US3718575A - Hydrocracking for lpg production - Google Patents

Hydrocracking for lpg production Download PDF

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Publication number
US3718575A
US3718575A US00161586A US3718575DA US3718575A US 3718575 A US3718575 A US 3718575A US 00161586 A US00161586 A US 00161586A US 3718575D A US3718575D A US 3718575DA US 3718575 A US3718575 A US 3718575A
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reaction zone
hydrocracking
further characterized
liquid phase
boiling range
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C Watkins
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Honeywell UOP LLC
Universal Oil Products Co
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Universal Oil Products Co
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Assigned to UOP, DES PLAINES, IL, A NY GENERAL PARTNERSHIP reassignment UOP, DES PLAINES, IL, A NY GENERAL PARTNERSHIP ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: KATALISTIKS INTERNATIONAL, INC., A CORP. OF MD
Assigned to UOP, A GENERAL PARTNERSHIP OF NY reassignment UOP, A GENERAL PARTNERSHIP OF NY ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: UOP INC.
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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
    • 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
    • C10G65/10—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only cracking steps
    • 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
    • C10G2400/28—Propane and butane

Definitions

  • ABSTRACT Liquefied petroleum gas herein referred to as LPG
  • LPG is produced from heavy hydrocarbon distillates through the utilization of a two-stage hydrocracking process.
  • the product effluent from the first stage is separated to provide a vaporous gasoline boiling range fraction which is utilized as the charge stock to the second stage.
  • the present invention involves a process for the conversion of heavy stocks into lower-boiling hydrocarbon products. More specifically, the inventive concept herein described is directed toward a two-stage hydrocracking process for the direct production of LPG from heavier-than-gasoline hydrocarbon fractions and/or distillates.
  • gasoline boiling range hydrocarbons is intended to connote various hydrocarbon fractions having an end boiling point which may range from about 350F. to about 450F. To some extent, the precise boiling range for a naphtha fraction depends upon the particular locale in which the same is defined.
  • suitable charge stocks include kerosene fractions, light gas oils boiling up to a temperature of about 700F., heavy vacuum or atmospheric gas oils boiling up to a temperature of about 1,050F. and either intermediate, or overlapping fractions and mixtures thereof.
  • Charge stocks, containing hydrocarbons which normally boil above a temperature of l,050F. are suitable but will generally require a special form of pretreatment for the purpose of convetting the 1,050F.-plus material into lower-boiling hydrocarbons as well as eliminating metallic and asphaltenic contaminants.
  • LPG serves as a substitute for natural gas primarily for cooking and heating.
  • a much preferred use for LPG is acknowledged to be as charge stock in a steam-reforming process for the production of a methane-rich synthetic natural gas, which is often referred to as town'gas.”
  • One object of the present invention is to convert heavy hydrocarbonaceous charge stocks to lower-boiling hydrocarbon products.
  • a corollary objective is to produce maximum quantities of a propane/butane concentrate (LPG) from charge stocks boiling above the gasoline boiling range.
  • LPG propane/butane concentrate
  • Another object of my invention is to afford a simplified, multi-stage process for the production of LPG from charge stocks boiling above the normal gasoline boiling range.
  • my invention is directed toward a process for the production of liquefied petroleum gas, which process comprises the steps of: (a) reacting a hydrocarbonaceous charge stock, boiling above the gasoline boiling range, and hydrogen in a first reaction zone, at hydrocracking conditions selected to produce gasoline boiling range hydrocarbons; (b) separating the resulting first reaction zone effluent in a first separation zone, at substantially the same pressure and at a temperature to provide a first vaporous phase containing gasoline boiling range hydrocarbons, and a first liquid phase containing hydrocarbons boiling above the gasoline boiling range; (0) reacting said first vaporous phase, in a second reaction zone, at hydrocracking conditions selected to convert normally liquid hydrocarbons to liquefied petroleum gas components; (d) separating the resulting second reaction zone effluent, in a second separation zone, at substantially the same pressure and a temperature in the range of about 60 to about F. to provide a second vaporous phase and a second liquid phase; and, (e) further separating said second liquid phase
  • LPG can be produced in relatively high yields from naphthas, or gasoline boiling range hydrocarbons, having end boiling points in the range of about 350F. to about 450F.
  • the general practice is to produce a naphtha charge stock with and end boiling point of about 380F. to about 410F.
  • charge stocks containing extremely heavy components e.g., those having normal boiling points in the range of 900F. to about l,050F.
  • a relatively high severity operation is required to maximize the yields of the LPG propane/butane concentrate.
  • the high severity operation required to convert such heavy components directly to LPG, produces an adverse effect upon the stability of the catalytic composite employed in the reaction zone.
