RU2012105283A - METHOD FOR CONVERSION OF HYDROCARBON RAW MATERIALS - Google Patents

METHOD FOR CONVERSION OF HYDROCARBON RAW MATERIALS Download PDF

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RU2012105283A
RU2012105283A RU2012105283/04A RU2012105283A RU2012105283A RU 2012105283 A RU2012105283 A RU 2012105283A RU 2012105283/04 A RU2012105283/04 A RU 2012105283/04A RU 2012105283 A RU2012105283 A RU 2012105283A RU 2012105283 A RU2012105283 A RU 2012105283A
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hydrotreated product
liquid
fraction
range
product
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RU2012105283/04A
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RU2543719C2 (en
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ДУСБЮРГ Эдмундо Стивен ВАН
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Шелл Интернэшнл Рисерч Маатсхаппий Б.В.
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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
    • 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
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/202—Heteroatoms content, i.e. S, N, O, P
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4018—Spatial velocity, e.g. LHSV, WHSV
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4093—Catalyst stripping
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/80—Additives
    • C10G2300/805—Water
    • C10G2300/807—Steam
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02—Gasoline
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/04—Diesel oil
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/08—Jet fuel

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Catalysts (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

1. Способ конверсии углеводородного сырья, включающий следующие стадии, на которых осуществляют:(a) контактирование исходного сырья с водородом в условиях проведения гидроочистки с получением гидроочищенного продукта;(b) обработку гидроочищенного продукта путем отделения по меньшей мере водорода от гидроочищенного продукта с получением жидкого потока гидроочищенного продукта;(c) обработку по меньшей мере части жидкого потока гидроочищенного продукта отпариванием для отделения легких продуктов от жидкого потока гидроочищенного продукта, в котором остается тяжелый гидроочищенный продукт;(d) разделение тяжелого гидроочищенного продукта в зоне разделения при пониженном давлении по меньшей мере на одну газообразную отпаренную фракцию и по меньшей мере жидкую отпаренную фракцию, при этом по меньшей мере часть жидкого отпаренного продукта повторно нагревают и возвращают обратно в зону разделения, причем по меньшей мере часть указанной жидкой отпаренной фракции повторно нагревают за счет теплообмена между по меньшей мере частью жидкого потока гидроочищенного продукта и/или по меньшей мере частью тяжелого гидроочищенного продукта.2. Способ по п.1, в котором углеводородное сырье содержит сернистые соединения, и условия проведения гидроочистки представляют собой условия гидродесульфуризации.3. Способ по п.1 или 2, в котором условия процесса гидроочистки включают температуру в интервале от 250°C до 480°C, давление в интервале от 10 до 150 бар и среднечасовую скорость подачи сырья от 0,1 до 10 ч.4. Способ по п.1 или 2, в котором катализатор содержит носитель и по меньшей мере один металл группы VIB и группы VIII Периодической та�1. A method for converting hydrocarbon feedstocks, comprising the following steps: (a) contacting the feedstock with hydrogen under conditions of hydrotreating to obtain a hydrotreated product; (b) treating the hydrotreated product by separating at least hydrogen from the hydrotreated product to obtain a liquid a hydrotreated product stream; (c) steaming at least a portion of the hydrotreated product fluid stream by stripping to separate light products from the hydrotreated product fluid stream the one in which the heavy hydrotreated product remains; (d) separating the heavy hydrotreated product in the separation zone under reduced pressure into at least one gaseous stripped fraction and at least a liquid stripped fraction, while at least a portion of the liquid stripped product is reheated and returning back to the separation zone, wherein at least a portion of said steamed liquid fraction is reheated by heat exchange between at least a portion of the hydrotreated product liquid stream and / or at least part of a heavy hydrotreated product. 2. The method according to claim 1, wherein the hydrocarbon feed contains sulfur compounds, and the conditions for hydrotreating are hydrodesulfurization conditions. The method according to claim 1 or 2, in which the conditions of the hydrotreating process include a temperature in the range from 250 ° C to 480 ° C, a pressure in the range from 10 to 150 bar and an hourly average feed rate from 0.1 to 10 hours. The method according to claim 1 or 2, in which the catalyst contains a carrier and at least one metal of group VIB and group VIII of the Periodic

