CN116440522A - Separation and purification system and method for separating and purifying crude cumene product - Google Patents
Separation and purification system and method for separating and purifying crude cumene product Download PDFInfo
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- CN116440522A CN116440522A CN202310309993.XA CN202310309993A CN116440522A CN 116440522 A CN116440522 A CN 116440522A CN 202310309993 A CN202310309993 A CN 202310309993A CN 116440522 A CN116440522 A CN 116440522A
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- RWGFKTVRMDUZSP-UHFFFAOYSA-N cumene Chemical compound CC(C)C1=CC=CC=C1 RWGFKTVRMDUZSP-UHFFFAOYSA-N 0.000 title claims abstract description 132
- 238000000746 purification Methods 0.000 title claims abstract description 41
- 238000000926 separation method Methods 0.000 title claims abstract description 39
- 238000000034 method Methods 0.000 title claims abstract description 32
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 90
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 claims description 58
- ODLMAHJVESYWTB-UHFFFAOYSA-N propylbenzene Chemical compound CCCC1=CC=CC=C1 ODLMAHJVESYWTB-UHFFFAOYSA-N 0.000 claims description 52
- YWAKXRMUMFPDSH-UHFFFAOYSA-N pentene Chemical compound CCCC=C YWAKXRMUMFPDSH-UHFFFAOYSA-N 0.000 claims description 24
- 238000011084 recovery Methods 0.000 abstract description 10
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 239000000047 product Substances 0.000 description 96
- 239000012535 impurity Substances 0.000 description 29
- 238000009835 boiling Methods 0.000 description 27
- 238000010992 reflux Methods 0.000 description 20
- 238000007599 discharging Methods 0.000 description 9
- 239000007788 liquid Substances 0.000 description 6
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 3
- 239000012043 crude product Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000004817 gas chromatography Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 229920000515 polycarbonate Polymers 0.000 description 2
- 239000004417 polycarbonate Substances 0.000 description 2
- 239000003377 acid catalyst Substances 0.000 description 1
- 229940106691 bisphenol a Drugs 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000011027 product recovery Methods 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
Classifications
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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
-
- 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
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/146—Multiple effect distillation
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention belongs to the technical field of separation and purification, and particularly relates to a separation and purification system and a method for separating and purifying a crude cumene product. The separation and purification system provided by the invention comprises a first storage tank 6, a first rectifying tower 1, a second rectifying tower 2, a third rectifying tower 3, and a third rectifying tower 3, wherein the first rectifying tower inlet 1-1 is connected with an outlet of the first storage tank 6, the second rectifying tower inlet 2-1 is connected with an outlet 1-3 of the bottom of the first rectifying tower, and the third rectifying tower inlet 3-1 is connected with an outlet 2-3 of the bottom of the second rectifying tower; the device also comprises a second storage tank 7 connected with the top outlet 2-2 of the second rectifying tower, a third storage tank 8 connected with the outlet 2-4 of the second rectifying tower and a fourth storage tank 9 connected with the top outlet 3-2 of the third rectifying tower. The separation and purification system provided by the invention is used for separating and purifying the crude cumene product, so that the cumene product with higher purity and higher recovery rate can be obtained. The separation and purification method provided by the invention has simple steps and low energy consumption.
Description
Technical Field
The invention belongs to the technical field of separation and purification, and particularly relates to a separation and purification system and a method for separating and purifying a crude cumene product.
Background
Cumene is an important basic organic chemical raw material, mainly for the production of phenol and acetone for a wide range of applications, and the demand for phenol for the production of bisphenol-a and subsequent production of polycarbonate is increasing due to the widening applications of polycarbonate in the electronics, healthcare and automotive industries. And the requirements of industrial development on the purity of the isopropyl benzene are also higher, however, the product prepared by the existing method for preparing the isopropyl benzene contains more impurities. Therefore, the process route for separating and purifying the isopropyl benzene is improved, the purity of the isopropyl benzene is improved, and the method has important economic significance and strategic significance.
At present, benzene and propylene are reacted under the condition of complete liquid phase or gas-liquid mixed phase in the presence of an acid catalyst, and after the reaction is finished, the crude product of the prepared isopropylbenzene is separated and purified mainly by a batch rectifying tower in a sectional purification mode, but the recovery rate of the isopropylbenzene is very low and is generally 55 percent.
Disclosure of Invention
In view of the above, the invention provides a separation and purification system and a method for separating and purifying crude cumene, and the cumene obtained by the separation and purification method provided by the invention has higher purity and recovery rate.
In order to solve the technical problems, the invention provides a separation and purification system, which comprises a first storage tank 6, a first rectifying tower 1, a second rectifying tower 2, a third rectifying tower 3, and a third rectifying tower inlet 3-1, wherein the first rectifying tower inlet 1-1 is connected with an outlet of the first storage tank 6, the second rectifying tower inlet 2-1 is connected with an outlet 1-3 of the bottom of the first rectifying tower, and the third rectifying tower 3 is connected with an inlet 3-1 of the third rectifying tower and an outlet 2-3 of the bottom of the second rectifying tower;
the device also comprises a second storage tank 7 connected with the top outlet 2-2 of the second rectifying tower, a third storage tank 8 connected with the outlet 2-4 of the second rectifying tower and a fourth storage tank 9 connected with the top outlet 3-2 of the third rectifying tower.
Preferably, the separation and purification system further comprises a fourth rectifying tower 4, wherein the inlet 4-1 of the fourth rectifying tower is connected with the outlet 3-3 of the bottom of the third rectifying tower; a seventh storage tank 11 connected with the top outlet 4-2 of the fourth rectifying tower, and an eighth storage tank 10 connected with the bottom outlet 4-3 of the fourth rectifying tower.
Preferably, the inner diameter of the fourth rectifying tower 4 is 200-800 mm, the fourth rectifying tower 4 is a plate tower or a packed tower, and when the fourth rectifying tower 4 is a plate tower, the number of plates is 30-70.
