CN208356129U - A kind of mocromembrane evaporator and the distillation system comprising mocromembrane evaporator - Google Patents
A kind of mocromembrane evaporator and the distillation system comprising mocromembrane evaporator Download PDFInfo
- Publication number
- CN208356129U CN208356129U CN201820657849.XU CN201820657849U CN208356129U CN 208356129 U CN208356129 U CN 208356129U CN 201820657849 U CN201820657849 U CN 201820657849U CN 208356129 U CN208356129 U CN 208356129U
- Authority
- CN
- China
- Prior art keywords
- mocromembrane
- evaporation
- evaporator
- shell
- evaporation plate
- 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.)
- Active
Links
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
A kind of distillation system the utility model relates to mocromembrane evaporator and comprising mocromembrane evaporator.Including the shell of mocromembrane evaporator, and material evaporation mouth is equipped at the top of shell, the bottom of shell is equipped with material outlet, material inlet and overflow port are equipped at the middle part of shell, multilayer hollow is equipped in the inside of mocromembrane evaporator and evaporates board group, and the evaporation board group is connected in series by multi-disc hollow evaporation plate A and evaporation plate B.When carrying out rectifying using the mocromembrane evaporator, tower bottoms is pumped into mocromembrane evaporator by material by the tower reactor metering pump of rectifying column, and liquid film is formed in evaporation plate, light component substance ascends into rectifying column along plate face, and heavy constituent substance passes back into tower reactor along plate face decline.The utility model relates to mocromembrane evaporator evaporation efficiency is high, disengaging time is short, energy consumption can be effectively reduced, and small in size, save installation space, the effective component purity is high of acquisition reduces the discharge of waste, reduces environmental pollution.
Description
Technical field
It is the utility model relates to a kind of evaporator of Chemical Manufacture, in particular to a kind of with the micro- of mocromembrane evaporation technique
Film evaporator.
Background technique
Liquid to be evaporated is set to form mocromembrane on the surface of heat-exchanger rig, then the method being evaporated is called mocromembrane evaporation.
For this method since it is with great gasifying surface product, calorie spread is fast and uniform, and without the influence of liquid association pressure, energy
Enough the advantages that preferably preventing material superheating phenomenon, it is widely used in the fields such as chemical industry, pharmacy, food, metallurgy.
Tower is very widely used in Chemical Manufacture, and main tower has reaction tower, rectifying column, destilling tower
Reboiler evaporation is relied primarily on Deng, traditional tower to work.In current distillation technique, most commonly used reboiler
For tubular heat exchanger, but the working efficiency of tubular heat exchanger is limited by the wall thickness and pipeline area of tubulation again, is exchanged heat
Efficiency is less desirable.
In order to improve heat exchange efficiency, we often through by the design of the effective heat exchange area of reboiler very greatly with accommodate compared with
More heat exchange pipelines increases heat exchange area, is required with reaching evaporation, as Chinese patent CN202128924U uses two kinds of diameters not
Same heat exchanger tube, the small pipeline of diameter cover in the big pipeline of diameter, form interlayer cavity between outer tube wall and the outer wall of inner tube,
Thermal medium is passed through in interlayer cavity and carries out heat exchange processing to material, although can improve heat exchange to a certain extent by this equipment
Efficiency, but substantially or by increasing heat exchange area reach heat exchange purpose.And it is carried out using tubular heat exchanger
When evaporating work, needs to consume a large amount of energy, cause biggish waste.Lead to component in material additionally, due to heating efficiency is low
Isolated speed is slow, and component separation is not thorough, so that the amount of waste of discharge be caused to increase.
Utility model content
First technical purpose of the utility model is to provide a kind of mocromembrane evaporator.
Second technical purpose of the utility model is to provide a kind of distillation system comprising the mocromembrane evaporator.
To overcome energy consumption height, reboiler size in existing distillation technology big, time-consuming, and product quality is influenced, thermal energy
Utilization rate is low, and amount of waste is more, the high disadvantage of operating cost.
