CN214051563U - Methyl acetate hydrogenation reactor and heat exchange system of multistage cold hydrogen feeding - Google Patents
Methyl acetate hydrogenation reactor and heat exchange system of multistage cold hydrogen feeding Download PDFInfo
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- CN214051563U CN214051563U CN202022454439.5U CN202022454439U CN214051563U CN 214051563 U CN214051563 U CN 214051563U CN 202022454439 U CN202022454439 U CN 202022454439U CN 214051563 U CN214051563 U CN 214051563U
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Abstract
The utility model provides a methyl acetate hydrogenation ware and heat transfer system of cold hydrogen feeding of multistage, the methyl acetate hydrogenation ware of the cold hydrogen feeding of multistage includes: a reactor body; the catalyst beds are arranged in the reactor body at intervals along the vertical direction, and an air replenishing space is formed between every two adjacent catalyst beds; and each air supplementing space is communicated with the outlet of at least one cold hydrogen feeding pipe. The utility model has the advantages that a plurality of catalyst bed layers are arranged at intervals along the vertical direction to form a sectional fixed bed reactor, and a cold hydrogen feeding pipe is arranged between two adjacent catalyst bed layers, so that on one hand, the molar ratio of hydrogen to methyl acetate can be improved, and the reaction is promoted to be carried out; on the other hand, the feeding temperature of the next section of bed layer is reduced, so that the activity of each temperature interval of the catalyst is fully utilized, and the purpose of improving the filling volume utilization rate of the catalyst is achieved.
Description
Technical Field
The utility model relates to a coal chemical industry field, concretely relates to methyl acetate hydrogenation ware and heat transfer system of cold hydrogen feeding of multistage.
Background
Ethanol gasoline is being popularized in the prior art, the gap of bioethanol production is large, and coal-based ethanol is developed rapidly. The synthesis gas is subjected to dimethyl ether carbonylation to prepare methyl acetate, and the process route for preparing ethanol by methyl acetate hydrogenation has the advantages of high reaction conversion rate, good selectivity of ethanol generation and no use of noble metal catalyst. Compared with other ethanol production processes, the method can effectively reduce equipment investment and energy consumption.
The catalyst for the methyl acetate hydrogenation reaction has a narrow applicable temperature range, generally 200-240 ℃, and the temperature is increased, so that byproducts are increased, which is not beneficial to the separation process. In the initial industrial demonstration apparatus, a shell-and-tube isothermal reactor for by-product steam was selected for better control of the reaction temperature. With the expansion of the industrial scale of the coal-based ethanol, the disadvantages of the tubular reactor gradually appear: large-scale equipment, high processing and manufacturing difficulty, low utilization rate of the filling volume of the catalyst and high equipment investment. Taking 50 ten thousand tons/year coal-based ethanol as an example, the diameter of a tubular hydrogenation reactor is about 5m, the length of a tubular reactor is about 12m, the successful application cases of reactors with similar sizes are rarely reported in China, and the number of manufacturers with processing capacity is also very large. In order to reduce the process risk and the processing and manufacturing difficulty caused by the large-scale equipment, the hydrogenation reaction should be further researched, and the reactor type should be optimized.
SUMMERY OF THE UTILITY MODEL
The utility model provides a methyl acetate hydrogenation ware and heat transfer system of cold hydrogen feeding of multistage to reach the purpose that improves catalyst loading volume utilization ratio.
The utility model provides a technical scheme that its technical problem adopted is: a multi-stage cold hydrogen-fed methyl acetate hydrogenation reactor comprising: a reactor body; the catalyst beds are arranged in the reactor body at intervals along the vertical direction, and an air replenishing space is formed between every two adjacent catalyst beds; and each air supplementing space is communicated with the outlet of at least one cold hydrogen feeding pipe.
Furthermore, the number of the catalyst bed layers is 3-8.
