CN1250578C - Method for removing catalyst from unsaturated copolymer hydrogenated solution - Google Patents
Method for removing catalyst from unsaturated copolymer hydrogenated solution Download PDFInfo
- Publication number
- CN1250578C CN1250578C CN 02142519 CN02142519A CN1250578C CN 1250578 C CN1250578 C CN 1250578C CN 02142519 CN02142519 CN 02142519 CN 02142519 A CN02142519 A CN 02142519A CN 1250578 C CN1250578 C CN 1250578C
- Authority
- CN
- China
- Prior art keywords
- aqueous solution
- copolymer
- removal methods
- solution
- extraction agent
- 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 - Fee Related
Links
Landscapes
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
- Catalysts (AREA)
Abstract
The present invention relates to a method for removing a rhodium and (or) ruthenium catalyst from an unsaturated copolymer homogeneous phase hydrogenated solution. The present invention is characterized in that peroxide and an extraction agent aqueous solution react with the unsaturated copolymer hydrogenated solution together; the rhodium and (or) ruthenium catalyst is extracted into the aqueous solution and is separated from the copolymer solution. In a butadiene-acrylonitrile copolymer hydrogenated solution using a rhodium organic complex as a catalyst, a one-step removing rate of rhodium reaches more than 98.8%. In the butadiene-acrylonitrile copolymer hydrogenated solution using a rhodium-ruthenium bimetallic organic complex as the catalyst, the one-step removing rate of the rhodium and ruthenium respectively reach 99.0% and 98.3%. The method is also suitable for removing the organic phosphine of a catalyst ligand and an additional ligand in the unsaturated copolymer hydrogenated solution, wherein the removing rate of a triphenylphosphine ligand reaches more than 99.0%.
Description
Technical field
The invention provides a kind of with superoxide and water-soluble extraction agent with rhodium or/and ruthenium noble metal catalyst and organophosphorus ligand thereof are removed to the method in the extraction agent aqueous solution from the heavy-gravity unsaturated copolymer hydrogenation solution, be particularly useful for rhodium in the perbutan homogeneous hydrogenation solution or/and the removing of ruthenium noble metal catalyst and organophosphorus ligand thereof.
Background technology
For example perbutan is because of carbon-carbon double bonds in the molecular chain (C=C) for unsaturated copolymer, and it is heat-resisting, ageing-resistant, corrosion-resistant etc., and performance is affected, and its Application Areas is restricted.With carbon-carbon double bond, especially the carbon-carbon double bond of nitrile group-containing is keeping having improved again on its original performance basis aging resistance such as heat-resisting, acid resistance fuel oil, anti-hydrogen sulfide, ozone, thereby the over-all properties of hydropolymer is improved after selecting hydrogenation.The process for selective hydrogenation of carbon-carbon double bond in the perbutan mainly is solution homogeneous catalytic hydrogenation and solution heterogeneous catalysis method of hydrotreating so far.Catalyst system therefor mainly is group VIII noble metals (rhodium, ruthenium, palladium an etc.) organic coordination compound catalyzer.They mainly are the hydrogenation catalysts by monometallic or bimetal and one or more organic ligand (as organophosphorus ligand) formation.For example behind the perbutan solution homogeneous hydrogenation, noble metal catalyst remains in the product unsaturated copolymer, and not only color and luster is dark, influence product appearance, and can quicken polymer degradation, aging, and performance there is potential impact, also can increase product cost.Therefore, for improving the quality of products, reducing cost, noble metal catalyst is removed recovery from hydrogenation of polymer solution be very necessary.But the viscosity of unsaturated copolymer homogeneous hydrogenation solution is big, and it is very difficult removing residual homogeneous catalyst from viscous solution.
From unsaturated copolymer, for example removing the reported in literature that separates the homogeneous hydrogenation catalyzer in the perbutan solution has following several: (1) kneader extraction process at present.
USP4,857,635 disclose a kind of kneader reaches the method for using catalyzer in the extraction agent separation removal hydrogenated nitrile-butadiene rubber (HNBR) in this kneader.The deficiency of this method is that a decreasing ratio is low, needs repeated multiple times to mediate extraction, and complex operation, time are long; (2) precipitator method.USP4,413,118 and USP4,944,926 have reported the method that adding precipitation agent (for example, polysaccharide, starch, gac or thiocarbamide) removes rhodium catalyst in the HNBR rubber solutions.Precipitation agent and rhodium catalyst form fine precipitation, after filtration or centrifuging, will precipitate with rubber solutions and separate.The deficiency of this method is that used precipitation dosage is big, and the deposit seeds of generation is fine, and separating difficulty is big from the thickness rubber solutions, and residual precipitation agent has secondary pollution to product; (3) absorption method.USP4,985,540 and USP5,403,566 have reported respectively with the wide aperture ion exchange resin that contains extraordinary functional group, or with organosiloxane copolymer as sorbent material, directly adsorb rhodium-containing in the HNBR rubber solutions or/and the method for ruthenium homogeneous hydrogenation catalyzer.This method can operate continuously, and simple and easy to do, its deficiency is that resistance to mass transfer is big because of rubber solutions viscosity is big, and absorption is slow, and is low to the primary sorption rate of catalyzer, and sorbent material needs special synthetic; (4) methanol wash method.USP3,700,637 propose the HNBR rubber solutions is removed with the methyl alcohol repetitive scrubbing post-treating method of catalyzer, be colourless until methanol wash liquid, the deficiency of this method is that methanol usage is big, complex operation, after HNBR formed micelle, catalyzer was difficult to complete wash-out and comes out.
