CN103570862B - A kind of emulsion splitter and its preparation method and application - Google Patents
A kind of emulsion splitter and its preparation method and application Download PDFInfo
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Abstract
The present invention relates to a kind of emulsion splitter and its preparation method and application, preparation method wherein comprises: polyethers and the methyl esters of unsaturated carboxylic acid and/or the ethyl ester of unsaturated carboxylic acid, under the existence of transesterification catalyst and stopper, are carried out transesterification reaction by (1); (2) methyl alcohol and/or ethanol are isolated in underpressure distillation; (3) add unsaturated carboxylic acid, water and free crowd initiator, carry out Raolical polymerizable.Emulsion splitter prepared by the inventive method is applicable to the breaking emulsion and dewatering of viscous crude.
Description
Technical field
The present invention relates to a kind of emulsion splitter and its preparation method and application.
Background technology
Viscous crude is a kind of unconventional petroleum resources, and along with the minimizing day by day of conventional thin oil reserves, the strategy becoming China important is taken over one of energy by viscous crude resource.In China, viscous crude refers to that viscosity is greater than the crude oil of 50mPa.s under reservoir temperature, can be common heavy oil (50 ~ 10000mPa.s), special thick oil (10000 ~ 50000mPa.s), super-viscous oil (more than 50000mPa.s) by viscous crude Further Division according to viscosity.Viscous crude has that density is high, viscosity is large, bituminous matter and the high feature of gum level, if the asphalt content of Tahe Crude Oil is up to 11%.Bituminous matter and colloid are natural water-in-oil emulsifiers, and can form skin shape film in water drops surface absorption, hinder the coalescent of water droplet, thus the breakdown of emulsion of high bituminous matter viscous crude is a puzzlement people's difficult problem always.
Bring into use from the twenties in 20th century and developed three generations's water-in-oil-type emulsion splitter so far.There is first-generation emulsion splitter in 20 ~ thirties of 20th century, mainly low-molecular-weight, anionic type tensio-active agent, comprising carboxylic acid type, sulfuric ester salt form and sulfonate type three major types, the advantage of this kind of emulsion splitter is low price, and shortcoming is consumption large (1000mg/L), efficiency is low, be subject to Influence of Electrolyte etc.; 40 ~ fifties of 20th century has developed s-generation emulsion splitter, mainly low molecule nonionogenic tenside, as OP type, Tween type tensio-active agent, though acidproof, alkaline-resisting, the salt tolerant of this kind of emulsion splitter energy, but emulsion splitter consumption is comparatively large (300 ~ 500mg/L) still, and demulsification is also not ideal enough; The sixties in 20th century has developed third generation emulsion splitter so far, mainly polymer nonionic surface active agent, and as the segmented copolymer of polyoxyethylene and polyoxypropylene, its advantage is consumption few (5 ~ 100mg/L), and shortcoming is that specificity is strong.
Along with the increase of viscous oil recovery amount, its breakdown of emulsion problem is more and more outstanding, impels people constantly to find better effects if, the emulsion splitter that universality is stronger.People find in practice, and molecular weight is high, and the emulsion splitter effect of racemosus wooden fork is better.The method improving emulsion splitter molecular weight mainly contains 3 kinds: (1) adopts new catalyst, as triisobutyl aluminium-methyl ethyl diketone-water or triisobutyl aluminium-methyl ethyl diketone-water-oil of mirbane system (2) use the chainextenders (3) such as tolylene diisocyanate (TDI) to introduce the polymerisable monomers such as vinylformic acid on pfpe molecule, by polymerization, pfpe molecule amount is increased.The third method overcomes first two method catalyzer or chainextender is expensive, poisonous, product dissolves the shortcomings such as difficulty.
