CN202752010U - Gas phase hydrogenation reactor - Google Patents
Gas phase hydrogenation reactor Download PDFInfo
- Publication number
- CN202752010U CN202752010U CN 201220326015 CN201220326015U CN202752010U CN 202752010 U CN202752010 U CN 202752010U CN 201220326015 CN201220326015 CN 201220326015 CN 201220326015 U CN201220326015 U CN 201220326015U CN 202752010 U CN202752010 U CN 202752010U
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Abstract
The utility model discloses a gas phase hydrogenation reactor which comprises a gas-cooled reactor and a water-cooled reactor, wherein the gas-cooled reactor is composed of a shell body and a heat exchange tube arranged in the shell body, and the water-cooled reactor is composed of a shell body and a reaction tube arranged in the shell body. A tube pass outlet of the gas-cooled reactor is connected with a tube pass inlet of the water-cooled reactor through a pipeline. A tube pass outlet of the water-cooled reactor is connected with a tube pass inlet of the gas-cooled reactor through a pipeline. A shell pass of the gas-cooled reactor is provided with catalytic agents. A tube pass of the water-cooled reactor is provided with catalytic agents. According to the gas phase hydrogenation reactor, a shell and tube reactor is changed into two independent reactors, namely the gas-cooled reactor and the water-cooled reactor. The gas-cooled reactor preheats fresh reaction gases and meanwhile takes away reaction heat; and the water-cooled reactor achieves most reactions, produces by-product steam and improves heat energy utilization.
Description
Technical field
The utility model relates to a kind of gas phase hydrogenation reaction device.
Background technology
Present domestic gas phase hydrogenation reaction is produced in the technique of ethylene glycol such as: Hydrogenation of Dimethyl Oxalate, adopt shell and tube reactor, reactor size is large, and specification is φ 3700X7000(heat exchanger tube length), and the filler packing factor is little, cause reaction efficiency low, because reaction is exothermic reaction, can produce a large amount of reaction heat in course of reaction simultaneously, this reaction heat is generally taken away by the steam of reactor shell side, and reclaim by the heat exchanger of outside, cause utilization of Heat of Reaction efficient lower.Production capacity is 50,000 ton/years of glycol units at present, its hydrogenation reaction workshop section needs reactor and the heat exchanger parallel operation of 2 above-mentioned sizes, as production capacity being increased to 200,000 ton/years, then need 6 reactor, heat exchangers that cover is similar, be similar to a little group of planes, bring very large difficulty, and be unfavorable for saving energy and reduce the cost 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, can be used for Hydrogenation of Dimethyl Oxalate and produces in the production technology of ethylene glycol etc.
A kind of gas phase hydrogenation reaction device provided by the invention comprises:
The air cooling reactor is made of housing and the heat exchanger tube that is arranged in the housing;
Water-cooled reactor is made of housing and the reaction tube that is arranged in the housing;
Wherein, the outlet of the tube side of air cooling reactor is connected with the tube side import of water-cooled reactor by pipeline; The tube side outlet of water-cooled reactor is connected by the import of pipeline with the shell side of air cooling reactor;
The shell side of air cooling reactor is provided with catalyst; The tube side of water-cooled reactor is provided with catalyst.
As optimal technical scheme, the gas phase hydrogenation reaction device also comprises gas preheater, is connected by the import of pipeline with air cooling reactor tube side.
As optimal technical scheme, the gas phase hydrogenation reaction device also comprises the low-temperature receiver feedway, is connected by the import of pipeline with the water-cooled reactor shell side.
As optimal technical scheme, the low-temperature receiver feedway is apparatus for supplying cool water.
As optimal technical scheme, the heat exchanger tube of air cooling reactor is radial bimetallic rib heat exchanging pipe.
As optimal technical scheme, the housing of air cooling reactor is made of body and the lid that covers on body, and lid and body are fixed by fixture.
As optimal technical scheme, the housing of water-cooled reactor is made of body and the lid that covers on body, and lid and body are fixed by fixture.
The utility model can reach following effect:
1, changes a shell and tube reactor into two independently reactors, air cooling reactor and water-cooled reactor.Air cooling reactor preheating fresh reactant gas is taken away reaction heat simultaneously; Water-cooled reactor realizes most of reaction, and byproduct steam, improves heat energy utilization.
2, the air cooling reactor adopts the Novel efficient heat exchange tube core, and the heat exchange tube core adopts the bimetallic rib heat exchanging pipe of arranging radially, and this heat exchanger tube can be taken away reaction heat fast.
