WO2016179895A1 - Système combiné constitué de multiples séparateurs optimisés, son procédé d'utilisation, et procédé de conception - Google Patents

Système combiné constitué de multiples séparateurs optimisés, son procédé d'utilisation, et procédé de conception Download PDF

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Publication number
WO2016179895A1
WO2016179895A1 PCT/CN2015/084342 CN2015084342W WO2016179895A1 WO 2016179895 A1 WO2016179895 A1 WO 2016179895A1 CN 2015084342 W CN2015084342 W CN 2015084342W WO 2016179895 A1 WO2016179895 A1 WO 2016179895A1
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temperature
pressure separator
separator
low pressure
medium
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PCT/CN2015/084342
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English (en)
Chinese (zh)
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李苏安
邓清宇
王坤朋
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北京中科诚毅科技发展有限公司
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Publication of WO2016179895A1 publication Critical patent/WO2016179895A1/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • 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
    • C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes

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  • the invention relates to a combined method of a separator combined system and a separator, belonging to the fields of petrochemical and coal chemical industry.
  • the conventional separation method of the refinery is to set only one high-temperature high-pressure separator at the outlet of the reactor. After the gas-liquid phase separation, the liquid phase enters the fractionation column to be fractionated and then hydrogenated, and the gas phase enters the light hydrocarbon recovery unit. This will undoubtedly cause a large separation pressure on the subsequent light hydrocarbon recovery unit.
  • Another method is to set a high-temperature high-pressure separator at the outlet of the reactor, a first-stage online hydrogenation reactor is arranged at the gas phase outlet of the separator, the reaction product enters the medium-temperature high-pressure separator, and a secondary online hydrogenation reactor is arranged at the outlet of the intermediate-temperature separator.
  • the outlet of the secondary online hydrogenation reactor is further equipped with a normal temperature high pressure separator to realize cascade hydrogenation, which avoids the trouble of increasing pressure after liquid phase decompression.
  • a normal temperature high pressure separator to realize cascade hydrogenation, which avoids the trouble of increasing pressure after liquid phase decompression.
  • the CO and CO 2 produced by the hydroliquefaction of coal are methanated in the online hydrogenation reactor, which increases the hydrogen consumption on the one hand and generates a large amount of reaction heat on the other hand.
  • a large amount of cooling hydrogen or cooling oil is injected to stabilize the temperature of the reactor.
  • the purpose of the separator is to separate the material at the outlet of the reactor.
  • the common feature of heavy oil hydrogenation, direct coal liquefaction and oil-coal mixing reactor is high temperature and high pressure.
  • the composition of the reactor outlet material is complex and simple to pass through a high temperature and high pressure separator. It is unrealistic to separate the gas and liquid phases. Because in addition to hydrogen in the gas phase, there are a large number of light hydrocarbons, CO, CO 2 and sulfides and nitrides. To recycle the hydrogen, the remaining components must be removed to ensure the purity of the recycled hydrogen. In addition to light and heavy distillates in the liquid phase, crystals that may appear when cooling are required to be removed.
  • the present invention provides a multi-optimized separator combination system, which forms six separator combination systems by arranging and combining three different temperatures of high temperature, medium temperature and low temperature, and two different pressures of high pressure and low pressure.
  • the step temperature and pressure are formed, and the gas phase and liquid phase products of different products are separated one by one.
  • the separation of the gas phase achieves the purpose of reducing the operating pressure of the downstream device and ensuring the purity of the circulating hydrogen, and the separation of the liquid phase achieves the purpose of removing S and N.
  • the invention also provides a multi-optimized combination method and design method of the separator.
  • a multiple optimized splitter combination system comprising:
  • High temperature and high pressure separator operating temperature is 350-470 ° C, operating pressure is 17-22 MPa, its inlet is connected to the outlet of the hydrogenation reactor, the upper outlet is connected to the inlet of the medium temperature high pressure separator, and the lower outlet is connected to the inlet of the high temperature and low pressure separator. connection;
  • the medium temperature high pressure separator has an operating temperature of 250-330 ° C and an operating pressure of 17-22 MPa, the upper outlet is connected to the inlet of the normal temperature high pressure separator, and the lower outlet is connected to the inlet of the medium temperature low pressure separator;
  • Normal temperature high pressure separator operating temperature is 30-80 ° C, operating pressure is 17-22 MPa, the upper outlet flows out of the gas phase separation product, and the lower outlet is connected to the inlet of the normal temperature low pressure separator;
  • a high temperature and low pressure separator an operating temperature of 350-470 ° C, an operating pressure of 1-5 MPa, an upper outlet connected to the inlet of the medium temperature low pressure separator, and a lower outlet flowing out of the high temperature liquid phase separation product;
  • the medium temperature low pressure separator has an operating temperature of 250-330 ° C and an operating pressure of 1-5 MPa, the upper outlet is connected to the inlet of the low pressure normal temperature separator, and the lower outlet flows out of the intermediate temperature liquid phase separation product;
  • the normal temperature low pressure separator has an operating temperature of 30-80 ° C and an operating pressure of 1-5 MPa.
  • the upper outlet flows out of the gas phase separation product, and the lower outlet flows out of the normal temperature liquid phase separation product.
  • the ambient temperature low pressure separator is horizontally placed horizontally, and the remaining separators are vertically placed vertically.
  • Preferred high pressure high temperature, medium temperature and normal temperature separator inlets are on the side; low pressure high temperature, medium temperature and normal temperature separator inlets are placed at the top.
  • a preferred system can include a plurality of level control valves and a temperature changer, the level control valve being located between the high temperature and high pressure separator and the high temperature and low pressure separator, between the intermediate temperature high pressure separator and the medium temperature low pressure separator, and Between the normal temperature high pressure separator and the normal temperature low pressure distributor, the temperature converter is located between the high temperature and high pressure separator and the medium temperature high pressure separator, between the medium temperature high pressure separator and the low temperature high pressure separator, and the high temperature and low pressure separation Between the medium temperature and low pressure separator, the medium temperature low pressure separator and the normal temperature low pressure distributor.
  • the demineralized water is injected into the gas phase pipeline of the intermediate temperature high pressure separator and the upper outlet of the medium temperature low pressure separator, and the desalted water is recovered to the liquid collection bag in the normal temperature low pressure separator, and the lower portion of the liquid collection bag is connected to the wastewater.
  • Processing device The liquid collecting bag is a downwardly protruding bag provided at the lower part of the normal temperature low pressure separator. Since the density of water is larger than oil, the water is gathered. Collected in the liquid collection bag, the liquid collection bag and the separator are integrated.
  • reaction product of the hydrogenation separator outlet is connected to the coolant line prior to the inlet of the high temperature and high pressure separator.
  • the high temperature and high pressure separator, the medium temperature high pressure separator have the same pressure or the pressure difference of less than 5% at normal temperature and high pressure separation; the high temperature low pressure separator and the medium temperature low pressure separator have the same pressure or a pressure difference of less than 5 at normal temperature and low pressure separation.
  • the temperature of the high temperature and high pressure separator is the same as the temperature of the high temperature and low pressure separator or the temperature difference is less than 5%; the temperature of the medium temperature high pressure separator is the same as the temperature of the medium temperature low pressure separator or the temperature difference is less than 5%; the normal temperature and high temperature separator is The ambient temperature low pressure separator has the same temperature or a temperature difference of less than 5%.
  • the reaction product flowing out of the hydrogenation reactor enters the high-temperature high-pressure separator for gas-liquid separation, and the gas phase separated in the upper portion is cooled to enter the medium-temperature high-pressure separator, and the liquid phase separated in the lower portion is depressurized and then enters.
