CN105060582A - Oil production wastewater processing and recycling method - Google Patents
Oil production wastewater processing and recycling method Download PDFInfo
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- CN105060582A CN105060582A CN201510553901.8A CN201510553901A CN105060582A CN 105060582 A CN105060582 A CN 105060582A CN 201510553901 A CN201510553901 A CN 201510553901A CN 105060582 A CN105060582 A CN 105060582A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
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- Y02A20/131—Reverse-osmosis
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Abstract
An oil production wastewater processing and recycling method includes the following steps of firstly, removing greasy dirt in preprocessed oil production wastewater through an oil removal process; secondly, adding lime milk and sodium carbonate to generate calcium carbonate and magnesium carbonate through cooperation with coagulant and flocculant, removing calcium carbonate and magnesium carbonate through sediment separation, and eradicating film calcification and preventing film blockage; thirdly, removing particle impurities through a microfiltration or ultrafiltration or nanofiltration membrane filtration after filtering clarification; fourthly, processing recycled reuse water and concentrated solutions through reverse osmosis, forward osmosis, electrodialysis and capacitance adsorption. By means of the method, greasy dirt can be effectively removed, CODcr can be effectively reduced, indexes such as SS and turbidity of the wastewater can be effectively reduced, metal ions in the water are removed, the salt content is lowered, and the oil production wastewater recycling rate can reach 50-65%.
Description
Technical field
The invention belongs to the field for the treatment of of water pollution of environmental engineering, more specifically refer to a kind of oil extraction waste water process and circulation utilization method thereof.
Background technology
Oil field extracted water is the sewage deviate from production treating processes of crude oil mainly.The process of oil field extracted water requires various ways according to discharge or reuse difference, as the feedwater of vapour generator or boiler, strictly will control the ion content of the easy fouling of calcium ion, magnesium ion etc. in water, the oleaginousness etc. in total mineralization, water.Utilize membrane separation technique to carry out desalting treatment to oil field extracted water, make the report producing the aspects such as water reuse recycle many.The principal pollutant index of oil field extracted water after general pre-treatment eliminates most oleaginousness and suspended substance is: calcium ion 200 ~ 3000mg/L, magnesium ion 20 ~ 500mg/L, sodium ion 200 ~ 8000mg/L, chlorion 200 ~ 10000mg/L, oil-containing 30 ~ 300mg/L and COD are 100 ~ 500mg/L.Calcium ion, magnesium ion, bicarbonate ion equal size are still very high.Total hardness is too high, directly adopts membrane separation technique to carry out desalting treatment, easily causes the calcification of film and dirt to block up, the material such as calcium carbonate, magnesiumcarbonate is filled with in the hole of mould material, on the one hand the effluent quality of film is deteriorated, have a strong impact on the steady running of film processing system, the calcification of the opposing party's facial mask can make mould material become fragile, easy fracture of wire, cause the work-ing life of film by common more than 3 years, shorten to less than 1 year, reduce the operation life of film, frequent replacing membrane module, infeasible economically.
Summary of the invention
The invention provides a kind of oil extraction waste water process and circulation utilization method thereof, its main purpose is to overcome the defect that oil field extracted water embrane method treating processes in prior art exists film calcification, dirt is blocked up seriously, cost is high.
The present invention adopts following technical scheme:
A kind of oil extraction waste water process and circulation utilization method thereof, comprise the steps:
(1) oil removing: by calcium ions 200 ~ 3000mg/L, magnesium ion 20 ~ 500mg/L, sodium ion 200 ~ 8000mg/L, chlorion 200 ~ 10000mg/L, oil-containing 30 ~ 300mg/L and COD be the oil extraction waste water of 100 ~ 500mg/L through oil removing process except degreasing, described oil removing process is the one of air supporting, charcoal absorption, adsorption by clay or diatomite adsorption;
(2) hard-off degree: toward calcium ions 200 ~ 3000mg/L, magnesium ion 20 ~ 500mg/L after step (1) oil removing, sodium ion 200 ~ 8000mg/L, chlorion 200 ~ 10000mg/L and COD be feeding lime breast in the oil extraction waste water of 30 ~ 150mg/L, sodium carbonate and coordinate coagulating agent, flocculation agent makes generation calcium carbonate, magnesiumcarbonate precipitate, remove calcium carbonate, magnesiumcarbonate precipitation through precipitate and separate, thus calcium ions and magnesium ions concentration is controlled be less than 80mg/L;
(3) membrane filtration: by the oil extraction waste water after step (2) hard-off degree after filtering clarification, through micro-filtration, ultrafiltration or nanofiltration membrane, removes graininess impurity;
(4) desalination: by the oil extraction waste water of step (3) membrane filtration gained through reverse osmosis, just permeate, reuse water and concentrated solution that electrodialysis, capacitive adsorption process obtain recycle.