3, the air cooling reactor is that heat exchanger tube loads catalyst outward, and the catalyst filling amount is large, and most reaction is finished in water-cooled reactor.
4, the structure of air cooling reactor and water-cooled reactor is that internals (heat exchanger tube) and housing are separable, and internals can separately be made installation, manufacturing, simple installation.
Description of drawings
Fig. 1 is gas phase hydrogenation reaction device schematic diagram of the present utility model.
1, water-cooled reactor; 11, housing; 111, import; 112, outlet; 113, body; 114, lid; 115, fixture; 12, reaction tube; 121, import; 122, outlet; 2, air cooling reactor; 21, housing; 211, import; 212, outlet; 213, body; 214, lid; 215, fixture; 22, heat exchanger tube; 221, import; 222, outlet; 3, gas preheater; 4, low-temperature receiver feedway.
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.
Gas phase hydrogenation reaction device of the present utility model comprises:
Water-cooled reactor 1 is made of housing 11 and the reaction tube 12 that is arranged in the housing;
Wherein, the outlet 222 of air cooling reactor tube side (heat exchanger tube 22) is connected by the import 121 of pipeline with water-cooled reactor tube side (reaction tube 12); The outlet 122 of water-cooled reactor tube side is connected by the import 211 of pipeline with air cooling reactor shell side.
Wherein, (tube side) is provided with the catalyst (not shown) in the reaction tube 12 of water-cooled reactor.
(shell side) is provided with catalyst 23 in the air cooling reactor shell 21, outside the heat exchanger tube 22.
The gas phase hydrogenation reaction device also comprises gas preheater 3, is connected by the import 221 of pipeline with air cooling reactor tube side.
Wherein, the gas phase hydrogenation reaction device also comprises low-temperature receiver feedway 4, is connected with the import 111 of water-cooled reactor shell side by pipeline.Low-temperature receiver feedway 4 is chosen as apparatus for supplying cool water.
The heat exchanger tube 22 of air cooling reactor is preferably bimetallic rib heat exchanging pipe radially.
Water-cooled reactor housing 11 is made of body 113 and the lid 114 that covers on body 113, and lid 114 and body 113 are fixing by fixture 115, and wherein fixture 115 can be screw.Because housing 11 is opening and closing type, then reaction tube 12 can be separated by housing 11 interior dismountings easily.
Air cooling reactor shell 21 is made of body 213 and the lid 214 that covers on body 213, and lid 214 and body 213 are fixing by fixture 215, and wherein fixture 215 can be screw.Because housing 21 is opening and closing type, then heat exchanger tube 22 can be separated by housing 21 interior dismountings easily.
Come the utility model is described as an example of the reaction of preparation of ethanediol by dimethyl oxalate hydrogenation example:
The fresh reactant gas that dimethyl oxalate and hydrogen mix enters heat exchanger tube 22 by the import 221 of air cooling reactor 2 tube sides, in heat exchanger tube 22 (have outside the heat exchanger tube unreacted of coming from water-cooled reactor 1 completely reaction gas under the effect of catalyst, continue reaction, and emit heat) after preheating, flow out from the outlet 222 of heat exchanger tube 22, then the import 121 by water-cooled reactor 1 tube side enters reaction tube 12.Be provided with catalyst in the reaction tube 12, gas under the catalysis of catalyst in reaction tube 12 interior generation hydrogenation reactions, simultaneously outside reaction tube 12, pass into cooling water to take away hydrogenation reaction heat, but byproduct steam after the outer cooling waters of reaction tube 12 are heated discharges waste heat boiler by the outlet 112 of water-cooled reactor shell side.Because, hydrogenation reaction is difficult to fully in the reaction tube 12, outlet 122 effluent airs of reaction tube 12, enter in the shell side of air cooling reactor 2 by the 2 shell side imports 211 of air cooling reactor, owing to being provided with equally hydrogenation catalyst 23 in its shell side, completely gas continuation of unreacted reaction under the catalysis of hydrogenation catalyst, and the fresh reactant gas that constantly passes through in heat exchanger tube 22 tube sides of air cooling reactor 2 is taken away the reaction heat of shell side, ethylene glycol was discharged by the outlet 212 of air cooling reactor 2 shell sides after reaction was finished, and collected.
Wherein, the most initial what react, fresh reactant gas is by the tube side that enters air cooling reactor 2 after gas preheater 3 preheatings.