First technical purpose of the utility model has the technical scheme that
A kind of mocromembrane evaporator including shell and is arranged in the intracorporal evaporation board group of the shell: setting at the top of the shell
Have a material evaporation mouth, the bottom of the shell is equipped with material outlet, the centre of the shell be equipped with material inlet, thermal medium into
Mouth, thermal medium outlet and overflow port；The evaporation board group is connected in series by multi-disc hollow evaporation plate A and evaporation plate B.
Material inlet is arranged at the middle part of shell in a kind of mocromembrane evaporator involved in the utility model, material inlet
Position is higher than the height of the intracorporal evaporation board group of shell, enters the rear plate face with evaporation plate in shell from material inlet convenient for material and connects
Touching forms liquid film in the plate face of evaporation plate when the intracorporal temperature of shell is 80-300 DEG C, and pressure is 30-100Pa.In addition exist
Overflow port is arranged in the intermediate of shell, can prevent tower reactor metering pump from adopting excessive into material, flood the evaporation board group of enclosure interior, from
And make that liquid film can not be formed in the plate face of evaporation plate, influence evaporation efficiency.
Preferably, the evaporation plate A(551), evaporation plate A(551 identical as the size of evaporation plate B(552)) and evaporation
Plate B(552) contain a cavity, evaporation plate A(551) with evaporation plate B(552) two sides be evagination cambered surface, evaporation plate A
(551) and evaporation plate B(552) positive and negative respectively have a circular hole, evaporation plate A(551) positive hole and evaporation plate B(552) back
The hole in face connects.
It connects to form evaporation board group for the evaporation plate A and evaporation plate B of cavity inside multi-disc, the hole on the front evaporation plate A exists
The underface in the hole on reverse side, the surface in hole of the hole on reverse side on the front evaporation plate B and is steamed at the positive hole evaporation plate A
The hole connection for sending out the back side plate B can be full of the cavity of entire evaporation plate, and steaming after guaranteeing that thermal medium enters evaporation board group
It is flowed in the form of baffling between hair board group, residence time of the thermal medium in evaporation board group can be increased, improve heat utilization rate,
Reduce energy consumption.
Preferably, the spacing between at the top of the overflow port nozzle base and evaporation board group is 10-20mm, to ensure overflow
Effect.
Doing so can prevent material from flooding evaporation plate, cannot form evaporating surface, influence evaporation efficiency.
Preferably, the gap of the housing bottom and evaporation board group bottom is 20-30mm.
Doing so can prevent material from walking short circuit, influence area and steaming that material forms liquid film in the plate face of evaporation board group
Send out effect.
Preferably, the size of the evaporation plate A and evaporation plate B is calculated according to evaporation capacity, be arranged corresponding outer diameter and
Length, according to the internal diameter of the outer diameter of evaporation plate A and evaporation plate B calculating shell, the outer diameter of evaporation plate A and evaporation plate B are in shell
0.5-0.9 times of diameter.
The occupied area of equipment size can be reduced, be easily installed while guaranteeing effective evaporating surface area by doing so.
Preferably, the thermal medium entrance is connect with evaporation board group by steam pipe, and thermal medium is in evaporation board group
It is flowed in the form of baffling inside；The thermal medium entrance and thermal medium outlet are distributed in the two sides of shell.
Time of the thermal medium in evaporation board group can be increased, and then the heat-exchange time of mocromembrane evaporator increases, and improves heat
Energy utilization rate, reduces energy consumption.
Preferably, the shell of the mocromembrane evaporator uses the design of round or ellipse.
Second technical purpose of the utility model has the technical scheme that
A kind of distillation system comprising the mocromembrane evaporator further includes that the tower reactor connecting with the mocromembrane evaporator is used tricks
Measure pump, material storage tank, filter, rectifying column, condenser and return tank；The material storage tank is connect with rectifying column, tower reactor meter
Amount pump is set at the tower reactor of rectifying column with the mocromembrane evaporator, connects condenser in the material outlet of the tower top of rectifying column,
Condenser is connect with return tank.
