CN107935232A - A kind of electro-desalting is given up the separation method of Organic substance in water - Google Patents

A kind of electro-desalting is given up the separation method of Organic substance in water Download PDF

Info

Publication number
CN107935232A
CN107935232A CN201711056059.2A CN201711056059A CN107935232A CN 107935232 A CN107935232 A CN 107935232A CN 201711056059 A CN201711056059 A CN 201711056059A CN 107935232 A CN107935232 A CN 107935232A
Authority
CN
China
Prior art keywords
xad
ionic
electro
separation method
volume
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.)
Pending
Application number
CN201711056059.2A
Other languages
Chinese (zh)
Inventor
张华�
刘译阳
张晓飞
罗臻
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
China National Petroleum Corp
Original Assignee
China National Petroleum Corp
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by China National Petroleum Corp filed Critical China National Petroleum Corp
Priority to CN201711056059.2A priority Critical patent/CN107935232A/en
Publication of CN107935232A publication Critical patent/CN107935232A/en
Pending legal-status Critical Current

Links

Classifications

    • 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
    • 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
    • C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation
    • 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
    • C07C51/48—Separation; Purification; Stabilisation; Use of additives by liquid-liquid treatment
    • 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
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • 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
    • 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
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • 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
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • C02F2001/425—Treatment of water, waste water, or sewage by ion-exchange using cation exchangers
    • 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
    • C02F2103/365—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 from petrochemical industry (e.g. refineries)
    • 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

Abstract

Give up the separation method of Organic substance in water the present invention provides a kind of electro-desalting.The separation method includes：Pre-process electro-desalting waste water；Pass through 8 non-ionic macroporous resin columns of XAD；8 non-ionic macroporous resin columns of XAD after being adsorbed with hydrochloric acid backwash；Pass through the 4 non-ionic macroporous resin column of 8 non-ionic macroporous resin columns of XAD and XAD of series connection；With 8 non-ionic macroporous resin columns of sodium hydroxide solution backwash XAD；With 4 non-ionic macroporous resin columns of sodium hydroxide solution backwash XAD；Surname extraction is carried out, rotary evaporated to dryness is carried out to obtained extracting solution；Cross MSC H cation exchange resin columns；Dichloromethane extracts；With sodium hydroxide solution backwash MSC H cation exchange resin columns, complete to separate electro-desalting waste water.The separation method of the present invention can the organic matter of the quickly and easily electro-desalting waste water to crude oil separate, and can purify mainly organic pollution aphthenic acids therein.

