CN106512450A - Miniaturized energy-saving evaporative regeneration device - Google Patents
Miniaturized energy-saving evaporative regeneration device Download PDFInfo
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- CN106512450A CN106512450A CN201611253324.1A CN201611253324A CN106512450A CN 106512450 A CN106512450 A CN 106512450A CN 201611253324 A CN201611253324 A CN 201611253324A CN 106512450 A CN106512450 A CN 106512450A
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- 230000008929 regeneration Effects 0.000 title abstract description 4
- 238000011069 regeneration method Methods 0.000 title abstract description 4
- 238000010438 heat treatment Methods 0.000 claims abstract description 50
- 239000007788 liquid Substances 0.000 claims abstract description 50
- 239000011550 stock solution Substances 0.000 claims abstract description 39
- 238000001816 cooling Methods 0.000 claims abstract description 17
- 239000002826 coolant Substances 0.000 claims abstract description 14
- 239000000243 solution Substances 0.000 claims abstract description 5
- 238000001704 evaporation Methods 0.000 claims description 41
- 230000008020 evaporation Effects 0.000 claims description 41
- 230000001172 regenerating effect Effects 0.000 claims description 20
- 230000008676 import Effects 0.000 claims description 14
- 239000003814 drug Substances 0.000 claims description 5
- 241000628997 Flos Species 0.000 claims description 4
- 239000002244 precipitate Substances 0.000 claims description 4
- 238000010025 steaming Methods 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 4
- 238000004821 distillation Methods 0.000 abstract 7
- 238000003889 chemical engineering Methods 0.000 abstract 1
- 239000000463 material Substances 0.000 description 10
- 230000006872 improvement Effects 0.000 description 7
- 238000000034 method Methods 0.000 description 7
- 239000000047 product Substances 0.000 description 4
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 239000011344 liquid material Substances 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000010512 thermal transition Effects 0.000 description 2
- 238000009835 boiling Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000006200 vaporizer Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/0011—Heating features
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/0011—Heating features
- B01D1/0041—Use of fluids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/0011—Heating features
- B01D1/0041—Use of fluids
- B01D1/0047—Use of fluids in a closed circuit
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/007—Energy recuperation; Heat pumps
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/02—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in boilers or stills
-
- 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
-
- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/10—Energy recovery
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention relates to a miniaturized energy-saving evaporative regeneration device. The device comprises a stock solution box, a concentrated solution box, a distillation still, a heat pump unit, a first heat exchanger, a second heat exchanger, a cooling fan and a steam-liquid cooling box; the distillation still comprises a main distillation still body and an auxiliary distillation still body, a first heating chamber and a first stock solution inlet are formed in the main distillation still body, and a first steam outlet is formed in the top of the main distillation still body; an outlet of the heat pump unit is connected with an inlet of the first heating chamber, an inlet of the heat pump unit is connected with a cooling medium outlet of the steam-liquid cooling box, and a cooling medium inlet is connected with an outlet of the first heating chamber through the cooling fan; an inlet of a second heating chamber of the auxiliary distillation still body is connected with the first steam outlet, an outlet of the second heating chamber is connected with a second steam-liquid inlet, a second vacuum pump is connected with a steam-liquid outlet, a second steam outlet is connected with a first steam-liquid inlet, and a second stock solution inlet communicates with the stock solution box. The miniaturized energy-saving evaporative regeneration device is small in size, low in investment and energy consumption, wide in application range and suitable for the industries of chemical engineering, pharmacy, water treatment and the like.
Description
Technical field
The present invention relates to a kind of liquid material processing meanss.Specifically, it is for trade effluent, containing the organic of impurity
The liquid materials such as solvent carry out the evaporation regenerating unit for purifying, regenerating.Suitable for industries such as chemical industry, pharmacy, water process.
Background technology
At present, in industries such as chemical industry, pharmacy, water process, for liquid such as trade effluent, the organic solvents containing impurity
The evaporation regenerating unit that material carries out purifying, regenerating mainly has multiple-effect evaporation, three kinds of sides of multistage flash evaporation and function of mechanical steam recompression
Formula.Multiple-effect evaporation therein and multistage flash evaporation mode need a large amount of steam as thermal source, and device therefor is large sized complete sets of equipment, no
Only energy consumption is more, invests larger.And function of mechanical steam recompression mode, heated using steam only in start, produced in device to be evaporated
After steam, the indirect steam produced in compressor is to vaporizer is compressed, improve indirect steam energy and plus
To utilize, so as to reclaim the potential of indirect steam, energy consumption is reduced.Although function of mechanical steam recompression mode can reduce energy
Consumption, but still need to be equipped with the auxiliary steam energy, and due to direct compressed liquid material steam, equipment failure rate is high.It is mentioned above
The traditional evaporation equipment for arriving is that mostly main equipment, the treating capacity of equipment and investment, all than larger, are not suitable for medium-sized and small enterprises,
The scope of application is restricted.
The content of the invention
The problem to be solved in the present invention is to provide a kind of energy-saving evaporation regenerating unit of miniaturization.This evaporation regeneration dress
Put, not only equipment volume is little, small investment, energy consumption are low and applied widely.
The invention solves the problems that the problems referred to above by technical scheme below realize：
The energy-saving evaporation regenerating unit of miniaturization of the present invention includes stock solution case, concentration liquid case and distillating still, is characterized in also wrapping
Include source pump, First Heat Exchanger, the second heat exchanger, cooling blower and vapour-liquid cooler bin.
The distillating still contains main distillating still and secondary distillating still, has the first heating chamber, the first stock solution to enter in the middle part of main distillating still
Mouthful, there is the first steam to go out at the top of main distillating still, the first stoste outflow is by the second heat exchanger and pipeline, valve, filter and original
Liquid case is connected.
There are cooling medium inlet, cooling medium outlet, the first vapour-liquid import, the second vapour-liquid import, vapour on vapour-liquid cooler bin
Liquid outlet, condensate outlet.
There is inlet and outlet in source pump, in the first heating chamber, have the first heating chamber inlet, the first heating chamber outlet, heat
Pump assembly is exported and is connected with the first heating chamber inlet, and source pump entrance is connected with cooling medium outlet, and cooling medium enters
Mouth is connected with the first heating chamber outlet by cooling blower.
There are the second heating chamber, the second stoste outflow in the middle part of the secondary distillating still, at the top of secondary distillating still, have the second steam (vapor) outlet,
There are the second heating chamber inlet, the second heating chamber outlet, the second heating chamber inlet and first steam (vapor) outlet in second heating chamber
It is connected, the second heating chamber outlet is connected with the second vapour-liquid import by the second heat exchanger, the second vacuum pump, the second vacuum pump
It is connected with vapour-liquid outlet, the second steam (vapor) outlet passes through First Heat Exchanger, the first vacuum pump and the first vapour-liquid import phase
Even, the second stoste outflow is connected with stock solution case by First Heat Exchanger and pipeline, valve, filter.
Wherein, the intracavity bottom of main distillating still and secondary distillating still is connected with the concentration liquid case by valve and pipeline.
Further improvement of the present invention scheme is that the First Heat Exchanger is formed in parallel by two elements exchange devices.
Second heat exchanger is formed in parallel by two elements exchange devices.
Further improvement of the present invention scheme is that have air valve at the top of main distillating still.
Further improvement of the present invention scheme is that have air valve at the top of secondary distillating still.
Further improvement of the present invention scheme be have on stock solution upper box part both sides box wall respectively oil slick outlet and valve and
Medicament adds mouth and valve.
Further improvement of the present invention scheme is that have the 3rd stoste outflow and valve on the side wall in stock solution bottom portion.
Further improvement of the present invention scheme is that have precipitate outlet and valve in the bottom of stock solution case.
The further improvement project of the present invention is that concentrated solution bottom portion has floss hole and valve.
As can be seen from the above scheme, the evaporation thermal source comes from source pump and indirect steam, using heat pump techniques
It is the evaporation after high product heat for material to absorb low product thermal transition, compared with traditional multiple-effect evaporation thermal source, it is possible to decrease energy expenditure.
Source pump of the present invention using external compression type, steam preheating when need not start shooting are pressed again with traditional mechanical steam
Contracting carrys out direct compressed material steam phase ratio, reduces operation difficulty.Meanwhile, the circulatory mediator in compression heat pump system is reduced
The fault rate of equipment.Using indirect heat exchange method, the complete equipment flames of anger, it is particularly suited for the inflammable and explosive solvent of low boiling again
Raw, concentration.
Preheating, evaporation and condensation of the present invention to material to be processed, make full use of the latent heat of material itself and the energy of system
Amount input, it is compared with traditional evaporation technique, more energy-saving.The present invention adopts high efficient heat exchanging technology, is inhaled using heat pump techniques
It is the evaporation after high product heat for material to receive low product thermal transition, provides evaporation thermal source for vapo(u)rization system, while the heat pump after lowering the temperature
Circulatory mediator is used for the condensation of clean steam after material evaporation, improves the utilization rate of energy by way of this heat exchange.Utilize
Material after evaporation carries out heat exchange with stock solution, fully reclaims the energy of material after evaporation.
The present invention reaches the evaporation equipment treating capacity that tradition 30 is imitated through the vapo(u)rization system of 2-5 effects, using high efficient heat exchanging skill
Art, improves evaporation efficiency, reduces energy consumption.Vapo(u)rization system is integrated by the present invention, reduces occupation area of equipment, because
This, it is adaptable to the field such as water process and solvent recovery of medium-sized and small enterprises, it is not only energy-saving, can also accomplish environmental emission reduction, drop
The operating cost of low enterprise.
Description of the drawings
Fig. 1 is the energy-saving evaporation regenerating unit structural representation of miniaturization of the present invention.
Specific embodiment
As shown in figure 1, the energy-saving evaporation regenerating unit of the miniaturization of the present invention contains stock solution case 21, concentration liquid case 24, steams
Evaporate kettle, source pump 11, First Heat Exchanger 10, the second heat exchanger 23, cooling blower 12 and vapour-liquid cooler bin 17.
The distillating still contains main distillating still 5 and secondary distillating still 8, be provided with the middle part of main distillating still 5 first heating chamber, first
Stoste outflow 26, is provided with the first steam (vapor) outlet 4 at the top of main distillating still 5, the first stoste outflow 26 by the second heat exchanger 23 and
Pipeline, valve, filter are connected with stock solution case 21.
It is processed on the vapour-liquid cooler bin 17 to have cooling medium inlet 14, cooling medium to export the 171, first vapour-liquid import
15th, the second vapour-liquid import 16, vapour-liquid outlet 172, condensate outlet 173.
Inlet and outlet is machined with source pump 11, is machined with the first heating chamber inlet 1, first and adds in the first heating chamber
Hot cell outlet 2, the outlet of source pump 11 are connected with the first heating chamber inlet 1, and the entrance of source pump 11 is situated between with the cooling
Matter outlet 171 is connected, and cooling medium inlet 14 is connected with the first heating chamber outlet 2 by cooling blower 12.Wherein, source pump
In medium by first heating chamber inlet 1 enter main distillating still 5 in, for main distillating still 5 evaporation heat.From the first heating
The medium that room outlet 2 is discharged is used for the condensation and cooling of vapour-liquid in vapour-liquid cooler bin 17.
The second heating chamber, the second stoste outflow 9 is provided with the middle part of the secondary distillating still 8, it is processed at the top of secondary distillating still 8 to have
Second steam (vapor) outlet 7, processing second in the second heating chamber heat chamber inlet 6, the second heating chamber outlet 25, the second heating chamber inlet
6 are connected with first steam (vapor) outlet 4, make the steam that main distillating still 5 is produced be used for the evaporation heating of secondary distillating still 8.
Second heating chamber outlet 25 passes through the second heat exchanger 23, the second vacuum pump 22 and second vapour-liquid import, 16 phase
Even, the second vacuum pump 22 is connected with vapour-liquid outlet 172, is provided power by the second vacuum pump 22, is made from the second heating chamber to go out
The steam that mouth 25 is discharged carry out, after heat exchange, entering back into vapour-liquid cold by the second heat exchanger 23 and the stock solution into main distillating still 5
But case 17 is condensed and is cooled down.Meanwhile, the second vacuum pump 22 makes to produce negative pressure in main distillating still 5.
Second steam (vapor) outlet 7 is connected with second vapour-liquid import 16 by First Heat Exchanger 10, the first vacuum pump 13, the
Two stoste outflows 9 are connected with stock solution case 21 by First Heat Exchanger 10 and pipeline, valve, filter.Carried by the first vacuum pump 13
For power, the steam discharged is made from the second steam (vapor) outlet 7 to carry out heat by First Heat Exchanger 10 with the stock solution for entering secondary distillating still 8
After exchange, enter back into vapour-liquid cooler bin 17 and condensed and cooled down.Meanwhile, the first vacuum pump 13 makes to produce in secondary distillating still 8 and bears
Pressure.
