CN202752008U - Gas phase hydrogenation reactor - Google Patents
Gas phase hydrogenation reactor Download PDFInfo
- Publication number
- CN202752008U CN202752008U CN 201220325746 CN201220325746U CN202752008U CN 202752008 U CN202752008 U CN 202752008U CN 201220325746 CN201220325746 CN 201220325746 CN 201220325746 U CN201220325746 U CN 201220325746U CN 202752008 U CN202752008 U CN 202752008U
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- phase hydrogenation
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- gas phase
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Abstract
The utility model discloses a gas phase hydrogenation reactor which comprises a shell. An upper tube plate, a first lower tube plate and a second lower tube plate are arranged in the shell from top to bottom and divide the inside of the shell into a feed gas recirculation zone, a reaction zone, a reaction gas out-flowing zone and a feed gas feeding zone. A cold source inlet and a cold source outlet are arranged in the position, corresponding to the reaction zone, of the shell, a reaction gas outlet is arranged in the position, corresponding to the reaction gas out-flowing zone, of the shell, and a feed gas inlet is arranged in the position, corresponding to the feed gas feeding zone, of the shell. The gas phase hydrogenation reactor further comprises a heat exchanging pipe which is composed of an inner pipe and a outer pipe sleeved outside the inner pipe, the inner pipe is longer than the outer pipe, catalytic agents are filled between the inner pipe and the outer pipe, the heat exchanging pipe is arranged in the shell, the upper end openings of the inner pipe and the outer pipe are communicated with the feed gas recirculation zone, the lower end opening of the outer pipe is communicated with the reaction gas out-flowing zone, and the lower end opening of the inner pipe is communicated with the feed gas feeding zone. The recycle ratio of the gas phase hydrogenation reactor is low, and under the condition that the quantity of the catalytic agents is fixed, high conversion per pass can be obtained.
Description
Technical field
The utility model relates to a kind of gas phase hydrogenation reaction device.
Background technology
Present domestic ethylene glycol adopts shell and tube reactor in producing in the hydrogenation reaction, reactor size is large, and the filler packing factor is little, causes reaction efficiency low.Production capacity is 50,000 ton/years of glycol units at present, its hydrogenation reaction workshop section needs the reactor parallel operation of 2 above-mentioned sizes, as production capacity being increased to 200,000 ton/years, then needs 6 similar reactors, be similar to a little group of planes, bring very large difficulty to device operation, operation, maintenance.
The utility model content
In order to solve the problems of the technologies described above, the utility model provides a kind of gas phase hydrogenation reaction device, comprising:
Housing, be provided with upper perforated plate, the first lower perforated plate and the second lower perforated plate in the housing from top to bottom and enter the district with being divided into unstripped gas recirculating zone, reaction zone, reaction gas outflow district and unstripped gas in the housing, the position of corresponding reaction zone is provided with low-temperature receiver import and low-temperature receiver outlet on the housing, the position that corresponding reaction gas flows out the district on the housing is provided with the reaction gas outlet, and the position that corresponding raw material enters the district on the housing is provided with the unstripped gas entrance;
Heat exchanger tube, the outer tube outer with being sheathed on inner tube by inner tube consists of, the length of inner tube is greater than the length of outer tube, be filled with catalyst between the inner and outer tubes, heat exchanger tube is located in the housing, wherein the upper port of inner and outer tubes is communicated with the unstripped gas recirculating zone, and the lower port of outer tube flows out the district with reaction gas and is communicated with, and the lower port of inner tube enters the district with unstripped gas and is communicated with.
As optimal technical scheme, the upper port of outer tube is fixed in upper perforated plate with welding manner, and the lower port of outer tube is fixed in the first lower perforated plate with welding manner.
As optimal technical scheme, the lower port of inner tube is fixed in the second lower perforated plate with thread connecting mode.
As optimal technical scheme, the position in corresponding reaction gas outflow district also is provided with the catalyst discharge port on the housing.
As optimal technical scheme, heat exchanger tube is a plurality of, evenly is arranged in the housing.
As optimal technical scheme, reaction gas flows out the district and is filled with filler.
As optimal technical scheme, also be provided with the temperature measurer for assaying reaction district temperature in the housing.
As optimal technical scheme, the low-temperature receiver import is cooling water inlet, and the low-temperature receiver outlet is steam (vapor) outlet.
As optimal technical scheme, the low-temperature receiver outlet is positioned at low-temperature receiver entrance top.
The utility model can reach following technique effect:
1, gas phase hydrogenation reaction device recycle ratio of the present utility model is low, in the certain situation of catalyst, can obtain higher conversion per pass.
2, synthesis gas is equivalent to a preheater and comes the preheating inlet gas, and fresh synthesis gas is preheating in reactor, thereby can save heat exchanger, saves cost.
