CN204564099U - Gas synthesis reaction unit - Google Patents
Gas synthesis reaction unit Download PDFInfo
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- CN204564099U CN204564099U CN201520167470.7U CN201520167470U CN204564099U CN 204564099 U CN204564099 U CN 204564099U CN 201520167470 U CN201520167470 U CN 201520167470U CN 204564099 U CN204564099 U CN 204564099U
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Abstract
The utility model discloses a kind of gas synthesis reaction unit, solve that the volume that existing gas synthesis reaction unit exists is large, distribution of gas with contact inequality, the problem that reaction efficiency is low, reactant yield is low.Technical scheme comprises housing, described case top is provided with air inlet, bottom is provided with gas outlet, beds is filled with in described housing, described beds periphery perforate also and between housing has gap, and be evenly distributed with cooling water pipe in beds, the vertical center line of described beds is provided with the discharge pipe of upper end closed, lower ending opening, the tube wall of described discharge pipe evenly has multiple open interior be communicated with beds, the lower end of discharge pipe is communicated with gas outlet.The utility model structure is simple, volume is little, side reaction is few, distribution of gas is even, and reaction efficiency is high, reactant yield and selective good.
Description
Technical field
The utility model relates to the gas synthesis reaction unit of chemical industry.
Background technology
Oxalic acid and oxalate are important Organic Chemicals, and one of its synthetic method is: CO reacts oxalic dimethyl ester and NO with methyl nitrite under catalyst action, and be called coupling reaction, reaction equation is as follows:
Above-mentioned reaction is carried out usually in gas synthesis reaction unit, CO gas phase is coupling synthesizing dimethyl oxalate in the presence of a catalyst, in current gas synthesis reaction unit, unstripped gas walks tube side usually, cooling medium walks shell side, because Catalyst packing is in reaction tube, because reasons in structure admission space is little, then reactor diameter is larger will to reach identical production capacity compared with fixed bed reactors, so just there is gas contact and be uniformly distributed reaction poor, the problem that reaction unit is bulky.Major diameter dimethyl oxalate reactor manufactures difficulty simultaneously, Catalyst packing difficulty is large, easily side reaction is produced in course of reaction, this is very large on the yield of dimethyl oxalate and selective impact, how to optimize its structure of reactor to improve the research emphasis becoming synthesis reactor in DMO synthesis technique of reactor maximization yield and solution Catalyst packing problem.
Summary of the invention
The object of the invention is to solve the problems of the technologies described above, providing that a kind of structure is simple, volume is little, side reaction is few, distribution of gas is even, reaction efficiency is high, reactant yield and selective good gas synthesis reaction unit.
Technical scheme comprises housing, described case top is provided with air inlet, bottom is provided with gas outlet, beds is filled with in described housing, described beds periphery perforate also and between housing has gap, and be evenly distributed with cooling water pipe in beds, the vertical center line of described beds is provided with the discharge pipe of upper end closed, lower ending opening, the tube wall of described discharge pipe evenly has multiple open interior be communicated with beds, the lower end of discharge pipe is communicated with gas outlet.
Described air inlet is connected with gas distributor, and described gas distributor is cylindrical pipeline, and its upper end communicates with air inlet, lower end closed, and the tube wall of described gas distributor evenly has multiple STH.
The ratio of described gap width and beds diameter is 1:10-15.
The ratio of described beds diameter and discharge pipe diameter is 5-8:1.
The pipe diameter of described gas distributor and the ratio 0.8-1 of air inlet diameter, the height of gas distributor and the ratio of diameter of the housing are 0.3-0.45.
The height of described STH and the ratio of gas distributor height are 0.5-0.9, and the width of STH is 30-50mm.
The spacing of adjacent two described STHs is equal with the width of STH.
Described cooling water pipe is coil pipe or around pipe, the import of described cooling water pipe and the outlet of drum, the outlet of cooling water pipe and the inlet communication of drum.
Beneficial effect:
1, the utility model Raw makes shell side leave with rage, namely Catalyst packing is in shell side part, cooling water walks tube side, cooling water pipe is with coil form or be evenly distributed in beds around form of tubes, be conducive to the control of homogeneous reaction temperature, this improvement decreases reaction volume, and under identical production capacity, the reaction volume of fixed bed reactors is less;
2, unstripped gas diffuses into beds by the perforate of beds outer peripheral face and top, ensure that the concentration of unstripped gas reaches unanimity in bed, be beneficial to the generation of reaction, reacted gas is radial through beds, resistance drop is less and shifted out fast by discharge pipe after reaction, is beneficial to gas transport and improves the conversion ratio of unstripped gas.
3, at air inlet, place is provided with gas distributor, adopt the cylindrical duct form of STH, structure is simple, can well meet the needs of beds side air inlet, unstripped gas speed after gas distributor distribution reaches unanimity and evenly enters the gap of beds and housing and catalyst top is spread and reacts.
4. the utility model structure simple, control easy, volume is little, side reaction is few, distribution of gas is even, reaction efficiency is high, reactant yield and selective good, is applicable to multiple gases reaction process.
Accompanying drawing explanation
Fig. 1 is the utility model structural representation.
Fig. 2 is the sectional view of the utility model beds.
Wherein, 1-housing, 1.1-air inlet, 1.2-gas outlet, 2-gas distributor, 2.1-STH, 3-beds, 3.1-hole, 4-cooling water pipe, 5-drum, 6-gap, 7-discharge pipe, 7.1-open interior.