Claims (15)

1. Способ конверсии углеводородного сырья, включающий следующие стадии, на которых осуществляют:1. The method of conversion of hydrocarbons, comprising the following stages, which carry out: (a) контактирование исходного сырья с водородом в условиях проведения гидроочистки с получением гидроочищенного продукта;(a) contacting the feedstock with hydrogen under conditions of hydrotreating to obtain a hydrotreated product; (b) обработку гидроочищенного продукта путем отделения по меньшей мере водорода от гидроочищенного продукта с получением жидкого потока гидроочищенного продукта;(b) treating the hydrotreated product by separating at least hydrogen from the hydrotreated product to obtain a liquid hydrotreated product stream; (c) обработку по меньшей мере части жидкого потока гидроочищенного продукта отпариванием для отделения легких продуктов от жидкого потока гидроочищенного продукта, в котором остается тяжелый гидроочищенный продукт;(c) treating at least a portion of the hydrotreated product fluid stream by stripping to separate light products from the hydrotreated product fluid stream in which the heavy hydrotreated product remains; (d) разделение тяжелого гидроочищенного продукта в зоне разделения при пониженном давлении по меньшей мере на одну газообразную отпаренную фракцию и по меньшей мере жидкую отпаренную фракцию, при этом по меньшей мере часть жидкого отпаренного продукта повторно нагревают и возвращают обратно в зону разделения, причем по меньшей мере часть указанной жидкой отпаренной фракции повторно нагревают за счет теплообмена между по меньшей мере частью жидкого потока гидроочищенного продукта и/или по меньшей мере частью тяжелого гидроочищенного продукта.(d) separating the heavy hydrotreated product in the separation zone under reduced pressure into at least one gaseous stripped fraction and at least a liquid stripped fraction, wherein at least a portion of the liquid stripped product is reheated and returned to the separation zone, at least at least a portion of said steamed liquid fraction is reheated by heat exchange between at least a portion of the hydrotreated product fluid stream and / or at least a portion of the heavy hydrotreated product itself. 2. Способ по п.1, в котором углеводородное сырье содержит сернистые соединения, и условия проведения гидроочистки представляют собой условия гидродесульфуризации.2. The method according to claim 1, in which the hydrocarbon feedstock contains sulfur compounds, and the conditions for hydrotreating are hydrodesulfurization conditions. 3. Способ по п.1 или 2, в котором условия процесса гидроочистки включают температуру в интервале от 250°C до 480°C, давление в интервале от 10 до 150 бар и среднечасовую скорость подачи сырья от 0,1 до 10 ч-1.3. The method according to claim 1 or 2, in which the conditions of the hydrotreating process include a temperature in the range from 250 ° C to 480 ° C, a pressure in the range from 10 to 150 bar and an hourly average feed rate from 0.1 to 10 h -1 . 4. Способ по п.1 или 2, в котором катализатор содержит носитель и по меньшей мере один металл группы VIB и группы VIII Периодической таблицы, предпочтительно сульфидированный.4. The method according to claim 1 or 2, in which the catalyst contains a carrier and at least one metal of group VIB and group VIII of the Periodic table, preferably sulfidized. 5. Способ по п.1 или 2, в котором отпаривание осуществляют с помощью водяного пара.5. The method according to claim 1 or 2, in which the steaming is carried out using water vapor. 6. Способ по п.1 или 2, в котором указанное отпаривание проводят при температуре в интервале от 100°C до 350°C и давлении в интервале от 1 до 50 бар.6. The method according to claim 1 or 2, in which the specified steaming is carried out at a temperature in the range from 100 ° C to 350 ° C and a pressure in the range from 1 to 50 bar. 7. Способ по п.1 или 2, в котором зона разделения на стадии (d) включает в себя отпарную секцию.7. The method according to claim 1 or 2, in which the separation zone in stage (d) includes a stripping section. 8. Способ по п.7, в котором зона разделения на стадии (d) в дополнение к отпарной секции включает в себя секцию ректификации.8. The method according to claim 7, in which the separation zone in stage (d) in addition to the stripping section includes a rectification section. 9. Способ по п.1 или 2, в котором теплообмен с указанной по меньшей мере частью жидкой отпаренной фракции осуществляют с указанной по меньшей мере частью жидкого потока гидроочищенного продукта.9. The method according to claim 1 or 2, in which heat exchange with the specified at least part of the liquid stripped fraction is carried out with the specified at least part of the liquid stream of the hydrotreated product. 10. Способ по п.1 или 2, в котором теплообмен с указанной по меньшей мере частью жидкой отпаренной фракции осуществляют с указанной по меньшей мере частью тяжелого гидроочищенного продукта.10. The method according to claim 1 or 2, in which heat exchange with the specified at least part of the liquid stripped fraction is carried out with the specified at least part of a heavy hydrotreated product. 11. Способ по п.1 или 2, в котором по меньшей мере 90 мас.% жидкой отпаренной фракции, предпочтительно всю жидкую отпаренную фракцию, повторно нагревают посредством теплообмена.11. The method according to claim 1 or 2, in which at least 90 wt.% Of the liquid stripped fraction, preferably the entire liquid stripped fraction, is reheated by heat exchange. 12. Способ по п.1 или 2, в котором часть жидкой отпаренной фракции извлекают в качестве продукта, содержащего средний дистиллят.12. The method according to claim 1 or 2, in which part of the liquid stripped fraction is recovered as a product containing a middle distillate. 13. Способ по п.1 или 2, в котором газообразную отпаренную фракцию разделяют по меньшей мере на фракцию, содержащую нафту, и водяную фракцию.13. The method according to claim 1 or 2, in which the gaseous stripped fraction is divided into at least a fraction containing naphtha and a water fraction. 14. Способ по п.1 или 2, в котором зона разделения представляет собой ректификационную колонну, в которой температура находится в интервале от 80°C до 300°C, а давление в интервале от 0,005 до 1 бар.14. The method according to claim 1 or 2, in which the separation zone is a distillation column in which the temperature is in the range from 80 ° C to 300 ° C, and the pressure in the range from 0.005 to 1 bar. 15. Способ по п.1 или 2, в котором по меньшей мере часть указанной жидкой отпаренной фракции повторно нагревают до температуры в интервале от 125°C до 350°C. 15. The method according to claim 1 or 2, in which at least a portion of the specified liquid stripped fraction is reheated to a temperature in the range from 125 ° C to 350 ° C.
RU2012105283/04A 2009-07-15 2010-07-15 Hydrocarbon stock conversion procedure RU2543719C2 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
EP09165519.1 2009-07-15
EP09165519 2009-07-15
PCT/EP2010/060257 WO2011006977A2 (en) 2009-07-15 2010-07-15 Process for the conversion of a hydrocarbonaceous feedstock

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RU2012105283A true RU2012105283A (en) 2013-08-20
RU2543719C2 RU2543719C2 (en) 2015-03-10

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US (1) US20120125819A1 (en)
EP (1) EP2454347B1 (en)
CN (1) CN102471701A (en)
IN (1) IN2012DN00236A (en)
RU (1) RU2543719C2 (en)
WO (1) WO2011006977A2 (en)

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RU2543719C2 (en) 2015-03-10
WO2011006977A3 (en) 2011-05-19
EP2454347B1 (en) 2018-03-28
US20120125819A1 (en) 2012-05-24
WO2011006977A2 (en) 2011-01-20
CN102471701A (en) 2012-05-23
EP2454347A2 (en) 2012-05-23
IN2012DN00236A (en) 2015-05-01

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