CN109052318B - Isothermal shift reactor - Google Patents
Isothermal shift reactor Download PDFInfo
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- CN109052318B CN109052318B CN201811160882.2A CN201811160882A CN109052318B CN 109052318 B CN109052318 B CN 109052318B CN 201811160882 A CN201811160882 A CN 201811160882A CN 109052318 B CN109052318 B CN 109052318B
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- heat exchange
- gas
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- exchange tube
- catalyst
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
- C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
- C01B3/16—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
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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
-
- 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
Abstract
The invention relates to an isothermal shift reactor, which comprises a furnace body and a catalyst frame arranged in the furnace body, wherein a shift gas collecting pipe is arranged in the middle of the catalyst frame, one port of the shift gas collecting pipe is closed, the other port of the shift gas collecting pipe is connected with the outside, and a plurality of air inlets are arranged on the side wall of the shift gas collecting pipe at intervals; the wall of the catalyst frame is provided with a through hole for communicating the inner space and the outer space of the catalyst frame; a plurality of heat exchange tubes are arranged in a cavity between the catalyst frame and the shift gas collecting tube; the heat exchange system is characterized in that each heat exchange tube is divided into a plurality of heat exchange tube sets, and each heat exchange tube set comprises a first heat exchange tube and a plurality of second heat exchange tubes; each second heat exchange pipe is arranged around the first heat exchange pipe; the lower port of the first heat exchange tube is connected with a cooling water pipeline, and the lower port of the second heat exchange tube is connected with a steam collecting pipeline; the lower port of the second heat exchange tube of the first heat exchange tube is communicated with a cavity between the catalyst frame and the furnace body; the upper ports of the first heat exchange tube and the second heat exchange tube are both communicated with the inner cavity of the tube cap, and the tube cap is of a closed cavity structure.
Description
Technical Field
The invention relates to chemical equipment, in particular to an isothermal shift reactor.
Background
CO shift reaction
The 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 materials need to be heated to the reaction temperature before the reaction. The existing methods for heating the raw material gas have various kinds, because of different medium components in the shift converter, when the water-gas ratio is too low, the temperature can rise rapidly, 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.
Disclosure of Invention
The invention aims to provide an isothermal transformation reactor with accurate temperature control 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 isothermal shift reactor comprises a furnace body and a catalyst frame arranged in the furnace body, wherein a shift gas collecting pipe is arranged in the middle of the catalyst frame; a raw material gas channel connected with the inner cavity of the furnace body is arranged between the catalyst frame and the side wall of the furnace body, and a plurality of through holes communicated with the raw material gas channel and the inner cavity of the catalyst frame are arranged on the side wall of the catalyst frame at intervals; one end of the change gas collecting pipe is closed, the other end of the change gas collecting pipe is connected with the outside, a plurality of air inlets are arranged on the side wall of the change gas collecting pipe at intervals, and a plurality of heat exchange pipes are arranged on a catalyst bed layer between the catalyst frame and the change gas collecting pipe;
a raw material gas inlet is formed in the top of the furnace body and communicated with an inner cavity of the furnace body;
the heat exchange tube is characterized in that each heat exchange tube is divided into a plurality of heat exchange tube groups, and each heat exchange tube group comprises a first heat exchange tube and a plurality of second heat exchange tubes; each second heat exchange tube is arranged around the first heat exchange tube;
the lower port of the first heat exchange tube is connected with a cooling water pipeline, and the lower port of the second heat exchange tube is connected with a steam collecting pipeline; the lower port of the first heat exchange tube and the lower port of the second heat exchange tube are communicated with a cavity between the catalyst frame and the furnace body;
the upper end ports of the first heat exchange tube and the second heat exchange tube are communicated with the inner cavity of the tube cap, and the tube cap is of a closed cavity structure.
Preferably, the number of the second heat exchange tubes in each heat exchange tube group is 3-8, and the second heat exchange tubes are uniformly arranged around the first heat exchange tubes.