  • a common practice involves the initial conversion of such heavy hydrocarbonaceous material into a 400F. end point naphtha through the use of a multiple-stage system, with a naphtha product subsequently being processed in a separate reaction zone for conversion into LPG.
  • the present invention involves a multiple-stage hydrocracking system for the direct production of liquefied petroleum gas from hydrocarbon charge stocks boiling above the normal gasoline boiling range.
  • These heavy charge stocks for example, a full boiling range gas oil having an initial boiling point of about 500F. and an end boiling point of about 1,050F., are generally contaminated through the inclusion of sulfurous and nitrogenous compounds.
  • These charge stocks will, therefore, generally be subjected to a hydrotreating, or hydrorefining technique whereby the deleterious contaminating influences are converted into hydrogen sulfide, ammonia and hydrocarbons.
  • I-Iydrorefining, or desulfurization reactions are effected at a maximum catalyst bed temperature of about 600F. to about 850F.
  • Suitable desulfurization catalysts are thoroughly described in the literature, and only brief reference thereto is necessary therein.
  • Suitable catalytic composites generally comprise a siliceous refractory inorganic oxide carrier material and at least one metallic component selected from the metals and compounds of the metals of Groups VHS and VIII of the Periodic Table.
  • One commonly employed carrier material is a composite of alumina and from about 10.0 to about 90.0 percent by weight of silica.
  • Suitable metallic components include chromium, molybdenum, tungsten, iron, cobalt and nickel.
  • the Group VI-B metal such as molybdenum, is usually present within the range of about 4.0 through about 30.0 percent by weight.
  • the Group VIII metals, such as nickel is present in an amount in the range of about 0.01 to about 10.0 percent by weight. In those instances where the catalytic composite is to contain a Group VIII noble metal, the same is generally present in an amount within the range of about 0.01 to about 2.0 percent by weight.
  • maximum catalyst bed temperatures will be within the range of about 650F. to about 950F. and preferably from about 700F. to about 900F. In most applications of the present invention, the maximum catalyst bed temperature within the second hydrocracking reaction zone will be higher than that in the first hydrocracking reaction zone.
  • the hydrocracking reaction zones are maintained under an imposed pressure in the range of about 1,000 to about 5,000 psig., and preferably from about 1,000 to about 2,500 psig.
  • the rate of hydrocarbon charge will be in the range of about 0.25 to about 5.0 liquid hourly space velocity, and the hydrogen concentration will be in an amount of about 3,000 to about 30,000 scf/Bbl.
  • the hydrocracking catalytic composites will comprise at least one metallic component selected from groups VI-B and VIII of the Periodic Table, rhenium, tin and germanium, and a composite and from about 12.0 to about 30.0 percent by weight of alumina.
  • a particularly preferred catalytic composite for utilization in the second hydrocracking reaction zone wherein the greater proportion of LPG is produced, is one where the metallic components are impregnated or ion-exchanged upon a crystalline aluminosilicate molecular sieve, a variety of which are commonly referred to in the art by the broad term zeolites.
  • one such catalyst which exhibits the desired characteristics of stability and activity is a composite of about 5.3 percent by weight of nickel and a synthetically prepared faujasite which is distributed throughout a silica matrix.
  • suitable zeolitic materials include mordenite, Type X or Type Y molecular sieves, as well as zeolitic material which is dispersed within an amorphous matrix of alumina, silica, or alumina-silica.
  • a quench. stream either normally liquid, or normally gaseous, may be introduced at one or more points in the hydrocracking reaction zone.
  • the fresh feed charge stock in admixture with hydrogen and a 400F.-plus normally liquid recycle stream, is introduced into the first hydrocracking reaction zone at a temperature such that the increasing temperature gradient is maintained at the desired, predetermined level.
  • the total product effluent is introduced, at substantially the same pressure, into a hot separator from which the gasoline boiling range hydrocarbons are removed as a vaporous phase.
  • the temperature of the first zone effluent Prior to entering the hot separator, the temperature of the first zone effluent is decreased, via heatexchange to a level such that the vaporous fraction will contain a minimum of material boiling above the gasoline boiling range.
  • the unconverted portion of the fresh feed charge stock is withdrawn from the hot separator as the liquid phase, and recycled to combine with the fresh feed charge stock.
  • the vaporous phase serves as the charge to the second hydrocracking reaction zone, wherein the same is subjected to conversion to liquefied petroleum gas. It is within the scope of the present invention to divert a portion of the effluent from the first hydrocracking reaction zone to a suitable separation system. This affords a measure of flexibility in that it permits recovery of gasoline boiling range material when fluctuations in marketing considerations so demand.
  • the pressure imposed on the second hydrocracking reaction zone is substantially the same as that at which the vaporous phase is withdrawn from the hot separator; however, the temperature will be increased to provide a higher severity operation.
