is connected with the inner wall of the pressure-bearing shell through the separating part to form a sealed gas side circulation cavity between the catalyst frame and the pressure-bearing shell, the catalyst frame is connected with the gas collecting cylinder through the separating part to form a sealed catalytic reaction cavity between the catalyst frame and the gas collecting cylinder, the gas collecting cylinder is connected with the inner wall of the pressure-bearing shell through the partition part to form a sealed gas collecting chamber between the partition part and the pressure-bearing shell, a catalyst is filled in the catalytic reaction chamber, a heat exchange assembly is arranged in the catalytic reaction chamber, a water distribution assembly is arranged in the gas collecting chamber, and the water distribution assembly is communicated with the heat exchange assembly.
Preferably, the separating part comprises a gas side cone and a gas side ball plate, the gas side cone is arranged as a ring-shaped member, an inner ring of the gas side cone is connected with the catalyst frame in a sealing manner, an outer ring of the gas side cone is connected with the pressure-bearing shell in a sealing manner, the gas side ball plate is arranged as a semispherical shell, the outer edge of the gas side ball plate is connected with the catalyst frame in a sealing manner, and the gas side ball plate is connected with the end part of the gas collecting cylinder.
Preferably, the pressure-bearing shell comprises a flat cover, a cylinder and a sealing head, the flat cover and the sealing head are respectively arranged at the upper end and the lower end of the cylinder, the cylinder is cylindrical, and the flat cover is detachably arranged on the cylinder.
Preferably, the catalyst frame comprises a catalyst frame flat cover, a catalyst frame cone and a distributor, the distributor is set to be cylindrical, the catalyst frame flat cover and the catalyst frame cone are respectively arranged at the upper end and the lower end of the distributor, the distributor is hermetically connected with the partition part through the catalyst frame cone, and the catalyst frame flat cover is detachably arranged on the distributor.
Preferably, the end enclosure is provided with an air inlet for air intake corresponding to the air side circulation cavity; the seal head is provided with an air outlet used for air outlet corresponding to the air collection chamber.
The preferred, the subassembly that divides includes the waterside barrel, the both ends of waterside barrel set up waterside low head and waterside ball board respectively in order to form sealed waterside cavity, be provided with the inlet tube sheet in the waterside cavity, the inlet tube sheet will the waterside cavity separates for catchmenting chamber and diversion chamber, and the one end of outlet header pipe is fixed to be set up on the inlet tube sheet and with the chamber intercommunication catchments, the other end passes the waterside low head sets up the waterside barrel is outside, be provided with the water inlet on the waterside low head just the water inlet with diversion chamber intercommunication.
Preferably, the heat exchange assembly comprises a cecum heat exchanger and a water guide pipe, one end of the cecum heat exchanger is sealed, the other end of the cecum heat exchanger is fixedly connected with the water side ball plate, and the cecum heat exchanger is communicated with the water collection cavity; one end of the water guide pipe is arranged in the cecum heat exchanger, the other end of the water guide pipe is fixedly connected with the water inlet pipe plate, and the water guide pipe is communicated with the water distribution chamber.
Preferably, the cecum heat exchangers are annularly arranged in the catalyst frame by taking the gas collecting cylinder as a center.
Preferably, the cecum heat exchanger extends along the extending direction of the water conduit.
Preferably, the water side cylinder is fixedly arranged on the sealing head, the water side lower sealing head is arranged outside the pressure-bearing shell, and the water side ball plate is arranged in the gas collecting chamber.
Compared with the prior art, the utility model has the beneficial effects that: according to the utility model, the caecum heat exchange tubes are buried in the catalyst bed layer, the catalyst bed layer is ensured to carry out synthetic ammonia reaction under the isothermal condition of 340 ℃, the content of outlet ammonia can reach 41.56 percent, which is about 2 times of the existing multistage adiabatic synthetic ammonia synthesis rate, compared with the multistage adiabatic traditional synthetic ammonia reactor, the system pressure is reduced by 2.0-5.0 MPa, the ammonia circulation gas per ton is reduced by-50 percent, the power consumption per ton ammonia is reduced by-18.48 percent, the cold energy consumption per ton ammonia is reduced by-69.49 percent, and the high-pressure steam with 12MPa per ton ammonia as multiple byproducts is 300-600 kg (traditionally 3.8MPa medium-pressure steam), and a direct-connection waste heat boiler which is easy to cause accidents is omitted, the ammonia synthesis catalyst bed layer can be reduced into one bed layer, and the investment in the ammonia synthesis engineering section is reduced by 20-30 percent.
Drawings
FIG. 1 is a structural view of the reactor for the radial isothermal synthesis of ammonia.
