RU94007336A - METHOD OF ACID DECOMPOSITION OF TECHNICAL HYDROPEROXIDE OF PHONOL, KETA AND METHYLSTYROL - Google Patents
METHOD OF ACID DECOMPOSITION OF TECHNICAL HYDROPEROXIDE OF PHONOL, KETA AND METHYLSTYROLInfo
- Publication number
- RU94007336A RU94007336A RU94007336/04A RU94007336A RU94007336A RU 94007336 A RU94007336 A RU 94007336A RU 94007336/04 A RU94007336/04 A RU 94007336/04A RU 94007336 A RU94007336 A RU 94007336A RU 94007336 A RU94007336 A RU 94007336A
- Authority
- RU
- Russia
- Prior art keywords
- decomposition
- reactor
- acetone
- chp
- cumene hydroperoxide
- Prior art date
Links
- 238000000354 decomposition reaction Methods 0.000 title claims 8
- 239000002253 acid Substances 0.000 title 1
- MHAJPDPJQMAIIY-UHFFFAOYSA-N hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 title 1
- QROGIFZRVHSFLM-UHFFFAOYSA-N prop-1-enylbenzene Chemical compound CC=CC1=CC=CC=C1 QROGIFZRVHSFLM-UHFFFAOYSA-N 0.000 title 1
- CSCPPACGZOOCGX-UHFFFAOYSA-N acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 claims 10
- 241000711969 Chandipura virus Species 0.000 claims 4
- YQHLDYVWEZKEOX-UHFFFAOYSA-N Cumene hydroperoxide Chemical group OOC(C)(C)C1=CC=CC=C1 YQHLDYVWEZKEOX-UHFFFAOYSA-N 0.000 claims 4
- 238000000034 method Methods 0.000 claims 3
- 238000002156 mixing Methods 0.000 claims 3
- 239000000047 product Substances 0.000 claims 3
- XMNIXWIUMCBBBL-UHFFFAOYSA-N 2-(2-phenylpropan-2-ylperoxy)propan-2-ylbenzene Chemical compound C=1C=CC=CC=1C(C)(C)OOC(C)(C)C1=CC=CC=C1 XMNIXWIUMCBBBL-UHFFFAOYSA-N 0.000 claims 2
- RWGFKTVRMDUZSP-UHFFFAOYSA-N Cumene Chemical compound CC(C)C1=CC=CC=C1 RWGFKTVRMDUZSP-UHFFFAOYSA-N 0.000 claims 2
- 238000006073 displacement reaction Methods 0.000 claims 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims 1
- 230000015572 biosynthetic process Effects 0.000 claims 1
- 239000007795 chemical reaction product Substances 0.000 claims 1
- 238000010276 construction Methods 0.000 claims 1
- 238000004821 distillation Methods 0.000 claims 1
- 238000005516 engineering process Methods 0.000 claims 1
- 238000001704 evaporation Methods 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 claims 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims 1
- 229920002451 polyvinyl alcohol Polymers 0.000 claims 1
- 238000007086 side reaction Methods 0.000 claims 1
- 238000003786 synthesis reaction Methods 0.000 claims 1
- 230000002194 synthesizing Effects 0.000 claims 1
- XYLMUPLGERFSHI-UHFFFAOYSA-N α-Methylstyrene Chemical compound CC(=C)C1=CC=CC=C1 XYLMUPLGERFSHI-UHFFFAOYSA-N 0.000 claims 1
Claims (1)
где GГ П К, Gа ц - количество подаваемого на разложение технического ГПК и ацетона, т/ч, [ГПК] концентрация ГПК в техническом ГПК, мас.ч. Разложение гидропероксида кумола и дикумилпероксида кумола ведут при одинаковом давлении (4 - 5 атм.) в реакторах смешения, где разлагается ГПК, и в реакторе вытеснения, где разлагается дикумилпероксид. Разложение гидропероксида кумола проводится в условиях, близких к изотермическим, в узком диапазоне температур 65 - 75°С. Концентрация неразложенного гидропероксида кумола на выходе из блока реакторов смешения определяется по разности температур Т1 на входе и выходе специально установленного мини-реактора (калориметра). В реактор вытеснения подается вода в количестве 100 - 500 кг/ч, определяемом величиной разности температур ΔT2 на входе и выходе из специально устанавливаемого калориметра на линии продуктов, выходящих из контура циркуляции после смешения продуктов разложения с водой и временем пребывания продуктов в мини-реакторе в течение 7 - 8 мин. Управление процессом разложения ГПК осуществляется через взаимосвязь величин ΔT1 и ΔT2 таким образом, что величина ΔT2 поддерживается на 0,2 - 3°С выше, чем ΔT1. Для исключения протекания нежелательных побочных реакций при отгонке из продуктов реакции введенного ацетона перед аппаратом испарения ацетона подается аммиак в мольном соотношении H2SO4 : NH3, равном от 1 : 1 до 1 : 2.The invention relates to the field of petrochemical synthesis, in particular to a method for producing phenol, acetone and alpha-methylstyrene by the cumene method. The purpose of the invention is to increase the productivity of existing industrial installations, reduce investment by reducing the amount of equipment during the construction of new installations, simplifying technology while maintaining a high selectivity of the process. The decomposition process is carried out with the supply of acetone in the reactor decomposition of cumene hydroperoxide according to the following algorithm:
wherein G T P K, G and n - number of fed technical CHP decomposition to acetone and t / hr [CHP] CHP concentration in technical CHP, pbw The decomposition of cumene hydroperoxide and dicumyl peroxide of cumene is carried out at the same pressure (4-5 atm.) In the mixing reactors, where the HPP decomposes, and in the displacement reactor, where dicumyl peroxide decomposes. The decomposition of cumene hydroperoxide is carried out under conditions close to isothermal, in a narrow temperature range of 65 - 75 ° C. The concentration of undecomposed cumene hydroperoxide at the exit of the mixing reactor unit is determined by the temperature difference T1 at the inlet and outlet of the specially installed mini-reactor (calorimeter). Water in the amount of 100 - 500 kg / h is supplied to the displacement reactor, determined by the temperature difference ΔT2 at the inlet and outlet of the specially installed calorimeter on the product line leaving the circulation circuit after mixing the decomposition products with water and the residence time of the products in the mini-reactor for 7 - 8 min. The process of decomposition of the CCP is controlled through the interrelation of the ΔT1 and ΔT2 values in such a way that the ΔT2 value is maintained 0.2–3 ° C higher than ΔT1. To eliminate the occurrence of undesirable side reactions during the distillation of the introduced acetone from the reaction products, ammonia is fed in front of the acetone evaporation apparatus in a molar ratio of H 2 SO 4 : NH 3 equal to 1: 1 to 1: 2.
Priority Applications (8)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| RU94007336A RU2108318C1 (en) | 1994-03-01 | 1994-03-01 | METHOD OF SYNTHESIS OF PHENOL, ACETONE AND α-METHYLSTYRENE |
| US08/369,104 US5530166A (en) | 1994-03-01 | 1995-01-13 | Method of technical cumene hydroperoxide acidic cleavage to phenol, acetone and alpha-methylstyrene |
| JP3991595A JP3711504B2 (en) | 1994-03-01 | 1995-02-28 | Method for acid decomposition of industrial cumene hydroperoxide to phenol, acetone and α-methylstyrene |
| DE1995605573 DE69505573T2 (en) | 1994-03-01 | 1995-02-28 | Acid cleavage of cumene hydroperoxide in phenol, acetone and alphamethylstyrene |
| KR1019950003985A KR100367444B1 (en) | 1994-03-01 | 1995-02-28 | Method of technical cumene hydroperoxided acidic cleavage to phenol, acetone and alpha-methylstyrene |
| EP19950301267 EP0670296B1 (en) | 1994-03-01 | 1995-02-28 | Acid cleavage of cumene hydroperoxide to phenol, acetone and alpha-methylstyrene |
| CA002143578A CA2143578A1 (en) | 1994-03-01 | 1995-02-28 | Method of technical cumene hydroperoxide acidic cleavage to phenol acetone and alpha-methylstyrene |
| ES95301267T ES2123908T3 (en) | 1994-03-01 | 1995-02-28 | CATALYZED EXCISION WITH CUMENE HYDROPEROXIDE ACID TO PHENOL, ACETONE AND ALPHA-METHYLTISTYRENE. |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| RU94007336A RU2108318C1 (en) | 1994-03-01 | 1994-03-01 | METHOD OF SYNTHESIS OF PHENOL, ACETONE AND α-METHYLSTYRENE |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| RU94007336A true RU94007336A (en) | 1995-11-10 |
| RU2108318C1 RU2108318C1 (en) | 1998-04-10 |
Family
ID=20153091
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| RU94007336A RU2108318C1 (en) | 1994-03-01 | 1994-03-01 | METHOD OF SYNTHESIS OF PHENOL, ACETONE AND α-METHYLSTYRENE |
