CN108128982A - Wastewater treatment method in 2- propyl enanthol process units - Google Patents
Wastewater treatment method in 2- propyl enanthol process units Download PDFInfo
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- CN108128982A CN108128982A CN201810009105.1A CN201810009105A CN108128982A CN 108128982 A CN108128982 A CN 108128982A CN 201810009105 A CN201810009105 A CN 201810009105A CN 108128982 A CN108128982 A CN 108128982A
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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
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/04—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste liquors, e.g. sulfite liquors
-
- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/02—Temperature
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/03—Pressure
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
Abstract
The present invention relates to wastewater treatment methods in a kind of 2 propyl enanthol process units, mainly solve the problems, such as that wastewater treatment process waste water treatment plant load is big in the prior art.The present invention includes the following steps by using wastewater treatment method in a kind of 2 propyl enanthol process units：(1) waste water enters concentration packet equipment, and the concentrate that concentration packet equipment obtains enters souring tank after cooler cools down, and the water that concentration packet equipment concentrates out enters biochemical treatment plants biochemical treatment；(2) concentrate of souring tank outlet enters chromatography device, obtains organic phase and water phase；(3) organic phase enters rectifying column, rectifying tower top obtains valeric acid, rectifying tower reactor heavy constituent enters incinerator, the water phase enters crystallizing evaporator, obtain water and solid salt, the technical solution that wherein water returns to concentration packet equipment reuse preferably solves the above problem, available in wastewater treatment in 2 propyl enanthol process units.
Description
Technical field
The present invention relates to wastewater treatment methods in a kind of 2- propyl enanthols process units.
Background technology
The existing 2- propyl enanthols production technology in China is mainly butylene oxo synthesis.This method is first with butylene and synthesis
Gas is Material synthesis valeral, then carries out aldol reaction generation decenal under catalysis of 2% sodium hydroxide or so by valeral
(PBA).PBA is by being hydrogenated to 2- propyl enanthols.Can generate water during aldol reaction causes concentration of lye to reduce, and
The natrium valericum of side reaction generation can add up in systems, so the fresh lye of a certain amount of high concentration must be added, discharge simultaneously
A part of lye thereby produces 2- propyl enanthol spent lyes.
The distinguishing feature of spent lye is pH value height, and content of organics is very high, COD COD high, and is fluctuated
Larger, major pollutants include amylalcohol, valeral, PBA and heavy constituent.Since poisonous and harmful substance is more in spent lye, concentration compared with
Height, the difficulty individually pre-processed are larger.The process units of domestic 2- propyl enanthols is less, is substantially for the spent lye of device
Dilute laggard sewage treatment plant.This has aggravated the load of sewage disposal system, wastes valuable water resource.
In recent years, one side national wastewater discharge standard is continuously improved, and the pressure of scale wastewater treatment qualified discharge is continuous
It aggravates, on the other hand, country can promote enterprise's continuous improvement using water wisely water for the purpose of water conservation, water rate up-regulation
It is flat, dilution water during wastewater biochemical processing is reduced, this also increases the difficulty of discharged wastewater met the national standard.Therefore exploitation one is needed
The effective 2- propyl enanthols salkali waste liquid processing method of kind, reduces waste water COD, mitigates the processing load of subsequent processes and use water
Burden.
The waste water of existing country's 2- propyl enanthol devices is discharged to sewage treatment plant's processing (at neutralization, air supporting, biochemistry
Reason), because sewage alkalinity is strong, and COD contents are high, and cost of sewage disposal is high and the organic matters such as valeric acid are difficult to biochemical decomposition, most of
It is adsorbed in biochemical sludge, monthly needs to clear up sludge, and the sludge containing valeric acid belongs to danger wastes, it is difficult to
Processing.
Invention content
The technical problems to be solved by the invention, which are that wastewater treatment process waste water treatment plant load is big in the prior art, asks
Topic, provides wastewater treatment method in a kind of new 2- propyl enanthol process units.This method has wastewater treatment process water process
The advantages of factory's load is small.
To solve the above problems, the technical solution adopted by the present invention is as follows：Waste water in a kind of 2- propyl enanthols process units
Processing method includes the following steps：(1) waste water enters concentration packet equipment, and the concentrate that concentration packet equipment obtains is cold through cooler
But enter souring tank afterwards, the water that concentration packet equipment concentrates out enters biochemical treatment plants biochemical treatment；(2) concentration of souring tank outlet
Liquid enters chromatography device, obtains organic phase and water phase；(3) organic phase enters rectifying column, and rectifying tower top obtains valeric acid, rectifying column
Kettle heavy constituent enters incinerator, and the water phase enters crystallizing evaporator, obtains water and solid salt, and wherein water returns to concentration packet equipment
Reuse.
