CN208545244U - Emulsifying liquid waste water processing system - Google Patents
Emulsifying liquid waste water processing system Download PDFInfo
- Publication number
- CN208545244U CN208545244U CN201820753691.6U CN201820753691U CN208545244U CN 208545244 U CN208545244 U CN 208545244U CN 201820753691 U CN201820753691 U CN 201820753691U CN 208545244 U CN208545244 U CN 208545244U
- Authority
- CN
- China
- Prior art keywords
- effect
- pipeline
- fractionator
- processing unit
- condensate
- 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.)
- Expired - Fee Related
Links
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model, which relates to, discloses a kind of emulsifying liquid waste water processing system, including head tank and with the tank connected evaporation concentration equipment group of the raw material, evaporation concentration equipment group include sequentially connected primary treatment portion, two effect processing units and one effect processing unit；The material of head tank is pumped into the material inlet in primary treatment portion by inlet pipe；The liquid product of one effect processing unit is pumped into the material inlet in primary treatment portion by reflux cycle pipeline, and reflux cycle pipeline is equipped with concentrate discharge line；Primary treatment portion and an effect processing unit are connected separately with steam and are passed through pipeline and condensate discharge line, and inlet pipe is equipped with condensate preheater, and all condensate discharge lines converge to the condensate preheater.Its remarkable result is that emulsifying liquid waste water makes full use of the heat for evaporation by three-effect evaporation and condensation, and while concentration and recovery waste oil, the thermal efficiency is high, and processing cost is low, reduces receipts water content in oil, improves oil quality, more conducively energy-saving and emission-reduction.
Description
Technical field
The utility model relates to field of waste water treatment, and in particular to a kind of processing system of oily waste water.
Background technique
Oil exploitation, refining, petrochemical industry, storage and shipping of oil products, steamer shipping, vehicle cleaning, machine-building, food processing etc.
In the production process of industry, a large amount of oily waste waters can be generated, oil mixing with water forms emulsifying liquid waste water.Currently, useless to emulsion
The processing method of water has: gas floatation process, absorption method, biochemical method, chemical method etc..
As energy-saving and environment-friendly attention degree increasingly improves in country in recent years, more and more manufacturers are to emulsifying liquid waste water
In waste oil carry out recycling and reusing, to realize bigger economic benefit.Before waste oil reprocessing, need to carry out emulsifying liquid waste water
It being concentrated, in existing distillation and concentration technology, device layout setting is not reasonable, and thermal losses is larger, and not only processing cost is higher,
It is high to recycle water content in oil, and quality is low, is also unfavorable for energy-saving and emission-reduction.
Utility model content
In view of this, in order to solve the above technical problems, the utility model provides a kind of emulsifying liquid waste water processing system, tool
The standby thermal efficiency is high, and the low advantage of processing cost can reduce water content in oil, improves oil quality.
Technical solution is as follows:
A kind of emulsifying liquid waste water processing system, including head tank and with the tank connected evaporation concentration equipment group of the raw material,
Key is: the evaporation concentration equipment group include by the sequentially connected primary treatment portion of liquid phase pipeline, two effect processing units and
One effect processing unit；
The material of the head tank is pumped into the material inlet in the primary treatment portion by inlet pipe；
The liquid product of the one effect processing unit is pumped into the material inlet in the primary treatment portion by reflux cycle pipeline,
The reflux cycle pipeline is equipped with concentrate discharge line；
The primary treatment portion and an effect processing unit are respectively arranged with steam and are passed through pipeline and condensate discharge line, described
Inlet pipe is equipped with condensate preheater, and all condensate discharge lines converge to the medium inlet of the condensate preheater, with
Material is preheated.
Using above technical scheme, material recycles concentration between primary treatment portion, two effect processing units and an effect processing unit,
Until concentration improve after excluded again by concentrate discharge line, emulsifying liquid waste water pass through three-effect evaporation and condensation, thermal losses compared with
It is small；After steam access steam is passed through pipeline, to primary treatment portion and an effect processing unit heating, steam is cooled to the solidifying of lower temperature
Low temperature lime set is accessed condensate preheater, preheats to material, further increase heat utilization ratio by liquid.
