CN214830035U - Optimized separation system for maleic anhydride direct hydrogenation reaction product - Google Patents
Optimized separation system for maleic anhydride direct hydrogenation reaction product Download PDFInfo
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- CN214830035U CN214830035U CN202121803059.6U CN202121803059U CN214830035U CN 214830035 U CN214830035 U CN 214830035U CN 202121803059 U CN202121803059 U CN 202121803059U CN 214830035 U CN214830035 U CN 214830035U
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Abstract
The utility model provides a direct hydrogenation reaction product's of maleic anhydride piece-rate system who optimizes, including dividing the tower crudely, the top of the tower that divides the tower crudely even has light processing line, and the tower side that divides the tower crudely even has azeotropic solvent processing line, and the tower cauldron that divides the tower crudely even has heavy processing line. The optimized separation system for the maleic anhydride direct hydrogenation reaction product realizes the separation and purification of different products of various hydrogenation processes such as 1, 4-Butanediol (BDO), gamma-butyrolactone (GBL), Tetrahydrofuran (THF), Succinic Anhydride (SA) and the like through the direct hydrogenation of the maleic anhydride; the circulation and maximum recovery of the reaction solvent are realized; the reaction wastewater is removed to the maximum extent, the content of organic matters in the wastewater is reduced to the maximum extent, and the separated wastewater can be directly discharged without being treated; the process flow is simple, the energy consumption is low, and the separated product has high quality and high yield; the tetrahydrofuran refining and dehydrating tower can realize the recycling of heat in the operation process, has high-efficiency energy-saving effect and greatly reduces the annual carbon emission.
Description
Technical Field
The utility model belongs to the technical field of the chemical industry, especially, relate to a separation system of direct hydrogenation reaction product of maleic anhydride of optimizing.
Background
Under the large background of policy promotion of various countries around the world and the increasing awareness of environmental protection of the people, the development of the global biodegradable plastics becomes a research focus in recent years. 1, 4-butanediol and succinic acid (starting material succinic anhydride) are used as upstream raw materials for biodegradable plastics, and the demand is kept continuously increasing. The maleic anhydride is subjected to hydrogenation reaction to prepare 1, 4-butanediol, gamma-butyrolactone, tetrahydrofuran, succinic anhydride and other process routes, and due to the advantages of raw material sources, technical economy, product composition, process flow and the like, the method is widely researched and realizes industrialization. Since the hydrogenation of maleic anhydride is a complex reaction, a series of byproducts are generated in addition to the main product, and the process of product separation is particularly critical for obtaining a high-purity target product.
At present, few reports are reported for the separation process of the direct hydrogenation reaction product of maleic anhydride, the industrialized separation process is complex, the energy consumption is high, the content of organic matters in the separated wastewater is high, and the treatment difficulty is high. Therefore, a separation technology with simple process, energy conservation, consumption reduction and environmental protection is urgently needed to be developed so as to effectively solve the problem of separation of the direct hydrogenation reaction product of maleic anhydride in the current industry and improve the comprehensive economic benefits of direct hydrogenation production of high-added-value products such as 1, 4-Butanediol (BDO), gamma-butyrolactone (GBL), Tetrahydrofuran (THF), Succinic Anhydride (SA) and the like from maleic anhydride.
Disclosure of Invention
In view of this, the utility model aims at overcoming the defects existing in the prior art, and provides a separation system of maleic anhydride direct hydrogenation reaction product, which has the advantages of simple flow, good product quality, high yield, low wastewater treatment difficulty, high solvent recovery degree and energy consumption saving.
