CA1182714A - Separation of oil fraction from oil-in-water emulsions - Google Patents
Separation of oil fraction from oil-in-water emulsionsInfo
- Publication number
- CA1182714A CA1182714A CA000426359A CA426359A CA1182714A CA 1182714 A CA1182714 A CA 1182714A CA 000426359 A CA000426359 A CA 000426359A CA 426359 A CA426359 A CA 426359A CA 1182714 A CA1182714 A CA 1182714A
- Authority
- CA
- Canada
- Prior art keywords
- oil
- ppm
- water
- cation
- agitation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
- B01D17/02—Separation of non-miscible liquids
- B01D17/04—Breaking emulsions
- B01D17/047—Breaking emulsions with separation aids
Abstract
Abstract Separation of Oil Fraction from Oil-in-Water Emulsions A method is provided for separating dispersed, fine oil droplets from crude oil produced water which method comprises adding very small amounts of an aluminum or iron cation emulsion breaker to the dispersion followed by agitation of the dispersion by a rotating paddle stirrer at a paddle tip speed of 0.15 to 0.40 meters per second for 10-30 minutes.
The method provides for a substantial reduction over previous methods in the amount of emulsion breaking chemical used and, as well, reduces the amount of oil retained in the water to levels as low as 0.5 ppm.
The method provides for a substantial reduction over previous methods in the amount of emulsion breaking chemical used and, as well, reduces the amount of oil retained in the water to levels as low as 0.5 ppm.
Description
7~
FIELD OF INVENTION
The present invention rela-tes to a process for separa-ting oil from oil-in-wa-ter emulsions by means of chcmical/physical methods. More particularly, the invention relates to -the breaking oE oil-in-water emulsions by the addition of paxticular inorganic salts to the emulsions under conditions of controlled agitation.
BACKGROUND OF THE INVENTION
lG In many areas of the world where crude oil is produced from oil wells, the very high viscosity o:E some crude requires that it be treated to reduce i-ts ~iscosity in order to render it flowable so tha-t it may be recovered from the wells at economic rates. A convenient method commonly employed to improve the Elow rate of heavy crude oil is to inject steam at high pressure into the oil-bearing strata. The steam effectively heats the crude thereby reducing its viscosity and permi.ts recovery of the oil by pumping or by pressure ejection from the well. During the oil heating process, the steam is condensed to water which water is dispersed in the oil in the form of a water-in-o.il emulsion.
~Eter being brought to the surface, the crude oil/water emulsion is allowed to settle in settling tanlcs or basins where the water phase containi~ dispersed, :Eine oil droplets separates from the oil. Thi.s water :Eraction, commonly called produced water, has a portion of crude oil, generally from about 500 ppm or more emulsified with it as an oil-in-water emulsion. In arid regions or the world, it is essential to conserve the water content of produced water for reuse in the generation of Eurther steam.
However, before reuse in steam generation, the oil content of the water must be reduced to acceptable concentrations in order ~o control frothing and to prevent damage to steam generating apparatus. Also, in some jurisdictions, problems may arise with respect to the discharge of untreated produced water onto terrain or into water courses without reduction or removal of the oil
FIELD OF INVENTION
The present invention rela-tes to a process for separa-ting oil from oil-in-wa-ter emulsions by means of chcmical/physical methods. More particularly, the invention relates to -the breaking oE oil-in-water emulsions by the addition of paxticular inorganic salts to the emulsions under conditions of controlled agitation.
BACKGROUND OF THE INVENTION
lG In many areas of the world where crude oil is produced from oil wells, the very high viscosity o:E some crude requires that it be treated to reduce i-ts ~iscosity in order to render it flowable so tha-t it may be recovered from the wells at economic rates. A convenient method commonly employed to improve the Elow rate of heavy crude oil is to inject steam at high pressure into the oil-bearing strata. The steam effectively heats the crude thereby reducing its viscosity and permi.ts recovery of the oil by pumping or by pressure ejection from the well. During the oil heating process, the steam is condensed to water which water is dispersed in the oil in the form of a water-in-o.il emulsion.