Chinese invention patent application number 00103779.X (publication number CN1313344A) discloses a kind of method that rhodium, ruthenium noble metal catalyst is removed to the extraction agent aqueous solution from butyronitrile class unsaturated copolymer hydrogenating rubber solutions.It is to add to contain-NH in the HNBR rubber solutions
2Or/and=complexing agent (for example thiobarbituric acid, thiocarbamide etc.) of C=S group, with the carboxylic-acid aqueous solution is extraction agent, rhodium, ruthenium noble metal catalyst in the butyronitrile class unsaturated copolymer homogeneous hydrogenation solution are removed in carboxylic acid extractant's aqueous solution, reach the purpose that removes separate rhodium, ruthenium noble metal catalyst.Its deficiency is that the decreasing ratio of ruthenium noble metal catalyst is high not enough, and the not mentioned situation that removes to organic ligand.
Summary of the invention
Situation in view of catalyst removal prior art in the above unsaturated copolymer hydrogenation solution, the present inventor is on the basis of Chinese invention patent publication number CN1313344A, again through further investigation, find superoxide can be oil-soluble rhodium, ruthenium precious metal organic coordination compound catalyst reaction, the title complex that generates is soluble in the aqueous solution of some extraction agent, this extraction agent is to have water miscible organic acid or organic bases, contain the extraction agent aqueous solution and the easy phase-splitting of rubber solutions that contains multipolymer of catalyzer, reach the purpose that removes separating catalyst.
Specifically, the present invention relates to a kind of with superoxide and the extraction agent aqueous solution together with the homogeneous hydrogenation rubber solutions reaction of unsaturated copolymer homogeneous hydrogenation rubber solutions especially perbutan, the homogeneous catalyst in the heavy-gravity copolymer rubber solution is removed the method that is separated in the extraction agent aqueous solution.The present invention has not only overcome the deficiency of non-aqueous solution removal methods in the prior art, and the reaction and the extraction separation process of superoxide and catalyzer finished simultaneously, contain the aqueous solution and the natural again phase-splitting of rubber solutions that contains multipolymer of catalyzer, simplified technology, catalyst removal rate height.Simultaneously, the unsaturated copolymer especially organophosphorus ligand of catalyzer and second organophosphorus ligand that adds in the perbutan hydrogenation solution have also been removed efficiently.
Therefore, an object of the present invention is to provide a kind of with rhodium and/or ruthenium precious metal organic coordination compound catalyzer from heavy-gravity unsaturated copolymer hydrogenating rubber solutions, particularly be removed to the method in the extraction agent aqueous solution in the perbutan homogeneous hydrogenation rubber solutions efficiently.
Another object of the present invention be above-mentioned with rhodium or/and when the ruthenium noble metal catalyst is removed to the extraction agent aqueous solution from heavy-gravity unsaturated copolymer hydrogenating rubber solutions especially perbutan hydrogenation rubber solutions, catalyst ligand organic phosphine in the unsaturated copolymer hydrogenating rubber solutions especially perbutan hydrogenation rubber solutions and the organophosphorus ligand that adds can be removed in the extraction agent aqueous solution simultaneously efficiently.
A further object of the present invention provide a kind of with above-mentioned rhodium or/and ruthenium noble metal catalyst and part organic phosphine thereof from heavy-gravity unsaturated copolymer homogeneous hydrogenation rubber solutions, particularly are removed to removing and separation processes in the extraction agent aqueous solution efficiently in the perbutan homogeneous hydrogenation rubber solutions.
Of the present inventionly above-mentioned can in further elaboration of the present invention, obtain embodying with other purpose, feature and advantage.
The objective of the invention is to realize by aqueous solution technological line: with the superoxide is oxygenant, the organic acid or the organic bases aqueous solution are extraction agent, the extraction agent aqueous solution and peroxide aqueous solution are added in the unsaturated copolymer hydrogenation solution, particularly in the perbutan hydrorubber solution, under the acting in conjunction of superoxide and extraction agent, rhodium and/or ruthenium noble metal catalyst and organophosphorus ligand thereof are removed in the extraction agent aqueous solution.
The technology of aqueous solution removal methods of the present invention is in two steps: (1) adds the organic acid or the organic bases extraction agent aqueous solution in unsaturated copolymer especially perbutan homogeneous hydrogenation rubber solutions, after adding peroxide aqueous solution again, stir temperature reaction down; (2) by behind the cooling stopped reaction, contain copolymer rubber solution and be divided into two-phase naturally with the extraction agent aqueous solution that contains catalyzer, catalyzer is separated with the hydrogenated copolymer rubber solutions, the hydrogenated copolymer rubber solutions is further being separated out hydrogenated copolymer in the last handling process, the catalyzer recovery of can further concentrating in the extraction agent aqueous solution.
Unsaturated copolymer described in the present invention can be copolymer, comprise butadiene-acrylonitrile (or methacrylonitrile), isoprene-vinyl cyanide (or methacrylonitrile), styrene-butadiene copolymer and polystyrene-poly divinyl-polystyrene (SBS) and polystyrene-poly isoprene-polystyrene (SIS) triblock copolymer, preferred butadiene-acrylonitrile copolymer, styrene butadiene copolymer and polystyrene-poly divinyl-polystyrene triblock copolymer (SBS); Or terpolymer, comprise butadiene-acrylonitrile (or methacrylonitrile)-vinylformic acid (or methacrylic acid), butadiene-acrylonitrile (or methacrylonitrile)-[N-(4-anilino phenyl) Methacrylamide] terpolymer.Typical example is a perbutan (paracril, its acrylonitrile content is 15～50%) hydrorubber solution, the degree of hydrogenation of its hydrogenated nitrile-butadiene rubber (HNBR) is 60～100%, and its degree of hydrogenation measuring method adopts bromine iodine method, or nuclear magnetic resonance method (NMR method).
Homogeneous hydrogenation catalyzer described in the present invention is the group VIII transition metal organic coordination compound, and they are a metal-organic complex homogeneous catalysts that rhodium, ruthenium, palladium precious metal and one or more parts constitute, preferred RhCl (PPh
3)
3, RhH (PPh
3)
4, RuCl
2(PPh
3)
3, Rh
aRu
bCl
n(PPh
3)
m(1≤a in this empirical formula≤4; B=1; 3≤m≤6; 6≤n≤15) etc. the catalyzer that contains Rh and/or Ru.They are to unsaturated copolymer, and especially the hydrogenation to perbutan has high reactivity, highly selective.Their preparation method is well known by persons skilled in the art, can be referring to Chinese invention patent ZL97110896.X embodiment 1-1,1-2 and comparative example 2-1 and U.S. Pat P6,084,033.
Catalyst ligand organic phosphine in the hydrogenated copolymer rubber solutions described in the present invention comprises the part organophosphorus that adds, and this part that adds is to be used to suppress catalyst ligand dissociate and generate the non-activity dimer.Adding organophosphorus ligand can be identical or different with the organophosphorus ligand of catalyzer.Described organophosphorus ligand is general formula PR
1R
2R
3Organic phosphine compound.R in the formula
1, R
2, R
3Can be identical or different, they are C1～C6 alkyl, C6～C12 cycloalkyl, aryl, aryloxy, C7～C12 aralkyl.Triphenylphosphine, triethyl phosphine, tripropyl phosphine, diphenyl-ethyl phosphine, more preferably triphenylphosphine.
Used superoxide is organo-peroxide and the inorganic peroxide with oxidisability among the present invention, comprises Peracetic Acid, hydrogen peroxide, sodium peroxide, ammonium persulphate, Potassium peroxide, preferred hydrogen peroxide, ammonium persulphate, more preferably hydrogen peroxide (H
2O
2).
Extraction agent used among the present invention is for having water miscible organic acid or organic bases.Described organic acid comprises C
1～C
4Straight-chain carboxylic acid's (as formic acid, acetate, propionic acid, butyric acid), C
2～C
4Straight chain hydroxy acid (as oxyacetic acid, lactic acid, butanoic acid).Preferable formic acid and acetate.Described organic bases comprises organic amine and alcohol amine compound, as quadrol, and propylene diamine, ammonium formate, methane amide, ethanamide, Monoethanolamine MEA BASF, diethanolamine and trolamine.Preferred trolamine or acetate, more preferably trolamine.
The concentration of hydrogenated copolymer is to contain 1.0～15.0 gram hydrogenated copolymers in 100 milliliters of solvents in the copolymer hydrogenating rubber solutions described in the present invention.The consumption of hydrogenation catalyst is 0.05～1.0% (mass percent) of the copolymer quality of not hydrogenation; The second part consumption that adds is 2～10 times of catalyst quality.Solvent for use solubilized multipolymer and catalyzer and second part thereof comprise aromatic hydrocarbons and derivative, halogenated alkane, ketone, naphthenic hydrocarbon or acid amides of being replaced by alkyl or halogen and composition thereof, preferred chlorobenzene, dimethylbenzene and composition thereof.
The preparation method and the process of described hydrogenated copolymer rubber solution are well known by persons skilled in the art, can be referring to Chinese invention patent ZL97110896.X and U.S. Pat P6,084,033.
Peroxide aqueous solution concentration described in the present invention is 5～50% (mass concentrations), and the peroxide aqueous solution consumption is 5～50% (volumes) of hydrogenated copolymer solution volume, and peroxide concentrations and adding volume are excessive just not economic; The extraction agent concentration of aqueous solution is 5～80% (mass concentrations), and the extraction agent amount of aqueous solution used is 25～200% (volumes) of hydrogenated copolymer solution volume, and extraction agent concentration of aqueous solution and consumption are excessive also not economic; Removing temperature of reaction is 50～130 ℃, and removing the reaction times is 0.5～4hr; Preferred 70～120 ℃ is 0.5～2.0 hour with removing the reaction times.Superoxide can join temperature reaction again in the copolymer hydrogenation solution simultaneously with extraction agent; Heat up after also can adding extraction agent earlier, add superoxide when reaching temperature of reaction again, superoxide also can add in batches or drip continuously.
Rhodium is or/and the rhodium of ruthenium noble metal catalyst, ruthenium bullion content or concentration atomic absorption spectrophotometer in the extraction agent aqueous solution or in the hydrogenated copolymer rubber solutions, the phosphorus element content of organic phosphine or concentration are by " organic micro quantitative determination analysis " (department of chemistry of Lanzhou University, Shanghai Pharmaceutical Inst., Chinese Academy of Sciences writes, Science Press, 1978) middle colorimetrically analysing.
The decreasing ratio of hydrogenation catalyst in the hydrorubber solution (or organic phosphine) calculates with the percentage that metal (or phosphorus) constituent content reduces:
After removing reaction, the extraction agent aqueous solution and the phase-splitting of hydrorubber solution.Rhodium in the extraction agent aqueous solution, ruthenium precious metal coordination organic compound can be with the method that the is suitable for this area recovery of concentrating, and this is that those skilled in the art can grasp.
Except as otherwise noted, concentration is represented with the total mass number of this material in the unit volume solvent among the application; The consumption of the superoxide and the extraction agent aqueous solution is based on volume; Other consumption, umber or per-cent are all based on quality.
Embodiment
Following embodiment is used to further specify the present invention, rather than is used for limiting the scope of the invention.Following examples are based on the perbutan rubber solutions, but those skilled in the art can understand the rubber solutions that this process is equally applicable to other unsaturated copolymer.
The hydrogenation general step of copolymer rubber solution:
Add concentration in the autoclave and be the dimethylbenzene or the chlorobenzene solution of 7.0% perbutan, the chlorobenzene solution that under temperature of reaction, adds rhodium catalyst/second part triphenylphosphine or butadiene rubber catalyzed by novel Rh-Ru bimetallic agent/second part triphenylphosphine again, and charge into hydrogen and carry out hydrogenation, obtain the following hydrogenated butyronitrile copolymer rubber solution of degree of hydrogenation.Concrete parameter sees Table 1.
Table 1
In the table,
| Sequence number | 1 | 2 | 3 | 4 | 5 | 6 |
| The NBR trade mark 1. | Nancar 1051 | Nancar 1052 | Nancar 1052 | Nancar 1052 | Nancar 1052 | Nancar 6004 |
| The multipolymer solvent | Chlorobenzene | Dimethylbenzene | Dimethylbenzene | Dimethylbenzene | Dimethylbenzene | Dimethylbenzene |
| Catalyzer (Cat.) 2. | Rh-Ru | Rh | Rh-Ru | Rh-Ru | Rh-Ru | Rh-Ru |
| Cat. concentration, % 3. | 0.30 | 0.30 | 0.35 | 0.3 | 0.25 | 0.55 |
| L2/Cat.，wt④ | 6/1 | 66/1 | 6/1 | 6/1 | 6/1 | 6/1 |
| Hydrogen pressure, MPa | 1.2 | 1.4 | 0.8 | 1.2 | 1.4 | 1.2 |
| Temperature of reaction, ℃ | 145 | 130 | 120/150⑥ | 145 | 120/150⑥ | 145 |
| Reaction times, hr | 4.0 | 4.0 | 2.0/2.0⑥ | 4.0 | 2.0/2.0⑥ | 5.0 |
| Degree of hydrogenation, % are 5. | 98.7 | 98.1 | 97.9 | 98.3 | 97.8 | 98.5 |
1. the acrylonitrile content 41% of the NBR trade mark: Nancar1051, the acrylonitrile content 33% of Nancar1052, the acrylonitrile content 19% of Nancar6004.
2. catalyzer: Rh is RhCl (PPh
3)
3, Rh-Ru is empirical formula Rh
aRu
bCl
m(PPh
3)
nCatalyzer, a/b=3/2 in the molecular formula that atomic absorption spectrophotometer records (atomic ratio), m=a+2b wherein, n=3 (a+b).
3. Cat. concentration: be the mass percent of catalyzer and multipolymer.
4. L2/Cat.:L2 is for adding the second part PPh
3Mass ratio with catalyzer.
5. degree of hydrogenation: be (before the hydrogenation and before the poor/hydrogenation of rear copolymer degree of unsaturation multipolymer degree of unsaturation) * 100%.The multipolymer degree of unsaturation is measured with bromine iodine method.
6. 120/150 and 2.0/2.0 be meant earlier and be warmed up to 150 ℃ and reacted again 2.0 hours 120 ℃ of reactions 2.0 hours.
The general step of catalyst removal in the hydrogenated copolymer rubber solutions:
In reactor, add hydrogenated butyronitrile copolymer rubber solution in the known table 1 of catalyst content, and the adding extraction agent aqueous solution, start and stir and intensification, adding peroxide aqueous solution when reaching temperature of reaction reacts, reaction finishes, the cooling layering is with the extraction agent aqueous solution and hydrogenated butyronitrile copolymer rubber solution separating.Hydrogenated butyronitrile copolymer rubber solution becomes very light yellow by deep yellow even near oyster white, the extraction agent aqueous solution is yellow or deep yellow.With hydrogenated butyronitrile copolymer rubber solution precipitating in Virahol, or with steam distillation cohesion, 60 ℃ of dryings obtain hydrogenated butyronitrile multipolymer (HNBR).With metallic element concentration (representing) in the atomic absorption spectrophotometer analytical extraction agent aqueous solution with μ g metal/ml extraction liquid, with phosphoric concentration in the colorimetrically analysing extraction agent aqueous solution (representing) with μ g phosphorus/ml extraction liquid, calculate the decreasing ratio of hydrogenation catalyst in the hydrogenated butyronitrile copolymer rubber solution and the decreasing ratio of part organic phosphine.
Embodiment 1
By the general step of above-mentioned catalyst removal; hydrogenated butyronitrile multipolymer (HNBR) the rubber solutions 20ml that gets table 1 sequence number 2 places reactor; add concentration and be 21.5% trolamine aqueous solution 40ml;; and be warmed up to 80 ℃; add concentration then and be 30% aqueous hydrogen peroxide solution 10ml, stir isothermal reaction 2 hours with about 100-120 rev/min stirring.Reaction finishes the afterreaction mixture through the cooling natural layering, and the extraction agent aqueous solution is separated with the HNBR rubber solutions.Get extraction liquid, analyze the concentration of metal rhodium in the catalyzer wherein, the decreasing ratio that records rhodium catalyst in the HNBR rubber solutions is 98.0%.
The comparative example 1
Repeat embodiment 1, different is not add superoxide, is that 10.6% the trolamine aqueous solution is extraction agent with concentration, adds 40ml, and the decreasing ratio that records rhodium catalyst in the HNBR rubber solutions is 5.9%.
The comparative example 2
Repeat comparative example 1, different is with concentration is that 88.0% aqueous formic acid is an extraction agent, the instead of triethanolamine aqueous solution, and adding 20ml, 110 ℃ of back flow reaction 2 hours, the decreasing ratio that records rhodium catalyst in the HNBR rubber solutions was 6.1%.
Above-mentioned comparative example 1,2 compares with embodiment 1, does not have the reaction of superoxide fellowship in the HNBR rubber solutions, and catalyzer is removed hardly in the HNBR rubber solutions.
The comparative example 3
Repeat embodiment 1, different is not add the extraction agent trolamine aqueous solution, only adds concentration and be 30% hydrogen peroxide 10ml, and 110 ℃ of back flow reaction 1 hour, rubber solutions was because emulsification and phase-splitting is slow.Analyze metal rhodium content in the aqueous solution, the decreasing ratio that records rhodium catalyst in the HNBR rubber solutions is 32.5%.
The comparative example 4
Repeat embodiment 1, different is to add isopyknic deionized water 40ml, substitutes the extraction agent trolamine aqueous solution, also add concentration and be 30% hydrogen peroxide 10ml, in 110 ℃ of back flow reaction 0.5 hour, not phase-splitting of rubber solutions serious emulsification as a result, can't separate rubber solution in catalyzer.
Above-mentioned comparative example 3,4 compares with embodiment 1, shows that catalyst reaction generates water-soluble metal organic coordination compounds in hydrogen peroxide and the rubber solutions, and pure water should not be used as extraction agent.
Embodiment 2-6
Repeat embodiment 1, the HNBR rubber solutions that in reactor, adds table 1 sequence number 2, select different superoxide and extraction agent for use, and consumption, after reaction finishes, the extraction agent aqueous solution and rubber solutions phase-splitting, the metal rhodium concentration of catalyzer in the analytical extraction agent aqueous solution, record rhodium catalyst decreasing ratio in the HNBR rubber solutions, see Table 2.
Table 2
| Embodiment | 2 | 3 | 4 | 5 | 6 |
| The rubber solutions amount, ml | 40 | 40 | 20 | 20 | 20 |
| Extractant concentration, % | 13.2% formic acid | 36.0% acetate | 36.0% acetate | 33.0% acetate | 10.6% trolamine |
| The extraction agent consumption, ml | 40 | 40 | 20 | 20 | 40 |
| Peroxide concentrations % | 30％H 2O 2 | 30％H 2O 2 | The ethanolic soln of 30% Peracetic Acid | 30% ammonium persulphate | 30％H 2O 2 |
| Amount of peroxides, ml | 10ml | 10ml | 7ml | 5.0ml | 5.0ml |
| Temperature of reaction, ℃ | 110 ℃ of backflows | 110 ℃ of backflows | 80℃ | 110 ℃ of backflows | 110 ℃ of backflows |
| Reaction times, hr | 0.5 | 2.0 | 1.0 | 2.0 | 2.0 |
| The rhodium decreasing ratio, % | 32.5 | 73.5 | 25.8 | 44.8 | 98.8 |
The foregoing description 2,3 is compared with embodiment 6, used extraction agent aqueous solution difference, and the decreasing ratio of catalyzer is also different in the HNBR rubber solutions, and the effect of extracting of extraction agent is that the trolamine aqueous solution is better than acetic acid aqueous solution, more is better than aqueous formic acid.
The foregoing description 4,5 compare with embodiment 6, used superoxide is different with the extraction agent system, after their fellowships remove reaction, catalyzer in the rubber solutions all there is removal effect, hydrogen peroxide/trolamine water solution system is better than ammonium persulphate/acetic acid aqueous solution system to the removal effect of rhodium catalyst in the HNBR rubber solutions, more is better than Peracetic Acid/acetic acid aqueous solution system.
Embodiment 7-13
Repeat embodiment 1, in reactor, add the HNBR rubber solutions in the table 1, different is superoxide and consumption difference thereof, or extractant concentration difference, reaction finishes the back extraction agent aqueous solution and rubber solutions phase-splitting, and the rhodium of catalyzer, ruthenium metal concentration in the analytical extraction liquid record rhodium or the rhodium and the ruthenium decreasing ratio of catalyzer in the HNBR rubber solutions, see Table 3,4.
Table 3
| Embodiment | 7 | 8 |
| The HNBR rubber solutions | Sequence number 5 in the table 1 | Sequence number 3 in the table 1 |
| HNBR rubber solutions amount, ml | 20 | 20 |
| Extractant concentration, % | 33% acetate | 33% acetate |
| The extraction agent consumption, ml | 20 | 40 |
| Peroxide concentrations, % | 30% ammonium persulphate | 30% ammonium persulphate |
| Amount of peroxides, ml | 5.0 | 20 |
| Temperature of reaction, ℃ | 110 ℃ of backflows | 110 ℃ of backflows |
| Reaction times, hr | 2.0 | 2.0 |
| The rhodium decreasing ratio, % | 48.3 | 70.9 |
Table 4
| Embodiment | 9 | 10 | 11 | 12 | 13 |
| The HNBR rubber solutions | Sequence number 3 in the table 1 | Sequence number 3 in the table 1 | Sequence number 3 in the table 1 | Sequence number 3 in the table 1 | Sequence number 3 in the table 1 |
| The rubber solutions amount, ml | 20 | 20 | 20 | 20 | 20 |
| Extractant concentration, % | 10.6% trolamine | 10.6% with a left side | 10.6% with a left side | 5.3% with a left side | 21.5% with a left side |
| The extraction agent consumption, ml | 40 | 40 | 40 | 40 | 40 |
| Peroxide concentrations % | 30％H 2O 2 | 30％H 2O 2 | 30％H 2O 2 | 30％H 2O 2 | 30％H 2O 2 |
| Amount of peroxides, ml | 2 | 5 | 10 | 5 | 5 |
| Temperature of reaction, ℃ | 80℃ | 80℃ | 80℃ | 80℃ | 80℃ |
| Reaction times, hr | 1.0 | 1.0 | 1.0 | 1.0 | 1.0 |
| The rhodium decreasing ratio, % | 65.7 | 84.7 | 95.8 | 70.2 | 90.7 |
| The ruthenium decreasing ratio, % | - | 82.4 | 92.9 | - | 90.0 |
Annotate: "-" expression undetermined.
The foregoing description 7 is compared with 8, and 9,10 compare with 11, shows that amount of peroxides increases, and helps removing of catalyzer in the HNBR rubber solutions.
The foregoing description 10,12 is compared with 13, shows that extraction agent trolamine concentration of aqueous solution increases, and helps removing of catalyzer in the HNBR rubber solutions.
Embodiment 14-18
Repeat embodiment 1, the HNBR rubber solutions that adds table 1 in the reactor, with the trolamine aqueous solution is extraction agent, different is the different of temperature of reaction and reaction times, after reaction finishes, the extraction agent aqueous solution and rubber solutions phase-splitting, the rhodium of catalyzer, ruthenium metal concentration in the analytical extraction liquid, record catalyst rhodium in the HNBR rubber solutions, ruthenium decreasing ratio, see Table 5.
Table 5
| Embodiment | 14 | 15 | 16 | 17 | 18 |
| The HNBR rubber solutions | Sequence number 4 | Sequence number 4 | Sequence number 4 | Sequence number 4 | Sequence number 4 |
| The rubber solutions amount, ml | 20 | 20 | 20 | 20 | 20 |
| Extractant concentration, % | 10.6% trolamine | 10.6% with a left side | 10.6% with a left side | 5.3% with a left side | 21.5% with a left side |
| The extraction agent consumption, ml | 40 | 40 | 20 | 20 | 20 |
| Peroxide concentrations % | 30％H 2O 2 | 30％H 2O 2 | 30％H 2O 2 | 30％H 2O 2 | 30％H 2O 2 |
| Amount of peroxides, ml | 5 | 5 | 5 | 5 | 5 |
| Temperature of reaction, ℃ | 40℃ | 110 ℃ of backflows | 110 ℃ of backflows | 110 ℃ of backflows | 110 ℃ of backflows |
| Reaction times, hr | 1.0 | 1.0 | 2.0 | 1.0 | 0.5 |
| The rhodium decreasing ratio, % | 15.6 | 98.0 | 99.0 | 95.0 | 85.0 |
| The ruthenium decreasing ratio, % | - | 97.0 | 98.3 | 91.2 | 83.5 |
Annotate: "-" expression undetermined.
The foregoing description 14,15 is compared with embodiment 10 in the table 4, shows that improving temperature of reaction helps catalyst removal in the HNBR rubber solutions.
The foregoing description 16,17 is compared with 18, shows that prolonging the reaction times helps removing of catalyzer in the HNBR rubber solutions.
Above-mentioned table 2 embodiment 6 compares with table 5 embodiment 16, shows that the increase of extraction agent consumption also helps removing of catalyzer in the HNBR rubber solutions.
Embodiment 19
With the foregoing description 1,11,15,16 remove the reacted extraction agent aqueous solution with the colorimetrically analysing concentration of phosphoric wherein, record in the HNBR rubber solutions catalyst ligand and add total decreasing ratio of part triphenylphosphine all greater than 99.0%.
Above embodiment is exemplary, those skilled in the art can be used for method of the present invention in other unsaturated copolymer (comprising butadiene-styrene copolymer, polystyrene-poly divinyl-polystyrene triblock copolymer etc.) hydrogenation rubber solutions rhodium and/or ruthenium catalyst (comprises RhCl (PPh
3)
3, RhH (PPh
3)
4, RuCl
2(PPh
3)
3, Rh
aRu
bCl
m(PPh
3)
nCatalyzer etc.) and the removing of part organic phosphine, all within the scope of the invention.
Claims (22)
- One kind to be used to remove with rhodium and/or ruthenium organic coordination compound be catalyzer, its part is the method for residual catalyst and part thereof in the unsaturated copolymer homogeneous catalytic hydrogenation solution of organic phosphine, when it is characterized in that in this unsaturated copolymer homogeneous hydrogenation solution, having the superoxide and the water-soluble extraction agent aqueous solution to exist jointly, catalyzer in the hydrorubber solution is removed reaction, and wherein said extraction agent is for having water miscible organic acid or organic bases.
- 2. according to the removal methods of claim 1, it is characterized in that superoxide is organo-peroxide or the inorganic peroxide with oxidisability, is selected from Peracetic Acid, hydrogen peroxide, ammonium persulphate, sodium peroxide or Potassium peroxide.
- 3. according to the removal methods of claim 2, it is characterized in that described superoxide is hydrogen peroxide or ammonium persulphate.
- 4. according to claim 1,2 or 3 removal methods, it is characterized in that described superoxide is a hydrogen peroxide.
- 5. according to the removal methods of claim 1, it is characterized in that water-soluble extraction agent is selected from formic acid, acetate, propionic acid, butyric acid, oxyacetic acid, lactic acid, butanoic acid, quadrol, propylene diamine, ammonium formate, methane amide, ethanamide, Monoethanolamine MEA BASF, diethanolamine or trolamine.
- 6. according to the removal methods of claim 1 or 5, it is characterized in that described water-soluble extraction agent is a trolamine.
- 7. according to the removal methods of claim 1, it is characterized in that the multipolymer in the described unsaturated copolymer homogeneous hydrogenation solution is a copolymer, be selected from butadiene-acrylonitrile, divinyl-methacrylonitrile, isoprene-vinyl cyanide, isoprene-methacrylonitrile, styrene-butadiene copolymer and polystyrene-poly divinyl-polystyrene or polystyrene-poly isoprene-polystyrene triblock copolymer; Or terpolymer, be selected from butadiene-acrylonitrile-vinylformic acid, divinyl-methacrylonitrile-vinylformic acid, butadiene-acrylonitrile-methacrylic acid, divinyl-methacrylonitrile-methacrylic acid, butadiene-acrylonitrile-[N-(4-anilino phenyl) Methacrylamide] or divinyl-methacrylonitrile-[N-(4-anilino phenyl) Methacrylamide] terpolymer.
- 8. according to the removal methods of claim 7, its thing is levied and is that described copolymer is selected from butadiene-acrylonitrile copolymer, styrene butadiene copolymer or polystyrene-poly divinyl-polystyrene triblock copolymer.
- 9. according to claim 1,7 or 8 removal methods, it is characterized in that the concentration of described hydrogenated copolymer in rubber solutions is to contain 1.0～15.0g hydrogenated copolymer in the 100ml solvent.
- 10. according to the removal methods of claim 1, the solvent that it is characterized in that described unsaturated copolymer homogeneous hydrogenation solution is a dimethylbenzene, chlorobenzene, or its mixture.
- 11., it is characterized in that described rhodium and/or ruthenium organic coordination compound catalyzer are RhCl (PPh according to the removal methods of claim 1 3) 3, RhH (PPh 3) 4, RuCl 2(PPh 3) 3, or empirical formula be Rh aRu bCl n(PPh 3) mCatalyzer, 1≤a≤4 wherein; B=1; 3≤m≤6; 6≤n≤15.
- 12., it is characterized in that described catalyst levels is 0.05～1.0% quality of hydrogenation copolymer quality not according to the removal methods of claim 11.
- 13. according to the removal methods of claim 1, it is characterized in that in the described unsaturated copolymer homogeneous hydrogenation solution that catalyst ligand is organophosphorus ligand and adds the part organic phosphine, it adds the part consumption is 2～10 times of catalyst quality.
- 14., it is characterized in that organophosphorus ligand is a compound as follows according to the removal methods of claim 13PR 1R 2R 3R in the formula 1, R 2And R 3Can be identical or different, and be selected from C separately 1-C 6Alkyl, C 6-C 12Cycloalkyl, aryl, aryloxy or C 7-C 12Aralkyl.
- 15., it is characterized in that organophosphorus ligand is selected from triphenylphosphine, triethyl phosphine, tripropyl phosphine or diphenyl-ethyl phosphine according to the removal methods of claim 14.
- 16., it is characterized in that described part is a triphenylphosphine according to the removal methods of claim 15.
- 17. removal methods according to claim 1, it is characterized in that, wherein said peroxide aqueous solution is to add the back temperature reaction simultaneously with the described extraction agent aqueous solution, or add earlier and add described peroxide aqueous solution when being warmed up to temperature of reaction behind the described extraction agent aqueous solution again, and in a kind of mode in back peroxide aqueous solution is added under temperature of reaction in batches, or peroxide aqueous solution is dripped under temperature of reaction continuously.
- 18. according to the removal methods of claim 17, described peroxide aqueous solution adding mode is to add described peroxide aqueous solution when being warmed up to temperature of reaction behind the described extraction agent aqueous solution of elder generation's adding again.
- 19. according to claim 1,17 or 18 removal methods, the mass concentration of described peroxide aqueous solution is 5～50%, its consumption is 5～50% of a hydrogenated copolymer solution volume.
- 20. according to claim 1,17 or 18 removal methods, the mass concentration of the described extraction agent aqueous solution is 5～50%, its consumption is 25～200% of a hydrogenated copolymer solution volume.
- 21. according to claim 1,17 or 18 removal methods, it is characterized in that removing temperature of reaction is 50～130 ℃, the time of removing is 0.5～4.0 hour.
- 22. according to the removal methods of claim 21, it is characterized in that removing temperature of reaction is 70～120 ℃, the time of removing is 0.5～2.0 hour.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02142519 CN1250578C (en) | 2002-09-20 | 2002-09-20 | Method for removing catalyst from unsaturated copolymer hydrogenated solution |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02142519 CN1250578C (en) | 2002-09-20 | 2002-09-20 | Method for removing catalyst from unsaturated copolymer hydrogenated solution |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1483744A CN1483744A (en) | 2004-03-24 |
| CN1250578C true CN1250578C (en) | 2006-04-12 |
Family
ID=34148069
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 02142519 Expired - Fee Related CN1250578C (en) | 2002-09-20 | 2002-09-20 | Method for removing catalyst from unsaturated copolymer hydrogenated solution |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1250578C (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2006070858A1 (en) * | 2004-12-28 | 2006-07-06 | Nippon Soda Co., Ltd. | Method for removing metal and method for producing polymer |
| CN101704926B (en) * | 2009-11-27 | 2011-06-22 | 北京化工大学 | Method for removing noble metal catalyst in hydrogenated copolymer solution |
| TWI653297B (en) * | 2013-12-30 | 2019-03-11 | 艾朗希歐德意志有限公司 | Hydrogenated nitrile rubber containing phosphine oxide or diphosphine oxide (1) |
| TWI653246B (en) * | 2013-12-30 | 2019-03-11 | 艾朗希歐德意志有限公司 | Hydrogenated nitrile rubber containing phosphine oxide or diphosphine oxide (2) |
| CN105985456B (en) * | 2015-02-05 | 2017-11-07 | 中国石油天然气股份有限公司 | Method for removing metal rhodium in hydrogenated nitrile rubber |
| CN108341898B (en) * | 2017-01-24 | 2020-09-15 | 中国石油化工股份有限公司 | Method for removing residual hydrogenation catalyst after unsaturated polymer hydrogenation |
| WO2020020677A1 (en) | 2018-07-23 | 2020-01-30 | Arlanxeo Deutschland Gmbh | Method for producing hydrogenated nitrile rubber and hnbr compositions thereof |
| CN109734828A (en) * | 2018-12-25 | 2019-05-10 | 山东玉皇化工有限公司 | A method of removing unsaturated polymer residure after hydrogenation treatment metallic catalyst |
-
2002
- 2002-09-20 CN CN 02142519 patent/CN1250578C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN1483744A (en) | 2004-03-24 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1250578C (en) | Method for removing catalyst from unsaturated copolymer hydrogenated solution | |
| CN1289515C (en) | Catalyst for asymmetric (transfer) hydrogenation | |
| EP0223151B1 (en) | Process for the selective hydrogenation of unsaturated compounds | |
| CN101037613A (en) | Nickel-based hydrogenation catalyst, and preparation method and application thereof | |
| CN1265094A (en) | Improved hydrocyanation process | |
| CN1636950A (en) | Process for the preparation of TCD-alcohol DM | |
| CN1285344A (en) | Process for preparation of 4-nitrodiphenylamine and 4-nitrosodiphenylamine from carbanilide | |
| CN1487917A (en) | Method for making nitrile compounds from ethylenically unsaturated compounds | |
| CN1120850C (en) | Process for removing hydrocatalyst from unsaturated copolymer | |
| US20110118482A1 (en) | Bidentate chiral ligands for use in catalytic asymmetric addition reactions | |
| CN1262667A (en) | Reduction of carbonyl compounds by silane in presence of zinc catalyst | |
| JP2008534469A (en) | Asymmetrically substituted phospholane catalysts | |
| CN1106374A (en) | Acidification of 1,3-butadiene | |
| CN1926083A (en) | Manufacturing method of optical activity alcohol | |
| CN1763107A (en) | Catalyst removal method from unsaturated copolymer hydrogenation solution | |
| CN101058546A (en) | Method for preparing 3-alkoxypropylamine | |
| CN108329488A (en) | Precious metal catalyst agent method is removed in chelating resin and preprocess method and noble metal removal methods and unsaturated copolymer hydrogenating liquid | |
| CN108329489A (en) | Precious metal catalyst agent method is removed in chelating resin and preprocess method and noble metal removal methods and unsaturated copolymer hydrogenating liquid | |
| CN1706781B (en) | Process for preparing TCD-alcohol DM | |
| CN1008095B (en) | Preparation of chiral rhodium-diphosphine complex | |
| CN1956972A (en) | Process for preparing epichlorohydrin from ethane | |
| CN1142836A (en) | Controlled functional density polyamines and method for preparation thereof | |
| CN1910208A (en) | Method for the hydrogenation of unsaturated polymers containing double bonds | |
| CN1847222A (en) | Temperature controlled ionic liquid two-phase system and its application in complexing catalytic hydrogenation | |
| CN1152035C (en) | Furylphosphines and organometallic complexes contg. them |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20060412 Termination date: 20180920 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |