CN102911015A - Di-(2-hydroxyl isopropyl) benzene production method - Google Patents
Di-(2-hydroxyl isopropyl) benzene production method Download PDFInfo
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- CN102911015A CN102911015A CN2011102215625A CN201110221562A CN102911015A CN 102911015 A CN102911015 A CN 102911015A CN 2011102215625 A CN2011102215625 A CN 2011102215625A CN 201110221562 A CN201110221562 A CN 201110221562A CN 102911015 A CN102911015 A CN 102911015A
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Abstract
The invention relates to a di-(2-hydroxyl isopropyl) benzene production method which mainly solves the problems of long technical process and excessive public project consumption in the prior art. The technical scheme for better solving the problems includes that the method includes the steps: 1) allowing reducing agent and material flow containing di-(hydrogen peroxide isopropyl) benzene to enter a reduction reactor, and obtaining material flow I by means of reduction reaction of the di-(hydrogen peroxide isopropyl) benzene and the reducing agent in the reduction reactor; 2) allowing the material flow I and solvent to enter a crystalline region to obtain material flow II after crystallization; and 3) allowing the material flow II to enter a separation region to obtain the di-(2-hydroxyl isopropyl) benzene after separation. The di-(2-hydroxyl isopropyl) benzene production method can be used for industrial production of di-(2-hydroxyl isopropyl) benzene.
Description
Technical field
The present invention relates to a kind of production method of two-(2-hydroxyl sec.-propyl) benzene.
Background technology
Two-(2-hydroxyl sec.-propyl) benzene (DC) are the intermediates of producing two-(tert-butyl peroxy sec.-propyl) benzene (BIPB).Document US 7557252 " Process for Producing Dihydroxybenzene and Diisopropylbenzenedicarbinol " discloses the diisopropylbenzene(DIPB) oxidation solution of-(hydrogen peroxide sec.-propyl) benzene (DHP) two to contain as raw material, extract two-(hydrogen peroxide sec.-propyl) benzene with methyl iso-butyl ketone (MIBK), then carry out decomposition reaction, carry out hydrogenation reduction, crystallization makes two-(2-hydroxyl sec.-propyl) benzene in methyl iso-butyl ketone (MIBK) at last again.
But the technological process for preparing two-(2-hydroxyl sec.-propyl) benzene in the above-mentioned document adopts four unit operation steps such as extraction, decomposition, reduction, crystallization, has the problem that technical process is long, general facilities consumption is many.
Summary of the invention
Technical problem to be solved by this invention is that prior art exists the problem that technical process is long, general facilities consumption is many, and a kind of production method of two-(2-hydroxyl sec.-propyl) benzene newly is provided.It is simple that the method has technical process, and general facilities consumes low characteristics.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of production method of two-(2-hydroxyl sec.-propyl) benzene may further comprise the steps:
1) logistics and the reductive agent that contain two-(hydrogen peroxide sec.-propyl) benzene enter reduction reactor, and two-(hydrogen peroxide sec.-propyl) benzene and reductive agent generation reduction reaction obtains the logistics I in reduction reactor; Described reductive agent is selected from least a in Sulfothiorine, Potassium Thiosulphate, potassium sulphide, potassium hydrogen sulfide, sodium sulphite or the sodium bisulfide;
2) logistics I and solvent enter crystallizing field, obtain the logistics II after the crystallization; Described solvent is selected from least a in phenyl ethyl ether, isopropyl ether, benzylalcohol, phenylethyl alcohol or the diisopropylbenzene(DIPB);
3) logistics II enters the disengaging zone, obtains product two-(2-hydroxyl sec.-propyl) benzene after the separation.