The method that patent reports to polyethers introducing polymerisable monomer more both domestic and external, as USP4,678,599 report the introducing allyl polyether of vinyl carbinol and the multipolymer of vinyl acetate or methyl methacrylate.USP5,661,220 report the acrylic acid polyethers of introducing and acrylic acid multipolymer.Domestic also have similar report, as CN1137247.These inventions adopt esterification to be connected with polyethers by unsaturated carboxylic acid polymer, and esterification needs to make water entrainer with toluene, to separate the water of generation, make to react completely, but toluene is poisonous on the one hand, when using toluene on the other hand, the polyether of generation can be separated out.Aqueous solution polymerization is seldom adopted to prepare the method for polyether in prior art, although CN1966138 reports a kind of preparation method of aqueous polymer polyethers, and as viscous crude reverse-phase emulsifier, but its direct polymerization and esterification in aqueous, effect can not be satisfactory.
Summary of the invention
The invention provides a kind of preparation method of emulsion splitter, the emulsion splitter adopting the present invention to prepare not only has good breaking emulsion and dewatering performance to high bituminous matter viscous crude, and has good storage stability.
A preparation method for emulsion splitter, comprising:
(1) under the existence of transesterification catalyst and stopper, polyethers and the methyl esters of unsaturated carboxylic acid and/or the ethyl ester of unsaturated carboxylic acid are carried out transesterification reaction, and described polyethers is-CH
2cH
2o-and-CH
2cH (CH
3) O-form segmented copolymer, it has at least an end group to be hydroxyl, and number-average molecular weight is 500 ~ 30000 ,-CH in polyethers
2cH
2o-and-CH
2cH (CH
3) mass ratio of O-is 0.1 ~ 10:1;
(2) methyl alcohol and/or ethanol are isolated in underpressure distillation;
(3) mix with unsaturated carboxylic acid, water and free crowd initiator, carry out Raolical polymerizable; In the quality of the polyethers raw material of step (1) for 1, the consumption of unsaturated carboxylic acid is 0.01 ~ 1;
In step (1) and (3), described unsaturated carboxylic acid can be identical or different, is all selected from one or more in vinylformic acid, methacrylic acid, maleic anhydride, toxilic acid and fumaric acid.
The temperature of reaction of step (1) is 100 ~ 120 DEG C, preferably 105 ~ 110 DEG C.
The reaction times of step (1) is 1 ~ 24 hour, preferably 2 ~ 6 hours.
Transesterification catalyst comprises basic catalyst, an acidic catalyst, biological enzyme agent etc.In the present invention, described transesterification catalyst is preferably sulfuric acid, phosphoric acid or tosic acid.When transesterification catalyst is tosic acid, consumption its be 0.1% ~ 8% of polyethers raw material and esters of unsaturated carboxylic acids total mass, be preferably 0.4% ~ 1.5%.
In step (1), described stopper is preferably Resorcinol or MEHQ, and consumption is 0.1% ~ 1% of esters of unsaturated carboxylic acids quality, is preferably 0.2% ~ 0.6%.
In step (1), the mass ratio of polyethers and esters of unsaturated carboxylic acids is 1 ~ 200:1, is preferably 10 ~ 130:1
The temperature of reaction of step (3) is 65 ~ 95 DEG C, preferably 80 ~ 90 DEG C.
The reaction times of step (3) is 1 ~ 24 hour, preferably 2 ~ 5 hours.
In the quality of the polyethers raw material of step (1) for 1, in step (3), the consumption of unsaturated carboxylic acid is 0.025 ~ 0.15.
Described radical polymerization initiator comprises azoic compound initiator, peroxide initiator and redox initiator.In step (3), described radical polymerization initiator is preferably persulphate, hydrogen peroxide or water-soluble azo initiator.In step (3), described radical polymerization initiator is more preferably ammonium persulphate, and consumption is 2% ~ 45% of the unsaturated carboxylic acid total mass in polyethers raw material, esters of unsaturated carboxylic acids and the step (3) in step (1), is preferably 10% ~ 20%.