Component separation is carried out using the distillation system, since mocromembrane evaporator can reduce the residence time of material, in turn
The time that rectifying column carries out distillation process can be shortened, improve the working efficiency of rectifying column, compared with prior art, mocromembrane evaporation
The size of device is small, and evaporation efficiency is high, multiple can connect and rectifying column integrated installation, and occupied area is small.
In conclusion the utility model has the following beneficial effects:
1, because the volume and actual evaporation of mocromembrane evaporator have relationship, the outer of evaporation plate is designed by actual evaporation
Diameter size can also reduce the volume of evaporator while guaranteeing effective disengagement area, save installation space, convenient for flexible
Installation；
2, material walks short circuit in order to prevent, influences area and evaporation effect that material forms liquid film in the plate face of evaporation board group
Fruit, evaporating the spacing between the bottom of board group and the bottom of mocromembrane evaporator is 20-30mm；
3, in order to guarantee evaporation effect, and evaporation plate is prevented to be submerged, evaporating surface cannot be formed, in mocromembrane evaporator
Overflow port is set among shell, and the spacing between the bottom of overflow port and the top for evaporating board group is 10-20mm.
4, evaporation board group is composed in series as heat-exchanger rig using multi-disc hollow evaporation plate A and evaporation plate B, heat can be made
Residence time of the matchmaker in evaporation plate is longer, and heat utilization rate is high, and the plate face surface area of evaporation plate is larger, can expand liquid
Film forming area of the film in evaporator, and then enhance evaporation efficiency.
5, accurate control is fed using metering pump, forms subtle evaporating film in the evaporation plate face of mocromembrane evaporator, no
It is fast with boiling point component separating rate, so that evaporation efficiency is high, be conducive to improve production efficiency.
6, the mocromembrane evaporator evaporation efficiency of the utility model is high, and residence time of material is short, and the decomposition caused by material gathers
The few side effects such as conjunction, can effectively improve the processing capacity of tower.
7, installation space can be not only saved using the mocromembrane evaporator that the technical program designs, reduces energy consumption, reduced and steam
The time is sent out, and the utilization rate of heating agent can be improved, it is energy saving, the quality of product is improved, operating cost is reduced.It thus can be wide
It is general to be used for the fields such as chemical industry, petroleum, metallurgy, pharmacy.
Detailed description of the invention
Fig. 1 is the rectification process flow chart of the utility model；
Fig. 2 is the main view of the mocromembrane evaporator of the utility model；
Fig. 3 is the left view of the mocromembrane evaporator of the utility model；
Fig. 4 is the left view inside the mocromembrane evaporator shell of the utility model；
Fig. 5 is the evaporation board group sectional view of the mocromembrane evaporator of the utility model；
Fig. 6 is the evaporation plate schematic diagram of the mocromembrane evaporator of the utility model.
In figure, 1- material storage tank；2- filter；3- rectifying column；4- tower reactor metering pump；5- mocromembrane evaporator；6 rectifying columns
Overhead product storage tank；7- return tank；8 condensers；51- shell；52- material inlet；53- material evaporation mouth；54- material outlet；
55- evaporates board group；56- overflow port；57- thermal medium inlet；58- thermal medium outlet；551- evaporation plate A；552- evaporation plate B.
Specific embodiment
The utility model is described further with reference to the accompanying drawing:
The utility model includes shell 51, and the top of shell 51 is equipped with material evaporation mouth 54, and bottom is equipped with material outlet 53,
Middle part is equipped with material inlet 52, overflow port 56, thermal medium inlet 57 and thermal medium outlet 58, is arranged in the inside of shell 51 by more
The evaporation board group 55 that the hollow evaporation plate 551 of piece and evaporation plate 552 are composed in series.The outer diameter of evaporation plate A and evaporation plate B are in shell
0.5-0.9 times of diameter.
