CN110538480A - condensing system and condensing method - Google Patents
condensing system and condensing method Download PDFInfo
- Publication number
- CN110538480A CN110538480A CN201910913008.XA CN201910913008A CN110538480A CN 110538480 A CN110538480 A CN 110538480A CN 201910913008 A CN201910913008 A CN 201910913008A CN 110538480 A CN110538480 A CN 110538480A
- Authority
- CN
- China
- Prior art keywords
- refrigerant
- heat exchange
- equipment
- pipeline
- valve
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 24
- 239000003507 refrigerant Substances 0.000 claims abstract description 206
- 239000007789 gas Substances 0.000 claims abstract description 63
- 238000001035 drying Methods 0.000 claims abstract description 59
- 239000007788 liquid Substances 0.000 claims abstract description 47
- 230000017525 heat dissipation Effects 0.000 claims abstract description 44
- 230000006835 compression Effects 0.000 claims abstract description 43
- 238000007906 compression Methods 0.000 claims abstract description 43
- 238000011084 recovery Methods 0.000 claims abstract description 40
- 239000002918 waste heat Substances 0.000 claims abstract description 40
- 238000000926 separation method Methods 0.000 claims abstract description 38
- 238000009833 condensation Methods 0.000 claims abstract description 27
- 230000005494 condensation Effects 0.000 claims abstract description 27
- 238000005373 pervaporation Methods 0.000 claims description 40
- 239000012528 membrane Substances 0.000 claims description 16
- 238000009834 vaporization Methods 0.000 claims description 16
- 230000008016 vaporization Effects 0.000 claims description 16
- 238000001704 evaporation Methods 0.000 claims description 9
- 230000008020 evaporation Effects 0.000 claims description 9
- 239000011521 glass Substances 0.000 claims description 6
- 230000001105 regulatory effect Effects 0.000 claims description 5
- 238000002309 gasification Methods 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 4
- 230000008595 infiltration Effects 0.000 abstract description 18
- 238000001764 infiltration Methods 0.000 abstract description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 6
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 239000002904 solvent Substances 0.000 abstract description 3
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical compound CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 description 18
- 230000008676 import Effects 0.000 description 12
- 239000012466 permeate Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 238000009835 boiling Methods 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 238000005485 electric heating Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000003960 organic solvent Substances 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000012046 mixed solvent Substances 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000013076 target substance Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0036—Multiple-effect condensation; Fractional condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0039—Recuperation of heat, e.g. use of heat pump(s), compression
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
- B01D5/0087—Recirculating of the cooling medium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
- B01D61/362—Pervaporation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
- B01D61/368—Accessories; Auxiliary operations
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/448—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by pervaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/34—Organic compounds containing oxygen
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/38—Organic compounds containing nitrogen
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Organic Chemistry (AREA)
- Drying Of Gases (AREA)
- Drying Of Solid Materials (AREA)
Abstract
the invention relates to a condensation system comprising: the system comprises a compression device, a waste heat recovery device, a heat dissipation device, a drying device, a first heat exchange device, a second heat exchange device and a vapor-liquid separation device. Also relates to a condensation method. The waste heat recovery device has the advantages that the waste heat recovery is carried out, the waste heat of the high-temperature and high-pressure gas compressed by the compression device is effectively utilized, and the power consumption of the heat dissipation device is reduced; carrying out fractional condensation on the permeation vaporized gas; the infiltration vaporized gas directly carries out the heat transfer condensation with the refrigerant, compares with the current indirect heat transfer condensation that carries on of water or other solvents, can save equipment investment, operation energy consumption and area.
Description
Technical Field
The invention relates to the technical field of pervaporation, in particular to a condensing system and a condensing method applied to a pervaporation membrane system.
Background
pervaporation (PV) is a new membrane separation technology. The technology is used for separating liquid mixture, and has the outstanding advantage of realizing separation tasks which are difficult to be completed by traditional methods such as distillation, extraction, adsorption and the like with low energy consumption. It is especially suitable for the separation of the mixture with near boiling point and constant boiling point which is difficult to separate or can not be separated by common rectification; the method has obvious economic and technical advantages for removing trace water in organic solvents and mixed solvents and separating a small amount of organic pollutants in wastewater. The pervaporation membrane separation technology is to utilize the difference of solubility (thermodynamic property) and diffusivity (kinetic property) of an organic solvent and water (or different components in the solvent) in a compact membrane to enable the water (or a certain component) to permeate the membrane and then vaporize on the other side of the membrane, thereby realizing the separation process; water (or a component) is vaporized on the other side of the membrane and then needs to be condensed and discharged.
However, pervaporation membrane separation techniques suffer from several drawbacks. For example, the membrane module feed of the pervaporation system needs to be heated to a specific temperature, and energy is consumed. The gas vaporized at the other side of the membrane module of the pervaporation system needs to be condensed, and the heat emitted by the condenser in the process of refrigeration cycle by the condensing equipment is directly discharged into the atmosphere, so that the heat is lost, and the thermal pollution is caused.
In addition, the permeation of the mixed gas on the vacuum side of the pervaporation membrane module is a problem in the prior art how to realize the high-efficiency recovery of the target substance.
Therefore, there is a need for a condensing system for a pervaporation membrane system that recovers heat during a refrigeration cycle, improves condensing efficiency and target recovery, and reduces energy consumption and footprint.
disclosure of Invention
the invention aims to provide a condensing system and a condensing method aiming at the defects in the prior art.
In order to achieve the purpose, the invention adopts the technical scheme that:
A condensing system for use with a pervaporation membrane system comprising:
A compression device;
the waste heat recovery device is communicated with the compression device through a pipeline, and a first valve is arranged on the pipeline which is communicated with the waste heat recovery device and the compression device;
The heat dissipation equipment is respectively communicated with the compression equipment and the waste heat recovery equipment through a pipeline, and a second valve is arranged on the pipeline;
The drying equipment is communicated with the heat dissipation equipment through a pipeline;
the first heat exchange equipment is communicated with the drying equipment through a pipeline, and a third valve and a first expansion valve are arranged on the pipeline;
the second heat exchange equipment is respectively communicated with the drying equipment and the first heat exchange equipment through pipelines, and a fourth valve and a second expansion valve are arranged on the pipeline communicated with the second heat exchange equipment and the drying equipment;
and the gas-liquid separation equipment is respectively communicated with the compression equipment, the first heat exchange equipment and the second heat exchange equipment through pipelines.
preferably, the waste heat recovery apparatus includes:
A feed inlet;
A feed outlet in communication with the feed inlet to form a feed line;
the first refrigerant inlet is communicated with the compression equipment through a pipeline, and the first valve is arranged on the pipeline;
the first refrigerant outlet is communicated with the first refrigerant inlet to form a first refrigerant pipeline, and the first refrigerant outlet is communicated with the heat dissipation equipment through a pipeline;
the feed line is not in communication with the first refrigerant line.
