US3649520A - Production of lead free gasoline - Google Patents

Production of lead free gasoline Download PDF

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US3649520A
US3649520A US19174A US3649520DA US3649520A US 3649520 A US3649520 A US 3649520A US 19174 A US19174 A US 19174A US 3649520D A US3649520D A US 3649520DA US 3649520 A US3649520 A US 3649520A
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gasoline
hydrocarbons
line
product
reforming
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Richard G Graven
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Mobil Oil AS
ExxonMobil Oil Corp
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
    • C10L1/06—Liquid carbonaceous fuels essentially based on blends of hydrocarbons for spark ignition
    • 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

Definitions

  • the present invention is concerned with the production of gasoline.
  • the present invention is concerned with a novel method and arrangement of known processing steps for producing lead-free gasoline.
  • the need for providing a lead free gasoline product has been prompted in recent years by air pollution problems confronting sections of the world employing combustion engines in relatively high density. Therefore the greatest application of lead-free gasoline will be in those areas of high automobile density where the presence of lead additive' combustion products are considered harmful and a major contributor to atmospheric pollution.
  • both relatively low and high octane gasoline products free of lead additives or other additives contributing to air pollution will be required in the near and/or immediate future to meet certain government restrictions and demands, on the one hand, while fulfilling the demands of the public and automobile manufacturers on the other hand.
  • the present invention is concerned with identifying a processing scheme compatible with present processing technology and/ or refinery installations, one might employ to upgrade relatively low octane gasoline material to an acceptable higher octane product suitable for use in a combustion engine known today and for the immediate future.
  • Some patents of interest in producing unleaded gasoline are US. Pats. 2,905,619, 3,165,461 and 2,900,323.
  • FIG. 1 identifies an arrangement of processing steps effective for upgrading naphtha or gasoline boiling range materials ina sequence of processing steps which includes 3,649,520 Patented Mar. 14, 1972 ice reforming C hydrocarbons, aromatics recovery, isomerization and fractionation steps which are particularly effective for isolating and upgrading C hydrocarbon components of low octane rating to higher octane constituents.
  • FIG. 2 identifies diagrammatically a block flow refinery process arrangement for upgrading crude oil to premium and regular gasoline product by a combination of refinery operations which includes the specific arrangement of FIG. 1.
  • a gasoline boiling range hydrocarbon fraction boiling in the range of from about C hydrocarbons up to about 380 F. and ob tained as straight run naphtha, coker naphtha or gasoline and in some cases catalytic-ally cracked or hydrocracked gasoline is introduced to the process by way of line 2 for passage to catalytic pretreatment such as desulfurization or denitrogenation in zone 4.
  • catalytic pretreatment such as desulfurization or denitrogenation in zone 4.
  • the gasoline charge is subjected to hydrogenation for the purpose of removing sulfur, nitrogen and any other undesired constituents or contaminants found in the gasoline charge.
  • the pretreated gasoline is thereafter passed by line 6 to a separator vessel 8 referred to herein as a dehexanizer tower 8 maintained under temperature and pressure conditions designed to separate and permit recovery from the upper portion thereof hydrocarbon boiling 180 F. and lower boiling by line 1-0.
  • a separator vessel 8 referred to herein as a dehexanizer tower 8 maintained under temperature and pressure conditions designed to separate and permit recovery from the upper portion thereof hydrocarbon boiling 180 F. and lower boiling by line 1-0.
  • Higher boiling gasoline hydrocarbons and boiling from about 180 F. up to about 380 F. and identified as stream B, in Table 1 are withdrawn from the bottom of dehexanizer 8 by line 12. It is, of course, recognized that a relatively rough separation may be made in dehaxanizer 8 and thus an amount of C hydrocarbons may be carried overhead and/or a portion of C hydrocarbons may withdraw from the bottom along with the intended higher boiling hydrocarbons.
  • the hydrocarbons in stream B and withdrawn by line 12 are thereafter passed to a reforming operation 14 wherein they are subjected to contact with a platinum catalyst in a catalytic reforming operation maintained under conditions selected to upgrade the gasoline and naphtha charge boiling above 180 F. to a higher octane product.
  • a reforming step the operating conditions of temperature, pressure and space velocity will be selected to produce reformate product thereof having a clear octane rating in the range of from about up to about 106 and preferably at least about 97 octane rating clear.
  • the reforming severity conditions may be selected to provide a product having an octane rating of at least 103 and preferably 104 octane rating clear.
  • the reforming operation pursued will normally be a relatively sophisticated reforming operation to take advantage of presently known technology.
  • the use of naphthene rich gasoline charge materials may be successfully employed; however with a parafiin rich feed, the hexane upgrading concept of this invention will be even more advantageous. It is to be understood that reforming step 14 may be a regenerative or semi-regenreative operation.
  • the efiluent of reforming step 14 is normally separated to recover a hydrogen rich gas from the remaining efiluent in equipment not shown-and which can be used in other parts of the process such as in a hydrogenation step or an isomerization step hereinafter discussed.
  • This recovery apparatus for hydrogen rich gas and circulation in the system is not specifically shown in the drawing since use of such hydrogen rich gas streams is generally known in the prior art.
  • the reformate product from which hydrogen rich gas has been recovered is thereafter passed by line 16 to separator tower 18 known as a depentanizer. In depentanizer tower 18 the operating conditions are selected and maintained to effect separation and recovery of C and any remaining lower boiling hydrocarbons from a reformate product effluent stream boiling above about C hydrocarbons.
  • the composition of the reformate product in line 22 is identified in Table 3 and comprises about 65% aromatics.
  • the C and lower boiling hydrocarbons are removed from the top of tower 18 by line 20 for further processing as desired and generally known in the prior art.
  • the reformate product boiling above C hydrocarbons are withdrawn from the bottom of depentanizer 18 by line 22. Since an important aspect of the processing sequence is to concentrate low octane C hydrocarbons, some C hydrocarbons may be withdrawn from the bottom of tower 18 by line 22.
  • the higher boiling reformate fraction obtained from depentanizer 18, such as identified in Table 3, is passed by line 22 to a dehexanizer tower 24 wherein the conditions of operation are selected to provide a cut point in the range of 158 F. up to about 225 F.
  • This recovered hydrocarbon fraction in line 28 comprises primarily the isolated C hydrocarbons of relatively low octane and C hydrocarbons of varying amount depending upon the cut point selected needs to be converted to higher octane product in order to be used in an unleaded gasoline product.
  • a cut point of about 225 F. in tower 24 more C7 hydrocarbons will be carried overhead thereby considerably upgrading the product in line 26 as evidenced by the data of Table 4.
  • the C hydrocarbon thus thrown ovehead may be recovered from the process by tower 56 discussed below.
  • the C hydrocarbons thus separated and recovered may be further processed such as by reforming, shape selective cracking or converted to olefin product as by fluid catalytic cracking or thermal cracking.
  • the light hydrocarbon fraction recovered as overhead from dehexanizer 8 by line and which may contain a small amount of C hydrocarbons may be combined with the C and lighter hydrocarbons recovered from depentanizer 18 or separately processed.
  • the C and lighter hydrocarbons in line 10 are thereafter debutanized and depentanized in the sequence of separation steps hereinafter briefly discussed.
  • the C hydrocarbons and lighter fraction thus recovered are initially passed to debutanizer 30 wherein C and lighter hydrocarbons are separated from higher boiling hydrocarbons to permit recovery thereof from the upper portion of the tower by line 32 with the remaining higher boiling portion being withdrawn from the bottom of debutanizer 30 and passed by line 34 to a depentanizer tower 36.
  • C hydrocarbons are separated and removed from the upper portion thereof by line 38 with the remaining C and higher boiling hydrocarbons being withdrawn from the bottom of depentaizer tower 36 by line 40.
  • the sequence above described provides a hydrocarbon stream rich in C hydrocarbons for upgrading to higher octane product.
  • the C rich hydrocarbon stream in line 40 and having the composition of stream A, Table 1, thereafter is passed to reforming step 42.
  • the reforming operation contemplated in step 42 is primarily one of dehydrogenation for the purpose of converting C naphthenes to aromatics.
  • the octane rating of the product therefrom will depend considerably upon the type of C hydrocarbons in the charge thereto.
  • reforming step 42 is operated under conditions which are particularly selective for effecting dehydrogenation of naphthenes to form aromatics and isomerization of isomerizable hydrocarbons.
  • the reformate product efiiuent of reforming step 42 is separated in a separation zone not shown to recover a hydrogen rich gas stream from a higher boiling reformate product stream.
  • the hydrogen rich gas stream is recycled to the process such as to the pretreating step, reforming step or isomerization step herein discussed.
  • the reformate product freed of hydroggen rich gas is recovered from reforming step 42 and passed by line 44 to a depentanizer tower 46 wherein C and lower boiling hydrocarbons are separated from higher boiling reformate product or aromatic enriched stream with the C hydrocarbons recovered from the upper portion of the tower by line 48. These C and lower boiling hydrocarbons may thereafter be stabilized in suitable equipment not shown and processed as by isomerization.
  • the aromatic enriched stream separated in depentanizer tower 46 is removed from the bottom thereof by line 50 and passed to an aromatics removal zone such as an extraction step 52.
  • the aromatic rich stream in line 50 and identified in Table 2 is combined with the isolated C hydrocarbon stream in line 28.
  • the combined C hydrocarbon stream is passed to the aromatic removal step 52.
  • Step 52 is primarily for the removal of aromatics such as benzene, toluene and perhaps xylene from the combined C hydrocarbon stream.
  • the aromatic separated in zone 52 as by extraction, molecular sieve adsorption or any other convenient method is withdrawn by line 54.
  • the aromatic removal step may be substantially any aromatic removal step suitable for effecting an economic recovery of aromatics from the remaining C hydrocarbon components introduced thereto.
  • the aromatic free hydrocarbons recovered from step 52 which may comprise some 0, hydrocarbons and a small amount of unremoved aromatics is thereafter fractionated when required to separate 0, hydrocarbons from the lower boiling C hydrocarbons.
  • the C hydrocarbons are then passed by line 56 to hydrogenation step 58.
  • Any separated C hydrocarbon may be recycled to the reforming steps herein discussed or processed in any desired manner.
  • hydrogenation step 58 aromatics remaining in the C hydrocarbons are hydrogenated and converted to naphthenes since it has been found that even a small amount of aromatics in the charge to the isomerization step is not particularly desirable. It is of course understood that hydrogen suitable for this hydrogenation step may be recovered from the hydrogen rich reformate product of reforming steps 14 and/or 42.
  • the hydro genated C fraction freed of aromatics and C hydro carbons is thereafter passed by line 60 to isomerization step 6 2.
  • the isomerization of hexane hydrocarbons to higher octane product is one requiring relatively strict operating conditions to avoid undesired cracking and low tempera tures in the range of 200 to 500 F. are known to favor the isomerization to the higher octane C hydrocarbon components.
  • the production of 2,2-dimethylbutane having an octane rating clear of about 91.8 and which blends as if it had an octane rating of about is enhanced by low temperature isomerization. It is desirable to recover any formed 2,3-dimethylbutane having a clear octane rating of about 103.5.
  • C hyrdrocarbons not isomerized in step 62 are withdrawn from a lower portion of the tower by line 70 essentially as a recycle stream for recycle to step 62 or step 42.
  • the C hydrocarbons may be recycled to the isomerization step all or in part, it being important, however, to limit the build up of naphthenes in this C recycle stream because of their undesirable influence on the isomerization step.
  • a naphthene bleed stream 74 is used to pass a portion of this recycle stream to reformer 42 or 14 or separator tower 56.
  • the processing scheme thus described eliminates low octane C hydrocarbon which may be converted to other products such as by shape selective cracking, fluid cracking and in some cases these hydrocarbons may be cyclized in a very selective low pressure reforming operation.
  • the reforming steps employed in the processing sequence of this invention preferably employ catalyst components comprising platinum and/or platinum-type com pound dispersed on alumina.
  • Bimetallic reforming catalysts may also be employed to considerable advantage and the amount of platinum required in the catalyst will be less than that required when platinum is used alone.
  • the catalyst may be halogen promoted and every suitable operating variable such as moisture control and cracking inhibitors known in the prior art may be called upon to enhance the reforming operation in the direction of optimizing the production of desired octane product.
  • the reforming operation may be effected at temperatures selected from within the range of from about 800 F. up to about 1050 F. under conditions of pressure in the range of from about 100 p.s.i.g.
  • the pressure will be selected from within the range of from about 200 p.s.i.g. up to about 500 p.s.i.g.
  • the space velocity on a liquid hourly basis may be in the range of from about 0.5 up to about 10in the presence of hydrogen at mol ratios known in 'the art.
  • the reforming operation may be semi-regenerative or a regenerative operation wherein regeneration of the catalyst occurs quite frequently and requires the use of an extra reactor in the reforming sequence known as a swing reactor.
  • Isomerization step 62 may be substantially any of the known isomerization processes of the priorart which will be effective for upgrading C hydrocarbon constituents.
  • the isomerization catalysts employed may be either solid isomerization catalysts or ones which require a liquid phase operation.
  • the extraction step for recovery of aromatics may also be substantially any known-method for effecting such separation in an economic manner.
  • extraction may be by adsorption and in particular a selective adsorption with a crystalline zeolite of proper pore dimensions.
  • the aromatic freed product may in one type of operation be recovered from the zeolite such as by stripping and thereafter passed to the isomerization step.
  • An effective material for the stripping operation could be hydrogen rich gas recovered from the reforming step of the process since the presence of such hydrogen gas is desirable in the isomerization step.
  • pretreater 4 may pass through a separate stabilizer tower not shown for removal of C and lower boiling constituents before passage of the remaining pretreated charge to dehexanizer tower such as tower 8.
  • the crude tower of the refining process may be relied upon to separate a hydrocarbon fraction boiling from about F. up to about 380 F. from a lower boiling C to 160 F. hydrocarbon fraction.
  • the thus obtained fraction boiling above 160 F. may be passed to desulfurization before being reformed in a platinum reforming operation.
  • a fraction boiling below about 160 F. may be recoverd from the crude tower and after stabilization thereof to recover C and C hydrocarbons therefrom, this hexane rich fraction may be separately desulfurized before effecting reforming thereof.
  • the important consideration within the concept of the present invention is to effect a separation of low octane C hydrocarbons from higher boiling gasoline constitutents so that each can be efliciently processed to a higher octane component thereby effecting a significant increse in overall product yield of desired higher octane product.
  • FIG. 2 identifies a block flow refinery arrangement for upgrading crude oil to premium and regular grade gasoline product.
  • the specific processing arrangement of FIG. I discussed hereinbefore may be employed in the overall refining operation of FIG. 2.
  • a crude oil is introduced to the process by line 1 for passage to an atmospheric crude tower and vacuum tower arrangement diagrammatically represented by block 2.
  • the operation of an atmospheric crude tower as well as a vacuum tower is well known in petroleum processing and suitable combinations thereof which will provide the refinery feeds hereinafter discussed will be suitable for use in the processing scheme of the invention herein described.
  • a catalytic cracking feed stock is Withdrawn by line 5 from the crude tower.
  • a charge stock suitable for hydrocracking is withdrawn by line 7.
  • the charge stocks for a coking operation is withdrawn by line 9 and a naphtha charge suitable for platinum reforming is withdrawn by line 11.
  • the gas'oil charge in line 5 and selected to be processed in a catalytic cracking unit such as a fluid catalytic cracking unit is passed to a catalytic cracker 13.
  • Products of catalytic cracking such as obtained by fluid catalytic cracking are separated in suitable fractioning equipment notshownto permit the recovery of olefin products suitable for passage by line 15 to an alkylation unit represented by block 17.
  • Higher boiling catalytic product material is passed by line 19 to a splitter tower 21 wherein a separation is made between light catalytic gasoline withdrawn overhead by line 23 from heavy catalytic gasoline withdrawn from the bottom thereof by line 25.
  • the light catalytic gasoline obtained from the catalytic cracking operation is passed by line 23 to a regular gasoline pool represented by block 27.
  • the product of alkylation is passed by line 29 to regular gasoline pool 27.
  • the heavy catalytic gasoline withdrawn by line maybe passed by line 31 to block 33 for effecting a shape selective cracking thereof or thermal upgrading to gasoline product.
  • the material thus treated is passed by line 35 to regular gasoline pool 27.
  • heavy catalytic gasoline instead of going through the steps of block 33 may be passed by line 37 to a pretreating step such as pretreater 39 for upgrading as discussed herein.
  • the hydrocarbon charge in line 7 and suitable for processing by hydrocracking is passed to hydrocracker 41 wherein the charge is converted to products including light hydrocracking gasoline withdrawn by line 43 and heavy hydrocracked naphtha withdrawn by line 45.
  • the light hydrocracked gasoline product in line 43 is passed to hexane upgrading represented by block 47.
  • the hydrocarbon charge in line 9 and suitable for conversion by coking such as a delayed coker is passed to coker 49.
  • the hydrocarbon charge is converted and a light coker gasoline is recoverd therefrom by line 51 with a high boiling product by line 53 which is suitable for further processing in a hydrocracker represented by 41.
  • the coker gasoline in line 51 is passed to pretreating step 39.
  • pretreting step 39 straight-run gasoline, coker gasoline, and heavy catalytic cracked gasoline, in combination with one another or separately, are treated under hydrogenation conditions to efiect desulfurization and denitrogenation of the charge where required.
  • the gasoline charge is thus pretreated by hydrogenation and may be combined with heavy naphtha product of hydrocracking obtained from 41 and thereafter the combined charge is passed by line 55 to a platinum reforming operation represented by block 57.
  • the processing scheme of FIG. 1 may replace the processing arrangement represented by pretreater 39 and platinum reforming 57.
  • the product of platinum reforming obtained in 57 is thereafter passed by line 59 to a separator 61 wherein separation is made between a light reformate product and a heavy reformate product.
  • the light reformate product is withdrawn by line 63 and passed to hexane upgrading 4,7. This, of course, is very much in the same manner but less detailed than that described in FIG. 1.
  • the heavy reformate product depending upon the cut point of splitter 61 may be passed to either premium gasoline pool, regular gasoline pool or both in some cases. In one arrangement the heavy reformate product is passed by line 65 to regular gasoline pool 27 or by line 67 to premium gasoline pool 69.
  • block 71 and identified as a gas plant is concerned with the refinery operation which effects the recovery 0.; hydrocarbons from pentanes and light straight-run naphtha. The C s are withdrawn by line 73, the pentanes by line 75 and the straight-run naphtha by line 77.
  • FIG. 2 shows isomerization of pentanes in block 79, from which is recovered an isopentane material in line 81 for passage to premium and regular gasoline pools 69 and .27 respectively.
  • the light straight-run naphtha in line 77 is passed to hexane upgrading 47 from which is recovered neohexane and aromatics by line 83 which may then be passed to either premium gasoline pool 69 or regular gasoline pool 27.
  • compositions comprising
  • a method for upgrading gasoline product of coking, hydrocracking, catalytic cracking and straight run gasoline which comprises (a) desulfnrizing gasoline product obtained as by coking and straight run gasoline,
  • a method for upgrading straight run gasoline hydrocracked gasoline, coker and heavy gasoline product of catalytic cracking which comprises,
  • a method for upgrading gasoline fractions boiling in the range of C hydrocarbons up to about 380 F. which comprises (a) stabilizing and desulfurizing said gasoline fraction so as to recover a first hydrocarbon stream rich in C hydrocarbons from a second higher boiling hydrocarbon stream comprising C hydrocarbons,

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Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3755140A (en) * 1971-08-11 1973-08-28 Universal Oil Prod Co Simultaneous production of aromatic hydrocarbons and isobutane
US3844935A (en) * 1973-01-02 1974-10-29 Phillips Petroleum Co Process for producing lead free motor fuel
US4594145A (en) * 1984-12-07 1986-06-10 Exxon Research & Engineering Co. Reforming process for enhanced benzene yield
US4594144A (en) * 1985-06-14 1986-06-10 Uop Inc. Process for making high octane gasoline
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
US5545788A (en) * 1991-06-19 1996-08-13 Mobil Oil Corporation Process for the alkylation of benzene-rich reformate using MCM-49
RU2131908C1 (ru) * 1997-11-10 1999-06-20 Уфимский государственный нефтяной технический университет Способ получения высокооктанового бензина
CN102099444A (zh) * 2008-06-05 2011-06-15 雪佛龙美国公司 生产高辛烷值汽油的催化重整法
WO2013166235A3 (fr) * 2012-05-02 2014-01-09 Saudi Arabian Oil Company Optimisation de la production de composés aromatiques à partir de naphtas hydrocraqués
US10093873B2 (en) 2016-09-06 2018-10-09 Saudi Arabian Oil Company Process to recover gasoline and diesel from aromatic complex bottoms
US11066344B2 (en) 2017-02-16 2021-07-20 Saudi Arabian Oil Company Methods and systems of upgrading heavy aromatics stream to petrochemical feedstock
US11591526B1 (en) 2022-01-31 2023-02-28 Saudi Arabian Oil Company Methods of operating fluid catalytic cracking processes to increase coke production
US11613714B2 (en) 2021-01-13 2023-03-28 Saudi Arabian Oil Company Conversion of aromatic complex bottoms to useful products in an integrated refinery process

Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3755140A (en) * 1971-08-11 1973-08-28 Universal Oil Prod Co Simultaneous production of aromatic hydrocarbons and isobutane
US3844935A (en) * 1973-01-02 1974-10-29 Phillips Petroleum Co Process for producing lead free motor fuel
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
US4594144A (en) * 1985-06-14 1986-06-10 Uop Inc. Process for making high octane gasoline
US4975179A (en) * 1989-08-24 1990-12-04 Mobil Oil Corporation Production of aromatics-rich gasoline with low benzene content
US5545788A (en) * 1991-06-19 1996-08-13 Mobil Oil Corporation Process for the alkylation of benzene-rich reformate using MCM-49
RU2131908C1 (ru) * 1997-11-10 1999-06-20 Уфимский государственный нефтяной технический университет Способ получения высокооктанового бензина
CN102099444A (zh) * 2008-06-05 2011-06-15 雪佛龙美国公司 生产高辛烷值汽油的催化重整法
WO2013166235A3 (fr) * 2012-05-02 2014-01-09 Saudi Arabian Oil Company Optimisation de la production de composés aromatiques à partir de naphtas hydrocraqués
CN104321412A (zh) * 2012-05-02 2015-01-28 沙特阿拉伯石油公司 最大程度地从加氢裂化石脑油生产芳烃
US9109169B2 (en) 2012-05-02 2015-08-18 Saudi Arabian Oil Company Maximizing aromatics production from hydrocracked naphtha
US10093873B2 (en) 2016-09-06 2018-10-09 Saudi Arabian Oil Company Process to recover gasoline and diesel from aromatic complex bottoms
US10934495B2 (en) 2016-09-06 2021-03-02 Saudi Arabian Oil Company Process to recover gasoline and diesel from aromatic complex bottoms
US11613713B2 (en) 2016-09-06 2023-03-28 Saudi Arabian Oil Company Process to recover gasoline and diesel from aromatic complex bottoms
US11066344B2 (en) 2017-02-16 2021-07-20 Saudi Arabian Oil Company Methods and systems of upgrading heavy aromatics stream to petrochemical feedstock
US11613714B2 (en) 2021-01-13 2023-03-28 Saudi Arabian Oil Company Conversion of aromatic complex bottoms to useful products in an integrated refinery process
US11591526B1 (en) 2022-01-31 2023-02-28 Saudi Arabian Oil Company Methods of operating fluid catalytic cracking processes to increase coke production

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