In rectifying involved in the utility model, form material in evaporation plate 551 and evaporation plate 552 thin
Then film is separated, cancel reboiler in the tower reactor of rectifying column 3, configures mocromembrane evaporator 5 and tower reactor metering pump 4.
Material enters 3 middle part of rectifying column, and the outside of rectifying column 3 is separately connected 8 return tank 7 of rectifying tower top condenser, overhead product storage tank
6, rectifying tower reactor metering pump 4, mocromembrane evaporator 5；Material passes through the object at 51 middle part of shell by tower reactor metering pump 4 from tower reactor
It is pumped into evaporator at material import 52, it is made to form mocromembrane in the plate face of evaporation board group 55, conduction oil is from thermal medium inlet 57
In the evaporation board group 55 formed in into the evaporation plate 551 and 552 hollow by multi-disc inside mocromembrane evaporator 5, and to attachment
Material mocromembrane in evaporation board group 55 is heated, and last conduction oil flows out from thermal medium outlet 58.In the process of evaporation
In, light component substance quickly rises along the plate face of evaporation board group 55, absorbs heat, gasification, the substance of heavy constituent is along evaporation
The plate face of board group 55 declines, and continues to absorb heat, finally pass back into tower reactor from material outlet 54.
Embodiment 1:
The utility model is used to evaporate purification vitamin E, uses petroleum ether extraction vitamin E product first, it then will packet
Petroleum ether containing vitamin E is passed through the middle part of rectifying column 3, and the outside of rectifying column 3 is separately connected the reflux of rectifying tower top condenser 8
Tank 7, overhead product storage tank 6, rectifying tower reactor metering pump 4, mocromembrane evaporator 5；The petroleum ether of vitamin E passes through in rectifying column 3
After crossing sufficient gas-liquid exchange, boiling point enters rectifying tower top return tank 7 after 30-80 DEG C of component enters condenser 8 by tower top,
Material a part in return tank 7 returns to rectifying column 3 and flows back, and a part extraction is used as overhead product, the boiling point in rectifying column 3
Component higher than 85 degree falls into the tower reactor of lower part, is pumped into mocromembrane evaporator 5 by tower reactor metering pump 4, controls the tower reactor being pumped into
Flow quantity is 2t/h, and tower bottoms forms liquid film, vacuum 30-60Pa, temperature in the plate face of the evaporation board group 55 of mocromembrane evaporator 5
Under conditions of 220-230 DEG C, boiling point is that 180-200 DEG C of component enters in rectifying column 3 from the top of mocromembrane evaporator 5, is boiled
The component that point is 200-220 DEG C is from the tower reactor that the bottom of mocromembrane evaporator 5 passes back into rectifying column 3, finally from the tower of rectifying column 3
Lurid vitamin E is produced in kettle, evaporation efficiency 98%-99%, wherein the equipment size of mocromembrane evaporator is compared with the prior art
Small 80%-85%.
Embodiment 2:
The utility model is used for the acetone exhausting section of acetylacetone,2,4-pentanedione preparation process, by after simple distillation acetone and acetic acid it is different
The middle part of rectifying column 3 is passed through after the gaseous mixture condensation of acrylic ester, the outside of rectifying column 3 is separately connected rectifying tower top condenser 8, returns
Flow tank 7, overhead product storage tank 6, rectifying tower reactor metering pump 4, mocromembrane evaporator 5；Acetone and acetic acid isopropyl alkene after simple distillation
For ester admixture in rectifying column 3 after the exchange of sufficient gas-liquid, boiling point enters condenser 8 by tower top in 50-58 DEG C of component
Enter rectifying tower top return tank 7 afterwards, material a part in return tank 7 returns to rectifying column 3 and flows back, and a part extraction is used as tower
Product is pushed up, the component of boiling point >=60 DEG C in rectifying column 3 falls into the tower reactor of lower part, is pumped into mocromembrane evaporation by tower reactor metering pump 4
In device 5, controlling the tower reactor flow quantity being pumped into is 2m3/ h, tower bottoms are formed in the plate face of the evaporation board group 55 of mocromembrane evaporator 5
Liquid film, vacuum 50-70Pa, under conditions of temperature is 95-110 DEG C, the components of boiling point≤90 DEG C from the top of mocromembrane evaporator 5 into
Enter in rectifying column 3, the component that boiling point is 92-95 DEG C is from the tower reactor that the bottom of mocromembrane evaporator 5 passes back into rectifying column 3, finally
Isopropenyl acetate is produced from the tower reactor of rectifying column 3, tower reactor product is passed through next workshop section, evaporation efficiency 98%-99%,
The wherein equipment size of mocromembrane evaporator 80%-90% small compared with the prior art.