In order to achieve the above purpose, the technical scheme of the utility model is realized like this:
an optimized separation system for maleic anhydride direct hydrogenation reaction products comprises a rough separation tower, wherein the tower top of the rough separation tower is connected with a light treatment line, the tower side of the rough separation tower is connected with an azeotropic solvent treatment line, and a tower kettle of the rough separation tower is connected with a heavy treatment line;
the light treatment line comprises a THF (tetrahydrofuran) tower, the tower top of the rough separation tower is connected with the tower side of the THF tower through a second pipeline, the top of the THF tower is connected with the upper part of the rough separation tower through a third pipeline, and the tower kettle of the THF tower is connected with a sixth pipeline;
the azeotropic solvent treatment line comprises an oil-water separator and a dehydration tower, wherein the tower side of the crude separation tower is connected with a feed inlet of the oil-water separator through a seventh pipeline, an oil phase outlet of the oil-water separator is connected with the middle part of the crude separation tower through an eighth pipeline, a water phase outlet of the oil-water separator is connected with a feed inlet of the dehydration tower through a ninth pipeline, the tower top of the dehydration tower is connected with an eleventh pipeline, and a tower kettle of the dehydration tower is connected with a twelfth pipeline;
the heavy processing line comprises a light component removal tower and a heavy component removal tower, a tower kettle of the coarse component removal tower is connected with a feed inlet of the light component removal tower through a fifteenth pipeline, the tower kettle of the light component removal tower is connected with the feed inlet of the heavy component removal tower through an eighteenth pipeline, the tower top of the light component removal tower is connected with a sixteenth pipeline, the tower side of the light component removal tower is connected with a seventeenth pipeline, the tower top of the heavy component removal tower is connected with a nineteenth pipeline, the tower kettle of the heavy component removal tower is connected with a twenty-first pipeline, and the tower side of the heavy component removal tower is connected with a twentieth pipeline.
Further, a tower kettle of the dehydration tower is connected with the lower part of the dehydration tower through a thirteenth pipeline; and a heat exchanger is arranged on the thirteenth pipeline.
Further, the third pipeline passes through the heat exchanger.
Further, the top of the THF column and the upper part of the THF column are connected by a fourth line.
Furthermore, the tower side of the dehydration tower is connected with the feed inlet of the oil-water separator through a tenth pipeline.
Further, the top of the dehydration tower is connected with a dryer through an eleventh pipeline.
Further, the dryer is connected with a feed inlet of the solvent recovery tower through a twenty-third pipeline, the top of the solvent recovery tower is connected with a twenty-fourth pipeline, and the tower kettle of the solvent recovery tower is connected with a twenty-fifth pipeline.
Compared with the prior art, the beneficial effects of the utility model are that:
(1) the optimized separation system for the maleic anhydride direct hydrogenation reaction product realizes the separation and purification of different products of various hydrogenation processes such as 1, 4-Butanediol (BDO), gamma-butyrolactone (GBL), Tetrahydrofuran (THF), Succinic Anhydride (SA) and the like by direct hydrogenation of maleic anhydride.
(2) The optimized separation system for the maleic anhydride direct hydrogenation reaction product has short flow, the separated product meets the industrial high-class product standard, has high quality, and meets the quality requirements of downstream medicines, foods, polymer grade PBAT and other products.
(3) The optimized separation system for the direct hydrogenation reaction product of maleic anhydride has the advantages of simple separation process of the water solvent azeotrope and low energy consumption.
(4) The optimized separation system for the maleic anhydride direct hydrogenation reaction product realizes the maximum separation of water in the reaction product and the maximum removal of organic matters in wastewater, and the separated wastewater can be directly discharged without treatment.
(5) The optimized separation system for the direct hydrogenation reaction product of maleic anhydride realizes the circulation and the maximum recovery of the solvent.
(6) According to the optimized separation system for the direct hydrogenation reaction product of maleic anhydride, a differential pressure rectification method is adopted in the tetrahydrofuran refining process, the rough separation tower is used as a low-pressure tower, the THF tower is used as a high-pressure tower, and a set of low-pressure tower system is saved. The gaseous latent heat at the top of the THF tower is fully and reasonably utilized and thermally coupled with the cold material in the tower kettle of the dehydration tower, so that the heat is recycled, the consumption of steam and condensing medium is saved, the production cost is saved, the efficient energy-saving effect is realized, and the annual carbon emission is greatly reduced.