~Eter being brought to the surface, the crude oil/water emulsion is allowed to settle in settling tanlcs or basins where the water phase containi~ dispersed, :Eine oil droplets separates from the oil. Thi.s water :Eraction, commonly called produced water, has a portion of crude oil, generally from about 500 ppm or more emulsified with it as an oil-in-water emulsion. In arid regions or the world, it is essential to conserve the water content of produced water for reuse in the generation of Eurther steam.
However, before reuse in steam generation, the oil content of the water must be reduced to acceptable concentrations in order ~o control frothing and to prevent damage to steam generating apparatus. Also, in some jurisdictions, problems may arise with respect to the discharge of untreated produced water onto terrain or into water courses without reduction or removal of the oil
- 2 - C-I-L 657 Eraction. It has been the aim of -the industry -to reduce the oil content of produced wa-ter to 20 ppm or less for reuse in steam generation as well as for environmental considerations.
The nature of the oil-in-water ~produced water) emulsions is such that the dispersed oil droplets are very small in size, tending to range from 1-12 ,um, the greater proportion ranging from 2-7 fum. Generally, oil droplets smaller than about 1 Jum are not visible under microscopic examination and it is believed that many droplets much smaller than 1 ~um are present in produced water. These produced water emulsions demonstrate particular s-tability and the oil droplets show little or no evidence of coalescence even after agi-tation. These near micro-emulsions are, thereEore, generally broken only with difficulty and only after prolonged and sometimes costly treatment procedures.
The processes of -the prior ark, which generally deal wi-th oil/water separation processes in general rather than with produced water emulsions, tend to rely on emulsion breaking or phase separation methods for oil-in-water emulsions which involve a method wherein up to 500 ppm of an emulsion breaker or separator, such as, or example, alum, ferrous sulpha-te or ferric cilloride, is added to each one million parts of emulsion. These emulsion breakers which comprise positively charged cations uncti.on to neutralize -the negative charge normal:Ly carried on the ~urface oE -the dispersed oil droplets thereby causing the droplets to coagulate and agglomerate into globules or flocs.
By subjecting the water/floc mixture to mechanical agitation, many of the flocs can be caused to further agglomerate in-to larger flocs. These larger flocs moving in a random manner through the water phase tend to entrain further droplets of oil and any other particles of insoluble matter present in -the water.
After agitation, the flocs which comprise a coagulant mass, then settle or float in the water phase depending on the density of the mass. After settling, the coagulant and the water can then be separated by means of filtra~on, centrifuge or other common '7~
The nature of the oil-in-water ~produced water) emulsions is such that the dispersed oil droplets are very small in size, tending to range from 1-12 ,um, the greater proportion ranging from 2-7 fum. Generally, oil droplets smaller than about 1 Jum are not visible under microscopic examination and it is believed that many droplets much smaller than 1 ~um are present in produced water. These produced water emulsions demonstrate particular s-tability and the oil droplets show little or no evidence of coalescence even after agi-tation. These near micro-emulsions are, thereEore, generally broken only with difficulty and only after prolonged and sometimes costly treatment procedures.
The processes of -the prior ark, which generally deal wi-th oil/water separation processes in general rather than with produced water emulsions, tend to rely on emulsion breaking or phase separation methods for oil-in-water emulsions which involve a method wherein up to 500 ppm of an emulsion breaker or separator, such as, or example, alum, ferrous sulpha-te or ferric cilloride, is added to each one million parts of emulsion. These emulsion breakers which comprise positively charged cations uncti.on to neutralize -the negative charge normal:Ly carried on the ~urface oE -the dispersed oil droplets thereby causing the droplets to coagulate and agglomerate into globules or flocs.
By subjecting the water/floc mixture to mechanical agitation, many of the flocs can be caused to further agglomerate in-to larger flocs. These larger flocs moving in a random manner through the water phase tend to entrain further droplets of oil and any other particles of insoluble matter present in -the water.
After agitation, the flocs which comprise a coagulant mass, then settle or float in the water phase depending on the density of the mass. After settling, the coagulant and the water can then be separated by means of filtra~on, centrifuge or other common '7~
- 3 ~ C-I-L 657 methods. It has been found, however, -that these prior art methods, in addition to employing large amounts of chemicals at high cost, are not generally applicable to crude oil produced water where the oil phase droplet size is less than 5 ~um and where the oil content is relatively low. Consequently, less costly but less effective physical methods are employed instead.
