CN215352059U - A kind of hydrogen peroxide heat pump rectification device - Google Patents
A kind of hydrogen peroxide heat pump rectification device Download PDFInfo
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- CN215352059U CN215352059U CN202121580150.6U CN202121580150U CN215352059U CN 215352059 U CN215352059 U CN 215352059U CN 202121580150 U CN202121580150 U CN 202121580150U CN 215352059 U CN215352059 U CN 215352059U
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- outlet
- film evaporator
- inlet
- falling film
- hydrogen peroxide
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- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 title claims abstract description 62
- 239000011552 falling film Substances 0.000 claims abstract description 59
- 239000007789 gas Substances 0.000 claims abstract description 42
- 239000007788 liquid Substances 0.000 claims abstract description 28
- 239000000463 material Substances 0.000 claims abstract description 16
- 238000004519 manufacturing process Methods 0.000 claims abstract description 5
- 239000010408 film Substances 0.000 claims abstract 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- 238000010992 reflux Methods 0.000 claims description 3
- 238000000605 extraction Methods 0.000 description 10
- 238000005265 energy consumption Methods 0.000 description 5
- 238000000034 method Methods 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 238000003809 water extraction Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000012824 chemical production Methods 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007907 direct compression Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- QOSATHPSBFQAML-UHFFFAOYSA-N hydrogen peroxide;hydrate Chemical compound O.OO QOSATHPSBFQAML-UHFFFAOYSA-N 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000004804 winding Methods 0.000 description 1
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
本实用新型公开了一种双氧水热泵精馏装置，包括有精馏塔、降膜蒸发器和预热器，其特征在于：预热器的进口连接有稀双氧水进料管路，预热器的出口连接降膜蒸发器的物料进口，降膜蒸发器的蒸汽出口连接精馏塔塔底的气体进口，精馏塔塔底的液体出口连接降膜蒸发器的液体进口；降膜蒸发器底部的液体出口连接有强制循环泵，强制循环泵的出口分别连接降膜蒸发器顶部的进液口与预热器的另一进口，预热器的另一出口连接有浓双氧水采出管路，降膜蒸发器的冷凝液出口连接缓冲罐的液体进口；精馏塔顶部的气体出口连接压缩机的气体进口，压缩机的气体出口连接降膜蒸发器的气体进口，降膜蒸发器上还设有生蒸汽进口。本实用新型节能降耗、节约成本。
The utility model discloses a hydrogen peroxide heat pump rectification device, comprising a rectification tower, a falling film evaporator and a preheater. The utility model is characterized in that: the inlet of the preheater is connected with a dilute hydrogen peroxide feed pipeline, and the The outlet is connected to the material inlet of the falling film evaporator, the vapor outlet of the falling film evaporator is connected to the gas inlet at the bottom of the rectification tower, and the liquid outlet at the bottom of the rectification tower is connected to the liquid inlet of the falling film evaporator; The liquid outlet is connected with a forced circulation pump, and the outlet of the forced circulation pump is respectively connected with the liquid inlet at the top of the falling film evaporator and the other inlet of the preheater, and the other outlet of the preheater is connected with the production pipeline of concentrated hydrogen peroxide. The condensate outlet of the film evaporator is connected to the liquid inlet of the buffer tank; the gas outlet at the top of the rectification tower is connected to the gas inlet of the compressor, and the gas outlet of the compressor is connected to the gas inlet of the falling film evaporator. The falling film evaporator is also provided with Raw steam inlet. The utility model saves energy, reduces consumption, and saves cost.
Description
Technical Field
The utility model relates to the technical field of hydrogen peroxide rectification, in particular to an improved hydrogen peroxide heat pump rectification device.
Background
Rectification is used as the most widely and important mass transfer separation operation unit in the chemical production process, and more than 90% of the product is proposed and recovered by rectification, 40-70% of the energy consumption in the chemical production process is used for separation, and the rectification energy consumption accounts for more than 90% of the energy consumption. Although the rectification technology is quite mature and widely applied, energy conservation and emission reduction are vigorously advocated in China, and energy conservation in the rectification process is more and more concerned. Most of the existing hydrogen peroxide concentration adopts a conventional rectification mode, so that the treatment capacity is large, the energy consumption is high, a new technology is urgently needed to reduce the energy consumption and save the operation cost.