Further, the hard-off degree of step (2) also comprises a precipitation of calcium carbonate treatment process, by this operation, calcium carbonate heated oxide is resolved into oxygen calcium.
Further, between the hard-off degree and the membrane filtration of step (3) of step (2), also comprise one and remove the step of COD, this removal COD step is the one of electrolysis, electro-flotation or Fenton's reaction, makes COD density loss in waste water to below 50mg/L by removing COD.
Further, between the hard-off degree and the membrane filtration of step (3) of step (2), also comprise precipitate and separate and filter progress, described precipitate and separate is the one that settling tank precipitation, tube settling or centrifugation are separated; Described sand filtration, multi-medium filtering or the fabric filter element of being filtered into filters, and removing larger particles impurity, ensures membrane filtration effect.
Further, the membrane filtration of above-mentioned steps (3) is micro-filtrate membrane filtration, ultrafiltration membrance filter or MBR; Described microfiltration membrane is the one in organic membrane, metallic membrane or ceramic membrane, and its aperture is between 1 μm-10 μm; Described ultrafiltration is the one in immersion ultrafiltration, pillar ultrafiltration, tubular type ultrafiltration, spiral wound or plate-type hyperfiltration, molecular weight cut-off is 1000 ~ 50000MWCO, working conditions is: normal temperature ~ 45 DEG C, the operating pressure of immersion ultrafiltration is-1 ~-50kPa, and the operating pressure of pillar ultrafiltration, tubular type ultrafiltration, spiral wound and plate-type hyperfiltration is 3 ~ 300kPa; The membrane pore size of described MBR membrane module is 0.10 ~ 0.2 μm, and operating pressure is-1 ~-50kPa, and working temperature is 5 ~ 45 DEG C.
Further, the membrane filtration of above-mentioned steps (3) is nanofiltration membrane, it is the nanofiltration membrane of at least 98% that nanofiltration membrane adopts magnesium sulfate rejection rate, the molecular weight cut-off of nanofiltration membrane is 200MWCO-500MWCO, and entrance pressure is 6bar-45bar, goes out pressure for 4.5bar-43.5bar, and the structure of its membrane module is rolled membrane module or tubular membrane component, working temperature is 20 ~ 45 DEG C, and nanofiltration not only can remove solids precipitation, can also remove the salt of 40 ~ 70%.
Further, the desalination of above-mentioned steps (4) is reverse osmosis desalination, reverse osmosis membrane assembly in reverse osmosis is rolled membrane module, mould material is cellulose acetate film or composite membrane in organic membrane, the molecular weight cut-off of mould material is 50 ~ 200MWCO, entrance pressure is 6.0 ~ 35.0bar, and going out pressure is 4.5 ~ 33.5bar.
Further, the desalination of above-mentioned steps (4) is for just to permeate, and the membrane module just permeated is the one in plate and frame module, rolled membrane module, tubular membrane component and packet mode membrane module.
Further, the desalination of above-mentioned steps (4) is electrodialysis, and electrodialytic working conditions is operating voltage pressure 0.5 ~ 3.0 ㎏/㎝
2, operating voltage 50 ~ 250V, strength of current 1 ~ 3A.
Further, the desalination of above-mentioned steps (4) is capacitive adsorption, and the working conditions of capacitive adsorption is volts DS is 110V ~ 2 × 10
6v.