The figures in the drawings represent:
1-flat cover; 2-catalyst frame flat cover; 3, a gas collecting cylinder; 4-a cecal heat exchanger; 5-a water conduit; 6-cylinder body; 7-a distributor; 8-distribution holes; 9-gas collecting holes; 10-a catalyst frame; 11-gas side ball panel; 12-catalyst frame cone; 13-water side ball board; 14-a water inlet pipe plate; 15-gas side cone; 16-an air inlet; 17-gas collection chamber; 18-air outlet; 19-a water separation chamber; 20-a water inlet; 21-water outlet; 22-a water collecting cavity; 23-sealing the end socket; 24-a water outlet main pipe; 25-water side lower end socket.
Detailed Description
The described and additional features and advantages of the present invention are described in more detail below with reference to the accompanying drawings.
As shown in FIG. 1, FIG. 1 is a structural view of the radial isothermal ammonia synthesis reactor. The radial isothermal ammonia synthesis reactor comprises a pressure-bearing shell, a gas collecting cylinder 3, a catalyst frame 10 and a separating part, wherein the catalyst frame 10 is arranged in the pressure-bearing shell, the gas collecting cylinder 3 is arranged in the catalyst frame 10, the gas collecting cylinder 3 is provided with a plurality of gas collecting holes 9, the interior of the catalyst frame 10 is communicated with the interior of the gas collecting cylinder 3 through the gas collecting holes 9, the catalyst frame 10 is provided with distribution holes 8, the interior of the pressure-bearing shell is communicated with the interior of the catalyst frame 10 through the distribution holes 8, the catalyst frame 10 is connected with the inner wall of the pressure-bearing shell through the separating part to form a sealed gas side circulation cavity between the catalyst frame 10 and the pressure-bearing shell, and the catalyst frame 10 is connected with the gas collecting cylinder 3 through the separating part to form a sealed catalytic reaction cavity between the catalyst frame 10 and the gas collecting cylinder 3, the gas collecting cylinder 3 is connected with the inner wall of the pressure-bearing shell through the partition part to form a sealed gas collecting chamber 17 between the partition part and the pressure-bearing shell, a catalyst is filled in the catalytic reaction cavity, a heat exchange assembly is arranged in the catalytic reaction cavity, the reaction temperature in the catalyst frame 10 is guaranteed to be stable through the heat exchange assembly, a water distribution assembly is arranged in the gas collecting chamber 17, and the water distribution assembly is communicated with the heat exchange assembly to realize circulation of heat exchange liquid in the heat exchange assembly.
Preferably, the separating part comprises a gas side cone 15 and a gas side ball plate 11, the gas side cone 15 is configured as an annular member, an inner ring of the gas side cone 15 is hermetically connected with the catalyst frame 10, an outer ring of the gas side cone 15 is hermetically connected with the pressure-bearing shell, the gas side ball plate 11 is configured as a hemispherical shell, an outer edge of the gas side ball plate 11 is hermetically connected with the catalyst frame 10, and the gas side ball plate 11 is connected with the end of the gas collecting cylinder 3.
An air side ball cavity is formed between the water diversion component and the air side ball plate 11.
Preferably, the pressure-bearing shell comprises a flat cover 1, a cylinder body 6 and a seal head 23, wherein the flat cover 1 and the seal head 23 are respectively arranged at the upper end and the lower end of the cylinder body 6, the cylinder body 6 is cylindrical, and the flat cover 1 is detachably arranged on the cylinder body 6 so that a user can conveniently enter the pressure-bearing shell to maintain or load a catalyst.
Generally, catalyst frame 10 includes catalyst frame flat cover 2, catalyst frame cone 12, distributor 7 sets up to the cylinder type, catalyst frame flat cover 2 with catalyst frame cone 12 sets up respectively the upper and lower both ends of distributor 7, distributor 7 passes through catalyst frame cone 12 with partition portion sealing connection, catalyst frame flat cover 2 can dismantle the setting and be in on the distributor 7, so that the user gets into inside maintenance or the loading catalyst of catalyst frame 10.
Generally, the end socket 23 is provided with an air inlet 16 for air inlet corresponding to the air side circulation cavity; the end socket 23 is provided with an air outlet 18 for air outlet corresponding to the air collection chamber 17.
The subassembly that divides water includes the water side barrel, the both ends of water side barrel set up water side low head 25 and water side ball board 13 respectively in order to form sealed water side cavity, be provided with inlet tube sheet 14 in the water side cavity, inlet tube sheet 14 will the water side cavity is separated for catchmenting chamber 22 and diversion chamber 19, and the one end of outlet header 24 is fixed to be set up inlet tube sheet 14 on and with the chamber 22 intercommunication catchments, the delivery port 21 of the other end passes water side low head 25 sets up the water side barrel is outside, be provided with on the water side low head 25 water inlet 20 just water inlet 20 with diversion chamber 19 intercommunication.
The heat exchange assembly comprises a caecum heat exchanger 4 and a water guide pipe 5, one end of the caecum heat exchanger 4 is sealed, the other end of the caecum heat exchanger is fixedly connected with the water side ball plate 13, and the caecum heat exchanger 4 is communicated with the water collecting cavity 22; one end of the water guide pipe 5 is arranged in the cecum heat exchanger 4, the other end of the water guide pipe is fixedly connected with the water inlet pipe plate 14, and the water guide pipe 5 is communicated with the water distribution chamber 19.
Preferably, the cecum heat exchangers 4 are annularly arranged in the catalyst frame 10 with the gas collecting cylinder 3 as a center.
The cecal heat exchanger 4 extends in the direction of extension of the water conduit 5.
The water side cylinder is fixedly arranged on the seal head 23, the water side lower seal head 25 is arranged outside the pressure-bearing shell, and the water side ball plate 13 is arranged in the gas collection chamber 17.
The catalyst frame flat cover 2, the gas collecting cylinder 3, the distributor 7, the gas side ball plate 11 and the catalyst frame cone 12 form a radial catalyst frame 10; the water guide pipe 5 is arranged inside the caecum heat exchange pipe 4, and the caecum heat exchange pipe 4 is buried inside the catalyst frame 10; the water side lower end socket 24, the water inlet 20, the water diversion chamber 19, the water inlet pipe plate 14, the water guide pipe 5, the cecum heat exchange pipe 4, the water ball cavity 13 and the water outlet main pipe 24 form a water path circulation system.
The flat cover 1, the cylinder 6, the air inlet 16 and the seal head 23 form a pressure-bearing shell.
The catalyst in the catalyst frame is an iron-based, iron-cobalt-based, ruthenium-based and other ammonia synthesis catalysts, the synthesis reaction pressure is in the range of 80-15.0 MPa, the bed layer temperature is in a certain isothermal zone in the range of 300-480 ℃, and the byproduct steam pressure is in the range of 10-15 MPa. The main technical parameters of a radial isothermal ammonia synthesis reactor for producing 200 tons of synthetic ammonia per day are as follows:
(1) the specification of the reactor is phi 3600;
(2) catalyst loading: 150m3；
(3) List of the most important economic indicators
| Parameter name | Electricity consumption | Cold energy consumption | By-product steam | Gas flow into the tower |
| Unit of | KWh/tNH3 | KCa1/tNH3 | kg/tNH3 | Nm3/tNH3 |
| Economic index | 105 | 73262.60 | 1689.20 | 4698.82 |
According to the utility model, the caecum heat exchange tubes are embedded into the catalyst bed layer, the catalyst bed layer reactor is removed in time, the catalyst bed layer is ensured to carry out synthetic ammonia reaction under the isothermal condition of 340 ℃, the content of outlet ammonia can reach 41.56%, which is about 2 times of the existing multistage adiabatic synthetic ammonia synthesis rate, compared with the multistage adiabatic traditional synthetic ammonia reactor, the system pressure is reduced by 2.0-5.0 MPa, the ammonia circulation gas per ton is reduced by-50%, the ammonia power consumption per ton is reduced by-18.48%, the ammonia cold energy consumption per ton is reduced by-69.49%, and the ammonia multiple byproduct 12MPa high-pressure steam is 300-600 kg (traditionally 3.8MPa medium-pressure steam), and a direct-connection waste heat boiler which is easy to cause accidents is omitted, the ammonia synthesis catalyst bed layer can be reduced into one bed layer, the engineering investment of an ammonia synthesis section is reduced by 20-30%, and the utility model is a revolutionary energy-saving innovation in the ammonia synthesis field.
The foregoing is merely a preferred embodiment of the utility model, which is intended to be illustrative and not limiting. It will be understood by those skilled in the art that various changes, modifications and equivalents may be made therein without departing from the spirit and scope of the utility model as defined in the appended claims.