Concentration liquid case 24 is connected with the intracavity bottom of main distillating still 5 and secondary distillating still 8 by valve and pipeline.
Wherein, the First Heat Exchanger 10 and the second heat exchanger 23 are formed in parallel by two elements exchange devices.
For convenience of the negative pressure state in control distillating still, sky is provided with brokenly at the top of main distillating still 5 and secondary distillating still 8
Valve 3.
For removing oil slick or other impurities in stock solution, oil slick outlet is machined with 21 top of stock solution case, one side box wall
19, valve is installed in the oil slick outlet.
For ease of adding medicament, medicament addition mouth 18, the medicament is machined with another side box wall on 21 top of stock solution case
Valve is installed on addition mouth.
For ease of to 21 internal-filling liquid of stock solution case, being machined with the 3rd stoste outflow 20 on the side wall of 21 bottom of stock solution case, should
Valve is installed in stoste outflow.
For ease of discharging the precipitate in stock solution case 21, precipitate outlet and valve is machined with the bottom of stock solution case 21
Door.
For ease of discharging concentrated solution, floss hole is machined with 24 bottom of concentration liquid case, valve is installed at floss hole.
When the energy-saving evaporation regenerating unit of miniaturization of the present invention runs, the stock solution in stock solution case 21 is all the way through second
The steam that second heating chamber outlet 25 is discharged in the middle part of heat exchanger 23 and secondary distillating still 8 carries out heat exchange, and the stock solution after intensification passes through
First stoste outflow 26 is evaporated in main distillating still 5.The origin of heat of the evaporation of main distillating still 5 is sent in source pump outlet
The medium for coming, the medium enter main distillating still 5 by the first heating chamber inlet 1, are discharged by the first heating chamber outlet 2, first
Heating interior is heated to stock solution, stock solution is evaporated under negative pressure state.The negative pressure is provided by the second vacuum pump 22.By
The steam that first steam (vapor) outlet 4 is discharged enters secondary distillating still 8 by the second heating chamber inlet 6, is stock solution evaporation in secondary distillating still 8
Thermal source is provided.
Second steam (vapor) outlet 7 of another road of stock solution in stock solution case 21 at the top of First Heat Exchanger 10 with secondary distillating still 8
The steam of discharge carries out heat exchange, and the stock solution after intensification is entered in secondary distillating still 8, and in negative pressure shape by the second stoste outflow 9
It is evaporated under state.Evaporation thermal source therein comes from the steam that first steam (vapor) outlet 4 of main distillating still 5 is discharged.Secondary distillating still 8
Interior negative pressure is provided by the first vacuum pump 13.
The steam that second steam (vapor) outlet 7 is discharged is provided by the first vacuum pump 13 after 10 preliminary cooling of First Heat Exchanger
Power is cooled down again in vapour-liquid cooler bin 17.Meanwhile, the steam that the first heating chamber outlet 25 is discharged is changed through second
After the 23 preliminary cooling of hot device, power is provided by the second vacuum pump 22 and cooled down into vapour-liquid cooler bin 17 again, after cooling
Clean or high-purity material is discharged by condensate outlet 173 in liquid form, is used in production.It is cold in vapour-liquid cooler bin 17
But medium sources are in the heat pump medium discharged by the first heating chamber outlet 2, this medium by pipeline, valve connection cooling blower 12 and
The cooling import 14 of vapour-liquid cooler bin 17 and coolant outlet 171.
By valve, pipeline, the concentrated solution of periodic exhaustion intracavity bottom is to concentrating liquid case for main distillating still 5 and secondary distillating still 8
In 24.
