CN216259172U - Three-tower differential pressure thermal coupling rectification system for separating methanol, dimethyl carbonate and phenol - Google Patents
Three-tower differential pressure thermal coupling rectification system for separating methanol, dimethyl carbonate and phenol Download PDFInfo
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- CN216259172U CN216259172U CN202122963547.XU CN202122963547U CN216259172U CN 216259172 U CN216259172 U CN 216259172U CN 202122963547 U CN202122963547 U CN 202122963547U CN 216259172 U CN216259172 U CN 216259172U
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Abstract
The utility model belongs to the technical field of chemical industry, and particularly relates to a three-tower differential pressure thermal coupling rectification system for separating methanol, dimethyl carbonate and phenol. The system comprises a DMC rectifying tower, wherein the middle lower part of the DMC rectifying tower is connected with a raw material pipeline, the top of the DMC rectifying tower is connected with a condensation pipeline, and the bottom of the DMC rectifying tower is connected with a mixed stream pipeline; the device also comprises a methanol refining tower, the other end of the condensation pipeline is connected to the middle part of the methanol refining tower, a return pipeline is connected between the top of the methanol refining tower and the middle upper part of the DMC rectifying tower, and the bottom of the methanol refining tower is connected with a methanol product pipeline; the device also comprises a DMC refining tower, the other end of the mixed stream pipeline is connected to the middle part of the DMC refining tower, the top of the DMC refining tower is connected with a DMC product pipeline, and the bottom of the DMC refining tower is connected with a phenol product pipeline. The utility model provides a three-tower differential pressure thermal coupling rectification system capable of effectively separating and refining methanol, dimethyl carbonate and phenol in a diphenyl carbonate plant stream.
Description
Technical Field
The utility model belongs to the technical field of chemical industry, and particularly relates to a three-tower differential pressure thermal coupling rectification system for separating methanol, dimethyl carbonate and phenol.
Background
Methanol is not only an important chemical raw material, but also an energy source and vehicle fuel with excellent performance, and can replace methyl tert-butyl ether to be used as a gasoline additive. Besides, the method can also prepare olefin, thereby solving the problem of resource shortage at present.
In the production process of diphenyl carbonate (DPC), a part of methanol is produced as a byproduct, the purity of the product is only 93 wt%, and the product cannot be sold as a commodity; however, methanol and dimethyl carbonate (DMC) as a raw material form a binary azeotropic system, if a high-grade methanol product is to be obtained, the separation is difficult by using a traditional rectification method, and the energy consumption is very high because special rectification is selected for the separation.
SUMMERY OF THE UTILITY MODEL
In order to solve the above problems in the prior art, an object of the present invention is to provide a three-tower differential pressure thermal coupling rectification system capable of effectively separating and refining methanol, dimethyl carbonate and phenol in a diphenyl carbonate plant stream.
The technical scheme adopted by the utility model is as follows:
the three-tower differential pressure thermal coupling rectification system for separating the methanol, the dimethyl carbonate and the phenol comprises a DMC rectification tower, wherein the middle lower part of the DMC rectification tower is connected with a raw material pipeline for introducing a stream from a diphenyl carbonate reaction tower, the top of the DMC rectification tower is connected with a condensation pipeline, and the bottom of the DMC rectification tower is connected with a mixed stream pipeline; the device also comprises a methanol refining tower, the other end of the condensation pipeline is connected to the middle part of the methanol refining tower, a return pipeline is connected between the top of the methanol refining tower and the middle upper part of the DMC rectifying tower, and the bottom of the methanol refining tower is connected with a methanol product pipeline; the device also comprises a DMC refining tower, the other end of the mixed stream pipeline is connected to the middle part of the DMC refining tower, the top of the DMC refining tower is connected with a DMC product pipeline, and the bottom of the DMC refining tower is connected with a phenol product pipeline.
The DMC rectifying tower can separate a stream containing methanol from the top, the stream condensed by the condensing pipeline is fully separated in the methanol refining tower, and a methanol product is separated from the methanol refining tower. And (3) delivering the stream at the top of the methanol rectifying tower to the top of the DMC rectifying tower, so that after the stream is separated by the DMC rectifying tower and the methanol rectifying tower, the purity of the methanol extracted from the methanol rectifying tower is higher, and DMC and phenol in the stream at the top of the DMC rectifying tower can be fully returned to the DMC rectifying tower. And sending the mixed stream containing DMC and phenol extracted from the DMC rectifying tower to a DMC refining tower, wherein the DMC refining tower can fully separate DMC and phenol, thereby respectively obtaining DMC products and phenol products with higher purity.