Description

A kind of electro-desalting is given up the separation method of Organic substance in water
Technical field
The present invention relates to a kind of separation method, more particularly to a kind of electro-desalting of crude oil is given up the separation side of Organic substance in water Method, belongs to crude oil polluted water process technical field.
Background technology
Water, inorganic salts, suspended solid and water-soluble trace metal are usually contained in crude oil.The first step of oil refining is by de- Dehydration of salt removes these materials, is blocked and incrustation with reducing the burn into of equipment, while prevent the catalyst of subsequent processing units Poisoning.Except indivedual super-viscous oils use three-level electro-desalting, most of crude oil uses two level technology of electric de-salting.
Electro-desalting waste water typically contains petroleum-type, inorganic salts, sulfide, phenol, suspended particulate substance and various organic matters, bag Include demulsifier added in desalting and dewatering etc..Crude oil heaviness, in poor quality trend are more and more obvious in recent years, electro-desalting waste water Component is more complicated, particularly contains more aphthenic acids, lower fatty acid and phenol in high acid crude oil electric desalting wastewater Compound, organic pollution load higher, bio-toxicity are stronger, and serious impact is caused to downstream wastewater facility for the central disposal, with useless Stringent, the qualified discharge problem of high acid crude oil electric desalting wastewater in the urgent need to address of water discharge standard.
Researcher thinks that electro-desalting waste water should carry out dual treatment, when its salt quality concentration is more than 1200mg/L, can return In saline sewage processing system；When salt quality concentration is less than or equal to 1200mg/L, oil-containing sewage treatment system is attributable to.It is but many More results of study show that the major issue for influencing electro-desalting wastewater treatment is not salt content, but organic pollution therein is asked Topic, it is therefore necessary to pre-processed according to the characteristic of pollutant.Wherein, aphthenic acids is difficult to biochemical degradation, biochemical treatment water outlet Middle residual concentration is higher, is to cause high acid crude oil electric desalting wastewater COD to be difficult to the main reason for up to standard；Crude oil electric desalting treats It is up to standard tired to also result in effluent quality for emulsified asphalt matter that may be present in various surfactants and electro-desalting waste water that journey adds It is difficult.
Cheng Bin (coagulation-Fenton method preprocess analog electro-desalting waste water《Environmental project》, the 6th phase of volume 28 in 2010, 31-35) simulation electro-desalting waste water is pre-processed using coagulation-Fenton methods, part organic loading can be reduced；Xie Jinqiao (the pretreatment of Electric Desalting Wastewater《Petrochemical industry environmental protection》, the 3rd phase in 1992,19-22) thrown in acid electro-desalting waste water Add chitin and poly-aluminium flocculant, CODCr and oil content remove obvious；Yang Xiujuan (the places of Shandong desalting in oil refinery waste water Reason research Qingdao University of Science and Technology Master's thesis, 2010) use coagulation-O3/H2O2Group technology handles electro-desalting waste water；Zou Zong (heavy crude Electric Desalting Wastewater further treatment technique studies in sea《Shandong petrochemical industry》, the 2nd phase of volume 2012,40,91-92) Advanced treating is carried out to the electro-desalting waste water after biochemistry using hypochlorite oxidation technique, effluent quality is preferable.