As preferred:
The two effects processing unit is provided with an effect gas phase and is passed through pipeline and an effect gas phase discharge line, the two effects processing unit
The gas-phase product that pipeline obtains the effect processing unit output is passed through through the effect gas phase.
The inlet pipe in condensate preheater downstream also extends through the effect processing unit, and the inlet pipe is successively
Heat exchange is carried out with the condensate preheater and an effect processing unit.
Using the above design, the gas-phase product temperature of an effect processing unit is higher, is accessed an effect gas phase and is passed through pipeline, made
For the heating source of two effect processing units, heat utilization ratio is further increased, heat waste is avoided.
Material in inlet pipe heats after the preheating of condensate preheater, then through an effect processing unit, to make full use of
Existing heat source.
As preferred:
The primary treatment portion, which is provided with, just steams heater and just steaming fractionator；
The medium inlet for wherein just steaming heater connects the steam and is passed through pipeline, and media outlet connects the condensate discharge
Pipeline；
The material inlet for just steaming heater is communicated with the inlet pipe and reflux cycle pipeline, and material outlet passes through
Liquid phase pipeline access is described just to steam fractionator, and the liquid product for just steaming fractionator is pumped at two effect by liquid phase pipeline
Reason portion.
The two effects processing unit includes two effect heaters and two effect separators；
Wherein the medium inlet connection of the two effect heaters one effect gas phase is passed through pipeline, media outlet connection one effect
Gas phase discharge line；
The material inlet of the two effects heater obtains the liquid product for just steaming fractionator and pumping out, and material outlet passes through
The liquid phase pipeline access two effects separator, the liquid product of the two effects separator are pumped into described one by the liquid phase pipeline
Imitate processing unit.
The one effect processing unit includes an effect heater and an effect fractionator；
Wherein the medium inlet of an effect heater connects the steam and is passed through pipeline, and medium, which goes out, connects the condensate discharge pipe
Road；
The material inlet of the one effect heater receives the liquid product that the two effects separator pumps out, material outlet connection
To the effect fractionator；
The liquid product of the one effect fractionator is pumped into the reflux cycle pipeline, the gas-phase product of the effect fractionator
It accesses the effect gas phase and is passed through pipeline；
The inlet pipe passes through the effect fractionator, to heat again to the material in inlet pipe.
Using the above design: just steam heater, two effect heaters, an effect heater and be respectively used to heat, just steam fractionator,
Two effect separators, an effect fractionator respectively fractionate out liquid product and gas-phase product.
As a preferred solution:
The just steaming fractionator and two effect separators are connected separately with gas phase condenser, and the gas phase condenser obtains respectively
The gas-phase product for just steaming fractionator and two effect separators, gas-phase product are separated respectively after condenser condenses to condensing gas
Pipe and condensate line；
Be connected with reflux concentration branch pipe with the corresponding condensate line of fractionator that just steams, the reflux be concentrated branch pipe with it is corresponding
It is described just steam fractionator refluxing opening connection.
The advantages of above design is that lower (100 DEG C of the normal pressure or so) oil of boiling point is just steaming fractionator gasification, passes through reflux
Continuous reflux, purification, the concentration of branch pipe is concentrated, is then exhausted from.
Scheme as a further preference:
After the inlet pipe is pierced by the effect processing unit, converge to the reflux cycle pipeline, the reflux cycle pipe
Road is equipped with the confluence positioned at the split point of upstream and positioned at downstream；
Wherein confluence and the inlet pipe are connected, and split point and concentrate discharge line are connected.
Using the program, starting material and recycle stock mixing from inlet pipe keep ingredient, temperature uniform, stablize
Process operating condition；Starting material from inlet pipe cannot directly be discharged from concentrate discharge line.
