CN115893446A - Nested multi-bed tail end isothermal ammonia synthesis reactor - Google Patents
Nested multi-bed tail end isothermal ammonia synthesis reactor Download PDFInfo
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Abstract
The invention discloses a nested multi-bed-layer tail end isothermal ammonia synthesis reactor, which belongs to the technical field of low-pressure ammonia synthesis reactors and comprises a gas mixing distribution assembly, a plurality of stages of radial catalyst beds, a synthetic gas collector and a water heat transfer tube bundle, wherein the plurality of stages of radial catalyst beds are sequentially arranged from outside to inside, adjacent two stages of radial catalyst beds are communicated, the gas mixing distribution assembly is arranged outside the radial catalyst bed positioned on the outermost side, and the gas mixing distribution assembly is communicated with the radial catalyst bed positioned on the outermost side. The invention has the advantages that the I-grade radial catalyst bed layer, the II-grade radial catalyst bed layer and the tail end isothermal radial bed layer are respectively sleeved at the periphery of the synthesis gas collector to form I-grade, II-grade, \ 8230 \ 8230and n-grade + tail end water heat transfer isothermal sleeved multi-bed tail end isothermal ammonia synthesis reactors, the equipment height is reduced, the stress is thoroughly eliminated, the engineering cost is reduced, the ammonia net value is high, the bed layer byproduct high-grade steam and the heat recovery rate are high.
Description
Technical Field
The invention relates to the technical field of low-pressure ammonia synthesis reactors, in particular to a nested multi-bed-layer tail-end isothermal ammonia synthesis reactor.
Background
At present, the existing large-scale low-pressure (15.0 MPa) ammonia synthesis reactors of domestic and foreign ammonia synthesis technology suppliers are all three-stage adiabatic radial catalyst beds, the three-stage adiabatic radial catalyst beds are overlapped up and down, although the catalyst beds are radial, the catalyst beds are overlapped, and the bed layers are connected with each other, sealed, thermally stress eliminated, gas conveying channels and the like, so that the large-scale low-pressure (15.0 MPa) ammonia synthesis reactors have many problems and are easy to damage in the operation process. The multi-stage radial bed layers and the indirect heat exchangers between the bed layers are connected into a whole in an up-down overlapping mode, the height of equipment reaches more than 28m, and the multi-stage radial bed layer and the indirect heat exchangers between the bed layers are difficult to transport and overhaul and high in engineering cost. To this end, a nested multi-bed, end-point, isothermal ammonia synthesis reactor is proposed.
Disclosure of Invention
The technical problem to be solved by the invention is as follows: the method solves the problems of overhigh equipment height, difficult transportation, difficult equipment maintenance, high engineering cost, low ammonia net value, high operation energy consumption and the like in the prior art, and provides the nested multi-bed tail end isothermal ammonia synthesis reactor.
The invention solves the technical problems through the following technical scheme that the multi-stage radial catalyst bed heat exchanger comprises a gas mixing distribution assembly, a plurality of stages of radial catalyst beds, a synthetic gas collector and a water heat transfer tube bundle, wherein the plurality of stages of radial catalyst beds are sequentially arranged from outside to inside, the adjacent two stages of radial catalyst beds are communicated, the gas mixing distribution assembly is arranged outside the radial catalyst bed positioned on the outermost side, the gas mixing distribution assembly is communicated with the radial catalyst bed positioned on the outermost side, the radial catalyst bed positioned on the innermost side is communicated with the synthetic gas collector, and the water heat transfer tube bundle removes the reaction heat of the radial catalyst bed positioned on the innermost side through the heat exchange effect to ensure that the radial catalyst bed is an isothermal bed;
the water heat transfer tube bundle comprises a water inlet main pipe, a water distribution ball cavity, a heat exchange water pipe, a water collection ball cavity and a water outlet main pipe; the heat exchange water pipes are distributed inside the innermost radial catalyst bed layer at intervals, the lower end of each heat exchange water pipe is communicated with the corresponding water distribution ball cavity, the upper end of each water distribution ball cavity is communicated with the corresponding water collection ball cavity, the upper end of each water collection ball cavity is communicated with the corresponding water outlet main pipe, the lower end of each water distribution ball cavity is communicated with the corresponding water inlet main pipe, the tail end of each water outlet main pipe is led out to the outside of the isothermal ammonia synthesis reactor at the tail end of the multiple beds of the suit, and the starting end of each water inlet main pipe is led out to the outside of the isothermal ammonia synthesis reactor at the tail end of the multiple beds of the suit.