Furthermore, the plurality of catalyst beds comprise a catalyst bed layer positioned at the bottom end and at least two catalyst bed layers positioned above, the heights of the at least two catalyst bed layers positioned above are the same, and the height of the catalyst bed layer positioned at the bottom end is larger than that of the catalyst bed layer positioned above.
Further, the height of the catalyst bed located at the bottom end ranges from 2.5m to 4.5m, and the height of the catalyst bed located above ranges from 1m to 3 m.
Furthermore, a filler layer is arranged between two adjacent catalyst bed layers and is arranged between the outlet of the cold hydrogen feeding pipe and the catalyst bed layer positioned below the outlet of the cold hydrogen feeding pipe.
Further, the height of the filler layer ranges from 200mm to 800 mm.
Furthermore, any one of the fillers of Raschig rings, pall rings, ladder rings, intalox rings, conjugate rings, double-arc rings, flat rings, nano rings or Intel rock is filled in the filler layer.
Further, a feeding hole is formed in the upper end of the reactor body, and the methyl acetate hydrogenation reactor with multi-section cold hydrogen feeding further comprises a gas distributor which is arranged in the reactor body and connected with the feeding hole.
Further, a gas distributor is disposed above the plurality of catalyst beds.
The utility model also provides a heat transfer system, including the methyl acetate hydrogenation reactor of the cold hydrogen feeding of foretell multistage, heat transfer system still includes that the reactor imports and exports the heat exchanger, and the material export of heat exchanger is connected with the feed inlet that reactor body upper end set up is imported and exported to the reactor, and the heat transfer entry that the heat exchanger was imported and exported to the reactor is connected with the discharge gate that reactor body lower extreme set up.
The utility model has the advantages that a plurality of catalyst bed layers are arranged at intervals along the vertical direction to form a sectional fixed bed reactor, and a cold hydrogen feeding pipe is arranged between two adjacent catalyst bed layers, so that on one hand, the molar ratio of hydrogen to methyl acetate can be improved, and the reaction is promoted to be carried out; on the other hand, the feeding temperature of the next section of bed layer is reduced, so that the activity of each temperature interval of the catalyst is fully utilized, and the purpose of improving the filling volume utilization rate of the catalyst is achieved.
Drawings
The accompanying drawings, which form a part of the present application, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention and not to limit the invention. In the drawings:
FIG. 1 is a schematic diagram of a methyl acetate hydrogenation reactor with multi-stage cold hydrogen feeding in an embodiment of the present invention;
fig. 2 is the schematic structural diagram of the heat exchange system in the embodiment of the present invention.
Reference numbers in the figures: 1. a reactor body; 2. a catalyst bed layer; 3. a cold hydrogen feed pipe; 4. a filler layer; 5. a gas distributor; 6. the inlet and outlet of the reactor are provided with heat exchangers.
Detailed Description
It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict. The present invention will be described in detail below with reference to the accompanying drawings in conjunction with embodiments.
As shown in fig. 1, the embodiment of the present invention provides a methyl acetate hydrogenation reactor with multi-stage cold hydrogen feeding, which comprises a reactor body 1, a plurality of catalyst beds 2 and a plurality of cold hydrogen feeding pipes 3 arranged in parallel. A plurality of catalyst bed layers 2 are arranged in the reactor body 1 at intervals along the vertical direction, and an air supplementing space is formed between every two adjacent catalyst bed layers 2; each gas supplementing space is communicated with the outlet of at least one cold hydrogen feeding pipe 3.
A plurality of catalyst bed layers 2 are arranged at intervals along the vertical direction to form a sectional fixed bed reactor, and a cold hydrogen feeding pipe 3 is arranged between two adjacent catalyst bed layers 2, so that the molar ratio of hydrogen to methyl acetate can be improved, and the reaction is promoted to be carried out; on the other hand, the feeding temperature of the next section of bed layer is reduced, so that the activity of each temperature interval of the catalyst is fully utilized, and the purpose of improving the filling volume utilization rate of the catalyst is achieved.
