CN218821743U - Solvent condensate recovery device for vacuum system - Google Patents
Solvent condensate recovery device for vacuum system Download PDFInfo
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- CN218821743U CN218821743U CN202222799932.XU CN202222799932U CN218821743U CN 218821743 U CN218821743 U CN 218821743U CN 202222799932 U CN202222799932 U CN 202222799932U CN 218821743 U CN218821743 U CN 218821743U
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Abstract
The utility model relates to a menstruum condensate recovery unit, concretely relates to a menstruum condensate recovery unit for vacuum system, the rate of recovery that exists organic menstruum condensate for solving among the prior art is low to lead to the high and polluted environment of manufacturing cost to and water replenishing tank sets up the weak point that increases occupation of land and equipment cost alone. A solvent condensate recovery device for a vacuum system comprises a primary recovery unit, a secondary recovery unit and a tertiary recovery unit, wherein the primary recovery unit and the secondary recovery unit are sequentially connected to an inlet of a liquid ring pump, an outlet of the liquid ring pump is connected with the tertiary recovery unit, the tertiary recovery unit comprises a water supplementing separation device, the water supplementing separation device comprises a liquid inlet cavity and a separation cavity, an outlet of the liquid ring pump is communicated with the separation cavity and used for gas-liquid separation, and the liquid inlet cavity is communicated with a liquid inlet of the liquid ring pump and used for supplementing liquid in the liquid ring pump; and cooling the vacuumized gas, condensing the solvent in the vacuumized gas, recovering the solvent and discharging the condensed solvent.
Description
Technical Field
The utility model relates to a menstruum condensate recovery unit, concretely relates to a menstruum condensate recovery unit for vacuum system.
Background
In an organic reaction vacuum system, the vacuumized gas comprises a volatile solvent during vacuumization, so that the gas cannot be directly discharged, and the solvent condensate needs to be recovered and then discharged. As shown in fig. 1, a solvent condensate recovery device of an existing vacuum system is provided with a heat exchanger 102, a vacuum buffer tank 103, a liquid ring pump 104 and a gas-water separator 105, wherein the liquid ring pump 104 is used for vacuumizing a device 101 to be vacuumized, and because the vacuumized gas contains volatile solvents, the heat exchanger 102 is arranged for cooling the vacuumized gas, condensing and recovering the solvents to the vacuum buffer tank 103, and finally discharging the vacuumized gas through the liquid ring pump 104 and the gas-water separator 105, and the liquid ring pump 104 is provided with an independent water replenishing tank 106 for replenishing water.
In the prior art, a primary heat exchanger is arranged for condensation, only part of solvent condensate can be recovered, and other unrecovered solvents are directly discharged, so that the production cost is increased, and the direct discharge can cause environmental pollution; meanwhile, the water replenishing tank of the liquid ring pump and the gas-water separator are separately arranged, so that the equipment occupies a large area and has higher equipment cost.
SUMMERY OF THE UTILITY MODEL
The utility model aims at solving the problem that the recovery rate of the organic solvent condensate is low in the prior art, so that the production cost is high and the environment is polluted, and the water supplementing tank is independently arranged to increase the defects of land occupation and equipment cost, so as to provide a solvent condensate recovery device for a vacuum system.
In order to achieve the above object, the present invention provides the following technical solutions:
a solvent condensate recovery device for a vacuum system comprises a primary recovery unit and a liquid ring pump, wherein the primary recovery unit comprises a primary heat exchanger and a vacuum buffer tank which are sequentially connected, a gas inlet and a gas outlet are formed in the vacuum buffer tank, and the vacuum buffer tank is used for recovering part of solvent condensate;
the inlet of the primary heat exchanger is connected with a device to be vacuumized, and the outlet of the primary heat exchanger is connected with the gas inlet of the vacuum buffer tank, and the primary heat exchanger is characterized in that: the device also comprises a secondary recovery unit and a tertiary recovery unit;
the secondary recovery unit comprises a secondary heat exchanger, and an inlet of the secondary heat exchanger is connected with a gas outlet of the vacuum buffer tank; the three-stage recovery unit comprises a water supplementing separation device, a circulating pump and a tail gas heat exchanger; the water supplementing separation device comprises a tank body and a partition plate arranged in the tank body, the partition plate divides the lower space in the tank body into a liquid inlet cavity and a separation cavity, and the upper space is communicated and provided with an evacuation port; the inlet of the liquid ring pump is communicated with the outlet of the secondary heat exchanger; the inlet of the tail gas heat exchanger is communicated with an exhaust port, and the outlet of the tail gas heat exchanger is communicated with the atmosphere;
the liquid inlet cavity is provided with a liquid ring pump liquid supply port, a circulating liquid inlet, a supplement port and a drain port, the separation cavity is provided with an air inlet and a liquid outlet, the air inlet is communicated with the outlet of the liquid ring pump, the liquid ring pump liquid supply port is communicated with the liquid inlet of the liquid ring pump, the supplement port is used for inputting a solvent for dissolving a solvent, and the liquid in the liquid inlet cavity overflows to the separation cavity through the partition plate; the liquid outlet and the drain port are both communicated with an inlet of a circulating pump, an outlet of the circulating pump is communicated with a circulating liquid inlet, a drain port is also arranged at an outlet of the circulating pump, and the outlet of the circulating pump is communicated with the circulating liquid inlet and/or the drain port through valve adjustment;
the liquid ring pump is used for vacuumizing the equipment to be vacuumized, the primary recovery unit and the secondary recovery unit, and after a gas-liquid mixture at the outlet of the liquid ring pump is subjected to gas-liquid separation through the separation cavity, gas is discharged from the outlet of the tail gas heat exchanger; the first-stage heat exchanger, the second-stage heat exchanger and the tail gas heat exchanger are used for cooling the gas, and condensing and recovering a solvent in the gas.
Furthermore, the horizontal height of the liquid supply port of the liquid ring pump is lower than the upper end part of the partition plate, and the liquid supply port and the liquid inlet of the liquid ring pump are positioned at the same horizontal height or higher than the horizontal position of the liquid inlet of the liquid ring pump.
The liquid inlet requirement of the liquid ring pump is met by the rated pressure drop formed by the height difference between the liquid level of the liquid inlet cavity and the liquid supply port of the liquid ring pump.
The circulating liquid heat exchanger is arranged at the outlet of the circulating pump and used for reducing the temperature of circulating liquid, the circulating liquid circulates through the liquid ring pump, the temperature is gradually increased, and the temperature is reduced to enable the system to be more stable; the outlet of the circulating liquid heat exchanger is adjusted and communicated with the discharge port and/or the circulating liquid inlet through a valve.
And further, the device also comprises a thermometer arranged close to the liquid supply port of the liquid ring pump and used for monitoring the temperature of the liquid in the water replenishing separation device.
Further, the cooling temperature of the primary heat exchanger is 20-25 ℃;
the cooling temperature of the secondary heat exchanger is 7-10 ℃;
the cooling temperature of the tail gas heat exchanger is 4-5 ℃.
Multistage cooling can improve the condensation and retrieve the effect, and cooling temperature needs rationally to set up according to the temperature in the actual production.
Further, the horizontal position of the outlet of the primary heat exchanger is higher than the gas inlet of the vacuum buffer tank, and the horizontal position of the outlet of the secondary heat exchanger is higher than the inlet of the liquid ring pump;
the horizontal position of the inlet of the tail gas heat exchanger is higher than the emptying port of the water supplementing and separating device.
The equipment is arranged by utilizing the height space, the floor area of the equipment is reduced, the installation space is saved, the gas can be automatically discharged along the equipment, and the operation efficiency of the equipment is improved.
Meanwhile, the inlet horizontal position of the tail gas heat exchanger of the water supplementing separating device is higher than the emptying port of the water supplementing separating device, so that liquid of the water supplementing separating device can be prevented from flowing backwards to the heat exchanger to block the heat exchanger, and the efficiency of the heat exchanger is influenced.
Furthermore, a first recovery port is arranged on the secondary heat exchanger, and a second recovery port is arranged on the tail gas heat exchanger and is used for recovering the solvent condensate.
Further, the air inlet is arranged at the upper part of the tank body of the water supplementing separation device, a pipeline of the air inlet extends into the separation cavity, and the inner end part of the pipeline adopts a 45-degree oblique cut.
Adopt 45 bevels to prevent that the pipeline from suck-back from inhaling the liquid in the separation chamber back to vacuum system, simultaneously, prevent that the gaseous flooding or the aeration phenomenon that produces of liquid-containing from getting into in the moisturizing device from influencing final exhaust emission.
