US3542667A - Process for the production of aromatic and olefinic hydrocarbons - Google Patents

Process for the production of aromatic and olefinic hydrocarbons Download PDF

Info

Publication number
US3542667A
US3542667A US714869A US3542667DA US3542667A US 3542667 A US3542667 A US 3542667A US 714869 A US714869 A US 714869A US 3542667D A US3542667D A US 3542667DA US 3542667 A US3542667 A US 3542667A
Authority
US
United States
Prior art keywords
pyrolysis
aromatics
aromatic
temperature
steam
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US714869A
Other languages
English (en)
Inventor
Joseph F Mcmahon
John J Loporto
George F Adams
Dana L Smith
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Sunoco Inc
Foster Wheeler Inc
Original Assignee
Sun Oil Co
Foster Wheeler Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Sun Oil Co, Foster Wheeler Inc filed Critical Sun Oil Co
Application granted granted Critical
Publication of US3542667A publication Critical patent/US3542667A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • 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
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
    • C10G69/06—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of thermal cracking in the absence of hydrogen
    • 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
    • C10G2400/20—C2-C4 olefins
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/40—Ethylene production

Definitions

  • the present invention relates to a process for obtaining from a naphtha feed stock two valuable products
  • an aromatic product including benzene and toluene, and an olefin product, primarily ethylene.
  • lNaphtha is a fraction obtained from crude distillation -of virgin petroleum oil. It boils in the gasoline range of approximately 150-400 F., and is a low value product,
  • the general practice has been to process naphthas Vcontaining a high proportion of parains to obtain a high olen yield, since an increased aromatic content was fusually associated with a decreased olenic yield.
  • the naphtha should ybe naphthenic in character containing a quantity, up to 5%, and preferably 30 to 50% naphthenes, as precursors of benzene and other aromatics.
  • the remainder of the naphtha is aliphatic, primarily straight-chain parains.
  • a known process for producing both ethylene and ben- "zene from-naphtha includes the step of subjecting the naphtha Afeed stockito reforming, followed by solvent extraction of Aaromatics from the reformate.
  • the reforming which may be carried out at about 900 F. in the presence of a catalyst and at a pressure between 100 and 600 p.s.i. produces a high yield of high octane reformate in which the cyclic naphthenes are converted to Athe aromatics.
  • a suitable solvent such as diethylene g'lycol extracts aromatics form ⁇ the reformate leaving a parafnic raffinate suitable for subsequent treatment. Solvent extraction is necessary, as
  • a second method for obtaining benzene and ethylene from a naphtha feed stock includes first subjecting the naphtha to pyrolysis in the presence of steam, at a high temperature, and in the absence of a catalyst to crack the long chain aliphatics to ethylene.
  • the pyrolsis is followed by hydrotreating, solvent extraction to produce an aromatic rich extract, and hydrodealkylation of the aromatics to yield benzene. ⁇
  • the straight chain single bonded parains are cracked to the double bonded olefns, and the naphthenes are partly converted to aromatics.
  • this second method suffers from the same disadvantage as the previous method mentioned above, namely the expense of solvent extraction.
  • the pyrolysis step causes a cracking of naphthenes particularly if the conditions are severe enough to obtain a high degree of removal of paraflins from the boiling range of the aromatics formed.
  • the present invention comprises the steps of catalytically reforming a naphtha fed stock (wherein the cyclic naphthenes are converted to aromatics), then subjecting the liquid reformate to pyrolysis or cracking in the presence of steam at high severity conditions so as to produce a highly aromatic liquid and a gaseous oleinic stream.
  • Ethylene is produced from the latter, and the aromatic liquid stream is subjected rst to hydrotreating, and then simple distillation to remove separate butane and pentane cuts, leaving substantially pure aromatic stream from which benzene can be produced.
  • the essence of the present invention is the discovery that a reformate stock could be subjected to cracking under such conditions as to avoid destruction of cyclic compounds, but at the same time reduce the molecular weight of the aliphatics to that which permits their separation from the cyclic compounds by simple distillation or fractionation methods.
  • the pyrolysis is severe, being carried out at a temperature in the range of 1300 F. to 1700 F., with an outlet temperature which preferably is in the range of 1450 F. to 1550 F., a preferred residence time between about 0.24 and about 0.60 second, and preferably a steam to hydrocarbon weight ratio of from zero to about 4.0.
  • FIG. 1 is a flow diagram illustrating the method in accordance with the invention, including those steps to produce benzene;
  • FIG. 2 is a graph showing pyrolysis conditions illustrating the concepts of the invention.
  • virgin petroleum naphtha obtained by crude distillation of petroleum oil, boils in the gasoline range of 150 to 400 F. and contains more than 5% naphthenic compounds preferably 30 to 50% naphthenes.
  • This naptha is introduced in line 12 to a desulfurization reactor 14, which is conventional, followed by cooling and HZS removal (item 16).
  • the naphtha is then preheated, in heater 18, and is contacted in vessel 20 with a reforming catalyst such as platinumalumina, or chromia-alumina, in the presence of hydrogen introduced in line 21 so that a substantial part of the naphthene compounds in the virgin naphtha are converted to aromatic compounds.
  • the reforming step is carried out at a temperature in the range of 600 F.
  • the hydrocarbon reformate from the reforming step is condensed in cooler 22, is separated in separator 23 from hydrogen product gas ,(which may be recycled to the naphtha feed stream via line 21), and is then reheated in heat exchanger 24.
  • Recycle low molecular weight hydrocarbons, for instance C olens from a later cut (to be described) in line 26 are mixed with the hydrocarbon effluent, as is stream, in line 28, and the mixture is then subjected to high severity (high temperature) pyrolysis cracking in heater 30.
  • Preferred pyrolysis conditions are a temperature in the range of 1300 to 1700 F., with outlet temperatures in the range of 1450 to 1550 F., preferably 1500 F.; a pressure in the range of 0 to 60 p.s.i.g.; a steam to hydrocarbon weight ratio of 0.1 to 2.0 (about 0.5 to mols of steam per mole of hydrocarbon); and a contact or residence time in the pyrolysis zone in the range of 0.05 to 1.0 second, preferably between 0.24 and 0.60 second.
  • the results of the cracking step can be understood by consideration of the effluent streams from quench tower 32, the gaseous pyrolysis product being subjected to quench in a conventional manner l(construction of such a tower and quench conditions are well known).
  • quench tower 32 From the quench tower 32, there are three product streams, an overhead gas stream in line 34 heading from the top of the tower 32, an intermediate side liquid stream or fraction in line 36, and a -bottom product in line 37.
  • the overhead stream or pyrolysis gas is primarily ethylene the conditions of pyrolysis causing cracking of the high boiling point long-chain aliphatics to the lower molecular weight lower 'boiling point double bonded olens and some diolefins.
  • the intermediate liquid steam or fraction of line 36 boils in the range of 169 F. to 350 F. and contains the bulk of the aromatics, which as mentioned, have been virtually unaffected in the pyrolysis step (in a subsequent example, it will be shown that a 90% or higher recovery of C5 ring compounds in the feed can be achieved, indicating little destruction of cyclic compound in the pyrolysis step), and some C4 and C5 butane cuts to be described.
  • a heavy 350 F. plus steam primarily cyclic compounds may be withdrawn from the bottom of the quench tower.
  • the hydrocarbon pyrolysis liquid line 36 from the quench tower 32 may be subjected to mild hydrotreating conditions in reactor 42 in which small quantities of olefinic and diolenic compounds are hydrogenated to the corresponding parafnic compounds without effecting hydrogenation of aromatic rings contained in the liquid.
  • This is a well known step, and the C., and C5 hydrogenated hydrocarbons can then be easily and readily fractionally distilled from the C5 ring compounds in the towers 38 and 40 to produce an aromatics rich fraction in line 44 boiling in the range of F. to 350 F.
  • Pentane and 'butane cuts are obtained in lines 46 and 48 respectively, and the pentane cut ⁇ (line 46) can then be recycled to line 26, mentioned above. This is for the purpose of making more ethylene in the pyrolysis reaction, increasing ethylene yield, the pentane being pyrolyzed to ethylene under the conditions in the furnace 30.
  • the pyrolysis hydrocarbon liquid from the quench zone, in line 36 can be fractionally distilled to produce an aromatics-rich fraction boiling between 150 F. and 350 F. which contains benzene, toluene, xylenes and other monocyclic aromatics, with subsequent treatment of olefins and diolens in the pyrolysis liquid effluent.
  • the pyrolysis gas stream (line 34) containing ethylene, propylene, butadiene and other light olens is sent to suitable recovery apparatus for the treatment of the pyrolysis product gas by conventional methods and recovery of ethylene.
  • the aromatics-rich fraction in line 44 may be sent to conventional dealkylation reactor S0 wherein methyl groups and other side chains are removed from C, and C8 aromatics to produce a benzene product.
  • This is carried out in the presence or absence of a catalyst, usually at a temperature of 1000 F. to 1300 F., a pressure in the range of 200 to 1000 p.s.i. and at a hydrogen to hydrocarbon mole ratio in the feed of about 1 to 10.
  • Stabilizer 56 and benzene tower 52 both simple distillation towers, complete the benzene recovery apparatus.
  • the pyrolysis reaction is more clearly illustrated with reference to FIG. 2.
  • This graph shows in curve A the variations with outlet temperature of non-aromatics essentially C5 and higher in the pyrolysis liquid stream following the pyrolysis reaction, quenching, and simple fractionation in vessels 38 and 40; reflecting, in other words, the percent non-aromatics remaining after pyrolysis which are so close in boiling point to the aromatics that they were not separated from the aromatics by fractionation.
  • the space velocities are lbs./hour/cu. ft. at about 15 p.s.i.g. outlet pressure.
  • the graph also shows in curves B and C variation in loss of C6 ring compounds with pyrolysis outlet temperature, the data of curve C being obtained at a space velocity in the range of 141 to 148, and that of curve B being obtained at a higher space velocity (lower residence time) of 433 to 442.
  • curve A it is apparent that at low outlet temperatures, for instance 1400 F., there will be clearly a substantial percentage of non-aromatics remaining in the pyrolysis liquid stream, indicating that there was little cracking of the higher boiling point aliphatics (C5 and higher).
  • FIG. 2 also shows that the cracking of the aliphatic compounds is not affected by throughput or space velocity (SV) (forinstance, at Y1500'? P. the percent non-aromatics remaining following the distillation steps of 38 and 40 is about 3% at space velocities of both 148 and 442), although the loss in C6 ring structure compounds is affected, being higher at the lower space velocity of 148 (curve C) as compared to a space velocity of about 442 for curve B. Accordingly a preferred space velocity is in the order of 442 lbs./hour/cu. ft. (about 0.24 second) although a 10% loss of aromatics is not excessive, and a contact time of about 0.60 second (148 lbs./hour/cu. ft.) is within the scope of this invention.
  • SV space velocity
  • the hot gas is admitted at the bottom of the tower, and spray quench water at the top. Trays near the middle of the tower collect the condensed 169-350 F. liquid, controls in the tower controlling the flow of quench water to maintain this temperature level on the collecting trays.
  • the above described catalytic reformate was vaporized, mixed with steam in a weight ration of 0.78 lb. steam per pound of oil, and the mixture preheated to a temperature of 1200 F.
  • the preheated mixture was passed through a steam pyrolysis coil which was contained in a heater red with natural gas.
  • the heater tubes were '1/2 inch Incoloy Schedule 40 pipe forming a series of loops in a vertical plane of the firebox.
  • the furnace was divided into four zones separated by refractory bridge walls. The first zone contained a steam coil and a preheater coil connected in series. The last three zones were reaction sections in which pyrolysis of hydrocarbons occurred.
  • the mixture of vaporized water and hydrocarbon is preheated to 1200 F in the preheat zone.
  • process fluid temperatures werecontrolled to establish a rising temperature profile in which the rate of temperature rise was highest in the rst reaction zone and lowest in the last reaction zone, typical profiles being:
  • flow rate of the catalyticreformate was 442.0 lbs. of oil per hour per cubic foot of coil volume.
  • the oil-steam mixture left the pyrolysis coil at a temperature of 1503 F. and a pressure of 14.8 p.s.i.g. Eluent from the pyrolysis coil was cooled to a temperature of about 750 VF. immediately after leaving the heater.
  • Product vapors were then cooled to 60 F. with water and refrigerant.
  • Pyrolysis liquid product and water were separated from gaseous product in the liquid accumulator. The following product yields and product qualities were obtained based on analysis of gaseous and liquid streams:
  • the catalytic reformate described in Example 1 was vaporized, mixed with steam in a weight ratio of 0.81 lb. steam per pound of oil and the mixture preheated to a temperature of 1200 F.
  • the preheated mixture was passed through the pyrolysis coil at a ow rate of 141 lbs. of oil per hour per cubic foot of coil volume.
  • the oilsteam mixture left the pyrolysis coil at a temperature of 1551e F. and a pressure of 15.0 p.s.i.g.
  • xylene yield decreased from 20.5 weight percent of feed at zero contact time to 8 weight percent of feed at 0.6 second contact time.
  • Toluene yield decreased from 19.6 weight percent to 17 weight percent and benzene yield increased from 7 to l1 weight percent over the same range of residence times.
  • Styrene yield reached a maximum of 4 weight percent at 0.25 second contact time and then decreased at longer residence times. Maximum styrene yield was about 30% higher than the concentration of ethylbenzene in the feedstock.
  • outlet temperature decreased from 94% at 0.25 second contact time to 87% at 0.6 second contact time.
  • outlet temperature C6 ring recovery varied from 91% to 85% over the same range of residence times.
  • a decrease in steam to hydrocarbon ratio from 0.8 to 0.55 increased C6 ring recovery at 1550 F., outlet temperature. This result was presumably due to increased formation of aromatics from the parai'linic and naphthene components of the feedstock.
  • the advantages of the process of this invention arise from the fact that an aromatics-rich liquid is produced directly from the pyrolysis step of the process thereby eliminating the need for extraction to separate parains from aromatics.
  • the process of this invention requires less processing equipment than conventional methods which require extraction.
  • the process of this invention provides higher yields of aromatics or benzene than conventional processes in which virgin naphtha is subjected directly to pyrolysis conditions without prior catalytic reforming, in that the naphthenes in the feedstock are less able to withstand the rigors of pyrolysis than the aromatics of the pyrolysis feedstock of the present invention.
  • the stream entering the pyrolysis furnace in the present invention is aromatic, the severity of cracking can be greater producing a higher purity benzene or aromatic yield.
  • the quenching being for a sufficient time and at such temperature as to produce a gas stream which is predominantly ethylene, and a liquid side stream which boils in the range of about 169 F. to about 350 F. and is primarily aromatic.
  • a process according to claim 5 including the step of preheating the reformate to a temperature of about 1200 F. prior to pyrolysis, the pyrolysis reaction being carried out at increasing temperatures in the range of about 1200 F. to about 1550 F.
  • coil outlet pressure in the pyrolysis step is about 15 p.s.i.g.
  • the quenching being at such temperature and for a sufficient period of time to produce a gas stream which is predominantly ethylene, and a liquid stream which boils in the range of about 169 F. to about 350 F. and is primarily aromatic, the liquid stream representing a recovery of at least about C6 ring compounds in the feed stock.
  • a process according to claim 11 including the steps of hydrotreating the pyrolysis liquid stream under such conditions as to hydrogenate oleiins and dioleiins therein to corresponding paraflinic compounds;
  • Pressure range 0 p.s.i.g. to 60 p.s.i.g.
  • the process further including the steps of hydrotreating the liquid stream to convert oleiins and diolefins therein to corresponding parains;