Preferably, the heat dissipating apparatus includes:
the second refrigerant inlet is communicated with the compression equipment through a pipeline, the second valve is arranged on the pipeline, and the second refrigerant inlet is communicated with the first refrigerant outlet through a pipeline;
And the second refrigerant outlet is communicated with the second refrigerant inlet to form a second refrigerant pipeline, and the second refrigerant outlet is communicated with the drying equipment through a pipeline.
preferably, the first heat exchange device comprises:
a pervaporation gas first inlet;
the first pervaporation gas outlet is communicated with the first pervaporation gas inlet to form a first pervaporation gas pipeline;
The third refrigerant inlet is communicated with the drying equipment through a pipeline, and the third valve and the first expansion valve are arranged on the pipeline;
a third refrigerant outlet communicated with the third refrigerant inlet to form a third refrigerant line, the third refrigerant outlet being communicated with the vapor-liquid separation device through a line;
The pervaporation gas first line is not communicated with the refrigerant third line.
preferably, the second heat exchange device comprises:
A second inlet for permeate boil-off gas;
the pervaporation gas second outlet is communicated with the pervaporation gas second inlet to form a pervaporation gas second pipeline, and the pervaporation gas second outlet is communicated with the pervaporation gas first inlet through a pipeline;
the fourth refrigerant inlet is communicated with the drying equipment through a pipeline, and the fourth valve and the second expansion valve are arranged on the pipeline;
a refrigerant fourth outlet communicated with the refrigerant fourth inlet to form a refrigerant fourth pipeline, and the refrigerant fourth outlet is communicated with the vapor-liquid separation device through a pipeline;
The pervaporation gas second pipe is not communicated with the refrigerant fourth pipe.
preferably, the method further comprises the following steps:
and the high-low pressure liquid storage equipment is communicated with the heat dissipation equipment and the drying equipment through pipelines respectively.
preferably, the method further comprises the following steps:
and the evaporation pressure regulating valve is arranged on a pipeline for communicating the second heat exchange equipment with the vapor-liquid separation equipment.
Preferably, the evaporation pressure regulating valve is arranged on a pipeline for communicating the fourth refrigerant outlet of the second heat exchange device with the vapor-liquid separation device.
Preferably, the method further comprises the following steps:
the first temperature sensor is arranged on the first heat exchange equipment;
the second temperature sensor is arranged on the second heat exchange equipment;
a third temperature sensor disposed at the waste heat recovery device;
A fourth temperature sensor disposed at the heat sink.
Preferably, said first temperature sensor is disposed at said permeate boil-off gas first outlet of said first heat exchange means.
preferably, said second temperature sensor is disposed at said permeate boil-off gas second outlet of said second heat exchange means.
Preferably, the third temperature sensor is arranged at the feeding inlet of the waste heat recovery device.
Preferably, the fourth temperature sensor is disposed at the refrigerant second inlet of the heat sink.
Preferably, the method further comprises the following steps:
and the sight glass equipment is arranged on a pipeline communicated with the drying equipment and the first heat exchange equipment and the second heat exchange equipment respectively.
preferably, the method further comprises the following steps:
a fan disposed at the heat sink.
A condensation method applied to the condensation system as described above, comprising the steps of:
Step S1, under the action of permeation vaporization gas, the first heat exchange device and the second heat exchange device vaporize refrigerants to obtain a first refrigerant, and the first refrigerant is conveyed to the vapor-liquid separation device through a pipeline;
step S2, the vapor-liquid separation device performs vapor-liquid separation on the first refrigerant to obtain a second refrigerant, and the second refrigerant is sent to the compression device through a pipeline;
step S3, the compression device compresses the second refrigerant to obtain a third refrigerant, and the third refrigerant is sent to the heat dissipation device and the waste heat recovery device through a pipeline;
Step S4, after the third refrigerant is processed by the combination of the heat dissipation device and the waste heat recovery device, obtaining a fourth refrigerant, and the fourth refrigerant is conveyed to the drying device through a pipeline;
step S5, after the drying device performs drying processing on the fourth refrigerant, the refrigerant is obtained, and the refrigerant is sent to the first heat exchange device and the second heat exchange device through a pipeline.
preferably, in step S1, the method includes the following steps:
Step S110, opening the third valve and the fourth valve, wherein the refrigerant passes through the first expansion valve and the second expansion valve and then enters the first heat exchange device and the second heat exchange device, and the permeated vaporized gas sequentially enters the second heat exchange device and the first heat exchange device and exchanges heat with the refrigerant;
Step S120, detecting a first temperature of the pervaporation gas at a first gasification gas outlet of the first heat exchange device through a first temperature sensor, and detecting a second temperature of the pervaporation gas at a second gasification gas outlet of the second heat exchange device through a second temperature sensor;
step S130, comparing the first temperature with a first preset value, and comparing the second temperature with a second preset value:
If the first temperature is higher than the first preset value, opening the third valve, and if the first temperature is equal to the first preset value, closing the third valve;
if the second temperature is higher than the second preset value, the fourth valve is opened, and if the second temperature is equal to the second preset value, the fourth valve is closed;
and if the first temperature and the second temperature are respectively equal to the first preset value and the second preset value at the same time, closing the third valve, the fourth valve and the compression equipment.
Preferably, the first preset value is greater than the second preset value.
Preferably, in the step S110, the following steps are included:
step S111, adjusting the first expansion valve and the second expansion valve to enable the temperature of the refrigerant entering the first heat exchange device to be lower than the temperature of the refrigerant entering the second heat exchange device;
Step S112, in the second heat exchange device, the refrigerant exchanges heat with the pervaporation gas to obtain the first refrigerant, and in the first heat exchange device, the refrigerant exchanges heat with the pervaporation gas to obtain the first refrigerant;
Step S113, the pressure of the first refrigerant output by the second heat exchange equipment is adjusted through an evaporation pressure adjusting valve, and the first refrigerant output by the second heat exchange equipment and the first refrigerant output by the first heat exchange equipment are mixed and then are conveyed to the vapor-liquid separation equipment through a pipeline.
preferably, in step S4, the method includes the following steps:
s410, feeding the feed of the pervaporation system into the waste heat recovery equipment, and feeding air into the heat dissipation equipment;
Step S420, detecting a third temperature of the feeding material through a third temperature sensor;
Step S430, comparing the third temperature with a third preset value:
if the third temperature is lower than a third preset value, opening the first valve, closing the second valve, and enabling the third refrigerant to sequentially enter the waste heat recovery device and the heat dissipation device, wherein the third refrigerant sequentially exchanges heat with the feed and the air to obtain a fourth refrigerant, and the fourth refrigerant is conveyed to the drying device through a pipeline;
If the third temperature is higher than the third preset value, opening the second valve, closing the first valve, and allowing the third refrigerant to enter the heat dissipation equipment;
Step S440 of detecting a fourth temperature of the third refrigerant at a second refrigerant inlet of the heat sink through a fourth temperature sensor;
Step S450, comparing the fourth temperature with a fourth preset value:
if the fourth temperature is higher than the fourth preset value, a fan of the heat dissipation device is started, the third refrigerant and the air are subjected to heat exchange to obtain a fourth refrigerant, and the fourth refrigerant is conveyed to the drying device through a pipeline;
if the fourth temperature is lower than the fourth preset value, the fan of the heat dissipation device is turned off, the third refrigerant does not need to exchange heat with the air, and the third refrigerant is conveyed to the drying device through a pipeline.
preferably, in step S4, the fourth refrigerant is delivered to a high-low pressure liquid storage device through a pipeline, and the high-low pressure liquid storage device delivers the fourth refrigerant to the drying device through a pipeline.
By adopting the technical scheme, compared with the prior art, the invention has the following technical effects:
according to the condensing system and the condensing method, waste heat is recovered, the waste heat of the high-temperature and high-pressure gas compressed by the compression equipment is effectively utilized, and the power consumption of the heat dissipation equipment is reduced; carrying out fractional condensation on the permeation vaporized gas; the infiltration vaporized gas directly carries out the heat transfer condensation with the refrigerant, compares with the current indirect heat transfer condensation that carries on of water or other solvents, can save equipment investment, operation energy consumption and area.
drawings
FIG. 1 is a schematic diagram of an exemplary embodiment of the present invention.
wherein the reference numerals are: the system comprises a compression device 1, a first valve 2, a second valve 3, a waste heat recovery device 4, a heat dissipation device 5, a fan 6, a high-low pressure liquid storage device 7, a drying device 8, a sight glass device 9, a third valve 10, a first expansion valve 11, a first temperature sensor 12, a first heat exchange device 13, a fourth valve 14, a second expansion valve 15, a second temperature sensor 16, a second heat exchange device 17, an evaporation pressure adjusting valve 18, a vapor-liquid separation device 19, a third temperature sensor 20 and a fourth temperature sensor 21.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
It should be noted that the embodiments and features of the embodiments may be combined with each other without conflict.
the invention is further described with reference to the following drawings and specific examples, which are not intended to be limiting.