3, energy reclaims, but byproduct steam.
4, uniformity of temperature profile can obtain suitable iptimum speed of reacting, and technology stability is good.
Description of drawings
Fig. 1 is the schematic diagram of gas phase hydrogenation reaction device of the present utility model.
Fig. 2 is local enlarged diagram of the present utility model.
1, housing; 11, unstripped gas recirculating zone; 12, reaction zone; 13, reaction gas flows out the district; 14, unstripped gas enters the district; 121, low-temperature receiver import; 122, low-temperature receiver outlet; 131, reaction gas outlet; 132, catalyst discharge port; 141, unstripped gas entrance; 2, heat exchanger tube; 21, inner tube; 22, outer tube; 23, catalyst; 211, upper port; 221, upper port; 212, lower port; 222, lower port; 31, upper perforated plate; 32, the first lower perforated plate; 33, the second lower perforated plate; 4, temperature measurer.
The specific embodiment
The utility model is described in further detail below in conjunction with the drawings and specific embodiments, so that those skilled in the art can better understand the utility model and being implemented, but illustrated embodiment is not as to restriction of the present utility model.
In conjunction with illustrated in figures 1 and 2,
Gas phase hydrogenation reaction device of the present utility model comprises:
Housing 1, be provided with upper perforated plate 31, the first lower perforated plate 32 and the second lower perforated plate 33 in the housing 1 from top to bottom and enter district 14 with being divided into unstripped gas recirculating zone 11, reaction zone 12, reaction gas outflow district 13 and unstripped gas in the housing, the position of corresponding reaction zone 12 is provided with low-temperature receiver import 121 and low-temperature receiver outlet 122 on the housing 1, the position that corresponding reaction gas flows out district 13 on the housing 1 is provided with reaction gas outlet 131, and the position that corresponding raw material enters district 14 on the housing 1 is provided with unstripped gas entrance 141;
The position in corresponding reaction gas outflow district 13 also is provided with catalyst discharge port 132 on the housing 1.
Also be provided with the temperature measurer 4 for assaying reaction district 12 temperature in the housing 1.
Low-temperature receiver import 121 is cooling water inlet, and low-temperature receiver outlet 122 is steam (vapor) outlet.Low-temperature receiver entrance 121 tops preferably are located in low-temperature receiver outlet 122.
Preferably, the upper port 221 of outer tube 22 is fixed in upper perforated plate 31 with welding manner, and the lower port 222 of outer tube 22 is fixed in the first lower perforated plate 32 with welding manner.The lower port 212 of inner tube 21 is fixed in the second lower perforated plate 33 with the thread connecting mode (not shown).
The utility model is three tube sheets, double-tube structure.Heat exchanger tube outer tube 22 adopts the connected mode of welding with upper lower perforated plate, and inner tube 21 and the second lower perforated plate 33 adopt thread connecting modes.Catalyst 23 is contained between inner tube 21 and the outer tube 23, unstripped gas enters reactor by lower feed gas entrance 141, the reacting gas that process inner tube 21 and outer tube are 22 carries out heat exchange, the unstripped gas of preheating is taken away partial reaction heat, unstripped gas after the preheating is through inner tube 21, enter into unstripped gas recirculating zone 11, enter again between the inner and outer pipes annular space fully to contact with catalyst 23 and react, the reaction gas that enters at last between the first lower perforated plate and the second lower perforated plate flows out district 13, discharges reactor by reaction gas outlet 131.Boiling water then circulates between shell, and the cooling reaction gas is taken away reaction heat, simultaneously by the gas cooled of the inside, then brings drum into by shell side hot water and produces steam.The air-flow that flows along inner and outer tubes is opposite, and the inlet temperature that synthesis gas enters catalyst layer is the highest, reducing gradually when outlet is flowed, prevents the generation of overtemperature and temperature runaway phenomenon.Make like this operating temperature more near the optimum temperature line, such Temperature Distribution can guarantee best reaction speed, namely can obtain high conversion ratio in the situation that reduces catalyst amount.Such reactor has unique catalyst cooling system.
Come the utility model is described as an example of the reaction of preparation of ethanediol by dimethyl oxalate hydrogenation example:
The unstripped gas that dimethyl oxalate and hydrogen mix enters unstripped gas from unstripped gas entrance 141 and enters district 14.Unstripped gas enters district 14 and is communicated with the lower port 212 of heat exchanger tube inner tube, and unstripped gas enters unstripped gas recirculating zone 11 after entering the reaction heat preheating of inner tube 21 by the hydrogenation reaction generation of outer tube 22 generations.The upper port 221 of outer tube 22 is communicated with raw material recirculating zone 11, unstripped gas refluxes and enters between inner tube 21 and outer tube 22 annular spaces, hydrogenation reaction occurs under the catalysis of catalyst 23, exothermic reaction heat is taken away (cooling water is discharged from steam (vapor) outlet after being heated to be steam, and is recycling) by the unstripped gas in the inner tube 21 and the outer tube 22 outer cooling waters that pass into.After the hydrogenation reaction, reaction gas flows into reaction gas outflow district 13 from the lower port 222 of outer tube 22, and flows out from reaction gas outlet 131.