As a further preferred solution:
The head tank is also connected with surge tank and filter in turn by pipeline, wherein the material outlet of filter and institute
State inlet pipe connection.
It further include oil-water separator, distilled water collecting pit and exhaust gas processing device；
Wherein oil-water separator obtains the concentrate of the concentrate discharge line discharge simultaneously, and divides with described just steam
Evaporate the concentrate of the corresponding condensate line discharge of device；
The distilled water collecting pit is collected simultaneously the distilled water being discharged by the condensate preheater media outlet, an effect
The distilled water of gas phase discharge line discharge, and the distilled water of the condensate line discharge corresponding with the two effect separator；
The air intake of the exhaust gas processing device and the condensation tracheae are connected, to handle condensing gas；
The one effect fractionator and just to steam fractionator be atmospheric fractionator, the two effects separator is negative pressure fractionating device.
The utility model has the advantages that the remarkable result using the utility model is, emulsifying liquid waste water passes through three-effect evaporation and condensation, heat
It is lost smaller；And the heat for evaporation is made full use of, while concentration and recovery waste oil, there is thermal efficiency height,
The low advantage of processing cost reduces water content in oil, improves oil quality, more conducively energy-saving and emission-reduction.
Detailed description of the invention
Fig. 1 is the corresponding main flow schematic diagram of the utility model；
Fig. 2 is the connection relationship diagram of the utility model capital equipment；
Fig. 3 is the detailed PID figure of the utility model.
Specific embodiment
Below with reference to embodiment and attached drawing, the utility model is described in further detail.
As shown in Figure 1, a kind of emulsifying liquid waste water processing system, including head tank y, surge tank g, filter h, evaporation and concentration
Equipment group, oil-water separator j, wherein the head tank y, surge tank g, filter h are in turn switched on by pipeline, the filter
The outlet of h is connect by inlet pipe y10 with the evaporation concentration equipment group, and the liquid phase of the evaporation concentration equipment group is output to
The oil-water separator j；
Specifically, in conjunction with Fig. 2, Fig. 3 it can be seen that
The evaporation concentration equipment group include by the sequentially connected primary treatment portion a of liquid phase pipeline, two effect processing unit b and
One effect processing unit c；Wherein, primary treatment portion a includes just steaming heater a20 and just steaming fractionator a21, the two effects processing unit b
It include an effect heater c20 and an effect fractionator including two effect heater b20 and two effect separator b21, the effect processing unit c
C21 is illustrated respectively below in conjunction with material-liquid phase, material-gas phase, heat exchange etc..
1., material-liquid phase part flow direction:
The inlet pipe y10 is connected to the material inlet for just steaming heater a20, described just to steam heater a20's
Material outlet is passed through the just steaming fractionator a21 by liquid phase pipeline, and the liquid product for just steaming fractionator a21 passes through liquid phase
Pipeline is pumped into the material inlet of the two effects heater b20, and the material outlet of two effect heater b20 passes to institute by liquid phase pipeline
The liquid product for stating two effect separator b21, the two effects separator b21 is pumped into the effect heater c20 by liquid phase pipeline
Material inlet, one effect heater c20 material outlet by liquid phase pipeline pass to it is described one effect fractionator c21, it is described one imitate
The liquid product of fractionator c21 is pumped into the material inlet for just steaming heater a20 by reflux cycle pipeline c10, described
Reflux cycle pipeline c10 is equipped with concentrate discharge line c11, and the reflux cycle pipeline liquid phase c10 liquid phase, which is equipped with, to be located at
The split point of upstream and confluence positioned at downstream；Wherein confluence and the inlet pipe liquid phase y10 liquid phase are connected, point
Flow point and concentrate discharge line liquid phase c11 liquid phase are connected；So that initial material and the material of reflux cycle are total after mixing
With the material inlet for just steaming heater a20 is pumped into, avoid operating condition variation excessive；
Material-liquid phase part is just steaming heater a20, is just steaming fractionator a21, two effect heater b20, two effect separators
It is circulated between b21, an effect heater c20, an effect fractionator c21, reflux cycle pipeline c10, first steaming heater a20, with not
The disconnected moisture steamed in emulsifying liquid waste water, thus enriched oil phase, after oily phase concentration reaches requirement, from concentrate discharge line
C11 is discharged and is linked into the oil-water separator j, is further separated by oil-water separator j.