Further, above-mentioned a kind of oil extraction waste water process and circulation utilization method thereof, also comprise the step reclaiming salt from a concentrated solution, the described step reclaiming salt from concentrated solution concentrated solution is concentrated post crystallization through multiple-effect evaporation be separated to obtain sodium-chlor and distilled water, or entered by concentrated solution in airing pond and be separated to obtain sodium-chlor through spontaneous evaporation or forced evaporation post crystallization.
Effect after above operation process is as following table 1:
The effect of table 1 oil extraction waste water each processing step
Compared to the prior art, tool has the following advantages in the present invention:
1, in oil extraction waste water, oil-contg is higher, the present invention by air supporting can effectively oil removing, reduction CODcr, in addition, the method such as charcoal absorption, adsorption by clay can also be adopted to remove a small amount of oil.
2, in oil extraction waste water, content of calcium and magnesium is high, film calcification and dirt is easily caused to block up, at preprocessing process, by feeding lime breast, sodium carbonate and coordinate coagulating agent, flocculation agent by calcium, magnesium ion remove, and remove a part of sulfate ion, thus the concentration of calcium, magnesium ion is controlled be less than 80mg/L, not only solve film calcification and problem is blocked up in dirt, and reduce waste water infiltration pressure.
3, the waste water after chemical process process, again through membrane filtration, reduces the index such as SS, turbidity of waste water, enters film requirement with what meet reverse osmosis;
4, the oil extraction waste water after membrane filtration process, through desalting treatment, removes the metal ion in water, reduces saltiness.
5, by the inventive method, the rate of recovery to oil extraction waste water 50 ~ 65% is realized.
Accompanying drawing explanation
Fig. 1 is the process flow sheet of the embodiment of the present invention 1.
Fig. 2 is the process flow sheet of the embodiment of the present invention 2.
Fig. 3 is the process flow sheet of the embodiment of the present invention 3.
Fig. 4 is the process flow sheet of the embodiment of the present invention 4.
Embodiment
Referring to figure, the specific embodiment of the present invention is described.
Embodiment 1
A kind of oil extraction waste water process and circulation utilization method thereof, comprise the steps:
1, oil removing
By calcium ions 3000mg/L, magnesium ion 500mg/L, sodium ion 8000mg/L, chlorion 10000mg/L, oil-containing 300mg/L and COD be the oil extraction waste water of 500mg/L through oil removing process except degreasing, wherein, oil removing process is the one of air supporting, charcoal absorption, adsorption by clay or diatomite adsorption.
2, hard-off degree
In the oil extraction waste water after step 1 oil removing feeding lime breast, sodium carbonate and coordinate coagulating agent, flocculation agent makes generation calcium carbonate, magnesiumcarbonate precipitate, remove calcium carbonate, magnesiumcarbonate precipitation through precipitate and separate, thus calcium, magnesium ion concentration are controlled be less than 80mg/L.This hard-off degree also can comprise a precipitation of calcium carbonate treatment process, by this operation, calcium carbonate heated oxide is resolved into oxygen calcium.
3, membrane filtration
By the oil extraction waste water after step 2 hard-off degree after filtering clarification, remove graininess impurity through membrane filtration.Wherein, membrane filtration is the one in micro-filtrate membrane filtration, ultrafiltration membrance filter, MBR or nanofiltration membrane.Microfiltration membrane is the one in organic membrane, metallic membrane or ceramic membrane, and its aperture is between 1 μm-10 μm; Ultrafiltration is the one in immersion ultrafiltration, pillar ultrafiltration, tubular type ultrafiltration, spiral wound or plate-type hyperfiltration, molecular weight cut-off is 1000 ~ 50000MWCO, working conditions is: normal temperature ~ 45 DEG C, the operating pressure of immersion ultrafiltration is-1 ~-50kPa, and the operating pressure of pillar ultrafiltration, tubular type ultrafiltration, spiral wound and plate-type hyperfiltration is 3 ~ 300kPa; The membrane pore size of MBR membrane module is 0.10 ~ 0.2 μm, and operating pressure is-1 ~-50kPa, and working temperature is 5 ~ 45 DEG C; It is the nanofiltration membrane of at least 98% that nanofiltration membrane adopts magnesium sulfate rejection rate, the molecular weight cut-off of nanofiltration membrane is 200MWCO-500MWCO, entrance pressure is 6bar-45bar, go out pressure for 4.5bar-43.5bar, and the structure of its membrane module is rolled membrane module or tubular membrane component, working temperature is 20 ~ 45 DEG C, and nanofiltration not only can remove solids precipitation, can also remove the salt of 40 ~ 70%.