The embodiment of the utility model provides an in 2 numbers of catalyst bed be 3 ~ 8, preferably 4 ~ 6, the catalyst bed 2 that sets up above-mentioned quantity can make the methyl acetate hydrogenation ware of the cold hydrogen feeding of multistage simple structure, the manufacturing degree of difficulty reduces, can shorten delivery cycle simultaneously.
As shown in fig. 1, the plurality of catalyst beds 2 includes one catalyst bed 2 located at the bottom and at least two catalyst beds 2 located above, the heights of the at least two catalyst beds 2 located above are the same, and the height of the catalyst bed 2 located at the bottom is greater than the height of the catalyst bed 2 located above. The height of the catalyst bed layer 2 at the bottom end is greater than that of the catalyst bed layer 2 above, so that the temperature difference between the inlet and the outlet of the embodiment is more than 15 ℃, and the heat exchange between the discharged material and the cold feed is conveniently realized.
It should be noted that the height of the catalyst bed 2 located at the bottom end is in the range of 2.5m to 4.5m, and the height of the catalyst bed 2 located above is in the range of 1m to 3 m. The height can ensure that the temperature difference between the inlet and the outlet is more than 15 ℃, and the working condition requirements are met.
A packing layer 4 is also arranged between two adjacent catalyst bed layers 2, and the packing layer 4 is arranged between the outlet of the cold hydrogen feeding pipe 3 and the catalyst bed layer 2 positioned below. The filler layer 4 can promote the mixing and distribution of cold and hot gases, and avoid the problems of catalyst pulverization and service life reduction caused by quenching the catalyst bed layer 2 by cold hydrogen.
It should be noted that the height of the filler layer 4 is in the range of 200mm to 800 mm. Preferably in the height range 300mm to 500 mm. The packing layer 4 is filled with any packing of Raschig rings, pall rings, ladder rings, intalox rings, conjugate rings, double-arc rings, flat rings, nano rings or Introlox packing in bulk, and the specification of the packing is preferably Dg25 and Dg 38.
As shown in fig. 1, a feed inlet is arranged at the upper end of the reactor body 1, and the methyl acetate hydrogenation reactor for multi-stage cold hydrogen feeding further comprises a gas distributor 5 which is arranged in the reactor body 1 and connected with the feed inlet. The gas distributor 5 enables the gas introduced to be distributed uniformly over the entire cross-section. The gas distributor 5 in the embodiment of the present invention is disposed above the plurality of catalyst beds 2. I.e. the bottom wall of the gas distributor 5 is higher than the uppermost catalyst bed 2.
As shown in fig. 2, the utility model also provides a heat transfer system, including the methyl acetate hydrogenation reactor of the cold hydrogen feeding of foretell multistage, heat transfer system still includes that the reactor imports and exports heat exchanger 6, and the material export that heat exchanger 6 was imported and exported to the reactor is connected with the feed inlet that reactor body 1 upper end set up, and the heat transfer entry that heat exchanger 6 was imported and exported to the reactor is connected with the discharge gate that reactor body 1 lower extreme set up. The embodiment of the utility model provides a can control the discharge gate temperature and be higher than feed inlet temperature more than 15 ℃, the reactor ejection of compact and feeding are in 6 heat exchanges of exit heat exchanger, directly heat the feeding to the required temperature of reaction, need not the middling pressure steam and overheat.