In the quality of the polyethers raw material in step (1) for 1, in step (3), the consumption of water is 0.5 ~ 2, is preferably 0.9 ~ 1.5.
In step (1), the number-average molecular weight of described polyethers is preferably 800 ~ 25000.
In step (1), described polyethers is preferably two blocks, three blocks or Tetrablock copolymer.
In step (1), described polyethers is preferably one or more with alcohol, amine, phenol, carboxylic acid, acid amides, resol, phenol-amine resin or polyethylene polyamine initiator gained polyethers.
In step (1), the preparation method of described polyethers raw material comprises: under the existence of catalyzer and initiator, proceed step by step anionoid polymerization, often walks polymerization and is used alternatingly oxyethane or propylene oxide as polymerization single polymerization monomer.Described being used alternatingly refers to that continuous print two-stage polymerization uses different polymerization single polymerization monomers respectively.
In the preparation method of polyethers, preferably in two steps, three steps or four steps carry out polyreaction, often walk polymerization and are used alternatingly oxidative ethane or propylene oxide as polymerization single polymerization monomer.
Described initiator is preferably by one or more in alcohol, amine, phenol, carboxylic acid, acid amides, resol, phenol-amine resin and polyethylene polyamine.
The general available following catalyst system of oxyethane, propylene oxide is polymerized.The anionoid polymerization of base catalysis, this kind of catalyzer has Na, K, Li, KOH, NaOH, and with the most use in production is KOH and NaOH; The cationoid polymerisation of lewis acid catalysis, this kind of catalyzer has BF
3, AlCl
3deng; Coordinated cationic polymerization, catalyzer is metal oxygen key compound and alkaline earth metal compound etc.The present invention can adopt above-mentioned three class catalyzer, and be preferably alkali catalyst, be more preferably alkali metal hydroxide, more preferably KOH and/or NaOH, its consumption is 0.1 ~ 2% of oxyethane and propylene oxide total mass.
Present invention also offers emulsion splitter prepared by aforesaid method.
A breaking dehydrating method for crude oil, comprising: by crude oil, water filling and above-mentioned emulsion splitter mixing, heat and/or electric field effect under breaking emulsion and dewatering, with the quality of crude oil for benchmark, emulsion splitter consumption is 20 ~ 100ppm, water injection rate is 2 ~ 50% of crude quality.
Emulsion splitter of the present invention can be used for the breaking emulsion and dewatering of hydrocarbon ils, is applicable to the breaking emulsion and dewatering of viscous crude, is specially adapted to the breaking emulsion and dewatering of high bituminous matter viscous crude.Emulsion splitter of the present invention can use in the electric desalting process of crude oil.
Embodiment
Embodiment 1
In autoclave, add 10g methyl alcohol and 1g potassium hydroxide, logical nitrogen deoxygenation, is warming up to 130 DEG C, drip 100g propylene oxide, when reaction pressure no longer reduces, be cooled to 110 DEG C, drip 200 grams of oxyethane, insulation, until pressure no longer reduces, obtains two block polyether D1A.
In autoclave, add 15g nonylphenolic resin (molecular weight is 1090) and 0.9g potassium hydroxide, drip 36.2g propylene oxide, when reaction pressure no longer reduces, then drip 65.8g oxyethane, control temperature of reaction 130 DEG C, pressure 2.3kg/cm
2, treat that reacting ethylene oxide is complete, add 72.5g propylene oxide at this temperature, obtain block polyether D1B.
In autoclave, add 5g tetraethylene pentamine, 2.4g potassium hydroxide and 400g propylene oxide, nitrogen replacement 2 ~ 3 times, is warming up to 115 DEG C, keep temperature until pressure is 0, after continuing to react half an hour, be warming up to 130 DEG C, drip 200g oxyethane, until pressure no longer reduces, obtain block polyether D1C.
