CN1013195B - Synthesis of diphenyl carbonate - Google Patents
Synthesis of diphenyl carbonateInfo
- Publication number
- CN1013195B CN1013195B CN 86107665 CN86107665A CN1013195B CN 1013195 B CN1013195 B CN 1013195B CN 86107665 CN86107665 CN 86107665 CN 86107665 A CN86107665 A CN 86107665A CN 1013195 B CN1013195 B CN 1013195B
- Authority
- CN
- China
- Prior art keywords
- phenol
- grams
- reaction
- phosgene
- ph2co3
- 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.)
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention develops a method for synthesizing diphenyl carbonate (Ph2CO3). Industrial lime hydrate is used for replacing caustic soda to generate calcium phenoxide salt, and subsequently, phosgenation reaction is carried at room temperature, under normal pressure, at high speed and in a quantitative way to prepare O and Ph2CO3. Examples: mixed liquid of 152 grams of Ca (OH) 2, 700 grams of water and 350 grams of phenol is supplied with 195 grams of phosgene at the temperature of 30 to 40 DEG C within 60 minutes, the mixed liquid is neutral, and 396 grams of Ph2CO3 is obtained after the mixed liquid is separated and purified. Compared with a caustic alkali method, the unit consumption of the phenol and the phosgene is respectively and approximately reduced by 10% and 25%, the yield coefficient of the Ph2CO3 is 100%, the post processing is simple, discharged waste water contains no free phenol, and the present invention have obvious economic and social benefits as well as a more ideal technical effect. C07C93/14, C07C103/375, C07C275/06, C07D279/02, C07D209/44, C07D211/88, C07D221/20, C07D295/04, C07D471/10, C07D521/00, A61K31/135 and A61K31/395.
Description
The invention discloses a kind of diphenyl carbonate (Ph
2CO
3) synthetic method.
Ph
2CO
3It is the important source material of transesterify～melt-polycondensation polycarbonate synthesis.Also its synthesis of polyurethane, polyureas, polybenzoate or other synthetic resins be can pass through, and solvent or softening agent or the like can be used as.
Ph
2CO
3Synthetic method can be divided into phenyl chloroformate pyrolysis condensation method, phenol ester exchange process, phenol～catalyzing carbon monoxide synthesis method and phenolate light phosgenation four big classes.In addition, utilize the chemical reaction of other related compound, also may generate Ph
2CO
3(C.A.64,3389; C.A.95,180053).
Phenyl chloroformate pyrolysis condensation method (U.S.P.3,234,261; U.S.P.3,234,263) need by the prefabricated phenyl chloroformate of phenol, and alkaline auxiliary material consumes higher.Phenol ester exchange process (C.A.91,124012; C.A.97,109651; The spy opens clear 54-63,023; The spy opens clear 56-25,138; Ger.Pat.2,950,069; GerPatDE3,308,921) need prefabricated lower aliphatic carbonic diester, and transformation efficiency is lower; And the high person of transformation efficiency needs prefabricated carbonic acid two (neighbour-nitro) phenyl ester, and makes catalyzer with right-dimethyl aminopyridine, and is more unrealistic.Phenol～catalyzing carbon monoxide synthesis method (C.A.95,6682; The spy opens clear 55-92,732; U.S.P.4,349,485) be the research trend of significant, but do not obtain desired result as yet.Phenol phosgenation rule is still current raw material sources reality and reacts the economically viable practical plan that is easy to realize.Wherein phenol direct sunshine evaporating method (U.S.P.2,362,865) ties up under the katalysis of amphoteric metal or its salt, react in 180～250 ℃ of high temperature, and yield 90～98%, the dephenolize of still needing is refining; Phenol light phosgenation (C.A.89,197873 in containing the organic solution of pyridine; CzeCh.Pat157,282), crystallization yield only 88.5%, and need with benzene and need the regeneration pyridine; Light phosgenation in alkaliferous liquid～liquid two-phase system (GerPat2,509,036), the reaction times short (40 minutes), yield 99%, but need add tertiary amine or quaternary ammonium compound is made catalyzer, cause to wastewater treatment and bring new trouble.By the light phosgenation (U.S.P.2,335,441) of the phenol caustic solution of U.S. G.E. company early development, be the prior synthesizing method that widely adopts in the suitability for industrialized production, but this method processing condition harshness always, unit consumption is higher, and aftertreatment is difficulty also.
The objective of the invention is to develop a kind of new synthetic method,, improve operational condition, reduce unit consumption and simplify post-processing operation to overcome the deficiency that traditional synthesis exists.
The present invention is achieved by the following scheme: promptly under room temperature, normal pressure with a certain amount of phosgene (COCl
2) feed the phenol calcium salt ((PhO)
2Ca) carries out phosgenation reaction in the aqueous solution, thereby make purpose product P h
2CO
3, its reaction formula is as follows:
The aqueous solution of said here phenol calcium salt is by industrial hydrogen calcium oxide (or by the slaked lime behind the quicklime slaking) (containing Ca(OH)
285～95%) add and add that phenol generates behind the water furnishing pasty state again:
For realizing above-mentioned reaction, the molar ratio theoretical value of each material should be COCl
2: PhOH: Ca(OH)
2=0.5: 1: 0.5, for asking high-quality, high yield, low consumption, actual molar ratio was got COCl
2: PhOH: Ca(OH)
2=(0.5+m): 1: (0.5+2m), m 〉=0, preferably m=0.01～0.05.At first with industrial slaked lime (containing Ca(OH)
285～95%) add the even soup compound of furnishing, add the phenol and the (H that stirs then
2O: PhOH=1.8～5: 1(Wt%)), keep 20～45 ℃ of temperature of reaction, best 30～40 ℃, in 30～300 minutes best 45～120 minutes, led to phosgene to reaction system when being neutral and can't check free phenol, phosgenation reaction is promptly accused and is finished.
In the phosgenation reaction process there be main side reaction:
The CaCO that generates
3Available hcl acidifying makes it to generate solubility chlorination calcium (CaCl
2) and and Ph
2CO
3Separate, also can be when underpressure distillation as still residual and Ph
2CO
3Separate.Thereby after phosgenation reaction finishes, but both direct filtration of its aftertreatment, underpressure distillation is to obtain Ph
2CO
3, also available hydrochloric acid acidizing reaction product, and then filter, separate its acid mother liquid, washing leaching cake, drying, underpressure distillation make Ph again
2CO
3Its mother liquor through desulfating, deironing, decolour, anhydrate after recyclable industrial calcium chloride.A small amount of wash water and mother liquor merge to be handled, and wash water can be made the proportioning process water in the neutral, to reduce quantity discharged.The end wash water only contains small amount of calcium chloride, can directly discharge.
Though this reaction can any ratio be carried out, can cause or certain reactant surplus, or certain reactant deficiency, can not obtain better result.For obtaining low unit consumption, high yield, the mole that feeds intake of three kinds of reactants is preferably got COCl
2: PhOH: Ca(OH)
2=(0.5+m): 1: (0.5+2m), and m=0.01～0.05; The phenol calcium salt may crystallization be separated out when temperature of reaction was too low, when too high the alkaline hydrolysis side reaction serious, preferably get 30～40 ℃; Logical COCl
2Speed makes COCl too soon easily
2Escape, reduced spatiotemporal efficiency too slowly and side reaction is increased, thereby be preferably in and led to the specified amount phosgene in 45～120 minutes.Mol ratio Ca(OH)
2During/PhOH=0.54, the phosgenation reaction temperature t (℃) to Ph
2CO
3Yield y(%) influence is shown below:
Y＝245.2-114.55（t/10）+30.45（t/10）
2-2.8（t/10）
3
The industrial hydrogen calcium oxide both can once add or add continuously, also can be in two batches or many batches of addings, and the latter is than the former best results.Because Ca(OH under temperature of reaction)
2Solubleness in water only 0.14～0.15%(wt%) is by time processing industry slaked lime, excessive partial C a(OH)
2The Ph that particle is easily separated out by phosgenation reaction
2CO
3Wrap, both influenced Ca(OH)
2The performance of effect influences its consumption again, also makes filter cake be difficult to be washed till neutrality.Add slaked lime in batches, just can guarantee to separate out Ph in phosgenation
2CO
3Main phase, do not have excessive Ca(OH)
2Exist, also just solved Ca(OH)
2By Ph
2CO
3The problem of parcel.Thereby another embodiment of the present invention is: processing industry slaked lime in batches.For guaranteeing to make phenol all change into Ph below 40 ℃
2CO
3Minimum Ca(OH)
2/ PhOH mol ratio total value N and photochemical to pH=7 and can't check the time-consuming τ of free phenol institute (hour) relational expression as follows:
N＝0.54+0.01τ
By this scheme, at first 90～95% industrial hydrogen calcium oxide of required total amount is blunged into and adds the liquefied carbolic acid of total amount again behind the even pasty state and keep stirring, then at 20～45 ℃, be preferably in 30～40 ℃ down logical phosgene carry out phosgenation reaction.When the pH of reaction system≤9, supply the industrial hydrogen calcium oxide by total amount, stirred for several minute follow-up logical phosgene to pH=7, the sampling of system adds the bromine water detection, if remaining phenol is arranged, then drink processing industry calcium hydroxide, stirring again, logical phosgene is to pH=7.0 and can't check free phenol again, reaction was finished in 30～300 minutes.Carry out aftertreatment then.
Press such scheme, phosgenation reaction is basically identical as a result: Ph
2CO
3Crude product yield (be undistilled product amount behind the filtration cakes torrefaction, in phenol) reaches 100 ± 0.5%, 79.5 ± 1 ℃ of fusing points, and the rate that distillates～99% of underpressure distillation, full fraction all can be used for transesterify～melt-polycondensation polycarbonate synthesis.Press the difference of polycondensation end control, the molecular weight of gained resin is between 2.8～50,000.Stillage residue is loose shape, very easily deslagging after the underpressure distillation.
The present invention compares with traditional phenol caustic solution light phosgenation, has the following advantages:
1. remarkable economic efficiency:
(1), the price of industrial hydrogen calcium oxide only reaches 1/10th of caustic soda, and consumption only is 65% of a caustic soda;
(2), the price of by product industrial calcium chloride is 15 times of Industrial Salt, its recovery value is suitable with former alkali valency;
(3), the unit consumption of phenol can reduce about 10%;
(4), the unit consumption of phosgene can reduce about 25%;
By this method synthetic Ph
2CO
3Its total cost reduces about 25% than causticity alkaline process.
2. good social benefit:
Because phenol can change into Ph fully
2CO
3, and CaCl in the mother liquor
2Content both can directly be used as chilled brine up to 20%, recyclable again calcium chloride, and can not contain phenol in institute's effluent, only contain a small amount of CaCl
2, no longer need special processing.
3. better technological effect:
(1), the phosgenation temperature can bring up to 20～45 ℃ by 15～20 ℃ of traditional technology, can not re-use chilled brine;
(2), the phosgenation time can shorten to 1～2 hour by common 4～10 hours, shortened the operational cycle exponentially;
(3), the pH value of reaction mass by～14 reduce to～11, help suppressing various alkaline hydrolysis side reactions;
(4), PH
2CO
3Filter cake moisture content only 31 ± 4%, and be the porousness particulate, be easy to wash most water-soluble impurity;
(5), the underpressure distillation still is residual is loose powdery, is easy to discharging.
(6), PH
2CO
3The inner quality of product is more guaranteed, and the tendency that generates phenyl chloroformate during building-up reactions difficulty is again discovered, and phenol conversion is complete, and the full fraction of underpressure distillation all is suitable for transesterify～synthetic usefulness of melt-polycondensation polycarbonate.
Below in conjunction with embodiment this invention is further described, among the embodiment,
Filter cake moisture content=(wet cake weight-drying back filter cake weight)/(wet cake weight) * 100%
Crude product yield=(the thick Ph of 2 * gained
2CO
3Mole number)/(add PhOH mole number) * 100%
Embodiment one
In 1 liter of three mouthfuls of balloon flask of attached agitator, add industrial hydrogen calcium oxide 166.2 grams (91.2% Ca(OH)
2), 700 milliliters in water stirs into and adds 350 gram phenol behind the pasty state again, continues to be stirred to even soup compound, and keeping temperature of reaction is 28～38 ℃, logical while stirring phosgene (～3 Grams Per Minute).System pH=7 when phosgenation reaction is total to 60 minutes consuming time stops logical phosgene, adds 36% hydrochloric acid and makes its acidifying for 40 milliliters, filters the collection filter cake then and also washs.The total micro-alkaline pH ≈ 8 of filter cake after washing repeatedly, filter cake weight in wet base 562 gram, 24 hours constant weights of 65 ℃ of dryings are 396.8 grams, promptly the filter cake moisture content be 29.4%, crude product yield 99.6%.Fusing point is 77～78 ℃.It is granular that product is white powder.Wash water and mother liquor merge, and sampling adds the bromine water inspection trace phenol, and processing industry calcium hydroxide 2 grams can't check in free phenol, the mother liquor its logical phosgene in alkalization back a moment to pH=7, filtration, the filtrate again and reclaim Ph
2CO
32.4 gram.
Embodiment two
In 1 liter of three mouthfuls of round-bottomed flask of a belt stirrer, add and contain Ca(OH)
285.0% industrial hydrogen calcium oxide 154 grams, 700 milliliters in water, phenol 350 restrain, stir into even soup compound, keep 35～40 ℃ of temperature of reaction, logical while stirring phosgene (～3 Grams Per Minute), about 40 minutes pH values are reduced to by～11 and were stopped logical phosgene at 8 o'clock, add industrial hydrogen calcium oxide 24.4 grams, stir 5 minutes follow-up logical phosgene to pH=7.Phosgenation about 60 minutes consuming time altogether.Add 36% hcl acidifying to no longer producing CO
2Bubble and pH＜2 are consumed 50 milliliters altogether.Filter then, wash.Filter cake is washed till pH=7 easily, and washes out and can't check calcium salt, filter cake weight in wet base 613 grams in the water again, 65 ℃ down dry 24 hours constant weights be 400 grams, promptly the filter cake moisture content is 34.8%, white powder granulous Ph
2CO
3Crude product yield 100.5%, 80～81 ℃ of fusing points.Wash water and mother liquor merge, and count 800 milliliters, sampling, to add bromine water detection phenol be tracer level; Processing industry slaked lime 2 gram makes alkalization back logical phosgene pH=7 in a moment, and acidifying, filtration can't check free phenol again in the filtrate, and filter Ph
2CO
3Only～0.1 restrain.
The neutral wash water of pH=7 gives over to down still batching water for 700 milliliters, to reduce blowdown flow rate.
Embodiment three
With Ca(OH)
2Content is 700 milliliters of even soup compounies of furnishing of neutral wash water of 85.0% industrial hydrogen calcium oxide, 154 grams, phenol 350 grams, embodiment 2, keep 30～40 ℃, logical while stirring phosgene (～4 Grams Per Minute), about 30 minutes pH values reduce to 7 by～11, add and renew logical phosgene behind above-mentioned industrial hydrogen calcium oxide 21.2 grams and reduce to 7 once again, 45 minutes consuming time altogether to pH.Sampling adds the bromine water detection still free phenol, adds above-mentioned industrial hydrogen calcium oxide 3.2 grams again, and logical again phosgene reduces to 7 once again to pH, and 2 minutes consuming time again, sampling analysis can't check free phenol again.Add 50 milliliters of acidifyings of 36% hydrochloric acid half an hour, filter, washing, drying.
800 milliliters of acid mother liquids, detection phenol are tracer level.
700 milliliters of the middle wash waters of pH～7 give over to down still batching water.
Wet cake weight is 595 grams, dry back constant weight 399.5 grams, and promptly moisture content is 32.9%, Ph
2CO
3Crude product yield 100.3%, 79.5～80.5 ℃ of fusing points.
Embodiment four
It is identical with example 3 to prepare burden, and the neutral wash water of use-case 3 makes the technology water, and logical phosgene speed is～1.5 Grams Per Minutes, and 100 minutes pH reduce to 7 in 36～40 ℃ of phosgenations.Divide and add industrial hydrogen calcium oxide totally 34.4 grams for 4 times, phenol is all transformed, totally 120 minutes consuming time of phosgenation, acidifying increases to 60 milliliters with 36% hydrochloric acid content.
Can't check free phenol in the mother liquor.
Filter cake moisture content 34.0%, pH
2CO
3Crude product yield 100.0%, 78.5～79.5 ℃ of fusing points.
Embodiment five
The Ca(OH of used industrial hydrogen calcium oxide)
2Content is 91.2%, granularity 70～90 orders.To go up an industrial hydrogen calcium oxide 151.1 grams, 700 milliliters in phenol 350 grams, water are deployed into even soup compound.Keep 30～26 ℃, logical while stirring phosgene (～2 Grams Per Minute), pH reduced to 9 in about 70 minutes, add the logical phosgene in above-mentioned industrial hydrogen calcium oxide 15.1 gram backs to pH=7, still can detect free phenol, so add above-mentioned industrial hydrogen calcium oxide 3.0 grams again, mend logical phosgene again and reduce to 7 once again to pH, and can't check free phenol.Phosgenation 100 minutes consuming time altogether.Add 45 milliliters of acidifyings of hydrochloric acid of 36%, filter, wash.
Can detect the free phenol of tracer level in the acid mother liquid.
Filter cake moisture content 27.4%, PH
2CO
3Crude product yield 99.5%, 78.5～79.5 ℃ of fusing points.
More than all routine gained Ph
2CO
3Crude product promptly gets pure Ph through simple underpressure distillation
2CO
3, its rate of distillating reaches～and 99%, wherein positive fraction accounts for and distillates more than 92% of total amount; The liquid chromatography comparative analysis, it is formed and former elaboration Ph
2CO
3Unanimity, and purity is slightly high.Account for and distillate the foreshot of total amount below 8%, melt is colourless, and is transparent, and detected result only phenol content is slightly higher than positive fraction.Foreshot, positive fraction fusing point all is 80～81 ℃, all the other every indexs are all qualified.It is as follows to beat sample polycarbonate synthesis result with transesterify～melt-polycondensation: (table is seen the literary composition back)
The result finds out from polycondensation: this law synthetic Ph
2CO
3, its foreshot, positive fraction all can be used as transesterify～melt polycondensation reaction.
During underpressure distillation, only otherwise reach the destructive distillation degree, just can guarantee that colourless, transparent, the full fraction of overhead product melt all can be used for polycarbonate synthesis.The last destructive distillation fraction of underpressure distillation only accounts for 0.3%, and yellow, fusing point＜49 ℃ mainly are high-temperature split product phenol and Ph
2CO
3The residual amount of retort only 1.4% is the loose powdery of beige, very easily discharges, and it consists of: sand 32%, CaCO
337%, CaCl
223%, Ph
2CO
38%, (PhO) of trace
2Ca.
Preface Ph
2CO
3Polycondensation molecular weight remarks
Source M, P, eventually warm time
Number (℃) (℃) (hr) (ten thousand)
1 embodiment, 2 positive fraction 80～81 300 2 3.87 resin synthesis conditions
2 embodiment, 3 positive fraction 80～81 310 2 5.22 proportionings: Ph
2CO
339.5 gram, the BPA40.0 gram,
3 embodiment, 1～5 foreshot 80～81 310 1.5 5.13 NaBPh
40.085 gram
4 embodiment, 1～5 foreshot 80～81 290 1 2.82 transesterifys: 140～10 torrs
175～230 ℃ 2 hours
Elaboration 79.5～80.5 290 1.5 2.92 polycondensations of 5 length weathering factories:＜1 torr,, stir motionless by 230 ℃～warm eventually
Claims (7)
1, the synthetic method of diphenyl carbonate is to make the aqueous solution of phenolate carry out phosgenation reaction, it is characterized in that used phenolate is the phenol calcium salt that is generated by calcium hydroxide and phenol reactant, the molar ratio COCl of reaction mass
2: PhOH: Ca (OH)
2=(0.5+m): 1: (0.5+2m), m 〉=0, preferably m=0.01～0.05.
2, synthetic method according to claim 1 is characterized in that calcium hydroxide preferably in two batches or many batches of addings, also can disposable adding or add continuously.
3, according to claim 1,2 described synthetic methods, the terminal point that it is characterized in that phosgenation reaction is neutral and can't check free phenol with reaction system and is as the criterion; Otherwise, should drink and mend logical phosgene again till can't check free phenol after mending calcium hydroxide.
4, according to claim 1,2 described synthetic methods is characterized in that the phosgenation reaction time is 30～300 minutes, are preferably 45～120 minutes.
5,, it is characterized in that the phosgenation reaction temperature is 20～45 ℃, preferably 30～40 ℃ according to claim 1,2 described synthetic methods.
6, according to claim 1,2 described synthetic methods, but it is characterized in that phosgenation reaction finish after direct filtration, underpressure distillation, but preferably add hcl acidifying earlier, filter then, wash, drying again underpressure distillation get Ph
2CO
3
7, synthetic method according to claim 7, the mother liquor after it is characterized in that separating are through purifying treatment, and industrial calcium chloride is reclaimed in the dehydration back, and the neutral wash water can be made the technology water.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 86107665 CN1013195B (en) | 1986-12-28 | 1986-12-28 | Synthesis of diphenyl carbonate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 86107665 CN1013195B (en) | 1986-12-28 | 1986-12-28 | Synthesis of diphenyl carbonate |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN86107665A CN86107665A (en) | 1988-08-17 |
| CN1013195B true CN1013195B (en) | 1991-07-17 |
Family
ID=4803637
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 86107665 Expired CN1013195B (en) | 1986-12-28 | 1986-12-28 | Synthesis of diphenyl carbonate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1013195B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4292210B2 (en) * | 2004-08-25 | 2009-07-08 | 旭化成ケミカルズ株式会社 | Industrial production method of high purity diphenyl carbonate |
| US20080064846A1 (en) * | 2004-09-03 | 2008-03-13 | Shinsuke Fukuoka | Industrial Process for Production of High-Purity Diaryl Carbonate |
| CN103086562B (en) * | 2011-11-01 | 2015-02-18 | 上海博丹环境工程技术有限公司 | Phenolic resin wastewater processing method and special-purposed device |
-
1986
- 1986-12-28 CN CN 86107665 patent/CN1013195B/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| CN86107665A (en) | 1988-08-17 |
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