Embodiment 3:
The utility model is used for the continuous rectification separation of propene carbonate crude product, operation temperature to be 90 DEG C, product purity
Enter the middle part of rectifying column 3 for 98% propene carbonate crude product, the outside of rectifying column 3 be separately connected rectifying tower top condenser 8,
Return tank 7, overhead product storage tank 6, rectifying tower reactor metering pump 4, mocromembrane evaporator 5；Propene carbonate crude product is in rectifying column 3
After the exchange of sufficient gas-liquid, boiling point enters condenser 8 by tower top in 80-100 DEG C of fraction, enters rectifying tower top afterwards and flows back
Tank 7, material a part in return tank 7 return to rectifying column 3 and flow back, and a part extraction is as overhead product, in rectifying column 3
The component of boiling point >=110 DEG C falls into the tower reactor of lower part, is pumped into mocromembrane evaporator 5 by tower reactor metering pump 4, controls the tower being pumped into
Kettle liquid flow is 1.5m3/ h, tower bottoms form liquid film, vacuum 40- in the plate face of the evaporation board group 55 of mocromembrane evaporator 5
70Pa, under conditions of temperature is 250-280 DEG C, the component of boiling point≤240 DEG C enters rectifying column 3 from the top of mocromembrane evaporator 5
In, the component that boiling point is 240-250 DEG C is from the tower reactor that the bottom of mocromembrane evaporator 5 passes back into rectifying column 3, finally from rectifying column
Propene carbonate is produced in 3 tower reactor, the purity of product is 99.6-99.9%, evaporation efficiency 98%-99%, and wherein mocromembrane evaporates
The equipment size of device 80%-90% small compared with the prior art.
Comparative example 1:
In a kind of the continuous rectification separation method and device of propene carbonate crude product, operation temperature is 90 DEG C, product purity
Enter the middle part of rectifying column for 98% propene carbonate crude product, rectifying column inner cavity is equipped with backflow distributor, multiple groups water chestnut from top to bottom
Shaped reaction promotion unit, feed distributor and multiple groups liquid stripping filtering table are separately connected on the outside of propene carbonate rectifying column
Rectifying tower top condenser and rectifying tower reactor reboiler；
In rectifying column after the exchange of sufficient gas-liquid, gas phase light component is produced propene carbonate crude product by rectifying tower top
Remove preceding reaction member；Heavy constituent falls into the tower reactor of lower part, after rectifying tower reactor recycles discharging pump, into rectifying tower reactor reboiler,
Conduction oil inlet oil temperature be 200-230 DEG C, oil outlet temperature be 180-200 DEG C, after reboiler heats, low-boiling point material again into
Entering in rectifying column, high boiling substance passes back into the tower reactor of rectifying column, and it is 98.7%~98.9% that product purity is produced from tower reactor,
And the control of tower reactor absolute pressure is in 1.9KPa, absolute pressure of top of the tower control is in 4.8KPa, and bottom temperature control is at 110 DEG C, tower top
Temperature is controlled at 110 DEG C.
Comparative example 2:
It is a kind of to be prepared in the method for natural VE with rectifying-molecular distillation coupled modes, by soybean oil deodorizer distillate
The material obtained after esterifying alcohol solution filters pressing sterol, is added in falling film evaporator, and the temperature of falling film evaporator is set as 180
~230 DEG C, under conditions of system pressure is 10~100Pa, material is continuously recycled by circulating pump and squeezes into falling film evaporator
In, material vaporizes in falling film evaporator；This vaporization liquid is through the isolated light component of rectifying column and heavy constituent.Wherein light component passes through
It is collected in corresponding storage tank after condenser condensation, heavy constituent returns in falling film evaporator, adjusts falling film evaporator heating temperature and is
200~250 DEG C, the top of the distillation column 10~100Pa of vacuum；It is concentrated to certain degree, rectifying terminates, and heavy constituent is transferred to accordingly
Storage tank in；Then by the resulting heavy constituent of above-mentioned steps, it is pumped up with the charging rate of 0.5~0.6kg/hr into molecular distillation
In device, under conditions of 210~220 DEG C, system pressure are 1~5Pa, knifing spinner velocity is 200~300rpm, molecule is carried out
Distillation obtains the product that light component 75.3% is natural VE, yield 85.1%.Heavy constituent 7 is plant asphalt.
It can be seen that the mocromembrane evaporator using the utility model from embodiment and comparative example and use the evaporation
The rectification process of device has evaporation efficiency high compared to existing technology, and energy loss is small, and evaporator size is small, tower reactor discharge
The features such as high-boiling components purity is higher, and tower reactor product quality can be improved or reduce waste discharge.
This specific embodiment is only the explanation to the utility model, is not limitations of the present invention, ability
Field technique personnel can according to need the modification that not creative contribution is made to the present embodiment after reading this specification, but
As long as all by the protection of Patent Law in the scope of the claims of the utility model.
Claims (8)
1. a kind of mocromembrane evaporator, it is characterised in that:
Including shell (51) and the evaporation board group (55) being arranged in the shell (51): the top of the shell (51) is equipped with object
Expect evaporation mouth (53), the bottom of the shell (51) is equipped with material outlet (54), the centre of the shell (51) be equipped with material into
Mouth (52), thermal medium inlet (57), thermal medium outlet (58) and overflow port (56)；The evaporation board group (55) is hollow by multi-disc
Evaporation plate A(551) and evaporation plate B(552) be connected in series.
2. mocromembrane evaporator according to claim 1, it is characterised in that: the evaporation plate A(551) and evaporation plate B(552)
Size it is identical, evaporation plate A(551) with evaporation plate B(552) contain a cavity, evaporation plate A(551) with evaporation plate B(552)
Two sides be evagination cambered surface, evaporation plate A(551) and evaporation plate B(552) positive and negative respectively have a circular hole, evaporation plate A
(551) positive hole is connect with the hole at the back side evaporation plate B(552).
3. mocromembrane evaporator according to claim 2, it is characterised in that: overflow port (56) nozzle base and evaporation plate
Spacing between at the top of group (55) is 10-20mm.
4. mocromembrane evaporator according to claim 3, it is characterised in that: shell (51) bottom and evaporation board group (55)
The gap of bottom is 20-30mm.
5. mocromembrane evaporator according to claim 4, it is characterised in that: the evaporation plate A(551) and evaporation plate B(552)
Outer diameter be 0.5-0.9 times of shell (51) internal diameter.
6. mocromembrane evaporator according to claim 5, it is characterised in that: the thermal medium inlet (57) and evaporation board group
(55) it is connected by steam pipe, and thermal medium is in the internal flowing in the form of baffling of evaporation board group (55)；The thermal medium into
Mouth (57) and thermal medium outlet (58) are distributed in the two sides of shell (51).
7. mocromembrane evaporator according to claim 6, it is characterised in that: the shell of the mocromembrane evaporator using round or
Ellipse.