Embodiment 2
Once add in there-necked flask, D1A polyethers 100g, tosic acid 0.62g, Resorcinol 0.012g, stirring is warmed up to 105 DEG C, slowly drips methyl methacrylate 5.8g, dropwises, in 105 DEG C of insulation reaction 4h, underpressure distillation removing methyl alcohol, obtains esterification products D2A solution.
In there-necked flask, add above-mentioned D2A esterification products 29.4g, deionized water 20ml, toxilic acid 2.6g, stir and heat up.Ammonium persulphate 4.6g is dissolved in 15ml deionized water, respectively 1.6g vinylformic acid and ammonium persulfate aqueous solution is placed in separating funnel, treat that still liquid is warmed up to 85 DEG C, start to drip vinylformic acid and initiator.Dropwise at 85 ~ 90 DEG C of insulation reaction 3h, obtain polymerisate D3A.
Embodiment 3
Once add in there-necked flask, D1B polyethers 100g, tosic acid 0.9g, Resorcinol 0.0034g, stirring is warmed up to 105 DEG C, slowly drips methyl methacrylate 1.18g, dropwises, in 105 DEG C of insulation reaction 4h, underpressure distillation removing methyl alcohol, obtains esterification products D2B solution.
In there-necked flask, add above-mentioned D2B esterification products 14g, deionized water 10ml, methylene-succinic acid 1.44g, stir and heat up.Ammonium persulphate 2.4g is dissolved in 9ml deionized water, respectively 0.8g vinylformic acid and ammonium persulfate aqueous solution is placed in separating funnel, treat that still liquid is warmed up to 85 DEG C, start to drip vinylformic acid and initiator.Dropwise at 85 ~ 90 DEG C of insulation reaction 3h, obtain polymerisate D3B.
Embodiment 4
Once add in there-necked flask, D1C polyethers 100g, tosic acid 0.5g, Resorcinol 0.0012g, stirring is warmed up to 105 DEG C, slowly drips methyl methacrylate 0.83g, dropwises, in 105 DEG C of insulation reaction 4h, underpressure distillation removing methyl alcohol, obtains esterification products D2C solution.
In there-necked flask, add above-mentioned D2C esterification products 58.6g, deionized water 41ml, acrylamide 1.72g, stir and heat up.Ammonium persulphate 9.0g is dissolved in 28ml deionized water, respectively 1.43g vinylformic acid and ammonium persulfate aqueous solution is placed in separating funnel, treat that still liquid is warmed up to 85 DEG C, start to drip vinylformic acid and initiator.Dropwise at 85 ~ 90 DEG C of insulation reaction 3h, obtain polymerisate D3C.
Comparative example 1
In there-necked flask, once add vinylformic acid 4.2g, D1A polyethers 50g, tosic acid 0.62g, Resorcinol 0.012g, toluene 60ml, loads onto water trap, stirs and is warmed up to 125 ~ 130 DEG C, back flow reaction 8h, obtain esterification products solution.
Get above-mentioned esterification products solution, add vinylformic acid 9.3g, benzoyl peroxide 3.1g, toluene 50ml, at N
2at environment and 85 DEG C, reaction 8h, steams solvent and obtains polymerisate D4.
Comparative example 2
In there-necked flask, once add vinylformic acid 0.85g, D1B polyethers 100g, tosic acid 0.9g, Resorcinol 0.0034g, toluene 173ml, loads onto water trap, back flow reaction 8h, obtains esterification products solution.
Get above-mentioned esterification products solution, add vinylformic acid 4.3g, maleic anhydride 4.3g, benzoyl peroxide 3.0g, at N
2at environment and 85 DEG C, reaction 8h, steams solvent and obtains polymerisate D5.
