CN1986055B - Catalyst system and catalyzing method of propylene hydrogenation and formylation - Google Patents
Catalyst system and catalyzing method of propylene hydrogenation and formylation Download PDFInfo
- Publication number
- CN1986055B CN1986055B CN2006101477352A CN200610147735A CN1986055B CN 1986055 B CN1986055 B CN 1986055B CN 2006101477352 A CN2006101477352 A CN 2006101477352A CN 200610147735 A CN200610147735 A CN 200610147735A CN 1986055 B CN1986055 B CN 1986055B
- Authority
- CN
- China
- Prior art keywords
- reaction
- catalyst
- rhodium
- hydroformylation
- propylene
- 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.)
- Active
Links
- 0 CC(C)(C)c(cc1-c(cc(C(C)(C)*)cc2C(C)(C)C)c2O)cc(C(C)(C)C)c1O Chemical compound CC(C)(C)c(cc1-c(cc(C(C)(C)*)cc2C(C)(C)C)c2O)cc(C(C)(C)C)c1O 0.000 description 2
- CBYWHFTZNVZQHV-UHFFFAOYSA-N CC(C)(C)c1cc(OC)cc(-c(cc(cc2C(C)(C)C)OC)c2O)c1O Chemical compound CC(C)(C)c1cc(OC)cc(-c(cc(cc2C(C)(C)C)OC)c2O)c1O CBYWHFTZNVZQHV-UHFFFAOYSA-N 0.000 description 2
- ANCSPRJFGGDREM-UHFFFAOYSA-N COc1cccc2c1cccc2OC Chemical compound COc1cccc2c1cccc2OC ANCSPRJFGGDREM-UHFFFAOYSA-N 0.000 description 1
- PPTXVXKCQZKFBN-UHFFFAOYSA-N Oc1ccc(cccc2)c2c1-c(c1ccccc1cc1)c1O Chemical compound Oc1ccc(cccc2)c2c1-c(c1ccccc1cc1)c1O PPTXVXKCQZKFBN-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/582—Recycling of unreacted starting or intermediate materials
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The present invention relates to catalyst system for propylene hydrogenation and formylation and process of catalytically synthesizing butyl aldehyde. The catalyst system is triaryl phosphine-Rh(I) catalyst system with proper additive, such as bisphosphite ester, in proper amount. Compared with similar available catalyst, the catalyst system has obviously higher catalytic acitivity, higher selectivity, higher stability and raised n-butyl aldehyde/isobutyl aldehyde ratio in the catalytically synthesized product.
Description
Technical field
The present invention uses the novel catalyst system of rhodium salt, triaryl phosphine and bis-phosphite additive preparation hydroformylation of propene, and is used for the method for the synthetic butyraldehyde of propylene catalysis hydroformylation.The present invention is in the propene hydroformylation reaction system of triaryl phosphine-Rh (I) catalysis; Through using the diphosphite ester additive; Like bis-phosphite; It is just different from (mol ratio of hutanal/isobutylaldehyde＞20) that discovery can obviously improve in Rh (I)/triaryl phosphine activity of such catalysts and the product butyraldehyde, and the service life of significant prolongation bisphosphite ligands, obviously reduces the consumption of triaryl phosphine.The characteristics of this type catalyst system are higher than third generation Rh (I)/triphenylphosphine activity of such catalysts and selectivity; Stability than the 4th generation Rh (I)/diphosphite ester catalyst is better; Therefore; Novel catalyst system provided by the invention can overcome the 3rd, the 4th generation catalyst shortcoming, reduce the cost of hydroformylation of propene suitability for industrialized production, for its commercial Application provides new catalyst technology.
Background technology
Hydroformylation of olefin can be converted into basic chemical raw materials cheap and easy to get such as propylene etc. multiple important chemical products such as butyraldehyde easily and effectively, is the maximum homogeneous catalysis process of production scale up to now.[Trzeciak，A.M.；Ziólkowski，J.J.Coord.Chem.Rev.1999，190-192，883-900.]。In many decades, the process of several updates has been experienced in the development of catalyst, up to now, has developed four types industrializeding catalyst altogether, i.e. cobalt carbonyl catalyst CoH (CO)
4, the cobalt carbonyl catalyst CoH (CO) that modifies of tertiary phosphine
3(RM-17), rhodium carbonyl phosphine catalyst RhH (CO) (PPh
3)
3, and biphosphinate/rhodium catalytic system of developing at present, they are as shown in table 1 in the operating condition and the performance of hydroformylation of olefin process.Can find out that each catalyst is compared with previous generation, reaction condition is gentle more, and reactive metal consumption, pressure and reaction temperature all are tending towards reducing, and on energy consumption, activity and/or selectivity, or aspect the recovery of noble metal catalyst, significant improvement have been arranged all.But on the catalyst metal components, remain cobalt and rhodium.Though expensive 3500 times than cobalt of rhodiums, the catalytic activity of rhodium agent exceeds 10 than cobalt
2～10
3One magnitude can under the situation of energy shortage and producing cost rising, can be catered to the needs of commercial production development effectively in reaction condition (low pressure and the lower temperature) operation down of milder.In addition, the rhodium series catalysts that tertiary phosphine is modified can significantly increase the selectivity of system to the high n-alkanal of commercial value, and the catalyst concn that uses in the reactant liquor is lower, and these all make high catalyst price pay to a certain extent and obtain compensation.Therefore, the catalytic process of rhodium-containing system has become the main use object of hydroformylation reaction since last century the seventies.Recently there is the people that the various transition metal of catalysis hydroformylation reaction are contrasted, finds that the activity without the rhodium catalyst of modifying will be higher than other single metallic catalyst far away.Therefore, can estimate that using various ligand modified rhodium-containing systems will be the dominant direction in the olefin hydroformylation research from now on.
The operating condition and the performance of table 1 propylene hydrocarbon hydroformylation reaction process
| Catalytic reaction condition | Catalyst | |||
| [CoH(CO) 4] | [CoH(CO) 3- (RM-17)] | [RhH(CO)- (PPh 3) 3] | Two-phosphinate Rh (acac) is (CO) 2 | |
| The industrialization time T, ℃ P (stagnation pressure), MPa reactive metal concentration (M/C ＝), % just/different aldehyde, % alcohol, % alkane, % other | 1946 110～180 20～35 0.1～1.0 ?80/20 80 10 1 9 | 1964 160～200 5～10 0.5～1.0 ?88/12 10 80 5 5 | 1976 85～115 1.5～2.0 10 -2～10 -3 ?92/8 96 -- 2 2 | -- 60-90 1～2 10 -3～10 -4 ?30-80 ＞96 -- -- -- |
In the industry, the hydroformylation reaction of alkene mainly comes catalysis to realize by the various co-ordination complexs of Co, two kinds of metals of Rh.But since last century the seventies; The rhodium catalyst that the phosphine part is modified has just been dominated the hydroformylation reaction research of alkene, and has progressively been replaced the catalyst that cobalt becomes the industrial hydroformylation technical process with its high activity, outstanding selectivity and gentle outstanding advantages such as reaction condition.Wherein, the composition of phosphine part and structure are the key factors of phosphine/rhodium catalyst system and catalyzing reaction efficiency, and it has directly determined important indicators such as activity of such catalysts, selectivity and service life.
The phosphine part of having developed at present is by the different of atom that link to each other with P; Can roughly be divided three classes, i.e. phosphoramidite ligand of linking to each other with one or more nitrogen-atoms of the phosphine part that links to each other with three carbon atoms of phosphorus atoms, phosphite ester ligand that phosphorus atoms links to each other with one or more oxygen atoms and phosphorus atoms etc.[M.Beller，B.Cornils，C.D.Frohling，C.W.Kohlpaintner，J.Mol.Catal.A.Chem.1995，104，17.]，[Billig，E.；Abatjoglou，A.G；Bryant，D.R.U.S.Pat.4?769?498，1988(to?Union?Carbide).]。Selection is applicable to the phosphine part of hydroformylation reaction of the specific olefin substrate of a certain metal catalytic; Need be in the multiple factor that is mutually related; Like stability and synthetic complexity, the production cost etc. of product selectivity, activity of such catalysts and stability, part, make comprehensive selection.Rh (I)/triphenylphosphine is the synthetic widely used catalyst system of butyraldehyde of present hydroformylation of propene; But the problem that exists be noble metal Rh (I) (200mg/L) with triphenylphosphine consumption big (mol ratio of triphenylphosphine and rhodium was generally 200: 1), the product butyraldehyde just/different ratio not high (＜20).