It has been the commonly held view that, use of a large excess oE
emulsion breaker relative to that re~uired to neutralize the oil droplet surface charge, is essential to achieve flocculation of the oil phase.
SUMMAR~ OF THE INVENTION
It has now been found that the clarification of crucle oil produced water can be measurably improved by a process comprising 15 the ste~ps of: (a) add.irlg to the produced water an optimum quan-tity o:E an emulsion breaker selected from the group of cations A1~, Fe~3 and Fe~~2, (b) subjecting t.he cation-trea-ted produced water to agitation by means of rotating paddles at a paddle tip speed of from 0.15 to 0.~0 m/s, and (c) allowing the treated and agitated mixture to separate by gravity. The rate of separation may be expedited by addin~ to the a~i.tated mixture an arnount of an anionic high molecular weight polymer and agita-ting the mi~-ture for a further period~
The process of the invention can be practised to clar:i.fy ~5 oi].-in-water emulsions having a wide range oE oil con-tent but is more particularly adapted to employment with produced water emulsions having a crude oil content up to 25,000 ppm wherein the oil droplet size is less than about 12 Jum. Practice of the process achieves a reduction of oil in these emulsions typically to less than 3 ppm and as low as 0~5 ppm. The resultant clarified water is sufficiently low in contaminants to alleviate concerns regarding ground disposal and may be employed in the generation of steam without risk of fouling or damage of steam generating apparatus.
The cation employed in the process of the present invention is l.imi.ted to the ~roup AlLr+, Fe+~ and Fe+~~~l~ and us~fully '7~
~ - C-I-L 657 includes any soluble salts comprising -these cations which foxm an insoluble hydroxide in water. Particularly useful because of ready availability and low cost are, for e~ample, commercial alum (A12(SO4)3.xH2O), ferric chloride and ferrous sulphate.
The number o-E molecules of water in the alum may vary from about 10 to 24. The concentration of cation floccuIant employed is from about 0.7 to 10.5 parts per million parts of produced water containing not more than 25,000 ppm of dispersed oil and excellent results are often obtained in the range of 1 to 3 ppm. In the case of A1-~++ ion, the preferred range of concen-tration of flocculan-t is from 1.5 to 2.6 parts per million par-ts of produced water (25,000 ppm max. oil). In the case of Fe~ and Fe~ , the preferred rangeof flocculant is from 2 to 6 parts per million parts produced watsr (25,000 ppm max. oil). The cation Elocculants of the invention are effective at the pH ran~e normally found in crude oil produced water, that is, a pH range from 7 to 8.5. Fe~3 and Fe~2 were found to be effective over a wider pH range than Al-~ , namely from pH 7 to 10. Salt, mainly sodium chloride, which is fre~uently present in crude oil produced water at concentrations of from 0.3 to 1~, has the eEfec-t of slightly increasing the amount of ~]~~ cation required to produce flocculation. The interference of the sodium ion which appears to compete with the ~ cation flocculant for the char~e on the oil droplet may re~uire a doublin~ oE -the amount o ~locculant used.
An optimum level of agitation is critical to the utility of the process of the invention. Agitation of the cation-treated emulsion provides a collision mechanism whereby the individual 3~ c~ispersed oil droplets are caused to come together and join to produce flocs which are easily separable from the a~ueous medium.
However, at unduly high levels of agitation, the flocs are prevented from forming and, hence, remain in suspension or separate only slowly. For optimum flocculation and separation, 3~ it has been found that the turbulence level within the treated r 7~
paddle-agitated emulsion must be controlled to be equivalent to a rotating paddle tip speed of from 0.15 to 0.4 m/s. By "paddle tip speed" is meant the circumferential rate o-f travel of the tip oE a horizontal blade rotated from a centre point thereon. It has been surprisingly found that a level of agitation of a metal cation-treated emulsion at a paddle tip speed less than 0.15 m/s and greater than ~.~ m/s produces a marked increase in the amount of oil retained in the water fraction after separation.
DESCRIPTION OF PREFERRED EMBODIMENT
The process of the invention may be practised batc~wise by introducing crude oil produced water into a tank or vessel equipped with a paddle stirrer. ~ portion of cationic flocculant chemical selected from Al~+, Fe-~+~ or Fe~ in an amount of from 0.7 to 10.5 parts per million parts of emulsion is added to the vessel and the mixture agitated by rotation of the paddle stirrer. The level of agitation is controlled ~y maintaining the speed of rotation of the paddle stirrer at a tip speed of 0.15 to 0.4 m/s. Agitation is continued for a p?riod of from 10 to 20 minutes after which time -the flocculant and water phase àre allowed to settle for 30 minutes. The separa-ted water phase is found to contain from 0.5 to 3 ppm of oil and insoluble solid matter. The settling or separation time may be reduced from 30 minutes to about 5 minutes if a small quantity, up to about 1 ppm and, preferably, about 0.1 ppm, of an anionic hish molecular weight polymer, such as polyacrylamides having various charge densities is added to the produced water after primary agitation. Fur-ther agitation at about half the initial speed for an additional 5 to 10 minutes after polymer addition is required.
The polymer dose chosen, if used, will depend on the speed of separation desired, with larger amounts of polymer generally decreasing the separation time.
The process may also be practised in a substantially continuous manner by employing an elongated vertical vessel or tower equipped with a central rotating shaft having a series of paddles attached thereto. The oily emuIsion and flocculating agent may be passed continuously into the base of the tower where it rises through the agitated zone to a top outlet where it is continuously removed to a separation vessel. The results achieved in such a continuous process are less dramatic than those achieved in a batch process.
E~AMPLE I
-A synthetic oil-in-water produced water emulsion was prepared having an oil content oE 250 ppm and wherein -the oil droplet size was 12 Jum or less. One litre of -the synthetic ~roduced water was placed in a polymethylpentene beak~r and 2.5 ml of ferric chloride solution containg 1 g/l as Fe~
~as added. The resultin~ concentration of Fe~ was 2.5 ppm of the total composition. The emulsion was agitated by means of paddle stirrer at a paddle tip speed of 0.4 m/s for 10 minutes after which time 0.1 ppm of a solution of Betz 1160 polymer was added. Stirring was continued for suc~essive 5 minute periods 20 at paddle tip speeds of 0.25, 0.2 and 0.15 m/s. The treated emulsion was then allowed to stand for 15 minutes durin~ which time tlle oil floc separated. Wa-ter from the separated aqueous phase was clear in appearance and, upon analysis, was found to contain 1 ppm of oil.
EXA~IPLE II
The method of Example 1 was repeated using the same synthetic produced water (250 ppm oil) except tha-t an aluminum potassium sulfate solution was used as the flocculant. The concentration of Al~ was l.S ppm of the total composition.
The emulsion was agitated at a paddle tip speed of 0O4 m/s for 10 minutes after which 0.1 ppm of a solu-tion of Be-tz 1160 polymer was added. Stirring was continued for successive one minute periods at paddle tip speeds of 0.3, 0.25, 0.15 and 0.13 m/s.
The treated emulsion was allowed to stand for 15 minutes while the oil floc separated. The separated water phase was clear in appearance and contained 2.4 ppm of oil and unidentified solids.
- 7 - C~I~L 657 The emulsion breaking method of the invention, while particularly applicable to the treatment of crude oil produced water, is also effective for treatment of a wide range of oily industrial waste waters having finely dispersed oil phases.
It has been the commonly held view that, use of a large excess oE
emulsion breaker relative to that re~uired to neutralize the oil droplet surface charge, is essential to achieve flocculation of the oil phase.
SUMMAR~ OF THE INVENTION
It has now been found that the clarification of crucle oil produced water can be measurably improved by a process comprising 15 the ste~ps of: (a) add.irlg to the produced water an optimum quan-tity o:E an emulsion breaker selected from the group of cations A1~, Fe~3 and Fe~~2, (b) subjecting t.he cation-trea-ted produced water to agitation by means of rotating paddles at a paddle tip speed of from 0.15 to 0.~0 m/s, and (c) allowing the treated and agitated mixture to separate by gravity. The rate of separation may be expedited by addin~ to the a~i.tated mixture an arnount of an anionic high molecular weight polymer and agita-ting the mi~-ture for a further period~
The process of the invention can be practised to clar:i.fy ~5 oi].-in-water emulsions having a wide range oE oil con-tent but is more particularly adapted to employment with produced water emulsions having a crude oil content up to 25,000 ppm wherein the oil droplet size is less than about 12 Jum. Practice of the process achieves a reduction of oil in these emulsions typically to less than 3 ppm and as low as 0~5 ppm. The resultant clarified water is sufficiently low in contaminants to alleviate concerns regarding ground disposal and may be employed in the generation of steam without risk of fouling or damage of steam generating apparatus.