  • the effluent from the second hydrocracking reaction zone is cooled to a temperature in the range of about 60F. to about F. and introduced into a cold separator.
  • a hydrogen-rich vaporous phase is withdrawn from the cold separator and recycled, by compressive means to combine with the fresh feed charge stock to the first hydrocracking zone.
  • Make-up hydrogen required to supplant that consumed within the overall process and lost via solution, is preferably introduced into the hydrogen recycle line downstream of the compressive means.
  • Pressure control over the entire system is facilitated by monitoring the pressure of the vaporous phase as it emanates from the cold separator.
  • a normally liquid phase, containing unreacted gasoline boiling range hydrocarbons, pentanes, hexanes, and the desired propane/butane concentrate is withdrawn from the cold separator and introduced into a suitable separation system wherein the various streams are recovered.
  • the unreacted gasoline boiling range hydrocarbons are, at least in part, preferably recycled to combine with the material being charged to the second reaction zone.
  • a portion of the unreacted gasoline boiling range hydrocarbons is admixed with the effluent from the first reaction zone prior to introducing the same into the hot separator.
  • the fresh feed charge stock is subjected to a hydrorefining technique utilizing a catalytic composite of an alumina-silica carrier material containing 37.0 percent by weight of silica, combined with 1.8 percent by weight of nickel and 16.0 percent by weight of molybdenum, calculated on an elemental basis.
  • the reaction zone is maintained under an imposed pressure of about 2,000 psig., with a maximum catalyst bed tem' perature of about 850F.
  • the fresh feed charge rate is 4,500 barrels per day, the hydrogen concentration is about 6,500 scf/Bbl. and the liquid hourly space velocity is 0.70.
  • Hydrogen consumption, within the hydrorefining system is about 770 scf/Bbl. or 1.32 percent by weight of the total fresh feed.
  • Table 11 The hydrorefining yields and product distribution are presented in the following Table 11:
  • the charge in line 1 is admixed with about 2,400 barrels per day of a normally liquid recycle stream from line 2, the source of which is hereinafter set forth, resulting in a combined liquid feed ratio of about 1.6.
  • Recycle hydrogen in an amount of about 10,000 scfJBbl is admixed via line 3, the total charge continuing through line 1 into hydrocracking reactor 4.
  • Reactor 4 is maintained under an imposed pressure of about 2,100 psig., with a maximum catalyst bed temperature of about 750F.
  • the liquid hourly space velocity, based only upon the 4,035 barrels per day of fresh feed, is 0.81.
  • the product effluent is withdrawn by way of line 5 and, following heat-exchange to reduce its temperature to a level of about 400F., is introduced into hot separator 6 at a pressure of about 2,075 psig.
  • the product yield and distribution from hydrocracking reactor 4 is given in the following Table 111:
  • a principally vaporous phase is withdrawn from hot separator 6 by way of line 7, combined with unreacted naphtha in line 8 and the 634 BbL/day of naphtha from the hydrorefining system (not illustrated in the drawing), the mixture continuing through line 7 into the second hydrocracking reaction zone 9.
  • the charge enters reaction zone 9 at a pressure of about 2,050 psig. the maximum catalyst bed temperature being about 900F.
  • the liquid hourly space velocity is about 1.0, and the quantity of hydrogen is the same as in reactor 4, less that which was consumed by the reactions being effected therein.
  • the product effluent from reaction zone 9 is withdrawn by way of line 10 and introduced into cold separator 11 at a pressure of about 2,025 lbs. following heat-exchange and further cooling to reduce the temperature to a level of about F.
  • a hydrogen-rich recycle gaseous phase is withdrawn through line 3 and admixed with the charge stock in line 1, while a principally liquid phase, containing the propane/butane concentrate is withdrawn by way of line 12 and introduced into separation system 13.
  • Ethane and lighter components are indicated as being withdrawn through line 14, the propane/butane concentrate through line 15, the pentane/hexane concentrate through line 16 and about 1,700 Bbl./day of normally liquid material by way of line 8 for recycle to combine with the vaporous phase in line 7.
  • Hydrogen consumption in reactor 9 is 1,560 scf./Bbl. of the total heptane-390F. material being charged thereto. Since the combined liquid feed ratio is 1.5, the hydrogen consumption, based only on fresh heptane- 390F. feed, is about 937 scf./Bbl.
  • Liquefied Petroleum Gas is produced in a total amount of 4,020 BbL /day, inclusive of the 111 BbL/day derived from the hydrorefining reaction zone, or 89.3 vol. percent of the original fresh feed of 4,500 Bbl./day.
  • a process for the production of liquefied petroleum gas which comprises the steps of:
  • first and second reaction zones are catalytic, and contain a catalytic composite of a porous carrier material and at least one metallic component selected from Groups Vl-B and VIII of the Periodic Table.
  • the process of claim 5 further characterized in that the catalyst disposed in said first reaction zone is a composite of an amorphous carrier material, a Group Vl-B metal component and an iron-group metal component.
  • the process of claim 5 further characterized in that the catalyst disposed in said second reaction zone is a composite of a zeolitic carrier material and a Group VIII metal component.

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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)
US00161586A 1971-07-12 1971-07-12 Hydrocracking for lpg production Expired - Lifetime US3718575A (en)

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AR (1) AR220881A1 (pl)
AU (1) AU458034B2 (pl)
BR (1) BR7204613D0 (pl)
CA (1) CA978126A (pl)
ES (1) ES404746A1 (pl)
FR (1) FR2145546B1 (pl)
GB (1) GB1391649A (pl)
IL (1) IL39832A (pl)
IT (1) IT965901B (pl)
NL (1) NL7209605A (pl)
PL (1) PL89010B1 (pl)
SE (1) SE373833B (pl)
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Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3847796A (en) * 1973-03-15 1974-11-12 Universal Oil Prod Co Hydrocracking process for the production of lpg
US3882014A (en) * 1972-10-26 1975-05-06 Universal Oil Prod Co Reaction zone effluents separation and hydrogen enrichment process
US3917562A (en) * 1974-07-16 1975-11-04 Universal Oil Prod Co Combination process for the conversion of heavy distillates to LPG
US3963600A (en) * 1974-07-16 1976-06-15 Universal Oil Products Company Combination process for the conversion of heavy distillates to LPG
US4247386A (en) * 1979-08-06 1981-01-27 Mobil Oil Corporation Conversion of hydrocarbons to olefins
US4842718A (en) * 1986-09-30 1989-06-27 Shell Oil Company Process for recovery of hydrocarbons from a fluid feed
US4875991A (en) * 1989-03-27 1989-10-24 Amoco Corporation Two-catalyst hydrocracking process
US6379533B1 (en) * 2000-12-18 2002-04-30 Uop Llc Hydrocracking process for production of LPG and distillate hydrocarbons
US20040038166A1 (en) * 2002-08-26 2004-02-26 Yan Tsoung Y. Self-propelled liquid fuel
US20120273390A1 (en) * 2011-04-28 2012-11-01 E. I. Du Pont Nemours And Company Liquid-full hydroprocessing to improve sulfur removal using one or more liquid recycle streams
WO2015128039A1 (en) * 2014-02-25 2015-09-03 Saudi Basic Industries Corporation Process for converting hydrocarbons into olefins
WO2015128037A1 (en) * 2014-02-25 2015-09-03 Saudi Basic Industries Corporation Process for converting hydrocarbons into olefins
WO2016102249A1 (en) 2014-12-22 2016-06-30 Sabic Global Technologies B.V. Process for producing lpg and btx
WO2016102248A1 (en) 2014-12-22 2016-06-30 Sabic Global Technologies B.V. Process for producing c2 and c3 hydrocarbons
WO2016102250A1 (en) 2014-12-22 2016-06-30 Sabic Global Technologies B.V. Process for producing lpg and btx
WO2016102247A1 (en) 2014-12-22 2016-06-30 Sabic Global Technologies B.V. Process for producing c2 and c3 hydrocarbons
WO2017101985A1 (en) 2015-12-15 2017-06-22 Sabic Global Technologies B.V. Process for producing c2 and c3 hydrocarbons

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS6238179U (pl) * 1985-08-26 1987-03-06
MY135793A (en) 2002-07-12 2008-06-30 Basf Ag Method for the production of butadiene from n-butane

Citations (6)

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US3047490A (en) * 1958-11-04 1962-07-31 Phillips Petroleum Co Hydrocracking process
US3215617A (en) * 1962-06-13 1965-11-02 Cities Service Res & Dev Co Hydrogenation cracking process in two stages
US3256178A (en) * 1965-05-25 1966-06-14 Union Oil Co Hydrocracking process
US3516925A (en) * 1964-03-10 1970-06-23 British Petroleum Co Catalytic conversion of hydrocarbons
US3607723A (en) * 1969-03-28 1971-09-21 Texaco Inc Split flow hydrocracking process
US3617483A (en) * 1968-04-25 1971-11-02 Texaco Inc Hydrocracking process

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3047490A (en) * 1958-11-04 1962-07-31 Phillips Petroleum Co Hydrocracking process
US3215617A (en) * 1962-06-13 1965-11-02 Cities Service Res & Dev Co Hydrogenation cracking process in two stages
US3516925A (en) * 1964-03-10 1970-06-23 British Petroleum Co Catalytic conversion of hydrocarbons
US3256178A (en) * 1965-05-25 1966-06-14 Union Oil Co Hydrocracking process
US3617483A (en) * 1968-04-25 1971-11-02 Texaco Inc Hydrocracking process
US3607723A (en) * 1969-03-28 1971-09-21 Texaco Inc Split flow hydrocracking process