Example 1
Condensing system
an exemplary embodiment of the present invention, as shown in fig. 1, is a condensation system, which includes a compression device 1, a waste heat recovery device 4, a heat dissipation device 5, a drying device 8, a first heat exchange device 13, a second heat exchange device 17, and a vapor-liquid separation device 19, wherein the compression device 1 is respectively communicated with the waste heat recovery device 4, the heat dissipation device 5, and the vapor-liquid separation device 19 through pipelines, the waste heat recovery device 4 is communicated with the heat dissipation device 5 through a pipeline, the drying device 8 is respectively communicated with the heat dissipation device 5, the first heat exchange device 13, and the second heat exchange device 17 through a pipeline, and the vapor-liquid separation device 19 is respectively communicated with the first heat exchange device 13, the second heat exchange device 17, and the compression device 1 through a pipeline.
The compression apparatus 1 includes a compression inlet provided at a lower portion of the compression apparatus 1 and a compression outlet provided at an upper portion of the compression apparatus 1.
Further, the compression apparatus 1 is a compressor.
the waste heat recovery device 4 comprises a feeding inlet, a feeding outlet, a first refrigerant inlet and a first refrigerant outlet, the feeding inlet and the first refrigerant outlet are arranged at the lower part of the waste heat recovery device 4, the feeding outlet and the first refrigerant inlet are arranged at the upper part of the waste heat recovery device 4, the feeding inlet and the feeding outlet are communicated through pipelines to form a feeding pipeline, the first refrigerant inlet and the first refrigerant outlet are communicated through pipelines to form a first refrigerant pipeline, and the feeding pipeline is not communicated with the first refrigerant pipeline.
the first refrigerant inlet is communicated with the compression outlet of the compression device 1 through a pipeline, and the first refrigerant outlet is communicated with the heat dissipation device 5 through a pipeline.
a first valve 2 is arranged on a pipeline for communicating the first inlet and the compression outlet of the refrigerant.
Further, the first valve 2 is a solenoid valve.
further, a third temperature sensor 20 is disposed at the feeding inlet of the waste heat recovery apparatus 4 for detecting the feeding temperature.
the heat dissipation device 5 comprises an air inlet, an air outlet, a second refrigerant inlet and a second refrigerant outlet, wherein the air inlet and the second refrigerant inlet are arranged at the lower part of the heat dissipation device 5, the air outlet and the second refrigerant outlet are arranged at the upper part of the heat dissipation device 5, the air inlet and the air outlet are communicated to form an air pipeline, the second refrigerant inlet and the second refrigerant outlet are communicated to form a second refrigerant pipeline, and the air pipeline is not communicated with the second refrigerant pipeline.
The second inlet of the refrigerant is communicated with the compression outlet of the compression device 1 through a pipeline, the second inlet of the refrigerant is communicated with the first outlet of the refrigerant of the waste heat recovery device 4 through a pipeline, and the second outlet of the refrigerant is communicated with the drying device 8 through a pipeline.
a second valve 3 is provided in a line communicating the second refrigerant inlet with the compression outlet.
further, the heat dissipating apparatus 5 further includes a fan 6, the fan 6 being disposed at an upper portion of the heat dissipating apparatus 5, and cool air is introduced from the air inlet and warm air is discharged from the air outlet by the fan 6.
Further, the second valve 3 is a solenoid valve.
further, a fourth temperature sensor 21 is provided at a refrigerant second inlet position of the heat radiating apparatus 5 for detecting the temperature of the third refrigerant.
the drying device 8 comprises a drying inlet and a drying outlet, the drying inlet is communicated with the second outlet of the refrigerant of the heat dissipation device 5 through a pipeline, and the drying outlet is respectively communicated with the first heat exchange device 13 and the second heat exchange device 17 through pipelines.
further, the drying device 8 is a dryer.
further, the condensing system further comprises a high-low pressure liquid storage device 7, and the high-low pressure liquid storage device 7 is communicated with the heat dissipation device 5 and the drying device 8 through pipelines respectively.
the high-low pressure liquid storage device 7 comprises a liquid storage inlet and a liquid storage outlet, the liquid storage inlet is communicated with a second refrigerant outlet of the heat dissipation device 5 through a pipeline, and the liquid storage outlet is communicated with a drying inlet of the drying device 8 through a pipeline.
first heat exchange equipment 13 includes the first import of infiltration boil-off gas, the first export of infiltration boil-off gas, refrigerant third import and refrigerant third export, the first import of infiltration boil-off gas sets up the lower part at first heat exchange equipment 13, the first export of infiltration boil-off gas sets up the upper portion at first heat exchange equipment 13, the refrigerant third import sets up the top at first heat exchange equipment 13, the refrigerant third export sets up the bottom at first heat exchange equipment 13, the first import of infiltration boil-off gas and the first export intercommunication of infiltration boil-off gas are in order to form the first pipeline of infiltration boil-off gas, refrigerant third import and refrigerant third export intercommunication are in order to form the refrigerant third pipeline, the first pipeline of infiltration boil-off gas and refrigerant third pipeline do not communicate.
The third inlet of the refrigerant is communicated with the drying outlet of the drying device 8 through a pipeline, the third outlet of the refrigerant is communicated with the vapor-liquid separation device 19 through a pipeline, and the first inlet of the permeation vaporization gas is communicated with the second heat exchange device 17 through a pipeline.
And a third valve 10 and a first expansion valve 11 are sequentially arranged on a pipeline communicated with the third inlet and the dry outlet of the refrigerant, wherein the third valve 10 is arranged at the upstream of the pipeline, and the first expansion valve 11 is arranged at the downstream of the pipeline.
a first temperature sensor 12 is provided at the first outlet position of the permeated boil-off gas.
further, the third valve 10 is a solenoid valve.
second heat exchange equipment 17 includes the gaseous second import of infiltration vaporization, the gaseous second export of infiltration vaporization, refrigerant fourth import and refrigerant fourth export, the gaseous second import of infiltration vaporization sets up the lower part at second heat exchange equipment 17, the gaseous second export of infiltration vaporization sets up the upper portion at second heat exchange equipment 17, the refrigerant fourth import sets up the top at second heat exchange equipment 6, the refrigerant fourth export sets up the bottom at second heat exchange equipment 17, the gaseous second import of infiltration vaporization and the gaseous second export intercommunication of infiltration vaporization are in order to form the gaseous first pipeline of infiltration vaporization, the refrigerant fourth import communicates with the refrigerant fourth export in order to form the refrigerant fourth pipeline, the gaseous second pipeline of infiltration vaporization and the refrigerant fourth pipeline do not communicate.
the fourth inlet of the refrigerant is communicated with the drying outlet of the drying device 8 through a pipeline, the fourth outlet of the refrigerant is communicated with the vapor-liquid separation device 19 through a pipeline, and the second outlet of the permeation vaporization gas is communicated with the first inlet of the permeation vaporization gas of the second heat exchange device through a pipeline.
And a fourth valve 14 and a second expansion valve 15 are sequentially arranged on a pipeline for communicating the fourth inlet of the refrigerant with the drying outlet, wherein the fourth valve 14 is arranged at the upstream of the pipeline, and the second expansion valve 15 is arranged at the downstream of the pipeline.
A second temperature sensor 16 is provided at the second outlet position of the permeated boil-off gas.
further, the fourth valve 14 is a solenoid valve.
further, the condensing system further comprises a sight glass device 9, and the sight glass device 9 is arranged on a pipeline of the drying device 8 communicated with the first heat exchange device 13 and the second heat exchange device 17 respectively.
