US3928174A - Combination process for producing LPG and aromatic rich material from naphtha - Google Patents

Combination process for producing LPG and aromatic rich material from naphtha Download PDF

Info

Publication number
US3928174A
US3928174A US538221A US53822175A US3928174A US 3928174 A US3928174 A US 3928174A US 538221 A US538221 A US 538221A US 53822175 A US53822175 A US 53822175A US 3928174 A US3928174 A US 3928174A
Authority
US
United States
Prior art keywords
fraction
reformate
product
components
aromatics
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
US538221A
Other languages
English (en)
Inventor
John C Bonacci
Henry P Ireland
Thomas R Stein
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.)
Mobil Oil AS
Original Assignee
Mobil Oil AS
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 Mobil Oil AS filed Critical Mobil Oil AS
Priority to US538221A priority Critical patent/US3928174A/en
Application granted granted Critical
Publication of US3928174A publication Critical patent/US3928174A/en
Priority to FR7540153A priority patent/FR2296606A1/fr
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
    • C10G59/00—Treatment of naphtha by two or more reforming processes only or by at least one reforming process and at least one process which does not substantially change the boiling range of the naphtha
    • C10G59/02—Treatment of naphtha by two or more reforming processes only or by at least one reforming process and at least one process which does not substantially change the boiling range of the naphtha plural serial stages only

