CN214763400U - System for reducing solvent consumption in maleic anhydride preparation process - Google Patents
System for reducing solvent consumption in maleic anhydride preparation process Download PDFInfo
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- CN214763400U CN214763400U CN202121214863.0U CN202121214863U CN214763400U CN 214763400 U CN214763400 U CN 214763400U CN 202121214863 U CN202121214863 U CN 202121214863U CN 214763400 U CN214763400 U CN 214763400U
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Abstract
The utility model provides a system for reduce solvent consumption in preparation cis-butenedioic anhydride technology, including temperature-reducing pressure reducer, pre-heater, rectifying column, condenser, backward flow jar, cis-butenedioic anhydride jar and reboiler, temperature-reducing pressure reducer's the mouth of adopting is connected with the reducing water respectively and adopts pipeline and high-pressure steam to adopt the pipeline, and temperature-reducing pressure reducer's the mouth of adopting passes through the pipeline and links to each other with the mouth of adopting of reboiler, and the mouth of adopting of reboiler is adopted the mouth through backward flow pipeline and rectifying column tower bottom lateral wall and is linked together, the utility model discloses high temperature high-pressure steam to getting into the reboiler cools down, reduces the consumption of solvent, practices thrift the cost.
Description
Technical Field
The utility model belongs to the technical field of chemical production, especially, relate to a system that reduces solvent consumption in preparation cis-butenedioic anhydride technology.
Background
In the process of preparing maleic anhydride by the n-butane oxidation method, certain raw materials are added into a reactor to react, a solvent is required to be continuously added into a reaction product to absorb and separate the maleic anhydride from the reaction product, and water absorption and organic solvent absorption can be divided according to different types of absorbents. The principle of the water absorption method is simple, but fumaric acid (fumaric acid for short) is easily generated due to improper temperature control, so that the problems of equipment corrosion, high energy consumption and the like are easily caused. The solvent absorption method uses an organic solvent as an absorbent, and significantly overcomes the problems commonly encountered in the water absorption method. Dibutyl phthalate (DBP) is used as a maleic anhydride absorption solvent, has low price and is more widely applied to domestic maleic anhydride production devices. However, because DBP is easily decomposed at high temperature, part of DBP is decomposed and lost, and the difficulty of post-treatment of a poor solvent is increased.
Disclosure of Invention
In view of this, the utility model aims at providing a system that reduces solvent consumption in the preparation cis-butenedioic anhydride technology, cools down the high temperature high pressure steam that gets into the reboiler, reduces the consumption of solvent, has reduced the degree of difficulty of poor solvent aftertreatment to the cost has been practiced thrift.
In order to achieve the above purpose, the technical scheme of the utility model is realized like this:
a system for reducing solvent consumption in a maleic anhydride preparation process comprises a temperature and pressure reduction device, a preheater, a rectifying tower, a condenser, a reflux tank, a maleic anhydride tank and a reboiler, wherein a sampling port of the preheater is communicated with a sampling port in the middle of a tower body of the rectifying tower through a pipeline, a sampling port at the top of the rectifying tower is connected with the reflux tank through a pipeline, and a sampling port of the reflux tank is communicated with a sampling port at the top side wall of the rectifying tower through a reflux pipeline;
a withdrawal outlet on the side wall of the top of the rectifying tower is connected with the maleic anhydride tank through a pipeline;
a bottom extraction outlet of the rectifying tower is connected with a poor solvent pump extraction inlet through a pipeline, the poor solvent pump extraction outlet is divided into two branches, one branch is communicated with the poor solvent extraction pipeline, and the other branch is communicated with the extraction inlet on the bottom side wall of the rectifying tower through a reboiler;
the extraction port of the temperature and pressure reducer is respectively connected with a temperature water extraction pipeline and a high-pressure steam extraction pipeline, the extraction port of the temperature and pressure reducer is connected with the extraction port of the reboiler through a pipeline, and the extraction port of the reboiler is communicated with the extraction port of the bottom side wall of the rectifying tower through a return pipeline.
Furthermore, a rich solvent intake pipeline is connected to the intake of the rich solvent pump, and the intake of the rich solvent pump is communicated with the intake of the preheater through a pipeline.
Further, a maleic anhydride pump is arranged on a pipeline between a collecting outlet of the side wall of the top of the rectifying tower and the maleic anhydride tank, the collecting outlet of the maleic anhydride pump is divided into two branches, one branch is communicated with a collecting inlet of the maleic anhydride tank through a pipeline, and the other branch is communicated with the collecting inlet of the side wall of the top of the rectifying tower through a return pipeline.
Furthermore, a condenser is arranged on a pipeline between a sampling port at the top of the rectifying tower and a sampling port of the reflux tank.
Furthermore, a reflux pump is arranged on a pipeline between a bottom extraction outlet of the reflux tank and an extraction inlet on the side wall of the top of the rectifying tower.