The heat pump rectification is based on the principle of a heat pump, the steam coming out of the tower top does not need to be condensed, the temperature and the pressure of the steam are directly increased through a compressor, the enthalpy value of the steam is increased, then the steam is used as a heat source of a reboiler to heat materials, the latent heat of the steam at the tower top is fully utilized, the consumption of the generated steam is reduced, and the operation cost is reduced. According to different external energy consumed by the heat pump, the heat pump rectification mode includes indirect heat pump rectification, tower top gas direct compression type heat pump rectification, split heat pump rectification, flash distillation reboiler type heat pump rectification and the like. The application of the energy-saving technology can bring greater economic benefits for enterprises.
SUMMERY OF THE UTILITY MODEL
The utility model aims to overcome the defects of the prior art and provide the hydrogen peroxide heat pump rectifying device which is energy-saving, consumption-reducing and cost-saving.
In order to solve the technical problems, the utility model is realized by adopting the following technical scheme: the hydrogen peroxide solution heat pump rectifying device comprises a rectifying tower, a falling film evaporator and a preheater, and is characterized in that: an inlet of the preheater is connected with a dilute hydrogen peroxide feeding pipeline, an outlet of the preheater is connected with a material inlet of the falling-film evaporator, a steam outlet of the falling-film evaporator is connected with a gas inlet at the bottom of the rectifying tower, and a liquid outlet at the bottom of the rectifying tower is connected with a liquid inlet of the falling-film evaporator; a liquid outlet at the bottom of the falling-film evaporator is connected with a forced circulation pump, an outlet of the forced circulation pump is respectively connected with a liquid inlet at the top of the falling-film evaporator and the other inlet of the preheater through a forced circulation return pipeline and a forced circulation extraction pipeline, the other outlet of the preheater is connected with a concentrated hydrogen peroxide extraction pipeline, a condensate outlet of the falling-film evaporator is connected with a liquid inlet of a buffer tank, a liquid outlet at the bottom of the buffer tank is connected with a return pump, an outlet of the return pump is respectively connected with a water extraction pipeline and a return port at the top of the rectifying tower, and a gas outlet at the top of the buffer tank is connected with a vacuum system; and a gas outlet at the top of the rectifying tower is connected with a gas inlet of a compressor, a gas outlet of the compressor is connected with a gas inlet of the falling film evaporator, and the falling film evaporator is also provided with a raw steam inlet.
Preferably, a gas outlet at the top of the buffer tank is connected with a condenser, a gas outlet of the condenser is connected with a vacuum system, and an outlet of the condenser is connected with a receiving tank.
Preferably, the compressor is a centrifugal compressor, a roots compressor or a screw compressor.
Preferably, the preheater adopts a spiral winding tube type heat exchanger, a shell and tube type heat exchanger, a spiral plate type heat exchanger or a plate type heat exchanger.
Preferably, the condenser adopts a spiral wound tube type heat exchanger, a shell and tube type heat exchanger, a spiral plate type heat exchanger or a plate type heat exchanger.
Preferably, the system operation pressure of the falling film evaporator is 5-50kPa absolute and the compressor pressure ratio is 1-5.
The improved hydrogen peroxide heat pump rectifying device has the advantages that steam at the top of the rectifying tower is pressurized and heated by the compressor to be used as a heat source of the falling film evaporator, the consumption of raw steam of the falling film evaporator is greatly reduced, the raw steam is saved by more than 90%, the total energy saving of the system is more than 50%, the energy saving effect is remarkable, a large amount of operating cost is saved, and the practical economic value is brought to enterprises.
Drawings
The following describes embodiments of the present invention in further detail with reference to the accompanying drawings.
FIG. 1 is a schematic structural diagram of the present invention.
In the figure: 1. a preheater; 2. a falling film evaporator; 3. a rectifying tower; 4. a buffer tank; 5. a forced circulation pump; 6. a reflux pump; 7. a compressor; 8. a condenser; 9. a receiving tank; 11. a dilute hydrogen peroxide feeding pipeline; 12. a concentrated hydrogen peroxide extraction pipeline; 13. a condensate line; 14. a material steam pipeline; 15. a liquid return line; 16. a vacuum line; 17. a vacuum system; 18. a return line; 19. a water production line; 20. a raw steam heating pipeline; 21. a forced circulation return line; 22. and forcibly circulating the extraction pipeline.
Detailed Description
The drawings show the structure of the utility model, and the details thereof are further described below with reference to the drawings. In the embodiment, the hydrogen peroxide heat pump rectifying device comprises a rectifying tower 3, a falling-film evaporator 2 and a preheater 1, wherein an inlet of the preheater 1 is connected with a dilute hydrogen peroxide feeding pipeline 11, an outlet of the preheater 1 is connected with a material inlet of the falling-film evaporator 2, a steam outlet of the falling-film evaporator 2 is connected with a gas inlet at the bottom of the rectifying tower 3, and a liquid outlet at the bottom of the rectifying tower 3 is connected with a liquid inlet of the falling-film evaporator 2; a liquid outlet at the bottom of the falling-film evaporator 2 is connected with a forced circulation pump 5, an outlet of the forced circulation pump 5 is respectively connected with a liquid inlet at the top of the falling-film evaporator 2 and another inlet of the preheater 1 through a forced circulation return pipeline 21 and a forced circulation extraction pipeline 22, another outlet of the preheater 1 is connected with a concentrated hydrogen peroxide extraction pipeline 12, a condensate outlet of the falling-film evaporator 2 is connected with a liquid inlet of the buffer tank 4, a liquid outlet at the bottom of the buffer tank 4 is connected with a return pump 6, an outlet of the return pump 6 is respectively connected with a water extraction pipeline 19 and a return port at the top of the rectifying tower 3, and a gas outlet at the top of the buffer tank 4 is connected with a vacuum system 17; the gas outlet at the top of the rectifying tower 3 is connected with the gas inlet of a compressor 7, the gas outlet of the compressor 7 is connected with the gas inlet of the falling film evaporator 2, the falling film evaporator 2 is also provided with a raw steam inlet, and the raw steam inlet is connected with raw steam through a raw steam heating pipeline 20.
As a further improved specific embodiment, a condenser 8 is connected to a gas outlet at the top of the buffer tank 4, a vacuum system 17 is connected to a gas outlet of the condenser 8, and a receiving tank 9 is connected to an outlet of the condenser 8. The condenser 8 is arranged to reduce the temperature of the gas exiting the buffer tank 4.
As a more improved embodiment, the compressor 7 is a centrifugal compressor, a roots compressor or a screw compressor.
As a further improved specific embodiment, the preheater 1 adopts a spiral wound tube type heat exchanger, a shell and tube type heat exchanger, a spiral plate type heat exchanger or a plate type heat exchanger.
In a further improved embodiment, the condenser 8 is a spiral wound tube heat exchanger, a shell and tube heat exchanger, a spiral plate heat exchanger or a plate heat exchanger.
As a further improved specific embodiment, the system operation pressure of the falling-film evaporator 2 is 5-50kPa absolute, the pressure ratio of a compressor is 1-5, the compressor compresses gas discharged from the top of the rectifying tower 3 at the pressure ratio of 1-5, and the pressure of gas discharged from the outlet of the compressor is consistent with the system operation pressure of the falling-film evaporator 2.
The specific process implementation steps of the utility model are described as follows:
in the first embodiment, 30% of dilute hydrogen peroxide water flow 26t/h enters the preheater 1 through the dilute hydrogen peroxide feeding pipeline 11, and flows into the falling film evaporator 2 after being preheated to 45 ℃ by the preheater 1, the system heats and gasifies the material in the falling film evaporator 2 through the raw steam 20 when the system is started, the absolute pressure of the system is 10kPa, the evaporation temperature of the falling film evaporator 2 is 55 ℃, the evaporated gas enters the rectifying tower 3 from the falling film evaporator 2 through the material steam pipeline 14, the liquid at the bottom of the rectifying tower 3 flows back into the falling film evaporator 2 through the liquid return pipeline 15, the gas at the top of the rectifying tower 3 enters the compressor 7, the temperature of the gas entering the compressor is 45 ℃, the gas is pressurized and heated by the compressor 7, the gas is changed into 75 ℃ steam and enters the falling film evaporator 2 for heat exchange, the system does not need the raw steam to heat the falling film evaporator 2 after normal operation, the condensate after heat exchange enters the buffer tank 4 from the falling film evaporator 2 through the cold condensation water pipeline 13, the buffer tank 4 is connected with a vacuum pipeline 16, the vacuum pipeline 16 is connected with a condenser 8, the condenser 8 is connected with a vacuum system 17, the whole system is evaporated and rectified under negative pressure through the vacuum system 17, condensate water in the condenser 8 flows into a receiving tank 9, part of the condensate water in the buffer tank 4 flows back into a rectifying tower 3 through a return pipeline 18 through a return pump 6, the return flow rate is 3.5t/h, part of the condensate water flows out 12.2t/h through a water extraction pipeline 19, part of materials in the falling-film evaporator 2 flows back into the top of the falling-film evaporator 2 through a forced circulation return pipeline 21 through a forced circulation pump 5, and part of the materials are extracted out to the preheater 1 through a forced circulation extraction pipeline 22 and exchange heat with feeding materials, the extraction flow rate is 13.8t/h, and the concentration of hydrogen peroxide is 55%.
In the second embodiment, 27% of the flow rate of the dilute hydrogen peroxide enters the preheater 1 through the dilute hydrogen peroxide feeding pipeline 11, the dilute hydrogen peroxide enters the falling film evaporator 2 after being preheated to 45 ℃ by the preheater 1, the material in the falling film evaporator 2 is heated and gasified by the raw steam 20 when the system is started, the absolute pressure of the system is 10kPa, the evaporation temperature of the falling film evaporator 2 is 55 ℃, the evaporated gas enters the rectifying tower 3 from the falling film evaporator 2 through the material steam pipeline 14, the liquid at the bottom of the rectifying tower 3 reflows into the falling film evaporator 2 through the liquid reflowing pipeline 15, the gas at the top of the rectifying tower 3 enters the compressor 7, the temperature of the gas entering the compressor is 45 ℃, the gas is changed into 75 ℃ steam after being pressurized and heated by the compressor 7, the steam enters the falling film evaporator 2 for heat exchange, the condensate after the heat exchange enters the buffer tank 4 from the falling film evaporator 2 through the water condensing pipeline 13, the vacuum pipeline 16 is connected to the buffer tank 4, and the vacuum pipeline 16 is connected with the condenser 8, the condenser 8 is connected with a vacuum system 17, the whole system is evaporated and rectified under negative pressure through the vacuum system 17, condensate water in the condenser 8 flows into the receiving tank 9, part of the condensate water in the buffer tank 4 flows back into the rectifying tower 3 through a return pipeline 18 through a return pump 6, the reflux flow is 1.1t/h, part of the condensate water flows out 9.0t/h through a water extraction pipeline 19, part of materials in the falling-film evaporator 2 flows back into the top of the falling-film evaporator 5 through a forced circulation return pipeline 21 through a forced circulation pump 5, and part of the materials are extracted out of the preheater 1 through a forced circulation extraction pipeline 22, and after heat exchange with feeding materials, the extraction flow is 11.9t/h, and the concentration of hydrogen peroxide is 50%.
In summary, the above description is only a preferred embodiment of the present invention, and is not intended to limit the scope of the present invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (6)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121580150.6U CN215352059U (en) | 2021-07-13 | 2021-07-13 | A kind of hydrogen peroxide heat pump rectification device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121580150.6U CN215352059U (en) | 2021-07-13 | 2021-07-13 | A kind of hydrogen peroxide heat pump rectification device |
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| Publication Number | Publication Date |
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| CN215352059U true CN215352059U (en) | 2021-12-31 |
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| CN202121580150.6U Withdrawn - After Issue CN215352059U (en) | 2021-07-13 | 2021-07-13 | A kind of hydrogen peroxide heat pump rectification device |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113509743A (en) * | 2021-07-13 | 2021-10-19 | 浙江亚光科技股份有限公司 | Hydrogen peroxide solution heat pump rectifier unit |
| CN118925424A (en) * | 2024-09-26 | 2024-11-12 | 江西世龙实业股份有限公司 | A hydrazine hydrate tail gas treatment system and method |
| CN119056189A (en) * | 2024-09-26 | 2024-12-03 | 江西世龙实业股份有限公司 | A tail gas treatment system and method for producing 80% hydrazine hydrate by distillation and purification |
-
2021
- 2021-07-13 CN CN202121580150.6U patent/CN215352059U/en not_active Withdrawn - After Issue
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113509743A (en) * | 2021-07-13 | 2021-10-19 | 浙江亚光科技股份有限公司 | Hydrogen peroxide solution heat pump rectifier unit |
| CN113509743B (en) * | 2021-07-13 | 2025-03-21 | 浙江亚光科技股份有限公司 | A hydrogen peroxide heat pump distillation device |
| CN118925424A (en) * | 2024-09-26 | 2024-11-12 | 江西世龙实业股份有限公司 | A hydrazine hydrate tail gas treatment system and method |
| CN119056189A (en) * | 2024-09-26 | 2024-12-03 | 江西世龙实业股份有限公司 | A tail gas treatment system and method for producing 80% hydrazine hydrate by distillation and purification |
| CN118925424B (en) * | 2024-09-26 | 2025-04-11 | 江西世龙实业股份有限公司 | A hydrazine hydrate tail gas treatment system and method |
| CN119056189B (en) * | 2024-09-26 | 2025-04-25 | 江西世龙实业股份有限公司 | Tail gas treatment system and method for producing 80% hydrazine hydrate by rectification and purification |
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