CN1397538A - Process for preparing cyclohexanone or cyclohexaneol from cyclohexane - Google Patents
Process for preparing cyclohexanone or cyclohexaneol from cyclohexane Download PDFInfo
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- CN1397538A CN1397538A CN 01114586 CN01114586A CN1397538A CN 1397538 A CN1397538 A CN 1397538A CN 01114586 CN01114586 CN 01114586 CN 01114586 A CN01114586 A CN 01114586A CN 1397538 A CN1397538 A CN 1397538A
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- China
- Prior art keywords
- pimelinketone
- hexalin
- section
- sodium hydroxide
- cyclohexyl hydroperoxide
- 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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- JHIVVAPYMSGYDF-UHFFFAOYSA-N cyclohexanone Chemical compound O=C1CCCCC1 JHIVVAPYMSGYDF-UHFFFAOYSA-N 0.000 title claims abstract description 47
- HPXRVTGHNJAIIH-UHFFFAOYSA-N cyclohexanol Chemical compound OC1CCCCC1 HPXRVTGHNJAIIH-UHFFFAOYSA-N 0.000 title claims abstract description 34
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 title claims abstract description 22
- 238000004519 manufacturing process Methods 0.000 title abstract 2
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 124
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims abstract description 52
- 229910000029 sodium carbonate Inorganic materials 0.000 claims abstract description 26
- 239000000203 mixture Substances 0.000 claims abstract description 24
- 239000007864 aqueous solution Substances 0.000 claims abstract description 16
- 150000001732 carboxylic acid derivatives Chemical class 0.000 claims abstract description 10
- 159000000000 sodium salts Chemical class 0.000 claims abstract description 10
- 238000000354 decomposition reaction Methods 0.000 claims description 56
- FGGJBCRKSVGDPO-UHFFFAOYSA-N hydroperoxycyclohexane Chemical compound OOC1CCCCC1 FGGJBCRKSVGDPO-UHFFFAOYSA-N 0.000 claims description 41
- 238000000034 method Methods 0.000 claims description 34
- 230000003647 oxidation Effects 0.000 claims description 30
- 238000007254 oxidation reaction Methods 0.000 claims description 30
- 235000017550 sodium carbonate Nutrition 0.000 claims description 23
- QAHREYKOYSIQPH-UHFFFAOYSA-L cobalt(II) acetate Chemical compound [Co+2].CC([O-])=O.CC([O-])=O QAHREYKOYSIQPH-UHFFFAOYSA-L 0.000 claims description 18
- 239000012074 organic phase Substances 0.000 claims description 15
- -1 transition metal salt Chemical class 0.000 claims description 7
- 229910052723 transition metal Inorganic materials 0.000 claims description 6
- 229930194542 Keto Natural products 0.000 claims description 3
- 125000000468 ketone group Chemical group 0.000 claims description 3
- 241000220317 Rosa Species 0.000 claims description 2
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical group [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 2
- 238000004821 distillation Methods 0.000 claims description 2
- 238000007210 heterogeneous catalysis Methods 0.000 claims description 2
- 238000000926 separation method Methods 0.000 claims description 2
- 239000002699 waste material Substances 0.000 abstract description 7
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 abstract 2
- 239000003513 alkali Substances 0.000 abstract 1
- 230000003247 decreasing effect Effects 0.000 abstract 1
- 230000001590 oxidative effect Effects 0.000 abstract 1
- 230000009466 transformation Effects 0.000 description 9
- 239000000243 solution Substances 0.000 description 8
- 239000012071 phase Substances 0.000 description 7
- 230000001131 transforming effect Effects 0.000 description 7
- 239000000463 material Substances 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 235000003140 Panax quinquefolius Nutrition 0.000 description 1
- 240000005373 Panax quinquefolius Species 0.000 description 1
- 229910001854 alkali hydroxide Inorganic materials 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 150000008044 alkali metal hydroxides Chemical class 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- 239000008346 aqueous phase Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A process for preparing cyclohexanone or cyclohexanol from cyclohexane includes oxidizing cyclohexane to obtain the oxide mixture containing cyclohexyl-contained hydrogen peroxide, decomposing the mixture by the alkaline aqueous solution containing sodium carbonate or the sodium carbonate and more sodium salts of carboxylic acid and then by the alkaline aqueous solution containing sodium hydroxide or the sodium hydroxide and more sodium salts of carboxylic acid to generate cyclohexaneone and cyclohexanol, separating, distilling to obtain the products, and burning the waste alkali in oxide mixture to obtain sodium carbonate. Its advantages are high output rate increased by 3-9%, and less consumption of sodium hydroxide (decreased by 45-88%).