In a preferred embodiment of the present invention, the condensation line is connected to a reboiler at the bottom of the methanol purification column, and the condensation line is connected to the tube side of the reboiler at the bottom of the methanol purification column. And condensing the stream extracted from the top of the DMC rectifying tower after passing through a tube pass of a reboiler at the bottom of the methanol refining tower.
In a preferred embodiment of the present invention, the condenser line is further connected to a first condenser at the top of the DMC rectification column. And condensing the stream condensed by the reboiler at the bottom of the methanol refining tower by the first condenser at the top of the DMC rectification tower, and sending the stream into the middle part of the methanol refining tower after full condensation.
As a preferable scheme of the utility model, one end of the condensation pipeline close to the methanol rectifying tower is also connected with a condensation return pipeline, and the other end of the condensation return pipeline is connected with the top of the DMC rectifying tower. Part of the stream condensed by the reboiler at the bottom of the methanol refining tower and the first condenser at the top of the DMC rectifying tower returns to the top of the DMC rectifying tower, so that DMC and phenol in the stream extracted from the top of the DMC rectifying tower can be fully sent back to the DMC rectifying tower.
As a preferable scheme of the utility model, a methanol return pipeline is connected to the methanol product pipeline, the other end of the methanol return pipeline is connected to the bottom of the methanol refining tower, and the methanol return pipeline is connected with the shell side of a reboiler at the bottom of the methanol refining tower. And part of the stream extracted from the bottom of the methanol refining tower is reboiled by a reboiler at the bottom of the methanol refining tower and then is sent back to the bottom of the methanol refining tower, so that components except methanol in the extracted stream are fully evaporated, and the purity of the extracted methanol product is improved. The heat source is provided for the reboiler at the bottom of the methanol refining tower by utilizing the gas phase condensation latent heat at the top of the DMC rectifying tower, the reutilization of the vaporization latent heat is realized, and the steam required by the reboiler at the bottom of the methanol refining tower is further saved.
In a preferred embodiment of the present invention, the methanol product pipeline is further connected to a methanol initial return pipeline, the other end of the methanol initial return pipeline is connected to the bottom of the methanol refining tower, and the methanol initial return pipeline is connected to a start-up reboiler. When the methanol refining tower is started for the first time, the stream at the bottom of the methanol refining tower is sent to the bottom of the methanol refining tower after passing through the start reboiler, so that the condition that no stream flows into the tube pass of the reboiler at the bottom of the methanol refining tower in the initial period is avoided.
In a preferred embodiment of the present invention, the return line is connected to a second condenser on the top of the methanol refining tower, the return line on the outlet side of the second condenser on the top of the methanol refining tower is connected to a methanol return line, and the other end of the methanol return line is connected to the top of the methanol refining tower. And condensing the stream on the reflux pipeline through a second condenser at the top of the methanol refining tower, and sending part of the stream back to the top of the methanol refining tower, so that the methanol in the extracted stream is reduced, and the methanol can be fully settled in the methanol refining tower.
As a preferred scheme of the utility model, the mixed stream pipeline is connected with a mixed stream reflux pipeline, the other end of the mixed stream reflux pipeline is connected to the bottom of the DMC rectification tower, and the mixed stream reflux pipeline is connected with a reboiler at the bottom of the DMC rectification tower. And the reboiler at the bottom of the DMC rectifying tower can ensure that part of stream extracted from the bottom of the DMC rectifying tower is fully reboiled and then sent back to the DMC rectifying tower, so that the methanol in the stream can be fully evaporated, and the content of the methanol in the stream sent to the middle part of the DMC rectifying tower is reduced.
In a preferred embodiment of the present invention, a DMC purification tower top condenser is connected to the DMC product line, a DMC reflux line is connected to the DMC product line on the outlet side of the DMC purification tower top condenser, and the other end of the DMC reflux line is connected to the top of the DMC purification tower. The DMC refining tower top condenser can fully condense the stream extracted from the top of the DMC refining tower, and the partially condensed stream is sent back to the top of the DMC refining tower, so that phenol in the stream can be fully settled, and the purity of the extracted DMC product is improved.
In a preferred embodiment of the present invention, the phenol product line is connected to a phenol return line, the other end of the phenol return line is connected to the bottom of the DMC purification column, and the phenol return line is connected to a DMC purification column bottom reboiler. And the reboiler at the bottom of the DMC refining tower can ensure that the stream produced at the bottom of the DMC refining tower is fully reboiled and then sent back to the bottom of the DMC refining tower, so that phenol in the stream produced at the bottom of the DMC refining tower is fully evaporated, and the purity of the produced DMC product is improved.
The utility model has the beneficial effects that:
the DMC rectifying tower can separate a stream containing methanol from the top, the stream condensed by the condensing pipeline is fully separated in the methanol refining tower, and a methanol product is separated from the methanol refining tower. And (3) delivering the stream at the top of the methanol rectifying tower to the top of the DMC rectifying tower, so that after the stream is separated by the DMC rectifying tower and the methanol rectifying tower, the purity of the methanol extracted from the methanol rectifying tower is higher, and DMC and phenol in the stream at the top of the DMC rectifying tower can be fully returned to the DMC rectifying tower. And sending the mixed stream containing DMC and phenol extracted from the DMC rectifying tower to a DMC refining tower, wherein the DMC refining tower can fully separate DMC and phenol, thereby respectively obtaining DMC products and phenol products with higher purity.
Drawings
Fig. 1 is a schematic structural view of the present invention.
In the figure, a 1-DMC rectifying tower; 2-a condensation line; 3-a mixed stream line; 4-methanol refining column; 5-a return line; 6-methanol product line; 7-DMC purification column; 8-DMC product line; a 9-phenol product line; 11-feed line; 21-methanol refining tower bottom reboiler; 22-DMC rectification overhead first condenser; 23-a condensate return line; 31-mixed stream return line; a 32-DMC rectification column bottom reboiler; a second condenser at the top of the 51-methanol refining tower; 52-methanol return line; 61-methanol return line; 62-methanol initial return line; 63-start-up reboiler; 81-DMC refining overhead condenser; 82-DMC return line; 91-phenol return line; 92-DMC refining bottoms reboiler.
Detailed Description
Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings, wherein like or similar reference numerals refer to the same or similar elements or elements having the same or similar function throughout. The embodiments described below with reference to the drawings are illustrative and intended to be illustrative of the utility model and are not to be construed as limiting the utility model.
As shown in fig. 1, the three-tower differential pressure thermal coupling rectification system for separating methanol from dimethyl carbonate and phenol of the present embodiment includes a DMC rectification tower 1, a raw material pipeline 11 for introducing a stream from a diphenyl carbonate reaction tower is connected to the middle lower part of the DMC rectification tower 1, a condensation pipeline 2 is connected to the tower top of the DMC rectification tower 1, and a mixed stream pipeline 3 is connected to the tower bottom of the DMC rectification tower 1; the device also comprises a methanol refining tower 4, the other end of the condensation pipeline 2 is connected to the middle part of the methanol refining tower 4, a return pipeline 5 is connected between the top of the methanol refining tower 4 and the middle upper part of the DMC rectifying tower 1, and the bottom of the methanol refining tower 4 is connected with a methanol product pipeline 6; the device further comprises a DMC refining tower 7, the other end of the mixed stream pipeline 3 is connected to the middle of the DMC refining tower 7, the top of the DMC refining tower 7 is connected with a DMC product pipeline 8, and the bottom of the DMC refining tower 7 is connected with a phenol product pipeline 9.
The DMC rectifying tower 1 can separate a stream containing methanol from the top, the stream condensed by the condensing pipeline 2 is fully separated in the methanol refining tower 4, and a methanol product is separated from the methanol refining tower 4. The stream at the top of the methanol refining tower 4 is sent to the top of the DMC rectifying tower 1, so that after the stream is separated by the DMC rectifying tower 1 and the methanol refining tower 4, the purity of the methanol extracted from the methanol refining tower 4 is higher, and DMC and phenol in the stream at the top of the DMC rectifying tower 1 can be fully returned to the DMC rectifying tower 1. The mixed stream containing DMC and phenol extracted from the DMC rectifying tower 1 is sent to a DMC refining tower 7, and the DMC refining tower 7 can fully separate DMC and phenol, thereby obtaining DMC products and phenol products with higher purity respectively.
Specifically, the condensation pipeline 2 is connected to a methanol refining tower bottom reboiler 21, and the condensation pipeline 2 is connected to a tube pass of the methanol refining tower bottom reboiler 21. The stream extracted from the top of the DMC rectification column 1 passes through the tube pass of the reboiler 21 at the bottom of the methanol refining column and is then condensed. The condensation pipeline 2 is also connected with a DMC rectification tower top first condenser 22. And the stream condensed by the reboiler 21 at the bottom of the methanol refining tower is condensed by the first condenser 22 at the top of the DMC rectifying tower, and the stream is sent to the middle part of the methanol refining tower 4 after being condensed completely. And one end of the condensation pipeline 2 close to the methanol refining tower 4 is also connected with a condensation return pipeline 23, and the other end of the condensation return pipeline 23 is connected to the top of the DMC rectification tower 1. Part of the stream condensed by the methanol refining tower bottom reboiler 21 and the DMC rectification tower top first condenser 22 returns to the top of the DMC rectification tower 1, so that DMC and phenol in the stream extracted from the top of the DMC rectification tower 1 can be fully returned to the DMC rectification tower 1.
Furthermore, a methanol return line 61 is connected to the methanol product line 6, the other end of the methanol return line 61 is connected to the bottom of the methanol refining column 4, and the methanol return line 61 is connected to the shell side of a reboiler 21 at the bottom of the methanol refining column. Part of the stream extracted from the bottom of the methanol refining tower 4 is reboiled by a reboiler 21 at the bottom of the methanol refining tower and then sent back to the bottom of the methanol refining tower 4, so that components except methanol in the extracted stream are fully evaporated, and the purity of the extracted methanol product is improved. The heat source is provided for the reboiler 21 at the bottom of the methanol refining tower by utilizing the gas phase condensation latent heat at the top of the DMC rectifying tower 1, the recycling of the vaporization latent heat is realized, and the steam required by the reboiler 21 at the bottom of the methanol refining tower is further saved.
Furthermore, the methanol product pipeline 6 is also connected with a methanol initial return pipeline 62, the other end of the methanol initial return pipeline 62 is connected to the bottom of the methanol refining tower 4, and the methanol initial return pipeline 62 is connected with a start-up reboiler 63. When the car is started for the first time, the stream at the bottom of the methanol refining tower 4 is sent to the bottom of the methanol refining tower 4 after passing through the car-starting reboiler 63, so that the condition that no stream flows into the tube pass of the methanol refining tower bottom reboiler 21 in the initial period is avoided.
Further, the return line 5 is connected to a second condenser 51 at the top of the methanol refining tower, the return line 5 on the outlet side of the second condenser 51 at the top of the methanol refining tower is connected to a methanol return line 52, and the other end of the methanol return line 52 is connected to the top of the methanol refining tower 4. After the stream on the reflux pipeline 5 is condensed by the second condenser 51 at the top of the methanol refining tower, part of the stream is sent back to the top of the methanol refining tower 4, so that the methanol in the extracted stream is reduced, and the methanol can be fully settled in the methanol refining tower 4.
Furthermore, a mixed stream return line 31 is connected to the mixed stream line 3, the other end of the mixed stream return line 31 is connected to the bottom of the DMC rectification column 1, and the mixed stream return line 31 is connected to a DMC rectification column bottom reboiler 32. The reboiler 32 at the bottom of the DMC rectifying tower can ensure that part of stream extracted from the bottom of the DMC rectifying tower 1 is fully reboiled and then sent back to the DMC rectifying tower 1, so that the methanol in the stream can be fully evaporated, and the content of the methanol in the stream sent to the middle part of the DMC rectifying tower 7 is reduced.
Further, a DMC purification overhead condenser 81 is connected to the DMC product line 8, a DMC reflux line 82 is connected to the DMC product line 8 on the outlet side of the DMC purification overhead condenser 81, and the other end of the DMC reflux line 82 is connected to the top of the DMC purification column 7. The DMC refining tower top condenser 81 can fully condense the stream extracted from the tower top of the DMC refining tower 7, and the partially condensed stream is sent back to the tower top of the DMC refining tower 7, so that phenol in the stream can be fully settled, and the purity of the extracted DMC product is improved.
Further, a phenol return line 91 is connected to the phenol product line 9, the other end of the phenol return line 91 is connected to the bottom of the DMC purification column 7, and a DMC purification column bottom reboiler 92 is connected to the phenol return line 91. The reboiler 92 at the bottom of the DMC refining tower can ensure that the stream extracted from the bottom of the DMC refining tower 7 is fully reboiled and then sent back to the bottom of the DMC refining tower 7, so that phenol in the stream extracted from the bottom of the DMC refining tower 7 is fully evaporated, and the purity of the extracted DMC product is improved.
The working process is as follows:
introducing the stream from the DPC reaction tower into the middle lower part of the DMC rectifying tower 1; and (3) feeding a gas stream (139.7 ℃) at the top of the DMC rectifying tower 1 into a reboiler 21 at the bottom of the methanol refining tower, feeding the condensed stream into a second condenser at the top of the DMC rectifying tower 1, refluxing the condensed stream to the top of the DMC rectifying tower 1, and feeding the other stream into the middle of the methanol refining tower 4 b. And the stream (202.2 ℃) at the bottom of the DMC rectifying tower 1 enters the bottom of the DMC rectifying tower 1 after passing through a reboiler 32 at the bottom of the DMC rectifying tower, and the extracted stream enters the middle part of a DMC refining tower 7. And a gas stream (67.7 ℃) at the top of the methanol refining tower 4 enters a condenser at the top of the methanol refining tower 4, a full-condensation rear split stream reflows to the top of the methanol refining tower 4, and the other part of the stream returns to the middle upper part of the DMC rectifying tower 1. The stream (70.6 ℃) at the bottom of the methanol refining tower 4 passes through a reboiler 21 at the bottom of the methanol refining tower and enters the bottom of the methanol refining tower 4, and the extracted stream is 99.96 wt% of methanol product. And when the automobile is started for the first time, the stream at the bottom of the methanol refining tower 4 enters the bottom of the methanol refining tower 4 after passing through the start reboiler 63. And a gas stream (69.5 ℃) at the top of the DMC refining tower 7 enters a DMC refining tower top condenser 81, a part of fully condensed stream reflows to the top of the DMC refining tower 7, and the other part of stream is 99.99 wt% of DMC product. And the stream (161 ℃) at the bottom of the DMC refining tower 7 enters the bottom of the DMC refining tower 7 after passing through a reboiler 92 at the bottom of the DMC refining tower, and the extracted stream is 99.99 wt% of phenol product.
The heat load at the top of the DMC rectifying tower 1 is matched with the heat load at the bottom of the methanol refining tower 4, and other heat exchange devices are not required to be started.
The operating pressure range of the DMC rectifying tower 1 is 0.8-1.2 MPaG, the operating pressure range of the methanol refining tower 4 is 0-0.3 MPaG, and the operating pressure range of the DMC refining tower 7 is-0.1 MPaG.
The feeding amount of methanol, DMC and phenol mixture was 10000kg/h, wherein the mass fraction of methanol was 3.0 wt%, and the mass fraction of DMC was 74.0 wt%. The optimum operating pressure for DMC column 1 was 0.98MPaG, the top temperature 139.7 ℃ and the bottom temperature 202.2 ℃. The optimum operating pressure of the DMC refining column 7 was 0.02MPaG, the top temperature was 67.7 ℃ and the bottom temperature was 70.6 ℃. The optimum operating pressure of the methanol refining column 4 was-0.051 MPaG, the column top temperature was 69.5 ℃ and the column bottom temperature was 161 ℃.
The gas phase condensation latent heat at the top of the DMC rectifying tower 1 in the prior method is completely taken away by circulating cooling water, thereby causing a great deal of waste of energy. The heat source is provided for the reboiler 21 at the bottom of the methanol refining tower by utilizing the gas phase condensation latent heat at the top of the DMC rectifying tower 1, the recycling of the vaporization latent heat is realized, and the steam required by the reboiler 21 at the bottom of the methanol refining tower is further saved.
The utility model is not limited to the above alternative embodiments, and any other various forms of products can be obtained by anyone in the light of the present invention, but any changes in shape or structure thereof, which fall within the scope of the present invention as defined in the claims, fall within the scope of the present invention.