To sum up, water-cooled reactor 1 of the present utility model adopts the mode of by-product middle pressure steam to shift out reaction heat, and the reaction heat of air cooling reactor 2 then by shifting out with the fresh synthesis gas countercurrent heat exchange method, is realized the heat coupling.In air cooling reactor 2, catalyst countercurrent flow in the virgin gas in the heat exchanger tube 22 of flowing through and the shell side, the tube side to water-cooled reactor 1 after the heating carries out hydrogenation reaction, enters the shell side internal reaction of air cooling reactor 2 again.
The reactor that the utility model provides adopts two settings in flow process: air cooling reactor and water-cooled reactor.Air cooling reactor preheating fresh reactant gas is taken away reaction heat simultaneously; Water-cooled reactor realizes most of reaction, and byproduct steam.
Change into and the separable independent part of housing in the internals (heat exchange tube core) of configuration aspects with water-cooled reactor, internals can separately be made installation, are easy to realize maximizing, and dismountable structure is made on top simultaneously, more is convenient to the filling work of catalyst.
In the design of parts, the preferred new type high efficient heat exchanger that adopts in the air cooling reactor, i.e. the bimetallic rib heat exchanging pipe of radial arrangement can be taken away reaction heat fast.
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 (7)
1. a gas phase hydrogenation reaction device is characterized in that, comprising:
The air cooling reactor is made of housing and the heat exchanger tube that is arranged in the described housing;
Water-cooled reactor is made of housing and the reaction tube that is arranged in the described housing;
Wherein, the outlet of the tube side of described air cooling reactor is connected with the tube side import of water-cooled reactor by pipeline; The tube side outlet of described water-cooled reactor is connected by the import of pipeline with the shell side of described air cooling reactor;
The shell side of described air cooling reactor is provided with catalyst; The tube side of described water-cooled reactor is provided with catalyst.
2. gas phase hydrogenation reaction device according to claim 1 is characterized in that, described gas phase hydrogenation reaction device also comprises gas preheater, is connected by the import of pipeline with described air cooling reactor tube side.
3. gas phase hydrogenation reaction device according to claim 1 is characterized in that, described gas phase hydrogenation reaction device also comprises the low-temperature receiver feedway, is connected by the import of pipeline with described water-cooled reactor shell side.
4. gas phase hydrogenation reaction device according to claim 3 is characterized in that, described low-temperature receiver feedway is apparatus for supplying cool water.
5. gas phase hydrogenation reaction device according to claim 1 is characterized in that, the heat exchanger tube of described air cooling reactor is radial bimetallic rib heat exchanging pipe.
6. gas phase hydrogenation reaction device according to claim 1 is characterized in that, the housing of described air cooling reactor is made of body and the lid that covers on described body, and described lid and described body are fixed by fixture.
7. gas phase hydrogenation reaction device according to claim 1 is characterized in that, the housing of described water-cooled reactor is made of body and the lid that covers on described body, and described lid and described body are fixed by fixture.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220326015 CN202752010U (en) | 2012-07-06 | 2012-07-06 | Gas phase hydrogenation reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220326015 CN202752010U (en) | 2012-07-06 | 2012-07-06 | Gas phase hydrogenation reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202752010U true CN202752010U (en) | 2013-02-27 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220326015 Expired - Lifetime CN202752010U (en) | 2012-07-06 | 2012-07-06 | Gas phase hydrogenation reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202752010U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105218310A (en) * | 2015-10-23 | 2016-01-06 | 湖南安淳高新技术有限公司 | Methanol-fueled CLC reactive system and methanol-fueled CLC reaction method |
| CN105233762A (en) * | 2015-10-23 | 2016-01-13 | 湖南安淳高新技术有限公司 | Methanol synthesis reaction system and method |
-
2012
- 2012-07-06 CN CN 201220326015 patent/CN202752010U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105218310A (en) * | 2015-10-23 | 2016-01-06 | 湖南安淳高新技术有限公司 | Methanol-fueled CLC reactive system and methanol-fueled CLC reaction method |
| CN105233762A (en) * | 2015-10-23 | 2016-01-13 | 湖南安淳高新技术有限公司 | Methanol synthesis reaction system and method |
| CN105218310B (en) * | 2015-10-23 | 2017-06-13 | 湖南安淳高新技术有限公司 | Methanol synthesis reaction device and methanol synthesis reaction method |
| CN105233762B (en) * | 2015-10-23 | 2018-06-26 | 湖南安淳高新技术有限公司 | Methanol synthesis reaction system and methanol synthesis reaction method |
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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 | ||
| CX01 | Expiry of patent term |
Granted publication date: 20130227 |