In above-mentioned technical proposal, it is preferable that for the waste water COD in 30000~100000mg/L, pH is 8~14.
In above-mentioned technical proposal, it is preferable that acid includes inorganic acid and organic acid.
In above-mentioned technical proposal, it is highly preferred that inorganic acid is sulfuric acid, hydrochloric acid, nitric acid, phosphoric acid, organic acid is formic acid, second
Acid, propionic acid.
In above-mentioned technical proposal, it is preferable that concentration packet equipment is multiple-effect evaporation packet equipment, MVR concentrates packet equipment or reverse osmosis
Concentration packet equipment thoroughly.
In above-mentioned technical proposal, it is preferable that the water that concentration packet equipment concentrates out is the 80-85%, COD of wastewater feed amount
Less than 500mg/L.
In above-mentioned technical proposal, it is preferable that the concentrate that concentration packet equipment obtains is after cooler is cooled to 15~60 DEG C
Into souring tank, souring tank control pH is 1~6.
In above-mentioned technical proposal, it is preferable that rectifying column operating condition be 15~80kpaA of operating pressure, column bottom temperature 130
~180 DEG C, 60~120 DEG C of tower top temperature.
In above-mentioned technical proposal, it is preferable that crystallizing evaporator operating condition is 10~110kpaA of operating pressure, and operation is warm
70~120 DEG C of degree.
In above-mentioned technical proposal, it is preferable that chromatograph device operating condition as normal pressure and micro-positive pressure, 15~45 DEG C of operation temperature.
The present invention is big for country 2- propyl enanthol spent lye wastewater treatment difficulty, develops a kind of high treating effect, energy
Consume the treatment process low, waste resource utilizes.By present treatment technique, the concentrated processing of 2- propyl enanthol spent lyes of high COD,
The waste water COD of biochemical treatment apparatus is sent in 500mg/L hereinafter, the removal rate of COD is more than 99%.Concentrate is quiet by being acidified
Layering is put, organic matter is made to be separated with high level salt solution.Organic phase obtains high-purity valeric acid product by rectifying, and high level salt solution is further
Condensing crystallizing obtains selling outside solid salt.Compared with this technique send biochemical treatment apparatus technique after being diluted through water, life is not only alleviated
Change the load for the treatment of plant and saved valuable water resource, and turn waste into wealth, obtain the valeric acid of high added value, achieve preferably
Technique effect.
Description of the drawings
Fig. 1 is the flow diagram of the method for the invention.
1- concentrates packet equipment 2- cooler 3- souring tanks 4- chromatography device 5- rectifying column 6- crystallizing evaporator 7- waste water 8- in Fig. 1
Biochemical treatment plants 9- acid 10- incinerator 11- salt 12- valeric acids.
The present invention will be further described below by way of examples, but is not limited only to the present embodiment.
Specific embodiment
【Embodiment 1】
Wastewater treatment method in a kind of 2- propyl enanthols process units, as shown in Figure 1,1000kg/h, 95 DEG C of 2- propyl
Enanthol spent lye waste water (COD 30000mg/L, NaOH 1.0wt% in waste water, natrium valericum 4.5wt%, valeral 0.2wt%, penta
Alcohol 0.15wt%) enter concentration packet equipment, concentration packet equipment is multi-effect evaporator, and the operating pressure 0.1bar of evaporator is operated
103 DEG C of temperature, evaporator shell side are heated by the low-pressure steam of 3barg, and waste water self-loopa in evaporator is concentrated by evaporation, evaporation
The vapor of 85kg/h is steamed at the top of device, becomes the water that COD is 300mg/L after cooling and is sent into biochemical treatment plants processing；15kg/h,
103 DEG C of concentrate is discharged from base of evaporator, and 15 DEG C are cooled into cooler, and concentrate after cooling enters souring tank,
2.5kg/h, 98% concentrated sulfuric acid are slowly dropped at the top of jar, control pH is a strong exothermal reaction for 6 dropwise addition processes, is acidified ladle bowl
Side is passed through circulating water, controls no more than 60 DEG C of temperature in souring tank, the concentrate after acidification enters chromatography device, chromatographs device
Operating condition is normal pressure, and 15 DEG C of temperature, from chromatography device top into rectifying column middle part, rectifying column operates the organic phase of 4.8kg/h
Condition is that operating pressure is 15kpaA, and 60 DEG C of tower top, 130 DEG C of bottom of towe, rectifying column tower top obtains the penta of 3.9kg/h purity 99.7%
Acid, rectifying column bottom obtain the heavy constituent of 0.9kg/h.The water phase that chromatography device bottom obtains 12.7kg/h enters evaporative crystallization room, steams
It is operating pressure 10kpaA to send out crystallizer operation condition, and 70 DEG C of operation temperature, evaporator shell-side is added with the low-pressure steam of 4barg
Heat, bottom obtain the sulfate crystal solid (containing the crystallization water) of 3.1kg/h, and the steam of crystallizing evaporator evaporated on top and charging are useless
It is hydrated and rear into evaporator.