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (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)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US714869A 1968-03-21 1968-03-21 Process for the production of aromatic and olefinic hydrocarbons Expired - Lifetime US3542667A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US71486968A 1968-03-21 1968-03-21

Publications (1)

Publication Number Publication Date
US3542667A true US3542667A (en) 1970-11-24

Family

ID=24871781

Family Applications (1)

Application Number Title Priority Date Filing Date
US714869A Expired - Lifetime US3542667A (en) 1968-03-21 1968-03-21 Process for the production of aromatic and olefinic hydrocarbons

Country Status (6)

Country Link
US (1) US3542667A (fr)
BE (1) BE730303A (fr)
DE (1) DE1914603A1 (fr)
FR (1) FR2004468A1 (fr)
GB (1) GB1258807A (fr)
NL (1) NL6904390A (fr)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3869377A (en) * 1971-12-14 1975-03-04 Metallgesellschaft Ag Production of extrapure aromatics
US4053388A (en) * 1976-12-06 1977-10-11 Moore-Mccormack Energy, Inc. Process for preparing aromatics from naphtha
US4133842A (en) * 1977-10-25 1979-01-09 Uop Inc. Production and recovery of linear mono-olefins
US4166025A (en) * 1973-08-22 1979-08-28 Bocharov Jury N Process for purifying aromatic hydrocarbons
US20080011645A1 (en) * 2006-07-13 2008-01-17 Dean Christopher F Ancillary cracking of paraffinic naphtha in conjuction with FCC unit operations
US20110226668A1 (en) * 2006-07-13 2011-09-22 Dean Christopher F Ancillary cracking of heavy oils in conjunction with fcc unit operations
US9458394B2 (en) 2011-07-27 2016-10-04 Saudi Arabian Oil Company Fluidized catalytic cracking of paraffinic naphtha in a downflow reactor