The cation employed in the process of the present invention is l.imi.ted to the ~roup AlLr+, Fe+~ and Fe+~~~l~ and us~fully '7~
~ - C-I-L 657 includes any soluble salts comprising -these cations which foxm an insoluble hydroxide in water. Particularly useful because of ready availability and low cost are, for e~ample, commercial alum (A12(SO4)3.xH2O), ferric chloride and ferrous sulphate.
The number o-E molecules of water in the alum may vary from about 10 to 24. The concentration of cation floccuIant employed is from about 0.7 to 10.5 parts per million parts of produced water containing not more than 25,000 ppm of dispersed oil and excellent results are often obtained in the range of 1 to 3 ppm. In the case of A1-~++ ion, the preferred range of concen-tration of flocculan-t is from 1.5 to 2.6 parts per million par-ts of produced water (25,000 ppm max. oil). In the case of Fe~ and Fe~ , the preferred rangeof flocculant is from 2 to 6 parts per million parts produced watsr (25,000 ppm max. oil). The cation Elocculants of the invention are effective at the pH ran~e normally found in crude oil produced water, that is, a pH range from 7 to 8.5. Fe~3 and Fe~2 were found to be effective over a wider pH range than Al-~ , namely from pH 7 to 10. Salt, mainly sodium chloride, which is fre~uently present in crude oil produced water at concentrations of from 0.3 to 1~, has the eEfec-t of slightly increasing the amount of ~]~~ cation required to produce flocculation. The interference of the sodium ion which appears to compete with the ~ cation flocculant for the char~e on the oil droplet may re~uire a doublin~ oE -the amount o ~locculant used.
An optimum level of agitation is critical to the utility of the process of the invention. Agitation of the cation-treated emulsion provides a collision mechanism whereby the individual 3~ c~ispersed oil droplets are caused to come together and join to produce flocs which are easily separable from the a~ueous medium.
However, at unduly high levels of agitation, the flocs are prevented from forming and, hence, remain in suspension or separate only slowly. For optimum flocculation and separation, 3~ it has been found that the turbulence level within the treated r 7~
paddle-agitated emulsion must be controlled to be equivalent to a rotating paddle tip speed of from 0.15 to 0.4 m/s. By "paddle tip speed" is meant the circumferential rate o-f travel of the tip oE a horizontal blade rotated from a centre point thereon. It has been surprisingly found that a level of agitation of a metal cation-treated emulsion at a paddle tip speed less than 0.15 m/s and greater than ~.~ m/s produces a marked increase in the amount of oil retained in the water fraction after separation.
DESCRIPTION OF PREFERRED EMBODIMENT
The process of the invention may be practised batc~wise by introducing crude oil produced water into a tank or vessel equipped with a paddle stirrer. ~ portion of cationic flocculant chemical selected from Al~+, Fe-~+~ or Fe~ in an amount of from 0.7 to 10.5 parts per million parts of emulsion is added to the vessel and the mixture agitated by rotation of the paddle stirrer. The level of agitation is controlled ~y maintaining the speed of rotation of the paddle stirrer at a tip speed of 0.15 to 0.4 m/s. Agitation is continued for a p?riod of from 10 to 20 minutes after which time -the flocculant and water phase àre allowed to settle for 30 minutes. The separa-ted water phase is found to contain from 0.5 to 3 ppm of oil and insoluble solid matter. The settling or separation time may be reduced from 30 minutes to about 5 minutes if a small quantity, up to about 1 ppm and, preferably, about 0.1 ppm, of an anionic hish molecular weight polymer, such as polyacrylamides having various charge densities is added to the produced water after primary agitation. Fur-ther agitation at about half the initial speed for an additional 5 to 10 minutes after polymer addition is required.
The polymer dose chosen, if used, will depend on the speed of separation desired, with larger amounts of polymer generally decreasing the separation time.