Preferably, the separation and purification system further comprises a fifth rectifying tower 5 with a fifth rectifying tower inlet 5-1 connected with the first rectifying tower top outlet 1-2, a fifth storage tank 12 connected with the fifth rectifying tower top outlet 5-2, and a sixth storage tank 13 connected with the fifth rectifying tower bottom outlet 5-3.
Preferably, the inner diameter of the fifth rectifying tower 5 is 300-1000 mm, the fifth rectifying tower 5 comprises a plate tower or a packed tower, and when the fifth rectifying tower 5 is a plate tower, the number of the plates is 10-40.
The invention also provides a method for separating and purifying the crude cumene product by using the separation and purification system, which comprises the following steps:
the crude cumene product stored in the first storage tank 6 is conveyed to a first rectifying tower 1 for primary rectification, and a first tower bottom product is obtained;
delivering the first tower bottom product to a second rectifying tower 2 for secondary rectification, obtaining a second tower bottom product at the tower bottom, obtaining benzene at the tower top, obtaining ethylbenzene at the side line, wherein the benzene is stored in a second storage tank 7, and the ethylbenzene is stored in a third storage tank 8;
and conveying the second tower bottom product to a third rectifying tower 3 for three-stage rectification, obtaining a third tower bottom product at the tower bottom, and obtaining a pure isopropyl benzene product at the tower top, wherein the pure isopropyl benzene product is stored in a fourth storage tank 9.
Preferably, the pressure of the primary rectification is 0.01-0.15 MPa, the temperature of the top of the first rectification column 1 is 53-89 ℃, and the temperature of the bottom of the first rectification column 1 is 122-145 ℃.
Preferably, the pressure of the secondary rectification is 0.01-0.05 MPa, the temperature of the top of the second rectification column 2 is 45-119 ℃, and the temperature of the bottom of the second rectification column 2 is 105-132 ℃.
Preferably, the pressure of the three-stage rectification is 0.01-0.05 MPa, the temperature of the top of the third rectification column 3 is 78-132 ℃, and the temperature of the bottom of the third rectification column 3 is 105-152 ℃.
Preferably, the method further comprises: conveying the third tower bottom product to a fourth rectifying tower 4 for fourth rectification, obtaining n-propylbenzene at the tower top and obtaining a fourth tower bottom product at the tower bottom; the n-propylbenzene is stored in the seventh tank 11 and the fourth bottom product is stored in the eighth tank 10;
the primary rectification further obtains a first tower top product, the first tower top product is conveyed to a fifth rectification tower 5 to carry out fifth rectification, n-pentene is obtained at the bottom of the tower, and the n-pentene is stored in a sixth storage tank 13.
The invention provides a separation and purification system, which comprises a first storage tank 6, a first rectifying tower 1, a second rectifying tower 2, a third rectifying tower 3, and a third rectifying tower inlet 3-1, wherein the first rectifying tower inlet 1-1 is connected with an outlet of the first storage tank 6, the second rectifying tower inlet 2-1 is connected with an outlet of the bottom of the first rectifying tower 1-3, and the third rectifying tower 3 is connected with an inlet of the third rectifying tower 3-1 and an outlet of the bottom of the second rectifying tower 2-3; the device also comprises a second storage tank 7 connected with the top outlet 2-2 of the second rectifying tower, a third storage tank 8 connected with the outlet 2-4 of the second rectifying tower and a fourth storage tank 9 connected with the top outlet 3-2 of the third rectifying tower. The separation and purification system provided by the invention is used for separating and purifying the crude cumene product, so that components in the crude product can be separated one by one to obtain cumene with higher purity and higher recovery rate, and the obtained pure cumene product has the purity of 99.992-99.994% and the recovery rate of 99.88-99.91% according to the results of the examples. The separation and purification method provided by the invention has the advantages of simple steps, low cost and low energy consumption.
Drawings
FIG. 1 is a schematic diagram of a separation and purification system provided by the invention, wherein 1 is a first rectifying tower, 1-1 is a first rectifying tower inlet, 1-3 is a first rectifying tower bottom outlet, 2 is a second rectifying tower, 2-1 is a second rectifying tower inlet, 2-2 is a first rectifying tower top outlet, 2-3 is a first rectifying tower bottom outlet, 2-4 is a second rectifying tower middle outlet, 3 is a third rectifying tower, 3-1 is a third rectifying tower inlet, 3-2 is a third rectifying tower top outlet, 6 is a first storage tank, 7 is a second storage tank, 8 is a third storage tank, and 9 is a fourth storage tank;
FIG. 2 is a schematic diagram showing the structure of a separation and purification system employed in separation and purification according to an embodiment, wherein 1 is a first rectifying column, 1-1 is a first rectifying column inlet, 1-2 is a first rectifying column top outlet, 1-3 is a first rectifying column bottom outlet, 2 is a second rectifying column, 2-1 is a second rectifying column inlet, 2-2 is a first rectifying column top outlet, 2-3 is a first rectifying column bottom outlet, 2-4 is a second rectifying column middle outlet, 3 is a third rectifying column, 3-1 is a third rectifying column inlet, 3-2 is a third rectifying column top outlet, 3-3 is a third rectifying column bottom outlet, 4 is a fourth rectifying column, 4-1 is a fourth rectifying column inlet, 4-2 is a fourth rectifying tower top outlet, 4-3 is a fourth rectifying tower bottom outlet, 5 is a fifth rectifying tower, 5-1 is a fourth rectifying tower inlet, 5-2 is a fourth rectifying tower top outlet, 5-3 is a fourth rectifying tower bottom outlet, 6 is a first storage tank, 7 is a second storage tank, 8 is a third storage tank, 9 is a fourth storage tank, 10 is an eighth storage tank, 11 is a seventh storage tank, 12 is a fifth storage tank, 13 is a sixth storage tank, 14 is a first conveying pump, 15 is a second conveying pump, 16 is a third conveying pump, 17 is a fourth conveying pump, 18 is a third condenser, 19 is a fourth condenser, 20 is a fifth condenser, 21 is a sixth condenser, 22 is a first condenser, and 23 is a second condenser.