Detailed description of the invention
Below in conjunction with accompanying drawing, explanation is further explained to the utility model:
With reference to Fig. 1, described housing 1 top is provided with air inlet 1.1, and bottom is provided with gas outlet 1.2, is filled with beds 3 in described housing 1, described beds 3 periphery perforate 3.1 also and between housing has gap 6, and the width in described gap 6 and the ratio of beds diameter are 1:10-15; Cooling water pipe 4 is evenly distributed with in beds 3, the vertical center line of described beds 3 is provided with the discharge pipe 7 of upper end closed, lower ending opening, the ratio of described beds 3 diameter and discharge pipe 7 diameter is 5-8:1, the tube wall of described discharge pipe 7 evenly has multiple open interior 7.1 be communicated with beds 3, the lower end of discharge pipe 7 is communicated with gas outlet 1.2.Described air inlet 1.1 is connected with gas distributor 2, described gas distributor 2 is cylindrical pipeline, the ratio 0.8-1 of its diameter and air inlet 1.1 diameter, the ratio of height and housing 1 diameter is 0.3-0.45, its upper end communicates with air inlet 1.1, lower end closed, the tube wall of described gas distributor 2 evenly has multiple STH 2.1, the ratio of the height of described STH 2.1 and gas distributor 2 height is 0.5-0.9, the width of STH is 30-50mm, and preferably the spacing of adjacent two described STHs is equal with the width of STH 2.1.
For the building-up process of dimethyl oxalate in gas synthesis reactor.
Unstripped gas: mole consist of CO 20%, methyl nitrite 10%, NO 5%, O
2<2000ppm, H
2<200ppm, all the other are N
2, hereinafter referred to as unstripped gas.
Unstripped gas enters gas distributor 2 by the air inlet 1.1 at housing 1 top, enter in housing by STH 2.1 side direction of gas distributor 2, the advantage that this mode to beds 3 side air inlet has gas and vapor permeation and is evenly distributed, unstripped gas part is directly axially entered by beds end face, part enters in beds 3 by hole 3.1 radial direction of gap 6 on beds 3, CO under the effect of catalyst in unstripped gas and methyl nitrite reaction oxalic dimethyl ester, it is 100-150 DEG C that the continuous heat exchange of the cooling water pipe detoured in beds 3 controls reaction temperature, ensure normally carrying out of reaction, reacted gas enters discharge gas 7 through beds 3 by open interior 7.1 collection, and housing is discharged in gas outlet 1.2 the most finally.The reaction heat that cooling water in cooling water pipe absorbs reclaims byproduct steam by drum 5.
After the reaction of discharging gas mole consist of CO 11.5%, methyl nitrite 1.1%, NO14.7%, dimethyl oxalate 4.7%, all the other are N
2.
Adopt the utility model device, the volume of gas synthesis reaction unit can reduce 20%, and the once through yield of reactant dimethyl oxalate is 90%, improves about 10%.
Claims (8)
1. a gas synthesis reaction unit, comprise housing, described case top is provided with air inlet, bottom is provided with gas outlet, it is characterized in that, beds is filled with in described housing, described beds periphery perforate also and between housing has gap, cooling water pipe is evenly distributed with in beds, the vertical center line of described beds is provided with the discharge pipe of upper end closed, lower ending opening, the tube wall of described discharge pipe evenly has multiple open interior be communicated with beds, the lower end of discharge pipe is communicated with gas outlet.
2. gas synthesis reaction unit as claimed in claim 1, it is characterized in that, described air inlet is connected with gas distributor, described gas distributor is cylindrical pipeline, its upper end communicates with air inlet, lower end closed, and the tube wall of described gas distributor evenly has multiple STH.
3. gas synthesis reaction unit as claimed in claim 1, it is characterized in that, the ratio of described gap width and beds diameter is 1:10-15.
4. the gas synthesis reaction unit as described in claim 1 or 3, is characterized in that, the ratio of described beds diameter and discharge pipe diameter is 5-8:1.
5. gas synthesis reaction unit as claimed in claim 2, it is characterized in that, the pipe diameter of described gas distributor and the ratio 0.8-1 of air inlet diameter, the height of gas distributor and the ratio of diameter of the housing are 0.3-0.45.
6. the gas synthesis reaction unit as described in claim 2 or 5, is characterized in that, the height of described STH and the ratio of gas distributor height are 0.5-0.9, and the width of STH is 30-50mm.
7. gas synthesis reaction unit as claimed in claim 6, it is characterized in that, the spacing of adjacent two described STHs is equal with the width of STH.
8. gas synthesis reaction unit as claimed in claim 1, is characterized in that, described cooling water pipe is coil pipe or around pipe, the import of described cooling water pipe and the outlet of drum, the outlet of cooling water pipe and the inlet communication of drum.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520167470.7U CN204564099U (en) | 2015-03-24 | 2015-03-24 | Gas synthesis reaction unit |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520167470.7U CN204564099U (en) | 2015-03-24 | 2015-03-24 | Gas synthesis reaction unit |
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| Publication Number | Publication Date |
|---|---|
| CN204564099U true CN204564099U (en) | 2015-08-19 |
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| CN201520167470.7U Active CN204564099U (en) | 2015-03-24 | 2015-03-24 | Gas synthesis reaction unit |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114247386A (en) * | 2021-11-24 | 2022-03-29 | 中国五环工程有限公司 | Evaporative isothermal hydrogenation reaction method and evaporative isothermal reaction system |
-
2015
- 2015-03-24 CN CN201520167470.7U patent/CN204564099U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114247386A (en) * | 2021-11-24 | 2022-03-29 | 中国五环工程有限公司 | Evaporative isothermal hydrogenation reaction method and evaporative isothermal reaction system |
| CN114247386B (en) * | 2021-11-24 | 2023-10-13 | 中国五环工程有限公司 | Evaporation type isothermal hydrogenation reaction method and evaporation type isothermal reaction system |
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| GR01 | Patent grant |