CN220404830U - Pressurized solvent recovery device - Google Patents
Pressurized solvent recovery device Download PDFInfo
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- CN220404830U CN220404830U CN202321507492.4U CN202321507492U CN220404830U CN 220404830 U CN220404830 U CN 220404830U CN 202321507492 U CN202321507492 U CN 202321507492U CN 220404830 U CN220404830 U CN 220404830U
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- cooler
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- pressurizing
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- 239000002904 solvent Substances 0.000 title claims abstract description 55
- 238000011084 recovery Methods 0.000 title claims abstract description 30
- 230000006835 compression Effects 0.000 claims abstract description 23
- 238000007906 compression Methods 0.000 claims abstract description 23
- 239000007788 liquid Substances 0.000 claims abstract description 20
- 239000003507 refrigerant Substances 0.000 claims abstract description 10
- 230000001105 regulatory effect Effects 0.000 claims description 10
- 239000004065 semiconductor Substances 0.000 claims description 4
- 230000001276 controlling effect Effects 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- 238000001816 cooling Methods 0.000 abstract description 14
- 238000002844 melting Methods 0.000 abstract description 5
- 230000008018 melting Effects 0.000 abstract description 5
- 238000005516 engineering process Methods 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 42
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 12
- 239000003960 organic solvent Substances 0.000 description 6
- 229920006395 saturated elastomer Polymers 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 238000009835 boiling Methods 0.000 description 3
- 239000000498 cooling water Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 2
- -1 polytetrafluoroethylene Polymers 0.000 description 2
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 2
- 239000004810 polytetrafluoroethylene Substances 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 241000357293 Leptobrama muelleri Species 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000005457 ice water Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 239000010888 waste organic solvent Substances 0.000 description 1
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Abstract
The utility model provides a pressurized solvent recovery device, which comprises a plurality of stages of pressurizing systems which are mutually connected in series, wherein pressure difference exists between the pressurizing systems; the supercharging system comprises a gas compression device, a cooler and a gas-liquid separator, wherein one end of the cooler is communicated with the gas compression device, and the other end of the cooler is communicated with the gas-liquid separator. By arranging the multistage pressurizing systems which are mutually connected in series, the pressure difference between the pressurizing systems at all stages reduces the solvent loss rate in the existing solvent recovery process by utilizing a pressurizing and cooling technology; meanwhile, the concentration of the solvent in the tail gas can be reduced by using a pressurizing and cooling technology, so that the limitation of the melting point temperature of the solvent is avoided, the technical requirement on the refrigerant is reduced, and the energy consumption is further reduced.
Description
Technical Field
The utility model relates to the technical field of solvent recovery, in particular to a pressurized solvent recovery device.
Background
In the production of chemical products and laboratory studies, it is often necessary to use various solvents as a medium for chemical reactions or purification of the products. Most of the solvents are organic matters or toxic inflammable matters, and meanwhile, the solvents are high in price and high in dosage. Recovery of these solvents is often required for environmental and economic reasons. At present, it is common to recover the solvent by heating and evaporating the solvent and then cooling the vapor of the solvent under normal pressure or reduced pressure. In the steam cooling stage in the actual operation process, because the system inevitably contains non-condensing air or other protective gas and the like, the gas is finally discharged through an exhaust system. Because the organic solvent has certain saturated vapor pressure, when the tail gases are discharged, partial vapor of the organic solvent is often entrained. This results in, on the one hand, the organic solvent not being completely recovered, with a certain loss, and on the other hand, the content of organic components in the tail gas being increased, resulting in pollution.
To solve this problem, the prior art generally starts from lowering the cooling temperature, reducing the temperature of the cooler as much as possible, reducing the saturated vapor pressure of the organic solvent vapor, and reducing the loss of the organic solvent. The prior patent CN206777898U discloses a waste organic solvent recovery device, which comprises a heating system, a cooling system and a control system, wherein the cooling system comprises a condensing pipeline and a vacuum decompression pump; the heating system comprises an explosion-proof recovery barrel and a heater, the explosion-proof recovery barrel of the heating system is connected with a condensation pipeline of the cooling system, and the control system comprises a time controller, a temperature controller, a high-temperature alarm controller and a high-pressure alarm controller.
According to the technical scheme, the modularized control system is arranged, solvent components with different boiling points are recycled in a sectional control mode, and the following defects still exist: firstly, the boiling point of part of the solvent is lower, and in order to reduce the saturated vapor pressure, the temperature of the solvent cooler is correspondingly reduced, so that higher requirements are put on public engineering conditions such as refrigerants and the like; second, the difference between the melting point and the boiling point of a part of the solvent is very small, and even if a high saturated vapor pressure is still present near the melting point, a good recovery effect cannot be obtained by simply cooling at low temperature.
