RU2011139641A - Способ получения высокооктанового бензина с пониженным содержанием бензола путем алкилирования бензола при высокой конверсии бензола - Google Patents
Способ получения высокооктанового бензина с пониженным содержанием бензола путем алкилирования бензола при высокой конверсии бензола Download PDFInfo
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- benzene
- propylene
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- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 title claims abstract 52
- 238000005804 alkylation reaction Methods 0.000 title claims abstract 6
- 230000029936 alkylation Effects 0.000 title claims abstract 5
- 238000006243 chemical reaction Methods 0.000 title claims abstract 5
- 238000004519 manufacturing process Methods 0.000 title 1
- 238000000034 method Methods 0.000 claims abstract 22
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims abstract 15
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims abstract 14
- 239000003054 catalyst Substances 0.000 claims abstract 12
- 238000009835 boiling Methods 0.000 claims abstract 6
- 239000000047 product Substances 0.000 claims abstract 6
- 125000003118 aryl group Chemical group 0.000 claims abstract 5
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims abstract 5
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract 4
- 150000001336 alkenes Chemical class 0.000 claims abstract 4
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims abstract 4
- 239000007791 liquid phase Substances 0.000 claims abstract 4
- 239000010457 zeolite Substances 0.000 claims abstract 4
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract 3
- 230000003197 catalytic effect Effects 0.000 claims abstract 3
- 229930195733 hydrocarbon Natural products 0.000 claims abstract 3
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract 3
- 150000004996 alkyl benzenes Chemical class 0.000 claims abstract 2
- 239000007795 chemical reaction product Substances 0.000 claims abstract 2
- 239000002994 raw material Substances 0.000 claims 4
- ODLMAHJVESYWTB-UHFFFAOYSA-N propylbenzene Chemical class CCCC1=CC=CC=C1 ODLMAHJVESYWTB-UHFFFAOYSA-N 0.000 claims 3
- LGXAANYJEHLUEM-UHFFFAOYSA-N 1,2,3-tri(propan-2-yl)benzene Chemical compound CC(C)C1=CC=CC(C(C)C)=C1C(C)C LGXAANYJEHLUEM-UHFFFAOYSA-N 0.000 claims 2
- OKIRBHVFJGXOIS-UHFFFAOYSA-N 1,2-di(propan-2-yl)benzene Chemical compound CC(C)C1=CC=CC=C1C(C)C OKIRBHVFJGXOIS-UHFFFAOYSA-N 0.000 claims 2
- 239000003153 chemical reaction reagent Substances 0.000 claims 1
- 238000001816 cooling Methods 0.000 claims 1
- RWGFKTVRMDUZSP-UHFFFAOYSA-N cumene Chemical class CC(C)C1=CC=CC=C1 RWGFKTVRMDUZSP-UHFFFAOYSA-N 0.000 claims 1
- 238000002347 injection Methods 0.000 claims 1
- 239000007924 injection Substances 0.000 claims 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 claims 1
- -1 propylene olefin Chemical class 0.000 claims 1
- 239000000376 reactant Substances 0.000 claims 1
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G35/00—Reforming naphtha
- C10G35/04—Catalytic reforming
- C10G35/06—Catalytic reforming characterised by the catalyst used
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- C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
- C07C2/64—Addition to a carbon atom of a six-membered aromatic ring
- C07C2/66—Catalytic processes
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- C10G29/00—Refining of hydrocarbon oils, in the absence of hydrogen, with other chemicals
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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- C10L1/00—Liquid carbonaceous fuels
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- C10L1/06—Liquid carbonaceous fuels essentially based on blends of hydrocarbons for spark ignition
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
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- C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- C07C2529/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65
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- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
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- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
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- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
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- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
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Abstract
1. Способ получения углеводородного продукта в интервале кипения бензина с низким содержанием бензола из потока легкого, содержащего бензол ароматического сырья, который включает алкилирование потока ароматического сырья в присутствии цеолитового катализатора MWW по меньшей мере в двух последовательных неподвижных слоях катализатора в режиме однократного прохождения потоком содержащего пропилен олефинового сырья, содержащего по меньшей мере 50 мас.% пропилена, вводимого на вход каждого каталитического слоя, при условиях повышенных температуры и давления для конверсии по меньшей мере 70 мас.%, предпочтительно по меньшей мере 90 мас.%, наиболее предпочтительно по меньшей мере 95 мас.% бензола, содержащегося в сырье, в алкилбензолы.2. Способ по п.1, в котором конверсия пропилена составляет по меньшей мере 97 мас.%.3. Способ по п.1, в котором температура (на входе в первый слой катализатора) составляет от 120 до 250°С, предпочтительно от 200 до 225°С.4. Способ по п.1, в котором давление является достаточным для поддержания условий жидкой фазы и составляет по меньшей мере 2500 кПа изб., предпочтительно по меньшей мере 4000 кПа изб.5. Способ по п.1, в котором количество бензола в продукте не превышает 1,3 об.%.6. Способ по п.1, в котором содержание бензола в сырье, состоящем из продукта риформинга, составляет по меньшей мере 15 мас.%, предпочтительно от 20 до 50 мас.%.7. Способ по п.1, в котором цеолитовый катализатор MWW представляет собой МСМ-22 катализатор.8. Способ по п.1, в котором продукт реакции содержит не более 5 об.% фракций с температурой кипения выше 225°С.9. Способ по п.1, в котором молярное отношение содержащего пропилен олефинового сырья к ароматичес
Claims (17)
1. Способ получения углеводородного продукта в интервале кипения бензина с низким содержанием бензола из потока легкого, содержащего бензол ароматического сырья, который включает алкилирование потока ароматического сырья в присутствии цеолитового катализатора MWW по меньшей мере в двух последовательных неподвижных слоях катализатора в режиме однократного прохождения потоком содержащего пропилен олефинового сырья, содержащего по меньшей мере 50 мас.% пропилена, вводимого на вход каждого каталитического слоя, при условиях повышенных температуры и давления для конверсии по меньшей мере 70 мас.%, предпочтительно по меньшей мере 90 мас.%, наиболее предпочтительно по меньшей мере 95 мас.% бензола, содержащегося в сырье, в алкилбензолы.