But it is also unapparent for the composition of electro-desalting Pollutants in Wastewater at present, it can not also select the pre-treatment work adapted to Skill.Chinese patent application CN102313658B and CN 02313659B individually disclose a kind of preparation of naphthenic acid sample in wastewater The separation of low concentration aphthenic acids and sample preparation methods in method and a kind of waste water, mainly by adsorbing resin and cation exchange Resin separating naphthenic acid, but other components in waste water are not separated, and the aphthenic acids after separation does not extract further Purification, being adjusted merely by pH value acidity can not still cause whole small molecule aphthenic acids to precipitate completely.Other researchers also utilize Characteristic contamination in the methods of GC-MS, ESI-MS, FTIR research electro-desalting waste water, but can not be more careful to electro-desalting Most of organic matter in waste water carries out classification characterization, it is also difficult to realizes to organic pollution component during treatment process Change into line trace.
The content of the invention
In order to solve the above-mentioned technical problem, quickly and easily the electricity of crude oil is taken off it is an object of the invention to provide a kind of The organic matter of salt waste water is separated, and can purify the processing method of main organic pollution aphthenic acids therein.
In order to realize above-mentioned technical purpose, a kind of separation method for the Organic substance in water that gives up the present invention provides electro-desalting should Separation method comprises the following steps：
Step 1：Suspended matter and oil slick in electro-desalting waste water is removed by glass fiber filter；
Step 2：Electro-desalting waste water is set to adsorb electro-desalting waste water by the non-ionic macroporous resin columns of XAD-8 through peristaltic pump In hydrophobic base organic matter and hydrophobic Neutral Organic Compound, water outlet be hydrophobic Acidic organic matter and hydrophilic organics hydrophilicity；
Step 3：Using concentration as the non-ionic macroporous resin columns of XAD-8 after the hydrochloric acid backwash absorption of 0.1mol/L, to wash De- hydrophobic base organic matter, wherein, the volume of hydrochloric acid is 0.5 times -2 times of the volume of the non-ionic macroreticular resins of XAD-8；
Step 4：It is less than or equal to 2 using the pH value of the water outlet of hydrochloric acid (preferred concentration is 6mol/L) regulating step two, makes adjusting The water outlet of step two after pH is non-ionic big by the non-ionic macroporous resin columns of XAD-8 and XAD-4 of series connection through peristaltic pump Hole resin column, water outlet are hydrophilic organics hydrophilicity；
Step 5：Using concentration as the non-ionic macropores of XAD-8 in the sodium hydroxide solution backwash step four of 0.1mol/L Resin column, water outlet are hydrophobic Acidic organic matter, wherein, the volume of sodium hydroxide solution is the non-ionic macroreticular resins of XAD-8 0.5 times -2 times of volume；
Step 6：Using concentration as the non-ionic macropore trees of the XAD-4 in 0.1mol/L sodium hydroxide solutions backwash step four Fat column, water outlet are weak hydrophobic Acidic organic matter, wherein, the body of the non-ionic macroreticular resins of volume XAD-4 of sodium hydroxide solution Long-pending 0.5 times -2 times；
Step 7：Surname extraction is carried out to the non-ionic macroporous resin columns of XAD-8 Jing Guo step 5 backwash with methanol, it is right Obtained extracting solution carries out rotary evaporated to dryness, obtains hydrophobic Neutral Organic Compound solid；
Step 8：The water outlet of step 5 is passed through MSC-H cation exchange resin columns, MSC-H cation exchange resin columns Water outlet be hydrophobic Acidic organic matter；
Step 9：The water outlet of step 8 is mixed with the water outlet of step 6, controls its pH to be less than or equal to 6 with hydrochloric acid solution, Extracted with dichloromethane, be concentrated to dryness under high pure nitrogen stripping, obtain small molecule naphthenic acid solids；
Step 10：Sodium hydroxide solution backwash MSC-H cation exchange resin columns using concentration as 0.1mol/L, backwash liquor It is less than or equal to 2 with salt acid for adjusting pH, is filtered after standing, be freeze-dried, obtain macromolecular naphthenic acid solids, wherein, sodium hydroxide The volume of solution is 2 times of MSC-H cation exchange resins, completes the separation to electro-desalting waste water.
In above-mentioned separation method, it is preferable that the micro-pore diameter of the glass fiber filter used is 0.45 μm.