4, desalination
The oil extraction waste water of step 3 membrane filtration gained is obtained reuse water and the concentrated solution of recycle through desalting treatment.Wherein, desalination be reverse osmosis, just permeate, one in electrodialysis or capacitive adsorption.Reverse osmosis membrane assembly in reverse osmosis is rolled membrane module, and mould material is cellulose acetate film or composite membrane in organic membrane, and the molecular weight cut-off of mould material is 50 ~ 200MWCO, and entrance pressure is 6.0 ~ 35.0bar, and going out pressure is 4.5 ~ 33.5bar; The membrane module just permeated is the one in plate and frame module, rolled membrane module, tubular membrane component and packet mode membrane module; Electrodialytic working conditions is operating voltage pressure 0.5 ~ 3.0 ㎏/㎝
2, operating voltage 50 ~ 250V, strength of current 1 ~ 3A; The working conditions of capacitive adsorption is volts DS is 110V ~ 2 × 10
6v.
The effect of table 2 oil extraction waste water each processing step
Embodiment 2
A kind of oil extraction waste water process and circulation utilization method thereof, comprise the steps:
1, oil removing
By calcium ions 200mg/L, magnesium ion 20mg/L, sodium ion 200mg/L, chlorion 200mg/L, oil-containing 30mg/L and COD be the oil extraction waste water of 100mg/L through oil removing process except degreasing, wherein, oil removing process is the one of air supporting, charcoal absorption, adsorption by clay or diatomite adsorption.
2, hard-off degree
In the oil extraction waste water after step 1 oil removing feeding lime breast, sodium carbonate and coordinate coagulating agent, flocculation agent makes generation calcium carbonate, magnesiumcarbonate precipitate, remove calcium carbonate, magnesiumcarbonate precipitation through precipitate and separate, thus calcium ions and magnesium ions concentration is controlled be less than 80mg/L.This hard-off degree also can comprise a precipitation of calcium carbonate treatment process, by this operation, calcium carbonate heated oxide is resolved into oxygen calcium.
3, COD is removed
By the COD density loss that the oil extraction waste water after step 2 hard-off degree makes in waste water through removing COD technique, this removal COD step is the one of electrolysis, electro-flotation or Fenton's reaction, makes COD density loss in waste water to below 50mg/L by removing COD.
4, membrane filtration
Step 3 is removed the oil extraction waste water after COD after filtering clarification, remove graininess impurity through membrane filtration.Wherein, membrane filtration is the one in micro-filtrate membrane filtration, ultrafiltration membrance filter, MBR or nanofiltration membrane.Microfiltration membrane is the one in organic membrane, metallic membrane or ceramic membrane, and its aperture is between 1 μm-10 μm; Ultrafiltration is the one in immersion ultrafiltration, pillar ultrafiltration, tubular type ultrafiltration, spiral wound or plate-type hyperfiltration, molecular weight cut-off is 1000 ~ 50000MWCO, working conditions is: normal temperature ~ 45 DEG C, the operating pressure of immersion ultrafiltration is-1 ~-50kPa, and the operating pressure of pillar ultrafiltration, tubular type ultrafiltration, spiral wound and plate-type hyperfiltration is 3 ~ 300kPa; The membrane pore size of MBR membrane module is 0.10 ~ 0.2 μm, and operating pressure is-1 ~-50kPa, and working temperature is 5 ~ 45 DEG C; It is the nanofiltration membrane of at least 98% that nanofiltration membrane adopts magnesium sulfate rejection rate, the molecular weight cut-off of nanofiltration membrane is 200MWCO-500MWCO, entrance pressure is 6bar-45bar, go out pressure for 4.5bar-43.5bar, and the structure of its membrane module is rolled membrane module or tubular membrane component, working temperature is 20 ~ 45 DEG C, and nanofiltration not only can remove solids precipitation, can also remove the salt of 40 ~ 70%.