Disclosure of Invention
In view of the above, the present utility model provides a pressurized solvent recovery device to solve the technical problems of low operation temperature and high solvent loss rate of the existing solvent recovery system.
The technical scheme of the utility model is realized as follows: the utility model provides a pressurized solvent recovery device, which comprises a plurality of stages of pressurizing systems which are mutually connected in series, wherein pressure difference exists between the pressurizing systems;
the supercharging system comprises a gas compression device, a cooler and a gas-liquid separator, wherein one end of the cooler is communicated with the gas compression device, and the other end of the cooler is communicated with the gas-liquid separator.
On the basis of the technical scheme, the pressure difference between the pressurizing systems is preferably 0.01-0.05 Mpa.
Based on the technical scheme, the inlet pressure of the head-end supercharging system is preferably 0-0.1 Mpa, and the exhaust pressure of the final-stage supercharging system is preferably 0.1-2.5 Mpa.
On the basis of the technical scheme, the exhaust pressure of the final stage supercharging system is preferably 0.1-0.7 Mpa.
On the basis of the technical scheme, the series-connection stage number of the pressurizing system is preferably 2-5.
On the basis of the technical proposal, preferably, the gas-liquid separator comprises a saving tank, a first outlet and a second outlet,
a hollow cavity is arranged in the accumulator tank;
the first outlet is arranged at the top end of the accumulator tank, and a regulating valve is arranged at the first outlet and used for controlling the internal pressure of the accumulator tank;
the second outlet is arranged at the bottom end of the accumulator tank, and a discharge valve is arranged at the second outlet and used for discharging the solvent.
On the basis of the technical scheme, preferably, the gas compression device is a diaphragm compressor, a screw compressor or a piston compressor.
On the basis of the technical scheme, the cooler is preferably a plate cooler, a tube cooler, a capillary cooler or a shell and tube cooler.
On the basis of the technical scheme, preferably, the cold source of the cooler is a low-temperature refrigerant or a semiconductor refrigerating sheet.
Compared with the prior art, the pressurized solvent recovery device has the following beneficial effects:
by arranging the multistage pressurizing systems which are mutually connected in series, the pressure difference between the pressurizing systems at all stages reduces the solvent loss rate in the existing solvent recovery process by utilizing a pressurizing and cooling technology; meanwhile, the concentration of the solvent in the tail gas can be reduced by using a pressurizing and cooling technology, so that the limitation of the melting point temperature of the solvent is avoided, the technical requirement on the refrigerant is reduced, and the energy consumption is further reduced.
Drawings
In order to more clearly illustrate the embodiments of the utility model or the technical solutions in the prior art, the drawings that are required in the embodiments or the description of the prior art will be briefly described, it being obvious that the drawings in the following description are only some embodiments of the utility model, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a perspective view of a pressurized solvent recovery apparatus of the present utility model.
Reference numerals
1. A gas compression device; 2. a cooler; 3. a gas-liquid separator; 4. a regulating valve; 5. a discharge valve.
Detailed Description
The following description of the embodiments of the present utility model will clearly and fully describe the technical aspects of the embodiments of the present utility model, and it is apparent that the described embodiments are only some embodiments of the present utility model, not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the present utility model without making any inventive effort, are intended to fall within the scope of the present utility model.
As shown in fig. 1, the pressurized solvent recovery device comprises a plurality of stages of pressurizing systems which are mutually connected in series, wherein pressure difference exists among the pressurizing systems, the pressurizing systems comprise a gas compression device 1, a cooler 2 and a gas-liquid separator 3, one end of the cooler 2 is connected with the gas compression device 1, and the other end is connected with the gas-liquid separator 3. According to the utility model, the internal pressure of the system is increased through the pressurizing system, and based on the principle that the saturated vapor pressure of the solvent at a specific temperature is constant, the duty ratio of the non-condensing components in the gas in the cooler 2 and the gas-liquid separator 3 is promoted to be increased, the duty ratio of the solvent components is reduced, and the effect of reducing the concentration of the solvent in tail gas is achieved.
In a preferred embodiment, the series of the pressurizing systems has a number of stages of 2 to 5, for example, 2 stages, 3 stages, 4 stages or 5 stages, each stage of pressurizing system is a first stage pressurizing system, a second stage pressurizing system, a third stage pressurizing system, a fourth stage pressurizing system and a fifth stage pressurizing system according to the gas flow sequence, and thus, the pressurizing system through which the gas finally passes is a final stage pressurizing system. The multistage supercharging systems are connected in series, and meanwhile, the pressure difference is arranged between the multistage supercharging systems, so that higher compression pressure can be achieved by using simple compression equipment, and the requirement on gas compression equipment is greatly reduced; meanwhile, the concentration of the solvent in the tail gas is reduced through pressurization, and compared with the traditional method, the method has no limitation on the melting point and the temperature of the solvent, greatly reduces the technical requirement on the refrigerant, has a simple and easy control system, and can greatly reduce the loss in the solvent recovery process; in addition, the solvent is recovered through the serially connected pressurizing systems, and the coolers 2 in each stage of pressurizing system can use refrigerants with different temperatures, so that the consumption of low-temperature refrigerants is reduced.
As a preferred implementation mode, the pressure in each stage of pressurizing system is gradually increased, the pressure difference between each stage of pressurizing system is 0.01-0.05 Mpa, wherein the inlet pressure of the first stage of pressurizing system is 0-0.1 Mpa, and the first stage of pressurizing system can be connected with a solvent air source through a pipeline so as to suck other solvent into the pressurizing system. The exhaust pressure of the final stage supercharging system is 0.1-2.5 Mpa, preferably 0.1-0.7 Mpa.
As a preferred embodiment, the gas compression device 1 is a diaphragm compressor, a screw compressor, and a piston compressor, preferably a diaphragm compressor. The diaphragm compressor is a positive displacement compressor with special structure, and has the characteristics of no secondary pollution, large compression ratio, good sealing performance, and no pollution of compressed gas by lubricating oil and other solid impurities. The gas compression device 1 is provided with a gas inlet and a gas outlet, the gas outlet is connected with the inlet of the cooler 2, and the outlet of the cooler 2 is connected with the inlet of the gas-liquid separator 3.
In a preferred embodiment, the cooler 2 is a plate cooler, a tube cooler, a capillary cooler or a tube cooler, preferably a plate cooler. The cold source of the cooler 2 is a low-temperature refrigerant or a semiconductor refrigerating sheet, preferably a semiconductor refrigerating sheet.
As a preferred embodiment, the gas-liquid separator 3 comprises a tank, a first outlet and a second outlet, and a hollow cavity is arranged in the tank and is used for separating the compressed gas and the solvent; the first export sets up in the accumulator bottom, and the first export is used for discharging gas, and first exit is provided with governing valve 4, and governing valve 4 is used for controlling accumulator internal pressure, when making gas in the gas-liquid separation jar reach specific pressure through governing valve 4 self structure or pressure control system, can pass through governing valve 4. The regulating valve 4 may be a back pressure valve, a drain valve, a throttle valve or a diaphragm valve, preferably a back pressure valve, and if the regulating valve 4 is a throttle valve or a diaphragm valve, the opening of the regulating valve 4 should be adjusted according to the pressure set in the gas-liquid separation tank, so as to ensure that the pressure in the tank is at a set value. The opening degree of the regulating valve 4 may be regulated manually, electrically or pneumatically, preferably electrically. A drain valve 5 is provided at the second outlet, which drain valve 5 is used to drain out solvent separated in the tank.
The following examples are merely illustrative of the present utility model and are not intended to represent or limit the scope of the utility model as claimed, but are representative but not limiting of the utility model.
Example 1
The present embodiment provides a pressurized solvent recovery apparatus.
The pressurized solvent recovery device comprises two pressurizing systems which are connected in series, wherein each pressurizing system comprises a gas compression device 1, a cooler 2 and a gas-liquid separator 3, the gas compression device 1 is a diaphragm compressor with polytetrafluoroethylene diaphragms, the air inlet pressure of the compressor is 0.005MPa, the flow is 60L/min, and the outlet pressure is 0-0.2 MPa. The cooler 2 is a capillary cooler, which is made by placing polytetrafluoroethylene capillary with the diameter of 1mm and the length of 1m in a cooling water tank, the cooling water tank is cooled by ice water bath, and the temperature of the cooling water tank is 0 ℃. The gas-liquid separator 3 is a stainless steel tank with a volume of 500ml, the regulating valve 4 is a stainless steel back pressure valve, and the discharge valve 5 is a manual needle valve. In this example, the first stage compression system operating pressure was controlled to 0.15MPa and the second stage compression system operating pressure was controlled to 0.3MPa.
Example 2
The present example provides a method of using the pressurized solvent recovery apparatus as described in example 1.
The inlet pipeline of the pressurizing system is connected with a gas source, the gas source is gas with ethanol content of 40% and air content of 60%, and the gas source is derived from the ethanol evaporating system. In the first stage supercharging system, after the diaphragm compressor is started, the inlet of the diaphragm compressor generates negative pressure to automatically suck the gas in the gas source into the compressor, and after the gas is compressed, the gas enters the cooler 2. The cooler 2 is in communication with the gas-liquid separator 3 and is set at a pressure by a back pressure valve, in this case 0.15MPa. The gas is compressed and then enters the cooler 2, and is cooled to 0 ℃ in the cooler 2. The cooled gas enters the second stage compression system.
The back pressure valve pressure in the second stage compression system is 0.3MPa, and the temperature of the cooler 2 is 0 ℃. The gas passes through a gas-liquid separation tank, the cooled ethanol is temporarily stored in the separation tank and then is discharged by a needle valve, and the residual tail gas is discharged by a back pressure valve.
The composition of the remaining tail gas was examined, and the concentration of ethanol in the tail gas was only 0.55% when the system pressure was 0.3MPa, since the saturated vapor pressure of ethanol was 1.67kPa at 0℃and the concentration was about 1.65%. And at the same cooling temperature, the device reduces 66% ethanol loss. If the same effect is to be achieved by lowering the cooling temperature, it is required that the cooling temperature is to reach-12 ℃. Therefore, the device can effectively reduce the loss of the organic solvent and reduce the requirement on the refrigerant.
The foregoing description of the preferred embodiments of the utility model is not intended to be limiting, but rather is intended to cover all modifications, equivalents, alternatives, and improvements that fall within the spirit and scope of the utility model.
Claims (8)
1. A pressurized solvent recovery device, characterized in that: the system comprises a plurality of stages of supercharging systems which are connected in series, wherein pressure difference exists between the supercharging systems;
the supercharging system comprises a gas compression device (1), a cooler (2) and a gas-liquid separator (3), wherein one end of the cooler (2) is communicated with the gas compression device (1), and the other end of the cooler is communicated with the gas-liquid separator (3);
the gas-liquid separator (3) comprises a saving tank, a first outlet and a second outlet,
a hollow cavity is arranged in the accumulator tank;
the first outlet is arranged at the top end of the accumulator tank, a regulating valve (4) is arranged at the first outlet, and the regulating valve (4) is used for controlling the internal pressure of the accumulator tank;
the second outlet is arranged at the bottom end of the accumulator tank, a discharge valve (5) is arranged at the second outlet, and the discharge valve (5) is used for discharging solvent.
2. A pressurized solvent recovery apparatus according to claim 1, wherein: the pressure difference between the pressurizing systems is 0.01-0.05 Mpa.
3. A pressurized solvent recovery apparatus according to claim 2, wherein: the inlet pressure of the head end pressurizing system is 0-0.1 Mpa, and the exhaust pressure of the final pressurizing system is 0.1-2.5 Mpa.
4. A pressurized solvent recovery apparatus according to claim 3, wherein: the exhaust pressure of the final stage supercharging system is 0.1-0.7 Mpa.
5. A pressurized solvent recovery apparatus according to claim 1, wherein: the series stage number of the supercharging system is 2-5.
6. A pressurized solvent recovery apparatus according to claim 1, wherein: the gas compression device (1) is a diaphragm compressor, a screw compressor or a piston compressor.
7. A pressurized solvent recovery apparatus according to claim 1, wherein: the cooler (2) is a plate cooler, a tube cooler, a capillary cooler or a shell and tube cooler.
8. A pressurized solvent recovery apparatus according to claim 7, wherein: the cold source of the cooler (2) is a low-temperature refrigerant or a semiconductor refrigerating sheet.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321507492.4U CN220404830U (en) | 2023-06-13 | 2023-06-13 | Pressurized solvent recovery device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321507492.4U CN220404830U (en) | 2023-06-13 | 2023-06-13 | Pressurized solvent recovery device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220404830U true CN220404830U (en) | 2024-01-30 |
Family
ID=89642376
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321507492.4U Active CN220404830U (en) | 2023-06-13 | 2023-06-13 | Pressurized solvent recovery device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220404830U (en) |
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2023
- 2023-06-13 CN CN202321507492.4U patent/CN220404830U/en active Active
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