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RU2012156272A - Способ и устройство для получения углеводородов из сырья, содержащего талловое масло и терпеновые соединения - Google Patents

Способ и устройство для получения углеводородов из сырья, содержащего талловое масло и терпеновые соединения Download PDF

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RU2012156272A
RU2012156272A RU2012156272/04A RU2012156272A RU2012156272A RU 2012156272 A RU2012156272 A RU 2012156272A RU 2012156272/04 A RU2012156272/04 A RU 2012156272/04A RU 2012156272 A RU2012156272 A RU 2012156272A RU 2012156272 A RU2012156272 A RU 2012156272A
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hydrotreating
hydrocarbon components
reactor
isomerization
tall oil
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RU2012156272/04A
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English (en)
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RU2566763C2 (ru
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Пекка КНУУТТИЛА
Якко НОУСИАЙНЕН
Арто РИССАНЕН
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Упм-Кюммене Корпорейшн
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Abstract

1. Способ получения углеводородных компонентов, включающий:предоставление сырья, содержащего талловое масло и терпеновые соединенияподвергание сырья и питающего газообразного водорода гидроочистке в присутствии NiO/МоОкатализатора на носителе AlOдля получения углеводородных компонентов, включающих н-парафины, иподвергание углеводородных компонентов, включающих н-парафины, изомеризации в присутствии NiW катализатора на носителе цеолит-AlOи в присутствии водорода для образования смеси углеводородных компонентов.2. Способ по п.1, где терпеновые соединения получают из растений, терпеновых масел, донного остатка перегонки терпенов и ароматизаторов и/или парфюмерной промышленности.3. Способ по п.2, где сырье содержит сырое талловое масло и сырой сульфатный скипидар, полученные при сульфатной варке древесины.4. Способ по п.3, где сырое талловое масло очищают перед подверганием гидроочистке.5. Способ по любому из предшествующих пп., где часть смеси углеводородных компонентов, полученных при изомеризации, направляют обратно на гидроочистку.6. Способ по п.1, где гидроочистку осуществляют при температуре от приблизительно 280°С до приблизительно 500°С, предпочтительно от приблизительно 330°С до приблизительно 430°С.7. Способ по п.1, где изомеризацию осуществляют при температуре от приблизительно 280°С до приблизительно 500°С, предпочтительно от приблизительно 330°С до приблизительно 430°С.8. Способ по п.1, где гидроочистку осуществляют под давлением от приблизительно 3 до приблизительно 20 МПа, предпочтительно от приблизительно 3 до приблизительно 10 МПа.9. Способ по п.1, где изомеризацию осуществляют под давлением от приблизительно 3 д

Claims (21)

1. Способ получения углеводородных компонентов, включающий:
предоставление сырья, содержащего талловое масло и терпеновые соединения
подвергание сырья и питающего газообразного водорода гидроочистке в присутствии NiO/МоО3 катализатора на носителе Al2O3 для получения углеводородных компонентов, включающих н-парафины, и
подвергание углеводородных компонентов, включающих н-парафины, изомеризации в присутствии NiW катализатора на носителе цеолит-Al2O3 и в присутствии водорода для образования смеси углеводородных компонентов.
2. Способ по п.1, где терпеновые соединения получают из растений, терпеновых масел, донного остатка перегонки терпенов и ароматизаторов и/или парфюмерной промышленности.
3. Способ по п.2, где сырье содержит сырое талловое масло и сырой сульфатный скипидар, полученные при сульфатной варке древесины.
4. Способ по п.3, где сырое талловое масло очищают перед подверганием гидроочистке.
5. Способ по любому из предшествующих пп., где часть смеси углеводородных компонентов, полученных при изомеризации, направляют обратно на гидроочистку.
6. Способ по п.1, где гидроочистку осуществляют при температуре от приблизительно 280°С до приблизительно 500°С, предпочтительно от приблизительно 330°С до приблизительно 430°С.
7. Способ по п.1, где изомеризацию осуществляют при температуре от приблизительно 280°С до приблизительно 500°С, предпочтительно от приблизительно 330°С до приблизительно 430°С.
8. Способ по п.1, где гидроочистку осуществляют под давлением от приблизительно 3 до приблизительно 20 МПа, предпочтительно от приблизительно 3 до приблизительно 10 МПа.
9. Способ по п.1, где изомеризацию осуществляют под давлением от приблизительно 3 до приблизительно 20 МПа, предпочтительно от приблизительно 3 до приблизительно 10 МПа.
10. Способ по п.1, где скорость подачи сырья WHSV составляет 0,6-1,2.
11. Способ по п.1, где смесь углеводородных компонентов подвергают сепарации для разделения углеводородных фракций бензинового, дизельного, реактивного и лигроинового диапазона.
12. Устройство для получения углеводородных компонентов из включающего талловое масло и терпеновые соединения сырья, включающее
- один или несколько реакторов гидроочистки (1, 1'),
- впускной канал сырья (4) для введения сырья в один или несколько реакторов гидроочистки,
- впускной канал водорода (6) для введения водорода в один или несколько реакторов гидроочистки,
- выпускной канал продукта (8) для отведения углеводородных компонентов из одного или нескольких реакторов гидроочистки, где по меньшей мере один из реакторов гидроочистки содержит каталитический слой (3) катализатора депарафинизации, которым является NiW на цеолит-Al2O3 носителе.
13. Устройство по п.12, где первый каталитический слой (3') NiO/МоО3 катализатора на Al2O3 носителе и второй каталитический слой (3) NiW катализатора на цеолит-Al2O3 носителе расположены в реакторе гидроочистки (1), первый каталитический слой (3') расположен выше по потоку от второго каталитического слоя (3).
14. Устройство по п.13, где устройство включает трубопровод рециркуляции продукта (80) для циркуляции потока продукта из смеси углеводородных компонентов, полученного из реактора (1), обратно в реактор (1).
15. Устройство по п.12, где первый каталитический слой (3') NiO/МоО3 катализатора на Al2O3 носителе расположен в первом реакторе гидроочистки (1'), и второй каталитический слой (3) NiW катализатора на цеолит-Al2O3 носителе расположен во втором реакторе гидроочистки (1), первый реактор (1') размещен выше по потоку от второго реактора (1).
16. Устройство по п.15, где устройство включает трубопровод рециркуляции продукта (80) для циркуляции потока продукта из смеси углеводородных компонентов, полученного из второго реактора (1), в первый реактор (1').
17. Устройство по любому из пп.12-16, где устройство содержит секцию очистки (13), которая расположена выше по потоку от по меньшей мере одного реактора гидроочистки (1, 1').
18. Устройство по п.12, где устройство включает сепаратор (2) для разделения углеводородных фракций бензинового, дизельного, реактивного и лигроинового диапазона.
19. Устройство по п.18, где тяжелую углеводородную фракцию удаляют из сепаратора и направляют по кругу в первый реактор через канал (11).
20. Применение углеводородных компонентов, полученных способом по любому из пп.1-11 в качестве топлива или в качестве присадки в топливные композиции.
21. Применение NiW катализатора на цеолит-Al2O3 носителе для изомеризации н-парафинов, полученных при гидроочистке сырья, содержащего талловое масло и терпеновые соединения.
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FI20095767L (fi) 2009-07-07 2011-01-08 Upm Kymmene Corp Menetelmä ja laite tärpätin konvertoimiseksi bensiinikomponenteiksi
SG178893A1 (en) * 2009-09-08 2012-04-27 Exxonmobil Res & Eng Co Fuel production from feedstock containing lipidic material
FI128142B (fi) * 2010-02-02 2019-10-31 Upm Kymmene Corp Menetelmä ja laitteisto hiilivetyjen tuottamiseksi

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FI20105583A7 (fi) 2011-12-12
US20130072730A1 (en) 2013-03-21
CN106590722B (zh) 2019-04-19
EP2576732A1 (en) 2013-04-10
FI125632B (fi) 2015-12-31
CA2800478C (en) 2018-01-02
RU2566763C2 (ru) 2015-10-27
BR112012029964A2 (pt) 2016-09-20
US9382483B2 (en) 2016-07-05
FI20105583L (fi) 2011-12-12
CA2800478A1 (en) 2011-12-01
CN106590722A (zh) 2017-04-26
CN103003392A (zh) 2013-03-27
FI20105583A0 (fi) 2010-05-25
WO2011148046A1 (en) 2011-12-01
BR112012029964B1 (pt) 2019-03-26

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