8. a kind of distillation system includes the described in any item mocromembrane evaporators (5) of claim 1-7, it is characterised in that:
It further include tower reactor metering pump (4), material storage tank (1), the filter (2), rectifying being connect with the mocromembrane evaporator (5)
Tower (3), condenser (8) and return tank (7)；The material storage tank (1) connect with rectifying column (3), tower reactor metering pump (4) with
The mocromembrane evaporator (5) is set at the tower reactor of rectifying column (3), connects condensation in the material outlet of the tower top of rectifying column (3)
Device (8), condenser (8) are connect with return tank (7).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820657849.XU CN208356129U (en) | 2018-05-04 | 2018-05-04 | A kind of mocromembrane evaporator and the distillation system comprising mocromembrane evaporator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820657849.XU CN208356129U (en) | 2018-05-04 | 2018-05-04 | A kind of mocromembrane evaporator and the distillation system comprising mocromembrane evaporator |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN208356129U true CN208356129U (en) | 2019-01-11 |
Family
ID=64933710
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201820657849.XU Active CN208356129U (en) | 2018-05-04 | 2018-05-04 | A kind of mocromembrane evaporator and the distillation system comprising mocromembrane evaporator |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN208356129U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108371825A (en) * | 2018-05-04 | 2018-08-07 | 吉林北沙制药有限公司 | A kind of mocromembrane evaporator, the distillation system comprising mocromembrane evaporator and the rectificating method using mocromembrane evaporator |
| CN114671476A (en) * | 2022-05-06 | 2022-06-28 | 江苏盈天化学有限公司 | Device and method for continuously recovering high-purity acetonitrile from waste liquid |
-
2018
- 2018-05-04 CN CN201820657849.XU patent/CN208356129U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108371825A (en) * | 2018-05-04 | 2018-08-07 | 吉林北沙制药有限公司 | A kind of mocromembrane evaporator, the distillation system comprising mocromembrane evaporator and the rectificating method using mocromembrane evaporator |
| CN114671476A (en) * | 2022-05-06 | 2022-06-28 | 江苏盈天化学有限公司 | Device and method for continuously recovering high-purity acetonitrile from waste liquid |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101229449A (en) | Pleietrepie counter current falling film evaporator of organic solvent recycle | |
| CN208356129U (en) | A kind of mocromembrane evaporator and the distillation system comprising mocromembrane evaporator | |
| CN107812393A (en) | A kind of methanol three-effect rectification system and technique | |
| CN102875329B (en) | A kind of heat pump distillation is separated technique and the device of primary isoamyl alcohol isomers | |
| CN105964008B (en) | A kind of high-purity vinyl acetate piece-rate system | |
| CN204522347U (en) | A kind of solvent distillation recovery device | |
| CN108371825A (en) | A kind of mocromembrane evaporator, the distillation system comprising mocromembrane evaporator and the rectificating method using mocromembrane evaporator | |
| CN103252105B (en) | Methyl alcohol pressure reducing and distilling device | |
| CN110105216A (en) | A kind of method and device from backheat rectifying | |
| CN2778277Y (en) | Chinese medicinal liquor vacuum condensation equipment | |
| CN203861950U (en) | Rectification device including double reboilers | |
| CN109011676A (en) | A kind of achievable material is rapidly heated the rectifying column of vaporization | |
| CN215250668U (en) | Negative pressure debenzolization device | |
| CN205925025U (en) | Grease leaches course of working and uses first evaporimeter | |
| CN202315342U (en) | Horizontal pipe falling film evaporation tower | |
| CN202020929U (en) | Jet type solution evaporation concentration device | |
| CN212308898U (en) | Fractionating tower and fractionating system for heat conduction oil production | |
| CN203474692U (en) | Efficient and energy-saving preparation device of acetyl acetone | |
| CN212594079U (en) | Gas phase separation device for low-boiling-point impurities in titanium tetrachloride | |
| CN201093884Y (en) | Cross current type jet condenser capable of regulating and controlling | |
| CN210813975U (en) | Double ethyl methyl ester efficient energy-saving distillation device | |
| CN203507575U (en) | Rectifying tower | |
| CN210331709U (en) | Self-backheating rectification device | |
| CN201823331U (en) | Solar rectification and purification device dedicated for crude pyroligneous acid | |
| CN208482031U (en) | A kind of rectifying column Steam reboiler with anti-corrosion function |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |