CN109395670B - Temperature-changing isothermal transformation reaction device - Google Patents
Temperature-changing isothermal transformation reaction device Download PDFInfo
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- CN109395670B CN109395670B CN201811160805.7A CN201811160805A CN109395670B CN 109395670 B CN109395670 B CN 109395670B CN 201811160805 A CN201811160805 A CN 201811160805A CN 109395670 B CN109395670 B CN 109395670B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0285—Heating or cooling the reactor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00194—Tubes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/02—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles
Abstract
The invention relates to a variable-temperature isothermal transformation reaction device, which comprises a furnace body and a catalyst frame arranged in the furnace body, wherein a synthesis gas collecting pipe is arranged in the middle of the catalyst frame; the device is characterized in that a plurality of raw material gas preheating pipes are also arranged in the catalyst frame, the inlets of the raw material gas preheating pipes are connected with a first raw material gas conveying pipeline, and the outlets of the raw material gas preheating pipes are communicated with a cavity between the catalyst frame and the furnace body; the furnace body is provided with a raw material gas inlet which is connected with a second raw material gas conveying pipeline, and the second raw material gas conveying pipeline is communicated with a first medium channel of the heat exchanger; the outlet of the synthesis gas collecting pipe is connected with a first branch and a second branch, and the second branch is communicated with a second medium channel of the heat exchanger; the first raw material gas conveying pipeline is provided with a first valve, and the second raw material gas conveying pipeline is provided with a second valve.
Description
Technical Field
The invention relates to chemical equipment, in particular to an isothermal transformation reaction device.
Background
CO + H shift reaction2O ↔H2+CO2The reaction is exothermic, the temperature of the conversion gas can reach about 450 ℃ after the reaction is completed, but the energy barrier (reaction activity) of the reaction is higher, and the reaction raw material, namely the raw gas, needs to be heated to 260 ℃ or higher before the reaction. Therefore, the prior conversion process uses a conversion gas crude gas heat exchanger, and utilizes conversion gas with high temperature generated after the conversion reaction to exchange heat with crude gas before the conversion reaction. Can save a large amount of energy sources and can greatly improve the reaction rate and efficiency. However, because the temperature at the outlet of the converter is very high, the pressure of the conversion reaction is very high, generally 3-6 MPa, and higher requirements are provided for the material and the thickness of the shell of the converter. With the further expansion of single-line production capacity of chemical engineering projects, the size of a single shift reactor is further increased, the diameter of the current large-scale shift converter can reach 4800mm, the thickness of an equipment shell reaches 110mm, the material cost and the manufacturing cost are greatly increased, and higher requirements are provided for processing technology and equipment transportation.
Because of different medium components in the shift converter, when the water-gas ratio is too low, the temperature can rise rapidly, and when the heat is not removed in time, the phenomena of temperature runaway (rapid rise of a reaction zone in equipment) and the like can occur. The methanation reaction can be caused after the temperature in the equipment is too high, when the condition occurs, the temperature in the equipment can reach 600-800 ℃, and when the working condition occurs, the catalyst loses activity due to the too high temperature, and needs to be replaced, thereby causing great economic loss. Moreover, when the temperature of the equipment wall is too high, the strength of the equipment is also sharply reduced, and a huge safety risk is brought to the production of the whole device.
In order to control the stable performance of the CO shift reaction at the designed temperature, it is generally adopted to arrange a heat exchange tube in the reactor, and to remove the heat generated by the shift reaction by passing cooling water through the heat exchange tube, thereby controlling the reaction temperature.
However, as the reaction proceeds, the catalyst activity decreases, and the catalyst activity temperature increases from about 240 ℃ to about 280 ℃, which requires a corresponding increase in the reaction temperature. The existing method for solving the problem generally increases the temperature of cooling water and heat exchange steam at the later stage of reaction, which inevitably leads to the pressure in a steam drum and a heat exchange tube to be increased sharply; and the design wall thickness of the steam pocket and the heat exchange tube is correspondingly increased. In addition to the strict requirement on equipment, a series of other problems can also be caused, for example, the heat transfer coefficient of the heat exchange tube is reduced due to the increase of the wall thickness of the heat exchange tube, and the heat exchange amount in the early stage of the reaction also needs to be increased; moreover, due to the change of the temperature and the pressure of the steam outlet drum, the corresponding change of the matched pipeline and the equipment is necessarily caused. A series of problems are brought about.
