RU2018125263A - Способ и устройство для превращения этилена, присутствующего в головном потоке из установки FCC, в целях повышения производства пропилена - Google Patents

Способ и устройство для превращения этилена, присутствующего в головном потоке из установки FCC, в целях повышения производства пропилена Download PDF

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RU2018125263A
RU2018125263A RU2018125263A RU2018125263A RU2018125263A RU 2018125263 A RU2018125263 A RU 2018125263A RU 2018125263 A RU2018125263 A RU 2018125263A RU 2018125263 A RU2018125263 A RU 2018125263A RU 2018125263 A RU2018125263 A RU 2018125263A
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stream
ethylene
gasoline
section
gas
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RU2018125263A
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RU2767522C2 (ru
RU2018125263A3 (ru
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Беатрис ФИШЕР
Венсан КУПАР
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Ифп Энержи Нувелль
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
    • C07C2/76—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation of hydrocarbons with partial elimination of hydrogen
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C6/00—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions
    • C07C6/02—Metathesis reactions at an unsaturated carbon-to-carbon bond
    • C07C6/04—Metathesis reactions at an unsaturated carbon-to-carbon bond at a carbon-to-carbon double bond
    • C07C6/06—Metathesis reactions at an unsaturated carbon-to-carbon bond at a carbon-to-carbon double bond at a cyclic carbon-to-carbon double bond
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B01D53/0423—Beds in columns
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
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    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
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    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
    • C10G11/04—Oxides
    • C10G11/05—Crystalline alumino-silicates, e.g. molecular sieves
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    • C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
    • C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
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    • C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
    • C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
    • C10G53/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step
    • C10G53/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step including only extraction steps, e.g. deasphalting by solvent treatment followed by extraction of aromatics
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    • C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
    • C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
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    • C10G57/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process
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    • C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
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    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
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    • F25J3/0209—Natural gas or substitute natural gas
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    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
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  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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Claims (21)