Preferably, the number of the second heat exchange tubes is 6.
As a further improvement of the above schemes, the pipe diameter of the second heat exchange pipe is smaller than that of the first heat exchange pipe. The first heat exchange tube is a cooling water tube, the second heat exchange tubes are main heat exchange tubes, the cross sections of all the second heat exchange tubes are larger than the cross section area of the first heat exchange tubes, so that the steam resistance is favorably reduced, and the heat exchange surface area can be increased by the plurality of second heat exchange tubes.
In order to stabilize the mounting structure of the first heat exchange tube and the second heat exchange tube, a first connecting rib plate is connected between the adjacent second heat exchange tubes in each heat exchange tube group; and second connecting rib plates are arranged between the first heat exchange tube and the second heat exchange tubes, and two ends of each second connecting rib plate are respectively connected with the outer wall of the first heat exchange tube and the corresponding first connecting rib plate.
Preferably, the first connection rib plates in the heat exchange tube sets are arranged along the same circumferential line.
In order to enable cooling water to uniformly enter each first heat exchange tube and uniformly heat the catalyst bed layer, the lower port of each first heat exchange tube is connected with a water inlet ring tube, and the inlet of the water inlet ring tube is connected with the cooling water pipeline;
in order to smoothly collect the generated steam, the lower port of each second heat exchange tube is connected with a steam collecting ring tube, and the outlet of the steam collecting ring tube is connected with the steam collecting pipeline.
Preferably, a raw material gas inlet is formed in the top of each furnace body, the raw material gas inlet is connected with an inlet of a gas distributor, and an outlet of the gas distributor is communicated with an inner cavity of the furnace body.
Better, for convenient the maintenance, the transform gas collecting pipe can be dismantled the connection in proper order by the multistage barrel and form, be equipped with a plurality of foot ladders along axial direction interval in proper order on the inside wall of barrel.
Compared with the prior art, the isothermal shift reaction device provided by the invention has the advantages that the heat exchange tubes are designed according to groups, the second heat exchange tubes in each group are uniformly distributed around the first heat exchange tubes, the retention time of the feed gas is long, secondary heat exchange is carried out in the catalyst bed layer, the heat removal of the catalyst bed layer is sufficient, the reaction temperature of the catalyst bed layer is accurately controlled, the feed gas is fully preheated, and the stable operation and the reaction effect of the device are ensured.
Drawings
FIG. 1 is a longitudinal cross-sectional view of an embodiment of the present invention;
FIG. 2 is a transverse cross-sectional view of an embodiment of the present invention;
FIG. 3 is a longitudinal cross-sectional view of a heat exchange tube set in an embodiment of the present invention;
FIG. 4 is a view taken along line A of FIG. 3;
fig. 5 is a sectional view taken along B-B in fig. 3.
Detailed Description
The invention is described in further detail below with reference to the accompanying examples.
As shown in fig. 1 to 5, the isothermal shift reactor 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 raw gas inlet 14, the lower seal head 12 is provided with a synthesis gas outlet 15, and the upper seal head and the lower seal head are both provided with manholes 16.
The upper end enclosure 11 is also internally provided with a gas distributor 7, the inlet of the gas distributor 7 is connected with a feed gas inlet 14, and the outlet of the gas distributor is communicated with the cavity of the upper end enclosure.
The catalyst frame 2 is used for filling a catalyst and is arranged in the cylinder 13. The catalyst frame 2 can be any one of the prior art according to the requirement, the embodiment is a radial reactor, a gap is arranged between the side wall of the catalyst frame and the inner side wall of the furnace body, and the gap is a raw material gas channel 17; the raw material gas channel 17 is communicated with the cavity of the upper end enclosure, the side wall of the catalyst frame is provided with a plurality of through holes (not shown in the figure), and the preheated raw material gas radially enters the catalyst bed layer in the catalyst frame from each through hole on the side wall of the catalyst frame 2.
