Epoxy propane recovery device for propylene carbonate device

Abstract

The utility model relates to a propylene oxide recovery device for a propylene carbonate device. According to the technical scheme, the upper end of a gas-liquid separator is connected with a propylene carbonate tail gas pipe, the lower end of the gas-liquid separator is connected with a crude cyclopropyl condensate tank, the lower end of the crude cyclopropyl condensate tank is connected to a side line of a degassing tower, and the lower end of the degassing tower is connected to a cyclopropyl distillation tower; the top of the gas-liquid separator is connected to a precooler through a pipeline, the side line of the precooler is connected with a separation tank through a pipeline and a compressor, and the lower end of the separation tank is connected to a crude product cyclopropyl condensate tank through a pipeline. The utility model has the beneficial effects that after epoxypropane liquid is separated by the separation tank, gas returns to the buffer tank, the liquid enters the degassing tower to remove substances with a boiling point lower than that of epoxypropane, the liquid with the boiling point lower than that of the epoxypropane is obtained at the bottom of the tower and then enters the epoxypropane rectifying tower, and high-purity epoxypropane is obtained at the top of the epoxypropane rectifying tower; and the recovery and reutilization of the epoxypropane are realized.

Description

Technical Field

[0001] The utility model relates to the field of propylene carbonate reaction recovery, in particular to a propylene oxide recovery device in a propylene carbonate device. Background Art

[0002] Propylene carbonate can be used as an excellent medium for high-performance batteries and capacitors in the electronics industry, and as a solvent and plasticizer for polymers in the polymer industry. It is a colorless, odorless, flammable liquid that is miscible with ether, acetone, benzene, chloroform, vinyl acetate, etc. It is soluble in water and carbon tetrachloride, has a strong ability to absorb carbon dioxide, and is stable in nature.

[0003] At present, in industry, propylene oxide and carbon dioxide are generally used to synthesize propylene carbonate under a certain temperature and pressure. During the production process, the propylene oxide that has not fully reacted in the reactor is distilled through the system, then extracted through the vacuum system and directly discharged, which not only causes the loss of propylene oxide and economic losses, but also pollutes the environment. Utility Model Content

[0004] The purpose of the utility model is to provide a propylene oxide recovery device in a propylene carbonate device in view of the above-mentioned defects in the prior art. By effectively recovering and separating propylene oxide, the loss of propylene oxide can be reduced, the yield can be improved, and the economic benefits can be improved, and the pollution to the environment can be reduced.

[0005] The utility model discloses a propylene oxide recovery device in a propylene carbonate device, and the technical scheme thereof is as follows: comprising a gas-liquid separator (V101), a crude cyclopropane condensate tank (V201), a precooler (L101), a compressor (C101), a separation tank (V102), a degassing tower (T101), a cyclopropane distillation tower (T102), a second feed pump (P102), a third feed pump (P103), a fourth feed pump (P104), and a fifth feed pump (P105), wherein the upper end of the gas-liquid separator (V101) is connected to a propylene carbonate tail gas pipe, and the lower end of the gas-liquid separator (V101) is connected to a crude cyclopropane condensate tank (V201) through a pipeline. A cyclopropane condensate tank (V201), the lower end of the crude cyclopropane condensate tank (V201) is connected to the side line of the degassing tower (T101) through a second feed pump (P102) and a pipeline, and the lower end of the degassing tower (T101) is connected to the cyclopropane distillation tower (T102) through a third feed pump (P103) and a pipeline; the top of the gas-liquid separator (V101) is connected to the precooler (L101) through a pipeline, the side line of the precooler (L101) is connected to the separation tank (V102) through a pipeline and a compressor (C101), and the lower end of the separation tank (V102) is connected to the crude cyclopropane condensate tank (V201) through a pipeline.

[0006] Preferably, the lower end of the gas-liquid separator (V101) is connected to the crude cyclopropane condensate tank (V201) via a pipeline and a first feed pump (P101).

[0007] Preferably, the lower end of the precooler (L101) is connected to the crude cyclopropane condensate tank (V201) via a pipeline.

[0008] Preferably, the upper end of the degassing tower (T101) is connected to the first cryogenic cooler (L102) via a pipeline, and the output end of the first cryogenic cooler (L102) is connected to the first buffer tank (E01).

[0009] Preferably, the upper end of the cyclopropane distillation tower (T102) is connected to the second cryogenic cooler (L103) via a pipeline, and the output end of the second cryogenic cooler (L103) is connected to the second buffer tank (E02).

[0010] Preferably, the lower end of the second buffer tank (E02) is connected to the side line of the cyclopropane distillation tower (T102) through one pipeline and the other pipeline is sent out.

[0011] The beneficial effects of the utility model are as follows: the utility model recovers and separates propylene carbonate tail gas through pre-cooling separation, compression, cooling separation, heavy distillation and light distillation; after the propylene oxide liquid is separated in a separation tank, the gas returns to the buffer tank; the liquid enters a degassing tower to remove substances with a lower boiling point than that of propylene oxide; after the liquid with a lower boiling point than that of propylene oxide is removed at the bottom of the tower, the liquid enters a propylene oxide distillation tower through a third feed pump; high-purity propylene oxide is obtained at the top of the propylene oxide distillation tower; and substances with a higher boiling point than that of propylene oxide discharged at the bottom of the propylene oxide tower are returned to the original system for recycling. BRIEF DESCRIPTION OF THE DRAWINGS

[0012] Figure 1 It is a structural schematic diagram of embodiment 1 of the utility model;

[0013] Figure 2 It is a structural schematic diagram of embodiment 2 of the utility model;

[0014] In the above figure: gas-liquid separator V101, crude cyclopropane condensate tank V201, precooler L101, compressor C101, separation tank V102, degassing tower T101, cyclopropane distillation tower T102, first cryogenic refrigerator L102, second cryogenic refrigerator L103, first feed pump P101, second feed pump P102, third feed pump P103, fourth feed pump P104, fifth feed pump P105, first buffer tank E01, second buffer tank E02. DETAILED DESCRIPTION

[0015] The preferred embodiments of the present invention are described below in conjunction with the accompanying drawings. It should be understood that the preferred embodiments described herein are only used to illustrate and explain the present invention, and are not used to limit the present invention.

[0016] Example 1, reference Figure 1 The utility model mentions a propylene oxide recovery device in a propylene carbonate device, comprising a gas-liquid separator V101, a crude cyclopropane condensate tank V201, a precooler L101, a compressor C101, a separation tank V102, a degassing tower T101, a cyclopropane distillation tower T102, a first cryogenic refrigerator L102, a second cryogenic refrigerator L103, a first feed pump P101, a second feed pump P102, a third feed pump P103, a first buffer tank E01 and a second buffer tank E02, wherein the upper end of the gas-liquid separator V101 is connected to a propylene carbonate tail gas pipe, and the gas-liquid separator V101 is connected to a propylene carbonate tail gas pipe. The lower end of the gas-liquid separator V101 is connected to the crude cyclopropane condensate tank V201 through a pipeline, the lower end of the crude cyclopropane condensate tank V201 is connected to the side line of the degassing tower T101 through a second feed pump P102 and a pipeline, and the lower end of the degassing tower T101 is connected to the cyclopropane distillation tower T102 through a third feed pump P103 and a pipeline; the top of the gas-liquid separator V101 is connected to the precooler L101 through a pipeline, the side line of the precooler L101 is connected to the separation tank V102 through a pipeline and a compressor C101, and the lower end of the separation tank V102 is connected to the crude cyclopropane condensate tank V201 through a pipeline.

[0017] The lower end of the gas-liquid separator V101 is connected to the crude cyclopropane condensate tank V201 through a pipeline and a first feed pump P101.

[0018] The lower end of the precooler L101 is connected to the crude cyclopropane condensate tank V201 through a pipeline.

[0019] The upper end of the degassing tower T101 is connected to the first cryogenic cooler L102 through a pipeline, and the output end of the first cryogenic cooler L102 is connected to the first buffer tank E01.

[0020] The upper end of the cyclopropane distillation tower T102 is connected to the second cryogenic cooler L103 through a pipeline, and the output end of the second cryogenic cooler L103 is connected to the second buffer tank E02.

[0021] The lower end of the second buffer tank E02 is connected to the side line of the cyclopropane distillation tower T102 through a pipeline.

[0022] When the utility model is used, the propylene carbonate tail gas from the vacuum distillation system of the propylene carbonate device enters the gas-liquid separation tank V101 through the propylene carbonate tail gas pipe, the condensed liquid phase material is transferred to the crude cyclopropane condensate tank V201, the uncondensed gas phase is condensed by the precooler L101, and its condensate enters the crude cyclopropane condensate tank V201, the gas phase is compressed by the compressor C101 and enters the separation tank V102 after the compressor, and the condensate produced after compression enters the crude cyclopropane condensate tank V201 by self-pressure. The crude cyclopropane in the crude cyclopropane condensate tank V201 is transferred to the side line of the degassing tower T101 by starting the second feed pump P102, and the top temperature of the degassing tower is controlled to condense propylene oxide to the bottom of the tower. The components lighter than propylene oxide are connected to the first deep freezer L102 via the top of the tower for condensation, and the condensed liquid is sent to the first buffer tank E01. A mixture of propylene oxide and propylene carbonate is obtained in the bottom of the degassing tower T101, which is transferred to the cyclopropane distillation tower T102 for distillation via the third feed pump P103. The bottom and top temperatures of the tower are controlled, and qualified industrial-grade propylene oxide products are produced from the top of the tower, and a part of them are refluxed to the cyclopropane distillation tower T102. The bottom of the cyclopropane distillation tower T102 obtains crude propylene carbonate.

[0023] Example 2, reference Figure 2 The utility model mentions a propylene oxide recovery device in a propylene carbonate device, comprising a gas-liquid separator V101, a crude cyclopropane condensate tank V201, a precooler L101, a compressor C101, a separation tank V102, a degassing tower T101, a cyclopropane distillation tower T102, a first cryogenic cooler L102, a second cryogenic cooler L103, a first feed pump P101, a second feed pump P102, a third feed pump P103, a fourth feed pump P104, a fifth feed pump P105, a first buffer tank E01 and a second buffer tank E02, wherein the upper end of the gas-liquid separator V101 is connected to a propylene carbonate tail gas tank. pipe, the lower end of the gas-liquid separator V101 is connected to the crude cyclopropane condensate tank V201 through a pipeline, the lower end of the crude cyclopropane condensate tank V201 is connected to the side line of the degassing tower T101 through the second feed pump P102 and a pipeline, and the lower end of the degassing tower T101 is connected to the cyclopropane distillation tower T102 through the third feed pump P103 and a pipeline; the top of the gas-liquid separator V101 is connected to the precooler L101 through a pipeline, the side line of the precooler L101 is connected to the separation tank V102 through a pipeline and the compressor C101, and the lower end of the separation tank V102 is connected to the crude cyclopropane condensate tank V201 through a pipeline.

[0024] The difference from Example 1 is:

[0025] Among them, the upper end of the first buffer tank E01 is connected to the exhaust gas catalytic treatment system through a pipeline; the lower end of the second buffer tank E02 is connected to the side line of the cyclopropane distillation tower T102 through one pipeline, and the other line is sent out for storage through the fourth feed pump P104 to obtain an industrial-grade propylene oxide product, thereby realizing the recovery and reuse of propylene oxide; the bottom of the cyclopropane distillation tower T102 obtains crude propylene carbonate, and is sent out through the fifth feed pump P105.

[0026] The above is only a preferred embodiment of the utility model. Any person skilled in the art may modify the utility model by using the above technical solution or modify it into an equivalent technical solution. Therefore, any simple modification or equivalent transformation based on the technical solution of the utility model shall fall within the scope of protection claimed by the utility model.

Claims

1. A propylene oxide recovery device in a propylene carbonate device, characterized in that: The invention comprises a gas-liquid separator (V101), a crude cyclopropane condensate tank (V201), a precooler (L101), a compressor (C101), a separation tank (V102), a degassing tower (T101), a cyclopropane distillation tower (T102), a second feed pump (P102), a third feed pump (P103), a fourth feed pump (P104), and a fifth feed pump (P105), wherein the upper end of the gas-liquid separator (V101) is connected to a propylene carbonate tail gas pipe, and the lower end of the gas-liquid separator (V101) is connected to a crude cyclopropane condensate tank (V201) through a pipeline. The lower end of the condensate tank (V201) is connected to the side line of the degassing tower (T101) through a second feed pump (P102) and a pipeline, and the lower end of the degassing tower (T101) is connected to the cyclopropane distillation tower (T102) through a third feed pump (P103) and a pipeline; the top of the gas-liquid separator (V101) is connected to the precooler (L101) through a pipeline, the side line of the precooler (L101) is connected to the separation tank (V102) through a pipeline and a compressor (C101), and the lower end of the separation tank (V102) is connected to the crude cyclopropane condensate tank (V201) through a pipeline.

2. The propylene oxide recovery device in the propylene carbonate device according to claim 1, characterized in that: The lower end of the gas-liquid separator (V101) is connected to the crude cyclopropane condensate tank (V201) through a pipeline and a first feed pump (P101).

3. The propylene oxide recovery device in the propylene carbonate device according to claim 1 or 2, characterized in that: The lower end of the precooler (L101) is connected to the crude cyclopropane condensate tank (V201) through a pipeline.

4. The propylene oxide recovery device in the propylene carbonate device according to claim 3, characterized in that: The upper end of the degassing tower (T101) is connected to the first cryogenic cooler (L102) through a pipeline, and the output end of the first cryogenic cooler (L102) is connected to the first buffer tank (E01).

5. The propylene oxide recovery device in the propylene carbonate device according to claim 4, characterized in that: The upper end of the cyclopropane distillation tower (T102) is connected to the second cryogenic cooler (L103) through a pipeline, and the output end of the second cryogenic cooler (L103) is connected to the second buffer tank (E02).

6. The propylene oxide recovery device in the propylene carbonate device according to claim 5, characterized in that: The lower end of the second buffer tank (E02) is connected to the side line of the cyclopropane distillation tower (T102) through one pipeline and the other pipeline is used for external delivery.

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