Cited By (42)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3882014A (en) * 1972-10-26 1975-05-06 Universal Oil Prod Co Reaction zone effluents separation and hydrogen enrichment process
US3847796A (en) * 1973-03-15 1974-11-12 Universal Oil Prod Co Hydrocracking process for the production of lpg
US3917562A (en) * 1974-07-16 1975-11-04 Universal Oil Prod Co Combination process for the conversion of heavy distillates to LPG
US3963600A (en) * 1974-07-16 1976-06-15 Universal Oil Products Company Combination process for the conversion of heavy distillates to LPG
US4247386A (en) * 1979-08-06 1981-01-27 Mobil Oil Corporation Conversion of hydrocarbons to olefins
US4842718A (en) * 1986-09-30 1989-06-27 Shell Oil Company Process for recovery of hydrocarbons from a fluid feed
US4875991A (en) * 1989-03-27 1989-10-24 Amoco Corporation Two-catalyst hydrocracking process
US6379533B1 (en) * 2000-12-18 2002-04-30 Uop Llc Hydrocracking process for production of LPG and distillate hydrocarbons
US20040038166A1 (en) * 2002-08-26 2004-02-26 Yan Tsoung Y. Self-propelled liquid fuel
US6953870B2 (en) * 2002-08-26 2005-10-11 Tsoung Y Yan Self-propelled liquid fuel
KR20140037852A (ko) * 2011-04-28 2014-03-27 이 아이 듀폰 디 네모아 앤드 캄파니 하나 이상의 액체 재순환 스트림을 사용하여 황 제거를 개선시키기 위한 액체-풀 수소화가공
CN103502396B (zh) * 2011-04-28 2016-03-30 纳幕尔杜邦公司 使用一个或多个液体再循环流以改善除硫的全液加氢处理
RU2615133C2 (ru) * 2011-04-28 2017-04-04 Е.И.Дюпон Де Немур Энд Компани Полностью жидкостная гидроочистка для улучшения удаления серы с применением одного или нескольких рециркуляционных потоков жидкости
US8926826B2 (en) * 2011-04-28 2015-01-06 E I Du Pont De Nemours And Company Liquid-full hydroprocessing to improve sulfur removal using one or more liquid recycle streams
CN103502396A (zh) * 2011-04-28 2014-01-08 纳幕尔杜邦公司 使用一个或多个液体再循环流以改善除硫的全液加氢处理
US20120273390A1 (en) * 2011-04-28 2012-11-01 E. I. Du Pont Nemours And Company Liquid-full hydroprocessing to improve sulfur removal using one or more liquid recycle streams
WO2015128039A1 (en) * 2014-02-25 2015-09-03 Saudi Basic Industries Corporation Process for converting hydrocarbons into olefins
EA033166B1 (ru) * 2014-02-25 2019-09-30 Сауди Бейсик Индастриз Корпорейшн Способ конверсии углеводородов в олефины
EA032846B1 (ru) * 2014-02-25 2019-07-31 Сауди Бейсик Индастриз Корпорейшн Способ конверсии углеводородов в олефины
US10316259B2 (en) * 2014-02-25 2019-06-11 Saudi Basic Industries Corporation Process for converting hydrocarbons into olefins
WO2015128037A1 (en) * 2014-02-25 2015-09-03 Saudi Basic Industries Corporation Process for converting hydrocarbons into olefins
CN106062148A (zh) * 2014-02-25 2016-10-26 沙特基础工业公司 用于将烃转化成烯烃的方法
CN106062147A (zh) * 2014-02-25 2016-10-26 沙特基础工业公司 用于将烃转化成烯烃的方法
CN106062148B (zh) * 2014-02-25 2019-01-15 沙特基础工业公司 用于将烃转化成烯烃的方法
US10301561B2 (en) * 2014-02-25 2019-05-28 Saudi Basic Industries Corporation Process for converting hydrocarbons into olefins
CN106062147B (zh) * 2014-02-25 2018-07-24 沙特基础工业公司 用于将烃转化成烯烃的方法
WO2016102247A1 (en) 2014-12-22 2016-06-30 Sabic Global Technologies B.V. Process for producing c2 and c3 hydrocarbons
US10287517B2 (en) 2014-12-22 2019-05-14 Sabic Global Technologies B.V. Process for producing C2 and C3 hydrocarbons
US10087378B2 (en) 2014-12-22 2018-10-02 Sabic Global Technologies B.V. Process for producing LPG and BTX
USRE49154E1 (en) 2014-12-22 2022-08-02 Sabic Global Technologies B.V. Process for producing LPG and BTX
US10174263B2 (en) 2014-12-22 2019-01-08 Sabic Global Technologies B.V. Process for producing C2 and C3 hydrocarbons
US10526551B2 (en) * 2014-12-22 2020-01-07 Sabic Global Technologies B.V. Process for producing C2 and C3 hydrocarbons
US10287518B2 (en) 2014-12-22 2019-05-14 Sabic Global Technologies B.V. Process for producing LPG and BTX
WO2016102249A1 (en) 2014-12-22 2016-06-30 Sabic Global Technologies B.V. Process for producing lpg and btx
WO2016102248A1 (en) 2014-12-22 2016-06-30 Sabic Global Technologies B.V. Process for producing c2 and c3 hydrocarbons
WO2016102250A1 (en) 2014-12-22 2016-06-30 Sabic Global Technologies B.V. Process for producing lpg and btx
WO2017101985A1 (en) 2015-12-15 2017-06-22 Sabic Global Technologies B.V. Process for producing c2 and c3 hydrocarbons
KR20180093907A (ko) * 2015-12-15 2018-08-22 사빅 글로벌 테크놀러지스 비.브이. C2 및 c3 탄화수소 제조 방법
CN108368435A (zh) * 2015-12-15 2018-08-03 沙特基础工业全球技术有限公司 生产c2和c3烃类的方法
CN108368435B (zh) * 2015-12-15 2020-10-20 沙特基础工业全球技术有限公司 生产c2和c3烃类的方法
EP3390582A1 (en) * 2015-12-15 2018-10-24 SABIC Global Technologies B.V. Process for producing c2 and c3 hydrocarbons
EP3390582B1 (en) * 2015-12-15 2024-02-21 SABIC Global Technologies B.V. Process for producing c2 and c3 hydrocarbons

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FR2145546B1 (pl) 1978-01-06
AR220881A1 (es) 1980-12-15
IL39832A (en) 1975-04-25
FR2145546A1 (pl) 1973-02-23
PL89010B1 (pl) 1976-10-30
JPS5127242B1 (pl) 1976-08-11
IT965901B (it) 1974-02-11
NL7209605A (pl) 1973-01-16
AU4442572A (en) 1974-01-17
ES404746A1 (es) 1975-07-01
IL39832A0 (en) 1972-09-28
GB1391649A (en) 1975-04-23
DE2233826B2 (de) 1975-11-13
AU458034B2 (en) 1975-02-13
SE373833B (pl) 1975-02-17
DE2233826A1 (de) 1973-02-08
BR7204613D0 (pt) 1973-05-24
ZA724588B (en) 1973-04-25
SU506302A3 (ru) 1976-03-05
CA978126A (en) 1975-11-18

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