Definitions

  • Reforming of hydrocarbons is a widely used process in petroleum technology for upgrading hydrocarbon fractions such as naphthas, gasolines and kerosines to improve the antiknock characteristics thereof.
  • Hydrocarbon fractions suitable for upgrading by reforming are composed of normal and branched paraffins, naphthenic hydrocarbons and even some aromatic hydrocarbons.
  • During reforming a multitude of reactions take place including dehydrogenation, isomerization, dehydrocyclization, hydrocracking, and combinations thereof to yield a product of increased aromatics con tent and branched chain hydrocarbons.
  • Normal and slightly branched paraffin hydrocarbons found in the above hydrocarbon fractions are generally of low octane rating. Highly branched-chain paraffin hydrocarbons, on the other hand, are characteristic of higher octane ratings. Therefore, one object of reforming is to effect isomerimtion of the normal and slightly branched chain paraftins to higher octane products by any one of the aforementioned reactions.
  • the production of aromatics during reforming is accomplished by one or more of the above identified reactions leading to the production of naphthenes which are then dehydrogenated to aromatics such as benzene, toluene and Xylene.
  • One method for producing aromatics involves the isomerization of alkyl cyclopentanes to form cyclohexanes which thereafter are dehydrogenated to aromatics.
  • This invention relates to a method and combination of processing steps for effecting a selective conversion and a rearrangement of petroleum hydrocarbon constituents to form aromatic enriched products and improve yields of LPG materials.
  • the present invention is concerned with one or more methods for selectively conducting chemical reactions with an arrangement of catalytic compositions possessing selective reaction properties with respect to different hydrocarbon components existing in the naphtha boiling range material.
  • the present invention relates to effecting a selective catalytic conversion of hydrocarbon components comprising, normal and isoparaffin hydrocarbon components in a se quence of hydrogenating conversion steps maintained under operating conditions selected to obtain products rich in aromatics and LPG material. More specifically, the invention is concerned with an arrangement and sequence of catalytic reactions designed to manipulate the reaction of hydrocracking, dehydrogenation, isomerization and dehydrocyclization to improve upon the yields of LPG products and aromatic components readily separated by distillation.
  • the present invention is concerned with contacting a relatively wide boiling range naphtha hydrocarbon material boiling in the range of C hydrocarbons up to about 380 or 400F. under selective reforming conditions in the presence of a platinum type reforming catalyst.
  • a platinum type reforming catalyst In this reforming operation the conditions employed lead to the production of relatively low octane branched and normal paraffin compounds which are available for conversion and production of additional LPG products.
  • the reforming catalyst may be relied upon to hydrocrack these low octane compounds formed during the reforming operation but it is preferred that the refonnate product comprising any C and higher boiling normal parafiin constituents be subjected to a selective zeolite hydrocracking operation designed to convert low boiling normal paraffins to LPG product.
  • the present invention includes the selective cracking of low and high boiling normal paraffin components comprising the naphtha boiling material processed in the combination of catalytic contact steps comprising this invention. It includes reforming a naphtha charge under reforming conditions providing normal and branched chain hydrocarbons component along with reactions of dehydrogenation and dehydrocyclization comprising catalytic reforming. This relationship between normal and branched chain hydrocarbon components provides normal paraffin constituents suitable for conversion to LPG material.
  • a platinum type reforming catalyst including bimetallic and non-bimetallic reforming catalysts and those comprising platinum or palladium in combination with another Group VIII metal component such as rhenium, iridium, ruthenium and osmium promoted with a halogen will indiscriminately effect hydrocracking under elevated temperature reforming conditions of the normal and branched paraffin components comprising the hydrocarbon material in the reforming operation.
  • a platinum type reforming catalyst under controlled isomerizing and hydrocracking severity conditions may be relied upon to produce LPG type products or products more easily converted to LPG products.
  • hydrocracking reactions performed with platinum reforming catalysts are more usually rate controlled reactions wherein, for example, a normal C, hydrocarbon will crack more easily than a C hydrocarbon or a lower carbon number paraffin and thus a high severity reforming operation would be required to crack, for example, a C paraffin.
  • a high severity non-selective hydrocracking operation with the platinum reforming catalyst is undesirable since cracking of branched C and C hydrocarbons will be accomplished before cracking of normal hexane. This will result in cracking desired high octane branched chain hydrocarbons.
  • Crystalline aluminosilicate conversion catalysts identified with the prior art which are not selective within the limits defined herein or those particularly known as methane producers rather than producers of propane and butane are of little interest in pursuing the concepts of this invention.
  • high methane producing cyrstalline aluminosilicate catalysts generally small pore crystalline zeolites promoted with Zn, Cd and Hg or other hydrocracking catalyst compositions which non selectively produce gaseous streams rich in methane are of little interest for practicing the concept of this invention unless they can be controlled by operating conditions to exclude the undesirable production of light gaseous hydrocarbon constituents particularly methane and ethane.
  • catalyst A platinum type of reforming catalyst used
  • catalyst B selective crystalline aluminosilicate hydrocracking catalyst relied upon particularly for the production of LPG gases
  • the platinum type reforming catalyst, catalyst A, selected for use in the sequence of process steps of this invention may be selected from any one of a number of known prior art reforming catalysts suitable for accomplishing the results desired.
  • These catalysts include generally. for example, alumina as the carrier material for one or more hydrogenation-dehydrogenation components distributed thereon with the alumina being in either the eta, chi, gamma or mixed forms thereof.
  • the alumina carrier is promoted with. for example, one or more Group Vlll metal components either with or without an acidic promoter such as silica, boron or a halogen.