  • the high temperature and low pressure separator ;
  • the gas phase separated in the upper portion is cooled and then enters the normal-temperature high-pressure separator, and the liquid phase separated in the lower portion is depressurized and then enters the medium-temperature low-pressure separator;
  • the upper gas phase flows out of the circulating hydrogen separation product, and the liquid phase separated in the lower portion is depressurized and then enters the normal-temperature low-pressure separator;
  • the gas phase separated in the upper portion is cooled and then enters the medium-temperature low-pressure separator, and the liquid phase high-temperature oil separated in the lower portion is depressurized and flows out;
  • the medium-temperature low-pressure separator After the medium-temperature low-pressure separator performs gas-liquid separation, the upper gas phase is cooled and then enters a normal-temperature low-pressure separator, and the liquid phase intermediate oil separated in the lower portion is depressurized and flows out;
  • the upper gas phase tail gas After the gas-liquid separation of the normal-temperature low-pressure separator, the upper gas phase tail gas enters the gas processing device, and the liquid phase separated oil at the lower portion flows out.
  • the reaction product has a residence time of 0.5 to 5 minutes at the high temperature and high pressure separator; a residence time of 3 to 15 minutes at the intermediate temperature and high pressure separator; and a residence time of 3 to 35 minutes at the normal temperature and high pressure separator.
  • the residence time in the high temperature low pressure separator is 0.5-5 minutes; the residence time in the medium temperature low pressure separator is 3-15 minutes; and the residence time in the normal temperature low pressure separator is 3-15 minutes.
  • the above-mentioned multiple optimized separator combination is characterized by being used for heavy oil hydrogenation process, coal direct liquefaction process and oil coal mixing process, and heavy oil hydrogenation process refers to heavy crude oil, residual oil, catalytic oil slurry, and off One or more combinations of oil pitch and coal tar are processed as raw materials; the oil-coal mixing process refers to one or a combination of crude oil, residual oil, catalytic oil slurry, deoiled asphalt and coal tar, and lignite, One or more combinations of bituminous coal and non-stick coal are processed as raw materials, and the ratio of oil to coal ranges from 97:3 to 40:60.
  • design of the splitter combination system comprises:
  • High temperature and high pressure separator operating temperature is 350-470 ° C, operating pressure is 17-22 MPa, its inlet is connected to the outlet of the hydrogenation reactor, the upper outlet is connected to the inlet of the medium temperature high pressure separator, and the lower outlet is connected to the inlet of the high temperature and low pressure separator. connection;
  • the medium temperature high pressure separator has an operating temperature of 250-330 ° C and an operating pressure of 17-22 MPa, the upper outlet is connected to the inlet of the normal temperature high pressure separator, and the lower outlet is connected to the inlet of the medium temperature low pressure separator;
  • Normal temperature high pressure separator operating temperature is 30-80 ° C, operating pressure is 17-22 MPa, the upper outlet flows out of the gas phase separation product, and the lower outlet is connected to the inlet of the normal temperature low pressure separator;
  • a high temperature and low pressure separator an operating temperature of 350-470 ° C, an operating pressure of 1-5 MPa, an upper outlet connected to the inlet of the medium temperature low pressure separator, and a lower outlet flowing out of the high temperature liquid phase separation product;
  • the medium temperature low pressure separator has an operating temperature of 250-330 ° C and an operating pressure of 1-5 MPa, the upper outlet is connected to the inlet of the low pressure normal temperature separator, and the lower outlet flows out of the intermediate temperature liquid phase separation product;
  • the normal temperature low pressure separator has an operating temperature of 30-80 ° C and an operating pressure of 1-5 MPa.
  • the upper outlet flows out of the gas phase separation product, and the lower outlet flows out of the normal temperature liquid phase separation product.
  • the invention provides a multi-optimized separator combination system, which sets reasonable temperature and pressure change gradients, organically combines different temperature and pressure separators to form two rows of temperature reduction, pressure constant and three columns of temperature constant, pressure Reduced separator combination system.
  • the high-temperature/intermediate-temperature/normal-temperature high-pressure separator connected in sequence maintains the high pressure and the temperature gradually decreases.
  • the reactor outlet material is gas-liquid separated step by step, and the liquefied product is sent to the corresponding high-temperature/intermediate/normal-temperature low-pressure separator, and finally the gas phase. It is purified to obtain recycled hydrogen for recycling.
  • the high-temperature/intermediate-temperature/normal-temperature low-pressure separator connected in series maintains the low pressure and the temperature gradually decreases.
  • the temperature of the liquefied product flowing out from the lower outlet of the high-temperature high-pressure separator is constant, the pressure is lowered, and the high-pressure low-pressure separator is separated, and the vaporized product is sent.
  • the gas phase of the upper outlet of the high-temperature low-pressure separator and the liquid phase of the lower outlet of the intermediate-temperature high-pressure separator are received, and the gas phase formed by liquefaction and vaporization respectively due to changes in temperature or pressure enters the low-pressure normal temperature separator.
  • the bottom part separates the liquid oil in the liquid phase.
  • the liquid phase of the upper outlet of the intermediate-temperature low-pressure separator and the lower outlet of the normal-temperature high-pressure separator are received, and the gas phase formed by the liquefaction and vaporization of the gas phase and the liquid phase respectively is discharged as a tail gas from the upper portion due to changes in temperature or pressure.
  • the bottom liquid phase oil is separated at the bottom.
  • the invention can realize the purity of circulating hydrogen can be increased by 1.5-5.5 vol%, the amount of separated oil can be increased by 3.5-15 wt%, the hydrogen entrainment in the exhaust gas is reduced by 2-7%, and the oil entrainment in the wastewater is reduced by 5-18%.
  • the separator combination system of the present invention employs a combination of vertical and horizontal depending on the need to separate the product.
  • the inlets of high-pressure high-temperature, medium-temperature and normal temperature separators are on the side, mainly for fear that the separated light components will be pressed and coked at the inlet of the feed, hindering the feeding; low-pressure high-temperature, medium-temperature and normal temperature separators, more need to be considered convenient
  • the incoming material of the high pressure separator is received, so the inlet is placed at the top.
  • the level control valve is used to reduce the pressure and the temperature changer is used to reduce the temperature.
  • the gas phase of the outlet of the medium-temperature high-pressure separator and the outlet of the medium-temperature low-pressure separator is sprayed to remove salt water, and the purpose is to prevent the ammonium salt such as ammonium hydrogencarbonate and ammonium sulfide from being crystallized and deposited on the pipe wall at a low temperature to cause blockage.
  • the mixed gas phase material at the outlet of the reactor is first cooled to partially liquefy, facilitating separation by the high temperature and high pressure separator.
  • a multi-optimized separator is used in combination, and after the reaction product is cooled three times, the gaseous hydrogen gas is separated and separated in the gas phase under normal temperature and high pressure conditions for reuse in the hydrogenation reaction cycle; Under low pressure and high temperature conditions, the liquid phase separation obtains the high temperature oil into the fractionation process; after two times of cooling and one step of depressurization, the liquid phase separation under low pressure and medium temperature conditions obtains the medium temperature oil into the fractionation process; after three times of temperature reduction and two depressurization gas phase separation, the tail gas enters. In the gas treatment device, the liquid phase separation obtains the normal temperature oil and enters the fractionation process.
  • the method effectively removes the S and N compounds in the gas phase by injecting the salt water, thereby greatly reducing the corrosion degree of the downstream device.
  • FIG. 1 is a schematic view of a separator according to an embodiment of the present invention.
  • 1-high temperature high pressure separator 2-medium temperature high pressure separator; 3-normal temperature high pressure separator; 4-high temperature low pressure separator; 5 medium temperature low pressure separator; 6-normal temperature low pressure separator; 7-reaction product; 8-cooling 9-demineralized water; 10-cycle hydrogen; 11-tail gas; 12-normal temperature oil; 13-waste water; 14-medium temperature oil; 15-high temperature oil.
