CN108640392A - A kind of water-oil separating treatment process - Google Patents
A kind of water-oil separating treatment process Download PDFInfo
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- CN108640392A CN108640392A CN201810580959.5A CN201810580959A CN108640392A CN 108640392 A CN108640392 A CN 108640392A CN 201810580959 A CN201810580959 A CN 201810580959A CN 108640392 A CN108640392 A CN 108640392A
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- waste water
- stripper
- vacuum pump
- effect evaporator
- tower
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- 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
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- 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
- C02F1/10—Treatment of water, waste water, or sewage by heating by distillation or evaporation by direct contact with a particulate solid or with a fluid, as a heat transfer medium
-
- 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
- C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
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- Chemical & Material Sciences (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)
- Analytical Chemistry (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention discloses a kind of process for treating oil-containing waste water, vacuum pump is provided, stripper, overhead condenser, chromatograph device, triple effect evaporator, to strip tower pressure interior force using vacuum pump reduces, discharge contains high salinity, the pipeline of oily waste water will contain high salinity, the waste water of oil is sent into stripper top, the top of packing layer, waste water is evenly distributed on packing layer and drops to bottom from stripper top, after stripper bottom of tower heater temperature raising heating, oil and moisture are cooled down after tower top discharge through overhead condenser by thermal stripping in waste water, it is detached into chromatography device, stripper bottom enters triple effect evaporation processing unit containing alkali waste water with high salt and is handled.The present invention can in waste water oil and saline solution be effectively separated, make the organic matter and salt content qualified discharge of waste water.
Description
Technical field
The present invention relates to a kind of process for treating oil-containing waste water, more particularly to a kind for the treatment of process of high salinity oily waste water.
Background technology
Currently, being condensed the Wastewater Treatment Technology of generation under alkaline environment for small molecule aldehyde (propionic aldehyde, butyraldehyde etc.) both at home and abroad
Art mainly has Bubble-floating Method, air catalytic oxidation method etc..
Bubble-floating Method refers to being adhered on Pollutants in Wastewater as carrier using the micro-bubble of high degree of dispersion, makes its buoyancy
More than gravity and floating resistance, to make pollutant float up to the water surface, foam is formed, then scrapes de-bubble from the water surface with scraping slag equipment
Foam realizes that the process of solid-liquid or Liquid liquid Separation is known as Bubble-floating Method.The necessary condition of air supporting process is：In processed waste water,
A large amount of fine gas bubbles should be distributed, and processed pollutant is made to be in suspended state, and suspended particulate surface should be in hydrophobicity, be easy to
It is adhered on bubble and floats.Containing organic salt soluble easily in water is contained in high salinity, oily waste water, Bubble-floating Method is to dissolubility, subdivision
It is relatively low to dissipate type organic salt removal rate.
Air catalytic oxidation method refers to that catalytic air carries out oxidation reaction to the pollutant in waste water.However, air catalytic
Oxidizing process is relatively low to oil content removal rate in waste water.Existing treatment technology is relatively low to useless Organic substance in water, oily removal rate, can not
Meet processing requirement.
Invention content
In order to solve the deficiencies in the prior art, an object of the present invention is to provide a kind of process for treating oil-containing waste water, energy
Enough oil and saline solution in waste water is effectively separated, and makes the organic matter and salt content qualified discharge of waste water.
To achieve the goals above, the technical scheme is that：
A kind of process for treating oil-containing waste water provides vacuum pump, stripper, overhead condenser, chromatography device, triple effect evaporator,
It is reduced using vacuum pump by tower pressure interior force is stripped, discharging the pipeline containing high salinity, oily waste water will be containing high salinity, oily waste water
It is sent into the top of stripper top, packing layer, waste water is evenly distributed on packing layer and drops to bottom from stripper top, through stripping
After the heater temperature raising heating of tower bottom of tower, oil and moisture are cooled down after tower top discharge through overhead condenser by thermal stripping in waste water, into
Enter to chromatograph device and be detached, stripper bottom enters triple effect evaporation processing unit containing alkali waste water with high salt and handled.
