Process water waste heat recovery system for acetic ether
By setting up multiple heat exchangers and thermal coupling devices during the ethyl acetate production process, the problem of the process of water heat cannot be recovered after condensation is solved, the heat reuse and environmental protection are achieved, and energy consumption and pollution are reduced.
Patent Information
- Application Number
- CN202420333700.1
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-02-22
- Publication Date
- 2024-12-31
- Estimated Expiration
- 2034-02-22
AI Technical Summary
During the production process of ethyl acetate, the heat in the process water after condensation cannot be completely cooled, resulting in energy waste and environmental pollution, and the failure to recover waste heat.
A process water waste heat recovery system is designed. By setting up multiple heat exchangers and thermal coupling devices, the heat in the process water is converted into useful thermal energy through heat exchange and recycled to prevent direct discharge of high-calorie condensate water.
It realizes the reuse of heat, saves resources, reduces energy consumption and environmental pollution, improves heat exchange efficiency, and ensures the safety and reliability of the system.
Smart Images
Figure CN222279459U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to the technical field of chemical production, and more specifically, particularly to a process water waste heat recovery system for ethyl acetate. Background Art
[0002] Ethyl acetate, also known as ethyl acetate, is an organic compound with the chemical formula C4H8O2. It is an ester with the functional group -COOR (a double bond between carbon and oxygen) and can undergo alcoholysis, aminolysis, transesterification, reduction and other common reactions of general esters. Pure ethyl acetate is a colorless, transparent liquid with a pungent odor. It is a widely used fine chemical product with excellent solubility and quick drying properties. It has a wide range of uses. It is a very important organic chemical raw material and an excellent industrial solvent. It is widely used in the production of cellulose acetate, ethyl cellulose, chlorinated rubber, vinyl resin, cellulose acetate resin, synthetic rubber, coatings and paints; it is also used as a fragrance and solvent for pharmaceutical preparations.
[0003] In the production process of ethyl acetate, process water will be reused or directly discharged. Direct discharge after condensation will lead to energy waste, because condensation cannot completely cool the heat in the process water, causing the heat energy provided by the original resources to be wasted. At the same time, the large-scale discharge of high-calorific value condensed water will cause great damage and pollution to the environment. In addition, waste heat recovery cannot be achieved in this process, resulting in heat waste. Utility Model Content
[0004] The present application provides a process water waste heat recovery system for ethyl acetate, which solves the problem that in the production process, direct discharge of process water after condensation will lead to energy waste, because condensation cannot completely cool the heat in the process water, causing the heat energy provided by the original resource to be consumed in vain. At the same time, the large amount of high-calorific value condensed water discharged will cause great damage and pollution to the environment. In addition, waste heat recovery cannot be achieved in this process, resulting in the problem of heat waste.
[0005] The present application provides a process water waste heat recovery system for ethyl acetate, comprising a process water recovery tower, an acidic water recovery tower and an esterification tower, wherein the feed end of the esterification tower is connected to a dehydration tower top phase separator through a pipeline, the esterification tower is respectively connected to a first heat exchanger and a second heat exchanger through pipelines, the liquid outlets of the first heat exchanger and the second heat exchanger are connected to a wastewater heat exchanger through pipelines, the liquid inlets of the first heat exchanger and the second heat exchanger are connected to a process water tank through pipelines, and the gas outlets of the first heat exchanger and the second heat exchanger are respectively connected to the process water recovery tower and the acidic water recovery tower through pipelines. The top of the process water recovery tower is connected to a process water recovery tower top condenser through a pipeline, the liquid outlet of the process water recovery tower top condenser is connected to a process water recovery buffer tank, the liquid outlet of the process water recovery buffer tank is connected to a process water recovery tower top reflux pump, the process water recovery tower top reflux pump is connected to a reflux pipe, the top of the acid water recovery tower is connected to an acid recovery tower top condenser through a pipeline, the liquid outlet of the acid recovery tower top condenser is connected to the acid recovery buffer tank, the liquid outlet of the acid recovery buffer tank is connected to the acid recovery tower top reflux pump, and the acid recovery tower top reflux pump is connected to a reflux pipe.