Drawings
The accompanying drawings, which form a part hereof, 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 without undue limitation. In the drawings:
FIG. 1 is a process schematic diagram of an optimized separation system for maleic anhydride direct hydrogenation reaction products according to the present invention.
Description of reference numerals:
1-rough separation tower; 2-THF column; 3-a dehydration column; 4-a light component removal tower; 5-a de-weighting tower; 6-a solvent recovery column; 7-oil water separator; 8-a dryer;
01-a first pipeline; 02-a second pipeline; 03-a third pipeline; 04-a fourth pipeline; 06-a sixth pipeline; 07-a seventh conduit; 08-eighth line; 09-ninth conduit; 10-tenth conduit; 11-eleventh line; 12-a twelfth conduit; 13-a thirteenth line; 15-a fifteenth pipeline; 16-a sixteenth conduit; 17-a seventeenth line; 18-eighteenth line; 19-nineteenth line; 20-twentieth pipeline; 21-twenty-first pipeline; 23-the twenty-third line; 24-a twenty-four circuit; 25-twenty-fifth pipeline.
Detailed Description
It should be noted that, in the present invention, the embodiments and features of the embodiments may be combined with each other without conflict.
In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like, indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are used merely for convenience of description and for simplicity of description, and do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore, should not be construed as limiting the present invention. Furthermore, the terms "first", "second", etc. are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first," "second," etc. may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless otherwise specified.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art through specific situations.
The invention will be described in detail with reference to the following examples with reference to the accompanying drawings:
as shown in fig. 1, the embodiment provides an optimized separation system for maleic anhydride direct hydrogenation reaction products, which comprises a rough separation tower 1, wherein the top of the rough separation tower 1 is connected with a light treatment line, the tower side of the rough separation tower 1 is connected with an azeotropic solvent treatment line, and the tower kettle of the rough separation tower 1 is connected with a heavy treatment line.
Taking the separation of reaction products of the BDO preparation process by direct hydrogenation of maleic anhydride as an example, the working process of the system is as follows:
after hydrogen and other non-condensable gases are separated from a maleic anhydride hydrogenation reaction product through a gas-liquid separation device, a liquid phase product enters a rough separation tower 1 through a first pipeline 01, a THF water azeotrope obtained at the tower top enters a light treatment line, the THF water azeotrope enters a THF tower 2 through a second pipeline 02, the THF tower 2 is communicated with the upper part of the rough separation tower 1 through a third pipeline 03, and a tower kettle of the THF tower 2 is communicated with a sixth pipeline 06, so that a THF product is extracted.
The solvent and the water azeotrope produced at the tower side of the rough separation tower 1 enter an azeotropic solvent treatment line, the solvent and the water azeotrope enter an oil-water separator 7 through a seventh pipeline 07, an oil phase produced at the upper part of the oil-water separator 7 flows back to the rough separation tower 1 through an eighth pipeline 08, and a water phase output at the lower part of the oil-water separator 7 is input into a dehydration tower 3 through a ninth pipeline 09.