  • the platinum type of reforming catalyst is intended to include platinum.
  • a bimetal catalyst composition suitable for the reforming operation of this invention may be platinum combined with either rhenium, ruthenium, osmium or 4 iridium and an alumina carrier promoted with chlorine to provide desired acid activity.
  • the operating conditions employed in the process combination of this invention and particularly those of the reforming operation with type A catalysts are those conditions which promote dehydrogenation of naphthenes along with reactions associated with paraffin isomerization which establish a relationship between normal paraffins to branched paraffins and include operating temperatures selected from the range of about 800F to about 1000F and preferably from 850F up to about 980F., liquid hourly space velocity in the range of about 0.1 to about 10, preferably about 0.5 to about 5; a pressure in the range of about atmospheric up to about 600 p.s.i.g. and preferably about to about 400 p.s.i.g. and a hydrogen to hydrocarbon ratio of about 0.5 to about 20 and preferably about I to 10.
  • the type B catalysts referred to herein are members of a special class of zeolites exhibiting some unusual properties. These zeolites induce profound transforma tions of aliphatic hydrocarbons to aromatic hydrocarbons in commercially desirable yields and are generally highly effective in alkylation. isomerization, disproportionation and other conversion reactions involving aromatic hydrocarbons. Although they have unusually low alumina contents, i.e., high silica to alumina ratios, they are very active even with silica to alumina ratios exceeding 30. This activity is surprising since catalytic activity of zeolites is generally attributed to framework aluminum atoms and cations associated with these aluminum atoms.
  • zeolites retain their crystallinity for long periods in spite of the presence of steam even at high temperatures which induce irreversible collapse of the crystal framework of other zeolites, e.g., of the X and A type. Furthermore, carbonaceous deposits. when formed, may be removed by burning at higher than usual temperatures to restore activity. In many environments the zeolites of this class exhibit very low coke forming capability, conducive to very long times on stream between burning regenerations.
  • the crystal structure of this class of zeolites provides constrained access to, and egress from, the intra-crystalline free space by virtue of having a pore dimension greater than about 5 Angstroms and pore windows of about a size such as would be provided by lO-membered rings of oxygen atoms.
  • lt is to be understood, of course, that these rings are those formed by the regular disposition of the tetrahedra making up the anionic framework of the crystalline aluminosilicate, the oxygen atoms themselves being bonded to the silicon or aluminum atoms at the centers of the tetrahedra.
  • the preferred zeolites useful in type B catalysts in this invention possess, in combination: a silica to alumina ratio of at least about 12; and a structure providing constrained access to the crystalline free space.
  • the silica to alumina ratio referred to may be determined by conventional analysis. This ratio is meant to represent, as closely as possible, the ratio in the rigid anionic framework of the zeolite crystal and to exclude aluminum in the binder or in cationic or other form within the channels.
  • zeolites with a silica to alumina ratio of at least 12 are useful, it is preferred to use zeolites having higher ratios of at least about 30. Such zeolites, after activation, acquire an intracrystalline sorption capacity for normal hexane which is greater than that for water, i.e., they exhibit hydrophobic" properties. It is believed that this hydrophobic character is advantageous in the present invention.
  • the zeolites useful as B catalysts in this invention freely sorb normal hexane and have a pore dimension greater than about 5 Angstroms.
  • their structure must provide constrained access to some larger molecules. It is sometimes possible tojudge from a known crystal structure whether such constrained access exists. For example, if the only pore windows in a crystal are formed by S-membered rings of oxygen atoms, then access by molecules of larger cross-section than normal hexane is substantially excluded and the zeolite is not of the desired type.
  • Zeolites with windows of l0membered rings are preferred, although excessive puckering or pore blockage may render these zeolites substantially ineffective.
  • Zeolites with windows of lZ-membered rings do not generally appear to offer sufficient constraint to produce the advantageous conversions desired in the instant invention, although structures can be conceived, due to pore blockage or other cause, that may be operative.
  • a simple determination of the constraint index may be made by continuously passing a mixture of equal weight of normal hexane and 3methylpentane over a small sample, approximately 1 gram or less, of zeolite at atmospheric pressure according to the following procedure.
  • a sample of the zeolite, in the form of pellets or extrudate, is crushed to a particle size about that of coarse sand and mounted in a glass tube.
  • the zeolite Prior to testing, the zeolite is treated with a stream of air at lO0OF for at least 15 minutes.
  • the zeolite is then flushed with helium and the temperature adjusted between 550F and 950F to give an overall conversion between l0% and 60%.
  • the mixture of hydrocarbons is passed at l liquid hourly space velocity (i.e., 1 volume of liquid hydrocarbon per volume of catalyst per hour) over the zeolite with a helium dilution to give a helium to total hydrocarbon mole ratio of 4:1.
  • l liquid hourly space velocity i.e., 1 volume of liquid hydrocarbon per volume of catalyst per hour
  • a helium dilution to give a helium to total hydrocarbon mole ratio of 4:1.
  • a sample of the effluent is taken and analyzed, most conveniently by gas chromatography, to determine the fraction remaining unchanged for each of the two hydrocarbons.
  • the constraint index is calculated as follows:
  • ZSM-ll is more particularly described in US. Pat. No. 3,709,979, the entire contents of which are incorporated herein by reference.
  • ZSM-l2 is more particularly described in US. Pat. No. 3,832,449, the entire contents of which are incorporated herein by reference.
  • the specific zeolites described, when prepared in the presence of organic cations, are substantially catalytically inactive, possibly because the intracrystalline free space is occupied by organic cations from the forming solution. They may be activated by heating in an inert atmosphere at lO0OF for 1 hour, for example. followed by base exchange with ammonium salts followed by calcination at lO0OF in air.
  • the presence of organic cations in the forming solution may not be absolutely essential to the formation of this special type zeolite; however, the presence of these cations does appear to favor the formation of this special type of zeolite. More generally, it is desirable to activate this type zeolite by base exchange with ammonium salts followed by calcination in air at about lO0OF for from about 15 minutes to about 24 hours.
  • Natural zeolites may sometimes be converted to this type zeolite by various activation procedures and other treatments such as base exchange, steaming, alumina extraction and calcination, alone or in combinations.
  • Natural minerals which may be so treated include ferrierite, brewsterite, stilbite, dachiardite, epistilbite, heu
  • the preferred crystalline aluminosilicates are ZSM-S, ZSM-l l, ZSM-l2 and ZSM-Zl, with ZSM-5 particularly preferred.
  • the zeolites used as catalysts in this invention may be in the hydrogen form or they may be base exchanged or impregnated to contain ammonium or a metal cation complement. It is desirable to calcine the Zeolite after base exchange.
  • the metal cations that may be present include any of the cations of the metals of Groups 1 through VIII of the periodic table. However, in the case of Group IA metals, the cation content should in no case be so large as to substantially eliminate the activity of the Zeolite for the catalysis being employed in the instant invention. For example, a completely sodium exchanged H-ZSM-S appears to be largely inactive for shape selective conversions required in the present invention.
  • the zeolites useful as catalysts herein are selected as those having a crystal framework density, in the dry hydrogen form, of not substantially below about 1.6 grams per cubic centimeter. It has been found that zeolites which satisfy all three of these criteria are most desired. Therefore, the preferred catalysts of this invention are those using zeolites having a constraint index as defined above of about 1 to 12, a silica to alumina ratio of at least about 12 and a dried crystal density of not substantially less than about 1.6 grams per cubic centimeter.
  • the dry density for known structures may be calculated from the number of silicon plus aluminum atoms per 1000 cubic Angstroms, as given, e.g., on page 19 of the article on Zeolite Structure by W. M. Meier.
  • crys tal framework density may be determined by classical pyknometer techniques. For example, it may be determined by immersing the dry hydrogen form of the zeolite in an organic solvent which is not sorbed by the crystal. It is possible that the unusual sustained activity and stability of this class of zeolites is associated with its high crystal anionic framework density of not less than about 1.6 grams per cubic centimeter. This high density of course must be associated with a relatively small amount of free space within the crystal, which might be expected to result in more stable structures. This free space, however, seems to be important as the locus of catalytic activity.
  • Crystal framework densities of some typical zeolites including some which are not within the preview of this invention are:
  • the heavier reformate fraction is overwhelmingly aromatic in composition, the aromatics comprising at least about volume percent, preferably at least about volume percent, thereof. At least a portion, and preferably all, of this heavier reformate is con tacted with a distinct mass of type B catalyst under conditions conducive to substantially eliminating any aliphatic components thereof. These conditions also induce aromatic isomerization, disproportionation, alkylation, dealkylation, transalkylation and side chain splitting so as to produce a product which is substan tially benzene and methyl substituted benzenes up to about C BTX preferably predominates in this product.
  • the light reformate comprises substantial proportions of aliphatic as well as aromatic components. It is contacted with a separate and distinct mass of type B catalyst under conditions conducive to cracking out the lower octane aliphatic components to produce LPG components and to simultaneously increase the propor tion of aromatics at least partially by alkylation of existing aromatics with fragments produced by such cracking.
  • the two separate and distinct type B catalyst conversions may be carried out under substantially similar or widely different reaction conditions depending upon the exact compositions of the light and heavier reformate fractions and upon the desired product distribution. It has been found, however, that if the reformate is split in the manner set forth hereinabove, each of the type B catalyst conversion performs its intended function admirably whereas if the reformate is split differently, these conversion are substantially less efficient at producing the desired product slate of high quality, aromatic enriched gasoline, high quality substantially aliphatic free aromatics concentrate, and large quanti ties of LPG.
  • the operating conditions selected for processing the light reformate fraction boiling below about 240F particularly include an operating pressure within the range of 200 to 1000 psig; a temperature within the range of about 500F to 800F; a volume hourly space velocity in the range of about 1 to 4 and a hydrogen to hydrocarbon ratio within the range of about 1 to 10 to 1. Hydrogen consumption is about or more SCF/B depending on the charge composition and operating conditions selected. Processing the heavy reformate fraction is preferably accomplished under more severe operating conditions including a temperature within the range of about 750 to 900F; a space velocity (vol. basis) in the range of about 0.5 to 2; a hydrogen to hydrocarbon ratio in the range of 1-20/1 and a pres sure within the range of about 200 to 1000 psig. Hydrogen consumption for the more severe operation is within the range of 2004400 SCF/B.
  • the drawing is diagrammatic sketch in elevation of the process combination comprising the separation of reformate product of catalytic reforming into a light and heavy reformate product fractions which are thereafter separately processed over type B catalyst under lower and higher severity conditions as aforesaid to particularly produce LPG, high octane gasoline and a benzene-toluene-xylene rich fraction.
  • a C9 full boiling range product of naphtha reforming is charged to the process by conduit 2.
  • the naphtha feed to a catalytic reforming operation may be one boiling in the range of C hydrocarbon up to about 380 or 400F. Reforming of naphtha boiling range hydrocarbons is well known in the prior art as discussed above and is a part of this invention to the extent that the material processed is a reformate product of catalytic reforming comprising a C; reformate.
  • the reformate charge introduced by conduit 2 to stabilizer 4 is separated in the stabilizer to recover toluene enriched C reformate material from the bottom thereof by conduit 8.
  • C and lower boiling components are recovered from the top of the stabilizer by conduit 10 and then passed to gas recovery equipment not shown to separate LPG materials from other gasiform materials.
  • a portion of the material withdrawn by conduit 8 from the bottom of the stabilizer is passed to gasoline pool equipment.
  • the remaining portion of the (3,;* material is passed by conduit 12 to a second separation zone 14, hereinafter sometimes referred to as a reformate splitter.
  • separation zone 14 conditions are maintained to separate the C reformate into an overhead fraction comprising some toluene and primarily lower boiling components withdrawn therefrom by conduit 16.
  • a Cf toluene-xylene rich fraction is withdrawn from the bottom portion of separation zone 14 by conduit 18. Separation of the CJ reformate in zone 14 is accomplished to provide a cut point between the fractions within the range of about 200 to about 240F.
  • the overhead fraction comprising primarily C and lower boiling components withdrawn by conduit 16 is passed with added hydrogen to a catalyst zone 20 containing a ZSM-S type of crystalline zeolite conversion catalyst.
  • zone 20 the fraction comprising toluene and lower boiling components is subjected to processing conditions comprising a pressure of about 400 psig at a start of run temperature of about 550F.
  • the reactant material is passed in contact with the catalyst at a volume hourly space velocity of about 2 and a hydrogen to hydrocarbon ratio of at least 1/ 1.
  • the light reformate comprising aromatic and C minus saturated hydrocarbons are processed to particularly produce LPG materials comprising propane and butane and some alkyl aromatics comprising toluene.
  • zone 20 The product effluent of zone 20 is then passed by conduit 22 to a high pressure separation zone 24.
  • high pressure separator 24 a separation is made which permits the recovery of C and lower boiling material comprising hydrogen from an upper portion of the zone by conduit 26. Some of this material may be withdrawn by conduit 28 and used as fuel.
  • the remaining portion of the material in conduit 26 is combined with makeup hydrogen added by conduit 30, compressed in compressor 32 to raise the pressure of this recycle stream about 50 pounds before recycle by conduit 34 to zone 20.
  • a product material comprising C and higher boiling components including benzene and toluene separated in zone 24 is withdrawn essentially as a liquid stream from the lower portion of separation zone 24 by conduit 36 and passed in its entirety to separation zone 4 10 wherein the C and lower boiling components are removed as overhead material and processed as above briefly discussed.
  • the heavy Cf reformate material, enriched with C? components from the separator 24, withdrawn from the lower portion of separation zone 14 is a toluene-xylene rich stream comprising Cf paraffins, having at most about 0.1 weight percent C parafl'ms, and boiling above about 225F which mixture is passed in a desired amount by conduit 38 to a second ZSM-5 zeolite catalytic conversion zone 40.
  • a portion of this toluene xylene enriched reformate in conduit 18 may be withdrawn as a product stream for use as desired.
  • zone 40 the herein identified Cf reformate is processed in the presence of added hydrogen which may come from conduit 28 over a ZSM-S type zeolite under relatively more severe processing conditions designed to particularly crack paraffin components and convert the aromatic containing reformate to a light aromatics mixture comprising (BTX) benzene, toluene and xylene by a combination of dealkylation and disproportionation reactions.
  • this catalytic conversion operation it is proposed to employ an operating pressure of about 401) psig and a start of run temperature of about 750F.
  • a hydrogen to hydrocarbon ratio of about 4/1 is used with a reactant volume space velocity of about 1.
  • zone 40 It is particularly important that the processing conditions of zone 40 be selected to particularly crack the paraffins to lower boiling components comprising LPG products and disproportionate charged aromatics to form a mixture of benzene, toluene, and aromatics since these materials are of a boiling range easily separated by simple distillation.
  • the product effluent of the aromatic forming zone 40 is passed by conduit 42 to a high pressure separation zone 44.
  • separation zone 44 a hydrogen rich gaseous stream is separated and recycled by conduit 46 to conduit 38 communicating with zone 40. Hydrogen rich make up gas is added to the recycled gas by conduit 48.
  • the remaining product separated in zone 44 comprising light aromatics and lower boiling components of cracking are passed by conduit 50 to a separation zone 52 maintained at a pressure of about psig and a temperature of about 450F.
  • separation zone 52 a separation is made between light aromatics comprising benzene and higher boiling aromatics and reaction components boiling below about benzene.
  • a light aromatic rich fraction is withdrawn by conduit 54 from zone 52 for further processing by distillation and other means not shown into desired components.
  • An important aspect of this invention resides in flashing the product of shape selective conversion of light reformate, preferably in a high pressure separator. to split it into a gas and a higher octane gasoline liquid. The liquid is recycled to the stabilizer along with the full range reformate. Thus the heavier reformate from the splitter is enriched with C components (predominantly Cf alkyl benzenes) from this higher octane gasoline liquid product.
  • a method for redistributing the paraffin-aromatic components of a reformate product of catalytic reforming comprising C and higher boiling hydrocarbons which comprises,
  • temperatures relied upon in the first zeolite catalyst conversion zone are within the range of 500F. to 800F.
  • the zeolite cata lyst is preferably a ZSM-S type crystalline zeolite.
  • a process of upgrading petroleum reformate to an aromatics concentrate comprising benzene, toluene and xylene (BTX), liquifiable petroleum gas (LPG) comprising C and C components, and high octane gasoline comprising:
  • a process as claimed in claim 11 including admixing a portion of said aromatics concentrate with said reformate prior to said splittingv 13.
  • a process as claimed in claim 11 including deleting a C fraction from said reformate and splitting the remaining CJ fraction.
  • a process as claimed in claim 11 including separating C and C components from said C gas.
  • a process as claimed in claim 11 including splitting a portion of the CJ portion of said reformate.
  • a process as claimed in claim 11 including admixing said aromatics enriched liquid, a portion of said aromatics concentrate and said reformate; and splitting said admixture into said Cf and C fractions.
  • a process as claimed in claim 11 including utilizing the same zeolite respectively in both of said conversions,

Landscapes

  • 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)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US538221A 1975-01-02 1975-01-02 Combination process for producing LPG and aromatic rich material from naphtha Expired - Lifetime US3928174A (en)

Priority Applications (2)

Application Number Priority Date Filing Date Title
US538221A US3928174A (en) 1975-01-02 1975-01-02 Combination process for producing LPG and aromatic rich material from naphtha
FR7540153A FR2296606A1 (fr) 1975-01-02 1975-12-30 Procede pour produire du gaz liquefiable et un produit riche en hydrocarbures a partir de naphtes

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US538221A US3928174A (en) 1975-01-02 1975-01-02 Combination process for producing LPG and aromatic rich material from naphtha

Publications (1)

Publication Number Publication Date
US3928174A true US3928174A (en) 1975-12-23

Family

ID=24146002

Family Applications (1)

Application Number Title Priority Date Filing Date
US538221A Expired - Lifetime US3928174A (en) 1975-01-02 1975-01-02 Combination process for producing LPG and aromatic rich material from naphtha

Country Status (2)

Country Link
US (1) US3928174A (enExample)
FR (1) FR2296606A1 (enExample)

Cited By (36)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2296606A1 (fr) * 1975-01-02 1976-07-30 Mobil Oil Procede pour produire du gaz liquefiable et un produit riche en hydrocarbures a partir de naphtes
US4002555A (en) * 1976-01-07 1977-01-11 Chevron Research Company Hydrocarbon reforming process
US4066531A (en) * 1975-09-26 1978-01-03 Mobil Oil Corporation Processing heavy reformate feedstock
US4111792A (en) * 1976-10-14 1978-09-05 Mobil Oil Corporation Combination process for upgrading synthol naphtha fractions
US4190519A (en) * 1978-10-23 1980-02-26 Chevron Research Company Combination process for upgrading naphtha
US4244807A (en) * 1978-05-25 1981-01-13 Shell Oil Company Process for the preparation of a hydrocarbon mixture rich in aromatics
US4388177A (en) * 1981-01-13 1983-06-14 Mobil Oil Corporation Preparation of natural ferrierite hydrocracking catalyst and hydrocarbon conversion with catalyst
US4443326A (en) * 1981-10-16 1984-04-17 Chevron Research Company Two-step reforming process
US4590322A (en) * 1985-06-12 1986-05-20 Mobil Oil Corporation Use of hydrogen sulfide to improve benzene production over zeolites
US4590323A (en) * 1985-06-12 1986-05-20 Mobil Oil Corporation Conversion of paraffins to aromatics over zeolites modified with oxides of group IIIA, IVA and VA elements
US4594145A (en) * 1984-12-07 1986-06-10 Exxon Research & Engineering Co. Reforming process for enhanced benzene yield
US4675461A (en) * 1983-06-29 1987-06-23 Mobil Oil Corporation Conversion of LPG hydrocarbons into distillate fuels using an integral LPG dehydrogenation-MOGD process
US4855431A (en) * 1983-01-13 1989-08-08 Mobil Oil Corp. Process for making alkyl pyrazines
US4906353A (en) * 1987-11-27 1990-03-06 Mobil Oil Corp. Dual mode hydrocarbon conversion process
US4936976A (en) * 1989-03-02 1990-06-26 Mobil Oil Corp. Integrated reforming/aromatization process
USRE33323E (en) * 1984-12-07 1990-09-04 Exxon Research & Engineering Company Reforming process for enhanced benzene yield
US4975179A (en) * 1989-08-24 1990-12-04 Mobil Oil Corporation Production of aromatics-rich gasoline with low benzene content
US5053573A (en) * 1990-09-14 1991-10-01 Mobil Oil Corporation Reduction of benzene content of reformate by reaction with cycle oils
US5082983A (en) * 1990-09-14 1992-01-21 Mobil Oil Corporation Reduction of benzene content of reformate in a catalytic cracking unit
WO1995005351A1 (en) * 1993-08-16 1995-02-23 Mobil Oil Corporation Heavy naphtha upgrading
WO1996010066A1 (en) * 1994-09-28 1996-04-04 Mobil Oil Corporation Hydrocarbon conversion
USH1723H (en) * 1992-09-11 1998-04-07 Leuenberger; Ernest L. Process for producing gasoline blending components from jet range and heavier aromatics
US5958218A (en) * 1996-01-22 1999-09-28 The M. W. Kellogg Company Two-stage hydroprocessing reaction scheme with series recycle gas flow
US6004452A (en) * 1997-11-14 1999-12-21 Chevron Chemical Company Llc Process for converting hydrocarbon feed to high purity benzene and high purity paraxylene
US6602404B2 (en) * 1997-10-30 2003-08-05 Exxon Mobil Chemical Patents Inc. Process for naphtha reforming
US6740228B1 (en) 1989-10-30 2004-05-25 Exxonmobil Chemical Patents Inc. Process for reforming petroleum hydrocarbon stocks
US6803493B1 (en) * 2003-08-15 2004-10-12 Fina Technology, Inc. Toluene disproportion process
US20060287561A1 (en) * 2005-06-21 2006-12-21 Sk Corporation Process for increasing production of light olefin hydrocarbon from hydrocarbon feedstock
US20060287564A1 (en) * 2005-06-21 2006-12-21 Sk Corporation Process for increasing production of benzene from hydrocarbon mixture
US20080051615A1 (en) * 2006-08-24 2008-02-28 Stavens Elizabeth L Process for the production of benzene, toluene, and xylenes
US20100029467A1 (en) * 2008-07-30 2010-02-04 Tomoyuki Inui Multiple zeolite catalyst
US8653315B2 (en) 2008-07-30 2014-02-18 King Fahd University Of Petroleum And Minerals Multiple zeolite catalyst and method of using the same for toluene disproportionation
WO2016102250A1 (en) 2014-12-22 2016-06-30 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
WO2017101985A1 (en) 2015-12-15 2017-06-22 Sabic Global Technologies B.V. Process for producing c2 and c3 hydrocarbons
US10876054B2 (en) 2015-12-30 2020-12-29 Uop Llc Olefin and BTX production using aliphatic cracking reactor

Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3702886A (en) * 1969-10-10 1972-11-14 Mobil Oil Corp Crystalline zeolite zsm-5 and method of preparing the same
US3709979A (en) * 1970-04-23 1973-01-09 Mobil Oil Corp Crystalline zeolite zsm-11
US3729409A (en) * 1970-12-24 1973-04-24 Mobil Oil Corp Hydrocarbon conversion
US3756942A (en) * 1972-05-17 1973-09-04 Mobil Oil Corp Process for the production of aromatic compounds
US3760024A (en) * 1971-06-16 1973-09-18 Mobil Oil Corp Preparation of aromatics
US3766093A (en) * 1972-01-07 1973-10-16 Mobil Oil Corp Treatment of organic cationcontaining zeolites
US3767565A (en) * 1971-12-10 1973-10-23 Phillips Petroleum Co Preparation of high octane gasoline using disproportionation, alkylation and dimerization steps
US3806443A (en) * 1972-05-26 1974-04-23 Mobil Oil Corp Selective hydrocracking before and after reforming
US3832449A (en) * 1971-03-18 1974-08-27 Mobil Oil Corp Crystalline zeolite zsm{14 12
US3849290A (en) * 1972-08-02 1974-11-19 Mobil Oil Corp Upgrading of reformates by catalyst compositions selective for cracking low and high boiling paraffin components
US3856873A (en) * 1973-09-13 1974-12-24 Mobil Oil Corp Xylene isomerization

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3928174A (en) * 1975-01-02 1975-12-23 Mobil Oil Corp Combination process for producing LPG and aromatic rich material from naphtha

Patent Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3702886A (en) * 1969-10-10 1972-11-14 Mobil Oil Corp Crystalline zeolite zsm-5 and method of preparing the same
US3709979A (en) * 1970-04-23 1973-01-09 Mobil Oil Corp Crystalline zeolite zsm-11
US3729409A (en) * 1970-12-24 1973-04-24 Mobil Oil Corp Hydrocarbon conversion
US3832449A (en) * 1971-03-18 1974-08-27 Mobil Oil Corp Crystalline zeolite zsm{14 12
US3760024A (en) * 1971-06-16 1973-09-18 Mobil Oil Corp Preparation of aromatics
US3767565A (en) * 1971-12-10 1973-10-23 Phillips Petroleum Co Preparation of high octane gasoline using disproportionation, alkylation and dimerization steps
US3766093A (en) * 1972-01-07 1973-10-16 Mobil Oil Corp Treatment of organic cationcontaining zeolites
US3756942A (en) * 1972-05-17 1973-09-04 Mobil Oil Corp Process for the production of aromatic compounds
US3806443A (en) * 1972-05-26 1974-04-23 Mobil Oil Corp Selective hydrocracking before and after reforming
US3849290A (en) * 1972-08-02 1974-11-19 Mobil Oil Corp Upgrading of reformates by catalyst compositions selective for cracking low and high boiling paraffin components
US3856873A (en) * 1973-09-13 1974-12-24 Mobil Oil Corp Xylene isomerization

Cited By (51)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2296606A1 (fr) * 1975-01-02 1976-07-30 Mobil Oil Procede pour produire du gaz liquefiable et un produit riche en hydrocarbures a partir de naphtes
US4066531A (en) * 1975-09-26 1978-01-03 Mobil Oil Corporation Processing heavy reformate feedstock
US4002555A (en) * 1976-01-07 1977-01-11 Chevron Research Company Hydrocarbon reforming process
US4111792A (en) * 1976-10-14 1978-09-05 Mobil Oil Corporation Combination process for upgrading synthol naphtha fractions
US4244807A (en) * 1978-05-25 1981-01-13 Shell Oil Company Process for the preparation of a hydrocarbon mixture rich in aromatics
US4190519A (en) * 1978-10-23 1980-02-26 Chevron Research Company Combination process for upgrading naphtha
US4388177A (en) * 1981-01-13 1983-06-14 Mobil Oil Corporation Preparation of natural ferrierite hydrocracking catalyst and hydrocarbon conversion with catalyst
US4443326A (en) * 1981-10-16 1984-04-17 Chevron Research Company Two-step reforming process
US4855431A (en) * 1983-01-13 1989-08-08 Mobil Oil Corp. Process for making alkyl pyrazines
US4675461A (en) * 1983-06-29 1987-06-23 Mobil Oil Corporation Conversion of LPG hydrocarbons into distillate fuels using an integral LPG dehydrogenation-MOGD process
US4594145A (en) * 1984-12-07 1986-06-10 Exxon Research & Engineering Co. Reforming process for enhanced benzene yield
USRE33323E (en) * 1984-12-07 1990-09-04 Exxon Research & Engineering Company Reforming process for enhanced benzene yield
US4590322A (en) * 1985-06-12 1986-05-20 Mobil Oil Corporation Use of hydrogen sulfide to improve benzene production over zeolites
US4590323A (en) * 1985-06-12 1986-05-20 Mobil Oil Corporation Conversion of paraffins to aromatics over zeolites modified with oxides of group IIIA, IVA and VA elements
US4906353A (en) * 1987-11-27 1990-03-06 Mobil Oil Corp. Dual mode hydrocarbon conversion process
US4936976A (en) * 1989-03-02 1990-06-26 Mobil Oil Corp. Integrated reforming/aromatization process
US4975179A (en) * 1989-08-24 1990-12-04 Mobil Oil Corporation Production of aromatics-rich gasoline with low benzene content
US6740228B1 (en) 1989-10-30 2004-05-25 Exxonmobil Chemical Patents Inc. Process for reforming petroleum hydrocarbon stocks
US5053573A (en) * 1990-09-14 1991-10-01 Mobil Oil Corporation Reduction of benzene content of reformate by reaction with cycle oils
US5082983A (en) * 1990-09-14 1992-01-21 Mobil Oil Corporation Reduction of benzene content of reformate in a catalytic cracking unit
USH1723H (en) * 1992-09-11 1998-04-07 Leuenberger; Ernest L. Process for producing gasoline blending components from jet range and heavier aromatics
WO1995005351A1 (en) * 1993-08-16 1995-02-23 Mobil Oil Corporation Heavy naphtha upgrading
US5396010A (en) * 1993-08-16 1995-03-07 Mobil Oil Corporation Heavy naphtha upgrading
WO1996010066A1 (en) * 1994-09-28 1996-04-04 Mobil Oil Corporation Hydrocarbon conversion
US5958218A (en) * 1996-01-22 1999-09-28 The M. W. Kellogg Company Two-stage hydroprocessing reaction scheme with series recycle gas flow
US6602404B2 (en) * 1997-10-30 2003-08-05 Exxon Mobil Chemical Patents Inc. Process for naphtha reforming
US6004452A (en) * 1997-11-14 1999-12-21 Chevron Chemical Company Llc Process for converting hydrocarbon feed to high purity benzene and high purity paraxylene
US6803493B1 (en) * 2003-08-15 2004-10-12 Fina Technology, Inc. Toluene disproportion process
US20060287561A1 (en) * 2005-06-21 2006-12-21 Sk Corporation Process for increasing production of light olefin hydrocarbon from hydrocarbon feedstock
US20060287564A1 (en) * 2005-06-21 2006-12-21 Sk Corporation Process for increasing production of benzene from hydrocarbon mixture
US7301063B2 (en) * 2005-06-21 2007-11-27 Sk Corporation Process for increasing production of light olefin hydrocarbon from hydrocarbon feedstock
US7304195B2 (en) * 2005-06-21 2007-12-04 Sk Corporation Process for increasing production of benzene from hydrocarbon mixture
US20080051615A1 (en) * 2006-08-24 2008-02-28 Stavens Elizabeth L Process for the production of benzene, toluene, and xylenes
US7563358B2 (en) * 2006-08-24 2009-07-21 Exxonmobil Chemical Patents Inc. Process for the production of benzene, toluene, and xylenes
US20100029467A1 (en) * 2008-07-30 2010-02-04 Tomoyuki Inui Multiple zeolite catalyst
US8329973B2 (en) 2008-07-30 2012-12-11 King Fahd University Of Petroleum And Minerals Multiple zeolite catalyst
US8653315B2 (en) 2008-07-30 2014-02-18 King Fahd University Of Petroleum And Minerals Multiple zeolite catalyst and method of using the same for toluene disproportionation
WO2016102249A1 (en) 2014-12-22 2016-06-30 Sabic Global Technologies B.V. Process for producing lpg and btx
US10287518B2 (en) 2014-12-22 2019-05-14 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
CN107109253A (zh) * 2014-12-22 2017-08-29 沙特基础工业全球技术有限公司 用于生产lpg和btx的方法
WO2016102250A1 (en) 2014-12-22 2016-06-30 Sabic Global Technologies B.V. Process for producing lpg and btx
US10526551B2 (en) 2014-12-22 2020-01-07 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
CN107109253B (zh) * 2014-12-22 2019-06-28 沙特基础工业全球技术有限公司 用于生产lpg和btx的方法
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
JP2018538303A (ja) * 2015-12-15 2018-12-27 サビック グローバル テクノロジーズ ベスローテン フェンノートシャップ Ｃ２およびｃ３炭化水素を生成するためのプロセス
KR20180093907A (ko) * 2015-12-15 2018-08-22 사빅 글로벌 테크놀러지스 비.브이. C2 및 c3 탄화수소 제조 방법
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
WO2017101985A1 (en) 2015-12-15 2017-06-22 Sabic Global Technologies B.V. Process for producing c2 and c3 hydrocarbons
US10876054B2 (en) 2015-12-30 2020-12-29 Uop Llc Olefin and BTX production using aliphatic cracking reactor

Also Published As

Publication number Publication date
FR2296606B1 (enExample) 1979-06-15
FR2296606A1 (fr) 1976-07-30

Similar Documents

Publication Publication Date Title
US3928174A (en) Combination process for producing LPG and aromatic rich material from naphtha
US3957621A (en) Production of alkyl aromatic hydrocarbons
US4181599A (en) Naphtha processing including reforming, isomerization and cracking over a ZSM-5-type catalyst
US3948758A (en) Production of alkyl aromatic hydrocarbons
US3890218A (en) Upgrading aliphatic naphthas to higher octane gasoline
EP0234684B1 (en) Xylene isomerization process
US4188282A (en) Manufacture of benzene, toluene and xylene
US4347394A (en) Benzene synthesis
US4594145A (en) Reforming process for enhanced benzene yield
KR100351326B1 (ko) 파라-크실렌 선택성 개질/방향족화
US3770614A (en) Split feed reforming and n-paraffin elimination from low boiling reformate
US4897177A (en) Process for reforming a hydrocarbon fraction with a limited C9 + content
EP0288622B1 (en) Process for the isomerization of paraffinic hydrocarbons
US5401386A (en) Reforming process for producing high-purity benzene
US3945913A (en) Manufacture of lower aromatic compounds
US4078990A (en) Manufacture of lower aromatic compounds
US4190519A (en) Combination process for upgrading naphtha
US4341622A (en) Manufacture of benzene, toluene and xylene
US4211886A (en) Manufacture of benzene, toluene and xylene
US3871993A (en) Upgrading the octane value of naphtha employing a crystalline aluminosilicate zeolite which has a high silica to alumina ratio wherein alumina is incorporated in the interstices of the zeolite crystal
US4935566A (en) Dehydrocyclization and reforming process
US5013423A (en) Reforming and dehydrocyclization
US7247762B2 (en) Process for xylene isomerization and ethylbenzene conversion
US3806443A (en) Selective hydrocracking before and after reforming
US11318452B2 (en) Single step process for the simultaneous production of aromatics, naphthenics and isoparaffins using transition metal functionalized zeolite based catalyst