2., material-gas phase portion flow direction:
Gas-phase product can be generated respectively when just steaming fractionator a21, two effect separator b21 and an effect fractionator c21 distillation:
The effect of the fractionator a21 and two separator b21 that just steams is connected separately with gas phase condenser f, the object of the condenser f
Material entrance receives the gas-phase product for just steaming the effect of fractionator a21 and two separator b21 respectively, and gas-phase product is cold through condenser f
After solidifying, respectively separation to condensation tracheae f10 and condensate line f11；
Condenser f corresponding with the just steaming fractionator a21 is the first condenser, the condensate line of first condenser
F11 be the first condensate line, the first condensate line be connected with reflux concentration branch pipe f12, the reflux be concentrated branch pipe f12 with it is corresponding
Described just to steam fractionator a21 connection, first condensate line is also coupled to the oil-water separator j, with the two effects separator
The corresponding condenser f of b21 is the second condenser, and the condensate line f11 of second condenser is the second condensate line, this is second cold
Condensate pipe drains into distilled water collecting pit k；
And the gas-phase product temperature of the effect fractionator c21 is higher, can be used as the heat source of the two effects heater b20,
The medium inlet of the two effects heater b20 is connected with an effect gas phase and is passed through pipeline b10, and media outlet is connected with an effect gas phase
Discharge line b11, the gas-phase product of the effect fractionator c21 are passed through the effect gas phase and are passed through pipeline b10, add as two effects
The heat source of hot device b20, finally by the effect gas phase discharge line after the gas-phase product cooling liquid of an effect fractionator c21
B11 discharge.
3., heat exchange (heating):
Just steam heater a20 and one effect heater c20 heating source select high-temperature steam, it is described just steam heater a20 and
The medium inlet of the one effect heater c20 is connected separately with steam and is passed through pipeline d10, the heater a20 and described of just steaming
The media outlet of one effect heater c20 is connected separately with condensate discharge line d11；
High-temperature steam accesses the steam and is passed through pipeline d10 and is discharged from condensate discharge line d11, due to being discharged from condensate
The condensate temperature of pipeline d11 discharge is higher, to further increase heat utilization ratio, is additionally provided on the inlet pipe y10 solidifying
The condensate being discharged from condensate discharge line d11 is used as the heating source of condensate preheater e, the condensate preheater by water preheater e
The medium inlet of e is connected to all condensate discharge line d11, and all condensate discharge line d11 converge to the condensate
Preheater e, to preheat to material, the media outlet of the condensate preheater e is connected with distillation water discharge pipe e10, passes through
Condensate temperature is further decreased as distilled water after condensate preheater e, and is discharged from the distillation water discharge pipe e10；
The heating source of two effect heater b20 is as described in " material-gas phase portion flow direction ", using the gas of an effect fractionator c21
Phase product；
Further to utilize existing heat source, the inlet pipe y10 in the downstream condensate preheater e passes through an effect
The gas-phase product output par, c of fractionator c21, to be heated again to the material in inlet pipe y10；Inlet pipe y10 protrudes into institute
It is pierced by again after stating an effect fractionator c21, in effect the protruding into of fractionator c21, is pierced by position and needs to carry out sealing, specifically can be
The outer wall of inlet pipe y10 and the wall of an effect fractionator c21 are welded and fixed.
4., heat exchange (cooling):
Condenser f is used to cool down to the gas-phase product for just steaming the effect of fractionator a21 and two separator b21, condenses
The medium inlet of device f and media outlet water receiving pipe, using cold water as its heat exchange medium.