Description
The present invention relates to prepare the method for pimelinketone, hexalin, particularly by the decomposition method of cyclohexyl hydroperoxide in cyclohexane oxidation preparing cyclohexanone, the hexalin process from hexanaphthene.
Preparation pimelinketone, hexalin, normally use the gas cyaniding hexanaphthene of molecule-containing keto, generation contains the oxidation mixture of cyclohexyl hydroperoxide, handle this oxidation mixture then, make cyclohexyl hydroperoxide wherein decompose generation pimelinketone, hexalin, unreacted hexanaphthene recycles, and reaction product obtains pimelinketone, hexalin through rectifying.The general employing of the decomposition of cyclohexyl hydroperoxide contains Co
2+The NaOH aqueous solution handle, it is undesirable that its shortcoming is that the cyclohexyl hydroperoxide decomposition reaction generates the molecular yield of pimelinketone, hexalin, generally about 84%, the consumption of NaOH is higher, pimelinketone per ton consumes NaOH at 100kg～150kg.
CN1105970A has introduced the technology that a kind of two steps decompose, and is characterized in that the first step post-treatment aqueous phase need not separate, and directly carried out for second step and decompose, but the consumption of NaOH does not reduce.
CN1156714A adopts the alkali hydroxide soln of alkali metal containing carbonate or carboxylate salt to handle cyclohexane oxidation product, can improve decomposition rate, but the consumption of sodium hydroxide does not reduce.
Patents such as CN1228755A have adopted solid-phase catalyst to handle cyclohexane oxidation product, and advantage is that product need not to separate, but catalytic activity is difficult to keep, and life of catalyst is shorter.
The purpose of this invention is to provide and a kind ofly prepare the method for pimelinketone, hexalin from hexanaphthene, the molecular yield that makes the cyclohexyl hydroperoxide decomposition reaction generate pimelinketone, hexalin obviously improves, and the consumption of NaOH significantly reduces.
Of the present invention being achieved in that
A. the gas cyaniding hexanaphthene with molecule-containing keto generates the oxidation mixture that contains cyclohexyl hydroperoxide in oxidation reactor; The oxidation mixture that B. will contain cyclohexyl hydroperoxide decomposes, and generates pimelinketone, hexalin; C. after in separator, separating, distill out pimelinketone and hexalin; D. the salkali waste of oxidation mixture is carried out burning disposal and obtain yellow soda ash.
The decomposition that contains the oxidation mixture of cyclohexyl hydroperoxide divides two sections to carry out:
First section with containing yellow soda ash or containing yellow soda ash and the alkaline aqueous solution of the sodium salt of multiple carboxylic acid carries out heterogeneous catalysis and decomposes;
Second section with containing sodium hydroxide or containing sodium hydroxide and the alkaline aqueous solution of the sodium salt of multiple carboxylic acid further decomposes;
The organic phase of coming out from first section decomposition reactor is separated mutually with inorganic, separate the organic phase that obtains and enter second section splitter.Separate the inorganic major part mutually that obtains and return first section decomposition reactor, small part is sent to incinerator and is burned.
First section decomposition reaction is under 60 ℃～120 ℃ of temperature, pressure 100kPa～1200kPa, water-soluble transition metal salt with concentration 0.1ppm～100ppm is made catalyzer, contain yellow soda ash or contain yellow soda ash and the alkaline aqueous solution of the sodium salt of multiple carboxylic acid in the presence of carry out.
The organic phase of coming out from second section decomposition reactor is separated mutually with inorganic, isolated organic phase enters the distillation tower separation and obtains pimelinketone and hexalin, separate the inorganic major part mutually that obtains and return second section decomposition reactor, small part is sent to incinerator and is burned.
Second section decomposition reaction is under 60 ℃～120 ℃ of temperature, pressure 100kPa～1200kPa condition, with concentration is that the water-soluble transition metal salt of 0.1ppm～10ppm is made catalyzer, contain sodium hydroxide or contain sodium hydroxide and the alkaline aqueous solution of the sodium salt of multiple carboxylic acid under carry out.
Transition metal salt as catalyzer is a cobalt salt, for example rose vitriol, cobaltous acetate.
Yellow soda ash can be the yellow soda ash with the preparation of people known method, also can be that the salkali waste with oxidation mixture carries out the yellow soda ash that burning disposal obtains.
The condition of first section decomposition is relatively gentleer, has avoided the vigorous reaction of cyclohexyl hydroperoxide, has reduced side reaction, thereby has made the yield of purpose product pimelinketone, hexalin be improved; Strengthened decomposition condition for second section, the decomposition of cyclohexyl hydroperoxide is able to fully.
After the invention process, the yield of pimelinketone, hexalin can improve 3%～9%; The consumption of sodium hydroxide can reduce by 45%～88%; Salkali waste is burned the yellow soda ash that obtains recycle, reduced waste residue, thereby reduced pollution environment.
Accompanying drawing and description of drawings
Fig. 1: the schematic flow sheet of air oxidation of cyclohexane.
Fig. 2: cyclohexyl hydroperoxide two-phase method decomposition process synoptic diagram.
Fig. 3: cyclohexyl hydroperoxide one-stage process decomposition process synoptic diagram.
The 1st, oxidation reactor, 2 is first section decomposition reactor, and 3 is first section separator, and 4 is second section decomposition reactor, and 5 is second section separator, the 6th, decomposition reactor, the 7th, separator.
Below in conjunction with embodiment the present invention is described in detail:
Embodiment 1:
The technical process of present embodiment as shown in Figure 1
In oxidation reactor, add the 80000kg hexanaphthene, 155 ℃～165 ℃ of controlled temperature, pressure 900kPa～1300kPa does not add catalyzer, make hexanaphthene in liquid phase by molecular oxygen partial oxidation in the air, conversion of cyclohexane is about 4.5mol%.Per hour contain the about 75000kg of hexanaphthene, pimelinketone 269kg, hexalin 638kg, cyclohexyl hydroperoxide 2738kg in the oxidation mixture of Sheng Chenging, and other by product.This oxidation mixture is as the raw material that decomposes experiment.
Embodiment 2:
The technical process of present embodiment as shown in Figure 2
Get the oxidation mixture 262.1g among the embodiment 1, the 10% aqueous sodium carbonate 61.4g that contains the 5ppm Cobaltous diacetate, add in first section decomposition reactor, temperature is controlled at about 100 ℃, pressure-controlling is about 300KPa, react and take out material after 30 minutes, isolate inorganic phase, cyclohexyl hydroperoxide transformation efficiency 65.8%.Isolated organic phase is sent into second section decomposition reactor, in second section decomposition reactor, add the 2.6% aqueous sodium hydroxide solution 64.2g that contains the 2ppm Cobaltous diacetate, 30%NaOH aqueous solution 1.25g, about 90 ℃ of controlled temperature, continue to decompose 30 minutes, cyclohexyl hydroperoxide decomposes fully, and transformation efficiency reaches 100%.In these two sections decomposition techniques, it is 93% that cyclohexyl hydroperoxide decomposes the molecular yield that generates pimelinketone, hexalin.It is 25kg that pimelinketone per ton consumes NaOH.
The comparative example 1:
The technical process of present embodiment as shown in Figure 3
Get the oxidation mixture 261.2g among the embodiment 1, contain 2.6% aqueous sodium hydroxide solution 64.5g of 2ppm Cobaltous diacetate, 30%NaOH aqueous solution 3.3g adds in the decomposition reactor, and temperature is controlled at about 90 ℃, and pressure-controlling was reacted 30 minutes about 300KPa.Cyclohexyl hydroperoxide decomposes fully, transformation efficiency 100%.In this step decomposition technique, it is 86% that cyclohexyl hydroperoxide decomposes the molecular yield that generates pimelinketone, hexalin.It is 91kg that pimelinketone per ton consumes NaOH.
Embodiment 3:
The technical process of present embodiment as shown in Figure 2.
Get the oxidation mixture 261.5g among the embodiment 1, what contain the 25ppm Cobaltous diacetate recycles 4 times 10% aqueous sodium carbonate 57.2g, add in first section decomposition reactor, temperature is controlled at about 100 ℃, pressure-controlling is about 300KPa, react and take out material after 30 minutes, isolate inorganic phase, cyclohexyl hydroperoxide transformation efficiency 55.5%.Isolated organic phase is sent into second section decomposition reactor, in second section decomposition reactor, add contain the 1ppm Cobaltous diacetate recycle 4 times 2.6% aqueous sodium hydroxide solution 57.2g, 30%NaOH aqueous solution 1.16g, about 90 ℃ of controlled temperature, continue to decompose 30 minutes, cyclohexyl hydroperoxide decomposes fully, and transformation efficiency reaches 100%.In these two sections decomposition techniques, it is 94% that cyclohexyl hydroperoxide decomposes the molecular yield that generates pimelinketone, hexalin.It is 49kg that pimelinketone per ton consumes NaOH.
The comparative example 2:
The technical process of present embodiment as shown in Figure 3.
Get the oxidation mixture 261.0g among the embodiment 1, what contain the 1ppm Cobaltous diacetate recycles 4 times 2.6% aqueous sodium hydroxide solution 67.9g, 30%NaOH aqueous solution 3.6g, add in the decomposition reactor, temperature is controlled at about 90 ℃, and pressure-controlling was reacted 30 minutes about 300KPa.The cyclohexyl hydroperoxide rates of decomposing and transforming is 90.5%.In this step decomposition technique, it is 85% that cyclohexyl hydroperoxide decomposes the molecular yield that generates pimelinketone, hexalin.It is 90kg that pimelinketone per ton consumes NaOH.
Embodiment 4:
The technical process of present embodiment as shown in Figure 2.
Get the oxidation mixture 261.5g among the embodiment 1, the 10% aqueous sodium carbonate 61.0g that contains the 100ppm Cobaltous diacetate, add in first section decomposition reactor, temperature is controlled at about 60 ℃, pressure-controlling is about 300KPa, react and take out material after 30 minutes, isolate inorganic phase, cyclohexyl hydroperoxide transformation efficiency 8.2%.Isolated organic phase is sent into second section decomposition reactor, in second section decomposition reactor, add the 4% aqueous sodium hydroxide solution 55.8g that contains the 0.1ppm Cobaltous diacetate, about 80 ℃ of controlled temperature continue to decompose 30 minutes.The cyclohexyl hydroperoxide rates of decomposing and transforming reaches 96%.In these two sections decomposition techniques, it is 94% that cyclohexyl hydroperoxide decomposes the molecular yield that generates pimelinketone, hexalin.It is 29kg that pimelinketone per ton consumes NaOH.
Embodiment 5:
The technical process of present embodiment as shown in Figure 2.
Get the oxidation mixture 262.2g among the embodiment 1, the 10% aqueous sodium carbonate 60.9g that contains the 0.1ppm Cobaltous diacetate, add in first section decomposition reactor, temperature is controlled at about 80 ℃, pressure-controlling is about 300KPa, react and take out material after 30 minutes, isolate inorganic phase, cyclohexyl hydroperoxide transformation efficiency 31%.Isolated organic phase is sent into second section reactor, in second section decomposition reactor, add the 4% aqueous sodium hydroxide solution 56.1g that contains the 2ppm Cobaltous diacetate, about 80 ℃ of controlled temperature continue to decompose 30 minutes.Cyclohexyl hydroperoxide rates of decomposing and transforming 98%.In these two sections decomposition techniques, it is 93% that cyclohexyl hydroperoxide decomposes the molecular yield that generates pimelinketone, hexalin.It is 35kg that pimelinketone per ton consumes NaOH.
Embodiment 6:
The technical process of present embodiment as shown in Figure 2.
Get the oxidation mixture 261.3g among the embodiment 1, the 10% aqueous sodium carbonate 61.0g that contains the 10ppm Cobaltous diacetate, add in first section decomposition reactor, temperature is controlled at about 120 ℃, pressure-controlling is about 300KPa, react and take out material after 30 minutes, isolate inorganic phase, cyclohexyl hydroperoxide transformation efficiency 70%.Isolated organic phase is sent into second section reactor.In second section decomposition reactor, add the 4% aqueous sodium hydroxide solution 55.9g that contains the 10ppm Cobaltous diacetate, about 80 ℃ of controlled temperature continue to decompose 30 minutes.Cyclohexyl hydroperoxide rates of decomposing and transforming 100%.In these two sections decomposition techniques, it is 89% that cyclohexyl hydroperoxide decomposes the molecular yield that generates pimelinketone, hexalin.It is 11kg that pimelinketone per ton consumes NaOH.
Embodiment 7:
The technical process of present embodiment as shown in Figure 2.
Get the oxidation mixture 195.3g among the embodiment 1, the 12% aqueous sodium carbonate 137.4g (yellow soda ash burns from waste lye and obtains) that contains the 5ppm Cobaltous diacetate, add in first section decomposition reactor, temperature is controlled at about 100 ℃, pressure-controlling is about 300KPa, react and take out material after 6 minutes, isolate inorganic phase, cyclohexyl hydroperoxide transformation efficiency 55%.Isolated organic phase is sent into second section decomposition reactor, in second section decomposition reactor, add the 4.6% aqueous sodium hydroxide solution 64.8g that contains the 1ppm Cobaltous diacetate, about 100 ℃ of controlled temperature continue to decompose 6 minutes.Cyclohexyl hydroperoxide rates of decomposing and transforming 99%.In these two sections decomposition techniques, it is 95% that cyclohexyl hydroperoxide decomposes the molecular yield that generates pimelinketone, hexalin.It is 35kg that pimelinketone per ton consumes NaOH.
The comparative example 3:
The technical process of present embodiment as shown in Figure 2.
The 12% aqueous sodium carbonate 64.0g (yellow soda ash burns from waste lye and obtains), the yellow soda ash 0.9952g that get oxidation mixture 258.9g among the embodiment 1, contain the 5ppm Cobaltous diacetate add in first section decomposition reactor, temperature is controlled at about 100 ℃, pressure-controlling was decomposed 6 minutes about 300KPa.Cyclohexyl hydroperoxide rates of decomposing and transforming 26%.Then the organic phase product is all added to second section decomposition reactor with inorganic product mutually, and add the 30%NaOH aqueous solution 3.2957g that contains the 1ppm Cobaltous diacetate, decomposed 6 minutes in 100 ℃ again.In this two steps decomposition technique, the cyclohexyl hydroperoxide rates of decomposing and transforming is 88.6%, and the molecular yield that generates pimelinketone and hexalin is 88%.It is 98kg that pimelinketone per ton consumes NaOH.
Claims (4)
1, prepares the method for pimelinketone, hexalin from hexanaphthene, comprise the steps:
A. the gas cyaniding hexanaphthene with molecule-containing keto generates the oxidation mixture that contains cyclohexyl hydroperoxide in oxidation reactor;
The oxidation mixture that B. will contain cyclohexyl hydroperoxide decomposes, and generates pimelinketone, hexalin;
C. after in separator, separating, distill out pimelinketone and hexalin;
It is characterized in that the decomposition that contains the oxidation mixture of cyclohexyl hydroperoxide divides two sections to carry out;
First section with containing yellow soda ash or containing yellow soda ash and the alkaline aqueous solution of the sodium salt of multiple carboxylic acid carries out heterogeneous catalysis and decomposes;
Second section with containing sodium hydroxide or containing sodium hydroxide and the alkaline aqueous solution of the sodium salt of multiple carboxylic acid further decomposes;
The organic phase of coming out from first section decomposition reactor is separated mutually with inorganic, and isolated organic phase enters second section splitter, isolates inorganic major part mutually and returns first section decomposition reactor, and small part is sent to incinerator and burned.
The organic phase of coming out from second section decomposition reactor is separated mutually with inorganic, and isolated organic phase enters the distillation tower separation and obtains pimelinketone and hexalin, and isolated inorganic major part is mutually returned second section decomposition reactor, and small part is sent to incinerator and burned.
2, the method for preparing pimelinketone, hexalin from hexanaphthene according to claim 1, it is characterized in that first section decomposition reaction is under 60 ℃～120 ℃ of temperature, pressure 100kPa～1200kPa, water-soluble transition metal salt with concentration 0.1ppm～100ppm is made catalyzer, contain yellow soda ash or contain yellow soda ash and the alkaline aqueous solution of the sodium salt of multiple carboxylic acid in the presence of carry out.
3, the method for preparing pimelinketone, hexalin from hexanaphthene according to claim 1 and 2, it is characterized in that second section decomposition reaction is under 60 ℃～120 ℃ of temperature, pressure 100kPa～1200kPa condition, with concentration is that the water-soluble transition metal salt of 0.1ppm～10ppm is made catalyzer, contain sodium hydroxide or contain sodium hydroxide and the alkaline aqueous solution of the sodium salt of multiple carboxylic acid in carry out.
4, according to claim 1ly prepare the method for pimelinketone, hexalin, it is characterized in that the transition metal salt as catalyzer is a cobalt salt, for example rose vitriol, cobaltous acetate from hexanaphthene.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011145862A CN1166602C (en) | 2001-07-13 | 2001-07-13 | Process for preparing cyclohexanone or cyclohexaneol from cyclohexane |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011145862A CN1166602C (en) | 2001-07-13 | 2001-07-13 | Process for preparing cyclohexanone or cyclohexaneol from cyclohexane |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1397538A true CN1397538A (en) | 2003-02-19 |
| CN1166602C CN1166602C (en) | 2004-09-15 |
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| Application Number | Title | Priority Date | Filing Date |
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| CNB011145862A Expired - Fee Related CN1166602C (en) | 2001-07-13 | 2001-07-13 | Process for preparing cyclohexanone or cyclohexaneol from cyclohexane |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1317247C (en) * | 2004-12-09 | 2007-05-23 | 中国石化集团巴陵石油化工有限责任公司 | Method of obtaining high purity cyclohexanol from cyclohexane oxidation product |
| CN100363345C (en) * | 2003-11-05 | 2008-01-23 | 因维斯塔技术有限公司 | Process for oxidation of cyclohexane |
| CN101172931B (en) * | 2006-11-01 | 2011-11-16 | 肖藻生 | Improved process for producing cyclohexanol and pimelinketone |
| CN102260136A (en) * | 2010-05-26 | 2011-11-30 | 北京石油化工学院 | Method for preparing mixture of cyclohexanone and cyclohexanol by oxidazing cyclohexane liquid phase |
| CN102627525A (en) * | 2012-03-31 | 2012-08-08 | 肖藻生 | Preparation process for preparing hexamethylene and cyclohexanone by cyclohexane oxidation |
| CN102643166A (en) * | 2012-04-13 | 2012-08-22 | 阜新恒通氟化学有限公司 | Method for preparing perfluoroalkyl alcohol |
| WO2017099072A1 (en) * | 2015-12-07 | 2017-06-15 | 宇部興産株式会社 | Ketone and/or alcohol production method, and system for same |
-
2001
- 2001-07-13 CN CNB011145862A patent/CN1166602C/en not_active Expired - Fee Related
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100363345C (en) * | 2003-11-05 | 2008-01-23 | 因维斯塔技术有限公司 | Process for oxidation of cyclohexane |
| CN1317247C (en) * | 2004-12-09 | 2007-05-23 | 中国石化集团巴陵石油化工有限责任公司 | Method of obtaining high purity cyclohexanol from cyclohexane oxidation product |
| CN101172931B (en) * | 2006-11-01 | 2011-11-16 | 肖藻生 | Improved process for producing cyclohexanol and pimelinketone |
| CN102260136A (en) * | 2010-05-26 | 2011-11-30 | 北京石油化工学院 | Method for preparing mixture of cyclohexanone and cyclohexanol by oxidazing cyclohexane liquid phase |
| CN102627525A (en) * | 2012-03-31 | 2012-08-08 | 肖藻生 | Preparation process for preparing hexamethylene and cyclohexanone by cyclohexane oxidation |
| CN102643166A (en) * | 2012-04-13 | 2012-08-22 | 阜新恒通氟化学有限公司 | Method for preparing perfluoroalkyl alcohol |
| CN102643166B (en) * | 2012-04-13 | 2014-03-05 | 阜新恒通氟化学有限公司 | Method for preparing perfluoroalkyl alcohol |
| WO2017099072A1 (en) * | 2015-12-07 | 2017-06-15 | 宇部興産株式会社 | Ketone and/or alcohol production method, and system for same |
| CN108602736A (en) * | 2015-12-07 | 2018-09-28 | 宇部兴产株式会社 | Manufacture the method and its system of ketone and/or alcohol |
| US10392334B2 (en) | 2015-12-07 | 2019-08-27 | Ube Industries, Ltd. | Method for producing ketone and/or alcohol, and system thereof |
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|---|---|
| CN1166602C (en) | 2004-09-15 |
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