Traditional stripper generally use normal pressure or pressurization are evaporated stripper, however which separative efficiency compared with
It is low, it is unfavorable for the separation of the oil and saline solution in waste water.The inventors found that reducing stripper by vacuum pump
Pressure can not only improve the output rate of gaseous phase materials, and the pressure for reducing stripper can increase the cocnentration factor of waste water, make
The oil and saline solution obtained in waste water is effectively separated.
The second object of the present invention is to provide a kind of device for realizing above-mentioned technique, including vacuum pump, stripper, triple effect steam
Device is sent out, the stripper top side wall opens up waste water inlet, and waste water inlet is located in stripper on packing layer, the stripping
Pipeline of the waste water inlet connection discharge of tower containing high salinity, oily waste water, the gaseous phase outlet of stripper top are equipped with vacuum lines,
The gaseous phase outlet of stripper top is connect by vacuum lines with vacuum pump, and flow direction of material is installed in vacuum lines and is equipped with tower successively
Condenser and chromatography device are pushed up, the gas phase import of the gaseous phase outlet and overhead condenser of stripper top connects, overhead condenser
Liquid-phase outlet is connect with the import of chromatography device, chromatographs the gas phase treatment connection vacuum pump of device, and the bottom liquid phases outlet of stripper connects
Connect triple effect evaporator.
Beneficial effects of the present invention：
The present invention provides a kind of completely new processing methods containing high salinity, oily waste water, realize oily, saline and alkaline in waste water
Liquid and water are effectively separated.There are following advantages by the present invention：
1, energy saving, heated time is short, cocnentration factor is big, separative efficiency is high, can continuous production.
2, waste water after processing can directly degrade use.
Description of the drawings
The accompanying drawings which form a part of this application are used for providing further understanding of the present application, and the application's shows
Meaning property embodiment and its explanation do not constitute the improper restriction to the application for explaining the application.
Fig. 1 is the structural schematic diagram of the device of the invention；
Wherein, 1, waste water storage tank, 2, wastewater feed tank, 3, heater, 4, stripper, 5, condenser, 6, chromatography device, 7, oil
Phase centrifugal pump, 8, oil phase recycling can, 9, water phase centrifugal pump, 10, vacuum pump, 11, one effect evaporation feed pump, 12, feed preheater
One, 13, feed preheater two, 14, one imitate knockout drum, 15, one effect circulating pump, 16, one effect heater, 17, one effect flash distillation
Tank, 18, two effect knockout drums, 19, two effect circulating pumps, 20, two effect heaters, 21, two effect flash tanks, 22, triple effect gas-liquid point
From tank, 23, triple effect cycle pump, 24, triple effect heater, 25, triple effect flash tank, 26, distillate cooler, 27, steam liquid storage tank,
28, distillate storage tank.
Specific implementation mode
It is noted that described further below be all exemplary, it is intended to provide further instruction to the application.Unless another
It indicates, all technical and scientific terms used herein has usual with the application person of an ordinary skill in the technical field
The identical meanings of understanding.
It should be noted that term used herein above is merely to describe specific implementation mode, and be not intended to restricted root
According to the illustrative embodiments of the application.As used herein, unless the context clearly indicates otherwise, otherwise singulative
It is also intended to include plural form, additionally, it should be understood that, when in the present specification using term "comprising" and/or " packet
Include " when, indicate existing characteristics, step, operation, device, component and/or combination thereof.
High salinity described herein refers to saline and alkaline molar content 0.5%~3.0%.
Triple effect evaporator described herein according to flow direction of material be divided into 1st effective evaporator, 2nd effect evaporator and
Third effect evaporator.
As background technology is introduced, exist in the prior art it is relatively low to useless Organic substance in water, oily removal rate, can not
The deficiency for meeting processing requirement, in order to solve technical problem as above, present applicant proposes a kind of process for treating oil-containing waste water.
A kind of exemplary embodiment of the application, provides a kind of process for treating oil-containing waste water, provides vacuum pump, stripping
Tower, overhead condenser, chromatography device, triple effect evaporator, using vacuum pump will strip tower pressure interior force reduce, discharge containing high salinity,
Waste water containing high salinity, oil is sent into the top of stripper top, packing layer by the pipeline of oily waste water, and waste water, which is evenly distributed on, to be filled out
The bed of material drops to bottom from stripper top, and after stripper bottom of tower heater temperature raising heating, oil and moisture are by hot vapour in waste water
It carries and being cooled down through overhead condenser after tower top discharge, detached into chromatography device, stripper bottom enters containing alkali waste water with high salt
Triple effect evaporation processing unit is handled.
Traditional stripper generally use normal pressure or pressurization are evaporated stripper, however which separative efficiency compared with
It is low, it is unfavorable for the separation of the oil and saline solution in waste water.The inventor of the present application discovered that reducing stripper by vacuum pump
Pressure can not only improve the output rate of gaseous phase materials, and the pressure for reducing stripper can increase the cocnentration factor of waste water, make
The oil and saline solution obtained in waste water is effectively separated.
Preferably, vacuum pump is reduced to -50~-30kPa by tower pressure interior force is stripped.The condition efficiency enough makes oil and saline solution
What is detached is more thorough.
Preferably, stripper bottom of tower heater heating temperature is set as 70~105 DEG C, and waste water temperature rises to 60 in stripper
~90 DEG C.Most oil and partial moisture are made to be discharged from tower top.
Preferably, overhead condenser is cooled down using recirculated water, and top gaseous phase is cooled to 30~50 DEG C.
Preferably, vacuum pump vacuumizes triple effect evaporator.
It is further preferred that the second effect is steamed the pressure reduction in 1st effective evaporator to -60~-40kPa by vacuum pump
The pressure reduction in device is sent out to -25~-15kPa, by the pressure reduction in third effect evaporator to -10~-5kPa.
It is further preferred that 1st effective evaporator steams the moisture of 23~27% (volumes), 2nd effect evaporator steams 23
The moisture of~27% (volume), third effect evaporator carry saliferous alkali waste water concentration to supersaturation, and crystallization treatment is discharged.
Preferably, the heat source of 1st effective evaporator is provided by the vapor that 2nd effect evaporator steams；2nd effect evaporator
The vapor that is steamed by third effect evaporator of heat source provide；Third effect evaporator heat source is provided by saturated vapor.The saturation
Steam is 1.3MPa saturated vapors.
Preferably, the moisture steamed in triple effect evaporator by steam liquid storage tank collect after, using distillate discharging pump outside
It send directly to degrade and use.
The another embodiment of the application provides a kind of device for realizing above-mentioned technique, including vacuum pump, stripping
Tower, triple effect evaporator, the stripper top side wall open up waste water inlet, and waste water inlet be located in stripper packing layer it
On, pipeline of the waste water inlet connection discharge containing high salinity, oily waste water of the stripper, the gaseous phase outlet of stripper top is set
There are vacuum lines, the gaseous phase outlet of stripper top to be connect with vacuum pump by vacuum lines, material stream is installed in vacuum lines
To overhead condenser and chromatography device is equipped with successively, the gas phase import of the gaseous phase outlet and overhead condenser of stripper top connects,
The liquid-phase outlet of overhead condenser is connect with the import of chromatography device, chromatographs the gas phase treatment connection vacuum pump of device, the bottom of stripper
Portion's liquid-phase outlet connects triple effect evaporator.
Preferably, three evaporators of triple effect evaporator are connect with vacuum pump.It is respectively triple effect evaporator to make vacuum pump
Three evaporators vacuumize.
Preferably, the often effect evaporator of triple effect evaporator is by knockout drum, circulating pump, heater and flash tank group
At.
In order to enable those skilled in the art can clearly understand the technical solution of the application, below with reference to tool
The technical solution of the application is described in detail with comparative example for the embodiment of body.
Embodiment use device as shown in Figure 1, including waste water storage tank 1, wastewater feed tank 2, heater 3, stripper 4,
Condenser 5, chromatography device 6, oil phase centrifugal pump 7, oil phase recycling can 8, water phase centrifugal pump 9, the effect evaporation feed pump of vacuum pump 10, one
11, feed preheater 1, feed preheater 2 13, triple effect evaporator, distillate cooler 26, steam liquid storage tank 27, steam
Liquid storage tank 28.
Triple effect evaporator by one effect knockout drum 14, one imitate circulating pump 15, one imitate heater 16, one imitate flash tank 17,
Two effect knockout drums 18, two imitate circulating pump 19, two and imitate the effect of heater 20, two flash tank 21, triple effect knockout drum 22, triple effect
Circulating pump 23, triple effect heater 24, triple effect flash tank 25 form.
Concrete technology is shown in following embodiment
Embodiment 1：
First, system pressure in stripper 4 is down to -35kPa using vacuum pump 10 hereinafter, then, giving up containing high salinity, oil
Water pumps 2 pipelines by wastewater feed from waste water storage tank 1 and is sent into 4 top of stripper, and the top of packing layer, waste water, which is evenly distributed on, to be filled out
The bed of material drops to bottom from 4 top of stripper, and bottom of tower heater heating temperature is set as 90 DEG C, adds through 3 temperature raising of bottom of tower heater
Heat is discharged after overwhelming majority oil and partial moisture are heated in waste water from tower top to 70 DEG C or more, the gas after the cooling of overhead condenser 5
Phase temperature is down to 35 DEG C and enters chromatography device 6, chromatographs the grease collected in device 6 and is layered in chromatography device, setting in chromatography device 6
Partition board separates oil and water, and oil phase, to 6 oil phase side of chromatography device, oil phase recycling can is sent to through oil phase centrifugal pump 7 through partition board overflow
8, chromatography 6 aqueous phase side of device sends waste water storage tank 1 back to through water phase centrifugal pump 9.Then 4 bottom saliferous alkali waste water of stripper is steamed by an effect
It sends out feed pump 11, feed preheater 1, feed preheater 2 13 and is sent into an effect evaporating, further carry out concentrate.
An effect evaporation process system pressure is down to -45kPa hereinafter, waste water enters an effect circulating pump 15 using vacuum pump 10
Inlet duct is pumped up into an effect circulatory system.Waste water is heated to 65 DEG C with two effect waste steams in an effect heater 16,
It is flashed subsequently into an effect vapor-liquid separation tank 14, saliferous alkali waste water is made to obtain concentrating for the first time, overhead waste water steam warp
After feed preheater 2 13 exchanges heat, distillate storage tank 27 is discharged into after tail gas condenser is cooled to 35 DEG C.It will using vacuum pump 10
Two effect evaporation process system pressures be down to -25kPa hereinafter, saliferous alkali waste water through one effect circulating pump 15 export branch line send to two effect follow
Waste water is heated to 100 DEG C by loop system in two effect heaters 20 with triple effect waste steam, and saliferous alkali waste water is in two effect vapour-liquids point
Second is carried out from the flash distillation of tank 18 to concentrate, heat source of the secondary wastewater steam that top generates as an effect heater 16, waste water steams
The waste water condensed water that vapour itself generates after being condensed cools down after effect 17 separate vapour of flash tank through 26 distillate coolers again
Enter distillate storage tank 27 afterwards.Triple effect evaporation processing system pressure is down to -10kPa hereinafter, containing saline and alkaline useless using vacuum pump 10
Water exports branch line through two effect circulating pumps 19 and send to triple effect cycle system, and the saliferous alkali waste water of triple effect cycle system is pumped through triple effect cycle
23 are sent to triple effect heater 24, after being heated to 125 DEG C with 1.3MPa steam, into 22 flash separation of triple effect vapor-liquid separation tank, top
Portion's steam as two effect the circulatory systems heat source, waste steam itself be condensed it is laggard two effect 21 separate vapour of steam flash tank,
Lime set, which enters, steams liquid storage tank 27.Triple effect heater condensate liquid is discharged into triple effect flash tank 25, flashes the steam of generation as two effects
The heat source of heater, flashes remaining moisture and is discharged into and steam liquid storage tank 27 or circulation.The thickened waste of triple effect cycle system
Waste tank is sent into liquid part through 23 outlet branch line of triple effect cycle pump.
Embodiment 2：
First, system pressure in stripper 4 is down to -45kPa using vacuum pump 10 hereinafter, then, giving up containing high salinity, oil
Water pumps 2 pipelines by wastewater feed from waste water storage tank 1 and is sent into 4 top of stripper, and the top of packing layer, waste water, which is evenly distributed on, to be filled out
The bed of material drops to bottom from 4 top of stripper, and bottom of tower heater heating temperature is set as 100 DEG C, through 3 temperature raising of bottom of tower heater
80 DEG C or more are heated to, is discharged from tower top after overwhelming majority oil and partial moisture are heated in waste water, after the cooling of overhead condenser 5
Gas phase temperature is down to 45 DEG C and enters chromatography device 6, chromatographs the grease collected in device 6 and is layered in chromatography device, chromatographs and set in device 6
It sets partition board to separate oil and water, oil phase is sent to oil phase recycling through partition board overflow to 6 oil phase side of chromatography device, through oil phase centrifugal pump 7
Tank 8, chromatography 6 aqueous phase side of device send waste water storage tank 1 back to through water phase centrifugal pump 9.Then 4 bottom saliferous alkali waste water of stripper passes through an effect
It evaporates feed pump 11, feed preheater 1, feed preheater 2 13 and is sent into an effect evaporating, further carried
It is dense.
An effect evaporation process system pressure is down to -55kPa hereinafter, waste water enters an effect circulating pump 15 using vacuum pump 10
Inlet duct is pumped up into an effect circulatory system.Waste water is heated to 75 DEG C with two effect waste steams in an effect heater 16,
It is flashed subsequently into an effect vapor-liquid separation tank 14, saliferous alkali waste water is made to obtain concentrating for the first time, overhead waste water steam warp
After feed preheater 2 13 exchanges heat, distillate storage tank 27 is discharged into after tail gas condenser is cooled to 35 DEG C.It will using vacuum pump 10
Two effect evaporation process system pressures be down to -20kPa hereinafter, saliferous alkali waste water through one effect circulating pump 15 export branch line send to two effect follow
Waste water is heated to 110 DEG C by loop system in two effect heaters 20 with triple effect waste steam, and saliferous alkali waste water is in two effect vapour-liquids point
Second is carried out from the flash distillation of tank 18 to concentrate, heat source of the secondary wastewater steam that top generates as an effect heater 16, waste water steams
The waste water condensed water that vapour itself generates after being condensed enters an effect heater 16, flash distillation after effect 17 separate vapour of flash tank again
Remaining moisture, which is discharged into, steams liquid storage tank 27.Triple effect evaporation processing system pressure is down to -5kPa hereinafter, containing using vacuum pump 10
Salt alkali waste water exports branch line through two effect circulating pumps 19 and send to triple effect cycle system, and the saliferous alkali waste water of triple effect cycle system is through triple effect
Circulating pump 23 is sent to triple effect heater 24, after being heated to 135 DEG C with 1.3MPa steam, into the flash distillation point of triple effect vapor-liquid separation tank 22
Heat source from, overhead vapor as the two effect circulatory systems, waste steam itself the laggard two effects steam flash tank 21 that is condensed detach
Steam, lime set, which enters, steams liquid storage tank 27.Triple effect heater condensate liquid is discharged into triple effect flash tank 25, flashes the steam conduct of generation
The heat source of two effect heaters, flashes remaining moisture and is discharged into and steam liquid storage tank 27 or circulation.Triple effect cycle system it is dense
Waste tank is sent into contracting waste liquid part through 23 outlet branch line of triple effect cycle pump, is then pumped to crystallizing pond through waste liquid conveying.