In above-mentioned separation method, it is preferable that in step 2 and step 4, the flow velocity of peristaltic pump is 1mL/min-2mL/ min；More preferably 1.5mL/min.
In above-mentioned separation method, it is preferable that Step 3: Step 5: in step 6 and step 10, the flow velocity of backwash is 0.1mL/min-0.5mL/min。
In above-mentioned separation method, it is preferable that in step 7, the temperature of surname extraction is 50 DEG C -60 DEG C, time 12h- 24h。
In above-mentioned separation method, it is preferable that in step 7, the temperature of the rotary evaporation of extracting solution is 35 DEG C -40 DEG C.
In above-mentioned separation method, it is preferable that in step 7, the non-ionic macropores of XAD-8 by step 5 backwash Before resin column carries out surname extraction, air at room temperature drying is carried out, wherein, the dry time is 12h-24h；More preferably 15h.
In above-mentioned separation method, it is preferable that in step 9, when dichloromethane extracts, the volume of dichloromethane is to wait to extract Take 0.05 times -0.1 times of the volume of liquid.
In above-mentioned separation method, it is preferable that the XAD-8 filled in the non-ionic macroporous resin columns of XAD-8 is non-ionic The humid volume of macroreticular resin and the volume ratio of electro-desalting waste water are 0.01-0.1：Filled out in 1, XAD-4 non-ionic macroporous resin column The humid volume of the non-ionic macroreticular resins of XAD-4 filled and the volume ratio of electro-desalting waste water are 0.01-0.1：1, MSC-H cation The humid volume for the MSC-H cation exchange resins filled in exchange resin column and the volume ratio of electro-desalting waste water are 0.01-0.05： 1。
In above-mentioned separation method, it is preferable that the non-ionic macroporous resin columns of XAD-8 are by the non-ionic macropores of XAD-8 Resin is filled in glass tube column, and the non-ionic macroporous resin columns of XAD-4 are that the non-ionic macroreticular resins of XAD-4 are filled in glass In glass tubing string, MSC-H cation exchange resin columns be by MSC-H cation exchange resin filling glass tubing strings, wherein, it is described The internal diameter of glass tube column is 3cm-5cm, is highly 30cm-50cm, and water outlet is taper, and sets sand core with glass tube junction Plate, glass tube column 2/3 are highly located to set water outlet.
In above-mentioned separation method, the non-ionic macroreticular resins of XAD-8 of use, the non-ionic macroreticular resins of XAD-4 and MSC-H cation exchange resins carry out purified treatment before use.
The present invention electro-desalting give up Organic substance in water separation method electro-desalting waste water in crude oil can be separated into it is hydrophobic Five kinds of alkaline organic, hydrophobic Neutral Organic Compound, hydrophobic Acidic organic matter, weak hydrophobic Acidic organic matter and hydrophilic organics hydrophilicity groups Point, and wherein main pollutant aphthenic acids is purified.
The give up separation method of Organic substance in water of the electro-desalting of the present invention uses the non-ionic macroreticular resins of XAD-8 and XAD-4, Avoid influence of the high salinity to organic matter separating effect in the electro-desalting waste water of crude oil., can be to electro-desalting after resin separates Each component organic matter in waste water carries out multifrequency nature characterization, and carries out the processing experimental study of different component and aphthenic acids, So as to lay the foundation for the research of electro-desalting wastewater to reach standard efflux technology and application.
The present invention electro-desalting give up Organic substance in water separation method use separator it is easy for installation, it is easy to operate, Systematic error is small, and analysis time is short, and reliability is high.
Brief description of the drawings
Fig. 1 be embodiment 1 in electro-desalting give up Organic substance in water separation method process flow chart.
Embodiment
In order to which technical characteristic, purpose and the beneficial effect of the present invention is more clearly understood, now to the skill of the present invention Art scheme carry out it is described further below, but it is not intended that to the present invention can practical range restriction.
Present embodiments provide a kind of electro-desalting to give up the separation method of Organic substance in water, its technological process is as shown in Figure 1, tool Body comprises the following steps：
Step 1：By micro-pore diameter it is 0.45 μm of glass fiber filter filter and remove suspended substances by 1L electro-desalting waste water After oil slick, through peristaltic pump with the flow velocity of 1.5mL/min by the non-ionic macroporous resin columns of XAD-8, water outlet is hydrophobic acidity And hydrophilic organics hydrophilicity；
Step 2：With the non-ionic macroporous resin columns of 0.1mol/L hydrochloric acid solution backwash XAD-8 of 0.5 times of resin volume, remove Water is hydrophobic base organic matter；
Step 3：It is 2 that the water outlet of step 1 is adjusted pH by 6mol/L hydrochloric acid solutions of concentration, successively with 1.5mL/min's For flow velocity by the XAD-8 resin columns and XAD-4 resin columns of series connection, water outlet is hydrophilic organics hydrophilicity；
Step 4：Sodium hydroxide solution backwash XAD-8 nonionics using the concentration of 1 times of XAD-8 resin volume as 0.1mol/L Type macroporous resin column, outflow component are hydrophobic Acidic organic matter；
Step 5：Sodium hydroxide solution backwash XAD-4 resins using the concentration of 1 times of XAD-4 resin volume as 0.1mol/L Column, collection water outlet are weak hydrophobic Acidic organic matter；
Step 6：Soxhlet is carried out with methanol to the non-ionic macroreticular resins of XAD-8 for being air-dried 15h or so at room temperature to carry Take, obtained extracting solution rotary evaporated to dryness at 40 DEG C, obtains hydrophobic Neutral Organic Compound solid；
Step 7：Hydrophobic Acidic organic matter after separation is through being poured slowly into MSC-H cation exchange resin columns；
Step 8：The outflow component of step 7 is mixed with hydrophobic Acidic organic matter, is equal to 5 with hydrochloric acid solution control pH, is used 5mL Dichloromethane is extracted twice respectively, is concentrated to dryness after mixing under high pure nitrogen stripping, obtains small molecule naphthenic acid solids；
Step 9：With the sodium hydroxide solution backwash MSC-H cation exchange resins of the 0.1mol/L of 2 times of resin volumes, instead Washing lotion is equal to 2 with salt acid for adjusting pH, is filtered after standing, is freeze-dried, obtains macromolecular naphthenic acid solids.
Wherein, the electro-desalting waste water handled by the method for the present embodiment comes from certain Petrochemical Enterprises, and refining feedstock oil is grand celebration Oil and Russia's oil, waste water TOC about 1200mg/L, electrical conductivity about 1400us/cm.
In step 1, the non-ionic macroporous resin columns of used XAD-8 be inside diameter be 3cm, length be 30cm's Glass tube column, away from there is a water outlet at the 10cm of upper end, the humid volume for the non-ionic macroreticular resins of XAD-8 being filled in column is 30mL。
In step 3, the non-ionic macroporous resin columns of used XAD-4 be inside diameter be 3cm, length be 30cm's Glass tube column, away from there is a water outlet at the 10cm of upper end, the humid volume for the non-ionic macroreticular resins of XAD-4 being filled in column is 30mL。
In step 7, used MSC-H cation exchange resin columns are the glass that inside diameter is 3cm, length is 30cm Glass tubing string, away from there is a water outlet at the 10cm of upper end, the humid volume for the MSC-H cation exchange resins being filled in column is 30mL。
Organic matter in electro-desalting waste water can be separated into five kinds of components by the above method provided through this embodiment, point This five kinds of components are not configured to the water sample of 1L (raw water volume), survey its TOC, and calculate the rate of recovery, the results are shown in Table 1.
Table 1
Above example illustrates, the give up separation method of Organic substance in water of electro-desalting of the invention can take off the electricity in crude oil Salt waste water is effectively separated, and can extract major pollutants aphthenic acids therein, and easy to operate, systematic error is small, and point The analysis time is short, and reliability is high.