Claims (10)
1. The three-tower differential pressure thermal coupling rectification system for separating methanol, dimethyl carbonate and phenol is characterized by comprising a DMC rectification tower (1), wherein the middle lower part of the DMC rectification tower (1) is connected with a raw material pipeline (11) for introducing a stream from a diphenyl carbonate reaction tower, the top of the DMC rectification tower (1) is connected with a condensation pipeline (2), and the bottom of the DMC rectification tower (1) is connected with a mixed stream pipeline (3); the device also comprises a methanol refining tower (4), the other end of the condensation pipeline (2) is connected to the middle part of the methanol refining tower (4), a reflux pipeline (5) is connected between the top of the methanol refining tower (4) and the middle upper part of the DMC rectifying tower (1), and the bottom of the methanol refining tower (4) is connected with a methanol product pipeline (6); the device is characterized by further comprising a DMC refining tower (7), the other end of the mixed stream pipeline (3) is connected to the middle of the DMC refining tower (7), the top of the DMC refining tower (7) is connected with a DMC product pipeline (8), and the bottom of the DMC refining tower (7) is connected with a phenol product pipeline (9).
2. The three-tower differential pressure thermal coupling rectification system for separating the methanol from the dimethyl carbonate and the phenol according to claim 1, wherein the condensation pipeline (2) is connected with a methanol refining tower bottom reboiler (21), and the condensation pipeline (2) is connected with the tube side of the methanol refining tower bottom reboiler (21).
3. The three-tower differential pressure thermal coupling rectification system for separating the methanol from the dimethyl carbonate and the phenol according to claim 2, characterized in that a DMC rectification tower top first condenser (22) is further connected to the condensation pipeline (2).
4. The three-tower differential pressure thermal coupling rectification system for separating the methanol from the dimethyl carbonate and the phenol according to claim 3, wherein one end of the condensation pipeline (2) close to the methanol refining tower (4) is also connected with a condensation return pipeline (23), and the other end of the condensation return pipeline (23) is connected to the top of the DMC rectification tower (1).
5. The three-tower differential pressure thermal coupling rectification system for separating methanol from dimethyl carbonate and phenol according to claim 2, wherein a methanol return line (61) is connected to the methanol product line (6), the other end of the methanol return line (61) is connected to the bottom of the methanol refining tower (4), and the methanol return line (61) is connected to the shell side of a reboiler (21) at the bottom of the methanol refining tower.
6. The three-tower differential pressure thermal coupling rectification system for separating methanol from dimethyl carbonate and phenol according to claim 5, wherein a methanol initial return line (62) is further connected to the methanol product line (6), the other end of the methanol initial return line (62) is connected to the bottom of the methanol refining tower (4), and a start-up reboiler (63) is connected to the methanol initial return line (62).
7. The three-tower differential pressure thermal coupling rectification system for separating methanol from dimethyl carbonate and phenol according to claim 1, wherein a second condenser (51) at the top of the methanol refining tower is connected to the return pipeline (5), a methanol return pipeline (52) is connected to the return pipeline (5) positioned at the outlet side of the second condenser (51) at the top of the methanol refining tower, and the other end of the methanol return pipeline (52) is connected to the top of the methanol refining tower (4).
8. The three-tower differential pressure thermal coupling rectification system for separating methanol from dimethyl carbonate and phenol according to claim 1, characterized in that a mixed stream return line (31) is connected to the mixed stream pipeline (3), the other end of the mixed stream return line (31) is connected to the bottom of the DMC rectification tower (1), and the mixed stream return line (31) is connected to a DMC rectification tower bottom reboiler (32).
9. The three-tower differential pressure thermal coupling rectification system for separating methanol from dimethyl carbonate and phenol according to claim 1, characterized in that a DMC purification overhead condenser (81) is connected to the DMC product pipeline (8), a DMC return pipeline (82) is connected to the DMC product pipeline (8) on the outlet side of the DMC purification overhead condenser (81), and the other end of the DMC return pipeline (82) is connected to the top of the DMC purification tower (7).
10. The three-tower differential pressure thermal coupling rectification system for separating methanol, dimethyl carbonate and phenol according to any one of claims 1 to 9, wherein a phenol return line (91) is connected to the phenol product line (9), the other end of the phenol return line (91) is connected to the bottom of the DMC purification tower (7), and a DMC purification tower bottom reboiler (92) is connected to the phenol return line (91).
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