5., the processing of product:
In order to which the concentrate, condensate liquid, condensing gas, the distilled water that generate to above procedure continue with, in addition to grease
Seperator j is additionally provided with distilled water collecting pit k and exhaust gas processing device m；
Wherein oil-water separator j obtains the concentrate and described first of the concentrate discharge line c11 discharge simultaneously
The concentrate of condensate line f11 discharge；
Distilled water collecting pit k is collected simultaneously the distilled water being discharged by the condensate preheater e media outlet, the effect gas
The distilled water of phase discharge line b11 discharge, the distilled water of the second condensate line discharge, and by the condenser f medium
Export the cold water of discharge；
The air intake of exhaust gas processing device m and all condensation tracheae f10 are connected, to handle condensing gas, tail
Flash Gas Compression Skid System m be activated carbon adsorber or other；
6., Flow of Goods and Materials power:
On the liquid phase pipeline between the filter h and condensate preheater e, the effect heating of fractionator a21 and two is just steamed
On the liquid phase pipeline between device b20, on the liquid phase pipeline between two effect separator b21 and an effect heater c20, with
And on an effect fractionator c21 and the first liquid phase pipeline steamed between heater a20, it is separately installed with pump.
7., other:
High-temperature steam is directly selected to heat due to just steaming the effect of heater a20 and one heater c20, thus the effect fractionation
The device c21 and first fractionator a21 that steams is atmospheric fractionator, and two effect heater b20 select the gas-phase product of an effect fractionator c21
Heating, temperature is lower, thus the two effects separator b21 is negative pressure fractionating device.
The surge tank g is also connected with flushing pipe, for cleaning whole system.
First steaming heater a20 in the present embodiment, two effect heater b20, an effect heater c20, condensate preheater e and cold
Condenser f is as a kind of heat-exchanger rig, heat transferring medium and not contacted between heat transferring medium, and heat transferring medium enters and leaves with medium
Mouthful, material entrance is had by heat transferring medium；Just steaming fractionator a21, two effect separator b21 and an effect fractionator c21 has object
Expect entrance, liquid-phase outlet, gaseous phase outlet.Those skilled in the art are to the above content is well known, it may be to know that how to connect, thus
Area's specific structure and installation connection relationship are repeated no more herein.
Finally, it should be noted that foregoing description is only the preferred embodiment of the utility model, the common skill of this field
Art personnel are under the enlightenment of the utility model, under the premise of without prejudice to the utility model aims and claim, can make
Multiple similar expressions, such transformation are each fallen within the protection scope of the utility model.
Claims (10)
1. a kind of emulsifying liquid waste water processing system, including head tank (y) and the evaporation concentration equipment being connect with the head tank (y)
Group, it is characterised in that: the evaporation concentration equipment group includes by the sequentially connected primary treatment portion (a) of liquid phase pipeline, two effects
Processing unit (b) He Yixiao processing unit (c)；
The material of the head tank (y) is pumped into the material inlet of the primary treatment portion (a) by inlet pipe (y10)；
The liquid product of one effect processing unit (c) is pumped into the object of the primary treatment portion (a) by reflux cycle pipeline (c10)
Expect import, the reflux cycle pipeline (c10) is equipped with concentrate discharge line (c11)；
Primary treatment portion (a) the He Yixiao processing unit (c) is respectively arranged with steam and is passed through pipeline (d10) and condensate discharge pipe
Road (d11), the inlet pipe (y10) are equipped with condensate preheater (e), and all condensate discharge lines (d11) are converged to institute
The medium inlet of condensate preheater (e) is stated, to preheat to material.
2. emulsifying liquid waste water processing system according to claim 1, it is characterised in that: two effects processing unit (b) setting
There is an effect gas phase to be passed through pipeline (b10) He Yixiao gas phase discharge line (b11), two effect processing unit (b) is through the effect gas
Mutually it is passed through the gas-phase product that pipeline (b10) obtains effect processing unit (c) output.
3. emulsifying liquid waste water processing system according to claim 2, it is characterised in that: condensate preheater (e) downstream
The inlet pipe (y10) also extend through effect processing unit (c), the inlet pipe (y10) is successively pre- with the condensate
Hot device (e) He Yixiao processing unit (c) carries out heat exchange.
4. emulsifying liquid waste water processing system according to claim 2, it is characterised in that: primary treatment portion (a) setting
Have and just steams heater (a20) and just steam fractionator (a21)；
The medium inlet for wherein just steaming heater (a20) connects the steam and is passed through pipeline (d10), and media outlet connection is described solidifying
Water discharge pipe road (d11)；
The material inlet for just steaming heater (a20) is communicated with the inlet pipe (y10) and reflux cycle pipeline (c10),
Material outlet accesses just steaming fractionator (a21) by liquid phase pipeline, and the liquid product for just steaming fractionator (a21) passes through
Liquid phase pipeline is pumped into two effect processing unit (b).
5. emulsifying liquid waste water processing system according to claim 4, it is characterised in that: described two, which imitate processing unit (b), includes
Two effects heater (b20) He Erxiao separator (b21)；
Wherein the medium inlet connection of two effects heater (b20) the one effect gas phase is passed through pipeline (b10), and media outlet connects institute
State an effect gas phase discharge line (b11)；
The material inlet of two effect heater (b20) obtains the liquid product for just steaming fractionator (a21) and pumping out, and material goes out
Mouth accesses two effect separator (b21) by liquid phase pipeline, and the liquid products of two effect separator (b21) pass through the liquid
Phase pipeline is pumped into effect processing unit (c).
6. emulsifying liquid waste water processing system according to claim 5, it is characterised in that: described one, which imitates processing unit (c), includes
One effect heater (c20) He Yixiao fractionator (c21)；
Wherein the medium inlet of effect heater (c20) connects the steam and is passed through pipeline (d10), and medium, which goes out, connects the condensate
Discharge line (d11)；
The material inlet of one effect heater (c20) receives the liquid product that two effect separator (b21) pumps out, and material goes out
Mouth is connected to effect fractionator (c21)；
The liquid product of one effect fractionator (c21) is pumped into the reflux cycle pipeline (c10), the effect fractionator
(c21) the gas-phase product access one effect gas phase is passed through pipeline (b10)；
The inlet pipe (y10) passes through effect fractionator (c21), to add again to the material in inlet pipe (y10)
Heat.
7. emulsifying liquid waste water processing system according to claim 6, it is characterised in that: it is described just steam fractionator (a21) and
Two effects separator (b21) are connected separately with gas phase condenser (f), and the gas phase condenser (f) obtains described just steam respectively and is fractionated
The gas-phase product of device (a21) He Erxiao separator (b21), gas-phase product are separated respectively after condenser (f) condensation to condensing gas
Manage (f10) and condensate line (f11)；
Condensate line (f11) corresponding with just steaming fractionator (a21) is connected with reflux concentration branch pipe (f12), and the reflux is dense
Contracting branch pipe (f12) is connected to the corresponding refluxing opening for just steaming fractionator (a21).
8. according to emulsifying liquid waste water processing system described in claim 4,5,6 or 7, it is characterised in that: the inlet pipe
(y10) it after being pierced by effect processing unit (c), converges to the reflux cycle pipeline (c10), the reflux cycle pipeline (c10)
It is equipped with the confluence positioned at the split point of upstream and positioned at downstream；
Wherein confluence and the inlet pipe (y10) are connected, and split point and concentrate discharge line (c11) are connected.
9. according to claim 1, emulsifying liquid waste water processing system described in 2,4,5,6 or 7, it is characterised in that: the head tank
(y) surge tank (g) and filter (h) are also connected in turn by pipeline, wherein the material outlet of filter (h) and the feed liquor
Pipeline (y10) is connected.