5, desalination
The oil extraction waste water of step 4 membrane filtration gained is obtained reuse water and the concentrated solution of recycle through desalting treatment.Wherein, desalination be reverse osmosis, just permeate, one in electrodialysis or capacitive adsorption.Reverse osmosis membrane assembly in reverse osmosis is rolled membrane module, and mould material is cellulose acetate film or composite membrane in organic membrane, and the molecular weight cut-off of mould material is 50 ~ 200MWCO, and entrance pressure is 6.0 ~ 35.0bar, and going out pressure is 4.5 ~ 33.5bar; The membrane module just permeated is the one in plate and frame module, rolled membrane module, tubular membrane component and packet mode membrane module; Electrodialytic working conditions is operating voltage pressure 0.5 ~ 3.0 ㎏/㎝
2, operating voltage 50 ~ 250V, strength of current 1 ~ 3A; The working conditions of capacitive adsorption is volts DS is 110V ~ 2 × 10
6v.
The effect of table 3 oil extraction waste water each processing step
Embodiment 3
A kind of oil extraction waste water process and circulation utilization method thereof, comprise the steps:
1, oil removing
By calcium ions 1500mg/L, magnesium ion 250mg/L, sodium ion 4000mg/L, chlorion 5000mg/L, oil-containing 150mg/L and COD be the oil extraction waste water of 250mg/L through oil removing process except degreasing, wherein, oil removing process is the one of air supporting, charcoal absorption, adsorption by clay or diatomite adsorption.
2, hard-off degree
In the oil extraction waste water after step 1 oil removing feeding lime breast, sodium carbonate and coordinate coagulating agent, flocculation agent makes generation calcium carbonate, magnesiumcarbonate precipitate, remove calcium carbonate, magnesiumcarbonate precipitation through precipitate and separate, thus calcium ions and magnesium ions concentration is controlled be less than 80mg/L.This hard-off degree also can comprise a precipitation of calcium carbonate treatment process, by this operation, calcium carbonate heated oxide is resolved into oxygen calcium.
3, precipitate and separate and filtration
By the oil extraction waste water after step 2 hard-off degree through precipitate and separate and filtration step, removing larger particles impurity, ensures membrane filtration effect.Wherein, precipitate and separate is the one that settling tank precipitation, tube settling or centrifugation are separated; Be filtered into sand filtration, multi-medium filtering or fabric filter element to filter.
4, membrane filtration
By the oil extraction waste water after step 3 precipitate and separate and filtration after filtering clarification, remove graininess impurity through membrane filtration.Wherein, membrane filtration is the one in micro-filtrate membrane filtration, ultrafiltration membrance filter, MBR or nanofiltration membrane.Microfiltration membrane is the one in organic membrane, metallic membrane or ceramic membrane, and its aperture is between 1 μm-10 μm; Ultrafiltration is the one in immersion ultrafiltration, pillar ultrafiltration, tubular type ultrafiltration, spiral wound or plate-type hyperfiltration, molecular weight cut-off is 1000 ~ 50000MWCO, working conditions is: normal temperature ~ 45 DEG C, the operating pressure of immersion ultrafiltration is-1 ~-50kPa, and the operating pressure of pillar ultrafiltration, tubular type ultrafiltration, spiral wound and plate-type hyperfiltration is 3 ~ 300kPa; The membrane pore size of MBR membrane module is 0.10 ~ 0.2 μm, and operating pressure is-1 ~-50kPa, and working temperature is 5 ~ 45 DEG C; It is the nanofiltration membrane of at least 98% that nanofiltration membrane adopts magnesium sulfate rejection rate, the molecular weight cut-off of nanofiltration membrane is 200MWCO-500MWCO, entrance pressure is 6bar-45bar, go out pressure for 4.5bar-43.5bar, and the structure of its membrane module is rolled membrane module or tubular membrane component, working temperature is 20 ~ 45 DEG C, and nanofiltration not only can remove solids precipitation, can also remove the salt of 40 ~ 70%.