Furthermore, the multistage radial catalyst bed layers comprise a first-stage radial catalyst bed layer, a second-stage radial catalyst bed layer and a tail-end radial catalyst bed layer; the second-stage radial catalyst bed layer is sleeved outside the tail-end radial catalyst bed layer and communicated with the tail-end radial catalyst bed layer, the first-stage radial catalyst bed layer is sleeved outside the second-stage radial catalyst bed layer and communicated with the second-stage radial catalyst bed layer, and the gas mixing distribution assembly is arranged outside the first-stage radial catalyst bed layer and communicated with the first-stage radial catalyst bed layer.
Furthermore, the gas mixing and distributing assembly comprises an F0 cold gas pipe, an internal flat cover, an F0 distributor, a gas mixing chamber, an internal cylinder, a gas distributing chamber, a catalyst frame lower end socket, an F1 cold gas pipe, an F2 cold gas pipe, a bed layer sealing pattern plate and a gas distributor; the flat lid of internals sets up the upper end of internals barrel, catalyst frame low head sets up the lower extreme of internals barrel, the gas distribution room is located gas distributor with between the internals barrel, the gas mixing room is located gas distributor with between the flat lid of internals, the gas mixing room is located the top of gas distribution room and communicates rather than, the distributor sets up in the gas mixing room, the bed seals the colored board setting and is in the upper end of one-level radial catalyst bed, second grade radial catalyst bed, terminal radial catalyst bed.
Furthermore, the first-stage radial catalyst bed layer comprises a first-stage radial catalyst bed, a first-stage heat exchanger, a first-stage cold air outlet of the heat exchanger, a first-stage redistribution heat exchanger and a first-stage gas redistributor; the device comprises a bed layer sealing pattern plate, a catalyst frame lower end socket, a first-stage radial catalyst bed, a first-stage heat exchanger, a first-stage redistribution heat exchanger and a first-stage gas redistributor, wherein the first-stage radial catalyst bed, the first-stage heat exchanger, the first-stage gas redistributor are sequentially arranged from outside to inside, a cold air outlet of the first-stage heat exchanger is arranged at the upper end of the first-stage heat exchanger and is positioned in a gas mixing chamber, the first-stage heat exchanger is arranged on the outer side of the first-stage redistribution heat exchanger, the first-stage heat exchanger and the first-stage redistribution heat exchanger are all in a cylinder shape, and a bed layer sealing pattern plate, a catalyst frame lower end socket, the first-stage radial catalyst bed, the first-stage heat exchanger, the first-stage redistribution heat exchanger and the first-stage gas redistributor form a hollow cylinder.
Furthermore, the secondary radial catalyst bed layer comprises a secondary radial catalyst bed, a secondary heat exchanger, a cold air outlet of the secondary heat exchanger, a secondary redistributor heat exchanger and a secondary gas redistributor; the secondary radial catalyst bed, the secondary heat exchanger, the secondary redistribution heat exchanger and the secondary gas redistributor are sequentially arranged from outside to inside, a cold air outlet of the secondary heat exchanger is arranged in the gas mixing chamber, the secondary heat exchanger is arranged on the outer side of the secondary redistribution heat exchanger, the secondary heat exchanger and the secondary redistribution heat exchanger are all in a cylindrical shape, and the bed layer sealing pattern plate, the catalyst frame lower end socket, the secondary radial catalyst bed, the secondary heat exchanger, the secondary redistribution heat exchanger and the secondary gas redistributor form a hollow cylinder.
Furthermore, the F0 cold air pipe penetrates through the flat cover of the internal part and is connected with the F0 distributor; the F1 cold air pipe and the F2 cold air pipe sequentially penetrate through the flat cover of the internal part and the upper end of the gas distributor from top to bottom and are respectively communicated with the primary heat exchanger and the secondary heat exchanger.
Furthermore, the tail end radial catalyst bed layer is a tail end radial catalyst bed, the synthesis gas collector comprises a gas collecting cylinder, a gas outlet direct connecting pipe, a gas side ball cavity and a gas side channel, the tail end radial catalyst bed is sleeved outside the gas collecting cylinder and communicated with the gas collecting cylinder, and is positioned on the inner side of the secondary gas redistributor, the upper end of the gas collecting cylinder is closed, the lower end of the gas collecting cylinder is communicated with the gas side channel through the gas side ball cavity, and the gas side channel is communicated with the gas outlet direct connecting pipe.
Furthermore, the catalysts filled in the first-stage radial catalyst bed, the second-stage radial catalyst bed and the end radial catalyst bed are synthetic ammonia catalysts.
Furthermore, the synthetic reaction pressure of the indirect heat exchange nested radial multi-section bed layer structure is 80-15.0 Mpa, and the temperature of the first-stage radial catalyst bed layer, the second-stage radial catalyst bed layer and the tail-end radial catalyst bed layer is 300-510 ℃.
Furthermore, the periphery of the gas mixing distribution assembly is provided with a shell upper end enclosure, a shell barrel and a shell lower end enclosure, and the shell upper end enclosure, the shell barrel and the shell lower end enclosure are sequentially connected to form a shell.
Compared with the prior art, the invention has the following advantages: a stage I radial catalyst bed layer, a stage II radial catalyst bed layer, \ 8230 \ 8230, a stage n radial catalyst bed layer and a tail end isothermal radial bed layer are respectively sleeved around a gas collecting cylinder to form stage I, stage II and stage III \8230 \ 8230, a stage n multi-section indirect heat exchange and water heat transfer sleeved radial catalyst bed layer, the height of equipment is reduced, the stress is eliminated thoroughly, and the construction cost is reduced.
Drawings
FIG. 1 is a schematic view of the overall structure of an axial section of a nested multi-bed end isothermal ammonia synthesis reactor according to an embodiment of the present invention;
FIG. 2 is a partial schematic view of an axial cross-section of a gas mixing chamber and a gas distribution chamber in an embodiment of the invention;
FIG. 3 is a schematic view of a partial structure of an axial cross section of a stage I radial catalyst bed in an example of the present invention;
FIG. 4 is a schematic view of a partial structure of a section in the axial direction of a II-stage radial catalyst bed in an example of the present invention;
FIG. 5 is a schematic view of the axial cross-section partial structure of the isothermal bed of the end water-heat-transfer radial catalyst in an embodiment of the present invention;
FIG. 6 is a schematic view of a partial structure in axial cross-section of a water-cooled heat transfer tube bundle in an embodiment of the present invention;
FIG. 7 is a schematic axial cross-sectional partial structure of a syngas collector in an embodiment of the invention.
Detailed Description
The following examples are given for the detailed implementation and specific operation of the present invention, but the scope of the present invention is not limited to the following examples.
As shown in fig. 1, the present embodiment provides a technical solution: a nested multi-bed tail end isothermal ammonia synthesis reactor comprises a gas mixing distribution assembly, a first-stage radial catalyst bed, a second-stage radial catalyst bed, a tail end water heat transfer radial catalyst isothermal bed, a water heat transfer tube bundle and a synthesis gas collector; the device comprises a water-transfer heat pipe bundle, a synthesis gas collector, a tail end isothermal ammonia synthesis reactor and a tail end water-transfer heat radial catalyst isothermal bed, wherein the tail end water-transfer heat radial catalyst isothermal bed is sleeved with the II-level radial catalyst bed and communicated with the II-level radial catalyst bed, the I-level radial catalyst bed is sleeved with the II-level radial catalyst bed and communicated with the II-level radial catalyst bed, a gas mixing distribution assembly is arranged outside the I-level radial catalyst bed and communicated with the I-level radial catalyst bed, the water-transfer heat pipe bundle is arranged inside the tail end water-transfer heat radial catalyst isothermal bed, the tail end radial catalyst bed is removed through heat exchange to react heat, the tail end water-transfer heat radial catalyst isothermal bed is made to be an isothermal bed, and synthesis gas generated through the tail end water-transfer heat radial catalyst isothermal bed reaction is collected by the synthesis gas collector and is led out of the multi-bed tail end isothermal ammonia synthesis reactor.
More specifically, in the present embodiment, the nested multi-bed end isothermal ammonia synthesis reactor includes components such as an F0 cold air pipe 1, an internal flat cover 2, an F0 distributor 3, a gas mixing chamber 4, a i-stage heat exchanger cold air outlet 5, a i-stage heat exchanger 6, a ii-stage heat exchanger 7, a gas collecting cylinder 8, an internal cylinder 9, a gas distribution chamber 10, a gas distributor 11, a catalyst frame lower head 12, a gas outlet straight connecting pipe 13, an F1 cold air pipe 14, an F2 cold air pipe 15, a ii-stage heat exchanger cold air outlet 16, a bed sealing pattern plate 17, a i-stage radial catalyst bed 18, a ii-stage radial catalyst bed 19, a ii-stage gas redistributor heat exchanger 23, a ii-stage redistributor heat exchanger 24, a shell upper head 25, a shell cylinder 26, a shell lower head 27, a shell F2 inlet pipe 28, a water outlet header 29, a water collecting sphere cavity 30, a heat exchange water pipe 31, a gas side sphere cavity 32, a water distributing sphere cavity 33, a water inlet header 34, and a gas side channel 35.