Specifically, the drying outlet of the drying device 8 is communicated with a main pipeline, the main pipeline is respectively communicated with two branch pipelines, one branch pipeline is communicated with the first heat exchange device 13, the other branch pipeline is communicated with the second heat exchange device 17, the sight glass device 9 is arranged on the main pipeline, the third valve 10 and the first expansion valve 11 are arranged on one branch pipeline, and the fourth valve 14 and the second expansion valve 15 are arranged on the other branch pipeline.
the vapor-liquid separation device 19 comprises a separation inlet and a separation outlet, the separation inlet is respectively communicated with the third outlet of the refrigerant of the first heat exchange device 13 and the fourth outlet of the refrigerant of the second heat exchange device 17 through pipelines, and the separation outlet is communicated with the compression inlet of the compression device 1 through a pipeline.
Further, the condensing system further comprises an evaporation pressure regulating valve 18, and the evaporation pressure regulating valve 18 is arranged on a pipeline of the second heat exchange device 17 communicated with the vapor-liquid separation device 19.
further, the first valve 2, the second valve 3, the third valve 10, the fourth valve 14 and the compression apparatus 1 are controlled by the PLC.
Condensation method
the condensation method applied to the condensation system comprises the following steps:
Step S1, under the action of the permeated vaporized gas, the first heat exchange device 13 and the second heat exchange device 17 vaporize the refrigerant to obtain a first refrigerant, and the first refrigerant is conveyed to the vapor-liquid separation device 19 through a pipeline;
step S2, the vapor-liquid separation device 19 performs vapor-liquid separation on the first refrigerant to obtain a second refrigerant, and the second refrigerant is sent to the compression device 1 through a pipeline;
Step S3, the compression device 1 compresses the second refrigerant to obtain a third refrigerant, and the third refrigerant is sent to the heat dissipation device 5 and the waste heat recovery device 4 through a pipeline;
Step S4, after the third refrigerant is subjected to combined processing by the heat dissipation device 5 and the waste heat recovery device 4, a fourth refrigerant is obtained, and the fourth refrigerant is conveyed to the drying device 8 through a pipeline;
In step S5, the drying device 8 dries the fourth refrigerant to obtain a refrigerant, and the refrigerant is sent to the first heat exchange device 13 and the second heat exchange device 17 through the pipeline.
further, step S110, opening the third valve 10 and the fourth valve 14, allowing the refrigerant to pass through the first expansion valve 11 and the second expansion valve 15 and then enter the first heat exchange device 13 and the second heat exchange device 17, and allowing the permeated vaporized gas to enter the second heat exchange device 17 and the first heat exchange device 13 in sequence and exchange heat with the refrigerant;
Step S120, detecting a first temperature of the pervaporation gas at the first vaporization gas outlet of the first heat exchange device 13 through the first temperature sensor 12, and detecting a second temperature of the pervaporation gas at the second vaporization gas outlet of the second heat exchange device 17 through the second temperature sensor 16;
step S130, comparing the first temperature with a first preset value, and comparing the second temperature with a second preset value:
if the first temperature is higher than the first preset value, the third valve 10 is opened, and if the first temperature is equal to the first preset value, the third valve 10 is closed;
if the second temperature is higher than the second preset value, the fourth valve 14 is opened, and if the second temperature is equal to the second preset value, the fourth valve 14 is closed;
if the first temperature and the second temperature are equal to the first preset value and the second preset value, respectively, the third valve 10, the fourth valve 14 and the compression device are closed.
further, the first preset value is greater than the second preset value.
further, in step S110, the following steps are included:
step S111, adjusting the first expansion valve 11 and the second expansion valve 15 to make the temperature of the refrigerant entering the first heat exchange device 13 lower than the temperature of the refrigerant entering the second heat exchange device 17;
step S112, in the second heat exchange device 17, the refrigerant exchanges heat with the permeated vaporized gas to obtain a first refrigerant, and in the first heat exchange device 13, the refrigerant exchanges heat with the permeated vaporized gas to obtain a first refrigerant;
step S113, the pressure of the first refrigerant output by the second heat exchange device 17 is adjusted by the evaporation pressure adjusting valve 18, and the first refrigerant output by the second heat exchange device 17 is mixed with the first refrigerant output by the first heat exchange device 13 and then is conveyed to the vapor-liquid separation device through a pipeline.
Further, in step S4, the following steps are included:
S410, feeding the feed of the pervaporation system into a waste heat recovery device 4, and feeding air into a heat dissipation device 5;
Step S420, detecting a third temperature of the feeding material through a third temperature sensor 20;
Step S430, comparing the third temperature with a third preset value:
if the third temperature is lower than a third preset value, the first valve 2 is opened, the second valve 3 is closed, the third refrigerant sequentially enters the waste heat recovery device 4 and the heat dissipation device 5, the third refrigerant sequentially exchanges heat with the feeding material and the air to obtain a fourth refrigerant, and the fourth refrigerant is conveyed to the drying device 8 through a pipeline;
If the third temperature is higher than a third preset value, the second valve 3 is opened, the first valve 2 is closed, the third refrigerant enters the heat dissipation device 5, the third refrigerant exchanges heat with air to obtain a fourth refrigerant, and the fourth refrigerant is conveyed to the drying device 8 through a pipeline;
Step S440 of detecting a fourth temperature of the third refrigerant at the second refrigerant inlet of the heat radiating apparatus 5 by the fourth temperature sensor 21;
step S450, comparing the fourth temperature with a fourth preset value:
If the fourth temperature is higher than a fourth preset value, starting a fan 6 of the heat dissipation device 5, carrying out heat exchange on the third refrigerant and air to obtain a fourth refrigerant, and conveying the fourth refrigerant to a drying device 8 through a pipeline;
If the fourth temperature is lower than the fourth preset value, the fan 6 of the heat dissipation device 5 is turned off, and the third refrigerant is delivered to the drying device 8 through the pipeline without exchanging heat with air.
further, in step S4, the fourth refrigerant is delivered to the high-low pressure liquid storage device 7 through a pipeline, and the high-low pressure liquid storage device 7 delivers the fourth refrigerant to the drying device 8 through a pipeline.
Further, in step S4, the third refrigerant is delivered to the high-low pressure liquid storage device 7 through a pipeline, and the high-low pressure liquid storage device 7 delivers the third refrigerant to the drying device 8 through a pipeline.
The invention has the advantages that the high-pressure gas treated by the compressor exchanges heat with the feed of the pervaporation system, thereby realizing waste heat recovery and reducing the power consumption of the heat dissipation equipment; the refrigerant is directly subjected to heat exchange condensation with the permeation vaporization gas, the first heat exchange equipment and the second heat exchange equipment are utilized to carry out fractional condensation, the low-boiling-point gas is firstly condensed, and the high-boiling-point gas is then condensed, so that the recycling of the high-purity organic liquid is realized.
example 2
this embodiment is a practical application of the condensing system of the present invention.
adding certain wastewater containing 10% of N, N Dimethylformamide (DMF) into a feeding tank of an pervaporation membrane system, starting a feeding circulating pump, a heater and a condensing system, heating the feeding temperature to 50 ℃ by electric heating and condensation waste heat recovery, then closing the electric heating, and realizing that the feeding temperature is maintained at 50 ℃ by waste heat recovery and heat preservation; setting the first-stage condensation temperature (second heat exchange equipment 17) of the condensation system to be 10 ℃, setting the second-stage condensation temperature (first heat exchange equipment 13) to be 0 ℃, then starting the vacuum pump, condensing and recovering DMF through the pervaporation membrane, enabling the DMF content of the first-stage condensate to reach 50 percent and the DMF content of the second-stage condensate to be 5 percent, and returning to the feeding tank for further pervaporation.
through the technical scheme, the energy consumption is reduced by 30%, the DMF recovery rate reaches 80%, and the condensation efficiency reaches 95%.