[0006] Preferably, the discharge port of the process water recovery tower is connected to the wastewater heat exchanger through a pipeline, the liquid outlet of the wastewater heat exchanger is connected to a discharge pipe through a process water recovery tower thermal coupling pump, and one end of the discharge pipe is connected to a dehydration feed phase separator.
[0007] Preferably, the gas outlet of the wastewater heat exchanger is connected to the process water recovery tower through a pipeline.
[0008] Preferably, a process water cooler is installed on the discharge pipe.
[0009] Preferably, the discharge port of the acidic water recovery tower is connected to an acidic wastewater heat exchanger via a pipeline, and the liquid outlet of the acidic wastewater heat exchanger is connected to the dehydration feed phase separator via an acidic recovery tower thermal coupling pump.
[0010] Preferably, the dehydration feed phase separator is connected to the acidic wastewater heat exchanger through a pipeline, and the gas outlet of the acidic wastewater heat exchanger is connected to the acidic water recovery tower through a pipeline.
[0011] Preferably, the reflux pipe is connected to the dehydration tower top phase separator.
[0012] Preferably, the discharge port of the esterification tower is connected to a finished product tank via a pipeline.
[0013] It can be seen from the above technical scheme that the present application provides a process water waste heat recovery system for ethyl acetate. When in use, the process water of the dehydration tower top phase separator and the process water from the esterification tower are combined into a material, and the material No. 29 (process water) in the process water tank is recovered through the first heat exchanger and the second heat exchanger to recover the waste heat in the gas phase material. The liquid outlets of the first heat exchanger and the second heat exchanger are connected to the wastewater heat exchanger, and the gas outlets of the first heat exchanger and the wastewater heat exchanger are both connected to the process water recovery tower, and the gas outlets of the second heat exchanger and the acid wastewater heat exchanger are both connected to the acid water recovery tower. The waste heat in the gas phase material enters the process water recovery tower and the acid water recovery tower respectively in the form of steam to provide them with temperature, realize heat exchange and recover waste heat. The process has good heat exchange effect and high heat exchange efficiency.
[0014] Compared with the prior art, the beneficial effects of the utility model are:
[0015] 1. The utility model realizes heat exchange and recovers waste heat by setting a heat exchanger, converts and reuses the heat in the process water after the reaction, saves resources and reduces costs.
[0016] 2. The utility model converts the waste heat of process water generated in the production process of ethyl acetate into useful thermal energy through a heat exchange device, preventing the direct discharge of condensed water containing high heat, thereby reducing energy consumption and environmental pollution.
[0017] 3. The utility model sets a plurality of thermally coupled heat exchangers to prevent cross leakage between gas and supplied liquid materials, which is safe and reliable.
[0018] In summary, a process water waste heat recovery system for ethyl acetate converts the process water waste heat generated in the production process of ethyl acetate into useful thermal energy through a heat exchange device, prevents the direct discharge of condensed water containing high heat, thereby reducing energy consumption and environmental pollution. A heat exchanger is set to realize heat exchange for waste heat recovery, and the heat in the process water after the reaction is converted and reused, saving resources and reducing costs. In addition, multiple thermally coupled heat exchangers prevent cross leakage between gas and supplied liquid materials, which is safe and reliable. BRIEF DESCRIPTION OF THE DRAWINGS
[0019] In order to more clearly illustrate the technical solution of the present invention, the following briefly introduces the drawings required for use in the embodiments. Obviously, for ordinary technicians in this field, other drawings can be obtained based on these drawings without inventiveness.
[0020] Figure 1 The utility model is a schematic diagram of a process water waste heat recovery system for ethyl acetate.
[0021] The reference numerals in the specific implementation manner are as follows:
[0022] 1. Process water recovery tower; 2. Acidic water recovery tower; 3. Esterification tower; 4. First heat exchanger; 5. Second heat exchanger; 6. Dehydration tower top phase separator; 7. Dehydration feed phase separator; 8. Process water recovery buffer tank; 9. Process water recovery tower top reflux pump; 10. Process water recovery tower top condenser; 11. Process water recovery reboiler; 12. Waste water heat exchanger; 13. Process water recovery tower thermal coupling pump; 14. Acidic recovery buffer tank; 15. Acidic recovery tower top reflux pump; 16. Acidic recovery tower top condenser; 17. Acidic recovery reboiler; 18. Acidic waste water heat exchanger; 19. Acidic recovery tower thermal coupling pump; 20. Process water cooler; 21. Process water tank; 22. Finished product tank; 23. Reflux pipe; 24. Discharge pipe. DETAILED DESCRIPTION
[0023] In order to enable those skilled in the art to better understand the technical solutions in the present invention, the technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the accompanying drawings.
[0024] See also Figure 1, a process water waste heat recovery system for ethyl acetate. This application aims to solve the problem that in the production process, direct discharge of process water after condensation will lead to energy waste, because condensation cannot completely cool the heat in the process water, resulting in the waste of heat energy provided by the original resources. At the same time, a large amount of condensed water with high calorific value will cause great damage and pollution to the environment. In addition, waste heat recovery cannot be achieved in this process, and there is a problem of heat waste. A process water waste heat recovery system for ethyl acetate is proposed. The waste heat of process water generated in the production process of ethyl acetate is converted into useful thermal energy through a heat exchange device, and the high-calorie condensed water is prevented from being directly discharged, thereby reducing energy consumption and environmental pollution. A heat exchanger is set to realize heat exchange for waste heat recovery, and the heat in the process water after the reaction is converted and reused, saving resources and reducing costs. In addition, multiple thermally coupled heat exchangers prevent cross leakage between gas and supplied liquid materials, which is safe and reliable. Specifically, a process water waste heat recovery system for ethyl acetate comprises a process water recovery tower 1, an acid water recovery tower 2 and an esterification tower 3, the discharge port of the esterification tower 3 is connected to a finished product tank 22 through a pipeline, and the finished product material after the reaction in the esterification tower 3 can enter the finished product tank 22 through the pipeline; the feed end of the esterification tower 3 is connected to a dehydration tower top phase separator 6 through a pipeline, the esterification tower 3 is respectively connected to a first heat exchanger 4 and a second heat exchanger 5 through pipelines, the liquid outlets of the first heat exchanger 4 and the second heat exchanger 5 are connected to a wastewater heat exchanger 12 through pipelines, the wastewater heat exchanger 12 converts the waste heat in the wastewater material into gas phase heat and supplies it to the process water recovery tower 1, the liquid inlets of the first heat exchanger 4 and the second heat exchanger 5 are connected to a process water tank 21 through pipelines, and the gas outlets of the first heat exchanger 4 and the second heat exchanger 5 are connected to a process water tank 21 through pipelines. The process water recovery tower 1 and the acidic water recovery tower 2 are connected by pipelines respectively. The process water from the dehydration tower top phase separator 6 and the process water from the esterification tower 3 form a material, and the material No. 29 (process water) in the process water tank 21 passes through the first heat exchanger 4 and the second heat exchanger 5 to recover the waste heat in the gas phase material. The liquid outlets of the first heat exchanger 4 and the second heat exchanger 5 are connected to the waste water heat exchanger 12. The gas outlets of the first heat exchanger 4 and the waste water heat exchanger 12 are both connected to the process water recovery tower 1. The gas outlets of the second heat exchanger 5 and the acidic waste water heat exchanger 18 are both connected to the acidic water recovery tower 2. The waste heat in the gas phase material enters the process water recovery tower 1 and the acidic water recovery tower 2 in the form of steam, respectively, to provide temperature for them, realize heat exchange and recover waste heat. The heat exchange effect of this process is good and the heat exchange efficiency is high.
[0025] The top of the process water recovery tower 1 is connected to a process water recovery tower top condenser 10 through a pipeline, the liquid outlet of the process water recovery tower top condenser 10 is connected to a process water recovery buffer tank 8, the liquid outlet of the process water recovery buffer tank 8 is connected to a process water recovery tower top reflux pump 9, the process water recovery tower top reflux pump 9 is connected to a reflux pipe 23, the gaseous material of the process water recovery tower 1 is cooled from the top of the process water recovery tower 1 by the process water recovery tower top condenser 10 and enters the process water recovery buffer tank 8, and then is pumped into the reflux pipe 23 by the process water recovery tower top reflux pump 9; the top of the acid water recovery tower 2 is connected to an acid recovery tower top condenser 16 through a pipeline, and the acid recovery tower top condenser The liquid outlet of the device 16 is connected to the acid recovery buffer tank 14, the liquid outlet of the acid recovery buffer tank 14 is connected to the acid recovery tower top reflux pump 15, the acid recovery tower top reflux pump 15 is connected to the reflux pipe 23, the reflux pipe 23 is connected to the dehydration tower top phase separator 6, the gas phase material of the acid water recovery tower 2 is cooled by the acid recovery tower top condenser 16 from the top of the acid water recovery tower 2 and enters the acid recovery buffer tank 14, and then is pumped into the reflux pipe 23 by the acid recovery tower top reflux pump 15, the reflux pipe 23 is connected to the dehydration tower top phase separator 6, and the dehydration tower top phase separator 6 is connected to the esterification tower 3 through a pipeline. The circular process route realizes resource recycling and saves resources.
[0026] The discharge port of the process water recovery tower 1 is connected to the wastewater heat exchanger 12 through a pipeline, and the liquid outlet of the wastewater heat exchanger 12 is connected to the discharge pipe 24 through the process water recovery tower thermal coupling pump 13. The material coming out of the discharge port of the process water recovery tower 1 passes through the wastewater heat exchanger 12, and the converted process water flows out from the liquid outlet of the wastewater heat exchanger 12 through the process water recovery tower thermal coupling pump 13 and enters the discharge pipe 24. One end of the discharge pipe 24 is connected to the dehydration feed phase separator 7, and the process water cooler 20 is installed on the discharge pipe 24. The process water flows out from the discharge pipe 24 and passes through the process water cooler 20 After cooling, it flows into the dehydration feed phase separator 7. The gas outlet of the wastewater heat exchanger 12 is connected to the process water recovery tower 1 through a pipeline. The waste heat converted in the wastewater heat exchanger 12 enters the process water recovery tower 1 along the pipeline through the gas outlet of the wastewater heat exchanger 12, providing temperature for it, realizing heat exchange and waste heat recovery; the discharge port of the acidic water recovery tower 2 is connected to the acidic wastewater heat exchanger 18 through a pipeline, and the liquid outlet of the acidic wastewater heat exchanger 18 is connected to the dehydration feed phase separator 7 through the acidic recovery tower thermal coupling pump 19. The material coming out of the discharge port of the acidic water recovery tower 2 After passing through the acid wastewater heat exchanger 18, the converted acidic water flows out from the liquid outlet of the acid wastewater heat exchanger 18 and enters the discharge pipe 24 through the acid recovery tower heat coupling pump 19. The acidic water flows out from the discharge pipe 24 and is cooled by the process water cooler 20 and then flows into the dehydration feed phase separator 7; the dehydration feed phase separator 7 is connected to the acid wastewater heat exchanger 18 through a pipeline, and the material in the dehydration feed phase separator 7 first enters the acid wastewater heat exchanger 18 through a pipeline, and the process water converted by the acid wastewater heat exchanger 18 flows out from the liquid outlet of the acid wastewater heat exchanger 18 to the discharge pipe. 24, the gas outlet of the acidic wastewater heat exchanger 18 is connected to the acidic water recovery tower 2 through a pipeline, and the waste heat converted in the acidic wastewater heat exchanger 18 enters the acidic water recovery tower 2 along the pipeline through the gas outlet of the acidic wastewater heat exchanger 18, providing temperature for it, realizing heat exchange and waste heat recovery; multiple heat exchangers are set to prevent cross leakage between the gas and the supplied liquid material, which is safe and reliable, and converts the process water waste heat generated in the ethyl acetate production process into useful thermal energy, preventing the direct discharge of high-calorie condensed water, thereby reducing energy consumption and environmental pollution.
[0027] It can be seen from the above technical scheme that a process water waste heat recovery system for ethyl acetate is provided. When in use, the process water from the dehydration tower top phase separator 6 and the process water from the esterification tower 3 form a material, and the material No. 29 (process water) in the process water tank 21 passes through the first heat exchanger 4 and the second heat exchanger 5 to recover the waste heat in the gas phase material. The liquid outlets of the first heat exchanger 4 and the second heat exchanger 5 are connected to the waste water heat exchanger 12, and the gas outlets of the first heat exchanger 4 and the waste water heat exchanger 12 are both connected to the process water recovery tower 1, and the gas outlets of the second heat exchanger 5 and the acid waste water heat exchanger 18 are both connected to the acid water recovery tower 2. The waste heat in the gas phase material enters the process water recovery tower 1 and the acid water recovery tower 2 respectively in the form of steam to provide temperature for them, realize heat exchange and recover waste heat. The heat exchange effect of this process is good and the heat exchange efficiency is high.
