CN216320045U - Propylene and propane separation system - Google Patents
Propylene and propane separation system Download PDFInfo
- Publication number
- CN216320045U CN216320045U CN202122529308.3U CN202122529308U CN216320045U CN 216320045 U CN216320045 U CN 216320045U CN 202122529308 U CN202122529308 U CN 202122529308U CN 216320045 U CN216320045 U CN 216320045U
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- China
- Prior art keywords
- tower
- buffer tank
- propane
- inlet
- propylene
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
- C07C11/06—Propene
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C9/00—Aliphatic saturated hydrocarbons
- C07C9/02—Aliphatic saturated hydrocarbons with one to four carbon atoms
- C07C9/08—Propane
Abstract
The utility model discloses a propylene and propane separation system, which comprises a propane-propylene rectifying tower, a tower kettle material buffer tank, a tower kettle-tower top material heat exchanger, a heat pump compressor and a compressor inlet buffer tank, wherein the tower kettle is connected with a tower top material heat exchanger; a tower bottom material line of the propane-propylene rectifying tower is connected with an inlet of a tower kettle material buffer tank; the gas phase line of the tower kettle material buffer tank is connected with the inlet of the compressor inlet buffer tank; the liquid phase outlet line of the tower kettle material buffer tank is connected with the cold flow inlet of the tower kettle-tower top material heat exchanger; a cold flow outlet line of the tower kettle-tower top material heat exchanger is connected with a tower kettle material buffer tank; a gas phase line at the top of the propane-propylene rectifying tower is connected with a heat flow inlet of a tower kettle-tower top material heat exchanger; the gas phase line at the outlet of the inlet buffer tank of the compressor is connected with the inlet of the heat pump compressor; the outlet gas phase line of the heat pump compressor is connected to the bottom of the propylene-propane tower. The system can effectively recycle the heat carried by the material at the top of the tower, and greatly reduces the separation energy consumption of the propane-propylene rectifying tower.
Description
Technical Field
The utility model relates to the field of compound separation devices, in particular to a propylene and propane separation system.
Background
Propylene is an intermediate with wide application in the chemical production process, is one of the basic raw materials of three synthetic materials (plastics, synthetic rubber and synthetic fibers), and is mainly used for producing polypropylene, acrylonitrile, isopropanol, acetone, propylene oxide and the like. Propylene is derived primarily from the by-products of petroleum cracking ethylene plants, often mixed with hydrogen, ethylene, ethane, and propane, among others. In the propylene refining process, the propylene can be well separated from lighter components such as hydrogen, ethane, ethylene and the like through conventional rectification, and the relative volatility of propylene and propane is close to 1, so that the propylene and the propane belong to components which are difficult to separate. In order to meet the requirement that the purity of the propylene is more than or equal to 99.6 percent (mole fraction), more tower plates are needed in the propylene tower, so the propylene tower generally adopts series-connected towers, the number of the tower plates is about 200, the conventional rectification method needs higher reflux ratio and consumes a large amount of energy. At present, researchers propose a pressure swing adsorption method, a vacuum swing adsorption method and the like which can achieve the effect of reducing energy consumption theoretically, but the material development, the production capacity and the operation time are all limited in the actual production. Therefore, conventional rectification remains the first choice for the separation of propane-propylene in large quantities industrially.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a propylene and propane separation system with lower energy consumption.
In order to achieve the purpose, the utility model adopts the following technical scheme: a propylene and propane separation system comprises a propane-propylene rectifying tower, a tower kettle material buffer tank, a tower kettle-tower top material heat exchanger, a heat pump compressor and a compressor inlet buffer tank;
a tower bottom material line of the propane-propylene rectifying tower is connected with an inlet of a tower kettle material buffer tank;
the gas phase line of the tower kettle material buffer tank is connected with the inlet of the compressor inlet buffer tank;
the liquid phase outlet line of the tower kettle material buffer tank is connected with the cold flow inlet of the tower kettle-tower top material heat exchanger;
a cold flow outlet line of the tower kettle-tower top material heat exchanger is connected with a tower kettle material buffer tank;
a gas phase line at the top of the propane-propylene rectifying tower is connected with a heat flow inlet of a tower kettle-tower top material heat exchanger;
the gas phase line at the outlet of the inlet buffer tank of the compressor is connected with the inlet of the heat pump compressor;
the outlet gas phase line of the heat pump compressor is connected to the bottom of the propylene-propane tower.