The tower top of the dehydration tower 3 is light sewage containing propanol and the like, the light sewage is extracted through an eleventh pipeline 11, the wastewater with solvent and other components removed is extracted from the bottom of the dehydration tower 3 through a twelfth pipeline 12, the tower side of the dehydration tower 3 is communicated with the middle part of a seventh pipeline 07 through a tenth pipeline 10 to form an oil-water circulation line, and the solvent and water azeotrope generated from the tower side of the dehydration tower 3 returns to the oil-water separator 7; the oil-water separator 7, the dehydration tower 3 and the crude separation tower 1 form circulation of solvent aqueous solution;
the bottom of the dehydrating tower 3 is connected with the lower part of the dehydrating tower 3 through a thirteenth pipeline 13 to form a circulating pipe, a heat exchanger is arranged on the thirteenth pipeline 13, a third pipeline 03 connecting the top of the THF tower 2 and the top of the rough separation tower 1 passes through the heat exchanger, the heat exchanger is a high-efficiency heat exchanger and is used as a condenser for condensing the gas phase at the top of the THF tower 2 and a reboiler for heating the liquid phase at the bottom of the dehydrating tower 3;
an eleventh pipeline 11 connected to the top of the dehydrating tower 3 is connected with an inlet of a dryer 8, the dryer 8 can be selected from equipment such as a drying tank, an outlet of the dryer 8 produces dehydrated mixture such as propanol and solvent, the mixture enters a solvent recovery tower 6 through a twenty-third pipeline 23, light substances such as propanol are arranged at the top of the solvent recovery tower 6 and are extracted through a twenty-fourth pipeline 24, the purified solvent is extracted from the bottom of the solvent recovery tower 6 through a twenty-fifth pipeline 25;
BDO, GBL, SA, solvent, heavy component products and the like are arranged in the tower bottom of the rough fractionating tower 1 and enter the light component removing tower 4 through a fifteenth pipeline 15, refined solvent is arranged at the tower top of the light component removing tower 4 and is extracted through a sixteenth pipeline 16, a mixture of the solvent, MA and GBL is arranged at the tower side of the light component removing tower 4 and is extracted through a seventeenth pipeline 17 and is circulated to the hydrogenation reaction part for continuous reaction, BDO, SA, the heavy component products and the like are arranged in the tower bottom of the light component removing tower 4 and enter the heavy component removing tower 5 through an eighteenth pipeline 18, GBL possibly existing in a very small amount and carried BDO are arranged at the tower top of the heavy component removing tower 5 and are extracted through a nineteenth pipeline 19 and are circulated to the hydrogenation reaction part for continuous reaction, BDO products are extracted at the tower side of the heavy component removing tower 5 through a twentieth pipeline 20, and heavy component products are extracted at the tower bottom of the heavy component removing tower 5 through a twenty first pipeline 21.
In the embodiment, the latent heat of the high-temperature position at the top of the high-pressure THF tower 2 is transferred to the kettle materials of the low-pressure dehydrating tower 3 through the heat exchanger, the gas phase at the top of the high-pressure tower is condensed while the kettle materials of the low-pressure tower are heated, and finally the condensed gas phase is circulated back to the high-pressure tower system, so that the latent heat of the gas phase at the top of the high-pressure tower is fully utilized for thermal coupling, the heat is recycled, the consumption of steam and cooling media is saved, the energy consumption is reduced, and the heat exchanger is used as a condenser and a reboiler, so that one heat exchanger is saved. In other embodiments, the tetrahydrofuran differential pressure rectification process takes the rough separation tower 1 as a low-pressure tower, and only one high-pressure THF tower 2 is needed to realize the THF differential pressure rectification, so that a set of tower system is saved. Therefore, in actual production, the investment of the device and the operation cost can be reduced to different degrees.
In this embodiment, according to the hydrogenation process route, the product composition, the wastewater treatment measures, and the like, the dryer 8 and the solvent recovery tower 6 may be operated intermittently or continuously, and the light wastewater containing propanol and the like at the top of the dehydration tower 3 is not treated by the dryer 8 and the solvent recovery tower 6, and is discharged after reaching the standard after being further treated.
The reaction product of direct hydrogenation production of BDO with 10 ten thousand tons of maleic anhydride per year (8000 hours of annual operation) is taken as a separation raw material, the purity of the main product BDO is more than or equal to 99.7 wt%, the purity of the byproduct THF is more than or equal to 99.95 wt%, and the yield is more than or equal to 98.0 wt%.
The latent heat of the gas phase at the top of the THF tower 22 is fully utilized, steam can be saved by 0.8-2.8 tons/hour, circulating water can be saved by 50-180 tons/hour, and annual carbon emission reduction is 450-1500 tons.
The above description is only a preferred embodiment of the present invention, and should not be taken as limiting the invention, and any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (7)
1. An optimized separation system for maleic anhydride direct hydrogenation reaction products is characterized by comprising a rough separation tower (1), wherein the top of the rough separation tower (1) is connected with a light treatment line, the tower side of the rough separation tower (1) is connected with an azeotropic solvent treatment line, and the tower kettle of the rough separation tower (1) is connected with a heavy treatment line;
the light treatment line comprises a THF (tetrahydrofuran) tower (2), the tower top of the crude separation tower (1) is connected with the tower side of the THF tower (2) through a second pipeline (02), the top of the THF tower (2) is connected with the upper part of the crude separation tower (1) through a third pipeline (03), and the tower kettle of the THF tower (2) is connected with a sixth pipeline (06);
the azeotropic solvent treatment line comprises an oil-water separator (7) and a dehydration tower (3), the tower side of the crude separation tower (1) is connected with a feed inlet of the oil-water separator (7) through a seventh pipeline (07), an oil phase outlet of the oil-water separator (7) is connected with the middle part of the crude separation tower (1) through an eighth pipeline (08), a water phase outlet of the oil-water separator (7) is connected with a feed inlet of the dehydration tower (3) through a ninth pipeline (09), the tower top of the dehydration tower (3) is connected with an eleventh pipeline (11), and a tower kettle of the dehydration tower (3) is connected with a twelfth pipeline (12);
the heavy processing line comprises a light component removal tower (4) and a heavy component removal tower (5), the tower kettle of the light component removal tower (1) is connected with the feed inlet of the light component removal tower (4) through a fifteenth pipeline (15), the tower kettle of the light component removal tower (4) is connected with the feed inlet of the heavy component removal tower (5) through an eighteenth pipeline (18), the tower top of the light component removal tower (4) is connected with a sixteenth pipeline (16), the tower side of the light component removal tower (4) is connected with a seventeenth pipeline (17), the tower top of the heavy component removal tower (5) is connected with a nineteenth pipeline (19), the tower kettle of the heavy component removal tower (5) is connected with a twenty-first pipeline (21), and the tower side of the heavy component removal tower (5) is connected with a twentieth pipeline (20).
2. The optimized separation system for the direct hydrogenation reaction product of maleic anhydride as claimed in claim 1, wherein: the tower kettle of the dehydration tower (3) is connected with the lower part of the dehydration tower (3) through a thirteenth pipeline (13); a heat exchanger is arranged on the thirteenth pipeline (13).
3. The optimized separation system for the direct hydrogenation reaction product of maleic anhydride as claimed in claim 2, wherein: the third pipeline (03) passes through the heat exchanger.
4. The optimized separation system for the direct hydrogenation reaction product of maleic anhydride as claimed in claim 1, wherein: the top of the THF column (2) is connected with the upper part of the THF column (2) through a fourth pipeline (04).
5. The optimized separation system for the direct hydrogenation reaction product of maleic anhydride as claimed in claim 1, wherein: the tower side of the dehydration tower (3) is connected with the feed inlet of the oil-water separator (7) through a tenth pipeline (10).
6. The optimized separation system for the direct hydrogenation reaction product of maleic anhydride as claimed in claim 1, wherein: the top of the dehydrating tower (3) is connected with a dryer (8) through an eleventh pipeline (11).
7. The optimized separation system for the direct hydrogenation reaction product of maleic anhydride as claimed in claim 6, wherein: the dryer (8) is connected with a feed inlet of the solvent recovery tower (6) through a twenty-third pipeline (23), the top of the solvent recovery tower (6) is connected with a twenty-fourth pipeline (24), and a tower kettle of the solvent recovery tower (6) is connected with a twenty-fifth pipeline (25).
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114272871A (en) * | 2022-01-24 | 2022-04-05 | 天津海成化工技术有限公司 | System and method for preparing NMP (N-methyl pyrrolidone) by taking maleic anhydride as raw material |
-
2021
- 2021-08-03 CN CN202121803059.6U patent/CN214830035U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114272871A (en) * | 2022-01-24 | 2022-04-05 | 天津海成化工技术有限公司 | System and method for preparing NMP (N-methyl pyrrolidone) by taking maleic anhydride as raw material |
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