Claims (10)
1. the energy-saving evaporation regenerating unit of miniaturization, including stock solution case（21）, concentration liquid case（24）And distillating still, it is characterised in that
Also include source pump（11）, First Heat Exchanger（10）, the second heat exchanger（23）, cooling blower（12）With vapour-liquid cooler bin
（17）；
The distillating still contains main distillating still（5）With secondary distillating still（8）, main distillating still（5）There is the first heating chamber, first former at middle part
Liquid import（26）, main distillating still（5）First steam (vapor) outlet is arranged at top（4）, the first stoste outflow（26）By the second heat exchanger
（23）And pipeline, valve, filter and stock solution case（21）Connection；
Vapour-liquid cooler bin（17）On have cooling medium inlet（14）, cooling medium outlet（171）, the first vapour-liquid import（15）,
Two vapour-liquid imports（16）, vapour-liquid outlet（172）, condensate outlet（173）；
Source pump（11）On have inlet and outlet, have the first heating chamber inlet in the first heating chamber（1）, the first heating chamber outlet
（2）, source pump（11）Outlet and the first heating chamber inlet（1）Connection, source pump（11）Entrance is gone out with the cooling medium
Mouthful（171）It is connected, cooling medium inlet（14）By cooling blower（12）With the first heating chamber outlet（2）Connection；
The secondary distillating still（8）There are the second heating chamber, the second stoste outflow in middle part（9）, secondary distillating still（8）Second steam is arranged at top
Outlet（7）, in the second heating chamber, have the second heating chamber inlet（6）, the second heating chamber outlet（25）, the second heating chamber inlet（6）
With first steam (vapor) outlet（4）It is connected, the second heating chamber outlet（25）By the second heat exchanger（23）, the second vacuum pump（22）
With the second vapour-liquid import（16）It is connected, the second vacuum pump（22）Export with the vapour-liquid（172）Connection, the second steam (vapor) outlet
（7）By First Heat Exchanger（10）, the first vacuum pump（13）With the first vapour-liquid import（15）It is connected, the second stoste outflow
（9）By First Heat Exchanger（10）And pipeline, valve, filter and stock solution case（21）Connection.
2. the energy-saving evaporation regenerating unit of miniaturization according to claim 1, it is characterised in that main distillating still（5）With secondary steaming
Evaporate kettle（8）Intracavity bottom by valve and pipeline and the concentration liquid case（24）Connection.
3. the energy-saving evaporation regenerating unit of miniaturization according to claim 1, it is characterised in that the First Heat Exchanger
（10）It is formed in parallel by two elements exchange devices.
4. the energy-saving evaporation regenerating unit of miniaturization according to claim 1, it is characterised in that second heat exchanger
（23）It is formed in parallel by two elements exchange devices.
5. the energy-saving evaporation regenerating unit of miniaturization according to claim 1, it is characterised in that main distillating still（5）Top
There is air valve（3）.
6. the energy-saving evaporation regenerating unit of miniaturization according to claim 1, it is characterised in that secondary distillating still（8）Top
There is air valve（3）.
7. the energy-saving evaporation regenerating unit of miniaturization according to claim 1, it is characterised in that stock solution case（21）Top two
There is oil slick outlet on side box wall respectively（19）And valve and medicament addition mouth（18）And valve.
8. the energy-saving evaporation regenerating unit of miniaturization according to claim 1, it is characterised in that the side of 21 bottom of stock solution case
There is the 3rd stock solution to enter on wall（20）And valve.
9. the energy-saving evaporation regenerating unit of miniaturization according to claim 1, it is characterised in that stock solution case（21）Bottom
On have precipitate outlet and valve.
10. the energy-saving evaporation regenerating unit of miniaturization according to any one of claim 1 ~ 9, it is characterised in that concentrated solution
Case（24）Floss hole and valve are arranged at bottom.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611253324.1A CN106512450B (en) | 2016-12-30 | 2016-12-30 | Minimize energy-saving evaporation regenerating unit |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611253324.1A CN106512450B (en) | 2016-12-30 | 2016-12-30 | Minimize energy-saving evaporation regenerating unit |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106512450A true CN106512450A (en) | 2017-03-22 |
| CN106512450B CN106512450B (en) | 2019-03-12 |
Family
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108273282A (en) * | 2018-02-28 | 2018-07-13 | 重庆云天化天聚新材料有限公司 | Metaformaldehyde synthesizes destilling tower vapour phase low level heat recovery system and its recovery method |
| CN109107209A (en) * | 2018-10-25 | 2019-01-01 | 苏州市洁力美工业设备有限公司 | Distillation still heating device based on heat pump system |
| CN109939454A (en) * | 2019-04-29 | 2019-06-28 | 邢淑辉 | A heat pump vacuum concentration system |
| CN110270120A (en) * | 2019-07-13 | 2019-09-24 | 深圳市科伟达超声波设备有限公司 | A kind of industrial wastes recovery and processing system |
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