Furthermore, the horizontal heights of the inner end parts of the pipelines of the circulating liquid inlet and the supplementing port are lower than the upper end part of the partition plate, and the inner end parts of the pipelines of the circulating liquid inlet and the supplementing port extend into the liquid level of the liquid inlet cavity to prevent liquid from splashing during normal operation.
Compared with the prior art, the utility model discloses following beneficial effect has:
1. the utility model discloses be provided with one-level recovery unit, second grade recovery unit and tertiary recovery unit, cool off step by step and retrieve the solvent condensate, it is effectual to the recovery of solvent condensate, reduce the solvent consumption, practice thrift the cost, and accord with ecological environmental protection requirement.
2. The utility model combines the water replenishing tanks of the gas-water separator and the liquid ring pump in the prior art into a water replenishing separation device, and the division plate is arranged to divide the inside of the tank body into a liquid inlet cavity and a separation cavity, thereby simultaneously meeting the functions of water replenishing and gas-liquid separation and reducing the occupied area of equipment and the input of external water or other solvents; the liquid in the liquid inlet cavity overflows to the separation cavity through the partition plate, the liquid in the liquid inlet cavity is enabled to be in an overflow state all the time by adjusting the rotating speed of the circulating pump to a suitable working condition, the liquid in the water supplementing separation device is continuously recycled, stable water supply is guaranteed for the liquid inlet of the liquid ring pump, the system is enabled to run more reasonably, and the vacuum degree of the production equipment is provided more stably.
3. The utility model discloses the level of well liquid ring pump liquid supply mouth is less than the upper end of division board, is located same level with the inlet of liquid ring pump, or is higher than the horizontal position of the inlet of liquid ring pump, provides feed liquor pressure through the difference in height of feed liquor chamber liquid level and liquid ring pump liquid supply mouth.
4. The utility model discloses utilize high spatial arrangement equipment, reduce equipment area, save installation space, and make the operation of liquefaction pump more stable, lift system production efficiency has fine economic benefits.
5. The utility model discloses the cooling temperature of well one-level heat exchanger is 20-25 ℃, and the cooling temperature of second grade heat exchanger is 7-10 ℃, and the cooling temperature of tail gas heat exchanger is 4-5 ℃, and tertiary temperature sets up rationally, reaches best cooling effect.
6. The utility model discloses be provided with first time binding off and second recovery mouth on second grade heat exchanger and the tail gas heat exchanger respectively, directly retrieve the menstruum condensate at the heat exchanger, simultaneously, first time binding off retrieves the back to the menstruum condensate, can reduce the menstruum that gets into the circulating pump to reduce the menstruum concentration of liquid ring pump inner loop liquid, improve recovery efficiency.
Drawings
FIG. 1 is a schematic diagram of a prior art in the background art;
fig. 2 is a schematic diagram of an embodiment of the present invention;
fig. 3 is a device connection diagram of an embodiment of the present invention;
description of reference numerals:
101-equipment to be vacuumized, 102-heat exchanger, 103-vacuum buffer tank, 104-liquid ring pump, 105-gas-water separator, 106-water replenishing tank;
210-equipment to be vacuumized; 220-primary heat exchanger; 230-vacuum buffer tank, 231-gas inlet, 232-gas outlet; 240-a secondary heat exchanger, 241-a first recovery port; 250-liquid ring pump, 251-liquid inlet; 260-a water supplementing separation device, 261-a liquid supply port of a liquid ring pump, 262-a liquid outlet, 263-a drain port, 264-an air inlet, 265-a drain port, 266-a circulating liquid inlet, 267-a supplement port, 268-a partition plate and 269-a thermometer; 270-a tail gas heat exchanger, 271-a second recovery port; 280-circulating pump; 290-circulating liquid heat exchanger.
Detailed Description
The invention is described in further detail below with reference to the following figures and specific examples:
the utility model discloses a solvent condensate recovery unit for vacuum system, as shown in fig. 2 to fig. 3, including the one-level recovery unit, the second grade recovery unit, the third grade recovery unit and the liquid ring pump 250 that set gradually, the one-level recovery unit includes the one-level heat exchanger 220 and the vacuum buffer tank 230 that connect gradually, the import of one-level heat exchanger 220 connects and waits to take out vacuum equipment 210; the vacuum buffer tank 230 is used for recovering partial solvent condensate, a gas inlet 231 and a gas outlet 232 are arranged on the vacuum buffer tank 230, and the gas inlet 231 is communicated with an outlet of the primary heat exchanger 220.
The secondary recovery unit comprises a secondary heat exchanger 240, an inlet of the secondary heat exchanger 240 is connected with a gas outlet 232 of the vacuum buffer tank 230, an outlet of the secondary heat exchanger 240 is communicated with an inlet of the liquid ring pump 250, and a first recovery port 241 is arranged on the secondary heat exchanger 240 and used for recovering solvent condensate.
The three-stage recovery unit comprises a water supplementing separation device 260 and a tail gas heat exchanger 270; the water supplementing separating device 260 comprises a tank body and a partition plate 268 arranged in the tank body, the lower part in the tank body is divided into a liquid inlet cavity and a separating cavity by the partition plate 268, and the upper part is communicated and provided with a drain port 265.
The liquid inlet cavity is provided with a liquid ring pump liquid supply port 261, a circulating liquid inlet 266, a supplement port 267 and a drain port 263, the separation cavity is provided with a gas inlet 264 and a liquid outlet 262, the gas inlet 264 is arranged at the upper part of the tank body and is used for being communicated with an outlet of the liquid ring pump 250, a pipeline of the gas inlet 264 extends into the separation cavity, and the inner end part adopts a 45-degree oblique notch; the liquid ring pump liquid supply port 261 is lower than the upper end of the partition plate 268 in horizontal height, is communicated with the liquid inlet 251 of the liquid ring pump 250, and is positioned at the same horizontal height with the liquid inlet 251 of the liquid ring pump 250 or is higher than the horizontal position of the liquid inlet 251 of the liquid ring pump 250; the supplement port 267 is used for inputting water or other solvents, and preferably selects the components of the solvent in the easily-dissolved vacuumized gas, which is beneficial to the recovery of the solvent in the gas; the liquid in the make-up water separation device 260 is circulated by a circulating pump 280, the liquid outlet 262 and the drain port 263 are connected in parallel to the inlet of the circulating pump 280, the outlet of the circulating pump 280 is provided with a circulating liquid heat exchanger 290, the outlet of the circulating liquid heat exchanger 290 is connected with a circulating liquid inlet 266 and is also provided with a drain port, the outlet of the circulating liquid heat exchanger 290 is communicated with the circulating liquid inlet 266 and/or the drain port by valve adjustment, and the drain port is communicated with external processing equipment; the level of the inner end of the pipeline of the supplement port 267 and the circulating liquid inlet 266 is lower than that of the upper end of the partition plate 268; a thermometer 269 is provided adjacent the liquid ring pump supply port 261 to monitor the temperature of the liquid in the make-up water separator 260.
In the embodiment, the volume ratio of the liquid inlet cavity to the separation cavity is about 1:2, the rotating speed of the circulating pump 280 is adjusted to realize stable circulation, the liquid level height of the liquid inlet cavity needs to be maintained at the upper end of the separation plate 268 to ensure that the liquid supply of the liquid ring pump 250 is stable and can continuously overflow, and the liquid level height in the separation cavity is about 1/2 of the height of the separation plate 268.
The inlet of the tail gas heat exchanger 270 is communicated with the evacuation port 265, the outlet is communicated with the atmosphere, and the tail gas heat exchanger 270 is provided with a second recovery port 271 for recovering solvent condensate.
In this embodiment, the cooling temperature of the primary heat exchanger 220 is 20-25 ℃, the cooling temperature of the secondary heat exchanger 240 is 7-10 ℃, and the cooling temperature of the tail gas heat exchanger 270 is 4-5 ℃; the primary heat exchanger 220, the secondary heat exchanger 240 and the tail gas heat exchanger 270 are cooled by circulating cooling water systems; in other embodiments of the present invention, the cooling temperature can be adjusted according to the actual system requirement.
In this embodiment, the outlet horizontal position of the primary heat exchanger 220 is higher than the gas inlet 231 of the vacuum buffer tank 230, the outlet horizontal position of the secondary heat exchanger 240 is higher than the inlet of the liquid ring pump 250, the inlet horizontal position of the tail gas heat exchanger 270 is higher than the evacuation port 265 of the water replenishing separation device 260, the evacuation port 265 and the outlet of the tail gas heat exchanger 270 do not need to be provided with additional power equipment, the gas can be automatically discharged along the equipment by utilizing the height difference setting, the energy consumption is reduced, and the operation efficiency of the equipment is improved.
The utility model discloses a theory of operation does: vacuumizing the equipment 210 to be vacuumized, the primary recovery unit and the secondary recovery unit through the liquid ring pump 250, wherein in the vacuumizing process, the vacuumized gas contains volatile solvents, the volatile solvents are condensed and recovered by utilizing the primary heat exchangers 220 and the secondary heat exchangers 240 in the primary recovery unit and the secondary recovery unit, a water supplementing and separating device 260 is arranged for supplementing liquid in the liquid ring pump 250, meanwhile, gas-liquid mixture at the outlet of the liquid ring pump 250 is subjected to gas-liquid separation, the separated liquid is recovered in the water supplementing and separating device 260, the gas is further cooled through a tail gas heat exchanger 270 and then discharged, and the tail gas heat exchanger 270 can condense and recover the volatile solvents; the liquid in the make-up water separator 260 can be recycled by the circulating pump 280, when the temperature is high or the liquid concentration is too high, the liquid is discharged through the discharge port, and the make-up port 267 replenishes water or other solvents to ensure the liquid level in the liquid inlet chamber.
With reference to the apparatus shown in fig. 3, the working flow of the apparatus specifically includes:
s1, high-temperature vacuum gas enters from an inlet of a primary heat exchanger 220, the high-temperature vacuum gas is cooled to a temperature below 25 ℃, part of solvent in the gas is condensed and then recovered through a recovery port of the primary heat exchanger 220, the cooled gas enters from a gas inlet 231 of a vacuum buffer tank 230, and part of solvent condensate is recovered from the vacuum buffer tank 230;
s2, allowing residual gas of the S1 to pass through a gas outlet 232 of the vacuum buffer tank 230 to reach a secondary heat exchanger 240, cooling to 7-10 ℃, and recovering solvent condensate from a first recovery port 241;
s3, gas-liquid mixture is generated after the residual gas of S2 passes through a liquid ring pump 250, gas-liquid separation is carried out through a separation cavity of a water supplementing separation device 260, the separated liquid is recovered in the separation cavity, the gas is reduced to 4-5 ℃ through a tail gas heat exchanger 270, the gas is discharged through an outlet of the tail gas heat exchanger 270, and the solvent condensate is recovered through a second recovery port 271; meanwhile, the feed water separator 260 communicates with the circulation pump 280 to circulate the internal liquid through the circulation liquid heat exchanger 290, and when the temperature is too high or the liquid concentration is too high, the valve is adjusted to discharge a part of the liquid, and water or other solvents are fed through the feed port 267.
The above description is only for the specific embodiments of the present invention, but the protection scope of the present invention is not limited thereto, and any person skilled in the art can easily think of various equivalent modifications or replacements within the technical scope of the present invention, and these modifications or replacements should be covered within the protection scope of the present invention.
Claims (9)
1. A solvent condensate recovery device for a vacuum system comprises a primary recovery unit and a liquid ring pump (250), wherein the primary recovery unit comprises a primary heat exchanger (220) and a vacuum buffer tank (230) which are sequentially connected, a gas inlet (231) and a gas outlet (232) are formed in the vacuum buffer tank (230), and the vacuum buffer tank (230) is used for recovering part of solvent condensate; the inlet of the primary heat exchanger (220) is connected with the equipment (210) to be vacuumized, and the outlet of the primary heat exchanger is connected with the gas inlet (231) of the vacuum buffer tank (230); the method is characterized in that:
the device also comprises a secondary recovery unit and a tertiary recovery unit;
the secondary recovery unit comprises a secondary heat exchanger (240), and an inlet of the secondary heat exchanger (240) is connected with a gas outlet (232) of the vacuum buffer tank (230); the three-stage recovery unit comprises a water supplementing separation device (260), a circulating pump (280) and a tail gas heat exchanger (270); the water supplementing separation device (260) comprises a tank body and a partition plate (268) arranged in the tank body, the partition plate (268) divides the lower space in the tank body into a liquid inlet cavity and a separation cavity, and the upper space is communicated and provided with an evacuation port (265); the inlet of the liquid ring pump (250) is communicated with the outlet of the secondary heat exchanger (240); an inlet of the tail gas heat exchanger (270) is communicated with an exhaust port (265), and an outlet of the tail gas heat exchanger is communicated with the atmosphere;
the liquid inlet cavity is provided with a liquid ring pump liquid supply port (261), a circulating liquid inlet (266), a supplement port (267) and a drain port (263), the separation cavity is provided with a gas inlet (264) and a liquid outlet (262), the gas inlet (264) is communicated with the outlet of the liquid ring pump (250), the liquid ring pump liquid supply port (261) is communicated with the liquid inlet (251) of the liquid ring pump (250), the supplement port (267) is used for inputting a solvent for dissolving the solvent, and the liquid in the liquid inlet cavity overflows to the separation cavity through a partition plate (268); the liquid outlet (262) and the clean discharging port (263) are both communicated with an inlet of a circulating pump (280), an outlet of the circulating pump (280) is communicated with a circulating liquid inlet (266), a discharging port is also arranged at an outlet of the circulating pump (280), and the outlet of the circulating pump (280) is communicated with the circulating liquid inlet (266) and/or the discharging port through valve adjustment;
the liquid ring pump (250) is used for vacuumizing the equipment to be vacuumized (210), the primary recovery unit and the secondary recovery unit, a gas-liquid mixture at the outlet of the liquid ring pump (250) is subjected to gas-liquid separation through the separation cavity, and then gas is discharged from the outlet of the tail gas heat exchanger (270); the primary heat exchanger (220), the secondary heat exchanger (240) and the tail gas heat exchanger (270) are used for cooling the gas and condensing and recovering the solvent in the gas.
2. The solvent condensate recovery device for a vacuum system as claimed in claim 1, wherein:
the liquid ring pump liquid supply port (261) is lower than the upper end of the partition plate (268) in horizontal height, and is positioned at the same horizontal height with the liquid inlet (251) of the liquid ring pump (250), or is higher than the horizontal position of the liquid inlet (251) of the liquid ring pump (250).
3. The solvent condensate recovery device for a vacuum system as claimed in claim 2, wherein:
the circulating pump also comprises a circulating liquid heat exchanger (290) arranged at the outlet of the circulating pump (280) and used for reducing the temperature of circulating liquid; the outlet of the circulating liquid heat exchanger (290) is adjusted and communicated with the discharge port and/or the circulating liquid inlet (266) through a valve.
4. The solvent condensate recovery device for a vacuum system as claimed in claim 3, wherein:
the device also comprises a thermometer (269) which is arranged close to the liquid supply port (261) of the liquid ring pump and is used for monitoring the temperature of the liquid in the water replenishing separation device (260).
5. The vehicle condensate recovery apparatus for a vacuum system as claimed in any one of claims 1 to 4, wherein:
the cooling temperature of the primary heat exchanger (220) is 20-25 ℃;
the cooling temperature of the secondary heat exchanger (240) is 7-10 ℃;
the cooling temperature of the tail gas heat exchanger (270) is 4-5 ℃.
6. The solvent condensate recovery device for a vacuum system as claimed in claim 5, wherein:
the outlet horizontal position of the primary heat exchanger (220) is higher than the gas inlet (231) of the vacuum buffer tank (230), and the outlet horizontal position of the secondary heat exchanger (240) is higher than the inlet of the liquid ring pump (250);
the horizontal position of the inlet of the tail gas heat exchanger (270) is higher than the drain port (265) of the water supplementing and separating device (260).
7. The solvent condensate recovery device for a vacuum system as claimed in claim 6, wherein:
the secondary heat exchanger (240) is also provided with a first recovery port (241), and the tail gas heat exchanger (270) is provided with a second recovery port (271) which are all used for recovering solvent condensate.
8. The solvent condensate recovery apparatus for a vacuum system of claim 7, wherein:
the air inlet (264) is arranged at the upper part of the tank body of the water supplementing separation device (260), a pipeline of the air inlet (264) extends into the separation cavity, and the inner end part of the pipeline adopts a 45-degree oblique cut.
9. The solvent condensate recovery device for a vacuum system of claim 8, wherein:
the horizontal heights of the inner ends of the pipelines of the circulating liquid inlet (266) and the supplementary port (267) are lower than the upper end of the partition plate (268).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222799932.XU CN218821743U (en) | 2022-10-24 | 2022-10-24 | Solvent condensate recovery device for vacuum system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222799932.XU CN218821743U (en) | 2022-10-24 | 2022-10-24 | Solvent condensate recovery device for vacuum system |
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| Publication Number | Publication Date |
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| CN218821743U true CN218821743U (en) | 2023-04-07 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202222799932.XU Active CN218821743U (en) | 2022-10-24 | 2022-10-24 | Solvent condensate recovery device for vacuum system |
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| CN (1) | CN218821743U (en) |
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- 2022-10-24 CN CN202222799932.XU patent/CN218821743U/en active Active
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