Claims (10)

  1. The separation method of Organic substance in water 1. a kind of electro-desalting is given up, it is characterised in that the separation method comprises the following steps：
    Step 1：Suspended matter and oil slick in electro-desalting waste water is removed by glass fiber filter；
    Step 2：Electro-desalting waste water is set to be adsorbed by the non-ionic macroporous resin columns of XAD-8 in electro-desalting waste water through peristaltic pump Hydrophobic base organic matter and hydrophobic Neutral Organic Compound, water outlet are hydrophobic Acidic organic matter and hydrophilic organics hydrophilicity；
    Step 3：Using concentration as the non-ionic macroporous resin columns of XAD-8 after the hydrochloric acid backwash absorption of 0.1mol/L, dredged with eluting Alkaline organic matter, wherein, the volume of hydrochloric acid is 0.5 times -2 times of the volume of the non-ionic macroreticular resins of XAD-8；
    Step 4：It is less than or equal to 2 with the pH value of the water outlet of hydrochloric acid regulating step two, the step two after peristaltic pump makes adjusting pH Water outlet has by the non-ionic macroporous resin columns of XAD-8 and the non-ionic macroporous resin columns of XAD-4, water outlet of series connection for hydrophily Machine thing；
    Step 5：Using concentration as the non-ionic macroreticular resins of XAD-8 in the sodium hydroxide solution backwash step four of 0.1mol/L Column, water outlet are hydrophobic Acidic organic matter, wherein, the volume of sodium hydroxide solution is the volume of the non-ionic macroreticular resins of XAD-8 0.5 times -2 times；
    Step 6：Using concentration as the non-ionic macroporous resin columns of XAD-4 in 0.1mol/L sodium hydroxide solutions backwash step four, Water outlet is weak hydrophobic Acidic organic matter, wherein, the volume of the non-ionic macroreticular resins of volume XAD-4 of sodium hydroxide solution 0.5 times -2 times；
    Step 7：Surname extraction is carried out to the non-ionic macroporous resin columns of XAD-8 Jing Guo step 5 backwash with methanol, to obtaining Extracting solution carry out rotary evaporated to dryness, obtain hydrophobic Neutral Organic Compound solid；
    Step 8：The water outlet of step 5 is passed through MSC-H cation exchange resin columns, MSC-H cation exchange resin columns go out Water is hydrophobic Acidic organic matter；
    Step 9：The water outlet of step 8 is mixed with the water outlet of step 6, controls its pH to be less than or equal to 6 with hydrochloric acid solution, with two Chloromethanes extracts, and is concentrated to dryness under high pure nitrogen stripping, obtains small molecule naphthenic acid solids；
    Step 10：Sodium hydroxide solution backwash MSC-H cation exchange resin columns using concentration as 0.1mol/L, backwash liquor is with salt Acid for adjusting pH is less than or equal to 2, is filtered after standing, is freeze-dried, obtains macromolecular naphthenic acid solids, wherein, sodium hydroxide solution Volume be 2 times of MSC-H cation exchange resins, complete the separation to electro-desalting waste water.
  2. 2. separation method according to claim 1, it is characterised in that the micro-pore diameter of the glass fiber filter is 0.45 μm。
  3. 3. separation method according to claim 1, it is characterised in that in step 2 and step 4, the flow velocity of peristaltic pump For 1mL/min-2mL/min；Preferably 1.5mL/min.
  4. 4. separation method according to claim 1, it is characterised in that Step 3: Step 5: step 6 and step 10 In, the flow velocity of backwash is 0.1mL/min-0.5mL/min.
  5. 5. separation method according to claim 1, it is characterised in that in step 7, the temperature of surname extraction is 50 DEG C -60 DEG C, time 12h-24h.
  6. 6. separation method according to claim 1, it is characterised in that in step 7, the temperature of extracting solution rotary evaporation is 35℃-40℃。
  7. 7. separation method according to claim 1, it is characterised in that in step 7, by the XAD-8 of step 5 backwash Before non-ionic macroporous resin column carries out surname extraction, air at room temperature drying is carried out, wherein, the dry time is 12h-24h；It is excellent Elect 15h as.
  8. 8. separation method according to claim 1, it is characterised in that in step 9, when dichloromethane extracts, dichloromethane Volume be 0.05 times -0.1 times of volume of liquid to be extracted.
  9. 9. separation method according to claim 1, it is characterised in that filled in the non-ionic macroporous resin columns of XAD-8 The humid volume of the non-ionic macroreticular resins of XAD-8 and the volume ratio of electro-desalting waste water are 0.01-0.1：1, XAD-4 is non-ionic big The humid volume for the non-ionic macroreticular resins of XAD-4 filled in the resin column of hole and the volume ratio of electro-desalting waste water are 0.01-0.1： The humid volume for the MSC-H cation exchange resins filled in 1, MSC-H cation exchange resin column and the volume of electro-desalting waste water Than for 0.01-0.05：1.
  10. 10. separation method according to claim 1, it is characterised in that the non-ionic macroporous resin columns of XAD-8 are by XAD- 8 non-ionic macroreticular resins are filled in glass tube column, and the non-ionic macroporous resin columns of XAD-4 are that XAD-4 is non-ionic big Hole resin is filled in glass tube column, and MSC-H cation exchange resin columns are by MSC-H cation exchange resin filling glass pipes In column, wherein, the internal diameter of the glass tube column is 3cm-5cm, is highly 30cm-50cm, water outlet is taper, and and glass tube Junction sets sand core plate, and glass tube column 2/3 is highly located to set water outlet.
CN201711056059.2A 2017-11-01 2017-11-01 A kind of electro-desalting is given up the separation method of Organic substance in water Pending CN107935232A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201711056059.2A CN107935232A (en) 2017-11-01 2017-11-01 A kind of electro-desalting is given up the separation method of Organic substance in water