Furthermore, the top extraction outlet of the reflux tank is connected with a noncondensable gas extraction pipeline.
Furthermore, the extraction port of the reboiler is also communicated with the condensate pipeline.
Compared with the prior art, the beneficial effects of the utility model are that:
the utility model discloses an increase the pressure reducer that reduces temperature before the adoption mouth of reboiler, under the effect of relief pressure valve and desuperheating water, the steam that will get into the reboiler reduces the temperature and reduces the pressure, has reduced the decomposition of solvent, avoids because temperature and pressure are too high, and absorption solvent DBP is easily decomposed under high temperature, causes the increase of phthalic anhydride volume, also causes the degree of difficulty of solvent aftertreatment to increase, to take 4 ten thousand tons of maleic anhydride scales of annual output as an example, can practice thrift cost about 10500 ten thousand yuan per year.
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 flow chart of a solvent desorption process according to an embodiment of the present invention.
Description of reference numerals:
1-temperature and pressure reduction device; 2-rich solvent pump; 3-a preheater; 4-a rectifying tower; 5-a condenser; 6-a reflux tank; 7-reflux pump; 8-maleic anhydride pump; 9-maleic anhydride tank; 10-lean solvent pump; 11-reboiler.
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 present invention will be described in detail below with reference to the accompanying drawings in conjunction with embodiments.
Example 1
As shown in figure 1, a raw material rich solvent is pressurized by a rich solvent pump 2 and then heated by a preheater 3 and then enters a rectifying tower 4, the mass ratio of maleic anhydride to the solvent in the rich solvent is 1:6, the rectifying tower 4 is operated under negative pressure, the operating pressure at the top of the rectifying tower 4 is 2.5kPaA, the operating pressure at the bottom of the rectifying tower 4 is 4.5kPaA, three sections of fillers are arranged in the rectifying tower, and the raw material is desorbed in a first packing layer and a second packing layer of the rectifying tower. The high-purity crude maleic anhydride is extracted to a maleic anhydride tank 9 through a maleic anhydride pump at the upper section of a packing section of a rectifying tower 4, the pressure of the maleic anhydride tank 9 is normal pressure, and the temperature is 70 ℃.
Maleic anhydride steam containing light components is extracted from the top of the rectifying tower 4 and condensed and refluxed into a reflux tank 6 through a condenser 5, the pressure of the reflux tank is 2kPaA, the temperature is 60 ℃, an incondensable gas pipeline at the top of the reflux tank is connected with a vacuum system to ensure that the interior of the tower is in a vacuum state, and a liquid phase returns to the rectifying tower 4 to meet the gas-liquid balance, so that the rectifying purpose is achieved.
After being pressurized by a lean solvent pump 10, a part of the material extracted from the bottom of the rectifying tower 4 enters a reboiler 11 and is heated and vaporized by the high-pressure steam with reduced temperature and reduced pressure, and then returns to the rectifying tower 4, and the vaporized lean solvent rises in the rectifying tower 4 to form gas-liquid balance with the refluxed liquid phase; the other part is conveyed to a lean solvent post-treatment system through a lean solvent post-treatment pipeline, the steam pressure is 2.0MPaA after temperature and pressure reduction, the temperature is 212 ℃, and the temperature of the temperature reduction water is 105 ℃.
Example 2
The embodiment of embodiment example 2 is substantially the same as embodiment example 1 except that: the operation pressure at the top of the rectifying tower 4 is 2.5kPaA, the operation pressure at the bottom of the rectifying tower is 6kPaA, four sections of fillers are arranged in the rectifying tower 4, raw materials are desorbed in a first packing layer, a second packing layer and a third packing layer of the rectifying tower, and high-purity crude maleic anhydride at the upper section of the packing section of the rectifying tower 4 is extracted by a maleic anhydride pump 8 and discharged into a maleic anhydride tank 9;
after temperature and pressure reduction, the steam pressure is 1.8MPaA, the temperature is 207 ℃, and the temperature of the temperature reduction water is 105 ℃.
Example 3
The embodiment of example 3 is substantially the same as example 1 except that: the rectifying column 4 was operated at a top pressure of 2.5kPaA and at a bottom pressure of 4.5 kPaA. Five sections of fillers are filled in the rectifying tower, raw materials are desorbed in a first packing layer, a second packing layer and a third packing layer of the rectifying tower, and high-purity crude maleic anhydride in the upper section of the fillers of the rectifying tower is extracted by a maleic anhydride pump and discharged into a crude anhydride tank;
after temperature reduction and pressure reduction, the steam pressure is 1.75MPaA, the temperature is 205.7 ℃, and the temperature of the temperature reduction water is 105 ℃.
The mass ratio of maleic anhydride to solvent in the raw material is about 1: 6-1: 9, the flow rate of the poor solvent is about 38800kg/h, the mass ratio of phthalic anhydride in the poor solvent of the embodiment of the utility model is about 0.2%, and the flow rate is about 77.6 kg/h; in the maleic anhydride system without adding the temperature and pressure reducing device, the mass ratio of the phthalic anhydride in the lean solvent is about 2 percent, and the flow rate is about 776 kg/h.
It can be seen from comparing two sets of data, the utility model discloses reducible phthalic anhydride's quantity is about 698.4kg/h, and the solvolysis reduction volume is about 1312.5kg/h to solvent unit price 10000 yuan/ton are counted, the utility model discloses can practice thrift cost about 10500 ten thousand yuan every year. Reduces the solvent decomposition and avoids the difficulty of solvent post-treatment caused by the increase of the amount of phthalic anhydride.
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. A system for reducing solvent consumption in a maleic anhydride preparation process is characterized in that: the system comprises a temperature and pressure reduction device (1), a preheater (3), a rectifying tower (4), a condenser (5), a reflux tank (6), a maleic anhydride tank (9) and a reboiler (11), wherein a production outlet of the preheater (3) is communicated with a production inlet in the middle of a tower body of the rectifying tower (4) through a pipeline, a production outlet at the top of the rectifying tower (4) is connected with the reflux tank (6) through a pipeline, and a production outlet of the reflux tank (6) is communicated with a production inlet at the top side wall of the rectifying tower (4) through a reflux pipeline;
a withdrawal outlet on the side wall of the top of the rectifying tower (4) is connected with a maleic anhydride tank (9) through a pipeline;
a bottom extraction port of the rectifying tower (4) is connected with an extraction port of the lean solvent pump (10) through a pipeline, the extraction port of the lean solvent pump (10) is divided into two branches, one branch is communicated with the lean solvent extraction pipeline, and the other branch is communicated with an extraction port on the bottom side wall of the rectifying tower (4) through a reboiler (11);
the extraction port of the temperature and pressure reducer (1) is respectively connected with a temperature water extraction pipeline and a high-pressure steam extraction pipeline, the extraction port of the temperature and pressure reducer (1) is connected with the extraction port of the reboiler (11) through a pipeline, and the extraction port of the reboiler (11) is communicated with the extraction port of the bottom side wall of the rectifying tower (4) through a reflux pipeline.
2. The system for reducing the solvent consumption in the process for preparing maleic anhydride according to claim 1, wherein: the extraction port of the rich solvent pump (2) is connected with a rich solvent extraction pipeline, and the extraction port of the rich solvent pump (2) is communicated with the extraction port of the preheater (3) through a pipeline.
3. The system for reducing the solvent consumption in the process for preparing maleic anhydride according to claim 1, wherein: a maleic anhydride pump (8) is arranged on a pipeline between a collecting outlet of the side wall of the top of the rectifying tower (4) and the maleic anhydride tank (9), the collecting outlet of the maleic anhydride pump (8) is divided into two branches, one branch is communicated with the collecting inlet of the maleic anhydride tank (9) through a pipeline, and the other branch is communicated with the collecting inlet of the side wall of the top of the rectifying tower (4) through a return pipeline.
4. The system for reducing the solvent consumption in the process for preparing maleic anhydride according to claim 1, wherein: a condenser (5) is arranged on a pipeline between a sampling port at the top of the rectifying tower (4) and a sampling port of the reflux tank (6).
5. The system for reducing the solvent consumption in the process for preparing maleic anhydride according to claim 1, wherein: a reflux pump (7) is arranged on a pipeline between a sampling port at the bottom of the reflux tank (6) and a sampling port on the side wall of the top of the rectifying tower (4).
6. The system for reducing the solvent consumption in the process for preparing maleic anhydride according to claim 1, wherein: the top extraction outlet of the reflux tank (6) is connected with a noncondensable gas extraction pipeline.
7. The system for reducing the solvent consumption in the process for preparing maleic anhydride according to claim 1, wherein: the extraction port of the reboiler (11) is also communicated with the condensate pipeline.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202121214863.0U CN214763400U (en) | 2021-06-01 | 2021-06-01 | System for reducing solvent consumption in maleic anhydride preparation process |
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| CN202121214863.0U CN214763400U (en) | 2021-06-01 | 2021-06-01 | System for reducing solvent consumption in maleic anhydride preparation process |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117504545A (en) * | 2024-01-08 | 2024-02-06 | 常州瑞华化工工程技术股份有限公司 | Device and method for obtaining maleic anhydride from gas phase containing maleic anhydride |
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2021
- 2021-06-01 CN CN202121214863.0U patent/CN214763400U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117504545A (en) * | 2024-01-08 | 2024-02-06 | 常州瑞华化工工程技术股份有限公司 | Device and method for obtaining maleic anhydride from gas phase containing maleic anhydride |
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