Country Status (3)
| Country | Link |
|---|---|
| US (1) | US5530166A (en) |
| KR (1) | KR100367444B1 (en) |
| RU (1) | RU2108318C1 (en) |
Families Citing this family (19)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3769050B2 (en) * | 1995-07-07 | 2006-04-19 | 三井化学株式会社 | Method for producing phenol |
| RU2125038C1 (en) * | 1996-09-24 | 1999-01-20 | Закошанский Владимир Михайлович | Run-down economic method of synthesis of phenol and acetone |
| RU2141938C1 (en) | 1996-12-15 | 1999-11-27 | ООО "Илла Интернешнл", Лтд. | Power saving and highly selective method of preparing phenol and acetone |
| DE10021482A1 (en) * | 2000-05-03 | 2001-11-08 | Phenolchemie Gmbh & Co Kg | Process for the thermal aftertreatment of cleavage product from the acid-catalyzed cleavage of cumene hydroperoxide |
| DE10051581A1 (en) * | 2000-10-18 | 2002-06-20 | Phenolchemie Gmbh & Co Kg | Process for the cleavage of alkylaryl hydroperoxides |
| RU2231045C2 (en) * | 2002-05-20 | 2004-06-20 | Общество с ограниченной ответственностью "Еврохим-СпбТрейдинг" | Method of measurement of concentration of hydroperoxides of alkyl aromatic hydrocarbons in liquid industrial flows |
| RU2219169C1 (en) * | 2002-07-29 | 2003-12-20 | Общество с ограниченной ответственностью "Петрофенол" | Method for preparing cumene hydroperoxide |
| US7282613B2 (en) * | 2003-02-14 | 2007-10-16 | Shell Oil Company | Process for producing phenol and methyl ethyl ketone |
| US7312365B2 (en) * | 2003-02-14 | 2007-12-25 | Shell Oil Company | Process for low temperature cleavage of an oxidation mixture comprising hydroperoxides |
| US7141703B2 (en) * | 2003-02-14 | 2006-11-28 | Shell Oil Company | Process for producing phenol and ketone using neutralizing base |
| KR20070002039A (en) * | 2004-03-31 | 2007-01-04 | 제너럴 일렉트릭 캄파니 | Process for producing phenol |
| US7205376B2 (en) * | 2004-05-04 | 2007-04-17 | General Electric Company | Processes for the production of cumene, polyetherimides, and polycarbonates |
| WO2007137020A2 (en) * | 2006-05-16 | 2007-11-29 | Shell Oil Company | Method for decomposing di(phenylalkyl)peroxides to produce hydroxybenzenes and phenylalkenes using solid catalysts |
| WO2007137021A2 (en) * | 2006-05-16 | 2007-11-29 | Shell Oil Company | Catalysts comprising a combination of oxidized metals and a method for cleaving phenylalkyl hydroperoxides using the catalysts |
| US20110306800A1 (en) * | 2010-06-09 | 2011-12-15 | Scott Roy Keenan | Method for the decomposition of cumene hydroperoxide |
| KR102445658B1 (en) * | 2014-10-24 | 2022-09-20 | 사빅 글로벌 테크놀러지스 비.브이. | System and process for cumene hydroperoxide cleavage with improved online instrumentation configuration |
| KR102523924B1 (en) | 2020-12-01 | 2023-04-19 | 김묘정 | Cosmetics container |
| EP4043420A4 (en) | 2020-12-21 | 2023-01-04 | LG Chem, Ltd. | Method for producing alpha-methylstyrene |
| KR20240069601A (en) | 2022-11-11 | 2024-05-20 | 주식회사 엘지화학 | Method for manufacturing of alpha-methylstyrene |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH05286879A (en) * | 1992-04-03 | 1993-11-02 | Mitsui Petrochem Ind Ltd | Production of high-purity phenol |
| US5245090A (en) * | 1992-09-11 | 1993-09-14 | Aristech Chemical Corporation | Two-stage cleavage of cumene hydroperoxide |
| US5254751A (en) * | 1992-09-14 | 1993-10-19 | General Electric Company | Method for the decomposition of cumene hydroperoxide by acidic catalyst to phenol and acetone |
| US5371305A (en) * | 1992-12-31 | 1994-12-06 | Hercules Incorporated | Process for producing phenol from cumene |
-
1994
- 1994-03-01 RU RU94007336A patent/RU2108318C1/en active
-
1995
- 1995-01-13 US US08/369,104 patent/US5530166A/en not_active Expired - Lifetime
- 1995-02-28 KR KR1019950003985A patent/KR100367444B1/en not_active IP Right Cessation
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