Taking 30 ten thousand tons of coal-based ethanol per year as an example, a gas distributor is arranged at a feed inlet, a catalyst bed layer 2 is divided into four sections, the bed layer height from the first section to the third section is 2m, and the bed layer height at the fourth section is 3 m; 300mm stainless steel pall ring packing is arranged above the second to fourth sections of catalyst bed layers 2. Mixing hydrogen at about 40 ℃ with methyl acetate according to a certain molar ratio, exchanging heat through an inlet heat exchanger 6 and an outlet heat exchanger of the reactor, heating to about 200 ℃, entering the reactor, and uniformly distributing feed gas through a gas distributor 5; then enters a catalyst bed layer 2 for reaction, the temperature of a reaction system and the catalyst bed layer 2 is increased by the released heat, and the outlet temperature of the first section is about 210 ℃; supplementing cold hydrogen to the outlet of the first section, wherein the molar flow of the cold hydrogen is 1.25 times of that of methyl acetate at the inlet of the reactor, fully mixing the cold hydrogen with the outlet gas of the first section in a pall ring packing layer above the second section, and allowing the cold hydrogen and the outlet gas of the first section to enter a second section of catalyst bed layer 2 when the temperature is reduced to about 200 ℃, wherein the outlet temperature of the second section of catalyst bed layer 2 is about 210 ℃; and cold hydrogen is supplemented to the outlet of the second section, the cold hydrogen is fully mixed with the gas at the outlet of the second section of the catalyst bed layer 2 at the pall ring packing layer above the third section, the temperature is reduced to about 200 ℃, and the mixture enters the fourth section of the catalyst bed layer, and the like. The outlet temperature of the fourth section, namely the outlet temperature of the reactor, is about 215 ℃, the reaction product directly exchanges heat with the feeding material, and the temperature is reduced to 96 ℃ and then the reaction product is sent to the third-stage fractional condensation process for treatment.
Further, the embodiment is made of chrome molybdenum steel with external dimension phi 3000x15000, and the net weight of the equipment is about 105 tons (corresponding to the external dimension phi 4100x11000 of the tubular reactor for capacity, the net weight of the equipment is about 275 tons, and the 2205 dual-phase steel is about 100 tons); the annual saving of medium pressure steam is 8 ten thousand tons.
From the above description, it can be seen that the above-mentioned embodiments of the present invention achieve the following technical effects: a plurality of catalyst bed layers 2 are arranged at intervals along the vertical direction to form a sectional fixed bed reactor, and a cold hydrogen feeding pipe 3 is arranged between two adjacent catalyst bed layers 2, so that the molar ratio of hydrogen to methyl acetate can be improved, and the reaction is promoted to be carried out; on the other hand, the feeding temperature of the next section of bed layer is reduced, so that the activity of each temperature interval of the catalyst is fully utilized, and the purpose of improving the filling volume utilization rate of the catalyst is achieved.
The above description is only for the specific embodiments of the present invention, and the scope of the present invention can not be limited by the embodiments, so that the replacement of the equivalent components or the equivalent changes and modifications made according to the protection scope of the present invention should still belong to the scope covered by the present patent. In addition, the utility model provides an between technical feature and the technical feature, between technical feature and the technical scheme, all can the independent assortment use between technical scheme and the technical scheme.
Claims (10)
1. A methyl acetate hydrogenation reactor with multi-stage cold hydrogen feeding, comprising:
a reactor body (1);
the catalyst beds (2) are arranged in the reactor body (1) at intervals along the vertical direction, and an air supplementing space is formed between every two adjacent catalyst beds (2);
a plurality of cold hydrogen feeding pipes (3) which are arranged in parallel, wherein each air supplementing space is communicated with the outlet of at least one cold hydrogen feeding pipe (3).
2. A multi-stage cold hydrogen-fed methyl acetate hydrogenation reactor according to claim 1, characterized in that the number of catalyst beds (2) is 3-8.
3. A multi-stage cold hydrogen-fed methyl acetate hydrogenation reactor according to claim 1, characterized in that the plurality of catalyst beds (2) comprises one catalyst bed (2) at the bottom and at least two catalyst beds (2) at the top, the height of at least two catalyst beds (2) at the top being the same, and the height of the catalyst bed (2) at the bottom being greater than the height of the catalyst bed (2) at the top.