Embodiment 5
Evaluate the dehydrating effect of emulsion splitter with the outer oil transportation of Tahe, oil property is in table 1.During experiment, emulsion splitter (consumption is 50ppm), water filling and the stock oil that is preheating to 90 ~ 100 DEG C are fully mixed in a mixer, pour in cone-shaped glass desalter, DPY-2 emulsion splitter competition instrument (analytical instrument factory of Jiangsu Jiangyan City) is adopted to carry out oily water separation, electric-force gradient 2000v/cm, temperature 80 DEG C, the water yield that time recording separates.The dehydrating effect of emulsion splitter is in table 2.As can be seen from the table, block polyether is after acrylic acid modified, and with conventional emulsion splitter TA1031 ratio, demulsification is improved to some extent; The acrylic acid modified polyethers that emulsion splitter of the present invention is more simple, demulsification significantly improves.In addition, bad according to the package stability of the demulsifier product of comparative example synthesis, layering after placing, and emulsion splitter D3A, D3B, the D3C in the embodiment of the present invention, excellent storage stability, not stratified after placing.
The outer oil transportation character of table 1 Tahe
| Analyze component | Analytical data |
| 20 DEG C of density, kg/m 3 | 946.9 |
| 80 DEG C of viscosity, mm 2/s | 203.2 |
| 10% carbon residue, % (w) | 15.9 |
| Moisture, % (w) | 0.25 |
| Total acid value, mgKOH/g | 0.14 |
| Stable hydrocarbon, % (w) | 29.8 |
| Aromatic hydrocarbons, % (w) | 26.8 |
| Colloid, %(w) | 28.9 |
| Bituminous matter, % (w) | 14.5 |
The dehydrating effect of table 2 emulsion splitter
TA1031: the ethylene oxide-propylene oxide block copolymer taking phenol-amine resin as initiator gained
The package stability of table 3 synthetic polymer polyethers
| Polyether | Package stability |
| D4 | Layering |
| D5 | Layering |
| D3A | Not stratified |
| D3B | Not stratified |
| D3C | Not stratified |
Note: sintetics is at room temperature placed and observed stability in 1 month.
Claims (27)
1. a preparation method for emulsion splitter, comprising:
(1) under the existence of transesterification catalyst and stopper, polyethers and the methyl esters of unsaturated carboxylic acid and/or the ethyl ester of unsaturated carboxylic acid are carried out transesterification reaction, and described polyethers is-CH
2cH
2o-and-CH
2cH (CH
3) O-form segmented copolymer, it has at least an end group to be hydroxyl, and number-average molecular weight is 500 ~ 30000 ,-CH in polyethers
2cH
2o-and-CH
2cH (CH
3) mass ratio of O-is 0.1 ~ 10:1;
(2) methyl alcohol and/or ethanol are isolated in underpressure distillation;
(3) add unsaturated carboxylic acid, water and radical polymerization initiator, carry out Raolical polymerizable; In the quality of the polyethers raw material of step (1) for 1, the consumption of unsaturated carboxylic acid is 0.01 ~ 1;
In step (1) and (3), described unsaturated carboxylic acid can be identical or different, is all selected from one or more in vinylformic acid, methacrylic acid, maleic anhydride, toxilic acid and fumaric acid.
2. in accordance with the method for claim 1, it is characterized in that, the temperature of reaction of step (1) is 100 ~ 120 DEG C.
3. in accordance with the method for claim 1, it is characterized in that, the reaction times of step (1) is 1 ~ 24 hour.
4. in accordance with the method for claim 1, it is characterized in that, in step (1), described transesterification catalyst is sulfuric acid, phosphoric acid or tosic acid.
5. in accordance with the method for claim 1, it is characterized in that, in step (1), described transesterification catalyst is tosic acid, and consumption is 0.1% ~ 8% of polyethers raw material and esters of unsaturated carboxylic acids total mass.
6. in accordance with the method for claim 5, it is characterized in that, the consumption of described transesterification catalyst is 0.4% ~ 1.5% of polyethers raw material and esters of unsaturated carboxylic acids total mass.
7. in accordance with the method for claim 1, it is characterized in that, in step (1), described stopper is Resorcinol or MEHQ, and consumption is 0.1% ~ 1% of esters of unsaturated carboxylic acids quality.