Claims (10)
1. The utility model provides a radial isothermal synthesis ammonia reactor, its characterized in that, including pressure-bearing casing, gas cylinder, catalyst frame, partition portion, the catalyst frame sets up in the pressure-bearing casing, the gas cylinder sets up in the catalyst frame, be provided with a plurality of gas collecting holes on the gas cylinder, the catalyst frame is inside to be passed through the gas collecting hole with the inside intercommunication of gas cylinder, be provided with the distribution hole on the catalyst frame, the pressure-bearing casing is inside to be passed through the distribution hole with the inside intercommunication of catalyst frame, the catalyst frame passes through partition portion with pressure-bearing shells inner wall connects the catalyst frame with form sealed gas side circulation chamber between the pressure-bearing casing, the catalyst frame passes through partition portion with the gas cylinder is connected catalyst frame with form sealed catalytic reaction chamber between the gas cylinder, the gas cylinder pass through partition portion with pressure-bearing shells inner wall connects partition portion with pressure-bearing shells A sealed gas collection chamber is formed between the bodies, a catalyst is filled in the catalytic reaction cavity, a heat exchange assembly is arranged in the catalytic reaction cavity, a water distribution assembly is arranged in the gas collection chamber, and the water distribution assembly is communicated with the heat exchange assembly.
2. The radial isothermal ammonia synthesis reactor according to claim 1, wherein the partition comprises a gas side cone and a gas side ball plate, wherein the gas side cone is configured as an annular member, an inner ring of the gas side cone is hermetically connected with the catalyst frame, an outer ring of the gas side cone is hermetically connected with the pressure-bearing shell, the gas side ball plate is configured as a hemispherical shell, an outer edge of the gas side ball plate is hermetically connected with the catalyst frame, and the gas side ball plate is connected with the end of the gas collecting barrel.
3. The radial isothermal ammonia synthesis reactor according to claim 2, wherein the pressure-bearing shell comprises a flat cover, a cylinder and end sockets, the flat cover and the end sockets are respectively arranged at the upper end and the lower end of the cylinder, the cylinder is cylindrical, and the flat cover is detachably arranged on the cylinder.
4. The radial isothermal ammonia synthesis reactor according to claim 2, wherein the catalyst frame comprises a catalyst frame flat cover, a catalyst frame cone and a distributor, the distributor is arranged in a cylindrical shape, the catalyst frame flat cover and the catalyst frame cone are respectively arranged at the upper end and the lower end of the distributor, the distributor is hermetically connected with the partition part through the catalyst frame cone, and the catalyst frame flat cover is detachably arranged on the distributor.
5. Radial isothermal ammonia synthesis reactor according to claim 3, wherein said head is provided with an inlet for inlet air in correspondence of said gas-side circulation chamber; the seal head is provided with an air outlet used for air outlet corresponding to the air collection chamber.
6. The radial isothermal ammonia synthesis reactor according to claim 5, wherein the water diversion assembly comprises a water side barrel, a water side lower end enclosure and a water side ball plate are respectively arranged at two ends of the water side barrel to form a sealed water side cavity, a water inlet pipe plate is arranged in the water side cavity and divides the water side cavity into a water collection cavity and a water diversion chamber, one end of a water outlet header pipe is fixedly arranged on the water inlet pipe plate and is communicated with the water collection cavity, the other end of the water outlet header pipe penetrates through the water side lower end enclosure and is arranged outside the water side barrel, and a water inlet is arranged on the water side lower end enclosure and is communicated with the water diversion chamber.
7. The radial isothermal ammonia synthesis reactor according to claim 6, wherein the heat exchange assembly comprises a cecum heat exchanger and a water conduit, wherein one end of the cecum heat exchanger is sealed, the other end of the cecum heat exchanger is fixedly connected with the water side ball plate, and the cecum heat exchanger is communicated with the water collection cavity; one end of the water guide pipe is arranged in the cecum heat exchanger, the other end of the water guide pipe is fixedly connected with the water inlet pipe plate, and the water guide pipe is communicated with the water distribution chamber.
8. Radial isothermal ammonia synthesis reactor according to claim 7, wherein said cecum heat exchangers are arranged annularly inside said catalyst frame, centered on said gas collection cylinder.
9. Radial isothermal ammonia synthesis reactor according to claim 7, wherein said cecum heat exchanger extends along the extension of said water conduits.
10. Radial isothermal ammonia synthesis reactor according to claim 7, wherein said water side vessel is fixedly arranged on said head, said water side bottom head is arranged outside said pressure-bearing shell, and said water side bulb is arranged in said gas collection chamber.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202123195280.0U CN216654502U (en) | 2021-12-17 | 2021-12-17 | Radial isothermal ammonia synthesis reactor |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202123195280.0U CN216654502U (en) | 2021-12-17 | 2021-12-17 | Radial isothermal ammonia synthesis reactor |
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| CN216654502U true CN216654502U (en) | 2022-06-03 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115253927A (en) * | 2022-09-27 | 2022-11-01 | 江苏永大化工机械有限公司 | Radial reactor of accurate accuse temperature |
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2021
- 2021-12-17 CN CN202123195280.0U patent/CN216654502U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115253927A (en) * | 2022-09-27 | 2022-11-01 | 江苏永大化工机械有限公司 | Radial reactor of accurate accuse temperature |
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