5, desalination
The oil extraction waste water of step 4 membrane filtration gained is obtained reuse water and the concentrated solution of recycle through desalting treatment.Wherein, desalination be reverse osmosis, just permeate, one in electrodialysis or capacitive adsorption.Reverse osmosis membrane assembly in reverse osmosis is rolled membrane module, and mould material is cellulose acetate film or composite membrane in organic membrane, and the molecular weight cut-off of mould material is 50 ~ 200MWCO, and entrance pressure is 6.0 ~ 35.0bar, and going out pressure is 4.5 ~ 33.5bar; The membrane module just permeated is the one in plate and frame module, rolled membrane module, tubular membrane component and packet mode membrane module; Electrodialytic working conditions is operating voltage pressure 0.5 ~ 3.0 ㎏/㎝
2, operating voltage 50 ~ 250V, strength of current 1 ~ 3A; The working conditions of capacitive adsorption is volts DS is 110V ~ 2 × 10
6v.
The effect of table 4 oil extraction waste water each processing step
Embodiment 4
1, oil removing
By calcium ions 800mg/L, magnesium ion 80mg/L, sodium ion 800mg/L, chlorion 800mg/L, oil-containing 90mg/L and COD be the oil extraction waste water of 200mg/L through oil removing process except degreasing, wherein, oil removing process is the one of air supporting, charcoal absorption, adsorption by clay or diatomite adsorption.
2, hard-off degree
In the oil extraction waste water after step 1 oil removing feeding lime breast, sodium carbonate and coordinate coagulating agent, flocculation agent makes generation calcium carbonate, magnesiumcarbonate precipitate, remove calcium carbonate, magnesiumcarbonate precipitation through precipitate and separate, thus calcium ions and magnesium ions concentration is controlled be less than 80mg/L.This hard-off degree also comprises a precipitation of calcium carbonate treatment process, by this operation, calcium carbonate heated oxide is resolved into oxygen calcium.
3, COD is removed
By the COD density loss that the oil extraction waste water after step 2 hard-off degree makes in waste water through removing COD technique, this removal COD step is the one of electrolysis, electro-flotation or Fenton's reaction, makes COD density loss in waste water to below 50mg/L by removing COD.
4, precipitate and separate and filtration
Step 3 is removed the oil extraction waste water after COD through precipitate and separate and filtration step, removing larger particles impurity, ensures membrane filtration effect.Wherein, precipitate and separate is the one that settling tank precipitation, tube settling or centrifugation are separated; Be filtered into sand filtration, multi-medium filtering or fabric filter element to filter.
5, membrane filtration
By the oil extraction waste water after step 4 precipitate and separate and filtration after filtering clarification, remove graininess impurity through membrane filtration.Wherein, membrane filtration is the one in micro-filtrate membrane filtration, ultrafiltration membrance filter, MBR or nanofiltration membrane.Microfiltration membrane is the one in organic membrane, metallic membrane or ceramic membrane, and its aperture is between 1 μm-10 μm; Ultrafiltration is the one in immersion ultrafiltration, pillar ultrafiltration, tubular type ultrafiltration, spiral wound or plate-type hyperfiltration, molecular weight cut-off is 1000 ~ 50000MWCO, working conditions is: normal temperature ~ 45 DEG C, the operating pressure of immersion ultrafiltration is-1 ~-50kPa, and the operating pressure of pillar ultrafiltration, tubular type ultrafiltration, spiral wound and plate-type hyperfiltration is 3 ~ 300kPa; The membrane pore size of MBR membrane module is 0.10 ~ 0.2 μm, and operating pressure is-1 ~-50kPa, and working temperature is 5 ~ 45 DEG C; It is the nanofiltration membrane of at least 98% that nanofiltration membrane adopts magnesium sulfate rejection rate, the molecular weight cut-off of nanofiltration membrane is 200MWCO-500MWCO, entrance pressure is 6bar-45bar, go out pressure for 4.5bar-43.5bar, and the structure of its membrane module is rolled membrane module or tubular membrane component, working temperature is 20 ~ 45 DEG C, and nanofiltration not only can remove solids precipitation, can also remove the salt of 40 ~ 70%.