2. Способ по п.1, в котором конверсия пропилена составляет по меньшей мере 97 мас.%.
3. Способ по п.1, в котором температура (на входе в первый слой катализатора) составляет от 120 до 250°С, предпочтительно от 200 до 225°С.
4. Способ по п.1, в котором давление является достаточным для поддержания условий жидкой фазы и составляет по меньшей мере 2500 кПа изб., предпочтительно по меньшей мере 4000 кПа изб.
5. Способ по п.1, в котором количество бензола в продукте не превышает 1,3 об.%.
6. Способ по п.1, в котором содержание бензола в сырье, состоящем из продукта риформинга, составляет по меньшей мере 15 мас.%, предпочтительно от 20 до 50 мас.%.
7. Способ по п.1, в котором цеолитовый катализатор MWW представляет собой МСМ-22 катализатор.
8. Способ по п.1, в котором продукт реакции содержит не более 5 об.% фракций с температурой кипения выше 225°С.
9. Способ по п.1, в котором молярное отношение содержащего пропилен олефинового сырья к ароматическому сырью составляет от 1,0:1 до 2:1.
10. Способ по п.1, в котором часть потока содержащего пропилен сырья вводят перед каждым слоем катализатора и поток содержащего пропилен сырья находится при температуре в точке введения, следующей за первым каталитическим слоем, ниже температуры потока остающегося реагента в той же точке введения, для обеспечения быстрого охлаждения реакции.
11. Способ по п.10, в котором температура потока содержащего пропилен сырья по меньшей мере на 10°С ниже температуры потока остающегося реагента в точке введения потока содержащего пропилен сырья.
12. Способ по п.1, в котором продукт реакции алкилирования содержит моно-, ди- и тризамещенные изопропилбензолы.
13. Способ по п.1, в котором получают углеводородный продукт в интервале кипения бензина, имеющий концентрацию бензола не более 1 об.%, из сырья, имеющего концентрацию бензола по меньшей мере 20 мас.%, и в котором алкилирование проводят в жидкой фазе потоком содержащего пропилен олефинового сырья, содержащего по меньшей мере 60 мас.% пропилена, введенного между слоями катализатора при температуре на входе реактора от 200 до 250°С и давлении, достаточном для поддержания условий жидкой фазы и составляющем от 4000 до 10000 кПа изб. (на входе в реактор), при объемной скорости ЧОСЖ от 1 до 5 ч-1, с массовым отношением содержащего пропилен олефинового потока к потоку ароматического сырья от 0,8 до 3,0, для преобразования по меньшей мере 90 мас.% бензола, содержащегося в сырье, в пропилбензолы и получения выходящего из реактора алкилирования потока, который имеет Т90 не выше 230°С и октановое число (ОЧим+ОЧмм)/2 не менее 82.
14. Моторный бензин, содержащий не более 1,0 об.% бензола и имеющий температуру выкипания (ASTM D 86) не выше 225°С, Т90 (ASTM D 86) не выше 185°С и содержащий монопропилбензол, диизопропилбензол и триизопропилбензол.
15. Моторный бензин по п.14, содержащий от 40 до 60 мас.% монопропилбензола, от 30 до 50 мас.% диизопропилбензола и от 5 до 10 мас.% триизопропилбензола.
16. Моторный бензин по п.14 или 15, содержащий не более 0,62 об.% бензола.