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201711056059.2A CN107935232A (en) 2017-11-01 2017-11-01 A kind of electro-desalting is given up the separation method of Organic substance in water

Publications (1)

Publication Number Publication Date
CN107935232A true CN107935232A (en) 2018-04-20

Family

ID=61933083

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201711056059.2A Pending CN107935232A (en) 2017-11-01 2017-11-01 A kind of electro-desalting is given up the separation method of Organic substance in water

Country Status (1)

Country Link
CN (1) CN107935232A (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111795884A (en) * 2020-06-12 2020-10-20 广东省测试分析研究所（中国广州分析测试中心） Grading separation treatment method for analyzing soluble organic matters in chemical wastewater

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102313658A (en) * 2010-07-07 2012-01-11 中国石油化工股份有限公司 Method for preparing naphthenic acid sample in wastewater
CN102313659A (en) * 2010-07-07 2012-01-11 中国石油化工股份有限公司 Method for separating low-concentration naphthenic acid in wastewater and preparing naphthenic acid sample
CN103012104A (en) * 2011-09-26 2013-04-03 中国石油天然气股份有限公司 Method for recycling butyric acid by treating butanol and octanol waste lye
CN104230079A (en) * 2013-06-19 2014-12-24 中国石油天然气股份有限公司 Method for separating organic matters in reverse osmosis concentrated water

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102313658A (en) * 2010-07-07 2012-01-11 中国石油化工股份有限公司 Method for preparing naphthenic acid sample in wastewater
CN102313659A (en) * 2010-07-07 2012-01-11 中国石油化工股份有限公司 Method for separating low-concentration naphthenic acid in wastewater and preparing naphthenic acid sample
CN103012104A (en) * 2011-09-26 2013-04-03 中国石油天然气股份有限公司 Method for recycling butyric acid by treating butanol and octanol waste lye
CN104230079A (en) * 2013-06-19 2014-12-24 中国石油天然气股份有限公司 Method for separating organic matters in reverse osmosis concentrated water

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111795884A (en) * 2020-06-12 2020-10-20 广东省测试分析研究所（中国广州分析测试中心） Grading separation treatment method for analyzing soluble organic matters in chemical wastewater

Similar Documents

Publication Publication Date Title
CN103771652B (en) A kind of processing method processing acid-containing raw oil waste water
CN102442746B (en) Method for recycling high acid crude oil electric desalting wastewater
CN102311201B (en) Advanced treatment method for high-acid crude oil electric desalting wastewater
CN110282767B (en) Advanced treatment method and system for solid-oil-containing low-concentration heavy metal wastewater
CN103922499B (en) A kind of heavy metal ions in wastewater eddy flow strengthening extraction method and device thereof
CN102949866A (en) Oil removal method for petrochemical emulsified process water
CN112408544A (en) Emulsified wastewater deoiling and purifying device based on special wetting material
CN105236682B (en) Processing method and processing device containing oil-polluted water
CN108467140A (en) A kind of coking wastewater combination desalinating process
CN204281479U (en) A kind for the treatment of system of coating wastewater
CN101525191B (en) Coking wastewater membrane method treating process
CN105621813A (en) System for purifying and treating petrochemical engineering waste water by means of hydrophilic and oleophobic membrane
CN107935232A (en) A kind of electro-desalting is given up the separation method of Organic substance in water
US20130206690A1 (en) Water Treatment Via Ultrafiltration
CN101386790B (en) Ground crude oil dewatering treater
CN103449674B (en) A kind for the treatment of Technology for Petroleum Water Flooding applying granular diatomaceous earth
CN208038181U (en) A kind of oil exploitation produced water treatment injected oil-containing sewage treatment system up to standard
CN114212853B (en) Air floatation tank for demulsification of emulsified oil-containing wastewater, wastewater treatment system comprising air floatation tank and method
CN215756548U (en) Phenol-containing wastewater treatment system
CN104944496A (en) Phenol removing method for sodium sulfate waste water of coal tar processing
CN113277597A (en) Method and device for separating oil-containing wastewater heterojunction microchannel
CN103864240B (en) A kind of ductwork type treating refuse penetrating fluid equipment
CN205275280U (en) Torch unit sewage treatment system
CN104016452A (en) Treatment process of oilfield produced water
CN112174414B (en) Comprehensive treatment device and method for acetone wastewater and organic halide wastewater

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
RJ01 Rejection of invention patent application after publication

Application publication date: 20180420

RJ01 Rejection of invention patent application after publication