Method using the present invention, the COD removal rates of 2- propyl enanthol spent lye waste water reach 99%, and organic phase passes through essence
Evaporate to obtain high-purity valeric acid product, sold, while reduce the load of biochemical treatment plants outside solid salt, it is concentrated, evaporate it is useless
It can be arranged outside after the simple biochemical treatment of water.
【Embodiment 2】
Wastewater treatment method in a kind of 2- propyl enanthols process units, as shown in Figure 1,1000kg/h, 95 DEG C of 2- propyl
Enanthol spent lye waste water (COD 30000mg/L, NaOH 1.0wt% in waste water, natrium valericum 4.5wt%, valeral 0.2wt%, penta
Alcohol 0.15wt%) enter concentration packet equipment, concentration packet equipment is multi-effect evaporator, and the operating pressure 0.1bar of evaporator is operated
103 DEG C of temperature, evaporator shell side are heated by the low-pressure steam of 3barg, and waste water self-loopa in evaporator is concentrated by evaporation, evaporation
The vapor of 85kg/h is steamed at the top of device, becomes the water that COD is 300mg/L after cooling and is sent into biochemical treatment plants processing；15kg/h,
103 DEG C of concentrate is discharged from base of evaporator, and 15 DEG C are cooled into cooler, and concentrate after cooling enters souring tank,
2.5kg/h, 98% concentrated sulfuric acid are slowly dropped at the top of jar, control pH is 1, and dropwise addition process is a strong exothermal reaction, souring tank
Shell-side is passed through circulating water, controls no more than 60 DEG C of temperature in souring tank, the concentrate after acidification enters chromatography device, chromatography
Device operating condition is normal pressure, and temperature 45 C, the organic phase of 4.8kg/h is from chromatographing at the top of device into rectifying column middle part, rectifying column behaviour
As condition be operating pressure it is 15kpa, 60 DEG C of tower top, 130 DEG C of bottom of towe, rectifying column tower top obtains 3.9kg/h purity 99.7%
Valeric acid, rectifying column bottom obtain the heavy constituent of 0.9kg/h.The water phase that chromatography device bottom obtains 12.7kg/h enters evaporative crystallization room,
Crystallizing evaporator operating condition is operating pressure 10kpaA, and 70 DEG C of operation temperature, evaporator shell-side is added with the low-pressure steam of 4barg
Heat, bottom obtain the sulfate crystal solid (containing the crystallization water) of 3.1kg/h, and the steam of crystallizing evaporator evaporated on top and charging are useless
It is hydrated and rear into evaporator.
Method using the present invention, the COD removal rates of 2- propyl enanthol spent lye waste water reach 99%, and organic phase passes through essence
Evaporate to obtain high-purity valeric acid product, sold, while reduce the load of biochemical treatment plants outside solid salt, it is concentrated, evaporate it is useless
It can be arranged outside after the simple biochemical treatment of water.
【Embodiment 3】
Wastewater treatment method in a kind of 2- propyl enanthols process units, as shown in Figure 1,1000kg/h, 95 DEG C of 2- propyl
Enanthol spent lye waste water (COD 50000mg/L, NaOH 1.0wt% in waste water, natrium valericum 5.1wt%, valeral 0.2wt%, penta
Alcohol 0.15wt%) enter concentration packet equipment, concentration packet equipment is multi-effect evaporator, and the operating pressure 0.1bar of evaporator is operated
104 DEG C of temperature, evaporator shell side are heated by the low-pressure steam of 3barg, and waste water self-loopa in evaporator is concentrated by evaporation, evaporation
The vapor of 84kg/h is steamed at the top of device, becomes the water that COD is 300mg/L after cooling and is sent into biochemical treatment plants processing；16kg/h,
104 DEG C of concentrate is discharged from base of evaporator, and 60 DEG C are cooled into cooler, and concentrate after cooling enters souring tank,
2.9kg/h, 98% concentrated sulfuric acid are slowly dropped at the top of jar, control pH is 3, and dropwise addition process is a strong exothermal reaction, souring tank
Shell-side is passed through circulating water, controls no more than 60 DEG C of temperature in souring tank, the concentrate after acidification enters chromatography device, chromatography
Device operating condition is normal pressure, and temperature 45 C, the organic phase of 5.8kg/h is from chromatographing at the top of device into rectifying column middle part, rectifying column behaviour
As condition be operating pressure it is 80kpa, 120 DEG C of tower top, 180 DEG C of bottom of towe, rectifying column tower top obtains 4.9kg/h purity 99.7%
Valeric acid, rectifying column bottom obtain the heavy constituent of 0.9kg/h.The water phase that chromatography device bottom obtains 13.1kg/h enters evaporative crystallization room,
Crystallizing evaporator operating condition be operating pressure 110kpaA, 120 DEG C of operation temperature, the low-pressure steam of evaporator shell-side 4barg
Heating, bottom obtain the sulfate crystal solid (containing the crystallization water) of 4.1kg/h, the steam of crystallizing evaporator evaporated on top and charging
Waste water enters evaporator after merging.
Method using the present invention, the COD removal rates of 2- propyl enanthol spent lye waste water reach 99%, and organic phase passes through essence
Evaporate to obtain high-purity valeric acid product, sold, while reduce the load of biochemical treatment plants outside solid salt, it is concentrated, evaporate it is useless
It can be arranged outside after the simple biochemical treatment of water.
【Embodiment 4】
Wastewater treatment method in a kind of 2- propyl enanthols process units, as shown in Figure 1,1000kg/h, 95 DEG C of 2- propyl
Enanthol spent lye waste water (COD 100000mg/L, NaOH 1.0wt%, natrium valericum 9.3wt%, valeral 0.2wt% in waste water,
Amylalcohol 0.15wt%) enter concentration packet equipment, concentration packet equipment is multi-effect evaporator, and the operating pressure 0.1bar of evaporator is grasped
Make 104 DEG C of temperature, evaporator shell side is heated by the low-pressure steam of 3barg, and waste water self-loopa in evaporator is concentrated by evaporation, and is steamed
The vapor of 78kg/h is steamed at the top of hair device, becomes the water that COD is 460mg/L after cooling and is sent into biochemical treatment plants processing；22kg/
H, 104 DEG C of concentrate are discharged from base of evaporator, are cooled to 60 DEG C into cooler, concentrate after cooling enters acidification
Tank, jar top are slowly dropped into 4.1kg/h, 98% concentrated sulfuric acid, and control pH is 1, and dropwise addition process is a strong exothermal reaction, is acidified
Ladle bowl side is passed through circulating water, controls no more than 60 DEG C of temperature in souring tank, the concentrate after acidification enters chromatography device, layer
Parser operating condition is micro-positive pressure, and temperature 45 C, the organic phase of 10.7kg/h is from chromatographing at the top of device into rectifying column middle part, rectifying
Tower operating condition is that operating pressure is 80kpa, and 120 DEG C of tower top, 180 DEG C of bottom of towe, rectifying column tower top obtains 9.8kg/h purity
99.7% valeric acid, rectifying column bottom obtain the heavy constituent of 0.9kg/h.The water phase that chromatography device bottom obtains 15.4kg/h enters evaporation
Crystallisation chamber, crystallizing evaporator operating condition are operating pressure 110kpaA, and 120 DEG C of operation temperature, evaporator shell-side is with 4barg's
Low-pressure steam heats, and bottom obtains the sulfate crystal solid (containing the crystallization water) of 5.2kg/h, the steaming of crystallizing evaporator evaporated on top
Gas enters evaporator after merging with charging waste water.
Method using the present invention, the COD removal rates of 2- propyl enanthol spent lye waste water reach 99%, and organic phase passes through essence
Evaporate to obtain high-purity valeric acid product, sold, while reduce the load of biochemical treatment plants outside solid salt, it is concentrated, evaporate it is useless
It can be arranged outside after the simple biochemical treatment of water.
【Comparative example】
The waste water of existing country's 2- propyl enanthol devices is discharged to sewage treatment plant's processing (at neutralization, air supporting, biochemistry
Reason), because sewage alkalinity is strong, and COD contents are high, and cost of sewage disposal is high, and processing cost is up to 300 yuan/ton, and valeric acid etc. is organic
Object is difficult to biochemical decomposition, is largely adsorbed in biochemical sludge, monthly needs to clear up sludge, and the dirt containing valeric acid
Mud belongs to danger wastes, it is difficult to handle.
Using this patent method, operating cost is concentrated mainly on multiple-effect evaporation workshop section, if using three-effect evaporation and condensation, this
The cost of sewage disposal of patent is about 80 yuan/ton, and processing cost is low.
Claims (10)
1. wastewater treatment method in a kind of 2- propyl enanthols process units, includes the following steps：(1) butylene oxo synthesis produces
Waste water in 2- propyl enanthol devices enters concentration packet equipment, and the concentrate that concentration packet equipment obtains enters after cooler cools down
Souring tank, the water that concentration packet equipment concentrates out enter biochemical treatment plants biochemical treatment；(2) souring tank outlet acidification concentrate into
Enter to chromatograph device, obtain organic phase and water phase；(3) organic phase enters rectifying column, and rectifying tower top obtains valeric acid, rectifying tower reactor weight
Component enters incinerator, and the water phase enters crystallizing evaporator, obtains water and solid salt, and wherein water returns to concentration packet equipment and returns
With.
2. wastewater treatment method in 2- propyl enanthols process units according to claim 1, it is characterised in that the waste water COD
In 30000~100000mg/L, pH is 8~14.
3. wastewater treatment method in 2- propyl enanthols process units according to claim 1, it is characterised in that acid includes inorganic
Acid and organic acid.
4. wastewater treatment method in 2- propyl enanthols process units according to claim 3, it is characterised in that inorganic acid is sulphur
Acid, hydrochloric acid, nitric acid, phosphoric acid, organic acid is formic acid, acetic acid, propionic acid.
5. wastewater treatment method in 2- propyl enanthols process units according to claim 1, it is characterised in that concentration packet equipment
Packet equipment or reverse osmosis concentration packet equipment are concentrated for multiple-effect evaporation packet equipment, MVR.
6. wastewater treatment method in 2- propyl enanthols process units according to claim 1, it is characterised in that concentration packet equipment
The water concentrated out is the 80-85% of wastewater feed amount, and COD is less than 500mg/L.
7. wastewater treatment method in 2- propyl enanthols process units according to claim 1, it is characterised in that concentration packet equipment
Obtained concentrate enters souring tank after cooler is cooled to 15~60 DEG C, and souring tank control pH is 1~6.
8. wastewater treatment method in 2- propyl enanthols process units according to claim 1, it is characterised in that rectifying column operates
Condition be 15~80kpaA of operating pressure, 130~180 DEG C of column bottom temperature, 60~120 DEG C of tower top temperature.
9. wastewater treatment method in 2- propyl enanthols process units according to claim 1, it is characterised in that crystallizing evaporator
Operating condition be 10~110kpaA of operating pressure, 70~120 DEG C of operation temperature.
10. wastewater treatment method in 2- propyl enanthols process units according to claim 1, it is characterised in that chromatography device operation
It is normal pressure and micro-positive pressure that condition, which is operating pressure, 15~45 DEG C of operation temperature.
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|---|---|---|---|---|
| WO2021037572A1 (en) | 2019-08-23 | 2021-03-04 | Basf Se | Process for treating wastewater from an aldolization process |
| CN113716777A (en) * | 2021-08-31 | 2021-11-30 | 定陶三化药业有限公司 | Process for separating organic matters in waste salt by utilizing concentration steam stripping method |
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| CN102730894A (en) * | 2011-04-15 | 2012-10-17 | 中国石油化工股份有限公司 | Method for treating waste alkaline liquor produced in butanol and octanol production device |
| WO2014016773A1 (en) * | 2012-07-24 | 2014-01-30 | Saudi Basic Industries Corporation | Method for treating alkaline wastewater |
| CN104071940A (en) * | 2013-03-28 | 2014-10-01 | 中国石油天然气股份有限公司 | Processing method of butanol and octanol waste alkaline solution |
| WO2016207272A1 (en) * | 2015-06-23 | 2016-12-29 | Shell Internationale Research Maatschappij B.V. | Apparatus and method for reactive distillation for waste water treatment |
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| WO2021037572A1 (en) | 2019-08-23 | 2021-03-04 | Basf Se | Process for treating wastewater from an aldolization process |
| CN113716777A (en) * | 2021-08-31 | 2021-11-30 | 定陶三化药业有限公司 | Process for separating organic matters in waste salt by utilizing concentration steam stripping method |
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