Disclosure of Invention
The invention aims to solve the technical problem of providing a temperature-variable isothermal shift reaction device which can maintain constant yield in the whole active period of a catalyst without increasing the wall thickness of equipment aiming at the current situation of the prior art.
The technical scheme adopted by the invention for solving the technical problems is as follows: the variable-temperature isothermal transformation reaction device comprises a furnace body and a catalyst frame arranged in the furnace body, wherein a synthesis gas collecting pipe is arranged in the middle of the catalyst frame, a heat exchange pipe is arranged in the catalyst frame, an inlet of the heat exchange pipe is connected with a water inlet pipeline, and an outlet of the heat exchange pipe is connected with a steam pipeline;
the method is characterized in that:
a plurality of raw material gas preheating pipes are further arranged in the catalyst frame, inlets of the raw material gas preheating pipes are connected with a first raw material gas conveying pipeline, and outlets of the raw material gas preheating pipes are communicated with a cavity between the catalyst frame and the furnace body;
the furnace body is provided with a raw material gas inlet, the raw material gas inlet is connected with a second raw material gas conveying pipeline, and the second raw material gas conveying pipeline is communicated with a first medium channel of the heat exchanger;
the outlet of the synthesis gas collecting pipe is connected with a first branch and a second branch, valves are arranged on the first branch and the second branch, the first branch is connected with the downstream, and the second branch is communicated with a second medium channel of the heat exchanger;
and a first valve is arranged on the first raw material gas conveying pipeline, and a second valve is arranged on the second raw material gas conveying pipeline.
Preferably the synthesis gas inlet is provided at the upper or top of the furnace.
Further, the inlet of each raw material gas preheating pipe can be communicated with a gas distributor, the inlet of the gas distributor is connected with the first raw material gas conveying pipeline, and the gas distributor is arranged at the lower part of the furnace body; and the outlet of each raw material gas preheating pipe is communicated with a cavity between the catalyst frame and the upper part of the furnace body. The design of the gas distributor can ensure that the raw material gas uniformly enters each raw material gas preheating pipe, thereby further ensuring the uniformity of heat removal of the catalyst bed layer.
Preferably, the synthesis gas collecting pipe is connected with a synthesis gas conveying pipeline, and the synthesis gas conveying pipeline is connected with the second medium channel of the heat exchanger.
As a further improvement of each of the above aspects, each of the feed gas preheating tubes is arranged uniformly in a cavity between the catalyst frame and the synthesis gas collecting tube along a cross section of the catalyst frame; the heat exchange tubes are respectively and uniformly arranged at the periphery of the corresponding raw material gas preheating tube, and at least three heat exchange tubes are uniformly distributed around each raw material gas preheating tube;
each feed gas preheating pipe and each heat exchange pipe arranged around the feed gas preheating pipe form a pipe group. The scheme can further ensure the uniformity of heat removal of the catalyst bed layer in the whole operation process of the device.
Preferably, 3-6 heat exchange tubes are arranged around each feed gas preheating tube.
Preferably, the centers of the heat exchange tubes in each tube group are uniformly distributed on a circumference line which takes the center of the feed gas preheating tube as a circle center.
Furthermore, part of the heat exchange tubes can be shared between the adjacent tube groups, so that the arrangement of each heat exchange tube at the position of the catalyst bed layer is more reasonable, and the heat removal of the catalyst bed layer is more uniform after the feed gas preheating tube is closed.
In each of the above schemes, the steam pipeline may include a steam connecting pipe and a steam collecting pipe, and an outlet of the steam collecting pipe is connected to the steam connecting pipe; an expansion joint is arranged on the steam connecting pipe;
the water inlet pipeline comprises a water inlet connecting pipe and a pipe box communicated with the outlet of the water inlet connecting pipe; and the inlet of each heat exchange tube is respectively communicated with the outlet of the tube box.
For convenient maintenance, the synthesis gas collecting pipe can be formed by connecting the multistage barrel in a detachable mode in sequence, and a plurality of foot ladders are arranged on the inner side wall of the barrel at intervals in sequence along the axial direction.
Compared with the prior art, the temperature-variable isothermal shift reaction device provided by the invention overcomes the prejudice of the prior art, the isothermal shift reactor is designed into the temperature-variable isothermal shift reaction device, the heat exchange tube and the feed gas preheating tube are arranged at the catalyst bed layer position, and the heat removal quantity can be changed according to the activity requirement of the catalyst at each stage of the operation of the device, so that the requirement of the catalyst activity temperature at different reaction stages is met, the yield is kept constant, and the problems of increased wall thickness of the heat exchange tube, increased wall thickness of the steam pocket, changed matching pipelines and equipment and the like caused by the method that the pressure in the steam pocket and the heat exchange tube is increased to improve the reaction temperature at the later reaction stage in the prior art are avoided, the equipment investment is reduced, and the problem of difficult later-stage control is avoided.
Drawings
FIG. 1 is a schematic diagram of an embodiment of the present invention;
FIG. 2 is a longitudinal sectional view of a reactor section in an embodiment of the invention;
FIG. 3 is a cross-sectional view taken along line A-A of FIG. 2;
FIG. 4 is a cross-sectional view taken along line B-B of FIG. 2;
FIG. 5 is an enlarged view of a portion C of FIG. 3;
fig. 6 is a partially enlarged view of a portion D in fig. 5.
Detailed Description
The invention is described in further detail below with reference to the accompanying examples.
As shown in fig. 1 to 6, the temperature-variable isothermal shift reaction apparatus includes:
the furnace body 1 is of a conventional structure and comprises an upper seal head 11, a lower seal head 12 and a cylinder body 13 connected between the upper seal head 11 and the lower seal head 12. The upper seal head 11 is provided with a manhole 15 and a raw material gas inlet 14, and the raw material gas inlet is connected with a second raw material gas conveying pipeline 62. The second raw material gas conveying pipeline 62 is provided with a heat exchanger 65 and a first medium channel communicated with the heat exchanger 65; a second valve 64 is also provided on the second feed gas delivery conduit 62. The inlet of the second raw material gas delivery pipe 62 is communicated with the raw material gas pipe.
The catalyst frame 2 is used for filling a catalyst and is arranged in the cylinder 13. The catalyst frame 2 may be any one of the prior art as required, and may be an axial reactor, a radial reactor, or an axial-radial reactor, for example, which may be set as required. In this embodiment, the reactor is a radial reactor, the raw material gas enters the catalyst frame from through holes (not shown) on the sidewall of the catalyst frame 2, and the through holes on the sidewall of the catalyst frame function as gas distributors.
The synthesis gas collecting pipe 3 is used for collecting synthesis gas and sending the synthesis gas out of the furnace body 1 through a synthesis gas conveying pipeline 33, is arranged in the middle of the inner cavity of the catalyst frame, and is formed by sequentially and detachably connecting a plurality of sections of cylinders 31, and in the embodiment, the cylinders 31 are connected through flanges 34; the side wall of each cylinder 31 is provided with a plurality of air inlets (not shown in the figure) for the synthesis gas to enter the synthesis gas collecting pipe 3 from the catalyst bed layer; a plurality of footsteps 32 are sequentially arranged on the inner side wall of the cylinder 31 at intervals along the axial direction. The end cover is detachably connected to the upper end port of the synthesis gas collecting pipe 3, and is communicated with the manhole 15 after being disassembled, so that an overhaul worker can enter the synthesis gas collecting pipe 3; the lower port of the synthesis gas collecting tube 3 is connected with a synthesis gas conveying pipe 33. The synthesis gas conveying pipeline 33 is connected with a first branch 35 and a second branch 36, valves are arranged on the first branch 35 and the second branch 36, the first branch 35 is connected with the downstream, and the second branch 36 is connected with a second medium channel of the heat exchanger 65.
The feed gas preheating pipes 6 are vertically arranged in a cavity between the catalyst frame and the synthesis gas collecting pipe in parallel with the axis of the furnace body 1 and are uniformly arranged. The inlet connection of each raw material gas preheating pipe 6 all communicates the gas distributor, first raw material gas pipeline 61 is connected to the entry of gas distributor, is equipped with first valve 63 on the first raw material gas pipeline 61, and first raw material gas pipeline 61 is connected the raw material gas pipeline.
The gas distributor is arranged at the lower part of the furnace body; the outlet of each raw material gas preheating pipe 6 is limited on the upper end plate of the catalyst frame 2 and exposed out of the upper end plate, so that the preheated raw material gas enters the cavity between the catalyst frame and the upper end enclosure and further enters the catalyst frame from the gap between the catalyst frame and the side wall of the cylinder body through each through hole.
And a plurality of heat exchange tubes 4 are arranged in the space between the catalyst frame 2 and the synthesis gas collecting tube 3 and are parallel to the feed gas preheating tubes 6. Each heat exchange tube can be a straight tube, a corrugated tube or a U-shaped tube, and any one of the prior art can be selected according to the requirement. This embodiment is a straight tube.
For the sake of distinction, each feed gas preheating tube is represented by a filled circle and each heat exchange tube is represented by a hollow circle in fig. 2.
In the embodiment, the heat exchange tubes 4 are uniformly arranged along the peripheries of the corresponding raw material gas preheating tubes 6, and six heat exchange tubes 4 are uniformly distributed around each raw material gas preheating tube 6; all the heat exchange tubes in all the heat exchange tube pairs are uniformly distributed on a circumferential line L which takes the center of the corresponding feed gas preheating tube as the circle center.
The number of heat exchange tubes in each tube group may be designed in other numbers depending on the scale of the apparatus and the specification of the reactor, for example, three, four, five or more.
Each raw material gas preheating pipe 6 and each heat exchange pipe 4 arranged around it form a pipe group, and a part of the heat exchange pipes 4 are shared between adjacent pipe groups, i.e. the circumferential lines L where each heat exchange pipe is located in the adjacent pipe groups are arranged crosswise.
A water inlet pipe for communicating a steam drum (not shown) with each heat exchange pipe, including a water inlet connection pipe 51 and a pipe box 52 communicated with an outlet of the water inlet connection pipe 51; the tube box 52 may be a loop structure, as shown in fig. 1 of the present embodiment, or a box structure, and any one of the prior arts may be used according to the needs.
The inlet of each heat exchange tube 4 is communicated with the tube box 52.
A steam pipe including a steam connection pipe 53 and a steam collection pipe to connect the steam drum; the outlet of the steam collecting pipe is connected with a steam connecting pipe 53, and the inlets of the steam collecting pipe are respectively connected with the outlet of the heat exchange pipe.
The steam collecting pipe can be a ring pipe structure, a box body structure or other structures.
And an expansion joint 55 provided in the two steam connection pipes 53 to provide an expansion margin of the steam connection pipes.
At the initial stage of the operation of the device, the activity of the catalyst is high, the first valve is opened, the second valve is closed, the valve on the second branch is closed, and the valve on the first branch is opened; cold feed gas enters the feed gas heat exchange tube from the first feed gas conveying pipeline; cooling water enters each heat exchange tube from a water inlet pipeline, after the cooling water exchanges heat with reaction heat of the catalyst bed layer, the raw material gas reaches the feeding temperature, enters the cavity of the upper end enclosure from the outlet of each raw material gas heat exchange tube, descends along the gap between the catalyst frame and the cylinder body, enters the catalyst bed layer through each through hole on the side wall of the catalyst frame, and performs conversion reaction; the cooling water in each heat exchange tube is heated to be changed into steam, and the steam is returned to the steam pocket through the steam pipeline. The synthesis gas obtained from the shift reaction is discharged through the first branch and enters the downstream.
The catalyst in the stage has low activity temperature and more heat to be removed, the raw material gas and the cooling water are heated simultaneously, the catalyst bed layer is maintained at the set temperature for conversion reaction, and the yield is constant at the set value.
In the later stage of the operation of the device, the activity temperature of the catalyst is increased due to the reduction of the activity of the catalyst; maintaining parameters such as water, steam pressure and the like of the steam drum and the boiler in the steam drum unchanged, closing the first valve, opening the second valve, opening the valve on the second branch and closing the valve on the first branch; the raw material gas enters the heat exchanger from the second raw material gas conveying pipeline, exchanges heat with the high-temperature synthesis gas from the second branch, and enters the cavity of the upper end enclosure through the raw material gas inlet. Cooling water is still introduced into each heat exchange tube to take away the reaction heat generated by the catalyst bed layer. Because the feed gas does not participate in the heat exchange of the catalyst bed layer, only the cooling water in the heat exchange tube takes heat, so the heat exchange amount is reduced, the heat removal amount of the catalyst bed layer is reduced, the temperature of the catalyst bed layer is increased, the requirement of the activity temperature of the catalyst at the later stage is met, the conversion reaction is normally carried out, and the yield is still maintained at the design value; and the steam pressure of the steam outlet drum is unchanged, and parameters of matched pipelines and equipment do not need to be changed.
Due to the special arrangement of the feed gas preheating tubes and the heat exchange tubes, the heat exchange tubes can still uniformly remove heat from the catalyst bed even if the feed gas preheating tubes are closed.
Claims (8)
1. A variable-temperature isothermal shift reaction device comprises a furnace body (1) and a catalyst frame (2) arranged in the furnace body (1), wherein a synthesis gas collecting pipe (3) is arranged in the middle of the catalyst frame (2), a heat exchange pipe (4) is arranged in the catalyst frame (2), an inlet of the heat exchange pipe is connected with a water inlet pipeline, and an outlet of the heat exchange pipe is connected with a steam pipeline;
the method is characterized in that:
a plurality of raw material gas preheating pipes (6) are further arranged in the catalyst frame (2), inlets of the raw material gas preheating pipes (6) are connected with a first raw material gas conveying pipeline (61), and outlets of the raw material gas preheating pipes (6) are communicated with a cavity between the catalyst frame (2) and the furnace body (1);
a raw material gas inlet (14) is formed in the furnace body (1), the raw material gas inlet (14) is connected with a second raw material gas conveying pipeline (62), and the second raw material gas conveying pipeline is communicated with a first medium channel of the heat exchanger (65);
the outlet of the synthesis gas collecting pipe (3) is connected with a first branch (35) and a second branch (36), valves are arranged on the first branch (35) and the second branch (36), the first branch (35) is connected with the downstream, and the second branch (36) is communicated with a second medium channel of the heat exchanger (65);
a first valve (63) is arranged on the first raw material gas conveying pipeline (61), and a second valve (64) is arranged on the second raw material gas conveying pipeline (62);
the raw material gas inlet is arranged at the upper part of the furnace body (1);
each feed gas preheating tube (6) is uniformly arranged in a cavity between the catalyst frame and the synthesis gas collecting tube along the cross section of the catalyst frame (2); the heat exchange tubes (4) are respectively and uniformly arranged at the periphery of the corresponding raw material gas preheating tube (6), and at least three heat exchange tubes (4) are uniformly distributed around each raw material gas preheating tube (6);
each raw material gas preheating pipe (6) and each heat exchange pipe (4) arranged around the raw material gas preheating pipe form a pipe group.
2. The temperature-changing isothermal shift reaction device according to claim 1, wherein the inlet of each raw material gas preheating pipe (6) is communicated with a gas distributor, the inlet of the gas distributor is connected with the first raw material gas conveying pipeline (61), and the gas distributor is arranged at the lower part of the furnace body; the outlet of each raw material gas preheating pipe (6) is communicated with a cavity between the catalyst frame (2) and the upper part of the furnace body (1).
3. The temperature-swing isothermal shift reaction device according to claim 1, characterized in that said synthesis gas collecting header (3) is connected to a synthesis gas conveying pipe (33), said synthesis gas conveying pipe (33) being connected to the second medium passage of said heat exchanger (65).
4. The temperature-changing isothermal shift reaction device according to claim 1, wherein 3-6 heat exchange tubes (4) are arranged around each feed gas preheating tube (6).
5. The temperature-changing isothermal shift reaction device according to claim 2, wherein the centers of the heat exchange tubes in each tube group are uniformly distributed on a circumferential line with the center of the feed gas preheating tube as a circle center.
6. The temperature-changing isothermal shift reaction device according to claim 3, characterized in that a part of said heat exchange tubes (4) are shared between adjacent tube groups.
7. The temperature-changing isothermal shift reaction device according to claim 1, characterized in that said vapor pipeline comprises a vapor connection pipe (53) and a vapor collection pipe, an outlet of said vapor collection pipe is connected to said vapor connection pipe (53); an expansion joint (55) is arranged on the steam connecting pipe (53);
the water inlet pipeline comprises a water inlet connecting pipe (51) and a pipe box (52) communicated with the outlet of the water inlet connecting pipe (51); the inlets of the heat exchange tubes are respectively communicated with the outlets of the tube box (52).
8. The temperature-changing isothermal shift reaction device according to claim 1, wherein said synthesis gas collecting tube (3) is formed by sequentially connecting a plurality of sections of tube bodies (31) in a detachable manner, and a plurality of step ladders (32) are sequentially arranged on the inner side wall of said tube bodies (31) at intervals along the axial direction.
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Citations (7)
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| US3663179A (en) * | 1970-04-20 | 1972-05-16 | Chemical Construction Corp | Apparatus for exothermic catalytic reactions |
| JPS6061544A (en) * | 1983-09-06 | 1985-04-09 | エム・アー・エン・マシーネンフアブリーク・アウクスブルク‐ニユルンベルク・アクチエンゲゼルシヤフト | Vertical reactor for methanol manufacture |
| CN102836676A (en) * | 2012-09-28 | 2012-12-26 | 神华集团有限责任公司 | Gas-solid phase catalytic reactor |
| CN202893318U (en) * | 2012-10-08 | 2013-04-24 | 中国石油化工集团公司 | CO total radial isothermal transformation furnace |
| CN205235934U (en) * | 2015-12-16 | 2016-05-18 | 河南顺达化工科技有限公司 | Adiabatic ethanol synthesis reactor |
| CN107398238A (en) * | 2016-05-20 | 2017-11-28 | 中国石化工程建设有限公司 | A kind of isothermal reactor |
| CN108404821A (en) * | 2018-05-22 | 2018-08-17 | 中石化宁波工程有限公司 | A kind of energy-saving and high efficient radial direction methanol reactor |
-
2018
- 2018-09-30 CN CN201811160805.7A patent/CN109395670B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3663179A (en) * | 1970-04-20 | 1972-05-16 | Chemical Construction Corp | Apparatus for exothermic catalytic reactions |
| JPS6061544A (en) * | 1983-09-06 | 1985-04-09 | エム・アー・エン・マシーネンフアブリーク・アウクスブルク‐ニユルンベルク・アクチエンゲゼルシヤフト | Vertical reactor for methanol manufacture |
| CN102836676A (en) * | 2012-09-28 | 2012-12-26 | 神华集团有限责任公司 | Gas-solid phase catalytic reactor |
| CN202893318U (en) * | 2012-10-08 | 2013-04-24 | 中国石油化工集团公司 | CO total radial isothermal transformation furnace |
| CN205235934U (en) * | 2015-12-16 | 2016-05-18 | 河南顺达化工科技有限公司 | Adiabatic ethanol synthesis reactor |
| CN107398238A (en) * | 2016-05-20 | 2017-11-28 | 中国石化工程建设有限公司 | A kind of isothermal reactor |
| CN108404821A (en) * | 2018-05-22 | 2018-08-17 | 中石化宁波工程有限公司 | A kind of energy-saving and high efficient radial direction methanol reactor |
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