As shown in fig. 2, more specifically, in the present embodiment, the gas mixing distribution assembly includes an F0 cold gas pipe 1, an internal flat cover 2, an F0 distributor 3, a gas mixing chamber 4, an internal cylinder 9, a gas distribution chamber 10, a catalyst frame lower head 12, an F1 cold gas pipe 14, an F2 cold gas pipe 15, a bed sealing flower plate 17, an F2 inlet pipe 28, and the like;
the F0 cold air pipe 1 is used for introducing 170-280 ℃ cold air into the F0 distributor 3, mixing the cold air with 420 ℃ gas at the outlets of the first-stage heat exchanger and the second-stage heat exchanger in the gas mixing chamber 4, and allowing the mixed three streams of gas to enter a first-stage radial catalyst bed layer from the gas distributor 11 for reaction at the temperature of 380 ℃; the F1 cold air pipe 14 is used for introducing cold air at 170-280 ℃ into the I heat exchanger 6, reducing the gas at 495 ℃ at the outlet of the I-stage radial catalyst bed 18 to 380 ℃, and simultaneously heating the cold air from the F1 cold air pipe 14 to 420 ℃ to enter the gas mixing chamber 4; the F2 cold air pipe 15 is used for introducing cold air at 170-280 ℃ into the II-stage heat exchanger 7 to reduce the temperature of 495 ℃ gas at the outlet of the II-stage radial catalyst bed 19 to 380 ℃, and simultaneously heating the cold air from the F2 cold air pipe 15 to 420 ℃ to enter the gas mixing chamber 4; the catalyst frame lower end cover 12 is arranged at the lower end of the internal part cylinder 9 and is used for sealing a first-stage radial catalyst bed, a second-stage radial catalyst bed, a tail end water-transfer thermal radial catalyst isothermal bed and the internal part cylinder 9, the gas distribution chamber 10 is positioned between the gas distributor 11 and the internal part cylinder 9, the gas mixing chamber 4 is positioned between the gas distributor 11 and the internal part flat cover 2, the gas mixing chamber 4 is positioned above and communicated with the gas distribution chamber 10, the F0 distributor 3 is arranged in the gas mixing chamber 4, and the bed sealing pattern plate 17 is arranged at the upper ends of the first-stage radial catalyst bed, the second-stage radial catalyst bed and the tail end water-transfer thermal radial catalyst isothermal bed and is used for sealing the upper ends of the first-stage radial catalyst bed 18, the second-stage radial catalyst bed 19 and the tail end radial catalyst bed 22;
the F0 cold air pipe 1 penetrates through the internal flat cover 2 and is connected with the F0 distributor 3; the F1 cold air pipe 14 and the F2 cold air pipe 15 sequentially penetrate through the internal flat cover 2 from top to bottom and are respectively connected with the I-stage heat exchanger 6 and the II-stage heat exchanger 7, the internal flat cover 2 is connected with the upper end of the internal cylindrical body 9, the internal flat cover 2 and the bed layer sealing flower plate 17 form a gas mixing chamber 4 to ensure that three gas streams (380 ℃) of the FO cold air pipe 1, the I-stage heat exchanger cold air outlet 5 and the II-stage heat exchanger cold air outlet 16 are mixed and then enter the I-stage radial catalyst bed 18, the II-stage radial catalyst bed 19 and the tail end moves horizontally through the gas distributor 11The isothermal bed 22 reaction of the thermal radial catalyst is carried out in the presence of iron catalyst to complete H 2 +N 2 →NH 3 The synthetic reaction task of (1).
It should be noted that the cold air at 170-280 ℃ in the F2 cold air pipe 15 comes from the F2 inlet pipe 28 on the shell.