The above embodiment is the preferred embodiment that proves absolutely that the utility model is lifted, and protection domain of the present utility model is not limited to this.Being equal to that those skilled in the art do on the utility model basis substitutes or conversion, all within protection domain of the present utility model.Protection domain of the present utility model is as the criterion with claims.
Claims (9)
1. a gas phase hydrogenation reaction device is characterized in that, comprising:
Housing, be provided with upper perforated plate, the first lower perforated plate and the second lower perforated plate in the described housing from top to bottom and enter the district with being divided into unstripped gas recirculating zone, reaction zone, reaction gas outflow district and unstripped gas in the described housing, the position of corresponding described reaction zone is provided with low-temperature receiver import and low-temperature receiver outlet on the described housing, the position that corresponding described reaction gas flows out the district on the described housing is provided with the reaction gas outlet, and the position that corresponding described raw material enters the district on the described housing is provided with the unstripped gas entrance;
Heat exchanger tube, the outer tube outer with being sheathed on inner tube by inner tube consists of, the length of described inner tube is greater than the length of outer tube, be filled with catalyst between the described inner and outer tubes, described heat exchanger tube is located in the described housing, the upper port of wherein said inner tube and described outer tube is communicated with described unstripped gas recirculating zone, and the lower port of described outer tube flows out the district with described reaction gas and is communicated with, and the lower port of described inner tube enters the district with described unstripped gas and is communicated with.
2. gas phase hydrogenation reaction device according to claim 1 is characterized in that, the upper port of described outer tube is fixed in described upper perforated plate with welding manner, and the lower port of described outer tube is fixed in described the first lower perforated plate with welding manner.
3. gas phase hydrogenation reaction device according to claim 1 is characterized in that, the lower port of described inner tube is fixed in the second lower perforated plate with thread connecting mode.
4. gas phase hydrogenation reaction device according to claim 1 is characterized in that, the position that corresponding described reaction gas flows out the district on the described housing also is provided with the catalyst discharge port.
5. gas phase hydrogenation reaction device according to claim 1 is characterized in that, described heat exchanger tube is a plurality of, evenly is arranged in the described housing.
6. gas phase hydrogenation reaction device according to claim 1 is characterized in that, described reaction gas flows out the district and is filled with filler.
7. gas phase hydrogenation reaction device according to claim 1 is characterized in that, also is provided be used to the temperature measurer of measuring described reaction zone temperature in the described housing.
8. gas phase hydrogenation reaction device according to claim 1 is characterized in that, described low-temperature receiver import is cooling water inlet, and described low-temperature receiver outlet is steam (vapor) outlet.
9. gas phase hydrogenation reaction device according to claim 1 is characterized in that, described low-temperature receiver outlet is positioned at described low-temperature receiver entrance top.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220325746 CN202752008U (en) | 2012-07-06 | 2012-07-06 | Gas phase hydrogenation reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220325746 CN202752008U (en) | 2012-07-06 | 2012-07-06 | Gas phase hydrogenation reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202752008U true CN202752008U (en) | 2013-02-27 |
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ID=47731204
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220325746 Expired - Lifetime CN202752008U (en) | 2012-07-06 | 2012-07-06 | Gas phase hydrogenation reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202752008U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108393044A (en) * | 2018-04-09 | 2018-08-14 | 南京聚拓化工科技有限公司 | The radial methanol reactor of combined type heat exchange and methanol synthesizing process |
| CN109925971A (en) * | 2019-04-23 | 2019-06-25 | 宁波巨化新材料有限公司 | A kind of hydrogenation of propionaldehyde device |
-
2012
- 2012-07-06 CN CN 201220325746 patent/CN202752008U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108393044A (en) * | 2018-04-09 | 2018-08-14 | 南京聚拓化工科技有限公司 | The radial methanol reactor of combined type heat exchange and methanol synthesizing process |
| CN108393044B (en) * | 2018-04-09 | 2023-10-27 | 南京聚拓化工科技有限公司 | Combined heat exchange radial methanol reactor and methanol synthesis process |
| CN109925971A (en) * | 2019-04-23 | 2019-06-25 | 宁波巨化新材料有限公司 | A kind of hydrogenation of propionaldehyde device |
| CN109925971B (en) * | 2019-04-23 | 2021-07-09 | 宁波巨化化工科技有限公司 | Propionaldehyde hydrogenation device |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20130227 |
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| CX01 | Expiry of patent term |