Detailed Description
The invention provides a separation and purification system, which comprises a first storage tank 6, a first rectifying tower 1, a second rectifying tower 2, a third rectifying tower 3, and a third rectifying tower inlet 3-1, wherein the first rectifying tower inlet 1-1 is connected with an outlet of the first storage tank 6, the second rectifying tower inlet 2-1 is connected with an outlet of the bottom of the first rectifying tower 1-3, and the third rectifying tower 3 is connected with an inlet of the third rectifying tower 3-1 and an outlet of the bottom of the second rectifying tower 2-3;
the device also comprises a second storage tank 7 connected with the top outlet 2-2 of the second rectifying tower, a third storage tank 8 connected with the outlet 2-4 of the second rectifying tower and a fourth storage tank 9 connected with the top outlet 3-2 of the third rectifying tower.
The separation and purification system provided by the invention comprises a first storage tank 6. As an embodiment of the present invention, the outlet of the first storage tank 6 is connected to the inlet 1-1 of the first rectifying tower through a first transfer pump 14.
The separation and purification system provided by the invention comprises a first rectifying tower 1, wherein the inlet 1-1 of the first rectifying tower is connected with the outlet of a first storage tank 6. The first rectifying column inlet 1-1 is located in the first rectifying column 1 as an embodiment of the present invention. In the present invention, the first rectifying column 1 is preferably a tray column or a packed column, more preferably a tray column, and the tray column is preferably a sieve tray column; when the first rectifying column 1 is a tray column, the tray number of the first rectifying column 1 is preferably 10 to 30, more preferably 15 to 25, still more preferably 16 to 24; the inlet 1-1 of the first rectifying tower is preferably positioned at the 6 th to 15 th tower plates in sequence from top to bottom, more preferably at the 8 th to 12 th tower plates. In the present invention, the inside diameter of the first rectifying column 1 is preferably 300 to 1000mm, more preferably 400 to 800mm, and still more preferably 500 to 700mm.
As an embodiment of the present invention, the first rectifying tower top outlet 1-2 is connected with the fifth rectifying tower inlet 5-1 of the fifth rectifying tower 5, and a first condenser 22 is connected between the first rectifying tower top outlet 1-2 and the fifth rectifying tower inlet 5-1. A fifth storage tank 12 is connected to the fifth rectifying tower top outlet 5-2 as an embodiment of the present invention, and a second condenser 23 is connected between the fifth rectifying tower top outlet 5-2 and the fifth storage tank 12. A sixth storage tank 13 is connected to the bottom outlet 5-3 of the fifth rectifying tower as an embodiment of the present invention. In the present invention, the fifth rectifying column 5 is preferably a tray column or a packed column, more preferably a tray column, and the tray column is preferably a sieve column; when the fifth rectifying column 5 is a tray column, the tray number of the fifth rectifying column 5 is preferably 10 to 40, more preferably 15 to 35, still more preferably 20 to 25; the fifth rectifying tower inlet 5-1 is preferably positioned at the 5 th to 15 th tower plates in sequence from top to bottom, more preferably at the 8 th to 12 th tower plates. In the present invention, the inside diameter of the fifth rectifying column 5 is preferably 300 to 1000mm, more preferably 400 to 800mm, and still more preferably 500 to 700mm.
The separation and purification system provided by the invention comprises a second rectifying tower 2, wherein the inlet 2-1 of the second rectifying tower is connected with the outlet 1-3 of the bottom of the first rectifying tower. The second rectifying column inlet 2-1 is located in the second rectifying column 2 as an embodiment of the present invention. As an embodiment of the present invention, a second delivery pump 15 is connected between the inlet 2-1 of the second rectifying tower and the outlet 1-3 of the bottom of the first rectifying tower. The second rectifying tower top outlet 2-2 is connected with a second storage tank 7 as an embodiment of the invention, and a third condenser 18 is connected between the second rectifying tower top outlet 2-2 and the second storage tank 7. As an embodiment of the invention, the outlet 2-4 of the second rectifying tower is connected with a third storage tank 8, and a fourth condenser 19 is connected between the outlet 2-4 of the second rectifying tower and the third storage tank 8. In the present invention, the second rectifying column 2 is preferably a tray column or a packed column, more preferably a tray column, and the tray column is preferably a sieve tray column; when the second rectifying column 2 is a tray column, the tray number of the second rectifying column 2 is preferably 80 to 110, more preferably 90 to 105, still more preferably 95 to 102; the inlet 2-1 of the second rectifying tower is preferably positioned at 55-65 trays, more preferably 57-62 trays, in sequence from top to bottom. In the present invention, the second rectifying column 2 preferably has a column inner diameter of 1000 to 2000mm, more preferably 1200 to 1800mm, and still more preferably 1300 to 1500mm.
The separation and purification system provided by the invention further comprises a third rectifying tower 3, wherein the inlet 3-1 of the third rectifying tower is connected with the outlet 2-3 of the bottom of the second rectifying tower. The third rectifying column inlet 3-1 is located in the third rectifying column 2 as an embodiment of the present invention. As an embodiment of the present invention, a third delivery pump 16 is connected between the third rectifying tower inlet 3-1 and the second rectifying tower bottom outlet 2-3. A fourth storage tank 9 is connected to the third rectifying tower top outlet 3-2 as an embodiment of the present invention, and a fifth condenser 20 is connected between the third rectifying tower top outlet 3-2 and the fourth storage tank 9. In the present invention, the third rectifying column 3 is preferably a tray column or a packed column, more preferably a tray column, and the tray column is preferably a sieve tray column; when the third rectifying column 3 is a tray column, the tray number of the third rectifying column 3 is preferably 60 to 100, more preferably 70 to 90, still more preferably 75 to 85; the third rectifying tower inlet 3-1 is preferably positioned at the 37 th to 48 th tower plates in sequence from top to bottom, and more preferably at the 38 th to 45 th tower plates. In the present invention, the inside diameter of the third rectifying column 3 is preferably 1000 to 2000mm, more preferably 1200 to 1800mm, and still more preferably 1400 to 1600mm.
As an embodiment of the invention, the bottom outlet 3-3 of the third rectifying tower is connected with a fourth rectifying tower 4, and a fourth delivery pump 17 is connected between the bottom outlet 3-3 of the third rectifying tower and the fourth rectifying tower inlet 4-1; the fourth rectifying tower inlet 4-1 is positioned in the tower. As an embodiment of the present invention, the fourth rectifying tower top outlet 4-2 is connected to a seventh storage tank 11, and a sixth condenser 21 is connected between the fourth rectifying tower top outlet 4-2 and the seventh storage tank 11. An eighth storage tank 10 is connected to the bottom outlet 4-3 of the fourth rectifying tower as an embodiment of the present invention. In the present invention, the fourth rectifying column 4 is preferably a tray column or a packed column, more preferably a tray column, and the tray column is preferably a sieve column; when the fourth rectifying column 4 is a tray column, the tray number of the fourth rectifying column 4 is preferably 30 to 70, more preferably 40 to 60, still more preferably 45 to 55; the fourth rectifying tower inlet 4-1 is preferably positioned at the 20 th to 30 th trays, more preferably at the 22 nd to 27 th trays, which are arranged in sequence from top to bottom. In the present invention, the inside diameter of the fourth rectifying column 4 is preferably 200 to 800mm, more preferably 300 to 700mm, and even more preferably 400 to 600mm.
The invention also provides a method for separating and purifying the crude cumene product by using the separation and purification system, which comprises the following steps:
the crude cumene product stored in the first storage tank 6 is conveyed to a first rectifying tower 1 for primary rectification, and a first tower bottom product is obtained;
delivering the first tower bottom product to a second rectifying tower 2 for secondary rectification, obtaining a second tower bottom product at the tower bottom, obtaining benzene at the tower top, obtaining ethylbenzene at the side line, wherein the benzene is stored in a second storage tank 7, and the ethylbenzene is stored in a third storage tank 8;
and conveying the second tower bottom product to a third rectifying tower 3 for three-stage rectification, obtaining a third tower bottom product at the tower bottom, and obtaining a pure isopropyl benzene product at the tower top, wherein the pure isopropyl benzene product is stored in a fourth storage tank 9.
The method comprises the step of conveying the crude cumene product stored in the first storage tank 6 to the first rectifying tower 1 for primary rectification to obtain a first bottom product. In the invention, the crude cumene product preferably comprises the following components in percentage by mass: 2 to 4 weight percent of high-low boiling impurities, 2 to 4 weight percent of n-pentene, 3 to 6 weight percent of ethylbenzene, 4 to 8 weight percent of n-propylbenzene, 34 to 36 weight percent of benzene, 47 to 50 weight percent of isopropyl benzene, more preferably 2 to 3 weight percent of high-low boiling impurities, 2 to 3 weight percent of n-pentene, 3 to 4 weight percent of ethylbenzene, 6 to 8 weight percent of n-propylbenzene, 35 to 36 weight percent of benzene and 47 to 48 weight percent of isopropyl benzene. In the present invention, the crude cumene is preferably liquid, preferably obtained from a process for producing a phenol feedstock. The invention preferably utilizes the first delivery pump 14 to deliver the crude cumene product from the first rectification column inlet 1-1 to the first rectification column 1. In the present invention, the temperature of the crude cumene is preferably 23 to 27 ℃, more preferably 25 ℃. In the present invention, the feeding pressure of the feeding is preferably 0.2MPa, and the feeding flow rate of the feeding is preferably 1000 to 5000kg/h, more preferably 1000 to 3500kg/h, still more preferably 1500 to 2500kg/h. In the present invention, the pressure of the primary rectification is preferably 0.01 to 0.15MPa, more preferably 0.07 to 0.1MPa. In the present invention, the reflux ratio of the primary rectification is preferably 1 to 7, more preferably 1 to 3, and still more preferably 1 to 2. In the present invention, the top temperature of the first rectifying column 1 is preferably 53 to 89 ℃, and the bottom temperature of the first rectifying column 1 is preferably 122 to 145 ℃.
In the invention, the primary rectification preferably also obtains a first tower top product, and the first tower top product is a crude product of n-pentene. The first tower top product is preferably conveyed to the fifth rectifying tower 5 through a fifth rectifying tower inlet 5-1 for fifth rectification, n-pentene is obtained from the tower bottom, a fifth tower top product is obtained from the tower top, and the n-pentene is stored in a sixth storage tank 13. The present invention preferably condenses the overhead product of the first rectification prior to delivery via a first condenser 22; the condensation is used to reduce the temperature of the stream to a temperature close to the fifth rectifying column feed plate temperature. In the present invention, the pressure of the fifth rectification is preferably 0.01 to 0.15MPa, more preferably 0.07 to 0.1MPa. In the present invention, the reflux ratio of the fifth rectification is preferably 1 to 4, more preferably 3 to 4, and still more preferably 3.2 to 3.5. In the present invention, the top temperature of the fifth rectifying column 5 is preferably 25 to 56 ℃, and the bottom temperature of the fifth rectifying column 5 is preferably 32 to 78 ℃. In the present invention, the fifth overhead product is a low boiling impurity, preferably stored in fifth storage tank 12. The present invention preferably utilizes a second condenser 23 for condensing the fifth overhead product before it is sent to the fifth storage tank.
After the first tower bottom product is obtained, the first tower bottom product is conveyed to a second rectifying tower 2 for secondary rectification, the second tower bottom product is obtained from the tower bottom, benzene is obtained from the tower top, ethylbenzene is obtained from the side line, the benzene is stored in a second storage tank 7, and the ethylbenzene is stored in a third storage tank 8. The present invention preferably utilizes a second transfer pump 15 to transfer the first bottoms product from the second rectifying column inlet 2-1 to the second rectifying column. In the present invention, the pressure of the secondary rectification is preferably 0.01 to 0.05MPa, more preferably 0.011 to 0.014MPa. In the present invention, the reflux ratio of the secondary rectification is preferably 3 to 6, more preferably 4 to 6, and even more preferably 4.5 to 5. In the present invention, the top temperature of the second rectifying column 2 is preferably 45 to 119 ℃, and the bottom temperature of the second rectifying column 2 is preferably 105 to 132 ℃. In the invention, the benzene is discharged from the top outlet 2-2 of the second rectifying tower, condensed by a third condenser 18 and stored in a second storage tank 7. In the present invention, the ethylbenzene is discharged from the outlets 2 to 4 of the second rectifying column, condensed by the fourth condenser 19, and stored in the third storage tank 8.
After the second tower bottom product is obtained, the second tower bottom product is conveyed to a third rectifying tower 3 for three-stage rectification, the third tower bottom product is obtained at the tower bottom, the isopropyl benzene pure product is obtained at the tower top, and the isopropyl benzene pure product is stored in a fourth storage tank 9. The present invention preferably utilizes a third transfer pump 16 to transfer the second bottoms product from the third rectifying column inlet 3-1 to the third rectifying column. In the present invention, the pressure of the three-stage rectification is preferably 0.01 to 0.05MPa, more preferably 0.011 to 0.014MPa. In the present invention, the reflux ratio of the three-stage rectification is preferably 2 to 5, more preferably 3 to 5, and still more preferably 3.2 to 4. In the present invention, the top temperature of the third rectifying column 3 is preferably 78 to 132 ℃, and the bottom temperature of the third rectifying column 3 is preferably 105 to 152 ℃. In the invention, the cumene is discharged from the top outlet 3-2 of the third rectifying tower, condensed by a fifth condenser 20 and stored in a fourth storage tank 9.
After obtaining a third tower bottom product, the third tower bottom product is preferably conveyed to a fourth rectifying tower 4 for fourth rectification, n-propylbenzene is obtained at the tower top, and a fourth tower bottom product is obtained at the tower bottom; the n-propylbenzene is stored in the seventh tank 11 and the fourth bottom product is stored in the eighth tank 10. The present invention preferably utilizes a fourth transfer pump 17 to transfer the third bottoms product from the fourth rectifying column inlet 4-1 to the fourth rectifying column. In the present invention, the pressure of the four-stage rectification is preferably 0.01 to 0.05MPa, more preferably 0.011 to 0.014MPa. In the present invention, the reflux ratio of the four-stage rectification is preferably 2 to 4, more preferably 3 to 4, and still more preferably 3 to 3.3. In the present invention, the top temperature of the fourth rectifying column 4 is preferably 78 to 132 ℃, and the bottom temperature of the fourth rectifying column 4 is preferably 132 to 168 ℃. In the invention, the n-propylbenzene is discharged from the top outlet 4-2 of the fourth rectifying tower, condensed by the sixth condenser 21 and stored in the seventh storage tank 11. In the present invention, the fourth bottom product is a high boiling impurity.
The separation and purification method provided by the invention has simple steps, high purification efficiency of the isopropyl benzene, impurity content not higher than 50ppm, recovery rate of the isopropyl benzene more than 99.9wt% and purity of the isopropyl benzene more than 99.99 wt%.
Fig. 2 is a schematic structural diagram of a separation and purification system used in separation and purification in an embodiment, the crude cumene product is stored in a first storage tank 6, and the crude cumene product is conveyed to a first rectifying tower 1 for primary rectification through a first conveying pump 14, so as to obtain a first top product and a first bottom product; condensing the first tower top product through a first condenser 22 from a first rectifying tower top outlet 1-2, then entering a fifth rectifying tower 5 through a fifth rectifying tower inlet 5-1 for fifth rectification to obtain low-boiling impurities and n-pentene, condensing the low-boiling impurities through a second condenser 23, storing the low-boiling impurities in a fifth storage tank 12, and storing the n-pentene in a sixth storage tank 13; the first tower bottom product is conveyed to a second rectifying tower 2 through a second conveying pump 15 from a first rectifying tower bottom outlet 1-3 through a second rectifying tower inlet 2-1 for secondary rectification to obtain benzene, ethylbenzene and a second tower bottom product, the benzene is discharged through a second rectifying tower top outlet 2-2 and then is condensed and stored in a second storage tank 7 through a third condenser 18, and the ethylbenzene is discharged through a second tower middle outlet 2-4 and then is condensed and stored in a third storage tank 8 through a fourth condenser 19; the second tower bottom product is conveyed to a third rectifying tower 3 through a third rectifying tower inlet 3-1 from a second rectifying tower bottom outlet 2-3 by a third conveying pump 16 for three-stage rectification to obtain isopropyl benzene and a third tower bottom product, and the isopropyl benzene is discharged through a third rectifying tower top outlet 3-2 and then condensed and stored in a fourth storage tank 9 by a fifth condenser 20; the third tower bottom product is conveyed to the fourth rectifying tower 4 through a fourth conveying pump 17 from a third rectifying tower bottom outlet 3-3 through a fourth rectifying tower inlet 4-1 for fourth rectification, n-propylbenzene and high-boiling impurities are obtained, the n-propylbenzene is discharged through a fourth rectifying tower top outlet 4-2 and then is condensed and stored in a seventh storage tank 11 through a sixth condenser 21, and the high-boiling impurities are stored in an eighth storage tank 10.
The technical solutions provided by the present invention are described in detail below in conjunction with examples for further illustrating the present invention, but they should not be construed as limiting the scope of the present invention.
And (3) separating and purifying the crude cumene product by using a separation and purification system shown in fig. 2.
Example 1
The crude cumene product (containing 2wt% of low-boiling impurities, 2wt% of n-pentene, 6wt% of ethylbenzene, 4wt% of n-propylbenzene, 36wt% of benzene and 50wt% of cumene) stored in a first storage tank 6 is subjected to primary rectification by using a first conveying pump 14 under the conditions that the feeding flow is 1000kg/h, the feeding temperature is 25 ℃ and the feeding pressure is 0.2MPa from a first rectifying tower inlet 1-1 to a first rectifying tower 1 (a sieve plate tower comprises 19 tower plates, the inner diameter of the tower is 550mm, the first rectifying tower inlet 1-1 is positioned at a 10 th tower plate in sequence from top to bottom, the tower top temperature is 55 ℃ and the tower bottom temperature is 130 ℃) to obtain a first tower top product and a first tower bottom product; the reflux ratio of the primary rectification is 1.5, and the pressure is 0.08MPa;
condensing the first tower top product from a first rectifying tower top outlet 1-2 through a first condenser 22, then entering a fifth rectifying tower 5 (a sieve plate tower comprises 20 tower plates, the inner diameter of the tower is 550mm, the fifth rectifying tower inlet 5-1 is positioned at a 10 th tower plate in sequence from top to bottom, the temperature of the tower top is 29 ℃, the temperature of the tower bottom is 42 ℃) through a fifth rectifying tower inlet 5-1, obtaining low-boiling impurities and n-pentene, condensing the low-boiling impurities through a second condenser 23, storing the low-boiling impurities in a fifth storage tank 12, and storing the n-pentene in a sixth storage tank 13; the reflux ratio of the fifth rectification is 3.3, and the pressure is 0.08MPa;
delivering the first tower bottom product to a second rectifying tower 2 (a sieve plate tower comprises 100 tower plates, the inner diameter of the tower is 1350 mm) through a second delivery pump 15 from a first rectifying tower bottom outlet 1-3 and a second rectifying tower inlet 2-1, performing secondary rectification on the second rectifying tower inlet 2-1 positioned at a 60 th tower plate in sequence from top to bottom, wherein the tower top temperature is 78 ℃, the tower bottom temperature is 112 ℃) to obtain benzene, ethylbenzene and a second tower bottom product, discharging the benzene through a second rectifying tower top outlet 2-2, condensing and storing the benzene in a second storage tank 7 through a third condenser 18, discharging the ethylbenzene through a second tower middle outlet 2-4, condensing and storing the ethylbenzene in a third storage tank 8 through a fourth condenser 19; the reflux ratio of the secondary rectification is 4.5, and the pressure is 0.012MPa;
conveying the second tower bottom product to a third rectifying tower 3 (a sieve plate tower comprises 80 tower plates, the inner diameter of the tower is 1450 mm) from a third conveying pump 16 through a third rectifying tower inlet 3-1 from a second rectifying tower bottom outlet 2-3, carrying out three-stage rectification on the tower top temperature 95 ℃ and the tower bottom temperature 110 ℃ at the 42 th tower plate position in sequence from top to bottom at the third rectifying tower inlet 3-1 to obtain isopropyl benzene and a third tower bottom product, discharging the isopropyl benzene through a third rectifying tower top outlet 3-2, and condensing and storing the isopropyl benzene in a fourth storage tank 9 through a fifth condenser 20; the reflux ratio of the three-stage rectification is 3.5, and the pressure is 0.012MPa;
and conveying the third tower bottom product to a fourth rectifying tower 4 (a sieve plate tower comprises 50 tower plates, the inner diameter of the tower is 450 mm) through a fourth conveying pump 17 from a third rectifying tower bottom outlet 3-3 to a fourth rectifying tower inlet 4-1, fourth rectifying tower inlet 4-1 is positioned at the tower top temperature 105 ℃ and the tower bottom temperature 130 ℃ at the 25 th tower plate in sequence from top to bottom), performing fourth rectification to obtain n-propylbenzene and high-boiling impurities, discharging n-propylbenzene through a fourth rectifying tower top outlet 4-2, condensing and storing the n-propylbenzene in a seventh storage tank 11 through a sixth condenser 21, storing the high-boiling impurities in an eighth storage tank 10, and enabling the fourth rectified reflux ratio to be 3.3 and the pressure to be 0.012MPa.
Separating raw material liquid and recovering products by using a rectification method, wherein the purity of the isopropyl benzene is 99.994wt% and the recovery rate is 99.91wt% measured by using a gas chromatography method; the purity of the n-pentene was 99.5wt%, the purity of the benzene was 99.6wt%, the purity of the ethylbenzene was 99.5wt%, and the purity of the n-propylbenzene was 99.6wt%.
Example 2
The crude cumene product (containing 3wt% of low-boiling impurities, 4wt% of n-pentene, 4wt% of ethylbenzene, 6wt% of n-propylbenzene, 36wt% of benzene and 47wt% of cumene) stored in a first storage tank 6 is fed to a first rectifying tower 1 (a sieve plate tower, containing 25 trays, with the inner diameter of the tower being 600mm, and the inlet 1-1 of the first rectifying tower being positioned at the 14 th tray in sequence from top to bottom, with the top temperature being 59 ℃ and the bottom temperature being 133 ℃ C.) by a first feeding pump 14 under the conditions of a feeding temperature of 25 ℃ and a feeding pressure of 0.2MPa, so as to obtain a first top product and a first bottom product; the reflux ratio of the primary rectification is 1.8, and the pressure is 0.1MPa;
condensing the first tower top product from a first rectifying tower top outlet 1-2 through a first condenser 22, then entering a fifth rectifying tower 5 (a sieve plate tower comprises 23 tower plates, the inner diameter of the tower is 600mm, the fifth rectifying tower inlet 5-1 is positioned at a 12 th tower plate in sequence from top to bottom, the temperature of the tower top is 31 ℃, the temperature of the tower bottom is 44 ℃) through a fifth rectifying tower inlet 5-1, obtaining low-boiling impurities and n-pentene, condensing the low-boiling impurities through a second condenser 23, storing the low-boiling impurities in a fifth storage tank 12, and storing the n-pentene in a sixth storage tank 13; the reflux ratio of the fifth rectification is 3.5, and the pressure is 0.1MPa;
the first tower bottom product is conveyed to a second rectifying tower 2 (a sieve plate tower comprises 105 tower plates, the inner diameter of the tower is 1400 mm) from a first rectifying tower bottom outlet 1-3 through a second conveying pump 15 to a second rectifying tower inlet 2-1, the second rectifying tower inlet 2-1 is positioned at a 65 th tower plate in sequence from top to bottom, the tower top temperature is 60 ℃, and the tower bottom temperature is 120 DEG C
) Performing secondary rectification to obtain benzene, ethylbenzene and a second tower bottom product, discharging benzene from an outlet 2-2 of the top of the second rectification tower, condensing and storing the benzene in a second storage tank 7 through a third condenser 18, discharging ethylbenzene from an outlet 2-4 of the second tower, condensing and storing the ethylbenzene in a third storage tank 8 through a fourth condenser 19; the reflux ratio of the secondary rectification is 5, and the pressure is 0.014MPa;
conveying the second tower bottom product to a third rectifying tower 3 (a sieve plate tower comprises 82 tower plates, the inner diameter of the tower is 1500mm, the third rectifying tower inlet 3-1 is positioned at a 43 th tower plate in sequence from top to bottom, the tower top temperature is 98 ℃ and the tower bottom temperature is 115 ℃) from a third conveying pump 16 through a third rectifying tower inlet 3-1 from a second rectifying tower bottom outlet 2-3, and condensing and storing the cumene in a fourth storage tank 9 through a fifth condenser 20 after the cumene is discharged from the third rectifying tower top outlet 3-2; the reflux ratio of the three-stage rectification is 4, and the pressure is 0.014MPa;
and conveying the third tower bottom product to a fourth rectifying tower 4 (a sieve plate tower comprises 55 tower plates, the inner diameter of the tower is 500 mm) through a fourth conveying pump 17 from a third rectifying tower bottom outlet 3-3 to a fourth rectifying tower inlet 4-1, fourth rectifying tower inlet 4-1 is positioned at the tower top temperature 108 ℃ and the tower bottom temperature 134 ℃ at the 28 th tower plate in sequence from top to bottom), performing fourth rectification to obtain n-propylbenzene and high-boiling impurities, discharging n-propylbenzene through a fourth rectifying tower top outlet 4-2, condensing and storing the n-propylbenzene in a seventh storage tank 11 through a sixth condenser 21, storing the high-boiling impurities in an eighth storage tank 10, and enabling the fourth rectified reflux ratio to be 3.3 and the pressure to be 0.014MPa.
Separating raw material liquid and recovering products by using a rectification method, wherein the purity of the isopropyl benzene is 99.993wt% and the recovery rate is 99.90wt% measured by using a gas chromatography method; the purity of the n-pentene was 99.4wt%, the purity of the benzene was 99.5wt%, the purity of the ethylbenzene was 99.4wt%, and the purity of the n-propylbenzene was 99.5wt%.
Example 3
The crude cumene product (containing 4wt% of low-boiling impurities, 3wt% of n-pentene, 3wt% of ethylbenzene, 8wt% of n-propylbenzene, 34wt% of benzene and 48wt% of cumene) stored in a first storage tank 6 is fed to a first rectifying tower 1 (a sieve plate tower, containing 17 plates, with the inner diameter of the tower being 650mm, and the inlet 1-1 of the first rectifying tower being positioned at the 9 th plate in sequence from top to bottom, with the top temperature being 61 ℃ and the bottom temperature being 134 ℃) by a first feeding pump 14 under the conditions of feeding temperature being 25 ℃ and feeding pressure being 0.2MPa, and is subjected to primary rectification to obtain a first top product and a first bottom product; the reflux ratio of the primary rectification is 1.3, and the pressure is 0.07MPa;
condensing the first tower top product from a first rectifying tower top outlet 1-2 through a first condenser 22, then entering a fifth rectifying tower 5 (a sieve plate tower comprises 18 tower plates, the inner diameter of the tower is 650mm, the fifth rectifying tower inlet 5-1 is positioned at a 9 th tower plate in sequence from top to bottom, the temperature of the tower top is 33 ℃, the temperature of the tower bottom is 46 ℃) through a fifth rectifying tower inlet 5-1, obtaining low-boiling impurities and n-pentene, condensing the low-boiling impurities through a second condenser 23, storing the low-boiling impurities in a fifth storage tank 12, and storing the n-pentene in a sixth storage tank 13; the reflux ratio of the fifth rectification is 3.2, and the pressure is 0.07MPa;
delivering the first tower bottom product to a second rectifying tower 2 (a sieve plate tower comprises 90 tower plates, the inner diameter of the tower is 1450 mm) through a second delivery pump 15 from a first rectifying tower bottom outlet 1-3 and a second rectifying tower inlet 2-1, performing secondary rectification on the second rectifying tower inlet 2-1 positioned at a 55 th tower plate in sequence from top to bottom, wherein the tower top temperature is 81 ℃, the tower bottom temperature is 117 ℃) to obtain benzene, ethylbenzene and a second tower bottom product, discharging the benzene through a second rectifying tower top outlet 2-2, condensing and storing the benzene in a second storage tank 7 through a third condenser 18, discharging the ethylbenzene through a second tower middle outlet 2-4, condensing and storing the ethylbenzene in a third storage tank 8 through a fourth condenser 19; the reflux ratio of the secondary rectification is 4, and the pressure is 0.011MPa;
conveying the second tower bottom product to a third rectifying tower 3 (a sieve plate tower comprises 75 tower plates, the inner diameter of the tower is 1550mm, the third rectifying tower inlet 3-1 is positioned at a 40 th tower plate in sequence from top to bottom, the tower top temperature is 100 ℃, the tower bottom temperature is 118 ℃) from a third conveying pump 16 through a third rectifying tower inlet 3-1 from a second rectifying tower bottom outlet 2-3, and performing three-stage rectification to obtain isopropyl benzene and a third tower bottom product, wherein the isopropyl benzene is discharged from a third rectifying tower top outlet 3-2 and then condensed and stored in a fourth storage tank 9 through a fifth condenser 20; the reflux ratio of the three-stage rectification is 3.2, and the pressure is 0.011MPa;
and conveying the third tower bottom product to a fourth rectifying tower 4 (a sieve plate tower comprises 47 tower plates, the inner diameter of the tower is 550mm, the fourth rectifying tower inlet 4-1 is positioned at a 23 rd tower plate in sequence from top to bottom, the tower top temperature is 110 ℃, the tower bottom temperature is 135) through a fourth conveying pump 17 from a third rectifying tower bottom outlet 3-3 to a fourth rectifying tower inlet 4-1, n-propylbenzene and high-boiling impurities are obtained, the n-propylbenzene is discharged from a fourth rectifying tower top outlet 4-2 and then condensed and stored in a seventh storage tank 11 through a sixth condenser 21, the high-boiling impurities are stored in an eighth storage tank 10, and the reflux ratio of the fourth rectification is 2.7, wherein the pressure is 0.011MPa.
Separating raw material liquid and recovering products by using a rectification method, wherein the purity of the isopropyl benzene is 99.992wt% and the recovery rate is 99.88wt% measured by using a gas chromatography method; the purity of the n-pentene was 99.2wt%, the purity of the benzene was 99.4wt%, the purity of the ethylbenzene was 99.2wt%, and the purity of the n-propylbenzene was 99.3wt%.
The invention designs the scheme of the continuous rectifying process of the isopropyl benzene, the synthetic liquid is put into a continuous rectifying device for separation, the heating steam consumption of all rectifying towers of the process before improvement is 3.32t/h, the circulating water consumption is 362.65t/h, the heating steam consumption of all rectifying towers of the process after improvement is 2.86t/h, the circulating water consumption is 311.52t/h, the steam consumption is reduced by 18.75%, and the circulating water consumption is reduced by 14.10%.
The purification method provided by the invention has the advantages of high product recovery rate, high product purity, high purity of cumene of more than 99.9wt%, recovery rate of more than 99wt%, purity of n-pentene of 99.2-99.5 wt%, purity of benzene of 99.4-99.6 wt%, purity of ethylbenzene of 99.4-99.5 wt% and purity of n-propylbenzene of 99.5-99.6 wt%, simple separation steps, high purification efficiency, simple equipment structure and low cost and low energy consumption.
Although the foregoing embodiments have been described in some, but not all, embodiments of the invention, it should be understood that other embodiments may be devised in accordance with the present embodiments without departing from the spirit and scope of the invention.
Claims (10)
1. A separation and purification system comprises a first storage tank (6), a first rectifying tower (1) with a first rectifying tower inlet (1-1) connected with an outlet of the first storage tank (6), a second rectifying tower (2) with a second rectifying tower inlet (2-1) connected with a first rectifying tower bottom outlet (1-3), and a third rectifying tower (3) with a third rectifying tower inlet (3-1) connected with a second rectifying tower bottom outlet (2-3);
the device also comprises a second storage tank (7) connected with the top outlet (2-2) of the second rectifying tower, a third storage tank (8) connected with the middle outlet (2-4) of the second rectifying tower and a fourth storage tank (9) connected with the top outlet (3-2) of the third rectifying tower.
2. The separation and purification system according to claim 1, further comprising a fourth rectifying column (4) with a fourth rectifying column inlet (4-1) connected to a third rectifying column bottom outlet (3-3); a seventh storage tank (11) connected with the top outlet (4-2) of the fourth rectifying tower, and an eighth storage tank (10) connected with the bottom outlet (4-3) of the fourth rectifying tower.
3. The separation and purification system according to claim 2, wherein the inner diameter of the fourth rectifying column (4) is 200-800 mm, the fourth rectifying column (4) is a plate column or a packed column, and the number of plates is 30-70 when the fourth rectifying column (4) is a plate column.
4. The separation and purification system according to claim 1, further comprising a fifth rectifying column (5) having a fifth rectifying column inlet (5-1) connected to the first rectifying column top outlet (1-2), a fifth storage tank (12) connected to the fifth rectifying column top outlet (5-2), and a sixth storage tank (13) connected to the fifth rectifying column bottom outlet (5-3).
5. The separation and purification system according to claim 4, wherein the inner diameter of the fifth rectifying column (5) is 300 to 1000mm, the fifth rectifying column (5) comprises a tray column or a packed column, and the number of trays is 10 to 40 when the fifth rectifying column (5) is a tray column.
6. The method for separating and purifying the crude cumene product by using the separation and purification system according to any one of claims 1 to 5, comprising the following steps:
the crude cumene product stored in a first storage tank (6) is conveyed to a first rectifying tower (1) for primary rectification, and a first tower bottom product is obtained;
delivering the first tower bottom product to a second rectifying tower (2) for secondary rectification, obtaining a second tower bottom product at the tower bottom, obtaining benzene at the tower top, obtaining ethylbenzene at the side line, storing the benzene in a second storage tank (7), and storing the ethylbenzene in a third storage tank (8);
and conveying the second tower bottom product to a third rectifying tower (3) for three-stage rectification, obtaining a third tower bottom product at the tower bottom, and obtaining a pure isopropyl benzene product at the tower top, wherein the pure isopropyl benzene product is stored in a fourth storage tank (9).
7. The method according to claim 6, wherein the pressure of the primary rectification is 0.01-0.15 MPa, the top temperature of the first rectification column (1) is 53-89 ℃, and the bottom temperature of the first rectification column (1) is 122-145 ℃.
8. The method according to claim 6, wherein the pressure of the secondary rectification is 0.01-0.05 MPa, the top temperature of the second rectification column (2) is 45-119 ℃, and the bottom temperature of the second rectification column (2) is 105-132 ℃.
9. The method according to claim 6, wherein the pressure of the three-stage rectification is 0.01-0.05 MPa, the top temperature of the third rectification column (3) is 78-132 ℃, and the bottom temperature of the third rectification column (3) is 105-152 ℃.
10. The method as recited in claim 6, further comprising: conveying the third tower bottom product to a fourth rectifying tower (4) for fourth rectification, and obtaining n-propylbenzene at the tower top and a fourth tower bottom product at the tower bottom; the n-propylbenzene is stored in a seventh storage tank (11), and the fourth bottom product is stored in an eighth storage tank (10);
the first tower top product is further obtained through the first rectification, the first tower top product is conveyed to a fifth rectification tower (5) to carry out fifth rectification, n-pentene is obtained from the tower bottom, and the n-pentene is stored in a sixth storage tank (13).
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