[0028] Those skilled in the art will readily come up with other embodiments of the present invention after considering the specification and practicing the application disclosed herein. The present invention is intended to cover any variation, use or adaptation of the present invention, which follows the general principles of the present invention and includes common knowledge or customary technical means in the art disclosed by the present invention. The specification and examples are to be regarded as exemplary only, and the true scope of the present invention is indicated by the claims.
[0029] It should be understood that the present invention is not limited to the precise structure described above and shown in the drawings, and various modifications and changes can be made without departing from its scope. The above-described embodiments of the present invention do not constitute a limitation on the scope of protection of the present invention.
Claims
1. A process water waste heat recovery system for ethyl acetate, characterized in that: The invention comprises a process water recovery tower (1), an acidic water recovery tower (2) and an esterification tower (3), wherein the feed end of the esterification tower (3) is connected to a dehydration tower top phase separator (6) through a pipeline, the esterification tower (3) is connected to a first heat exchanger (4) and a second heat exchanger (5) through pipelines, respectively, the liquid outlets of the first heat exchanger (4) and the second heat exchanger (5) are connected to a wastewater heat exchanger (12) through pipelines, the liquid inlets of the first heat exchanger (4) and the second heat exchanger (5) are connected to a process water tank (21) through pipelines, the gas outlets of the first heat exchanger (4) and the second heat exchanger (5) are connected to the process water recovery tower (1) and the acidic water recovery tower (2) through pipelines, respectively, and the process water recovery tower (1) The top of the tower is connected to a process water recovery tower top condenser (10) through a pipeline, the liquid outlet of the process water recovery tower top condenser (10) is connected to a process water recovery buffer tank (8), the liquid outlet of the process water recovery buffer tank (8) is connected to a process water recovery tower top reflux pump (9), the process water recovery tower top reflux pump (9) is connected to a reflux pipe (23), the top of the acid water recovery tower (2) is connected to an acid recovery tower top condenser (16) through a pipeline, the liquid outlet of the acid recovery tower top condenser (16) is connected to an acid recovery buffer tank (14), the liquid outlet of the acid recovery buffer tank (14) is connected to an acid recovery tower top reflux pump (15), and the acid recovery tower top reflux pump (15) is connected to a reflux pipe (23).
2. The process water waste heat recovery system for ethyl acetate according to claim 1, characterized in that: The discharge port of the process water recovery tower (1) is connected to the wastewater heat exchanger (12) via a pipeline, and the liquid outlet of the wastewater heat exchanger (12) is connected to a discharge pipe (24) via a process water recovery tower thermal coupling pump (13), and one end of the discharge pipe (24) is connected to a dehydration feed phase separator (7).
3. The process water waste heat recovery system for ethyl acetate according to claim 2, characterized in that: The gas outlet of the wastewater heat exchanger (12) is connected to the process water recovery tower (1) through a pipeline.
4. The process water waste heat recovery system for ethyl acetate according to claim 2, characterized in that: A process water cooler (20) is installed on the discharge pipe (24).
5. The process water waste heat recovery system for ethyl acetate according to claim 2, characterized in that: The discharge port of the acidic water recovery tower (2) is connected to the acidic wastewater heat exchanger (18) via a pipeline, and the liquid outlet of the acidic wastewater heat exchanger (18) is connected to the dehydration feed phase separator (7) via an acidic recovery tower thermal coupling pump (19).
6. The process water waste heat recovery system for ethyl acetate according to claim 5, characterized in that: The dehydration feed phase separator (7) is connected to the acid wastewater heat exchanger (18) through a pipeline, and the gas outlet of the acid wastewater heat exchanger (18) is connected to the acid water recovery tower (2) through a pipeline.
7. The process water waste heat recovery system for ethyl acetate according to claim 1, characterized in that: The reflux pipe (23) is connected to the dehydration tower top phase separator (6).
8. The process water waste heat recovery system for ethyl acetate according to claim 1, characterized in that: The discharge port of the esterification tower (3) is connected to a finished product tank (22) via a pipeline.