The process may also be practised in a substantially continuous manner by employing an elongated vertical vessel or tower equipped with a central rotating shaft having a series of paddles attached thereto. The oily emuIsion and flocculating agent may be passed continuously into the base of the tower where it rises through the agitated zone to a top outlet where it is continuously removed to a separation vessel. The results achieved in such a continuous process are less dramatic than those achieved in a batch process.
E~AMPLE I
-A synthetic oil-in-water produced water emulsion was prepared having an oil content oE 250 ppm and wherein -the oil droplet size was 12 Jum or less. One litre of -the synthetic ~roduced water was placed in a polymethylpentene beak~r and 2.5 ml of ferric chloride solution containg 1 g/l as Fe~
~as added. The resultin~ concentration of Fe~ was 2.5 ppm of the total composition. The emulsion was agitated by means of paddle stirrer at a paddle tip speed of 0.4 m/s for 10 minutes after which time 0.1 ppm of a solution of Betz 1160 polymer was added. Stirring was continued for suc~essive 5 minute periods 20 at paddle tip speeds of 0.25, 0.2 and 0.15 m/s. The treated emulsion was then allowed to stand for 15 minutes durin~ which time tlle oil floc separated. Wa-ter from the separated aqueous phase was clear in appearance and, upon analysis, was found to contain 1 ppm of oil.
EXA~IPLE II
The method of Example 1 was repeated using the same synthetic produced water (250 ppm oil) except tha-t an aluminum potassium sulfate solution was used as the flocculant. The concentration of Al~ was l.S ppm of the total composition.
The emulsion was agitated at a paddle tip speed of 0O4 m/s for 10 minutes after which 0.1 ppm of a solu-tion of Be-tz 1160 polymer was added. Stirring was continued for successive one minute periods at paddle tip speeds of 0.3, 0.25, 0.15 and 0.13 m/s.
The treated emulsion was allowed to stand for 15 minutes while the oil floc separated. The separated water phase was clear in appearance and contained 2.4 ppm of oil and unidentified solids.
- 7 - C~I~L 657 The emulsion breaking method of the invention, while particularly applicable to the treatment of crude oil produced water, is also effective for treatment of a wide range of oily industrial waste waters having finely dispersed oil phases.
Claims (8)
1. A method of separating oil droplets having a size less than 12 µm from an aqueous dispersion containing up to 25,000 ppm of said oil droplets, which method comprises the steps of adding to the dispersion an emulsion breaker selected from group of cations Al+3, Fe+3 and Fe+2 and mixtures thereof, subjecting the cation-treated dispersion to rotating paddle agitation at a paddle tip speed of from 0.15 to 0.40 meters per second for a period of from 10-30 minutes and allowing the treated and agitated mixture to separate by gravity into an aqueous and an oil layer.
2. A method as claimed in Claim 1 also comprising the step of adding to the treated and agitated mixture up to 1 ppm of an anionic high molecular weight polymer with further agitation prior to the separation step.
3. A method as claimed in Claims 1 and 2 wherein the amount of Al+3 cation added is 1.5 ppm.
4. A method as claimed in Claims 1 and 2 wherein the amount of Fe+2 and Fe+3 cation added is 3 ppm.
5. A method as claimed in Claims 1 and 2 wherein the Al+3 cation is in the form of commercial grade alum (Al2(SO4)3 . xH2O) where x is from 10 to 24.
6. A method as claimed in Claims 1 and 2 wherein the Fe+2 cation is in the form of ferrous sulphate.
7. A method as claimed in Claims 1 and 2 wherein the Fe+3 cation is in the form of ferric chloride.
8. A method as claimed in Claim 2 wherein the anionic high molecular weight polymer is selected from polyacrylamides of various charge densities and mixtures thereof.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000426359A CA1182714A (en) | 1983-04-21 | 1983-04-21 | Separation of oil fraction from oil-in-water emulsions |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000426359A CA1182714A (en) | 1983-04-21 | 1983-04-21 | Separation of oil fraction from oil-in-water emulsions |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1182714A true CA1182714A (en) | 1985-02-19 |
Family
ID=4125067
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000426359A Expired CA1182714A (en) | 1983-04-21 | 1983-04-21 | Separation of oil fraction from oil-in-water emulsions |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA1182714A (en) |
-
1983
- 1983-04-21 CA CA000426359A patent/CA1182714A/en not_active Expired
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