4. A multi-stage cold hydrogen-fed methyl acetate hydrogenation reactor according to claim 3, characterized in that the height of the catalyst bed (2) at the bottom end is in the range of 2.5m to 4.5m and the height of the catalyst bed (2) above is in the range of 1m to 3 m.
5. A multi-stage cold hydrogen-fed methyl acetate hydrogenation reactor according to claim 1, characterized in that a packing layer (4) is further arranged between two adjacent catalyst beds (2), and the packing layer (4) is arranged between the outlet of the cold hydrogen feeding pipe (3) and the catalyst bed (2) below.
6. A multistage cold hydrogen fed methyl acetate hydrogenation reactor according to claim 2, characterized in that the height of the packing layer (4) ranges from 200mm to 800 mm.
7. A multistage cold hydrogen fed methyl acetate hydrogenation reactor according to claim 2, characterized in that the packing layer (4) is filled with any one of raschig rings, pall rings, ladder rings, intalox rings, conjugate rings, double-arc rings, flat rings, nano-rings or inteloxes.
8. The methyl acetate hydrogenation reactor with multi-stage cold hydrogen feeding according to claim 1, characterized in that the upper end of the reactor body (1) is provided with a feeding hole, and the methyl acetate hydrogenation reactor with multi-stage cold hydrogen feeding further comprises a gas distributor (5) arranged in the reactor body (1) and connected with the feeding hole.
9. A multi-stage cold hydrogen-fed methyl acetate hydrogenation reactor according to claim 8, characterized in that the gas distributor (5) is arranged above the plurality of catalyst beds (2).
10. A heat exchange system comprising the multi-stage cold hydrogen feeding methyl acetate hydrogenation reactor according to any one of claims 1 to 9, wherein the heat exchange system further comprises a reactor inlet and outlet heat exchanger (6), a material outlet of the reactor inlet and outlet heat exchanger (6) is connected with a feeding port arranged at the upper end of the reactor body (1), and a heat exchange inlet of the reactor inlet and outlet heat exchanger (6) is connected with a discharging port arranged at the lower end of the reactor body (1).
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| Application Number | Priority Date | Filing Date | Title |
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| CN202022454439.5U CN214051563U (en) | 2020-10-29 | 2020-10-29 | Methyl acetate hydrogenation reactor and heat exchange system of multistage cold hydrogen feeding |
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| CN202022454439.5U CN214051563U (en) | 2020-10-29 | 2020-10-29 | Methyl acetate hydrogenation reactor and heat exchange system of multistage cold hydrogen feeding |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112169710A (en) * | 2020-10-29 | 2021-01-05 | 北京石油化工工程有限公司 | Methyl acetate hydrogenation reactor and heat exchange system of multistage cold hydrogen feeding |
| CN116020351A (en) * | 2021-10-26 | 2023-04-28 | 中国石油化工股份有限公司 | Maleic anhydride hydrogenation reaction method and maleic anhydride hydrogenation reactor |
| CN116020352A (en) * | 2021-10-26 | 2023-04-28 | 中国石油化工股份有限公司 | Method for preparing succinic anhydride by maleic anhydride hydrogenation and hydrogenation reactor |
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2020
- 2020-10-29 CN CN202022454439.5U patent/CN214051563U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112169710A (en) * | 2020-10-29 | 2021-01-05 | 北京石油化工工程有限公司 | Methyl acetate hydrogenation reactor and heat exchange system of multistage cold hydrogen feeding |
| CN116020351A (en) * | 2021-10-26 | 2023-04-28 | 中国石油化工股份有限公司 | Maleic anhydride hydrogenation reaction method and maleic anhydride hydrogenation reactor |
| CN116020352A (en) * | 2021-10-26 | 2023-04-28 | 中国石油化工股份有限公司 | Method for preparing succinic anhydride by maleic anhydride hydrogenation and hydrogenation reactor |
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