6, desalination
The oil extraction waste water of step 5 membrane filtration gained is obtained reuse water and the concentrated solution of recycle through desalting treatment.Wherein, desalination be reverse osmosis, just permeate, one in electrodialysis or capacitive adsorption.Reverse osmosis membrane assembly in reverse osmosis is rolled membrane module, and mould material is cellulose acetate film or composite membrane in organic membrane, and the molecular weight cut-off of mould material is 50 ~ 200MWCO, and entrance pressure is 6.0 ~ 35.0bar, and going out pressure is 4.5 ~ 33.5bar; The membrane module just permeated is the one in plate and frame module, rolled membrane module, tubular membrane component and packet mode membrane module; Electrodialytic working conditions is operating voltage pressure 0.5 ~ 3.0 ㎏/㎝
2, operating voltage 50 ~ 250V, strength of current 1 ~ 3A; The working conditions of capacitive adsorption is volts DS is 110V ~ 2 × 10
6v.
7, salt is reclaimed
Step 6 desalination is separated the concentrated solution obtained and concentrates post crystallization through multiple-effect evaporation and be separated to obtain sodium-chlor and distilled water, or is entered by concentrated solution in airing pond and be separated to obtain sodium-chlor through spontaneous evaporation or forced evaporation post crystallization.
The effect of table 5 oil extraction waste water each processing step
Above are only the specific embodiment of the present invention, but design concept of the present invention is not limited thereto, all changes utilizing this design the present invention to be carried out to unsubstantiality, all should belong to the behavior of invading scope.
Claims (11)
1. oil extraction waste water process and a circulation utilization method thereof, is characterized in that, comprises the steps:
(1) oil removing: by calcium ions 200 ~ 3000mg/L, magnesium ion 20 ~ 500mg/L, sodium ion 200 ~ 8000mg/L, chlorion 200 ~ 10000mg/L, oil-containing 30 ~ 300mg/L and COD be the oil extraction waste water of 100 ~ 500mg/L through oil removing process except degreasing, described oil removing process is the one in air supporting, charcoal absorption, adsorption by clay or diatomite adsorption;
(2) hard-off degree: in the oil extraction waste water after step (1) oil removing feeding lime breast, sodium carbonate and coordinate coagulating agent, flocculation agent makes generation calcium carbonate, magnesiumcarbonate precipitate, remove calcium carbonate, magnesiumcarbonate precipitation through precipitate and separate, thus calcium, magnesium ion concentration are controlled be less than 80mg/L;
(3) membrane filtration: by the oil extraction waste water after step (2) hard-off degree after filtering clarification, through membrane filtration process, removes graininess impurity;
(4) desalination: by the oil extraction waste water of step (3) membrane filtration gained through reverse osmosis, just permeate, reuse water and concentrated solution that electrodialysis, capacitive adsorption process obtain recycle.
2. a kind of oil extraction waste water process as claimed in claim 1 and circulation utilization method thereof, is characterized in that: described step (2) hard-off degree also comprises a precipitation of calcium carbonate treatment process, by this operation, calcium carbonate heated oxide is resolved into oxygen calcium.
3. a kind of oil extraction waste water process as claimed in claim 1 and circulation utilization method thereof, it is characterized in that: between the hard-off degree and the membrane filtration of step (3) of step (2), also comprise the step that is removed COD, this removal COD step is the one of electrolysis, electro-flotation or Fenton's reaction, makes COD density loss in waste water to below 50mg/L by removing COD.
4. a kind of oil extraction waste water process as claimed in claim 1 and circulation utilization method thereof, it is characterized in that: between the hard-off degree and the membrane filtration of step (3) of step (2), also comprise precipitate and separate and filter progress, described precipitate and separate is the one that settling tank precipitation, tube settling or centrifugation are separated; Described sand filtration, multi-medium filtering or the fabric filter element of being filtered into filters, and removing larger particles impurity, ensures membrane filtration effect.