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3114696A (en) * 1958-10-03 1963-12-17 Socony Mobil Oil Co Inc Upgrading of naphthas
US3215750A (en) * 1962-12-31 1965-11-02 Shell Oil Co Hydrogenation process for converting polyolefins or acetylenes to monoolefins
US3219419A (en) * 1957-06-07 1965-11-23 Braconier Frederic Fran Albert Adjustable quench pyrolysis furnace

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3219419A (en) * 1957-06-07 1965-11-23 Braconier Frederic Fran Albert Adjustable quench pyrolysis furnace
US3114696A (en) * 1958-10-03 1963-12-17 Socony Mobil Oil Co Inc Upgrading of naphthas
US3215750A (en) * 1962-12-31 1965-11-02 Shell Oil Co Hydrogenation process for converting polyolefins or acetylenes to monoolefins

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3869377A (en) * 1971-12-14 1975-03-04 Metallgesellschaft Ag Production of extrapure aromatics
US4166025A (en) * 1973-08-22 1979-08-28 Bocharov Jury N Process for purifying aromatic hydrocarbons
US4053388A (en) * 1976-12-06 1977-10-11 Moore-Mccormack Energy, Inc. Process for preparing aromatics from naphtha
US4133842A (en) * 1977-10-25 1979-01-09 Uop Inc. Production and recovery of linear mono-olefins
US20080011645A1 (en) * 2006-07-13 2008-01-17 Dean Christopher F Ancillary cracking of paraffinic naphtha in conjuction with FCC unit operations
US20110226668A1 (en) * 2006-07-13 2011-09-22 Dean Christopher F Ancillary cracking of heavy oils in conjunction with fcc unit operations
US20110240520A1 (en) * 2006-07-13 2011-10-06 Dean Christopher F Ancillary cracking of paraffinic naphtha in conjunction with fcc unit operations
US8877042B2 (en) 2006-07-13 2014-11-04 Saudi Arabian Oil Company Ancillary cracking of heavy oils in conjunction with FCC unit operations
US9458394B2 (en) 2011-07-27 2016-10-04 Saudi Arabian Oil Company Fluidized catalytic cracking of paraffinic naphtha in a downflow reactor

Also Published As

Publication number Publication date
FR2004468A1 (fr) 1969-11-21
FR2004468B1 (fr) 1974-03-15
GB1258807A (fr) 1971-12-30
DE1914603A1 (de) 1969-10-09
BE730303A (fr) 1969-09-22
NL6904390A (fr) 1969-09-23

Similar Documents

Publication Publication Date Title
US10822558B2 (en) Method for cracking a hydrocarbon feedstock in a steam cracker unit
KR102560961B1 (ko) 개선된 제품 수율을 갖는 원유를 석유화학제품으로 전환하기 위한 공정 및 장치
US9856425B2 (en) Method of producing aromatics and light olefins from a hydrocarbon feedstock
US20190322952A1 (en) Method for cracking a hydrocarbon feedstock in a steam cracker unit
US2953513A (en) Hydrogen donor diluent cracking process
US3726789A (en) Hydrocarbon conversion process for the production of olefins and aromatics
KR102374392B1 (ko) 탄화수소를 올레핀으로 전환하는 공정
EP3017027A1 (fr) Procédé de production d'oléfines et de composés aromatiques légers à partir d'une matière première hydrocarbonée
US10676681B2 (en) Process and installation for the conversion of crude oil to petrochemicals having an improved carbon-efficiency
US3472909A (en) Process for producing olefinic hydrocarbons
KR102454266B1 (ko) 고비점 탄화수소 공급원료를 보다 저비점의 탄화수소 생성물로 전환하는 방법
EP3110924B1 (fr) Procédé de convertion d'hydrocarbures en oléfines et btx.
US3103485A (en) Temperature
US3542667A (en) Process for the production of aromatic and olefinic hydrocarbons
US3457163A (en) Method for selective hydrogenation of diolefins with separation of gum formers prior to the reaction zone
IL35865A (en) High octane gasoline production
US2431243A (en) Conversion of hydrocarbon oils
US2974099A (en) Catalytic conversion of heavy naphtha fractions
US2400363A (en) Production of aromatics
US2313346A (en) Catalytic conversion of hydrocarbon oils
US2243298A (en) Process for the manufacture of gasoline and iso-octane
US2968605A (en) Preparation of high octane number motor fuel blending stocks
US2381466A (en) Hydrocarbon conversion process