Compare with widely used phosphine part in the present industry, phosphite ester ligand can show better catalytic activity and selectivity in the hydroformylation of olefin of Rh (I) catalysis.[van der Slot, S.C.; Duran, J.; Luten, J.; Kamer, P.C.J.; Van Leeuwen, P.W.N.M.Organometallics 2002,21,3873-3883.], [Magee, M.P.; Luo, W; Hersh, W.H.Organometallics 2002,21,362-372], [than woods etc., Chinese patent CN 1029774C].Although the more previous technology of this catalyst has tangible advantage and has begun to receive the generally attention of academia and industrial quarters, not extensive use in industry as yet up to now.A wherein very important reason is because the trace oxygen that is difficult to avoid in the reaction system or the existence of water; Cause catalyst oxidation or hydrolysis easily and decompose inactivation; And and then reactivity and selectivity are descended rapidly, this becomes a difficult problem of olefin hydroformylation industrial technology exploitation of puzzlement bis-phosphite/rhodium catalysis.
A kind of mechanism of degradation that possibly cause employed phosphite ester ligand in the hydroformylation of olefin has been discussed in US4599206 and US4717775, and promptly alleged self-catalysis is decomposed.This mechanism is thought, under the effect of this type of part water in reaction system hydrolysis takes place gradually, and each component generation series reaction such as the aldehyde product in warp and the reactant mixture generates hydroxyalkyl phosphonic acids again.The hydrolysis of the further catalysis part of these phosphonic acids, this chain effect make and to remain in the rapid hydrolysis of phosphite ester ligand in the reaction system and disappear, cause reactivity and selectivity sharply to descend.In the study on the industrialization process of applicant to novel phosphite-rhodium system catalyzing propone hydroformylation; Once found during using phosphite ester-rhodium catalyst system and catalyzing continuously; Do not using any additives to come under the situation of rugged catalyst, reactivity and selectivity descend rapidly in the short period of time, find the rhodium black deposition in the reactor; The residual composition of still is separated and analyze through modern analysis means such as utilization proton nmr spectra, nuclear magnetic resonance phosphorus spectrum and high resolution mass spectrums; The proof phosphite ester ligand is oxidized to phosphate, though the skeleton of part is not destroyed, the phosphate that is generated does not have catalytic activity basically.The internality deactivation phenomenom of this type catalyst is described in US4769498 embodiment 14 to some extent, and the bidentate phosphite ester ligand that wherein is used for the continuous hydroformylation reaction of propylene has reduced the catalytic activity of rhodium catalyst because of degraded.
Disclose a kind of ion-exchange of utilizing among US4599206 and the US4712775 and controlled acidity, thereby slowed down the method for phosphite ester ligand degraded.This method is through making the partial reaction mixture through weakly alkaline ion exchange resin, and the acidic materials that self-catalysis is formed remove from reactant mixture, and the mixture circulation that will handle again turns back in the reactor.The weak point of this method is when the ion exchange resin bed reaction mixture, can cause catalyst attrition to a certain degree inevitably, need be in reaction system the concentration of make-up catalyst to make it to reach suitable; Moreover this method also need be added a large-scale optional equipment, has significantly increased the cost of investment operation.
Disclose a kind of utilization among the US4567306 and in reaction system, added the method that tertiary amine reduces cyclic phosphite ligands degraded in the carbonylation.This method adds tertiary amine and contains in the reaction system of phosphite ester ligand, utilizes in the tertiary amine and forms ammonium salt with acidic materials, slows down the part that the open loop because of part hydrolysis and cyclic phosphites causes and destroys.But above-mentioned these tertiary amines of patent statement can not suppress the degraded of non-annularity phosphite ester ligand.In addition; [Chem.Abstr., 1974,80 (23); 132739j] in reported the polymerization that many aminated compounds can the catalysis aldehydes, therefore use the amine additive obviously to increase the formation of accessory substance and cause productive rate to reduce and loaded down with trivial details separating technology in the hydroformylation of propene system.
CN1092058 proposes to adopt epoxide as stabilizing agent.But epoxide is comparatively expensive, and reactant liquor is controlled in the weakly alkaline environment, can quicken the butyraldehyde polymerization reaction take place, and epoxide decomposition back is not fully aware of to the influence of product quality.
Therefore the objective of the invention is through using phosphorous acid ester additive agent; A kind of hydroformylation of propene system of rhodium (I)/triaryl phosphine catalysis of improvement is provided; Improve the just different selectivity that compares of butyraldehyde in Rh (I)/triaryl phosphine activity of such catalysts and the product; And the service life of significant prolongation bisphosphite ligands, the consumption of reduction triaryl phosphine.The characteristics of this type catalyst system are higher than third generation Rh (I)/triphenylphosphine activity of such catalysts and selectivity; Stability than the 4th generation Rh (I)/diphosphite ester catalyst is better; Therefore; Novel catalyst system provided by the invention can overcome the 3rd, the 4th generation catalyst shortcoming, reduce the cost of hydroformylation of propene suitability for industrialized production, for its commercial Application provides new catalyst technology.
Summary of the invention
The purpose of this invention is to provide a kind of hydroformylation of propene catalyst system and catalyzing;
Another object of the present invention provides the method for the synthetic butyraldehyde of a kind of hydroformylation of propene catalysis. and this method adds a kind of phosphite ester ligand as additive in the catalyst system of rhodium-containing and triaryl phosphine; Can obviously improve in rhodium/triaryl phosphine activity of such catalysts and the product the just different ratio of butyraldehyde optionally on the basis; And the service life of significant prolongation phosphite ester ligand, the consumption of minimizing triaryl phosphine.
Hydroformylation of propene catalyst system and catalyzing of the present invention be adopt the catalyst system of rhodium-containing, triaryl phosphine and phosphite ester ligand hydrogen catalyzed, carbon monoxide and olefine reaction generate butyraldehyde.
Spendable in the present invention triaryl phosphine part can be used general formula P (Ar)
3Expression, wherein Ar is the aromatic group of 6-22 carbon atom, for example phenyl, o-tolyl, a tolyl, p-methylphenyl, rubigan, p-methoxyphenyl, 3; 5-3,5-dimethylphenyl, 3,5-dibromo phenyl, 3,5-two (trifluoromethyl) phenyl, 1-naphthyl, 2-naphthyl, 1; 1 '-biphenyl-2,2 '-two bases, 3,5-two (phenyl) phenyl, 3; 5-two (3, the 5-3,5-dimethylphenyl) phenyl and 3,5-diisopropyl-4-methoxyphenyl etc.And described three Ar groups both can be identical, also can be different.Described triaryl phosphine derivative P (Ar)
3Comprise but be not subject to following example:
Wherein, R is H, C
1～4Alkyl, C
1～4Perfluoroalkyl or halogen, n=1 or 2, Ar=3, the 5-xylyl, the Ph=phenyl,
iThe Pr=isopropyl.
P1～9 can be P1, R=H; P2, R=o-CH
3, P3=m-CH
3, P4=p-CH
3, P5=p-Cl, P6=P-OCH
3, R7=3,5-Di-CH
3, P8=3,5-Di-Br, P9=3,5-Di-CF
3
At above-mentioned triaryl phosphine derivative P (Ar)
3In, triphenylphosphine P1 is a commercialization reagent, obtains some other P (Ar) easily
3Derivative can adopt various known method preparations in this area.For example about the preparation of P3, P7, P16 and P17, can be with reference to Adv.Syn.Catal., 2005, the 347th volume, 1193-1197 page or leaf and the literature method of wherein being quoted from; References such as Compound P 9, P10 and P18 are synthetic with the P7 similar methods.About the preparation of P5, referring to J.Am.Chem.Soc., 1967, the 89th volume, the description in the 5235-5246 page or leaf; About the preparation of P6, referring to J.Am.Chem.Soc., 1975, the 97th volume, the description in the 1787-1794 page or leaf; About the preparation of P8, referring to J.Organomet.Chem., 1981, the 215th volume, the method described in the 281-191 page or leaf; About the preparation of P11 and P12, referring to J.Chem.Soc., nineteen fifty-five, the method described in the 4107-4114 page or leaf; About the preparation of P13, referring to Bll.Chem.Soc.Jpn., 1991, the 64th volume, the method described in the 3128-3184 page or leaf; About the preparation of P14 and P15, referring to Eur.J.Inorg.Chem., 2000, the 4th volume, the method described in the 647-654 page or leaf.
Diphosphite ester additive described in the present invention can be represented with following general structure:
Wherein X can be C
6-C
28Substituted or unsubstituted organic divalence bridging arlydene, comprise 1,1 '-biphenyl-2,2 '-two bases, 3,3 '-dual-tert-butyl-5; 5 '-bi-methoxy-1,1 '-biphenyl-2,2 '-two bases, 3,3 ', 5; 5 '-tetra-tert-1,1 '-biphenyl-2,2 '-two bases, 1,4-phenylene, 1,3-phenylene, 1; 5-naphthylene or 2,7,9,9-tetramethyl-9H-(folder) xanthene-4,5-two bases etc.; Y
1, Y
2, Z
1Or Z
2Can be respectively hydrogen, the tert-butyl group or methoxyl group etc., both can be identical, also can be different; Each Q is no key or a chemical single bond in the general formula.
Can adopt the various known methods in this area about the synthetic of above-mentioned phosphite ester ligand additive, for example can be with reference at US4769498, US4885401, US5874641, US6265620B1, US5202297, CN1019104B, US6583324B2, US5710344 and J.Chem.Soc., 1991; 803-804 page or leaf, J.Am.Chem.Soc.; 1993, the 115th volume, the 2066th page and Organometallics; 1996; Method described in the 15th volume, 835-847 page or leaf prepares described bi-ester of phosphite.
The example that is applicable to the rhodium catalyst precursor of the inventive method is Rh (OAc)
3, Rh
2O
3, Rh (acac) (CO)
2, [Rh (OAc) (COD)]
2, Rh
4(CO)
12, Rh
6(CO)
16, RhH (CO) (P1)
3, Rh (acac) (CO) (P1), [RhCl (COD)]
2Or [Rh (OAc) (CO)
2]
2Wherein Ac is an acetyl group, and acac is a pentanedione, and COD is 1, and the 5-cyclo-octadiene is preferably Rh (acac) (CO)
2Or Rh (acac) (CO) (P1), but described rhodium catalyst precursor need not be confined to above-claimed cpd.
Comprise Rh as herein described (I)/formed complex compound catalyst of triaryl phosphine part in the methods of the invention, both be included in the reaction system on-the-spot formation, also can comprise preparation in advance.If desired, can also use this type mixture of catalysts.According to well-known complex compound synthetic method; Through suitable rhodium catalyst precursor is mixed with described triaryl phosphine part in optional suitable solvent; Can prepare the rhodium/triaryl phosphine complex compound catalyst that is used for the inventive method; Its consumption only needs in the propene hydroformylation reaction medium, to provide required a certain amount of rhodium concentration, and the concentration range of usually preferred rhodium is 10 to 500mg/L, most preferably is 10 to 100mg/L.The mol ratio of triaryl phosphine part and rhodium is generally 1～50: 1, be preferably 1～10: and 1, most preferably be 4～8: 1.
The applicant finds under study for action; In the reaction system of said hydroformylation of propene, add the catalytic activity that a certain proportion of bisphosphite ligands can significantly improve Rh (I)/triaryl phosphine; And the service life of prolongation bisphosphite ligands and catalyst thereof; Though slightly descend than Rh (I)/bis-phosphite catalyst reaction activity sometimes, help the too fast and serious exothermic phenomenon of reaction speed is regulated and control; In addition, the adding of bisphosphite ligands can obviously improve Rh (I)/triaryl phosphine selection of catalysts property, under proper condition, compares with independent use Rh (I)/diphosphite ester catalyst, and just different ratio does not descend and improves on the contrary.The mechanism of action of Rh (I)/triaryl phosphine catalyst system of improveing through the diphosphite ester additive at present it be unclear that; Supposition possibly be because real active catalytic species have been stablized in triaryl phosphine and rhodium coordination, has reduced receiving electronic capability and corresponding phosphite ester decomposition process being slowed down of rhodium simultaneously.No matter above whether the supposition of the mechanism of action of the catalyst system and catalyzing about the phosphorous acid ester additive agent improvement correct, and the present invention is not limited to above-mentioned supposition.In view of triphenyl (P1) phosphine cheap and easy to get, though and phosphorous acid ester additive agent is synthetic slightly has any problem, consumption is less, helps improving the economy of technology, so triphenyl (P1) phosphine is preferred triaryl phosphine part.The mol ratio of triphenylphosphine and rhodium is generally 1～50: 1, be preferably 1～10: 1.
Described in the methods of the invention solvent generally all is a solvent used in the hydroformylation reaction, everyly can not bring the suitable solvent of too much adverse effect all can use to reaction.Representative appropriate solvent comprises those for example disclosed solvents in US4668651.If desired, can use the mixture of one or more different solvents.First-selected is the solvent that can dissolve propylene, rhodium/triaryl phosphine complex compound catalyst and above-mentioned phosphite derivative thing additive preferably, and preferred solvent is toluene, hutanal and isobutylaldehyde.
This hydroformylation reaction temperature is generally room temperature to 150 ℃, and preferred reaction temperature is 60～150 ℃, most preferably from about 80～120 ℃.The total gas pressure scope of the hydrogen of hydroformylation reaction, carbon monoxide and propylene is generally 0.1～20MPa, is preferably 0.1～5MPa, most preferably is 1～3MPa.Mainly the amount through the control reactant limits stagnation pressure to minimum and reaction is carried out with required speed.Wherein, the mol ratio 1～10: 1～10: 1～10 of described hydrogen, carbon monoxide and propylene; Adopt the hydrogen of more ratios, to not influence of reaction, more preferably the mol ratio of hydrogen and carbon monoxide is 1～2: 1～2.
Hydroformylation of propene method of the present invention can intermittently or be carried out in a continuous manner.In the commercial run of continuation mode; Can be with starting continuation method in described triaryl phosphine, rhodium catalyst precursor compound and the adding reactors such as a kind of phosphite derivative thing additive and reaction dissolvent in an operating procedure; After being heated to desired reaction temperature, in above-mentioned reactant mixture, import propylene, carbon monoxide and hydrogen with continuous or mode intermittently.In the effluent of reactor, contain hutanal and isobutylaldehyde, rhodium/triaryl phosphine catalyst, free phosphorous acid ester additive agent and derivative thereof, on-the-spot accessory substance such as aldehydes condensation product, unreacted propylene, carbon monoxide, hydrogen and the reaction dissolvent etc. that produce of propene hydroformylation reaction, from reactor, export in evaporimeter/separator.Through being decompressed to for example 0.1MPa, gaseous reactant carbon monoxide and hydrogen are told from mixture, and required aldehyde product can be separated and collect by usual manner in one or more separating step from liquid reaction mixture.Circulations such as derivative, solvent and not isolated all accessory substances with remaining rhodium-containing/triaryl phosphine catalyst, free phosphite derivative thing additive, triaryl phosphine part and oxidation thereof turn back in the propene hydroformylation reaction device then, and are reused in the method for the present invention.The isolation technics that adopts any this area professional person to be total to know can be separated described butyraldehyde product from reactant mixture, for example evaporation etc.
Method of the present invention needs regularly or the concentration of above-described triaryl phosphine of continuous monitoring and described phosphite ester the reaction system of moving; Be lower than said value if find described concentration; Then possibly cause the loss of said compound owing to reasons such as degradeds, add triaryl phosphine and bi-ester of phosphite in the reactant mixture that recycles this moment.
Description of drawings
Accompanying drawing 1 is flow process of the present invention and installation drawing.
Accompanying drawing is a kind of continuous propene hydroformylation reaction device, and wherein B1, B2 are force (forcing) pump, and M is a stirring motor.
The specific embodiment
The following example helps to further specify the present invention, but the present invention is not constituted any restriction.
Employed bidentate phosphite ester ligand L1-12 has following structure in the following example:
Embodiment 1
Bidentate phosphite ester L1's is synthetic: with 2,2 '-xenol joins excessive PCl
3In, reflux (reflux) after 5 hours decompression distillation remove excessive PCl
3, obtain white solid compd A (yield is 71%).Under the ice bath temperature, with 2,2 '-xenol (0.37g, 2mmol) and triethylamine (2.8mL; Oxolane 20mmol) (THF) drips of solution is added to A, and (1.25g is in tetrahydrofuran solution 5mmol), after dripping; Rise to room temperature (r.t) gradually and stir post processing in 24 hours, recrystallization obtains product L1 behind the silicagel column purifying excessively; White crystal, yield are 90% (1.1g)
1H NMR with
31P NMR identifies structure, 124 ℃ of fusing points.
Embodiment 2
Bidentate phosphite ester L2's is synthetic:
Under-40 ℃ of conditions, with the dinaphthalene diphenol (1.43g, 5mmol) and triethylamine (5.6mL, tetrahydrofuran solution 40mmol) is added drop-wise to PCl
3(0.43mL in tetrahydrofuran solution 5mmol), is warming up to room temperature gradually after dripping, stir and be cooled to-40 ℃ after 2 hours; Splash into again compd B (0.82g, 2mmol) and triethylamine (2.8mL, tetrahydrofuran solution 20mmol) are warming up to room temperature gradually after dripping; Stir post processing in 2 hours, cross the silicagel column purifying, obtain product L2; White solid, yield are 67% (1.39g)
1H NMR with
31P NMR identifies structure, and fusing point is 249-251 ℃.
Embodiment 3
Bidentate phosphite ester L3's is synthetic: under the room temperature, with compd B (1.0g, 2.5mmol) and triethylamine (2.8mL, toluene solution 20mmol) is added drop-wise to PCl
3(0.22mL, in toluene solution 2.5mmol), temperature rising reflux was cooled to room temperature after 2 hours, splashed into 2 again; 2 '-xenol (0.18g, 1mmol) and triethylamine (1.4mL, toluene solution 10mmol) drip back temperature rising reflux 2 hours; The silicagel column purifying is crossed in the cooling post processing, obtains product L3; White solid, yield are 30% (0.31g)
1H NMR with
31P NMR identifies structure, and fusing point is 145-147 ℃.
Embodiment 4
Bidentate phosphite ester L4's is synthetic: under-20 ℃ of conditions, with Compound C (0.69g, 2mmol) and triethylamine (2.8mL; Tetrahydrofuran solution 20mmol) is added drop-wise to compd A, and (0.96g in tetrahydrofuran solution 4mmol), rises to room temperature gradually after dripping; Stir post processing in 24 hours, add the acetonitrile recrystallization, obtain product L4; White crystal, yield are 69% (1.05g)
1H NMR with
31P NMR identifies structure, and fusing point is 175-178 ℃.
Embodiment 5
Bidentate phosphite ester L5's is synthetic: under 50 ℃ of conditions, with compd B (0.82g, 2mmol) and triethylamine (2.8mL; Tetrahydrofuran solution 20mmol) is added drop-wise to compd A, and (0.98g in tetrahydrofuran solution 4mmol), reduces to room temperature gradually after dripping; Stir post processing in 24 hours, cross the silicagel column purifying, obtain product L5; White solid, yield are 32% (0.53g)
1H NMR with
31P NMR identifies structure, and fusing point is 124 ℃.
Embodiment 6
Bidentate phosphite ester L6's is synthetic: under the ice-water bath, with hydroquinones (0.22g, 2mmol) and triethylamine (2.8mL; Tetrahydrofuran solution 20mmol) is added drop-wise to compd A, and (0.98g is in tetrahydrofuran solution 4mmol), after dripping; Rise to room temperature gradually and stir post processing in 24 hours, recrystallization obtains product L6, light gray crystal behind the silicagel column purifying excessively; Yield is 52% (0.56g)
1H NMR with
31P NMR identifies structure, and fusing point is 89-92 ℃.
Embodiment 7
Bidentate phosphite ester L7's is synthetic: under the ice-water bath, and with 2,6-naphthalenediol (0.32g; 2mmol) and triethylamine (2.8mL, tetrahydrofuran solution 20mmol) are added drop-wise to compd A, and (0.98g is in tetrahydrofuran solution 4mmol); After dripping, rise to room temperature gradually and stir post processing in 24 hours, recrystallization obtains product L7 behind the silicagel column purifying excessively; White crystal, yield are 41% (0.48g)
1H NMR with
31P NMR identifies structure, and surveying fusing point is 194-196 ℃.
Embodiment 8
Bidentate phosphite ester L8's is synthetic: under-40 ℃ of conditions, with the dinaphthalene diphenol (1.43g, 5mmol) and triethylamine (5.6mL, tetrahydrofuran solution 40mmol) is added drop-wise to PCl
3(0.43mL in tetrahydrofuran solution 5mmol), is warming up to room temperature gradually after dripping, stir and be cooled to-40 ℃ after 2 hours; Splash into again resorcinol (0.22g, 2mmol) and triethylamine (2.8mL, tetrahydrofuran solution 20mmol) are warming up to room temperature gradually after dripping; Stir post processing in 2 hours, cross the silicagel column purifying, obtain product L8; White solid, yield are 60% (0.88g)
1H NMR with
31P NMR identifies structure, and fusing point is 75-78 ℃.
Embodiment 9
Bidentate phosphite ester L9's is synthetic:
Under the ice-water bath, with Compound C (7.16g, 20mmol) and triethylamine (28mL, tetrahydrofuran solution 0.2mol) is added drop-wise to PCl
3(1.7mL in tetrahydrofuran solution 20mmol), is warming up to backflow after dripping; Stir and be cooled to-40 ℃ after 2 hours, splash into the tetrahydrofuran solution of equivalent Compound C and triethylamine again, be warming up to room temperature after dripping gradually; Stir post processing in 24 hours, cross the silicagel column purifying, obtain Compound D; Thick weak yellow liquid, yield are 80.6% (12g)
1H NMR with
31P NMR identifies structure.
Under the ice-water bath, with Compound D (1.0g, 1.34mmol) and triethylamine (1.9mL, toluene solution 13.4mmol) is added drop-wise to PCl
3(0.17mL in toluene solution 2mmol), is warming up to backflow after dripping, and stirs and is cooled to 0 ℃ after 2 hours; Splash into again phenol (0.25g, 2.68mmol) and triethylamine (2.8mL, toluene solution 20mmol) are warming up to room temperature gradually after dripping; Stir post processing in 2 hours, cross the silicagel column purifying, obtain product L9; White solid, yield are 73.6% (0.95g)
1H NMR with
31P NMR identifies structure, and fusing point is 75-76 ℃.
Embodiment 10
Bidentate phosphite ester L10's is synthetic:
Under the ice-water bath, with Compound D (1.0g, 1.34mmol) and triethylamine (1.9mL, toluene solution 13.4mmol) is added drop-wise to PCl
3(0.17mL in toluene solution 2mmol), is warming up to backflow after dripping, and stirs and is cooled to 0 ℃ after 2 hours; Splash into 2 again, and 2 '-xenol (0.25g, 1.34mmol) and triethylamine (1.9mL, toluene solution 13.4mmol); Be warming up to backflow after dripping, stir and be cooled to room temperature treatment after 2 hours, be recrystallized behind the silicagel column purifying excessively, obtain product L10; White crystal, yield are 63.7% (0.85g)
1H NMR with
31P NMR identifies structure, and fusing point is 223 ℃.
Embodiment 11
Bidentate phosphite ester L11's is synthetic:
Under the ice-water bath, with Compound C (7.16g, 20mmol) and triethylamine (28mL, tetrahydrofuran solution 0.2mol) is added drop-wise to PCl
3(1.7mL in tetrahydrofuran solution 20mmol), is warming up to backflow after dripping; Stir and remove solvent under reduced pressure after 2 hours, add triethylamine (6mL, toluene solution 40mmol) (50mL); Be added drop-wise to the compd E (2.16g of ice-water bath cooling under 0 ℃; 8mmol) and triethylamine (6mL, in toluene solution 40mmol) (100mL), adularescent deposition forms immediately.Mixture is heated to 80 ℃ and stirred overnight, crosses the silicagel column purifying, obtains product L11, and white solid, yield are 62% (5.17g),
1H NMR with
31P NMR identifies structure, and fusing point is 248 ℃.
Embodiment 12
Bidentate phosphite ester L12's is synthetic:
Under the ice-water bath, with compd B (8.2g, 20mmol) and triethylamine (28mL, tetrahydrofuran solution 0.2mol) is added drop-wise to PCl
3(1.7mL in tetrahydrofuran solution 20mmol), is warming up to backflow after dripping; Stir and remove solvent under reduced pressure after 2 hours, add triethylamine (6mL, toluene solution 40mmol) (50mL); Be added drop-wise to the compd E (2.16g of ice-water bath cooling under 0 ℃; 8mmol) and triethylamine (6mL, in toluene solution 40mmol) (100mL), adularescent deposition forms immediately.Mixture is heated to 80 ℃ and stirred overnight, crosses the silicagel column purifying, obtains product L11, and white solid, yield are 78% (7.16g),
1H NMR with
31P NMR identifies structure, and fusing point is 305 ℃.
Embodiment 13
Under air atmosphere, be equipped with in the manometric stainless steel autoclave and add that [Rh (acac) (CO) to 400mL
2] (0.01mmol, 2.5mg, 103mg/L) with table 1 in triphenylphosphine and the bidentate phosphite ester ligand 0.04mmol L1-12 additive of specified amount, and 10mL dry toluene stirs the generation rhodium catalyst solution with magnetic stirrer.Connect gas line, after argon replaces gas reactor three times, import the propylene of specified amount in the table 1, feeding hydrogen and carbon monoxide (1: 1) gaseous mixture to stagnation pressure is 2MPa.With hot mode heat temperature raising beyond the reactor to temperature required (80 ℃), tonifying Qi is 2MPa to keep gross pressure for several times in the middle of the reaction, reacts to the fixed time under magnetic agitation; Reactor cools off with frozen water; The emptying residual gas is weighed in fume hood, drives still; Sampling is measured just different from (mol ratio of hutanal/isobutylaldehyde) with gas-chromatography (GC), the result lists table 1 in.
Table 1
| L | Rh (mmol) | P1 (mmol) | Propylene (g) | Reaction time (h) | Conversion ratio (%) | Space-time yield (mol/Lh) | Just different ratio |
| -- | 0.01 | 0.04 | 10 | 3 | 17.5 | 1.4 | 2.1 |
| L1 | 0.01 | -- | 10 | 4 | 80 | 3.8 | 4 |
| L1 | 0.01 | 0.04 | 10 | 4 | 45 | 2.1 | 4.3 |
| L2 | 0.01 | -- | 9 | 3 | 99 | 7.4 | 24 |
| L2 | 0.01 | 0.04 | 9 | 3 | 65 | 4.9 | 23.6 |
| L3 | 0.01 | -- | 10 | 3 | 58 | 3.4 | 1.1 |
| L3 | 0.01 | 0.04 | 10 | 3 | 20 | 1.2 | 2.2 |
| L4 | 0.01 | -- | 10 | 3 | 99 | 7.8 | 42 |
| L4 | 0.01 | 0.04 | 10 | 3 | 46 | 3.7 | 43 |
| L5 | 0.01 | -- | 10 | 3 | 99 | 7.8 | 25.1 |
| L5 | 0.01 | 0.04 | 10 | 3 | 38 | 3.0 | 24.5 |
| L6 | 0.01 | -- | 10 | 5.5 | 49 | 1.2 | 1.2 |
| L6 | 0.01 | 0.04 | 10 | 5.5 | 22 | 0.7 | 2.0 |
| L7 | 0.01 | 0.04 | 10 | 6 | 25 | 0.7 | 1.1 |
| L8 | 0.01 | 0.04 | 10 | 6 | 0 | 0 | 0 |
| L9 | 0.01 | -- | 10 | 3 | 80 | 6.4 | 21.2 |
| L9 | 0.01 | 0.04 | 10 | 3 | 45 | 3.6 | 20 |
| L10 | 0.01 | -- | 9 | 4 | 77 | 4.1 | 10.1 |
| L10 | 0.01 | 0.04 | 10 | 4 | 35 | 1.9 | 11.1 |
| L11 | 0.01 | -- | 10 | 3 | 51.3 | 4.1 | 52 |
| L11 | 0.01 | 0.04 | 10 | 3 | 27.5 | 2.2 | 54 |
| L12 | 0.01 | -- | 10 | 3 | 48 | 3.8 | 49 |
| L12 | 0.01 | 0.04 | 10 | 3 | 23.8 | 1.9 | 47 |
Can find out from table 1; The adding of diphosphite ester additive can improve Rh (I)/triphenylphosphine activity of such catalysts and selectivity; Compare with Rh (I)/diphosphite ester catalyst, though reactivity descends to some extent, the just different ratio of product is kept basically preferably.
Embodiment 14
Under air atmosphere, be equipped with in the manometric stainless steel autoclave and add that [Rh (acac) (CO) to 400ml
2] (0.01mmol, 2.5mg, 103mg/L) with table 2 in triphenylphosphine and the bidentate phosphite ester L4 additive of different proportion, and 10mL dry toluene stirs the generation rhodium catalyst solution with magnetic stirrer.Connect gas line, after argon replaces gas reactor three times, import the propylene of specified amount in the table 1, feeding hydrogen and carbon monoxide (1: 1) gaseous mixture to stagnation pressure is 2MPa.With hot mode heat temperature raising beyond the reactor to temperature required (80 ℃), tonifying Qi is 2MPa to keep gross pressure for several times in the middle of the reaction, reacts to the fixed time under magnetic agitation; Reactor cools off with frozen water; The emptying residual gas is weighed in fume hood, drives still; Sampling is with the mol ratio of gas-chromatography (GC) mensuration hutanal and isobutylaldehyde, and the result lists table 1 in.
Table 2
| Rh (mmol) | P1 (mmol) | L4 (mmol) | Propylene (g) | Reaction time (h) | Conversion ratio (%) | Space-time yield (mol/Lh) | Just different ratio |
| 0.01 | 0.16 | 0 | 10 | 3 | 17.5 | 1.4 | 2.1 |
| 0.01 | 0 | 0.04 | 10 | 3 | 81.7 | 6.5 | 35.1 |
| 0.01 | 0.16 | 0.04 | 10 | 3 | 11.6 | 0.92 | 32.8 |
| 0.01 | 0.10 | 0.04 | 10 | 3 | 17.5 | 1.4 | 35.4 |
| 0.01 | 0.08 | 0.08 | 10 | 3 | 40.8 | 3.2 | 39.3 |
| 0.01 | 0.04 | 0.04 | 10 | 3 | 46.4 | 3.7 | 42.4 |
| 0.01 | 0.02 | 0.04 | 10 | 3 | 58.3 | 4.6 | 30 |
| 0.01 | 0.01 | 0.04 | 10 | 3 | 81.7 | 6.5 | 31.5 |
Can find out that from table 2 additive bis-phosphite L4 adds makes the activity of Rh (I)/triphenylphosphine catalystic converter system and the just different ratio of product obviously improve.
Embodiment 15
Single still simulated circulation test: under air atmosphere, be equipped with and add in the manometric stainless steel autoclave that [Rh (acac) (CO) to 400ml
2] (0.02mmol, 5mg) and the bidentate phosphite ester L2 additive of 21mg (0.08mmol) triphenylphosphine and 83mg (0.08mmol), the 20mL dry toluene stirs with magnetic stirrer, generates rhodium catalyst solution.Connect gas line, after argon replaces gas reactor three times, import the 10g propylene, feeding hydrogen and carbon monoxide (1: 1) gaseous mixture to stagnation pressure is 2MPa.With hot mode heat temperature raising to 80 beyond the reactor ℃, tonifying Qi is 2MPa to keep gross pressure for several times in the course of reaction, reacts after 3 hours under magnetic agitation; Reactor cools off with frozen water, and the emptying residual gas is weighed in fume hood; Do not drive still, add the 10g propylene at every turn again and react next time.After the repetitive operation 10 times, weigh according to the method described above, sampling is 24 with the just different ratio that gas-chromatography (GC) records hutanal and isobutylaldehyde, and conversion ratio 41% reacts trouble-free operation 30 hours and selection of catalysts property is uninfluenced.
Embodiment 16
The reaction condition of hydroformylation of propene and equipment repeat embodiment 15, and difference is that with three (-tolyl) phosphine (P3) is as part and Rh (OAc)
3Prepare catalyst solution with L2, the mol ratio that makes Rh/P3/L2 is 1: 4: 4, and reaction is 24 with the continuous operation of above-mentioned single still simulated circulation test mode records the product butyraldehyde after 48 hours just different ratio, conversion ratio 49%.
Embodiment 17
The reaction condition of hydroformylation of propene and equipment repeat embodiment 15, and difference is with three (right-chlorphenyl) phosphines (P5) as part and [Rh (acac) (CO)
2] and L2 prepare catalyst solution, the mol ratio that makes Rh/P5/L2 is 1: 4: 4, reaction with above-mentioned single still simulated circulation test mode continuously the operation just different ratio that records the product butyraldehyde after 42 hours be 25, conversion ratio 44%.
Embodiment 18
The reaction condition of hydroformylation of propene and equipment repeat embodiment 15, and triphenylphosphine is as part and [Rh (OAc) (COD)]
2Prepare catalyst solution with L5, the mol ratio that makes Rh/P1/L5 is 1: 4: 4, and reaction is 25 with the continuous operation of above-mentioned single still simulated circulation test mode records the product butyraldehyde after 48 hours just different ratio, conversion ratio 39%.
Embodiment 19
The reaction condition of hydroformylation of propene and equipment repeat embodiment 15, and difference is with three (3, the 5-dibromo phenyl) phosphine (P8) as part and [Rh (acac) (CO)
2] and L5 prepare catalyst solution, the mol ratio that makes Rh/P8/L5 is 1: 4: 4, reaction with above-mentioned single still simulated circulation test mode continuously the operation just different ratio that records the product butyraldehyde after 72 hours be 24, conversion ratio 28%.
Embodiment 20
The reaction condition of hydroformylation of propene and equipment repeat embodiment 15, and difference is with three (3,5-two (trifluoromethyl) phenyl) phosphine (P9) as part and [Rh (OAc) (COD)]
2Prepare catalyst solution with L9, the mol ratio that makes Rh/P9/L9 is 1: 4: 4, and reaction is 20 with the continuous operation of above-mentioned single still simulated circulation test mode records the product butyraldehyde after 40 hours just different ratio, conversion ratio 53%.
Embodiment 21
The reaction condition of hydroformylation of propene and equipment repeat embodiment 15, and difference is with three (2-naphthyl) phosphines (P10) as part and [Rh (OAc) (CO)
2]
2Prepare catalyst solution with L9, the mol ratio that makes Rh/P10/L9 is 1: 4: 8, and reaction is 21 with the continuous operation of above-mentioned single still simulated circulation test mode records the product butyraldehyde after 96 hours just different ratio, conversion ratio 35%.
Embodiment 22
The reaction condition of hydroformylation of propene and equipment repeat embodiment 15, and difference is with described triaryl phosphine P12 as part and [Rh (acac) (CO)
2] and L10 prepare catalyst solution, the mol ratio that makes Rh/P12/L10 is 1: 4: 6, reaction with above-mentioned single still simulated circulation test mode continuously the operation just different ratio that records the product butyraldehyde after 24 hours be 10, conversion ratio 33%.
Embodiment 23
The reaction condition of hydroformylation of propene and equipment repeat embodiment 15, and difference is with described triaryl phosphine P13 as part and Rh
4(CO)
12Prepare catalyst solution with L11, the mol ratio that makes Rh/P13/L11 is 1: 4: 4, and reaction is 54 with the continuous operation of above-mentioned single still simulated circulation test mode records the product butyraldehyde after 48 hours just different ratio, conversion ratio 25%.
Embodiment 24
The reaction condition of hydroformylation of propene and equipment repeat embodiment 15, and difference is with described triaryl phosphine P15 as part and [RhCl (COD)]
2Prepare catalyst solution with L11, the mol ratio that makes Rh/P15/L11 is 1: 4: 8, and reaction is 50 with the continuous operation of above-mentioned single still simulated circulation test mode records the product butyraldehyde after 48 hours just different ratio, conversion ratio 30%.
Embodiment 25
The reaction condition of hydroformylation of propene and equipment repeat embodiment 15, and difference is with described triphenylphosphine as part and [Rh (acac) (CO)
2] and L12 prepare catalyst solution, the mol ratio that makes Rh/P1/L12 is 1: 4: 6, reaction with above-mentioned single still simulated circulation test mode continuously the operation just different ratio that records the product butyraldehyde after 72 hours be 43, conversion ratio 35%.
Embodiment 26
The reaction condition of hydroformylation of propene and equipment repeat embodiment 15, and difference is with described P12 as part and Rh
6(CO)
16Prepare catalyst solution with L12, the mol ratio that makes Rh/P12/L4 is 1: 4: 8, and reaction is 45 with the continuous operation of above-mentioned single still simulated circulation test mode records the product butyraldehyde after 96 hours just different ratio, conversion ratio 65%.
Embodiment 27
The reaction condition of hydroformylation of propene and equipment repeat embodiment 15, and difference is to replace triphenylphosphine as part and [Rh (acac) (CO) with described triaryl phosphine P18
2] and L12 prepare catalyst solution, the mol ratio that makes Rh/P18/L12 is 1: 4: 4, reaction with above-mentioned single still simulated circulation test mode continuously the operation just different ratio that records the product butyraldehyde after 36 hours be 44, conversion ratio 52%.
Embodiment 28
Accompanying drawing 1 is a kind of continuous propene hydroformylation reaction device, and wherein B1, B2 are force (forcing) pump, and M is a stirring motor.With the argon replaces volume is the gas in hydroformylation reaction device, the 1# evaporimeter of 10L, No. 2 evaporimeters and the stripping tower.In the container of a 15L Rh (acac) (CO) P1, triphenylphosphine P1 be dissolved in the 10L hutanal, the concentration that makes Rh (I) is 30mg/L, the mol ratio of Rh/ triphenylphosphine (P1) is 1: 200.Through interim pipeline this 10L solution is driven into the hydroformylation reaction device that volume is 10L through circulating pump B1; And make 1# evaporimeter, No. 2 evaporimeters and stripping tower bottom respectively maintain the solution of 0.7L successively, promptly remove interim pipeline after the completion.Propylene is sent into the hydroformylation reaction device with 3.33g/min.Carbon monoxide and hydrogen get into stripping tower with the speed of 2.22g/min and 0.16g/min respectively, and then get into the hydroformylation reaction device.Reactor temperature is 95 ± 1 ℃, and the total gas pressure of hydrogen, carbon monoxide and propylene is 1.9 ± 0.1MPa.Propylene, carbon monoxide and hydrogen react the propane that generates hutanal and isobutylaldehyde and trace under the catalysis of Rh/P1; The mixed solution that contains product and catalyst flow into evaporimeter No. 1 from the hydroformylation reaction device; Part propylene, propane and a spot of butyraldehyde are evaporated in the mixed solution; Rest solution gets into No. 2 evaporimeters and evaporates part butyraldehyde and micro-propylene, propane again, and the remaining solution that contains catalyst then is circulated back in the hydroformylation reaction device.Evaporate the butyraldehyde that and be condensed into the liquid that is dissolved with propylene and propane, be pumped into stripping tower by B2 then.Adopt carbon monoxide and propylene and the propane flammable gas that the hydrogen gas mixture handle is dissolved in wherein to put forward, and together get into the hydroformylation reaction device, receive the hutanal and the isobutylaldehyde of mixing at the bottom of the stripping tower tower with the speed of 4.7 ± 0.1g/min.The liquid level of hydroformylation reaction device, 1# evaporimeter, No. 2 evaporimeters and stripping tower bottom keeps constant.Measure the mol ratio of hutanal and isobutylaldehyde with gas-chromatography (GC).
The concentration of triphenylphosphine P1 is monitored by liquid chromatogram in the hydroformylation reaction device.Reaction was carried out 780 hours altogether continuously, and it is constant that the mol ratio of hutanal/isobutylaldehyde of receiving at the bottom of the stripping tower tower kept after 120 hours, and remain 7.8 always.
Embodiment 29
The process conditions of hydroformylation of propene and equipment repeat embodiment 28, and difference is to adopt in the reaction system Rh (acac) (CO)
2Replacement Rh (acac) is P1 (CO), L2 replacement triphenylphosphine P1, and the mol ratio of Rh/L2 is 1: 4, and the system concentration of Rh maintains 30mg/L, and the hydroformylation reaction temperature is 78 ± 1 ℃.
The concentration of L2 is monitored by liquid chromatogram in the hydroformylation reaction device, along with carrying out continuously of reaction, finds that L2 constantly reduces.For keeping the constant concentration of L2, need in the reaction response device, add 0.9g L2 in per 24 hours.The method of adding is: 0.9g L2 is dissolved in hutanal and the isobutylaldehyde mixed solution of receiving at the bottom of the 0.5L stripping tower tower, through interim pipeline solution is driven into the hydroformylation reaction device through circulating pump B1, promptly remove interim pipeline after the completion.Reaction was carried out 610 hours altogether continuously, and it is constant that the mol ratio of hutanal/isobutylaldehyde of receiving at the bottom of the stripping tower tower kept after 120 hours, and remain 22 always.
Embodiment 30
The process conditions of hydroformylation of propene and equipment repeat embodiment 28, and difference is also to have added in the reaction system additive bis-phosphite (L2), and the mol ratio of Rh/P1/L2 is 1: 4: 4, and the hydroformylation reaction temperature is 92 ± 1 ℃.
The concentration of P1 and L2 is monitored by liquid chromatogram in the hydroformylation reaction device, along with carrying out continuously of reaction, do not find that L2 reduces significantly, but P1 concentration reduces gradually.Reaction was carried out 760 hours altogether continuously, the L2 that adds that feeds intake during except that the reaction beginning, during do not add L2 again.Receive the hutanal and the isobutylaldehyde of mixing at the bottom of the stripping tower tower with the speed of 4.7 ± 0.1g/min, it is constant that the mol ratio of hutanal/isobutylaldehyde kept after 120 hours, and remain 25 always.It is thus clear that to having played good activation, and P1 has good stable to turn usefulness into to L2 to L2 to Rh (I)/P1 catalyst, the mol ratio of hutanal/isobutylaldehyde is improved has certain promotion simultaneously.
Embodiment 31
The process conditions of hydroformylation of propene and equipment repeat embodiment 29, and difference is to adopt in the reaction system L4 replacement L2, and the mol ratio of Rh/L4 is 1: 4, and the hydroformylation reaction temperature is 78 ± 1 ℃.
Along with carrying out continuously of reaction, find that L4 constantly reduces.For keeping the constant concentration of L4, needed per 24 hours in the reaction response device, to add 1g L4, the method for adding is identical with embodiment 29.Reaction was carried out 1026 hours altogether continuously, received the hutanal and the isobutylaldehyde of mixing at the bottom of the stripping tower tower with the speed of 4.8 ± 0.1g/min, and it is constant that the mol ratio of hutanal/isobutylaldehyde kept after 120 hours, and remain 32 always.
Embodiment 32
The process conditions of hydroformylation of propene and equipment repeat embodiment 30, and difference is to adopt in the reaction system L4 replacement L2,, the mol ratio of Rh/P1/L4 is 1: 4: 4, the hydroformylation reaction temperature is 93 ± 1 ℃.
Along with carrying out continuously of reaction, do not find that L4 reduces significantly, reaction was carried out 810 hours altogether continuously, the L4 that adds that feeds intake during except that the reaction beginning, during do not add L4 again.Receive the hutanal and the isobutylaldehyde of mixing at the bottom of the stripping tower tower with the speed of 4.8 ± 0.1g/min, it is constant that the mol ratio of hutanal/isobutylaldehyde kept after 120 hours, and remain 36 always.It is thus clear that to having played good activation, and P1 has good stable to turn usefulness into to L4 to L4 to Rh (I)/P1 catalyst, the mol ratio of hutanal/isobutylaldehyde is improved has certain promotion simultaneously.
Embodiment 33
The process conditions of hydroformylation of propene and equipment repeat embodiment 30, and difference is to adopt in the reaction system L5 replacement L2,, the mol ratio of Rh/P1/L5 is 1: 4: 4, the hydroformylation reaction temperature is 91 ± 1 ℃.
Along with carrying out continuously of reaction, do not find that L5 reduces significantly, reaction was carried out 1236 hours altogether continuously, the L5 that adds that feeds intake during except that the reaction beginning, during do not add L5 again.Receive the hutanal and the isobutylaldehyde of mixing at the bottom of the stripping tower tower with the speed of 4.8 ± 0.1g/min, it is constant that the mol ratio of hutanal/isobutylaldehyde kept after 120 hours, and remain 28 always.
Embodiment 34
The process conditions of hydroformylation of propene and equipment repeat embodiment 30, and difference is to adopt in the reaction system L9 replacement L2,, the mol ratio of Rh/P1/L9 is 1: 4: 4, the hydroformylation reaction temperature is 95 ± 1 ℃.
Along with carrying out continuously of reaction, do not find that L9 reduces significantly, reaction was carried out 926 hours altogether continuously, the L9 that adds that feeds intake during except that the reaction beginning, during do not add L9 again.Receive the hutanal and the isobutylaldehyde of mixing at the bottom of the stripping tower tower with the speed of 4.6 ± 0.1g/min, it is constant that the mol ratio of hutanal/isobutylaldehyde kept after 120 hours, and remain 24 always.
Embodiment 35
The process conditions of hydroformylation of propene and equipment repeat embodiment 30, and difference is to adopt in the reaction system L11 replacement L2, and the mol ratio of Rh/P1/L11 is 1: 4: 4, and the hydroformylation reaction temperature is 95 ± 1 ℃.
Along with carrying out continuously of reaction, do not find that L12 reduces significantly, reaction was carried out 1248 hours altogether continuously, the L11 that adds that feeds intake during except that the reaction beginning, during do not add L11 again.Receive the hutanal and the isobutylaldehyde of mixing at the bottom of the stripping tower tower with the speed of 4.7 ± 0.1g/min, it is constant that the mol ratio of hutanal/isobutylaldehyde kept after 120 hours, and remain 54 always.
Claims (7)
1. the method for a hydroformylation of propene; It is characterized in that in solvent, under 80～120 ℃ of temperature, the concentration of hydrogen, rhodium is the total gas pressure scope of 10～500mg/L and hydrogen, carbon monoxide and propylene when being 0.1～20MPa, adopts rhodium, triaryl phosphine and phosphite ester ligand catalyst hydrogen, carbon monoxide and propylene reaction to generate butyraldehyde;
The mol ratio of described hydrogen, carbon monoxide and propylene is 1～10: 1～10: 1～10;
Described solvent is the solvent of dissolving propylene, rhodium and triaryl phosphine complex compound catalyst and phosphite ester ligand catalyst;
Described triaryl phosphine is selected from general formula P (Ar)
3, wherein Ar is the aromatic group of 6-22 carbon atom, and described three Ar groups are identical or inequality:
Described phosphite ester ligand has following general structure:
Wherein:
(1) X is 3,3 '-dual-tert-butyl-5,5 '-bi-methoxy-1,1 '-biphenyl-2,2 '-two bases or 2,7,9,9-tetramethyl-9H-(folder) xanthene-4,5-two bases;
(2) Y
1, Y
2, Z
1Or Z
2Be hydrogen, the tert-butyl group or methoxyl group;
(3) each Q is no key or singly-bound.
2. method according to claim 1, described triaryl phosphine has following structural formula:
Wherein, R is H, C
1～4Alkyl, C
1～4Perfluoroalkyl or halogen, n=1 or 2, Ar=3, the 5-xylyl, the Ph=phenyl,
iThe Pr=isopropyl.
3. method according to claim 1, the mol ratio that it is characterized in that described triaryl phosphine part and rhodium is 1～10: 1.
4. method according to claim 1, the mol ratio that it is characterized in that described hydrogen and carbon monoxide is 1～2: 1～2.
5. method according to claim 1 is characterized in that the total gas pressure of described hydrogen, carbon monoxide and propylene is 0.1～5MPa.
6. method according to claim 1, the concentration that it is characterized in that described rhodium are 10 to 100mg/L.
7. method according to claim 1 is characterized in that described solvent is toluene, hutanal or isobutylaldehyde.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2006101477352A CN1986055B (en) | 2006-12-22 | 2006-12-22 | Catalyst system and catalyzing method of propylene hydrogenation and formylation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2006101477352A CN1986055B (en) | 2006-12-22 | 2006-12-22 | Catalyst system and catalyzing method of propylene hydrogenation and formylation |
Related Child Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011101653567A Division CN102266796A (en) | 2006-12-22 | 2006-12-22 | Propylene hydroformylation catalyzing system and method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1986055A CN1986055A (en) | 2007-06-27 |
| CN1986055B true CN1986055B (en) | 2012-06-27 |
Family
ID=38183078
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2006101477352A Active CN1986055B (en) | 2006-12-22 | 2006-12-22 | Catalyst system and catalyzing method of propylene hydrogenation and formylation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1986055B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2018236623A1 (en) | 2017-06-19 | 2018-12-27 | Dow Technology Investments Llc | Processes for purifying ligands |
| EP4180439A1 (en) * | 2021-11-15 | 2023-05-17 | Evonik Operations GmbH | Method for reducing the chlorine content of organobisphosphites by means of inert gas frit |
Families Citing this family (25)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101835786A (en) * | 2007-11-06 | 2010-09-15 | 三菱化学株式会社 | Method of inhibiting metal precipitation from transition metal complex |
| DE102008043582A1 (en) | 2008-11-07 | 2010-05-12 | Evonik Oxeno Gmbh | Process for the preparation of 6-chlorodibenzo (d, f) (1,3,2) -dioxaphosphepin |
| DE102008043584A1 (en) | 2008-11-07 | 2010-05-12 | Evonik Oxeno Gmbh | Process for the preparation of 6-chlorodibenzo (d, f) (1,3,2) -dioxaphosphepin |
| RU2541537C2 (en) | 2009-03-31 | 2015-02-20 | Дау Текнолоджи Инвестментс Ллс | Method of hydroformylation by means of double open-end bisphosphite ligand |
| CN103153462B (en) * | 2010-10-05 | 2016-06-01 | 陶氏技术投资有限责任公司 | Hydroformylation process |
| DE102011002639A1 (en) | 2011-01-13 | 2012-07-19 | Evonik Oxeno Gmbh | Process for the preparation of biphephos |
| DE102011002640B4 (en) | 2011-01-13 | 2021-10-07 | Evonik Operations Gmbh | Process for the purification of Biphephos |
| EP2797938B8 (en) * | 2011-12-30 | 2017-08-30 | Basf Se | Method for producing 6-chlorodibenzo [d,f][1,3,2]dioxaphosphepin |
| EP2855016A1 (en) | 2012-06-04 | 2015-04-08 | Dow Technology Investments LLC | Hydroformylation process |
| CN103509055B (en) * | 2013-10-10 | 2016-08-17 | 中国海洋石油总公司 | A kind of microwave synthesis method of diphosphite three (3,3 '-di-t-butyl-5,5 '-dimethoxy-2,2 '-xenol) ester |
| CN105013537B (en) * | 2015-06-17 | 2017-11-03 | 天津渤化永利化工股份有限公司 | A kind of method for improving failure octyl alconyl oxo catalyst activity |
| US10077281B2 (en) | 2015-06-19 | 2018-09-18 | Dow Technology Investments Llc | Crystalline ligand |
| CN105541916A (en) * | 2015-10-29 | 2016-05-04 | 天津渤化永利化工股份有限公司 | Synthetic method of Lianfeifusi ligand |
| CN105294764A (en) * | 2015-11-11 | 2016-02-03 | 天津渤化永利化工股份有限公司 | Synthetic method of 2,2'-dis(benzo[d,f][1,3,2]dioxaphosphepin-6-oxygroup)-1,1'-biphenyl intermediate |
| CN105440081A (en) * | 2015-12-07 | 2016-03-30 | 中国海洋石油总公司 | Diphosphite synthesis method |
| CN105566081A (en) * | 2015-12-15 | 2016-05-11 | 上海华谊（集团）公司 | Method for preparing aldehyde through olefin hydroformylation |
| CN105801625B (en) * | 2016-05-30 | 2017-08-25 | 郑州大学 | The preparation method of bidentate phosphite ester ligand and its application in Buchwald Hartwig reactions |
| SE1730036A1 (en) * | 2017-02-09 | 2018-08-10 | Perstorp Ab | Carbonylation process and ligand composition |
| KR20210013702A (en) | 2018-05-30 | 2021-02-05 | 다우 테크놀로지 인베스트먼츠 엘엘씨. | How to slow the deactivation of the catalyst and/or slow the use of tetraphosphine ligands in the hydroformylation process |
| MX2020011380A (en) | 2018-05-30 | 2020-11-24 | Dow Technology Investments Llc | Methods of controlling hydroformylation processes. |
| JP2022539376A (en) | 2019-06-27 | 2022-09-08 | ダウ テクノロジー インベストメンツ リミティド ライアビリティー カンパニー | Process for preparing solutions from hydroformylation processes for precious metal recovery |
| CN114436792A (en) * | 2020-11-02 | 2022-05-06 | 中国石油化工股份有限公司 | Method for producing high-carbon aldehyde |
| CN114057791B (en) * | 2021-12-01 | 2023-12-19 | 万华化学集团股份有限公司 | Hydrolysis-resistant phosphite ligand, preparation method and application of phosphite ligand in preparation of linear aldehyde by catalyzing olefin hydroformylation reaction |
| CN114832860A (en) * | 2022-03-17 | 2022-08-02 | 江西苏克尔新材料有限公司 | Olefin hydroformylation catalyst composition and preparation method and application thereof |
| CN114773172B (en) * | 2022-06-20 | 2022-10-18 | 中海油天津化工研究设计院有限公司 | Optimization method of process for preparing aldehyde by olefin hydroformylation |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4733008A (en) * | 1986-08-23 | 1988-03-22 | Degussa Aktiengesellschaft | Process for the production of 1,12-dodecanoic diacid |
| CN1241993A (en) * | 1996-11-04 | 2000-01-19 | Dsm有限公司 | Process for the preparation of an aldehyde |
| CN1768944A (en) * | 2004-11-01 | 2006-05-10 | 中国科学院大连化学物理研究所 | Catalyst using phosphine-phosphoramidite ester as ligand, its preparation method and application |
-
2006
- 2006-12-22 CN CN2006101477352A patent/CN1986055B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4733008A (en) * | 1986-08-23 | 1988-03-22 | Degussa Aktiengesellschaft | Process for the production of 1,12-dodecanoic diacid |
| CN1241993A (en) * | 1996-11-04 | 2000-01-19 | Dsm有限公司 | Process for the preparation of an aldehyde |
| CN1768944A (en) * | 2004-11-01 | 2006-05-10 | 中国科学院大连化学物理研究所 | Catalyst using phosphine-phosphoramidite ester as ligand, its preparation method and application |
Non-Patent Citations (5)
| Title |
|---|
| JP特开2001-316321A 2001.11.13 |
| 蒋文等.磷配体在氢甲酰化反应中的应用.上海化工31 5.2006,31(5),30-34. |
| 蒋文等.磷配体在氢甲酰化反应中的应用.上海化工31 5.2006,31(5),30-34. * |
| 郭红超等.不对称催化氢化的新进展－－单齿磷配体的复兴.科学通报49 16.2004,49(16),1575-1588. |
| 郭红超等.不对称催化氢化的新进展--单齿磷配体的复兴.科学通报49 16.2004,49(16),1575-1588. * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2018236623A1 (en) | 2017-06-19 | 2018-12-27 | Dow Technology Investments Llc | Processes for purifying ligands |
| EP4180439A1 (en) * | 2021-11-15 | 2023-05-17 | Evonik Operations GmbH | Method for reducing the chlorine content of organobisphosphites by means of inert gas frit |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1986055A (en) | 2007-06-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1986055B (en) | Catalyst system and catalyzing method of propylene hydrogenation and formylation | |
| CN102266796A (en) | Propylene hydroformylation catalyzing system and method | |
| CN101288852B (en) | Catalyst composition for reaction of hydroformylation of propene, | |
| CN101332437A (en) | Butene hydroformylation catalyst composition and uses thereof | |
| CN103990495B (en) | Olefin hydroformylation catalyst | |
| KR102157915B1 (en) | Bidentate ligands for hydroformylation of ethylene | |
| KR930003936B1 (en) | Process for the production of aldehydes | |
| CN1972889A (en) | Method for hydroformylating olefins in the presence of organophosphoric compounds | |
| AU2507792A (en) | Asymmetric syntheses | |
| CN104058944A (en) | Method for preparing aldehyde through alkene hydroformylation reaction | |
| EP0019296A1 (en) | Process for removing triorganophosphine from a liquid composition | |
| TWI399364B (en) | Co-production method of normal butanol and isobutyl aldehyde | |
| Sutradhar et al. | Application of molybdenum complexes for the oxidation of cyclohexane in acetonitrile, ionic liquid and supercritical CO2 media, a comparative study | |
| CN101113154A (en) | Catalyst precursor for an Rh complex catalyst | |
| Kumar et al. | Hydroformylation of olefins by metals other than rhodium | |
| CN1909964B (en) | Phsphorus-containing catalyst composition and process for hydroformylation reaction using the same | |
| TWI813689B (en) | Methods for slowing deactivation of a catalyst and/or slowing tetraphosphine ligand usage in hydroformylation processes | |
| Naili et al. | Chiral aminophosphonite-phosphite ligands: synthesis and use in platinum-and rhodium-based enantioselective hydroformylation of styrene. Crystal structure of [(S)-N-(2, 2′ biphenoxyphosphino)-2-(2, 2′ biphenoxyphosphinoxymethyl) pyrrolidine] dichloroplatinum (II) | |
| Drommi et al. | An effective diphosphoramidite rhodium catalyst for selective hydroformylation of 1-octene | |
| Keglevich et al. | Hydroformylation of styrene in the presence of rhodium-2, 4, 6-trialkylphenyl-phosphole in situ catalytic systems | |
| Pàmies et al. | Rhodium cationic complexes using macrocyclic diphosphines as chiral ligands:: Application in asymmetric hydroformylation | |
| US4315867A (en) | Secondary and tertiary 2-carboxyethyl- and carboxymethylphosphines and the salts thereof, as well as their preparation and use | |
| Gerdin et al. | Enantioselective silicon–boron additions to cyclic 1, 3-dienes catalyzed by the platinum group metal complexes | |
| Tang et al. | Highly regioselective homogeneous isomerization-hydroformylation of 2-butene with water-and air-stable phosphoramidite bidentate ligand | |
| CN101306387A (en) | Stable catalyst precursor of rh complex catalysts |
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 | ||
| ASS | Succession or assignment of patent right |
Owner name: SHANGHAI HUAYI ENERGY + CHEMICAL INDUSTRY CO., LTD Free format text: FORMER OWNER: SHANGHAI COKING CO., LTD. Effective date: 20150331 |
|
| TR01 | Transfer of patent right |
Effective date of registration: 20150331 Address after: 200032 Shanghai city Xuhui District Fenglin Road No. 354 Patentee after: Shanghai Institute of Organic Chemistry, Chinese Academy of Sciences Patentee after: Shanghai Hua Yi derived energy chemical Co., Ltd Address before: 200032 Shanghai city Xuhui District Fenglin Road No. 354 Patentee before: Shanghai Institute of Organic Chemistry, Chinese Academy of Sciences Patentee before: Shanghai Coking Co., Ltd. |