RU2015143652A - Способ улучшения низкотемпературных свойств и увеличения выхода среднедистиллятного исходного сырья через полностью жидкостную гидроочистку и депарафинизацию - Google Patents
Способ улучшения низкотемпературных свойств и увеличения выхода среднедистиллятного исходного сырья через полностью жидкостную гидроочистку и депарафинизацию Download PDFInfo
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- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
- C10G45/22—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing with hydrogen dissolved or suspended in the oil
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- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
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- C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
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- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
- C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
- C10G45/62—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used containing platinum group metals or compounds thereof
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- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
- C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
- C10G45/64—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
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- C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
- C10G49/18—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 in the presence of hydrogen-generating compounds, e.g. ammonia, water, hydrogen sulfide
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- C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
- C10G49/22—Separation of effluents
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- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
- C10G65/043—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a change in the structural skeleton
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- C10L1/00—Liquid carbonaceous fuels
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- C10L10/00—Use of additives to fuels or fires for particular purposes
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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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Claims (22)
1. Полностью жидкостный способ гидрообработки исходного сырья среднедистиллятного топлива, включающий
(a) введение в контакт исходного сырья с (i) разбавителем и (ii) водородом с получением смеси исходного сырья/разбавителя/водорода, где водород растворяют в смеси для получения жидкого сырья;
(b) введение в контакт смеси исходного сырья/разбавителя/водорода с катализатором гидрообработки в первой реакционной зоне, с получением первого эффлюента продукта и
(c) введение в контакт первого эффлюента продукта с катализатором депарафинизации во второй реакционной зоне, с получением второго эффлюента продукта, содержащего лигроин и среднедистиллятный продукт;
где среднедистиллятный продукт имеет по меньшей мере одно улучшенное низкотемпературное свойство по сравнению с исходным сырьем среднедистиллятного топлива и имеет выход по меньшей мере 85 мас.%.
2. Способ по п. 1, где исходное сырье среднедистиллятного топлива имеет содержание азота по меньшей мере 200 wppm (массовых частей на миллион), и среднедистиллятный продукт имеет температуру помутнения, по меньшей мере на 15°C более низкую по сравнению с исходным сырьем среднедистиллятного топлива.
3. Способ по п. 1, где исходное сырье среднедистиллятного топлива имеет содержание азота по меньшей мере 200 wppm, и среднедистиллятный продукт характеризуется увеличением соотношения изо- и н-парафинов по меньшей мере 1,5 по сравнению с исходным сырьем среднедистиллятного топлива.
4. Способ по п. 1, где исходное сырье среднедистиллятного топлива имеет содержание азота по меньшей мере 90 wppm, и среднедистиллятный продукт имеет температуру помутнения, по меньшей мере на 25°C более низкую по сравнению с исходным сырьем среднедистиллятного топлива.
5. Способ по п. 1, где исходное сырье среднедистиллятного топлива имеет содержание азота по меньшей мере 90 wppm, и среднедистиллятный продукт характеризуется увеличением соотношения изо- и н-парафинов по меньшей мере 18 по сравнению с исходным сырьем среднедистиллятного топлива.
6. Способ по п. 1, где стадии (b) и (c) проводят в одном реакторе, содержащем один или более слоев катализатора.
7. Способ по п. 1, где стадии (b) и (c) проводят в отдельных реакторах, при этом каждый из реакторов содержит один или более слоев катализатора.
8. Способ по п. 1, где первый эффлюент продукта содержит растворенные в нем H2S и NH3 и подается непосредственно во вторую реакционную зону.
9. Способ по п. 1, где первая реакционная зона имеет температуру в пределах диапазона от приблизительно 225°C до приблизительно 425°C и давление в пределах диапазона от приблизительно 3,0 МПа до приблизительно 17,5 МПа.
10. Способ по п. 1, где вторая реакционная зона имеет температуру в пределах диапазона от приблизительно 225°C до приблизительно 425°C и давление в пределах диапазона от приблизительно 3,0 МПа до приблизительно 17,5 МПа.
11. Способ по п. 1, где и исходное сырье среднедистиллятного топлива, и среднедистиллятный продукт являются дизельными топливами.
12. Способ по п. 1, где катализатор депарафинизации содержит кристаллическую, микропористую структуру оксида.
13. Способ по п. 1, где катализатор депарафинизации содержит цеолит.
14. Способ по п. 13, где цеолит имеет 8-членную кольцевую структуру, 10-членную кольцевую структуру или 12-членную кольцевую структуру.
15. Способ по п. 1, где катализатор депарафинизации содержит цеолит, не имеющий удерживаемого на нем металла.
16. Способ по п. 1, дополнительно включающий введение в контакт второго эффлюента продукта с катализатором гидрообработки в третьей реакционной зоне с получением третьего эффлюента продукта.
17. Способ по п. 1, дополнительно включающий выделение второго эффлюента продукта.
18. Способ по п. 1, дополнительно включающий рециркуляцию части второго эффлюента продукта для применения в качестве всего разбавителя или его части.
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US5100535A (en) * | 1987-12-03 | 1992-03-31 | Mobil Oil Corporation | Method for controlling hydrocracking operations |
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US7569136B2 (en) * | 1997-06-24 | 2009-08-04 | Ackerson Michael D | Control system method and apparatus for two phase hydroprocessing |
US7803269B2 (en) * | 2007-10-15 | 2010-09-28 | Uop Llc | Hydroisomerization process |
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US8377286B2 (en) | 2008-12-31 | 2013-02-19 | Exxonmobil Research And Engineering Company | Sour service hydroprocessing for diesel fuel production |
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US9499750B2 (en) | 2016-11-22 |
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