1. Устройство фракционирования газообразной фракции, выходящей из верхней части фракционной колонны установки каталитического крекинга, причем фракция содержит сжиженный нефтяной газ (СНГ), легкий бензин и остаточный газ, называемый "горючим газом", который сам содержит некоторое количество этилена, причем устройство включает в себя:
- первую секцию абсорбции (6), позволяющую разделить горючий газ (15) и поток (10) легкого бензина и СНГ, причем указанная секция обычно имеется в существующей установке каталитического крекинга,
- установку (22) каталитической конверсии этилена в пропилен и другие представляющие интерес продукты, причем сырьем для нее является горючий газ (15), в которой большая часть этилена превращается преимущественно в пропилен, а также ароматические соединения и другие представляющие интерес продукты в присутствии катализатора на основе цеолита,
- новую секцию абсорбции (31), в которую вводят потоки с установки конверсии (22) после повторного сжатия, причем пропилен, бутен и бензиновые фракции, содержащиеся в указанных потоках, извлекают в указанной секции абсорбции (31), используя бензин (32), поступающий из существующего дебутанизатора (11),
- вторую секцию (16) вспомогательной абсорбции, в которую вводят газ (33), выходящий из новой секции абсорбции (31),
- секцию дебутанизации (35), в которую вводят фракции СНГ и бензина (34), выходящие из новой секции абсорбции (31), и которая производит стабилизированный бензин (36) и легкую фракцию СНГ (37).
2. Устройство фракционирования газообразной фракции, выходящей из верхней части фракционной колонны установки каталитического крекинга по п. 1, причем установка (22) конверсии этилена в пропилен содержит по меньшей мере два реактора (223) и (227), разделенных промежуточным охлаждением потока (224) из первого реактора (223), идущего во второй реактор (227), в теплообменнике (225) на выходе реактора (227), и преобразованный поток (228) направляют на охлаждение.
3. Способ фракционирования газообразной фракции, выходящей из верхней части фракционной колонны установки каталитического крекинга, причем указанная фракция содержит СНГ, легкий бензин и остаточный газ, называемый "горючим газом", который в свою очередь содержит некоторое количество этилена, причем способ включает следующие стадии:
- разделение горючего газа (15) и потока (10) легкого бензина и СНГ в первой секции абсорбции (6), причем указанная первая секция имеется в существующей установке каталитического крекинга,
- превращение большой части этилена главным образом в пропилен, а также в ароматические соединения и другие представляющие интерес продукты, в присутствии катализатора на основе цеолита в установке (22) каталитической конверсии этилена в пропилен и другие представляющие интерес продукты, сырьем для которой является горючий газ (15),
- впуск потока, выходящего из установки конверсии (22), после повторного сжатия, в новую секцию абсорбции (31), причем пропилен, бутен и бензиновые фракции, содержащиеся в указанных потоках, выделяют в указанной новой секции абсорбции (31), используя бензин, поступающий из существующего дебутанизатора (11),
- ввод газа (33) из новой секция абсорбции (31) во вторую секцию вспомогательной абсорбции (16),
- ввод фракций СНГ и бензина (34), выходящих из новой секции абсорбции (31), в секцию дебутанизации (35), чтобы получить стабилизированный бензин (36) и легкую фракцию СНГ (37).
4. Способ по п. 3, причем установка (22) конверсии этилена в пропилен содержит по меньшей мере два реактора (223) и (227), разделенных промежуточным охлаждением потока (224) из первого реактора (223), направляемого во второй реактор (227), посредством теплообменника (225), причем на выходе реактора (227) преобразованный поток (228) направляют на охлаждение.
5. Способ по п. 3, причем часть газообразного потока (27), выходящего с установки (23) конверсии этилена в пропилен, возвращают на вход установки конверсии (22) после сжатия в компрессоре (26), причем указанная возвращаемая часть может составлять от 25% до 200% от потока (27), поступающего в новую секцию адсорбции (31).
6. Способ по п. 4, причем оба реактора установки конверсии (22) работают поочередно один в режиме реакции, а другой в режиме регенерации, причем реактор, работающий в режиме регенерации, соединен с секцией регенерации, содержащей теплообменник сырье/выходящий поток, холодильник, сепаратор, позволяющий сконденсировать воду реакции, и компрессор для рециркуляции регенерационного газа.
7. Способ по п. 6, причем, когда один из двух реакторов установки конверсии (22) находится в режиме регенерации, указанная регенерация осуществляется путем сжигания кокса, осажденного на катализаторе, в течение нескольких часов, нагнетая в регенерационный газ подходящее количество воздуха, возможно разбавленного инертным газом, например, азотом, или газообразными продуктами горения, обедненными кислородом, чтобы повышение температуры в реакторе не превышало 50°C.
8. Способ по п. 3, причем сырье (15) для установки конверсии (22) поступает в смеси с возвращаемым потоком (38), представляющим собой часть потока (27) на теплообменник (221) сырье/выходящий поток, причем оба смешанных потока предварительно нагревают до рабочей температуры, а затем направляют в реактор (223) установки конверсии (22), преобразованный поток (228) направляют в теплообменник (221) сырье - выходящий поток, где он охлаждается за счет косвенного обмена с сырьем (объединение потоков 15 и 38), затем в холодильник (230), где охлаждение завершается с помощью охлаждающей воды, и охлажденный поток (23) направляют в сепаратор (24), где жидкая фаза отделяется от газовой фазы, указанную газовую фазу (25) сжимают в компрессоре (26), затем направляют в новую секцию абсорбции (31), а жидкость (28) направляют в новую секцию абсорбции (31) с помощью наноса (29).
9. Способ по п. 3, причем установка конверсии этилена в пропилен (22) функционирует с катализатором на основе цеолита в следующих рабочих условиях:
- температура от 500°C до 650°C,
- парциальное давление этилена от 1 до 2 бар абс.
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