The foregoing is merely the preferred embodiments of the application, are not intended to limit this application, for the skill of this field
For art personnel, the application can have various modifications and variations.Within the spirit and principles of this application, any made by repair
Change, equivalent replacement, improvement etc., should be included within the protection domain of the application.
Claims (10)
1. a kind of process for treating oil-containing waste water, characterized in that provide vacuum pump, stripper, overhead condenser, chromatography device, triple effect
Evaporator, will strip tower pressure interior force using vacuum pump reduces, discharge the pipeline containing high salinity, oily waste water will contain high salinity,
The waste water of oil is sent into the top of stripper top, packing layer, and waste water is evenly distributed on packing layer and drops to bottom from stripper top
Portion, through the heater temperature raising of stripper bottom of tower heating after, in waste water oil and moisture by thermal stripping from tower top discharge after through overhead condensation
Device cools down, and is detached into chromatography device, stripper bottom enters triple effect evaporation processing unit containing alkali waste water with high salt and handled.
2. technique as described in claim 1, characterized in that vacuum pump is reduced to -50~-30kPa by tower pressure interior force is stripped.
3. technique as described in claim 1, characterized in that stripper bottom of tower heater heating temperature is set as 70~105 DEG C,
Waste water temperature rises to 60~90 DEG C in stripper.
4. technique as described in claim 1, characterized in that overhead condenser is cooled down using recirculated water, by top gaseous phase
It is cooled to 30~50 DEG C.
5. technique as described in claim 1, characterized in that vacuum pump vacuumizes triple effect evaporator.
6. technique as claimed in claim 5, characterized in that vacuum pump by the pressure reduction in 1st effective evaporator extremely
- 60~-40kPa, by the pressure reduction in 2nd effect evaporator to -25~-15kPa, by the pressure in third effect evaporator
Power is reduced to -10~-5kPa.
7. technique as claimed in claim 5, characterized in that 1st effective evaporator steams the moisture of 23~27% (volumes), the
2nd effect evaporator steams the moisture of 23~27% (volumes), and third effect evaporator carries saliferous alkali waste water concentration to supersaturation,
Crystallization treatment is discharged.
8. technique as described in claim 1, characterized in that the water that the heat source of 1st effective evaporator is steamed by 2nd effect evaporator
Steam provides；The heat source of 2nd effect evaporator is provided by the vapor that third effect evaporator steams；Third effect evaporator heat source by
Saturated vapor provides.
9. technique as described in claim 1, characterized in that the moisture steamed in triple effect evaporator is collected by steaming liquid storage tank
Afterwards, it sends outside directly to degrade using distillate discharging pump and use.
10. a kind of device for realizing technique described in claim 1, characterized in that including vacuum pump, stripper, triple effect evaporator,
The stripper top side wall opens up waste water inlet, and waste water inlet is located in stripper on packing layer, the stripper
Pipeline of the waste water inlet connection discharge containing high salinity, oily waste water, the gaseous phase outlet of stripper top are equipped with vacuum lines, stripping
The gaseous phase outlet of top of tower is connect by vacuum lines with vacuum pump, and it is cold equipped with tower top successively that flow direction of material is installed in vacuum lines
Condenser and chromatography device, the gas phase import of the gaseous phase outlet and overhead condenser of stripper top connect, the liquid phase of overhead condenser
It exports and is connect with the import of chromatography device, chromatograph the gas phase treatment connection vacuum pump of device, the bottom liquid phases outlet connection three of stripper
Imitate evaporator.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110498463A (en) * | 2019-08-20 | 2019-11-26 | 石家庄惠洁科技有限公司 | The process for cleanly preparing of low concentration volatile waste in a kind of water |
| CN110980847A (en) * | 2019-12-25 | 2020-04-10 | 山东东岳氟硅材料有限公司 | Treatment and recovery system and method for waste alkali in methane chloride production |
| CN112955427A (en) * | 2019-04-04 | 2021-06-11 | 株式会社Lg化学 | System for continuous purification of esterification reaction products |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1902012A (en) * | 2003-11-07 | 2007-01-24 | 拉肯耐尔能量及环境公司 | Oil contaminated substrate treatment method and apparatus |
| JP2008023411A (en) * | 2006-07-18 | 2008-02-07 | Mhi Solution Technologies Co Ltd | Method for treating waste water when biodiesel fuel is washed |
| CN102504852A (en) * | 2011-11-03 | 2012-06-20 | 中润天海（北京）环保科技有限公司 | Improved Litwin coal tar processing technic |
| CN203451486U (en) * | 2013-07-24 | 2014-02-26 | 中国石油化工股份有限公司 | Negative pressure air stripping desulfurizer |
| CN105271585A (en) * | 2014-06-11 | 2016-01-27 | 中国石油化工股份有限公司 | Method for processing wastewater generated in a process for preparing butadiene through oxidative dehydrogenation of industrial butylene |
| CN108069479A (en) * | 2016-11-11 | 2018-05-25 | 中国石油化工股份有限公司抚顺石油化工研究院 | A kind of wastewater treatment method and system |
-
2018
- 2018-06-07 CN CN201810580959.5A patent/CN108640392B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1902012A (en) * | 2003-11-07 | 2007-01-24 | 拉肯耐尔能量及环境公司 | Oil contaminated substrate treatment method and apparatus |
| JP2008023411A (en) * | 2006-07-18 | 2008-02-07 | Mhi Solution Technologies Co Ltd | Method for treating waste water when biodiesel fuel is washed |
| CN102504852A (en) * | 2011-11-03 | 2012-06-20 | 中润天海（北京）环保科技有限公司 | Improved Litwin coal tar processing technic |
| CN203451486U (en) * | 2013-07-24 | 2014-02-26 | 中国石油化工股份有限公司 | Negative pressure air stripping desulfurizer |
| CN105271585A (en) * | 2014-06-11 | 2016-01-27 | 中国石油化工股份有限公司 | Method for processing wastewater generated in a process for preparing butadiene through oxidative dehydrogenation of industrial butylene |
| CN108069479A (en) * | 2016-11-11 | 2018-05-25 | 中国石油化工股份有限公司抚顺石油化工研究院 | A kind of wastewater treatment method and system |
Non-Patent Citations (1)
| Title |
|---|
| 瞿新东: "多效蒸发及气提工艺处理丁辛醇装置含碱废水", 《齐鲁石油化工》 * |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112955427A (en) * | 2019-04-04 | 2021-06-11 | 株式会社Lg化学 | System for continuous purification of esterification reaction products |
| CN112955427B (en) * | 2019-04-04 | 2024-04-19 | 株式会社Lg化学 | System for continuous purification of esterification reaction products |
| CN110498463A (en) * | 2019-08-20 | 2019-11-26 | 石家庄惠洁科技有限公司 | The process for cleanly preparing of low concentration volatile waste in a kind of water |
| CN110498463B (en) * | 2019-08-20 | 2022-02-11 | 石家庄惠洁科技有限公司 | Clean production process of low-concentration volatile waste in water |
| CN110980847A (en) * | 2019-12-25 | 2020-04-10 | 山东东岳氟硅材料有限公司 | Treatment and recovery system and method for waste alkali in methane chloride production |
| CN110980847B (en) * | 2019-12-25 | 2022-04-12 | 山东东岳氟硅材料有限公司 | Treatment and recovery system and method for waste alkali in methane chloride production |
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