8. in accordance with the method for claim 7, it is characterized in that, in step (1), the consumption of described stopper is 0.2% ~ 0.6% of esters of unsaturated carboxylic acids quality.
9. in accordance with the method for claim 1, it is characterized in that, in step (1), the mass ratio of polyethers and esters of unsaturated carboxylic acids is 1 ~ 200:1.
10. in accordance with the method for claim 9, it is characterized in that, in step (1), the mass ratio of polyethers and esters of unsaturated carboxylic acids is 10 ~ 130:1.
11. in accordance with the method for claim 1, it is characterized in that, the temperature of reaction of step (3) is 65 ~ 95 DEG C.
12. in accordance with the method for claim 1, it is characterized in that, the reaction times of step (3) is 1 ~ 24 hour.
13. in accordance with the method for claim 1, it is characterized in that, in the quality of the polyethers raw material in step (1) for 1, in step (3), the consumption of unsaturated carboxylic acid is 0.025 ~ 0.15.
14. in accordance with the method for claim 1, it is characterized in that, in step (3), described radical polymerization initiator is persulphate, hydrogen peroxide or water-soluble azo initiator.
15. according to the method for claim 14, it is characterized in that, in step (3), described radical polymerization initiator is ammonium persulphate, and consumption is 2% ~ 45% of the unsaturated carboxylic acid total mass in polyethers raw material, esters of unsaturated carboxylic acids and the step (3) in step (1).
16., according to the method for claim 15, is characterized in that, the consumption of described ammonium persulphate is 10% ~ 20% of the unsaturated carboxylic acid total mass in polyethers raw material, esters of unsaturated carboxylic acids and the step (3) in step (1).
17. in accordance with the method for claim 1, it is characterized in that, in the quality of the polyethers raw material of step (1) for 1, in step (3), the consumption of water is 0.5 ~ 2.
18. in accordance with the method for claim 17, it is characterized in that, in the quality of the polyethers raw material of step (1) for 1, in step (3), the consumption of water is 0.9 ~ 1.5.
19. in accordance with the method for claim 1, it is characterized in that, the number-average molecular weight of described polyethers is 800 ~ 25000.
20. in accordance with the method for claim 1, it is characterized in that, described polyethers is two blocks, three blocks or Tetrablock copolymer.
21. in accordance with the method for claim 1, it is characterized in that, described polyethers is be one or more of initiator gained polyethers with alcohol, amine, phenol, carboxylic acid, acid amides, resol, phenol-amine resin or polyethylene polyamine.
22. in accordance with the method for claim 1, it is characterized in that, in step (1), the preparation method of described polyethers raw material comprises: under the existence of catalyzer and initiator, proceed step by step anionoid polymerization, often walks polymerization and is used alternatingly oxyethane or propylene oxide as polymerization single polymerization monomer.
23. in accordance with the method for claim 22, it is characterized in that, in the preparation method of the polyethers described in step (1), in two steps, three steps or four steps carry out polyreaction.
24. in accordance with the method for claim 22, it is characterized in that, in the preparation method of described polyethers, described catalyzer is KOH and/or NaOH, and its consumption is 0.1 ~ 2% of oxyethane and propylene oxide total mass.
25. in accordance with the method for claim 22, it is characterized in that, in the preparation method of described polyethers, described initiator is one or more in alcohol, amine, phenol, carboxylic acid, acid amides, resol, phenol-amine resin and polyethylene polyamine.
26. emulsion splitters obtained according to either method in claim 1 ~ 25.
The breaking dehydrating method of 27. 1 kinds of crude oil, comprise: by the emulsion splitter mixing described in crude oil, water filling and claim 26, heat and/or electric field effect under breaking emulsion and dewatering, with the quality of crude oil for benchmark, emulsion splitter consumption is 20 ~ 100ppm, water injection rate is 2 ~ 50% of crude quality.
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