As shown in fig. 3, more specifically, in the present embodiment, the i-stage radial catalyst bed includes components such as an i-stage radial catalyst bed 18, an i-stage heat exchanger 6, a i-stage cold air outlet 5 of the i-stage heat exchanger, an i-stage gas redistributor 21, and an i-stage redistributor 23, wherein the i-stage heat exchanger 6 is disposed outside the i-stage redistributor 23, the i-stage heat exchanger 6 and the i-stage redistributor 23 are all in a cylindrical shape, and the bed sealing rosette 17, the catalyst frame bottom head 12, the i-stage radial catalyst bed 18, the i-stage heat exchanger 6, the i-stage redistributor 23, and the i-stage gas redistributor 21 form a hollow cylindrical i-stage radial catalyst bed;
the cold air outlet 5 of the I-stage heat exchanger is arranged at the upper end of the I-stage heat exchanger 6 and is positioned in the gas distributor 11, and is used for feeding 170-280 ℃ gas of the F1 cold air pipe 14 into the I-stage heat exchanger 6, reducing 495 ℃ gas at the outlet of the I-stage radial catalyst bed layer 18 to 380 ℃, simultaneously heating the cold air from the F1 cold air pipe 14 to 420 ℃, and feeding the cold air into the gas mixing chamber 4 through the cold air outlet 5 of the I-stage heat exchanger.
As shown in fig. 4, more specifically, in this embodiment, the second-stage radial catalyst bed includes a second-stage radial catalyst bed 19, a second-stage heat exchanger 7, a second-stage heat exchanger cold air outlet 16, a second-stage redistributor heat exchanger 24, a second-stage gas redistributor 20, and the like, wherein the second-stage heat exchanger 7 is disposed outside the second-stage redistributor heat exchanger 24, the second-stage heat exchanger 7 and the second-stage redistributor heat exchanger 24 are all in a cylindrical shape, and the bed sealing face plate 17, the catalyst frame bottom head 12, the second-stage radial catalyst bed 19, the second-stage heat exchanger 7, the second-stage heat exchanger cold air outlet 16, the second-stage redistributor heat exchanger 24, the second-stage gas redistributor the like forms a hollow cylindrical second-stage radial catalyst bed;
the cold air outlet 16 of the II-stage heat exchanger is arranged at the upper end of the II-stage heat exchanger 7 and is positioned in the gas distributor 11, and is used for enabling 170-280 ℃ gas of the F2 cold air pipe 15 to enter the II-stage heat exchanger 7, reducing 495 ℃ gas at the outlet of the II-stage radial catalyst bed layer 19 to 380 ℃, and simultaneously heating the cold air from the F2 cold air pipe 15 to 420 ℃ and enabling the cold air to enter the gas mixing chamber 4 through the cold air outlet 16 of the II-stage heat exchanger.
More specifically, as shown in FIG. 5, in this embodiment the end water-heat-transfer radial catalyst isothermal bed comprises an end radial catalyst bed 22, said end radial catalyst bed 22 being disposed inside a stage II gas redistributor 24.
As shown in fig. 6, in the present embodiment, more specifically, the water heat transfer tube bundle includes a water inlet header pipe 34, a water diversion sphere cavity 33, a heat exchange water pipe 31, a water collection sphere cavity 30, and a water outlet header pipe 29.
Wherein, 31 interval distributions of heat transfer water pipe are inside terminal radial catalyst bed 22, the lower extreme with divide water ball chamber 33 intercommunication, the upper end with the ball chamber 30 intercommunication that catchments, the upper end of ball chamber 30 that catchments with outlet manifold 29 intercommunication, divide the lower extreme of ball chamber 33 with inlet manifold 34 intercommunication, outlet manifold 29 is terminal to be drawn forth to the terminal isothermal ammonia synthesis reactor of the many beds of suit outside, the beginning of inlet manifold 34 is drawn forth to the terminal isothermal ammonia synthesis reactor of the many beds of suit outside.
It should be noted that the water for heat transfer sequentially enters the water inlet main pipe 34, the water dividing sphere cavity 33, the heat exchange water pipe 31, the water collecting sphere cavity 30 and the water outlet main pipe 29, and the water after heat exchange is transferred out of the reaction heat of the terminal radial catalyst bed layer 20, so that the terminal water heat transfer radial catalyst isothermal bed layer is an isothermal bed layer.
As shown in fig. 7, more specifically, in the present embodiment, the synthesis gas collector includes a gas collecting cylinder 8, an outlet straight connecting pipe 13, a gas-side sphere cavity 32, and a gas-side channel 35;
the isothermal bed 22 of the tail-end water heat transfer radial catalyst is sleeved outside the gas collecting cylinder 8, is communicated with the gas collecting cylinder 8, is positioned on the inner side of the stage II gas redistributor 24, the upper end of the gas collecting cylinder 8 is closed, the lower end of the gas collecting cylinder 8 is communicated with a gas side channel 35 through a gas side spherical cavity 32, and the gas side channel 35 is communicated with the gas outlet straight connecting pipe 13.
In this embodiment, a shell upper end enclosure 25, a shell cylinder 26, and a shell lower end enclosure 27 are disposed on the periphery of the gas mixing distribution assembly, and the shell upper end enclosure 25, the shell cylinder 26, and the shell lower end enclosure 27 constitute a shell capable of bearing a grade of 80-15.0 MPa.
In this embodiment, the upper end of the water dividing sphere cavity 33 is fixedly connected with the lower end of the gas side sphere cavity 32 to form a channel for the synthesized gas, and the upper end of the gas collecting cylinder 8 is connected with the lower end of the water collecting sphere cavity 30.
The working principle is as follows: the working principle that an isothermal bed layer of a first-stage radial catalyst bed layer, a second-stage radial catalyst bed layer and a tail-end water heat transfer radial catalyst is filled with catalysts for synthesizing ammonia such as Fe system, ruthenium Ru and the like is adopted, an F1 cold air pipe 14 is used for introducing cold air of 170-280 ℃ into the first-stage heat exchanger 6, reducing the temperature of 495 ℃ gas at the outlet of the first-stage radial catalyst bed layer 18 to 380 ℃, and simultaneously heating the cold air from the F1 cold air pipe 14 to 420 ℃ to enter a gas mixing chamber 4; the F2 cold air pipe 15 is used for introducing cold air at 170-280 ℃ into the II-stage heat exchanger 7, reducing the 495 ℃ gas at the outlet of the II-stage radial catalyst bed 19 to 380 ℃, simultaneously heating the cold air from the F2 cold air pipe 15 to 420 ℃ and then introducing the cold air into the gas mixing chamber 4, the F0 cold air pipe 1 is used for introducing the cold air at 170-280 ℃ into the F0 distributor 3, the cold air is mixed with the gas at 420 ℃ at the outlets of the I-stage heat exchanger 6 and the II-stage heat exchanger 7 in the gas mixing chamber 4, the mixed three streams of gas are 380 ℃, the mixed gas enters the I-stage radial catalyst bed 18 from the gas distributor 11 for reaction, the temperature of the I-stage radial catalyst bed 18 is increased from 380 ℃ to 495 ℃, and simultaneously, the first H is completed 2 +N 2 →NH 3 The adiabatic reaction task of (2); the synthesis gas at 495 deg.C is cooled to 380 deg.C by cold air from F1 cold air pipe 14 in I-stage heat exchanger 6, and then enters II-stage radial catalyst bed 19, and the temperature is raised from 380 deg.C to 495 deg.C, and at the same time, the second H is completed 2 +N 2 →NH 3 The adiabatic reaction task of (2); the synthesis gas at 495 ℃ is cooled to 380 ℃ by cold air from a F2 cold air pipe 15 in the II-stage heat exchanger 7, then enters the end-stage radial catalyst bed 22 for reaction, the temperature is increased from 380 ℃ to 495 ℃, and the third H is completed 2 +N 2 →NH 3 In the reaction task of the synthetic ammonia, the reaction heat of the end-stage radial catalyst bed layer 22 is absorbed by a water heat transfer tube bundle embedded in the catalyst bed layer and converted into 12.0MPa steam, and meanwhile, the temperature of the end-stage radial catalyst bed layer 22 is always kept in an isothermal state at 380 ℃.
The nested multi-bed tail end isothermal ammonia synthesis reactor in the embodiment comprises a I-level radial catalyst bed 18, a II-level radial catalyst bed 19, a \8230a \8230ann-level radial catalyst bed, a tail end radial catalyst isothermal bed 22, a gas distributor 11, an I-level redistribution heat exchanger 23, a II-level redistribution heat exchanger 24, an \8230an \8230anl-level redistribution heat exchanger and the like which are respectively sleeved around a gas collecting cylinder 8 to form I-level, II-level and III-level \8230an \8230andan n-level multi-section indirect heat exchange nested radial catalyst bed;
the catalyst in each level of radial catalyst bed is a synthetic ammonia catalyst such as Fe system, ruthenium Ru, etc., the synthetic reaction pressure is in the range of 80-15.0 MPa, the bed temperature is in a certain isothermal zone in the range of 300-510 ℃, and the bed structure is a three-section nested radial bed.
The main technical parameters of a nested multi-bed-layer tail-end isothermal ammonia synthesis reactor for synthesizing 2000 tons of ammonia per day are as follows:
(1) Reactor specification phi 3200;
(2) Catalyst loading: 200m 3 The loading of catalyst in the bed layer from outside to inside is 40m 3 、60m 3 、100m 3 ；
(3) The most important operating economic index list:
| parameter name | Electric power consumption | Cold energy consumption | Byproduct steam | Gas flow into the tower | Byproduct of 12MPa steam |
| Unit | KWh/tNH 3 | KCal/tNH 3 | kg/tNH 3 | Nm 3 /tNH 3 | kg/tNH 3 |
| Economic index | 105 | 73262.60 | 1689.20 | 4698.82 | 1100 |
In summary, the nested multi-bed-layer tail-end isothermal ammonia synthesis reactor of the embodiment comprises a stage I radial catalyst bed, a stage II radial catalyst bed, a stage 8230, a stage n radial catalyst bed and a tail-end isothermal radial bed which are respectively sleeved around a gas collecting cylinder to form stage I, stage II and stage III 8230, a stage n multi-section indirect heat exchange and water heat transfer nested radial catalyst bed, and the nested multi-bed tail-end isothermal ammonia synthesis reactor has the advantages of reduced equipment height, thorough stress elimination and reduced engineering cost.
Although embodiments of the present invention have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention, and that variations, modifications, substitutions and alterations can be made to the above embodiments by those of ordinary skill in the art within the scope of the present invention.
Claims (10)
1. A nested multi-bed, end-point, isothermal ammonia synthesis reactor, characterized by: the multi-stage radial catalyst bed layers are sequentially arranged from outside to inside, adjacent two-stage radial catalyst bed layers are communicated, the gas mixing distribution assembly is arranged outside the radial catalyst bed layer positioned on the outermost side, the gas mixing distribution assembly is communicated with the radial catalyst bed layer positioned on the outermost side, the radial catalyst bed layer positioned on the innermost side is communicated with the synthesis gas collector, and the water heat transfer tube bundle removes reaction heat of the radial catalyst bed layer positioned on the innermost side through a heat exchange effect to enable the reaction heat to be an isothermal bed layer;
the water heat transfer tube bundle comprises a water inlet main pipe, a water dividing ball cavity, a heat exchange water pipe, a water collecting ball cavity and a water outlet main pipe; the heat exchange water pipes are distributed inside the innermost radial catalyst bed layer at intervals, the lower end of each heat exchange water pipe is communicated with the corresponding water distribution ball cavity, the upper end of each water distribution ball cavity is communicated with the corresponding water collection ball cavity, the upper end of each water collection ball cavity is communicated with the corresponding water outlet main pipe, the lower end of each water distribution ball cavity is communicated with the corresponding water inlet main pipe, the tail end of each water outlet main pipe is led out to the outside of the isothermal ammonia synthesis reactor at the tail end of the multiple beds of the suit, and the starting end of each water inlet main pipe is led out to the outside of the isothermal ammonia synthesis reactor at the tail end of the multiple beds of the suit.
2. The nested multi-bed, end-point, isothermal ammonia synthesis reactor of claim 1, wherein: the multistage radial catalyst bed layer comprises a first-stage radial catalyst bed layer, a second-stage radial catalyst bed layer and a tail end radial catalyst bed layer; the second-stage radial catalyst bed layer is sleeved outside the tail-end radial catalyst bed layer and communicated with the tail-end radial catalyst bed layer, the first-stage radial catalyst bed layer is sleeved outside the second-stage radial catalyst bed layer and communicated with the second-stage radial catalyst bed layer, and the gas mixing distribution assembly is arranged outside the first-stage radial catalyst bed layer and communicated with the first-stage radial catalyst bed layer.
3. The nested multi-bed, end-point, isothermal ammonia synthesis reactor of claim 2, wherein: the gas mixing and distributing assembly comprises an F0 cold gas pipe, an internal flat cover, an F0 distributor, a gas mixing chamber, an internal cylinder, a gas distributing chamber, a catalyst frame lower end socket, an F1 cold gas pipe, an F2 cold gas pipe, a bed layer sealing pattern plate and a gas distributor; the flat lid of internals sets up the upper end of internals barrel, catalyst frame low head sets up the lower extreme of internals barrel, the gas distribution room is located gas distributor with between the internals barrel, the gas mixing room is located gas distributor with between the flat lid of internals, the gas mixing room is located the top of gas distribution room and communicates rather than, the distributor sets up in the gas mixing room, the bed seals the card setting and is in the upper end of radial catalyst bed of one-level, the radial catalyst bed of second grade, the radial catalyst bed of end.
4. A nested multi-bed end-point isothermal ammonia synthesis reactor according to claim 3, wherein: the first-stage radial catalyst bed layer comprises a first-stage radial catalyst bed, a first-stage heat exchanger, a first-stage cold air outlet of the heat exchanger, a first-stage redistribution heat exchanger and a first-stage gas redistributor; the catalyst bed comprises a bed layer sealing flower plate, a catalyst frame lower end socket, a primary radial catalyst bed, a primary heat exchanger, a primary redistribution heat exchanger and a primary gas redistributor, wherein the primary radial catalyst bed, the primary heat exchanger, the primary redistribution heat exchanger and the primary gas redistributor are sequentially arranged from outside to inside, a cold air outlet of the primary heat exchanger is arranged at the upper end of the primary heat exchanger and is positioned in a gas mixing chamber, the primary heat exchanger is arranged on the outer side of the primary redistribution heat exchanger, the primary heat exchanger and the primary redistribution heat exchanger are all in a cylinder shape, and the bed layer sealing flower plate, the catalyst frame lower end socket, the primary radial catalyst bed, the primary heat exchanger, the primary redistribution heat exchanger and the primary gas redistributor form a hollow cylinder.
5. The nested multi-bed end-point isothermal ammonia synthesis reactor of claim 4, wherein: the second-stage radial catalyst bed layer comprises a second-stage radial catalyst bed, a second-stage heat exchanger, a cold air outlet of the second-stage heat exchanger, a second-stage redistributor heat exchanger and a second-stage gas redistributor; the secondary radial catalyst bed, the secondary heat exchanger, the secondary redistribution heat exchanger and the secondary gas redistributor are sequentially arranged from outside to inside, a cold air outlet of the secondary heat exchanger is arranged in the gas mixing chamber, the secondary heat exchanger is arranged on the outer side of the secondary redistribution heat exchanger, the secondary heat exchanger and the secondary redistribution heat exchanger are all in a cylindrical shape, and the bed layer sealing pattern plate, the catalyst frame lower end socket, the secondary radial catalyst bed, the secondary heat exchanger, the secondary redistribution heat exchanger and the secondary gas redistributor form a hollow cylinder.
6. The nested multi-bed end-point isothermal ammonia synthesis reactor of claim 5, wherein: the F0 cold air pipe penetrates through the flat cover of the internal part and is connected with the F0 distributor; the F1 cold air pipe and the F2 cold air pipe sequentially penetrate through the flat cover of the internal part and the upper end of the gas distributor from top to bottom and are respectively communicated with the primary heat exchanger and the secondary heat exchanger.
7. The nested multi-bed end-point isothermal ammonia synthesis reactor of claim 6, wherein: the tail end radial catalyst bed layer is a tail end radial catalyst bed, the synthetic gas collector comprises a gas collecting cylinder, a gas outlet straight connecting pipe, a gas side ball cavity and a gas side channel, the tail end radial catalyst bed is sleeved outside the gas collecting cylinder and communicated with the gas collecting cylinder, and is positioned on the inner side of the secondary gas redistributor, the upper end of the gas collecting cylinder is closed, the lower end of the gas collecting cylinder is communicated with the gas side channel through the gas side ball cavity, and the gas side channel is communicated with the gas outlet straight connecting pipe.
8. The nested multi-bed end-point isothermal ammonia synthesis reactor structure of claim 2, wherein: the catalyst filled in the first-stage radial catalyst bed, the second-stage radial catalyst bed and the tail end radial catalyst bed is a synthetic ammonia catalyst.
9. The nested multi-bed end-point isothermal ammonia synthesis reactor of claim 8, wherein: the synthetic reaction pressure of the indirect heat exchange nested radial multi-section bed layer structure is 80-15.0 Mpa, and the temperature of the first-stage radial catalyst bed layer, the second-stage radial catalyst bed layer and the tail-end radial catalyst bed layer is 300-510 ℃.
10. The nested multi-bed, end-point, isothermal ammonia synthesis reactor of claim 1, wherein: the gas mixing distribution assembly is provided with a shell upper end enclosure, a shell barrel and a shell lower end enclosure at the periphery, and the shell upper end enclosure, the shell barrel and the shell lower end enclosure are sequentially connected to form a shell.
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| CN202211501863.8A CN115893446A (en) | 2022-11-28 | 2022-11-28 | Nested multi-bed tail end isothermal ammonia synthesis reactor |
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| CN202211501863.8A CN115893446A (en) | 2022-11-28 | 2022-11-28 | Nested multi-bed tail end isothermal ammonia synthesis reactor |
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