The shift 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 pipeline 33, is arranged in the middle position in the cavity of the catalyst frame 2, and is formed by sequentially and detachably connecting a plurality of sections of cylinder bodies 31, and in the embodiment, the cylinder bodies 31 are connected through flanges 34; a plurality of air inlets (not shown) are arranged on the side wall of the barrel 31 at intervals, and a plurality of footsteps 32 are sequentially arranged on the inner side wall of the barrel 31 at intervals along the axial direction. The end cover is detachably connected to the upper port of the shift gas collecting pipe 3, the lower port of the shift gas collecting pipe 3 is connected with the synthesis gas outlet 15, the synthesis gas outlet 15 is connected with the synthesis gas pipeline 33, and synthesis gas generated by reaction is sent out through the synthesis gas pipeline 33.
And a plurality of groups of heat exchange tubes provided in the space between the catalyst frame 2 and the shift gas collecting header 3, the heat exchange tube groups 4 being arranged uniformly in the space between the catalyst frame 2 and the shift gas collecting header 3. Each group of heat exchange tube groups 4 comprises:
a first heat exchange tube 41 and a plurality of second heat exchange tubes 42; each of the second heat exchanging pipes 42 is arranged around the first heat exchanging pipe 41; in this embodiment, six second heat exchange tubes 42 are arranged around each first heat exchange tube 41, and the tube diameter of the second heat exchange tubes 42 is smaller than the tube diameter 41 of the first heat exchange tubes. The second heat exchange pipes 42 are uniformly distributed on the same circumference outside the first heat exchange pipe 41.
The lower end of each first heat exchange tube 41 is provided with a steam collecting loop 54, the outlet of the steam collecting loop 54 is connected with a steam collecting pipeline 52, and high-quality steam generated after heat exchange is sent out of the furnace body through the steam collecting pipeline 52.
The upper end parts of the first heat exchange tube 41 and the second heat exchange tube 42 are fixed on a cover plate 46 of a tube cap 45, the tube cap 6 is of a closed cavity structure, and the upper end openings of the first heat exchange tube 41 and the second heat exchange tube 42 are communicated with the inner cavity of the tube cap 45.
In each heat exchange tube set: a first connecting rib plate 43 is connected between the adjacent second heat exchange tubes 42; the first connection rib plates 43 in the heat exchange tube groups are arranged along the same circumferential line. Second connecting rib plates 44 are arranged between the first heat exchange tube 41 and the second heat exchange tube 42, and two ends of each second connecting rib plate 44 are respectively connected with the outer wall of the first heat exchange tube and the corresponding first connecting rib plate 43.
The second connection rib 44 and the first connection rib 43 may have a plate-like structure, or may have a rod-like or tubular structure.
The rest of the non-related content is the same as the prior art.
When the device is operated, the raw material gas enters the furnace body from the raw material gas inlet through the gas distributor, is uniformly dispersed by the gas distributor, enters the cavity of the furnace body, enters the catalyst bed layer from the raw material gas channel through the through holes, and carries out conversion reaction in the catalyst bed layer. The shift reaction gives off heat.
Boiler water, namely cooling water enters the cooling water ring pipe from a cooling water pipeline and then uniformly enters each first heat exchange pipe, the cooling water flows from bottom to top and exchanges heat with the reaction heat of the catalyst bed layer, and then sequentially enters the inner cavity of the pipe cap and each second heat exchange pipe to continuously exchange heat with the reaction heat of the catalyst bed layer to heat steam; the generated high-quality steam enters the steam collecting circular pipe and is sent out from the outside through the steam conveying pipeline.
After the raw material gas reacts in the catalyst bed layer, heat is generated, and reaction heat of the catalyst bed layer is taken away, so that the temperature of the catalyst bed layer is kept constant at the catalyst activity temperature; the synthesis gas generated by the reaction enters the shift gas collecting pipe from each gas inlet hole and is sent out through the synthesis gas pipeline.
Claims (1)
1. An isothermal shift reactor comprising:
the furnace body comprises an upper seal head, a lower seal head and a cylinder body connected between the upper seal head and the lower seal head; the upper end enclosure is provided with a raw gas inlet, the lower end enclosure is provided with a synthesis gas outlet, and the upper end enclosure and the lower end enclosure are both provided with manholes;
the upper end enclosure is internally provided with a gas distributor, the inlet of the gas distributor is connected with the feed gas inlet, and the outlet of the gas distributor is communicated with the cavity of the upper end enclosure;
the catalyst frame is used for filling a catalyst and is arranged in the cylinder; a gap is arranged between the side wall of the catalyst frame and the inner side wall of the furnace body, and the gap is a feed gas channel; the raw material gas channel is communicated with the cavity of the upper end enclosure, the side wall of the catalyst frame is provided with a plurality of through holes, and the preheated raw material gas radially enters the catalyst bed layer in the catalyst frame from each through hole on the side wall of the catalyst frame;
it is characterized by also comprising:
the shift gas collecting pipe is used for collecting the synthesis gas and sending the synthesis gas out of the furnace body through a synthesis gas pipeline, is arranged in the middle position in the cavity of the catalyst frame and is formed by sequentially and detachably connecting a plurality of sections of cylinders, and the cylinders are connected through flanges; a plurality of air inlets are arranged on the side wall of the barrel at intervals, and a plurality of foot ladders are sequentially arranged on the inner side wall of the barrel at intervals along the axial direction; the end cover is detachably connected to the upper port of the shift gas collecting pipe, the lower port of the shift gas collecting pipe is connected with a synthetic gas outlet, the synthetic gas outlet is connected with a synthetic gas pipeline, and synthetic gas generated by reaction is sent out through the synthetic gas pipeline;
the heat exchange tubes are arranged in the space between the catalyst frame and the conversion gas collecting tube, all the heat exchange tube groups are uniformly arranged in the space between the catalyst frame and the conversion gas collecting tube, and each heat exchange tube group comprises:
a first heat exchange tube and a plurality of second heat exchange tubes; each second heat exchange tube is arranged around the first heat exchange tube; six second heat exchange tubes are arranged around each first heat exchange tube, the pipe diameters of the second heat exchange tubes are smaller than those of the first heat exchange tubes, and the second heat exchange tubes are uniformly distributed on the same circumference line outside the first heat exchange tubes;
the lower port of each first heat exchange tube is provided with a steam collecting ring tube, the outlet of the steam collecting ring tube is connected with a steam collecting pipeline, and steam generated after heat exchange is sent out of the furnace body through the steam collecting pipeline;
the upper end parts of the first heat exchange tube and the second heat exchange tube are fixed on a cover plate of a tube cap, the tube cap is of a closed cavity structure, and the upper end ports of the first heat exchange tube and the second heat exchange tube are communicated with the inner cavity of the tube cap;
in each heat exchange tube set: a first connecting rib plate is connected between the adjacent second heat exchange tubes; each first connecting rib plate in each heat exchange pipe group is arranged along the same circumferential line; second connecting rib plates are arranged between the first heat exchange tube and the second heat exchange tubes, and two ends of each second connecting rib plate are respectively connected with the outer wall of the first heat exchange tube and the corresponding first connecting rib plate;
the second connecting rib plate and the first connecting rib plate are of plate-shaped structures, rod-shaped structures or tubular structures;
when the device is operated, raw material gas enters the furnace body from the raw material gas inlet through the gas distributor, is uniformly dispersed by the gas distributor, enters the cavity of the furnace body, enters the catalyst bed layer from the raw material gas channel through the through holes, and carries out conversion reaction in the catalyst bed layer, and the conversion reaction releases heat;
boiler water, namely cooling water enters the cooling water ring pipe from a cooling water pipeline and then uniformly enters each first heat exchange pipe, the cooling water flows from bottom to top and exchanges heat with the reaction heat of the catalyst bed layer, and then sequentially enters the inner cavity of the pipe cap and each second heat exchange pipe to continuously exchange heat with the reaction heat of the catalyst bed layer to heat steam; the generated steam enters a steam collecting ring pipe and is sent out of the room from a steam conveying pipeline;
after the raw material gas reacts in the catalyst bed layer, heat is generated, and reaction heat of the catalyst bed layer is taken away, so that the temperature of the catalyst bed layer is kept constant at the catalyst activity temperature; the synthesis gas generated by the reaction enters the shift gas collecting pipe from each gas inlet hole and is sent out through the synthesis gas pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811160882.2A CN109052318B (en) | 2018-09-30 | 2018-09-30 | Isothermal shift reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811160882.2A CN109052318B (en) | 2018-09-30 | 2018-09-30 | Isothermal shift reactor |
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| Publication Number | Publication Date |
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| CN109052318A CN109052318A (en) | 2018-12-21 |
| CN109052318B true CN109052318B (en) | 2022-04-08 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201811160882.2A Active CN109052318B (en) | 2018-09-30 | 2018-09-30 | Isothermal shift reactor |
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Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110898768A (en) * | 2019-10-24 | 2020-03-24 | 中石化宁波工程有限公司 | Double-isothermal-system conversion furnace |
| CN110876913A (en) * | 2019-11-05 | 2020-03-13 | 中国石油化工股份有限公司 | Radial bed isothermal transformation reaction device |
Citations (7)
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| US4732918A (en) * | 1984-04-18 | 1988-03-22 | Linde Aktiengesellschaft | Heat interchanging process and reactor therefor |
| CN104368279A (en) * | 2014-11-18 | 2015-02-25 | 安徽新月化工设备有限公司 | Radial constant-temperature reactor by using water to transfer heat |
| CN104399413A (en) * | 2014-11-18 | 2015-03-11 | 安徽新月化工设备有限公司 | Controllable heat-removing reactor |
| CN104645897A (en) * | 2015-02-11 | 2015-05-27 | 南京敦先化工科技有限公司 | Dual-seal-head controllable water heat removing reactor |
| CN106861590A (en) * | 2017-02-20 | 2017-06-20 | 北京石油化工工程有限公司 | Aromatic hydrocarbons conversion reactor |
| CN206508988U (en) * | 2017-02-20 | 2017-09-22 | 北京石油化工工程有限公司 | Aromatic hydrocarbons conversion reactor |
| CN108325476A (en) * | 2018-02-08 | 2018-07-27 | 湖南安淳高新技术有限公司 | A kind of suspension type U-shaped vapour pipe isothermal reactor and reaction method |
-
2018
- 2018-09-30 CN CN201811160882.2A patent/CN109052318B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4732918A (en) * | 1984-04-18 | 1988-03-22 | Linde Aktiengesellschaft | Heat interchanging process and reactor therefor |
| CN104368279A (en) * | 2014-11-18 | 2015-02-25 | 安徽新月化工设备有限公司 | Radial constant-temperature reactor by using water to transfer heat |
| CN104399413A (en) * | 2014-11-18 | 2015-03-11 | 安徽新月化工设备有限公司 | Controllable heat-removing reactor |
| CN104645897A (en) * | 2015-02-11 | 2015-05-27 | 南京敦先化工科技有限公司 | Dual-seal-head controllable water heat removing reactor |
| CN106861590A (en) * | 2017-02-20 | 2017-06-20 | 北京石油化工工程有限公司 | Aromatic hydrocarbons conversion reactor |
| CN206508988U (en) * | 2017-02-20 | 2017-09-22 | 北京石油化工工程有限公司 | Aromatic hydrocarbons conversion reactor |
| CN108325476A (en) * | 2018-02-08 | 2018-07-27 | 湖南安淳高新技术有限公司 | A kind of suspension type U-shaped vapour pipe isothermal reactor and reaction method |
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