  • a multi-optimized separator combination system in this embodiment is composed of 6 separators with different temperatures and pressures, namely high temperature and high pressure separator 1, medium temperature high pressure separator 2, normal temperature high pressure separator 3, low pressure high temperature separator. 4. Low pressure intermediate temperature separator 5 and low pressure normal temperature separator 6. And spraying the demineralized water 9 in the gas phase at the outlet of the intermediate temperature high pressure separator 2 and the intermediate temperature low pressure separator 5, the purpose is to prevent the ammonium salt such as ammonium hydrogencarbonate and ammonium sulfide from being crystallized and deposited on the pipe wall at a low temperature to cause clogging, and the product can be further separated. Remove sulfur and nitrogen from it.
  • the normal temperature low pressure separator 6 is horizontally placed horizontally, and the remaining separators are vertically placed vertically.
  • the temperature of the reaction product 7 was 460 ° C, and after cooling to the high temperature and high pressure separator 1 by the coolant 8, the operating temperature was 420 ° C and the operating pressure was 18.7 MPa.
  • the gas phase separated in the upper part of the high-temperature high-pressure separator 1 is cooled and then enters the medium-temperature high-pressure separator 2, and the liquid phase is adjusted by the liquid level control valve and then enters the high-temperature low-pressure separator 4.
  • the operating temperature of the medium-temperature high-pressure separator 2 is 285 ° C, the operating pressure is 18.6 MPa, and the gas phase separated from the upper part is cooled, filled with water 9 and cooled to the normal temperature high-pressure separator 3, and the liquid phase is adjusted by the liquid level control valve to enter the intermediate temperature.
  • the low pressure separator 5 in addition to the gas phase injection of the medium temperature high pressure separator 2, the desalted water enters the normal temperature low pressure separator 6 and is finally collected by the liquid collection bag.
  • the normal temperature high pressure separator 3 has an operating temperature of 55 ° C and an operating pressure of 18.5 MPa.
  • the gas phase separated in the upper portion is used as the circulating hydrogen 10, and the lower liquid phase is adjusted by the liquid level control valve to enter the normal temperature low pressure separator 6.
  • the operating temperature of the high-temperature low-pressure separator 4 is 420 ° C, the operating pressure is 3.0 MPa, and the gas phase separated from the upper portion is cooled and then enters the medium-temperature low-pressure separator 5, and the liquid phase is adjusted by the liquid level control valve as a high-temperature oil 15 separator.
  • the operating temperature of the medium-temperature low-pressure separator 5 is 285 ° C, the operating pressure is 2.9 MPa, the upper gas phase is cooled, and after water injection, the demineralized water 9 of the medium-temperature high-pressure separator 2 enters the normal-temperature low-pressure separator 6, and the liquid phase is adjusted by the liquid level control valve. After that, it is used as a medium temperature oil 14 out of the medium temperature low pressure separator 5.
  • the normal temperature low pressure separator 6 operating temperature is 55 ° C, the operating pressure is 2.8 MPa, the upper gas phase as the exhaust gas 11 separator into the gas treatment device, the lower liquid phase as the normal temperature oil 12 out of the separator, the desalinated water is recovered to the normal temperature and low pressure separation
  • a liquid collection bag in the device, and the lower portion of the liquid collection bag is connected to the wastewater treatment device.
  • the liquid collecting bag is a downwardly protruding bag provided at the lower portion of the normal temperature low pressure separator 6. Since the density of water is larger than that of the oil, the water is collected in the liquid collecting bag, and the liquid collecting bag and the separator are integrated.
  • the wastewater 13 containing ammonium salts such as ammonium hydrogencarbonate and ammonium sulfide contained in the liquid collection bag is finally discharged to the wastewater treatment device.
  • the purity of the circulating hydrogen was increased by 4 vol%, the amount of separated oil was increased by 8 wt%, the hydrogen entrainment in the exhaust gas was reduced by 3%, and the oil entrainment in the waste water was reduced by 6%, as compared with the comparative example in which only one separator was used.