5. a kind of oil extraction waste water process as claimed in claim 1 and circulation utilization method thereof, it is characterized in that: the membrane filtration of step (3) is the one in micro-filtrate membrane filtration, ultrafiltration membrance filter or MBR, described microfiltration membrane is the one in organic membrane, metallic membrane or ceramic membrane, and its aperture is between 1 μm-10 μm; Described ultrafiltration is the one in immersion ultrafiltration, pillar ultrafiltration, tubular type ultrafiltration, spiral wound or plate-type hyperfiltration, molecular weight cut-off is 1000 ~ 50000MWCO, working conditions is: normal temperature ~ 45 DEG C, the operating pressure of immersion ultrafiltration is-1 ~-50kPa, and the operating pressure of pillar ultrafiltration, tubular type ultrafiltration, spiral wound and plate-type hyperfiltration is 3 ~ 300kPa; The membrane pore size of described MBR membrane module is 0.10 ~ 0.2 μm, and operating pressure is-1 ~-50kPa, and working temperature is 5 ~ 45 DEG C.
6. a kind of oil extraction waste water process as claimed in claim 1 and circulation utilization method thereof, it is characterized in that: the membrane filtration of step (3) is nanofiltration membrane, it is the nanofiltration membrane of at least 98% that nanofiltration membrane adopts magnesium sulfate rejection rate, the molecular weight cut-off of nanofiltration membrane is 200MWCO-500MWCO, entrance pressure is 6bar-45bar, go out pressure for 4.5bar-43.5bar, and the structure of its membrane module is rolled membrane module or tubular membrane component, working temperature is 20 ~ 45 DEG C, nanofiltration not only can remove solids precipitation, can also remove the salt of 40 ~ 70%.
7. a kind of oil extraction waste water process as claimed in claim 1 and circulation utilization method thereof, it is characterized in that: the desalination of step (4) is reverse osmosis desalination, reverse osmosis membrane assembly in reverse osmosis is rolled membrane module, mould material is cellulose acetate film or composite membrane in organic membrane, the molecular weight cut-off of mould material is 50 ~ 200MWCO, entrance pressure is 6.0 ~ 35.0bar, and going out pressure is 4.5 ~ 33.5bar.
8. a kind of oil extraction waste water process as claimed in claim 1 and circulation utilization method thereof, it is characterized in that: the desalination of step (4) is for just to permeate, and the membrane module just permeated is the one in plate and frame module, rolled membrane module, tubular membrane component and packet mode membrane module.
9. a kind of oil extraction waste water process as claimed in claim 1 and circulation utilization method thereof, is characterized in that: the desalination of step (4) is electrodialysis, and electrodialytic working conditions is operating voltage pressure 0.5 ~ 3.0 ㎏/㎝
2, operating voltage 50 ~ 250V, strength of current 1 ~ 3A.
10. a kind of oil extraction waste water process as claimed in claim 1 and circulation utilization method thereof, is characterized in that: the desalination of step (4) is capacitive adsorption, and the working conditions of capacitive adsorption is volts DS is 110V ~ 2 × 10
6v.
11. a kind of oil extraction waste water process as claimed in claim 1 and circulation utilization methods thereof, it is characterized in that: also comprise the step reclaiming salt from a concentrated solution, the described step reclaiming salt from concentrated solution concentrated solution is concentrated post crystallization through multiple-effect evaporation be separated to obtain sodium-chlor and distilled water, or entered by concentrated solution in airing pond and be separated to obtain sodium-chlor through spontaneous evaporation or forced evaporation post crystallization.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510553901.8A CN105060582A (en) | 2015-09-02 | 2015-09-02 | Oil production wastewater processing and recycling method |
| PCT/CN2016/082615 WO2017036182A1 (en) | 2015-09-02 | 2016-05-19 | Oil production wastewater treatment and recycling and reuse method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510553901.8A CN105060582A (en) | 2015-09-02 | 2015-09-02 | Oil production wastewater processing and recycling method |
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| CN109863123A (en) * | 2016-10-26 | 2019-06-07 | 苏特沃克技术有限公司 | The controlled recovered water desalting processing for being used to improve the recovery of hydrocarbons rate |
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| CN115259429A (en) * | 2021-04-30 | 2022-11-01 | 中国石油天然气股份有限公司 | Processing device for flowback liquid |
| CN115259429B (en) * | 2021-04-30 | 2023-12-26 | 中国石油天然气股份有限公司 | Treatment device for flowback fluid |
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