Energy-saving production system for tert-amyl methyl ether

Abstract

The utility model relates to the technical field of production of tert-amyl methyl ether, in particular to an energy-saving production system of tert-amyl methyl ether, which comprises an etherification reactor, a catalytic distillation tower, an extraction tower and a methanol recovery tower, the tower top of the etherification reactor is connected with an etherification reaction preheater through a pipeline, the etherification reaction preheater is connected with a methanol pipeline and a C5 pipeline, and the methanol pipeline and the C5 pipeline are connected through a pipeline. The C5 pipeline is connected with an etherification reaction raw material heater, the tower bottom of the etherification reactor is connected with the catalytic distillation tower through a pipeline, and the pipeline between the etherification reactor and the catalytic distillation tower is connected with a catalytic distillation tower feeding and discharging heat exchanger; a tower bottom pipeline of the catalytic distillation tower is sequentially connected with a catalytic distillation tower feeding and discharging heat exchanger, an etherification reaction raw material heater and a TAME cooler. The utility model provides an energy-saving production system for tert-amyl methyl ether, which can realize low investment, effectively reduce the consumption of steam and circulating water and reduce the comprehensive energy consumption of a device, and is easy to implement on site.

Description

Technical Field

[0001] The utility model relates to the technical field of production of tert-amyl methyl ether, in particular to an energy-saving production system of tert-amyl methyl ether. Background Art

[0002] Tertiary amyl methyl ether (TAME) is a high-octane gasoline additive and an important chemical raw material. It can be used to crack and produce high-purity isopentene, etc. Existing tertiary amyl methyl ether devices generally use C5 olefins and methanol as raw materials to produce TAME through etherification reaction, catalytic distillation, methanol extraction and methanol recovery.

[0003] In the traditional process, the raw materials need to be preheated before the etherification reaction, usually using steam or hot water to preheat the raw materials from 20°C to about 50°C; in addition, the product TAME needs to be cooled to 40°C by the TAME cooler after being discharged from the catalytic distillation tower and sent to the tank area. In the above production process, on the basis of obtaining a large amount of heat from the outside, the heat generated in the production process is not effectively utilized.

[0004] On the other hand, the condensation heat of the gaseous methanol after methanol recovery is relatively large, and it is directly cooled to 40°C in the condenser. The condensation heat of the high-temperature gaseous methanol is not fully utilized. Instead, a large amount of circulating water is wasted for condensing and cooling the high-temperature gaseous methanol.

[0005] In summary, how to make full use of the heat of hot TAME and high-temperature gaseous methanol with low investment, reduce the steam and circulating water consumption of the device, and reduce the comprehensive energy consumption of the methyl tert-amyl ether production system is the key problem to be solved by the utility model. Utility Model Content

[0006] The technical problem to be solved by the utility model is to overcome the defects of the prior art and provide an energy-saving production system for tert-amyl methyl ether.

[0007] In order to solve the above technical problems, the utility model provides the following technical solutions:

[0008] A tert-amyl methyl ether energy-saving production system comprises an etherification reactor, a catalytic distillation tower, an extraction tower and a methanol recovery tower, wherein the top of the etherification reactor is connected with an etherification reaction preheater through a pipeline, the etherification reaction preheater is connected with a methanol pipeline and a C5 pipeline, the C5 pipeline is connected with an etherification reaction raw material heater, the bottom of the etherification reactor is connected with the catalytic distillation tower through a pipeline, the pipeline between the etherification reactor and the catalytic distillation tower is connected with a catalytic distillation tower inlet and outlet heat exchanger, and the bottom pipeline of the catalytic distillation tower is sequentially connected with the catalytic distillation tower inlet and outlet heat exchanger, the etherification reaction raw material heater and a TAME cooler.

[0009] The top pipeline of the catalytic distillation tower is connected to the extraction tower, the extraction tower is connected to the methanol recovery tower, and the top pipeline of the methanol recovery tower is sequentially connected to the catalytic distillation tower feed preheater and the methanol recovery tower top water cooler.

[0010] The catalytic distillation tower feed preheater is connected to the pipeline between the etherification reactor and the catalytic distillation tower.

[0011] The catalytic distillation tower feed preheater is arranged at the output end of the catalytic distillation tower feed and discharge heat exchanger.

[0012] The output end of the water cooler at the top of the methanol recovery tower is connected to the methanol pipeline and the methanol recovery tower respectively.

[0013] The bottom pipeline of the methanol recovery tower is connected to the extraction tower.

[0014] The feed preheater of the catalytic distillation tower is arranged at a height higher than the top water cooler of the methanol recovery tower.

[0015] The beneficial effects achieved by the utility model are:

[0016] The utility model provides an energy-saving production system for tert-amyl methyl ether, which can achieve low investment, effectively reduce steam and circulating water consumption, reduce the comprehensive energy consumption of the device, and is easy to implement on site. The specific advantages include:

[0017] (1) An etherification reaction raw material heater is set up to use hot TAME logistics to heat the cold raw material C5. The cooled TAME logistics enters the TAME cooler, and the heated raw material C5 enters the etherification reaction preheater, thereby reducing the steam consumption of the etherification reaction preheater;

[0018] (2) A catalytic distillation tower feed preheater is provided, and the gaseous methanol at the top of the methanol recovery tower is used as the heat source of the preheater to preheat the etherification reaction product entering the catalytic distillation tower, thereby increasing the temperature and vaporization fraction of the inlet material, reducing the heat load of the reboiler at the bottom of the catalytic distillation tower, and reducing the amount of heating steam for the reboiler. At the same time, the gaseous methanol at the top of the methanol recovery tower is condensed through the preheater, thereby reducing the amount of circulating water used for the water cooler at the top of the methanol recovery tower;

[0019] (3) The feed preheater of the catalytic distillation tower is arranged at a higher height than the water cooler on the top of the methanol recovery tower, ensuring that the methanol flows smoothly to the water cooler on the top of the methanol recovery tower below after condensation, and the equipment investment is low. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] The accompanying drawings are used to provide a further understanding of the present invention and constitute a part of the specification. Together with the embodiments of the present invention, they are used to explain the present invention and do not constitute a limitation of the present invention. In the accompanying drawings:

[0021] Figure 1It is a system flow chart of the utility model.

[0022] In the figure: 1. etherification reaction preheater; 2. etherification reactor; 3. catalytic distillation tower; 4. extraction tower; 5. methanol recovery tower; 6. etherification reaction raw material heater; 7. catalytic distillation tower inlet and outlet heat exchanger; 8. catalytic distillation tower feed preheater; 9. methanol recovery tower top water cooler; 10. TAME cooler. DETAILED DESCRIPTION

[0023] The preferred embodiments of the present invention are described below in conjunction with the accompanying drawings. It should be understood that the preferred embodiments described herein are only used to illustrate and explain the present invention, and are not used to limit the present invention.

[0024] Example:

[0025] like Figure 1 As shown, an energy-saving production system of tert-amyl methyl ether includes an etherification reactor 2, a catalytic distillation tower 3, an extraction tower 4 and a methanol recovery tower 5. The top of the etherification reactor 2 is connected to an etherification reaction preheater 1 through a pipeline, the etherification reaction preheater 1 is connected to a methanol pipeline and a C5 pipeline, the C5 pipeline is connected to an etherification reaction raw material heater 6, the bottom of the etherification reactor 2 is connected to the catalytic distillation tower 3 through a pipeline, the pipeline between the etherification reactor 2 and the catalytic distillation tower 3 is connected to a catalytic distillation tower inlet and outlet heat exchanger 7 and a catalytic distillation tower feed preheater 8, and the bottom pipeline of the catalytic distillation tower 3 is sequentially connected to the catalytic distillation tower inlet and outlet heat exchanger 7, the etherification reaction raw material heater 6 and a TAME cooler 10.

[0026] The top pipeline of the catalytic distillation tower 3 is connected to the extraction tower 4, the extraction tower 4 is connected to the methanol recovery tower 5, and the top pipeline of the methanol recovery tower 5 is connected to the catalytic distillation tower feed preheater 8 and the methanol recovery tower top water cooler 9 in sequence.

[0027] The output end of the methanol recovery tower top water cooler 9 is connected to the methanol pipeline and the methanol recovery tower 5 respectively.

[0028] The bottom pipeline of the methanol recovery tower 5 is connected to the extraction tower 4 .

[0029] The catalytic distillation tower feed preheater 8 is arranged at a height higher than the methanol recovery tower top water cooler 9 .

[0030] The process flow of the utility model is:

[0031] The raw material C5 and methanol are preheated in a certain proportion through the etherification reaction preheater 1 and enter the etherification reactor 2. The isopentene component in the raw material C5 reacts with methanol in the etherification reactor 2 to generate TAME. The etherification reaction product is heat exchanged with the hot TAME flowing out of the bottom of the catalytic distillation tower 3 through the catalytic distillation tower inlet and outlet heat exchanger 7, and then enters the catalytic distillation tower 3. The unreacted isopentene and methanol continue to react in the catalytic distillation tower 3. During the reaction, TAME is separated and flows out from the bottom of the catalytic distillation tower 3. The unreacted C5 and methanol at the top of the catalytic distillation tower 3 enter the bottom of the extraction tower 4 together. The methanol in the unreacted C5 is extracted with water from the bottom of the methanol recovery tower 5. The extracted C5 is sent to the tank area, and the methanol aqueous solution at the bottom of the extraction tower 4 is self-pressurized to the methanol recovery tower 5 for methanol recovery. The top of the methanol recovery tower 5 is connected to a methanol recovery tower top water cooler 9, and the methanol recovered by the methanol recovery tower top water cooler 9 is circulated back to the etherification reactor 2 for further use, and the bottom water is recycled to the top of the extraction tower 4 for further use;

[0032] Among them, an etherification reaction raw material heater 6 is set, and the hot TAME flow is used to heat the cold raw material C5, and the cooled TAME flow enters the TAME cooler 10, and the heated raw material C5 flow enters the etherification reaction preheater 1;

[0033] A catalytic distillation tower feed preheater 8 is also provided, which uses the gaseous methanol at the top of the methanol recovery tower 5 as the preheater heat source to preheat the etherification reaction product entering the catalytic distillation tower 3, thereby increasing the temperature and vaporization fraction of the material entering the catalytic distillation tower 3, reducing the heat load of the reboiler at the bottom of the catalytic distillation tower 3, and reducing the amount of heating steam for the reboiler. At the same time, the gaseous methanol at the top of the methanol recovery tower 5 is condensed by this preheater, reducing the amount of circulating water used in the water cooler 9 at the top of the methanol recovery tower.

[0034] The specific application cases of this utility model are as follows:

[0035] Case 1: Taking the cracking of C5, where the isopentene concentration is 35%, and the 70,000 tons / year TAME device as an example, after the implementation of this technical solution, the inlet temperature of the catalytic distillation tower 3 is increased from 75°C to 85°C, and the vaporization fraction is increased from 3% to 15%, which can save a total of 1t / h of heating steam for the bottom reboiler of the catalytic distillation tower 3 and steam for the etherification reaction preheater 1, and save 60t / h of circulating water for the top water cooler 9 of the methanol recovery tower and the TAME cooler 10. The comprehensive energy consumption of the device is reduced from 4333.9 tons of standard oil / year to 3741.1 tons of standard oil / year, and the energy consumption is reduced by about 13.7%.

[0036] Case 2: Taking the catalytic C5, isopentene concentration 25%, 70,000 tons / year TAME device as an example, after the implementation of this technical solution, the inlet temperature of the catalytic distillation tower 3 increased from 74°C to 81°C, and the vaporization fraction increased from 2.8% to 11.1%, which can save a total of 0.7t / h of heating steam for the bottom reboiler of the catalytic distillation tower 3 and steam for the etherification reaction preheater 1, and save 40t / h of circulating water for the methanol recovery tower top water cooler 9 and TAME cooler 10. The comprehensive energy consumption of the device was reduced from 4625.5 tons of standard oil / year to 4211.5 tons of standard oil / year, and the energy consumption was reduced by about 9%.

Claims

1. An energy-saving production system for tert-amyl methyl ether, characterized in that: The invention comprises an etherification reactor (2), a catalytic distillation tower (3), an extraction tower (4) and a methanol recovery tower (5); the top of the etherification reactor (2) is connected to an etherification reaction preheater (1) via a pipeline; the etherification reaction preheater (1) is connected to a methanol pipeline and a C5 pipeline; the C5 pipeline is connected to an etherification reaction raw material heater (6); the bottom of the etherification reactor (2) is connected to the catalytic distillation tower (3) via a pipeline; the pipeline between the etherification reactor (2) and the catalytic distillation tower (3) is connected to a catalytic distillation tower inlet and outlet heat exchanger (7); the bottom pipeline of the catalytic distillation tower (3) is connected in sequence to the catalytic distillation tower inlet and outlet heat exchanger (7), the etherification reaction raw material heater (6) and a TAME cooler (10); The top pipeline of the catalytic distillation tower (3) is connected to the extraction tower (4), the extraction tower (4) is connected to the methanol recovery tower (5), and the top pipeline of the methanol recovery tower (5) is connected in sequence to the catalytic distillation tower feed preheater (8) and the methanol recovery tower top water cooler (9); The catalytic distillation tower feed preheater (8) is connected to the pipeline between the etherification reactor (2) and the catalytic distillation tower (3).

2. The energy-saving production system of tert-amyl methyl ether according to claim 1, characterized in that: The catalytic distillation tower feed preheater (8) is arranged at the output end of the catalytic distillation tower feed and discharge heat exchanger (7).

3. The energy-saving production system of tert-amyl methyl ether according to claim 1, characterized in that: The output end of the methanol recovery tower top water cooler (9) is connected to the methanol pipeline and the methanol recovery tower (5) respectively.

4. The energy-saving production system of tert-amyl methyl ether according to claim 1, characterized in that: The bottom pipeline of the methanol recovery tower (5) is connected to the extraction tower (4).

5. The energy-saving production system of tert-amyl methyl ether according to claim 1, characterized in that: The catalytic distillation tower feed preheater (8) is arranged at a height higher than the methanol recovery tower top water cooler (9).

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