In the technique scheme, temperature of reaction is 40～200 ℃ in the reduction reactor, and preferable range is 120～180 ℃; Reaction pressure is 0.2～1.0MPa, and preferable range is 0.7～0.8MPa; The weight ratio of two-(hydrogen peroxide sec.-propyl) benzene and reductive agent is (1～30): (1～20), preferable range are (7～20): (5～15).The inventive method preferred version is that described crystallizing field comprises the first crystallizing field and the second crystallizing field, and described disengaging zone comprises the first disengaging zone and the second disengaging zone; The logistics I enters the first crystallizing field, obtains the logistics III after the crystallization; The logistics III enters the first disengaging zone, after centrifugation, obtains the first mother liquor and logistics IV; Logistics IV and solvent enter the second crystallizing field, obtain the logistics II after the crystallization; The logistics II enters the second disengaging zone, after centrifugation, obtains the second mother liquor and product two-(2-hydroxyl sec.-propyl) benzene; The first mother liquor and the second mother liquor enter follow-up flow process.The first crystallizing field service temperature is 20～120 ℃, and preferable range is 60～100 ℃; Working pressure is 0.1～0.8MPa, and preferable range is 0.5～0.6MPa.The second crystallizing field service temperature is 20～120 ℃, and preferable range is 60～100 ℃; Working pressure is 0.1～0.8MPa, and preferable range is 0.4～0.5MPa.Contain two-(hydrogen peroxide sec.-propyl) logistics of benzene and the weight ratio of solvent and be (6～8): (1～3).Described reductive agent preferred version is to be selected from least a in Sulfothiorine or the potassium sulphide.Described solvent preferred version is to be selected from least a in phenyl ethyl ether or the diisopropylbenzene(DIPB).The described logistics that contains two-(hydrogen peroxide sec.-propyl) benzene is for containing the diisopropylbenzene(DIPB) oxidation solution of two-(hydrogen peroxide sec.-propyl) benzene, and wherein the content of two-(hydrogen peroxide sec.-propyl) benzene is 10～20 % by weight.
In the inventive method, described reaction pressure all refers to gauge pressure.
The inventive method need not to extract and decomposition course, be selected from least a for reductive agent in Sulfothiorine, Potassium Thiosulphate, potassium sulphide, potassium hydrogen sulfide, sodium sulphite or the sodium bisulfide by employing, diisopropylbenzene(DIPB) oxidation solution and the reductive agent generation reduction reaction that directly will contain two-(hydrogen peroxide sec.-propyl) benzene, after Crystallization Separation, just can obtain two-(2-hydroxyl sec.-propyl) benzene, simplify technical process, reduced the consumption of general facilities.Adopt the inventive method, the refrigerated water consumption of producing 1 ton two-(2-hydroxyl sec.-propyl) benzene DC drops to 40 tons of the present invention by 50 tons of prior art, recirculated water consumption drops to 280 tons of the present invention by 350 tons of prior art, steam consumption drops to 3.1 tons of the present invention by 4.0 tons of prior art, power consumption drops to 375kWh of the present invention by the 450kWh of prior art, has obtained preferably technique effect.
Description of drawings
Fig. 1 is the inventive method schematic flow sheet.
Among Fig. 1,1 is reduction reactor, 2 is the first crystallizing field, 3 is the second crystallizing field, 4 is the first disengaging zone, 5 is the second disengaging zone, and 6 is solvent, and 7 is reductive agent, 8 for containing the logistics of two-(hydrogen peroxide sec.-propyl) benzene, 9 is product two-(2-hydroxyl sec.-propyl) benzene, and 10 is the first mother liquor, and 11 is the second mother liquor, the logistics I is the logistics that flows out from reduction reactor, the logistics II is the logistics that flows out from crystallizing field, and the logistics III is the logistics that flows out from the first crystallizing field, and the logistics IV is the logistics that flows out from the first disengaging zone.
Among Fig. 1, the logistics 8 and the reductive agent 7 that contain two-(hydrogen peroxide sec.-propyl) benzene enter reduction reactor 1, and two-(hydrogen peroxide sec.-propyl) benzene and reductive agent generation reduction reaction obtains the logistics I in reduction reactor 1.The logistics I enters the first crystallizing field 2, obtains the logistics III after the crystallization.The logistics III enters the first disengaging zone 4, after centrifugation, obtains the first mother liquor 10 and logistics IV.Logistics IV and solvent 6 enter the second crystallizing field 3, obtain the logistics II after the crystallization.The logistics II enters the second disengaging zone 5, after centrifugation, obtains the second mother liquor 11 and product two-(2-hydroxyl sec.-propyl) benzene 9; The first mother liquor 10 and the second mother liquor 11 enter follow-up flow process.
The present invention is further elaborated below by embodiment.
Embodiment
[embodiment 1]
Adopt flow process shown in Figure 1, the logistics 8 and the reductive agent 7 that contain two-(hydrogen peroxide sec.-propyl) benzene enter reduction reactor 1, and two-(hydrogen peroxide sec.-propyl) benzene and reductive agent generation reduction reaction obtains the logistics I in reduction reactor 1.The logistics I enters the first crystallizing field 2, obtains the logistics III after the crystallization.The logistics III enters the first disengaging zone 4, after centrifugation, obtains the first mother liquor 10 and logistics IV.Logistics IV and solvent 6 enter the second crystallizing field 3, obtain the logistics II after the crystallization.The logistics II enters the second disengaging zone 5, after centrifugation, obtains the second mother liquor 11 and product two-(2-hydroxyl sec.-propyl) benzene 9; The first mother liquor 10 and the second mother liquor 11 enter follow-up flow process.
Contain the logistics of two-(hydrogen peroxide sec.-propyl) benzene for containing the diisopropylbenzene(DIPB) oxidation solution of two-(hydrogen peroxide sec.-propyl) benzene, wherein the content of two-(hydrogen peroxide sec.-propyl) benzene is 15.33 % by weight.In the reduction reactor, 180 ℃ of temperature of reaction, under the reaction pressure 0.8MPa condition, two-(hydrogen peroxide sec.-propyl) benzene and the reaction of reductive agent Sulfothiorine obtain two-(2-hydroxyl sec.-propyl) benzene; Wherein, the weight ratio of two-(hydrogen peroxide sec.-propyl) benzene and reductive agent Sulfothiorine is 10: 7.The first crystallizing field working pressure is 0.6MPa, and service temperature is 100 ℃.The second crystallizing field working pressure is 0.5MPaG, and service temperature is 100 ℃; Solvent is phenyl ethyl ether, and containing two-logistics of (hydrogen peroxide sec.-propyl) benzene and the weight ratio of solvent benzol ether is 6: 1.
The purity of product two-(2-hydroxyl sec.-propyl) benzene 9 is 85.1% (weight).
General facilities consumption is: refrigerated water consumes 40 tons of/ton DC, and recirculated water consumes 280 tons of/ton DC, 3.1 tons of/ton DC of steam consumption, power consumption 375kWh/ ton DC.
[embodiment 2]
With [embodiment 1], just reductive agent is potassium sulphide, and the weight ratio of two-(hydrogen peroxide sec.-propyl) benzene and potassium sulphide is 10: 8.
The purity of product two-(2-hydroxyl sec.-propyl) benzene 9 is 85.1% (weight).
General facilities consumption is: refrigerated water consumes 39 tons of/ton DC, and recirculated water consumes 275 tons of/ton DC, 3.0 tons of/ton DC of steam consumption, power consumption 365kWh/ ton DC.
[embodiment 3]
With [embodiment 1], be in the reduction reactor, 120 ℃ of temperature of reaction, reaction pressure 0.7MPa.The first crystallizing field working pressure is 0.5MPa, and service temperature is 60 ℃.The second crystallizing field working pressure is 0.45MPaG, and service temperature is 60 ℃
The purity of product two-(2-hydroxyl sec.-propyl) benzene 9 is 85.1% (weight).
General facilities consumption is: refrigerated water consumes 41 tons of/ton DC, and recirculated water consumes 287 tons of/ton DC, 3.2 tons of/ton DC of steam consumption, power consumption 388kWh/ ton DC.
[comparative example 1]
Produce two-(2-hydroxyl sec.-propyl) benzene according to document US 7557252 disclosed methods, its technological process adopts four unit operation steps such as extraction, decomposition, reduction, crystallization.
Take the oxidation solution of pure position diisopropylbenzene(DIPB) or pure contraposition diisopropylbenzene(DIPB) as raw material, at first extract two-(hydrogen peroxide sec.-propyl) benzene with methyl iso-butyl ketone (MIBK); Next two-(hydrogen peroxide sec.-propyl) benzene decomposes under acidic conditions and generation reduction reaction generation two-(2-hydroxyl sec.-propyl) benzene under the effect of reductive agent hydrogen, the temperature of its reduction reaction is 280 ℃, pressure is 3.0MPa, and hydrogen is 200: 1 with the volume ratio of two-(hydrogen peroxide sec.-propyl) benzene; Go out two-(2-hydroxyl sec.-propyl) benzene with the methyl iso-butyl ketone (MIBK) crystallization at last.
The purity of product two-(2-hydroxyl sec.-propyl) benzene 9 is 85.0% (weight).
General facilities consumption is: refrigerated water consumes 50 tons of/ton DC, and recirculated water consumes 350 tons of/ton DC, 4.0 tons of/ton DC of steam consumption, power consumption 450kWh/ ton DC.
Claims (9)
1. the production method of one kind two-(2-hydroxyl sec.-propyl) benzene may further comprise the steps:
1) logistics and the reductive agent that contain two-(hydrogen peroxide sec.-propyl) benzene enter reduction reactor, and two-(hydrogen peroxide sec.-propyl) benzene and reductive agent generation reduction reaction obtains the logistics I in reduction reactor; Described reductive agent is selected from least a in Sulfothiorine, Potassium Thiosulphate, potassium sulphide, potassium hydrogen sulfide, sodium sulphite or the sodium bisulfide;
2) logistics I and solvent enter crystallizing field, obtain the logistics II after the crystallization; Described solvent is selected from least a in phenyl ethyl ether, isopropyl ether, benzylalcohol, phenylethyl alcohol or the diisopropylbenzene(DIPB);
3) logistics II enters the disengaging zone, obtains product two-(2-hydroxyl sec.-propyl) benzene after the separation.
2. the production method of described two-(2-hydroxyl sec.-propyl) benzene according to claim 1, it is characterized in that temperature of reaction is 40～200 ℃ in the reduction reactor, reaction pressure is 0.2～1.0MPa, and the weight ratio of two-(hydrogen peroxide sec.-propyl) benzene and reductive agent is (1～30): (1～20).
3. the production method of described two-(2-hydroxyl sec.-propyl) benzene according to claim 2, it is characterized in that temperature of reaction is 120～180 ℃ in the reduction reactor, reaction pressure is 0.7～0.8MPa, and the weight ratio of two-(hydrogen peroxide sec.-propyl) benzene and reductive agent is (7～20): (5～15).
4. the production method of described two-(2-hydroxyl sec.-propyl) benzene according to claim 1 is characterized in that described crystallizing field comprises the first crystallizing field and the second crystallizing field, and described disengaging zone comprises the first disengaging zone and the second disengaging zone; The logistics I enters the first crystallizing field, obtains the logistics III after the crystallization; The logistics III enters the first disengaging zone, after centrifugation, obtains the first mother liquor and logistics IV; Logistics IV and solvent enter the second crystallizing field, obtain the logistics II after the crystallization; The logistics II enters the second disengaging zone, after centrifugation, obtains the second mother liquor and product two-(2-hydroxyl sec.-propyl) benzene; The first mother liquor and the second mother liquor enter follow-up flow process.
5. the production method of described two-(2-hydroxyl sec.-propyl) benzene according to claim 4 is characterized in that the first crystallizing field service temperature is 20～120 ℃, and working pressure is 0.1～0.8MPa; The second crystallizing field service temperature is 20～120 ℃, and working pressure is 0.1～0.8MPa.
6. the production method of described two-(2-hydroxyl sec.-propyl) benzene according to claim 5 is characterized in that the first crystallizing field service temperature is 60～100 ℃, and working pressure is 0.5～0.6MPa; The second crystallizing field service temperature is 60～100 ℃, and working pressure is 0.4～0.5MPa.
7. the production method of described two-(2-hydroxyl sec.-propyl) benzene according to claim 1, it is characterized in that containing two-(hydrogen peroxide sec.-propyl) logistics of benzene is (6～8) with the weight ratio of solvent: (1～3).
8. the production method of described two-(2-hydroxyl sec.-propyl) benzene according to claim 1 is characterized in that described reductive agent is selected from least a in Sulfothiorine or the potassium sulphide, and described solvent is selected from least a in phenyl ethyl ether or the diisopropylbenzene(DIPB).
9. the production method of described two-(2-hydroxyl sec.-propyl) benzene according to claim 1, it is characterized in that the described logistics that contains two-(hydrogen peroxide sec.-propyl) benzene for containing the diisopropylbenzene(DIPB) oxidation solution of two-(hydrogen peroxide sec.-propyl) benzene, wherein the content of two-(hydrogen peroxide sec.-propyl) benzene is 10～20 % by weight.
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1093352A (en) * | 1993-03-31 | 1994-10-12 | 兰州大学 | The manufacture method of 2-phenyl-2-propyl alcohol |
| JP2007246512A (en) * | 2006-02-17 | 2007-09-27 | Sumitomo Chemical Co Ltd | Production method for dihydroxybenzene and diisopropylbenzene dicarbinol |
| US7557252B2 (en) * | 2006-02-17 | 2009-07-07 | Sumitomo Chemical Company, Limited | Process for producing dihydroxybenzene and diisopropylbenzendicarbinol |
| CN101544587A (en) * | 2009-04-30 | 2009-09-30 | 湖南以翔化工有限公司 | Preparation method of alpha, alpha'-bis(tert-butyl peroxy) diisopropylbenzene |
| CN102040482A (en) * | 2009-10-13 | 2011-05-04 | 中国石油化工股份有限公司 | Method for preparing alpha, alpha-dimethyl benzyl alcohol by hydrogenating hydrogen dioxide isopropyl benzene |
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2011
- 2011-08-04 CN CN201110221562.5A patent/CN102911015B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1093352A (en) * | 1993-03-31 | 1994-10-12 | 兰州大学 | The manufacture method of 2-phenyl-2-propyl alcohol |
| JP2007246512A (en) * | 2006-02-17 | 2007-09-27 | Sumitomo Chemical Co Ltd | Production method for dihydroxybenzene and diisopropylbenzene dicarbinol |
| US7557252B2 (en) * | 2006-02-17 | 2009-07-07 | Sumitomo Chemical Company, Limited | Process for producing dihydroxybenzene and diisopropylbenzendicarbinol |
| CN101544587A (en) * | 2009-04-30 | 2009-09-30 | 湖南以翔化工有限公司 | Preparation method of alpha, alpha'-bis(tert-butyl peroxy) diisopropylbenzene |
| CN102040482A (en) * | 2009-10-13 | 2011-05-04 | 中国石油化工股份有限公司 | Method for preparing alpha, alpha-dimethyl benzyl alcohol by hydrogenating hydrogen dioxide isopropyl benzene |
Non-Patent Citations (1)
| Title |
|---|
| 徐裕等: "二一(2一羟基异丙基)苯的制备", 《高桥石化》, 28 February 2001 (2001-02-28) * |
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