Further, a heat flow outlet of the tower kettle-tower top material heat exchanger is connected with an inlet of a tower reflux tank.
By applying the technical scheme of the utility model, the utility model has the following beneficial effects: the separation system reduces the pressure of the tower kettle material buffer tank through the compressor, the tower kettle material automatically flows into the tower kettle material buffer tank, liquid propane in the buffer tank is vaporized due to the reduction of the pressure, the vaporized propane takes away heat, and the liquid phase temperature in the buffer tank is reduced. At the moment, the temperature of the liquid phase in the buffer tank is lower than the temperature of the gas-phase material at the top of the tower, the heat of the gas-phase material at the top of the tower is taken away by the heat exchange between the low-temperature liquid phase in the buffer tank and the gas-phase material at the top of the tower, and the liquid phase is vaporized and returned to the material buffer tank at the bottom of the tower. The gas phase vaporized by the tower kettle material buffer tank firstly enters the compressor inlet buffer tank, and then returns to the tower kettle after being pressurized by the compressor, so as to heat the tower kettle material. The gas phase material at the top of the tower enters a reflux tank at the top of the tower after being condensed and then flows back to the tower through the top of the tower. By the process and the equipment, the heat at the top of the propylene-propane separation tower is recovered and is used for heating the tower kettle material; therefore, by increasing a small amount of power consumption of the compressor, the energy consumption of the propylene-propane separation tower is greatly saved, and the energy conservation of the device is realized.
Drawings
FIG. 1 is a schematic diagram of the system of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, but the technical solutions do not limit the scope of the present invention.
Referring to fig. 1, a propylene and propane separation system comprises a propane-propylene rectification column a, a column bottom material buffer tank V1, a column bottom-column top material heat exchanger E1, a heat pump compressor C1, and a compressor inlet buffer tank V2;
a bottom material line 1 of a propane-propylene rectifying tower A is connected with an inlet of a material buffer tank V1 at the bottom of the tower;
the gas phase line 2 of the tower bottom material buffer tank V1 is connected with the inlet of a compressor inlet buffer tank V2;
a liquid phase outlet line 3 of the tower kettle material buffer tank V1 is connected with a cold flow inlet of a tower kettle-tower top material heat exchanger E1;
a cold flow outlet line 4 of the tower kettle-tower top material heat exchanger E1 is connected with a tower kettle material buffer tank V1;
the gas phase line 5 at the top of the propane-propylene rectifying tower A is connected with a heat flow inlet of a tower kettle-top material heat exchanger E1;
the outlet gas phase line 7 of the compressor inlet buffer tank V2 is connected with the inlet of the heat pump compressor C1;
a gas phase line 8 at the outlet of the heat pump compressor C1 is connected to the tower kettle of the propylene-propane tower;
the heat flow outlet 6 of the tower kettle-tower top material heat exchanger E1 is connected with the inlet of the tower reflux tank.
Specifically, the liquid-phase material in the tower bottom automatically flows into a material buffer tank V1 in the tower bottom, the pressure of the material buffer tank in the tower bottom is reduced by a heat pump compressor C1, and the liquid propane in the buffer tank is vaporized due to the pressure reduction. The vaporized propane takes away heat and reduces the liquid phase temperature in the buffer tank. At the moment, the liquid phase temperature in the buffer tank is lower than the gas phase material temperature at the top of the tower. The low-temperature liquid phase in the buffer tank exchanges heat with the gas-phase material at the top of the propane-propylene rectifying tower through a heat exchanger E1, the gas-phase heat at the top of the tower is taken away and vaporized, the vaporized propane gas phase returns to the material buffer tank V1 at the bottom of the tower, and the gas phase at the top of the tower enters a reflux tank of the propylene-propylene rectifying tower after being cooled and liquefied and then flows back to the tower through the top of the tower.
The gas phase vaporized by the V1 in the tower bottom material buffer tank firstly enters the inlet buffer tank V2 of the heat pump compressor, and returns to the tower bottom after being pressurized by the heat pump compressor C1 to heat the tower bottom material.
In conclusion, the propylene and propane separation system is not only suitable for a propane-propylene separation system, but also suitable for a system with similar boiling point and larger energy consumption in common rectification separation; meanwhile, the system effectively recycles the heat carried by the tower top material, reduces the steam consumption of the propane-propylene rectifying tower and greatly reduces the separation energy consumption of the propane-propylene rectifying tower by additionally arranging the tower bottom material buffer tank, the tower bottom-tower top material heat exchanger, the heat pump compressor and the compressor inlet buffer tank.
While the foregoing is directed to the preferred embodiment of the present invention, it will be understood by those skilled in the art that various changes and modifications may be made without departing from the spirit and scope of the utility model.
Claims (2)
1. A propylene and propane separation system characterized by: comprises a propane-propylene rectifying tower (A), a tower bottom material buffer tank (V1), a tower bottom-tower top material heat exchanger (E1), a heat pump compressor (C1) and a compressor inlet buffer tank (V2);
a bottom material line (1) of the propane-propylene rectifying tower (A) is connected with an inlet of a material buffer tank (V1) at the bottom of the tower;
the gas phase line (2) of the tower bottom material buffer tank (V1) is connected with the inlet of a compressor inlet buffer tank (V2);
a liquid phase outlet line (3) of the tower kettle material buffer tank (V1) is connected with a cold flow inlet of a tower kettle-tower top material heat exchanger (E1);
a cold flow outlet line (4) of the tower kettle-tower top material heat exchanger (E1) is connected with a tower kettle material buffer tank (V1);
the gas phase line (5) at the top of the propane-propylene rectifying tower (A) is connected with a heat flow inlet of a tower kettle-top material heat exchanger (E1);
the outlet gas phase line (7) of the compressor inlet buffer tank (V2) is connected with the inlet of the heat pump compressor (C1);
the outlet gas phase line (8) of the heat pump compressor (C1) is connected to the bottom of the propylene-propane tower.
2. A propylene and propane separation system as recited in claim 1, wherein: a heat flow outlet (6) of the tower kettle-tower top material heat exchanger (E1) is connected with an inlet of a tower reflux tank.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122529308.3U CN216320045U (en) | 2021-10-20 | 2021-10-20 | Propylene and propane separation system |
| PCT/CN2021/131076 WO2023065443A1 (en) | 2021-10-20 | 2022-07-08 | Propylene-propane separation system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122529308.3U CN216320045U (en) | 2021-10-20 | 2021-10-20 | Propylene and propane separation system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN216320045U true CN216320045U (en) | 2022-04-19 |
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ID=81177614
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202122529308.3U Active CN216320045U (en) | 2021-10-20 | 2021-10-20 | Propylene and propane separation system |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN216320045U (en) |
| WO (1) | WO2023065443A1 (en) |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7875758B2 (en) * | 2007-01-08 | 2011-01-25 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes George Claude | Systems and methods for the separation of propylene and propane |
| CN204601653U (en) * | 2015-01-20 | 2015-09-02 | 苏州天荣能源环境科技有限公司 | A kind of enclosed heat pump rectification system being applicable to the large temperature difference |
| CN204589029U (en) * | 2015-04-15 | 2015-08-26 | 山东齐鲁石化工程有限公司 | Separation of olefins thermal-pump unit |
| CN109715258A (en) * | 2016-09-07 | 2019-05-03 | 沙特基础全球技术有限公司 | System and method for separating propylene and propane |
| CN110105216B (en) * | 2019-04-12 | 2024-02-27 | 天津乐科节能科技有限公司 | Self-backheating rectification method and device |
| CN210495280U (en) * | 2019-06-26 | 2020-05-12 | 山东齐旺达石油化工有限公司 | Heat pump rectification separation system of butane raw materials in ethylene preparation process |
| CN111302922A (en) * | 2020-03-27 | 2020-06-19 | 北京诺维新材科技有限公司 | Rectification separation method and rectification system |
| CN111467825A (en) * | 2020-05-22 | 2020-07-31 | 浙江奇彩环境科技股份有限公司 | Rectification tower tail gas self-recycling system with high-temperature booster compressor |
-
2021
- 2021-10-20 CN CN202122529308.3U patent/CN216320045U/en active Active
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2022
- 2022-07-08 WO PCT/CN2021/131076 patent/WO2023065443A1/en unknown
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| Publication number | Publication date |
|---|---|
| WO2023065443A1 (en) | 2023-04-27 |
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