17. Моторный бензин по п.16, имеющий Т90 (ASTM D 86) не выше 145°С.
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US20999509P | 2009-03-13 | 2009-03-13 | |
| US61/209,995 | 2009-03-13 | ||
| US12/720,345 | 2010-03-09 | ||
| US12/720,345 US8395006B2 (en) | 2009-03-13 | 2010-03-09 | Process for making high octane gasoline with reduced benzene content by benzene alkylation at high benzene conversion |
| PCT/US2010/000731 WO2010104581A2 (en) | 2009-03-13 | 2010-03-11 | Process for making high octane gasoline with reduced benzene content by benzene alkylation at high benzene conversion |
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| US (1) | US8395006B2 (ru) |
| EP (1) | EP2408880A2 (ru) |
| JP (1) | JP5636382B2 (ru) |
| KR (1) | KR101474599B1 (ru) |
| CN (1) | CN102625823B (ru) |
| AU (1) | AU2010223041B2 (ru) |
| BR (1) | BRPI1009400B1 (ru) |
| CA (1) | CA2754816C (ru) |
| MX (1) | MX2011009373A (ru) |
| RU (1) | RU2515525C2 (ru) |
| WO (1) | WO2010104581A2 (ru) |
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| US8563795B2 (en) * | 2010-01-19 | 2013-10-22 | Uop Llc | Aromatic aklylating agent and an aromatic production apparatus |
| US8609917B2 (en) * | 2010-01-19 | 2013-12-17 | Uop Llc | Process for increasing methyl to phenyl mole ratios and reducing benzene content in a motor fuel product |
| WO2012108924A1 (en) * | 2011-02-07 | 2012-08-16 | Badger Licensing Llc | Process for reducing the benzene content of gasoline |
| EP2673247B1 (en) * | 2011-02-07 | 2020-05-06 | Badger Licensing LLC | Process for reducing the benzene content of gasoline |
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| US9200215B2 (en) | 2011-02-07 | 2015-12-01 | Badger Licensing Llc | Process for reducing the benzene content of gasoline |
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| US9598330B2 (en) | 2011-08-19 | 2017-03-21 | Badger Licensing | Process for reducing the benzene content of gasoline |
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| CN103540343B (zh) * | 2012-07-12 | 2016-01-13 | 中国石油化工股份有限公司 | 提高汽油辛烷值的方法 |
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| WO2014109766A1 (en) * | 2013-01-14 | 2014-07-17 | Badger Licensing Llc | Process for balancing gasoline and distillate production in a refinery |
| HK1198615A2 (en) | 2014-11-19 | 2015-04-30 | Man Yin Lam | Lighting and diffuser apparatus for a flashlight |
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- 2010-03-11 MX MX2011009373A patent/MX2011009373A/es active IP Right Grant
- 2010-03-11 KR KR1020117023950A patent/KR101474599B1/ko active IP Right Grant
- 2010-03-11 BR BRPI1009400-8A patent/BRPI1009400B1/pt not_active IP Right Cessation
- 2010-03-11 CN CN201080011857.3A patent/CN102625823B/zh not_active Expired - Fee Related
- 2010-03-11 AU AU2010223041A patent/AU2010223041B2/en not_active Ceased
- 2010-03-11 RU RU2011139641/04A patent/RU2515525C2/ru not_active IP Right Cessation
- 2010-03-11 EP EP10713043A patent/EP2408880A2/en not_active Withdrawn
- 2010-03-11 JP JP2011554046A patent/JP5636382B2/ja not_active Expired - Fee Related
- 2010-03-11 CA CA2754816A patent/CA2754816C/en not_active Expired - Fee Related
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Also Published As
| Publication number | Publication date |
|---|---|
| RU2515525C2 (ru) | 2014-05-10 |
| EP2408880A2 (en) | 2012-01-25 |
| CN102625823B (zh) | 2015-02-11 |
| CA2754816A1 (en) | 2010-09-16 |
| WO2010104581A3 (en) | 2012-05-24 |
| CA2754816C (en) | 2015-10-27 |
| MX2011009373A (es) | 2011-10-03 |
| US20100300930A1 (en) | 2010-12-02 |
| BRPI1009400B1 (pt) | 2018-07-03 |
| KR101474599B1 (ko) | 2014-12-18 |
| AU2010223041B2 (en) | 2015-02-05 |
| CN102625823A (zh) | 2012-08-01 |
| KR20120002586A (ko) | 2012-01-06 |
| JP5636382B2 (ja) | 2014-12-03 |
| WO2010104581A2 (en) | 2010-09-16 |
| JP2012520376A (ja) | 2012-09-06 |
| BRPI1009400A2 (pt) | 2016-03-08 |
| US8395006B2 (en) | 2013-03-12 |
| AU2010223041A1 (en) | 2011-11-03 |
| ZA201106630B (en) | 2015-05-27 |
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