  • the multi-optimized separator combination method of the present invention is simple in operation, and can separate hydrogen in the gas phase from components such as light hydrocarbons, and can also separate S and N compounds therein. Come out, greatly reducing the degree of corrosion of downstream devices. At the same time, the light and heavy liquid oils are separated, and the pressure is low, and can directly enter the downstream fractionation tower.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

Cette invention concerne un système combiné constitué de multiples séparateurs optimisés, son procédé d'utilisation, et son procédé de conception. Le système combiné de séparateurs comporte un séparateur à haute température, haute pression, un séparateur à moyenne température, haute pression, un séparateur à température ambiante, haute pression, un séparateur à basse pression, haute température, un séparateur à basse pression, moyenne température, et un séparateur à basse pression, température ambiante. Trois températures différentes, à savoir, haute température, moyenne température, et basse température et deux pressions différentes, à savoir, haute pression et basse pression, sont permutées pour former un système combiné constitué de six séparateurs, qui forment des températures et des pressions graduées et séparent individuellement différents produits en phase gazeuse et produits en phase liquide. Ceci permet d'atteindre, en termes de séparation d'une phase gazeuse, le but consistant à réduire la pression de fonctionnement sur les équipements en aval tout en garantissant la pureté de l'hydrogène recyclé, et permet d'atteindre, en termes d'isolement d'une phase liquide, le but consistant à séparer S et N.
PCT/CN2015/084342 2015-05-08 2015-07-17 Système combiné constitué de multiples séparateurs optimisés, son procédé d'utilisation, et procédé de conception WO2016179895A1 (fr)

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CN104845664A (zh) * 2015-05-08 2015-08-19 北京中科诚毅科技发展有限公司 一种多重优化的分离器组合系统与使用方法及设计方法
CN105273759B (zh) * 2015-10-23 2018-04-17 北京中科诚毅科技发展有限公司 一种脱除结晶盐的方法及其设计方法和用途
CN113019038A (zh) * 2021-03-10 2021-06-25 北京中科诚毅科技发展有限公司 一种加氢分离工艺及其设计方法和用途

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1036600A (zh) * 1988-03-31 1989-10-25 国际壳牌研究有限公司 氢加工流出物的分离方法
CN1417301A (zh) * 2001-10-30 2003-05-14 中国石油化工股份有限公司 一种柴油深度脱硫脱芳烃的方法
CN1485413A (zh) * 2002-09-28 2004-03-31 中国石油化工股份有限公司 柴油深度脱硫脱芳烃的工艺方法
CN101239887A (zh) * 2008-02-01 2008-08-13 七台河宝泰隆煤化工有限公司 焦炉煤气制甲醇合成尾气联产煤焦油加氢制取油品工艺

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1088089C (zh) * 1999-10-13 2002-07-24 中国石油化工集团公司 一种烃类原料加氢处理方法
CN100510021C (zh) * 2007-01-22 2009-07-08 中国石油天然气华东勘察设计研究院 加氢反应流出物分离流程
CN101348235B (zh) * 2007-07-19 2013-08-07 中国石油化工集团公司 一种加氢装置的氢气回收方法
CN103242871B (zh) * 2013-05-28 2015-05-13 中国石油大学(华东) 一种重油-生物质加氢共液化处理工艺
CN104845664A (zh) * 2015-05-08 2015-08-19 北京中科诚毅科技发展有限公司 一种多重优化的分离器组合系统与使用方法及设计方法

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1036600A (zh) * 1988-03-31 1989-10-25 国际壳牌研究有限公司 氢加工流出物的分离方法
CN1417301A (zh) * 2001-10-30 2003-05-14 中国石油化工股份有限公司 一种柴油深度脱硫脱芳烃的方法
CN1485413A (zh) * 2002-09-28 2004-03-31 中国石油化工股份有限公司 柴油深度脱硫脱芳烃的工艺方法
CN101239887A (zh) * 2008-02-01 2008-08-13 七台河宝泰隆煤化工有限公司 焦炉煤气制甲醇合成尾气联产煤焦油加氢制取油品工艺

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
SHI, SHIDONG, BASIC ENGINEERING OF COAL HYDROLIQUEFACTION, 31 May 2012 (2012-05-31), ISBN: 978-7-122-07064-7 *

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