10. emulsifying liquid waste water processing system according to claim 7, it is characterised in that: further include oil-water separator (j),
Distilled water collecting pit (k) and exhaust gas processing device (m)；
Wherein oil-water separator (j) obtains the concentrate of the concentrate discharge line (c11) discharge simultaneously, and with it is described just
Steam the concentrate of fractionator (a21) corresponding condensate line (f11) discharge；
The distilled water collecting pit (k) be collected simultaneously by condensate preheater (e) media outlet be discharged distilled water, described one
Imitate the distilled water of gas phase discharge line (b11) discharge, and the condensate line corresponding with two effect separator (b21)
(f11) distilled water being discharged；
The air intake of the exhaust gas processing device (m) and the condensation tracheae (f10) are connected, to handle condensing gas；
One effect fractionator (c21) and just steaming fractionator (a21) are atmospheric fractionator, and two effect separator (b21) is
Negative pressure fractionator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820753691.6U CN208545244U (en) | 2018-05-18 | 2018-05-18 | Emulsifying liquid waste water processing system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820753691.6U CN208545244U (en) | 2018-05-18 | 2018-05-18 | Emulsifying liquid waste water processing system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN208545244U true CN208545244U (en) | 2019-02-26 |
Family
ID=65421492
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201820753691.6U Expired - Fee Related CN208545244U (en) | 2018-05-18 | 2018-05-18 | Emulsifying liquid waste water processing system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN208545244U (en) |
-
2018
- 2018-05-18 CN CN201820753691.6U patent/CN208545244U/en not_active Expired - Fee Related
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101580457B (en) | Device and process for preparing absolute ethyl alcohol by taking fermented liquor as the raw material | |
| CN100453137C (en) | Alcohol quinque-towel differential pressure distilling arrangement and technique thereof | |
| CN105423266B (en) | A kind of high/low temperature sewage remaining energy cascade utilization and recycling reclaiming system and its method | |
| CN109908616B (en) | Energy-saving distillation system for preparing ethanol from carbon monoxide and distillation method thereof | |
| CN201473512U (en) | Distilling system provided with preheating device | |
| CN104383704B (en) | A kind of step heating system to the preheating of gas fractionator inlet feed | |
| CN103611328B (en) | Process for extracting naphthalene by continuously rectifying heavy benzol | |
| CN102584524A (en) | Alcohol recovery tower | |
| CN108251144B (en) | Process and system for realizing final dehydration of tar by recycling waste heat of heat pump unit | |
| CN109276898B (en) | Integrated system for concentrating fruit juice and recovering essence | |
| CN206705724U (en) | A kind of environmental protection and energy saving waste water distilling apparatus | |
| CN108905257A (en) | A kind of waste-heat recovery device of product equipment for purifying | |
| CN108329193A (en) | One kind being used for coal-ethylene glycol industry ethylene glycol recovery process method and system | |
| CN208545244U (en) | Emulsifying liquid waste water processing system | |
| CN106924985A (en) | Condensing source heat pump drives multi-effect distilling technique | |
| CN204723786U (en) | Three six sections, tower differential distillation energy conserving systems | |
| CN104744195B (en) | After a kind of ether, carbon four purifies de-dimethyl ether tower energy saving technique | |
| CN206995904U (en) | Condensing source heat pump driving multiple-effect horizontal tube falling film destilling tower | |
| CN206081667U (en) | MVR distillation plant | |
| CN104606910A (en) | Heat pump rectifying device based on heat storage technology and starting method of heat pump rectifying device | |
| CN210021208U (en) | Distillation energy-saving system for preparing ethanol from carbon monoxide | |
| CN103342733A (en) | Extraction method for protein in juice | |
| CN210176751U (en) | Industrial naphthalene production system | |
| CN206881178U (en) | Condensing source heat pump driving multiple-effect distillation device | |
| CN208911479U (en) | A kind of waste-heat recovery device of product equipment for purifying |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20190226 |