While the invention has been described with reference to a preferred embodiment, it will be understood by those skilled in the art that various changes in form and detail may be made therein without departing from the spirit and scope of the invention.
Claims (10)
1. A condensing system for use with a pervaporation membrane system, comprising:
A compression device;
The waste heat recovery device is communicated with the compression device through a pipeline, and a first valve is arranged on the pipeline which is communicated with the waste heat recovery device and the compression device;
The heat dissipation equipment is respectively communicated with the compression equipment and the waste heat recovery equipment through a pipeline, and a second valve is arranged on the pipeline;
The drying equipment is communicated with the heat dissipation equipment through a pipeline;
The first heat exchange equipment is communicated with the drying equipment through a pipeline, and a third valve and a first expansion valve are arranged on the pipeline;
The second heat exchange equipment is respectively communicated with the drying equipment and the first heat exchange equipment through pipelines, and a fourth valve and a second expansion valve are arranged on the pipeline communicated with the second heat exchange equipment and the drying equipment;
and the gas-liquid separation equipment is respectively communicated with the compression equipment, the first heat exchange equipment and the second heat exchange equipment through pipelines.
2. the condensing system of claim 1, further comprising:
and the high-low pressure liquid storage equipment is communicated with the heat dissipation equipment and the drying equipment through pipelines respectively.
3. the condensing system of claim 1, further comprising:
and the evaporation pressure regulating valve is arranged on a pipeline for communicating the second heat exchange equipment with the vapor-liquid separation equipment.
4. the condensing system of claim 1, further comprising:
The first temperature sensor is arranged on the first heat exchange equipment;
the second temperature sensor is arranged on the second heat exchange equipment;
a third temperature sensor disposed at the waste heat recovery device;
A fourth temperature sensor disposed at the heat sink.
5. The condensing system of claim 1, further comprising:
the sight glass equipment is arranged on a pipeline which is communicated with the drying equipment and the first heat exchange equipment and the second heat exchange equipment respectively;
A fan disposed at the heat sink.
6. A condensation method applied to the condensation system as claimed in any one of claims 1 to 5, characterized by comprising the following steps:
step S1, under the action of permeation vaporization gas, the first heat exchange device and the second heat exchange device vaporize refrigerants to obtain a first refrigerant, and the first refrigerant is conveyed to the vapor-liquid separation device through a pipeline;
Step S2, the vapor-liquid separation device performs vapor-liquid separation on the first refrigerant to obtain a second refrigerant, and the second refrigerant is sent to the compression device through a pipeline;
Step S3, the compression device compresses the second refrigerant to obtain a third refrigerant, and the third refrigerant is sent to the heat dissipation device and the waste heat recovery device through a pipeline;
step S4, after the third refrigerant is processed by the combination of the heat dissipation device and the waste heat recovery device, obtaining a fourth refrigerant, and the fourth refrigerant is conveyed to the drying device through a pipeline;
step S5, after the drying device performs drying processing on the fourth refrigerant, the refrigerant is obtained, and the refrigerant is sent to the first heat exchange device and the second heat exchange device through a pipeline.
7. a condensation method according to claim 6, characterized by comprising, in step S1, the steps of:
Step S110, opening the third valve and the fourth valve, wherein the refrigerant passes through the first expansion valve and the second expansion valve and then enters the first heat exchange device and the second heat exchange device, and the permeated vaporized gas sequentially enters the second heat exchange device and the first heat exchange device and exchanges heat with the refrigerant;
Step S120, detecting a first temperature of the pervaporation gas at a first gasification gas outlet of the first heat exchange device through a first temperature sensor, and detecting a second temperature of the pervaporation gas at a second gasification gas outlet of the second heat exchange device through a second temperature sensor;
Step S130, comparing the first temperature with a first preset value, and comparing the second temperature with a second preset value:
if the first temperature is higher than the first preset value, opening the third valve, and if the first temperature is equal to the first preset value, closing the third valve;
If the second temperature is higher than the second preset value, the fourth valve is opened, and if the second temperature is equal to the second preset value, the fourth valve is closed;
If the first temperature and the second temperature are respectively equal to the first preset value and the second preset value at the same time, closing the third valve, the fourth valve and the compression equipment;
Wherein the first preset value is greater than the second preset value.
8. a condensation method according to claim 7, characterized by comprising, in said step S110, the steps of:
step S111, adjusting the first expansion valve and the second expansion valve to enable the temperature of the refrigerant entering the first heat exchange device to be lower than the temperature of the refrigerant entering the second heat exchange device;
Step S112, in the second heat exchange device, the refrigerant exchanges heat with the pervaporation gas to obtain the first refrigerant, and in the first heat exchange device, the refrigerant exchanges heat with the pervaporation gas to obtain the first refrigerant;
step S113, the pressure of the first refrigerant output by the second heat exchange equipment is adjusted through an evaporation pressure adjusting valve, and the first refrigerant output by the second heat exchange equipment and the first refrigerant output by the first heat exchange equipment are mixed and then are conveyed to the vapor-liquid separation equipment through a pipeline.
9. a condensation method according to claim 6, characterized by comprising, in step S4, the steps of:
s410, feeding the feed of the pervaporation system into the waste heat recovery equipment, and feeding air into the heat dissipation equipment;
Step S420, detecting a third temperature of the feeding material through a third temperature sensor;
step S430, comparing the third temperature with a third preset value:
If the third temperature is lower than a third preset value, opening the first valve, closing the second valve, and enabling the third refrigerant to sequentially enter the waste heat recovery device and the heat dissipation device, wherein the third refrigerant sequentially exchanges heat with the feed and the air to obtain a fourth refrigerant, and the fourth refrigerant is conveyed to the drying device through a pipeline;
If the third temperature is higher than the third preset value, opening the second valve, closing the first valve, and allowing the third refrigerant to enter the heat dissipation equipment;
step S440 of detecting a fourth temperature of the third refrigerant at a second refrigerant inlet of the heat sink through a fourth temperature sensor;
Step S450, comparing the fourth temperature with a fourth preset value:
If the fourth temperature is higher than the fourth preset value, a fan of the heat dissipation device is started, the third refrigerant and the air are subjected to heat exchange to obtain a fourth refrigerant, and the fourth refrigerant is conveyed to the drying device through a pipeline;
if the fourth temperature is lower than the fourth preset value, the fan of the heat dissipation device is turned off, the third refrigerant does not need to exchange heat with the air, and the third refrigerant is conveyed to the drying device through a pipeline.
10. a condensation method according to claim 6 or 9, wherein in step S4, the fourth refrigerant is delivered through a line to a high-low pressure liquid storage device which delivers the fourth refrigerant through a line to the drying device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910913008.XA CN110538480B (en) | 2019-09-25 | 2019-09-25 | Condensing system and condensing method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910913008.XA CN110538480B (en) | 2019-09-25 | 2019-09-25 | Condensing system and condensing method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110538480A true CN110538480A (en) | 2019-12-06 |
| CN110538480B CN110538480B (en) | 2024-09-17 |
Family
ID=68714706
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910913008.XA Active CN110538480B (en) | 2019-09-25 | 2019-09-25 | Condensing system and condensing method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110538480B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111991828A (en) * | 2020-09-29 | 2020-11-27 | 广州市爱百伊生物技术有限公司 | Device and method for purifying tender repair essence |
| CN112537873A (en) * | 2020-10-12 | 2021-03-23 | 太原理工大学 | Treatment process and device for coal chemical wastewater containing fine dust |
Citations (60)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR54754E (en) * | 1946-05-21 | 1950-08-01 | Standard Oil Dev Co | Fuel treatment process |
| AU4384085A (en) * | 1984-07-18 | 1986-01-23 | Voest-Alpine Industrieanlagenbau Gmbh | Apparatus for cooling a hot product gas |
| EP0264113A1 (en) * | 1986-10-14 | 1988-04-20 | Gkss-Forschungszentrum Geesthacht Gmbh | Pervaporation of phenols |
| JPH0295419A (en) * | 1988-09-30 | 1990-04-06 | Niigata Eng Co Ltd | Liquid/liquid separating device |
| JPH02273519A (en) * | 1989-04-14 | 1990-11-08 | Toray Ind Inc | Concentrate of volatile organic liquid aqueous solution |
| JPH05137969A (en) * | 1991-11-19 | 1993-06-01 | Mitsui Eng & Shipbuild Co Ltd | Method of recovering organic substances by pervaporation |
| JPH0634225A (en) * | 1992-07-22 | 1994-02-08 | Daikin Ind Ltd | Apparatus and method for air conditioning using moisture absorption liquid |
| JPH07227517A (en) * | 1994-02-17 | 1995-08-29 | Nisso Eng Kk | Separation of liquid mixture |
| JPH10314551A (en) * | 1997-05-20 | 1998-12-02 | Sekiyu Sangyo Kasseika Center | Separation method |
| CN1212677A (en) * | 1996-01-25 | 1999-03-31 | 埃克森化学有限公司 | Processf or preparing parasylene |
| JP2000249409A (en) * | 1999-02-26 | 2000-09-14 | Kobe Steel Ltd | Flow rate control method of non-azeotropic mixed refrigerant in cooler |
| US6481243B1 (en) * | 2001-04-02 | 2002-11-19 | Wei Fang | Pressure accumulator at high pressure side and waste heat re-use device for vapor compressed air conditioning or refrigeration equipment |
| JP2003028518A (en) * | 2001-07-19 | 2003-01-29 | Fujitsu General Ltd | Air conditioner |
| KR20030041380A (en) * | 2001-11-20 | 2003-05-27 | 이미자 | Refrigeration system |
| CN1421405A (en) * | 2001-10-25 | 2003-06-04 | 雅马哈株式会社 | Waste liquid treatment method and waste liquid treating equipment with the same method |
| ES1063534U (en) * | 2006-07-27 | 2006-11-01 | Mondetu, S.L. | Water cooling machine |
| JP2006346607A (en) * | 2005-06-17 | 2006-12-28 | Orion Mach Co Ltd | Freezing preventive method for heat exchanger in dehumidification apparatus of compressed gas, and dehumidification apparatus of compressed gas |
| JP2007017107A (en) * | 2005-07-08 | 2007-01-25 | Green Seiju:Kk | Drying system |
| US20070101759A1 (en) * | 2003-06-20 | 2007-05-10 | Daikin Industries, Ltd. | Refrigeration apparatus constructing method, and refrigeration apparatus |
| WO2008055322A1 (en) * | 2006-11-10 | 2008-05-15 | Atlas Copco Airpower, Naamloze Vennootschap | Method for cool drying. |
| CN101239884A (en) * | 2008-03-09 | 2008-08-13 | 大连理工大学 | Film separation method for difluo-monochloromethane and trifluoromethane mixture |
| WO2009006307A1 (en) * | 2007-06-28 | 2009-01-08 | Trans Ionics Corporation | Benzene recovery process |
| KR20090015458A (en) * | 2007-08-08 | 2009-02-12 | 신영중공업주식회사 | A bog re-liquefaction system and method for lng carrier |
| CN201295584Y (en) * | 2008-11-14 | 2009-08-26 | 嘉园环保股份有限公司 | Organic waste gas recycling device |
| CN102040303A (en) * | 2009-10-23 | 2011-05-04 | 中国石油化工股份有限公司 | Method for recovering organic matters in wastewater generated in process for preparing olefin from methanol |
| CN102444967A (en) * | 2011-12-12 | 2012-05-09 | 青岛海尔空调电子有限公司 | Method and system for recovering waste heat of air conditioning system |
| CN102500236A (en) * | 2011-12-30 | 2012-06-20 | 北京清大国华环保科技有限公司 | Method and device of high-efficient energy-saving hydropower molecular film |
| JP2013002714A (en) * | 2011-06-15 | 2013-01-07 | Tlv Co Ltd | Waste vapor recovering device |
| CN103052437A (en) * | 2010-08-05 | 2013-04-17 | 新日铁住金工程技术株式会社 | Membrane separation apparatus and membrane separation method |
| CN103071307A (en) * | 2013-01-23 | 2013-05-01 | 江苏九天高科技股份有限公司 | Rectification-steam penetration-coupled organic solvent dewatering method and device |
| CN103551036A (en) * | 2013-11-21 | 2014-02-05 | 洪梅 | High-efficiency permeation and evaporation device and technology of ceramic molecular sieve membrane |
| CN103709016A (en) * | 2013-12-21 | 2014-04-09 | 江苏九天高科技股份有限公司 | Process and device for refining glycol dimethyl ether by using pervaporation method |
| CN103958398A (en) * | 2011-09-27 | 2014-07-30 | 国际热化学恢复股份有限公司 | System and method for syngas clean-up |
| CN203886225U (en) * | 2014-05-09 | 2014-10-22 | 常州市西屋自动化有限公司 | Heat energy and solvent recycling device for drying equipment |
| CN104109078A (en) * | 2014-06-25 | 2014-10-22 | 江苏九天高科技股份有限公司 | Method for recovering ethanol in analginum production |
| CN204301555U (en) * | 2014-09-11 | 2015-04-29 | 华北水利水电大学 | One utilizes industrial exhaust heat condensed water demist cooling tower |
| CN104587834A (en) * | 2015-01-27 | 2015-05-06 | 太原理工大学 | Device and method for separating and recovering high-boiling-point organic matter from low-concentration aqueous solution |
| US20150174523A1 (en) * | 2012-07-13 | 2015-06-25 | L'air Liquide, Societé Anonyme Pour L'etude Et L'exploitation Des Procédés Georges Claude | Process and apparatus for the separation of a stream containing carbon dioxide, water and at least one light impurity including a separation step at subambient temperature |
| CN105218317A (en) * | 2015-11-03 | 2016-01-06 | 江苏九天高科技股份有限公司 | A kind of method that in hexanitrobibenzyl production, ethanol reclaims and device |
| CN204958383U (en) * | 2015-08-05 | 2016-01-13 | 陕西延长石油兴化化工有限公司 | Recycle system of tail gas is retrieved to methanol synthesis hydrogen |
| CN105263602A (en) * | 2013-04-16 | 2016-01-20 | 恩必安有限公司 | Air purifying filter with desorption unit using microwave heating and air purifying device using the same |
| CN105289018A (en) * | 2015-11-13 | 2016-02-03 | 中国海洋石油总公司 | MVR-vapor permeation coupling device and method used for organic solvent dehydration |
| CA2966050A1 (en) * | 2014-10-27 | 2016-05-06 | Intex Holdings Pty Ltd | System and method of cooling by latent energy transfer |
| KR101621523B1 (en) * | 2014-12-05 | 2016-05-17 | 하이에어공조 주식회사 | Heat pump type dehumidification system for drying paint |
| CN105817123A (en) * | 2016-04-18 | 2016-08-03 | 东南大学 | Compressed air deep-drying device and method capable of adjusting pressure dew point |
| CN106277537A (en) * | 2016-11-02 | 2017-01-04 | 中国石油大学(华东) | A kind of a new combined process processed for high level salt solution continuous dehydration |
| CN106742888A (en) * | 2016-12-15 | 2017-05-31 | 安徽科海压缩机制造有限公司 | The shallow cold recovery device of the supercharging of volatile organic steam in a kind of oil gas |
| CN107300262A (en) * | 2017-08-05 | 2017-10-27 | 广州赛普里仪器有限公司 | A kind of intelligent condenser system and its control method |
| CN107469555A (en) * | 2017-08-30 | 2017-12-15 | 陈进 | Gas recovery system for oil and oil-gas recovery method |
| CN107758618A (en) * | 2016-08-17 | 2018-03-06 | 中国石油化工股份有限公司 | The recovery system and recovery method of the hydrogeneous emission of low volume fraction |
| US20180094844A1 (en) * | 2015-04-03 | 2018-04-05 | Mitsubishi Electric Corporation | Refrigeration cycle apparatus and refrigeration cycle system |
| EP3385248A1 (en) * | 2017-04-07 | 2018-10-10 | Linde Aktiengesellschaft | Method and installation for the production of one or more olefins |
| CN109052526A (en) * | 2018-08-28 | 2018-12-21 | 盛发环保科技（厦门）有限公司 | Flue gas disappears white coupling high temperature bypass flue evaporation high slat-containing wastewater Zero discharging system |
| CN109224755A (en) * | 2018-10-19 | 2019-01-18 | 南京工业大学 | Utilize cryogenic VOCs multistage cooling recovery system of air expansion |
| CN208736034U (en) * | 2018-08-16 | 2019-04-12 | 大连欧科膜技术工程有限公司 | A kind of polypropylene tail gas recovery device |
| CN109833641A (en) * | 2019-04-04 | 2019-06-04 | 上海电气集团股份有限公司 | A kind of strong brine crystal system and application method |
| US20190255459A1 (en) * | 2016-10-28 | 2019-08-22 | Agisen Limited | Compressed gas drying system |
| CN209286702U (en) * | 2018-12-17 | 2019-08-23 | 中化弘润石油化工有限公司 | Energy-saving recovery device is used in a kind of production of polypropylene |
| CN211383863U (en) * | 2019-09-25 | 2020-09-01 | 上海电气集团股份有限公司 | Novel condensing system |
| CN114716098A (en) * | 2022-03-25 | 2022-07-08 | 上海电气集团股份有限公司 | Treatment method and treatment system for crystalline silicon texturing wastewater |
-
2019
- 2019-09-25 CN CN201910913008.XA patent/CN110538480B/en active Active
Patent Citations (61)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR54754E (en) * | 1946-05-21 | 1950-08-01 | Standard Oil Dev Co | Fuel treatment process |
| AU4384085A (en) * | 1984-07-18 | 1986-01-23 | Voest-Alpine Industrieanlagenbau Gmbh | Apparatus for cooling a hot product gas |
| EP0264113A1 (en) * | 1986-10-14 | 1988-04-20 | Gkss-Forschungszentrum Geesthacht Gmbh | Pervaporation of phenols |
| JPH0295419A (en) * | 1988-09-30 | 1990-04-06 | Niigata Eng Co Ltd | Liquid/liquid separating device |
| JPH02273519A (en) * | 1989-04-14 | 1990-11-08 | Toray Ind Inc | Concentrate of volatile organic liquid aqueous solution |
| JPH05137969A (en) * | 1991-11-19 | 1993-06-01 | Mitsui Eng & Shipbuild Co Ltd | Method of recovering organic substances by pervaporation |
| JPH0634225A (en) * | 1992-07-22 | 1994-02-08 | Daikin Ind Ltd | Apparatus and method for air conditioning using moisture absorption liquid |
| JPH07227517A (en) * | 1994-02-17 | 1995-08-29 | Nisso Eng Kk | Separation of liquid mixture |
| CN1212677A (en) * | 1996-01-25 | 1999-03-31 | 埃克森化学有限公司 | Processf or preparing parasylene |
| JPH10314551A (en) * | 1997-05-20 | 1998-12-02 | Sekiyu Sangyo Kasseika Center | Separation method |
| JP2000249409A (en) * | 1999-02-26 | 2000-09-14 | Kobe Steel Ltd | Flow rate control method of non-azeotropic mixed refrigerant in cooler |
| US6481243B1 (en) * | 2001-04-02 | 2002-11-19 | Wei Fang | Pressure accumulator at high pressure side and waste heat re-use device for vapor compressed air conditioning or refrigeration equipment |
| JP2003028518A (en) * | 2001-07-19 | 2003-01-29 | Fujitsu General Ltd | Air conditioner |
| CN1421405A (en) * | 2001-10-25 | 2003-06-04 | 雅马哈株式会社 | Waste liquid treatment method and waste liquid treating equipment with the same method |
| KR20030041380A (en) * | 2001-11-20 | 2003-05-27 | 이미자 | Refrigeration system |
| US20070101759A1 (en) * | 2003-06-20 | 2007-05-10 | Daikin Industries, Ltd. | Refrigeration apparatus constructing method, and refrigeration apparatus |
| JP2006346607A (en) * | 2005-06-17 | 2006-12-28 | Orion Mach Co Ltd | Freezing preventive method for heat exchanger in dehumidification apparatus of compressed gas, and dehumidification apparatus of compressed gas |
| JP2007017107A (en) * | 2005-07-08 | 2007-01-25 | Green Seiju:Kk | Drying system |
| ES1063534U (en) * | 2006-07-27 | 2006-11-01 | Mondetu, S.L. | Water cooling machine |
| WO2008055322A1 (en) * | 2006-11-10 | 2008-05-15 | Atlas Copco Airpower, Naamloze Vennootschap | Method for cool drying. |
| WO2009006307A1 (en) * | 2007-06-28 | 2009-01-08 | Trans Ionics Corporation | Benzene recovery process |
| KR20090015458A (en) * | 2007-08-08 | 2009-02-12 | 신영중공업주식회사 | A bog re-liquefaction system and method for lng carrier |
| CN101239884A (en) * | 2008-03-09 | 2008-08-13 | 大连理工大学 | Film separation method for difluo-monochloromethane and trifluoromethane mixture |
| CN201295584Y (en) * | 2008-11-14 | 2009-08-26 | 嘉园环保股份有限公司 | Organic waste gas recycling device |
| CN102040303A (en) * | 2009-10-23 | 2011-05-04 | 中国石油化工股份有限公司 | Method for recovering organic matters in wastewater generated in process for preparing olefin from methanol |
| CN103052437A (en) * | 2010-08-05 | 2013-04-17 | 新日铁住金工程技术株式会社 | Membrane separation apparatus and membrane separation method |
| JP2013002714A (en) * | 2011-06-15 | 2013-01-07 | Tlv Co Ltd | Waste vapor recovering device |
| CN103958398A (en) * | 2011-09-27 | 2014-07-30 | 国际热化学恢复股份有限公司 | System and method for syngas clean-up |
| CN102444967A (en) * | 2011-12-12 | 2012-05-09 | 青岛海尔空调电子有限公司 | Method and system for recovering waste heat of air conditioning system |
| CN102500236A (en) * | 2011-12-30 | 2012-06-20 | 北京清大国华环保科技有限公司 | Method and device of high-efficient energy-saving hydropower molecular film |
| US20150174523A1 (en) * | 2012-07-13 | 2015-06-25 | L'air Liquide, Societé Anonyme Pour L'etude Et L'exploitation Des Procédés Georges Claude | Process and apparatus for the separation of a stream containing carbon dioxide, water and at least one light impurity including a separation step at subambient temperature |
| CN103071307A (en) * | 2013-01-23 | 2013-05-01 | 江苏九天高科技股份有限公司 | Rectification-steam penetration-coupled organic solvent dewatering method and device |
| CN105263602A (en) * | 2013-04-16 | 2016-01-20 | 恩必安有限公司 | Air purifying filter with desorption unit using microwave heating and air purifying device using the same |
| CN103551036A (en) * | 2013-11-21 | 2014-02-05 | 洪梅 | High-efficiency permeation and evaporation device and technology of ceramic molecular sieve membrane |
| CN103709016A (en) * | 2013-12-21 | 2014-04-09 | 江苏九天高科技股份有限公司 | Process and device for refining glycol dimethyl ether by using pervaporation method |
| CN203886225U (en) * | 2014-05-09 | 2014-10-22 | 常州市西屋自动化有限公司 | Heat energy and solvent recycling device for drying equipment |
| CN104109078A (en) * | 2014-06-25 | 2014-10-22 | 江苏九天高科技股份有限公司 | Method for recovering ethanol in analginum production |
| CN204301555U (en) * | 2014-09-11 | 2015-04-29 | 华北水利水电大学 | One utilizes industrial exhaust heat condensed water demist cooling tower |
| CA2966050A1 (en) * | 2014-10-27 | 2016-05-06 | Intex Holdings Pty Ltd | System and method of cooling by latent energy transfer |
| KR101621523B1 (en) * | 2014-12-05 | 2016-05-17 | 하이에어공조 주식회사 | Heat pump type dehumidification system for drying paint |
| CN104587834A (en) * | 2015-01-27 | 2015-05-06 | 太原理工大学 | Device and method for separating and recovering high-boiling-point organic matter from low-concentration aqueous solution |
| US20180094844A1 (en) * | 2015-04-03 | 2018-04-05 | Mitsubishi Electric Corporation | Refrigeration cycle apparatus and refrigeration cycle system |
| CN204958383U (en) * | 2015-08-05 | 2016-01-13 | 陕西延长石油兴化化工有限公司 | Recycle system of tail gas is retrieved to methanol synthesis hydrogen |
| CN105218317A (en) * | 2015-11-03 | 2016-01-06 | 江苏九天高科技股份有限公司 | A kind of method that in hexanitrobibenzyl production, ethanol reclaims and device |
| CN105289018A (en) * | 2015-11-13 | 2016-02-03 | 中国海洋石油总公司 | MVR-vapor permeation coupling device and method used for organic solvent dehydration |
| CN105817123A (en) * | 2016-04-18 | 2016-08-03 | 东南大学 | Compressed air deep-drying device and method capable of adjusting pressure dew point |
| WO2017181439A1 (en) * | 2016-04-18 | 2017-10-26 | 东南大学 | Pressure dew point adjustable compressed air deep-drying apparatus and method |
| CN107758618A (en) * | 2016-08-17 | 2018-03-06 | 中国石油化工股份有限公司 | The recovery system and recovery method of the hydrogeneous emission of low volume fraction |
| US20190255459A1 (en) * | 2016-10-28 | 2019-08-22 | Agisen Limited | Compressed gas drying system |
| CN106277537A (en) * | 2016-11-02 | 2017-01-04 | 中国石油大学(华东) | A kind of a new combined process processed for high level salt solution continuous dehydration |
| CN106742888A (en) * | 2016-12-15 | 2017-05-31 | 安徽科海压缩机制造有限公司 | The shallow cold recovery device of the supercharging of volatile organic steam in a kind of oil gas |
| EP3385248A1 (en) * | 2017-04-07 | 2018-10-10 | Linde Aktiengesellschaft | Method and installation for the production of one or more olefins |
| CN107300262A (en) * | 2017-08-05 | 2017-10-27 | 广州赛普里仪器有限公司 | A kind of intelligent condenser system and its control method |
| CN107469555A (en) * | 2017-08-30 | 2017-12-15 | 陈进 | Gas recovery system for oil and oil-gas recovery method |
| CN208736034U (en) * | 2018-08-16 | 2019-04-12 | 大连欧科膜技术工程有限公司 | A kind of polypropylene tail gas recovery device |
| CN109052526A (en) * | 2018-08-28 | 2018-12-21 | 盛发环保科技（厦门）有限公司 | Flue gas disappears white coupling high temperature bypass flue evaporation high slat-containing wastewater Zero discharging system |
| CN109224755A (en) * | 2018-10-19 | 2019-01-18 | 南京工业大学 | Utilize cryogenic VOCs multistage cooling recovery system of air expansion |
| CN209286702U (en) * | 2018-12-17 | 2019-08-23 | 中化弘润石油化工有限公司 | Energy-saving recovery device is used in a kind of production of polypropylene |
| CN109833641A (en) * | 2019-04-04 | 2019-06-04 | 上海电气集团股份有限公司 | A kind of strong brine crystal system and application method |
| CN211383863U (en) * | 2019-09-25 | 2020-09-01 | 上海电气集团股份有限公司 | Novel condensing system |
| CN114716098A (en) * | 2022-03-25 | 2022-07-08 | 上海电气集团股份有限公司 | Treatment method and treatment system for crystalline silicon texturing wastewater |
Non-Patent Citations (1)
| Title |
|---|
| 刘志勇;沈长海;邹金校;崔亚;彭政瑜;: "电动汽车空调与电池热管理系统设计与匹配", 制冷与空调, no. 01, 28 January 2018 (2018-01-28) * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111991828A (en) * | 2020-09-29 | 2020-11-27 | 广州市爱百伊生物技术有限公司 | Device and method for purifying tender repair essence |
| CN112537873A (en) * | 2020-10-12 | 2021-03-23 | 太原理工大学 | Treatment process and device for coal chemical wastewater containing fine dust |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110538480B (en) | 2024-09-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CA2750780C (en) | Method and device for separating of carbon dioxide from an exhaust gas of a fossil-fired power plant | |
| CN101906800B (en) | Device and method for recovering liquid water from air based on vacuum dehumidification membrane | |
| WO2017181439A1 (en) | Pressure dew point adjustable compressed air deep-drying apparatus and method | |
| CN210495768U (en) | Device for recycling dichloromethane of diaphragm of lithium battery by wet process through compression condensation membrane separation technology | |
| EP2478312A1 (en) | Auto-refrigerated gas separation system for carbon dioxide capture and compression | |
| CN107940801B (en) | A kind of space division system recycling compressed air waste-heat | |
| CN113175687B (en) | System and method for capturing and purifying carbon dioxide in flue gas | |
| CN110538480B (en) | Condensing system and condensing method | |
| CN114279254B (en) | Flue gas waste heat utilization and carbon dioxide capturing and recycling process | |
| CN110255855B (en) | Dual-cold-heat-source heat pump sludge low-temperature drying system with waste heat recovery function and application method thereof | |
| WO2022112366A1 (en) | Providing heat energy to direct air carbon dioxide capture processes using waste heat from data centre | |
| CN106315717A (en) | MVR wastewater evaporation and concentration system | |
| WO2020019922A1 (en) | Heat pump solution concentration cogeneration system and method | |
| US20230143266A1 (en) | Method and system for the production of liquid biogas | |
| CN211383863U (en) | Novel condensing system | |
| CN210764423U (en) | Heat pump vacuum waste liquid concentration treatment device | |
| CN214700775U (en) | Flue gas carbon dioxide entrapment purification system | |
| CN103900346A (en) | Method and device for liquefying carbon dioxide generated through efficient gas source heat pump in cold and hot combination mode | |
| CN103881781A (en) | Marsh gas membrane separation methane purifying technology | |
| CN203525336U (en) | Low-temperature evaporation and concentration device | |
| JP3867662B2 (en) | Air dryer | |
| CN102949911B (en) | Device for efficiently separating gas mixture of helium and carbon dioxide and separation method | |
| CN210521790U (en) | Traditional chinese medicine enrichment facility based on carbon dioxide heat pump technology | |
| CN110960955B (en) | Carbon dioxide capture system | |
| RU2321797C1 (en) | Method of preparing oil gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |