US2852439A - Integrated fractionation, fluid coking and catalytic cracking process for hydrocarbon oils - Google Patents

Integrated fractionation, fluid coking and catalytic cracking process for hydrocarbon oils Download PDF

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Publication number
US2852439A
US2852439A US382977A US38297753A US2852439A US 2852439 A US2852439 A US 2852439A US 382977 A US382977 A US 382977A US 38297753 A US38297753 A US 38297753A US 2852439 A US2852439 A US 2852439A
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United States
Prior art keywords
zone
cracking
coke
gas oil
line
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Expired - Lifetime
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US382977A
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English (en)
Inventor
Charles E Jahnig
Frank T Barr
James W Brown
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ExxonMobil Technology and Engineering Co
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Exxon Research and Engineering Co
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Priority to BE532013D priority Critical patent/BE532013A/xx
Application filed by Exxon Research and Engineering Co filed Critical Exxon Research and Engineering Co
Priority to US382977A priority patent/US2852439A/en
Priority to GB22611/54A priority patent/GB757769A/en
Priority to FR1111174D priority patent/FR1111174A/fr
Priority to DEST8750A priority patent/DE964086C/de
Application granted granted Critical
Publication of US2852439A publication Critical patent/US2852439A/en
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G51/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only
    • C10G51/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural parallel stages only
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B55/00—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material
    • C10B55/02—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material with solid materials
    • C10B55/04—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material with solid materials with moving solid materials
    • C10B55/08—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material with solid materials with moving solid materials in dispersed form
    • C10B55/10—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material with solid materials with moving solid materials in dispersed form according to the "fluidised bed" technique

Definitions

  • the present invention relates to an integrated conversion process yand system for hydrocarbon oils. More particularly, it relates to a system for hydrocarbon conver- -and others as will be explained in greater detail hereinafter.
  • a conversion system described in an application of Barr et al., Serial No. 302,646, filed August 5, 1952, upon which the present invention is an improvement, has several advantages over prior art systems, e. g. in thermal elciency of fractionation, in simplicity of apparatus, etc.
  • a feedstock which may be either a Whole crude or a topped or reduced crude, is fed to a fractionator along with the total effluent from a catalytic cracking zone. rhe heat from the latter contributes substantially to the over all economy of fractionation.
  • These pdyantages are largely retained in the instant case, with Gas oils obtained by drastic thermal treaty Patentes sept.
  • Another advantage of the present invention is the re duction of the load on the catalytic cracking zone, as compared with the dual zone (coking followed by cracking) process described above.
  • the gas and naphtha formed in the coking zone are not passed through the cracking zone. Hence its over all capacity can be kept to a minimum. Moreover, heat balance in the cracking zone is more easily maintained.
  • feed such as a topped crude may be brought through a line l@ into a vacuum tower 1l of conventional type.
  • the feed may be brought into a fractionator di?, to be more fully described below, when the use of the relatively expensive vacuum tower is not economically justifiable. ln either case a bottoms fraction and a more volatile fraction or fractions are obtained.
  • the vacuum tower outlet l2 is connected to or comprises a conventional condensing means such as a cooling coil or .condenser 13 and a water separator ld.
  • the separator is connected to a vacuum pump l5 on the vapor side and with a liquid pump l?. From pump i7 the distillate oil passes through a line i@ to the catalytic cracker feed line 21.
  • the bottoms from vacuum tower i3 pass through line 23 to a coker feed line 25.
  • Valve 2'? may be provided in line 25.
  • the vessel 35 preferably has a lower section or portion 37 o-f reduced cross-section, which may serve as a stripping zone. a tapering or upwardly expanding section 39 above the stripping zone, an enlarged upper section 41 constituting the top of the .coking zone proper, and disengaging section 43, preferably of somewhat smaller cross-section than the top part of coking zone 41.
  • the coking zone must be such that a bed of finely d-ivided solid particles, which are good heat carriers, but are relatively inert catalytically, may be fluidized therein.
  • Such particles may be metal shot, beads, sand, purnice, etc.,-but coke particles of a size within the general range of 50 to 400 microns average particle diameter are usually preferred. The reason for this is that coke is produced in the process, is readily available, and is a reasonably good heat carrier. lt is also quite inexpensive or of relatively low economic value. ⁇
  • Hot solid inert particles are brought into the reactor 35 through a line 45 from heater or burner vessel 47. As is now well known in the art, these particles are preheated in vessel 47 to a temperature between about 900 and 1500 F., either by burning colte formed inthe coking vessel, or by burning extraneous fuel, or both.
  • a uidizing gas such as steam may be injected into coking vessel 35 through line 43.
  • the oil feed to the coker vessel is injected into or onto and among the preheated solid particles therein in Such a manner as to secure as uniform distribution as possible.
  • each particle is coated with a thin layer or film of the feed.
  • the heat of the particle evaporates the volatile constituents of the oil film and converts the residue to coke and to cracked vapors and gases.
  • the coke is deposited upon the particle and each of the coated particles thus tends to grow or increase in size while in the reactor.
  • the vaporized and cracked products pass from the coking reactor through a gas-solids separator 49 with a solids return tine S1 extending into the fluidized solids bed 34.
  • the gaseous or vaporous products, now relatively free of entrained solids, pass out through a line 53 into a line 55 leading to the fractionator 50 previously mentioned.
  • Spent solid particles, carrying coke deposits, are Withdrawn by gravity through a stripping zone 37 at the bottom of the reactor vessel.
  • a stripping gas such as steam is introduced through a line 59 into this stripping zone which may be provided with bafes 61 to improve distribution of the stripping gas.
  • the spent particles pass through a coarse screening device 63 into an outlet line 65 through which they are conveyed to the heater vessel 47. Solid particles sometimes agglomerate or grow to such dimensions that they cannot conveniently be uidized and such are diverted by the coarse screening device 63 into withdrawal line 67 from which they may be removed through a closure such as the large Valves 69 and 70.
  • the spent particles are introduced through a standpipe or conduit 71 wherein they may be fluidized and propelled by a suitable gas stream, such as steam, admitted through a line 73.
  • a suitable gas stream such as steam
  • a uidizing gas which supports combustion, such as air or oxygen, is introduced into the burner by means of a line 77.
  • a fuel gas is introduced through a line 79 for starting up the burner, after which the combustion-supporting gas reacts with the coke deposited on the solid particles to supply the necessary heat.
  • the extraneous heating gas from line 79 may be burned continuously and preferentially where it is desired to produce maximum colic as a product of the process.
  • Product coke is Withdrawn through line 67, or it may be withdrawn from the system at any other suitable point, such as outlets (not shown) from lines 65 or S9.
  • the iiuidized solids in vessel 47 form a bed 81 whose upper level 83 .is controlled by suitable means, shown herein as a notched weir 35 constituting the upper end of a withdrawal line 87.
  • suitable means shown herein as a notched weir 35 constituting the upper end of a withdrawal line 87.
  • the latter connects through a suit- .f
  • Suitable means are provided, as is well understood in the art, for keeping the solids uidized or otherwise mobile in lines 65, 39, 4S, etc.
  • the arrangement preferably is such that both the light products from the cracking operation, to be described below, and from the coking operation, pass through the flash zone and assist in vaporizing the heavy ends.
  • Gaseous products are withdrawn overhead through a line 91, naphtha through line S3, and gas oil through line 95.
  • the bottoms fract n, reduced to a minimum by the ample heat of the iight products from both co-king and cracking is passed through line 97 to the coker feed line 25.
  • Other fractions, not shown, may be taken from the fractionator if desired. Modifications can be made in the fractionation system, for example the naphtha product may be taken overhead as a vapor and then condensed.
  • the gas oil in line 95 is taken through line 21 into the inlet 102 of a catalytic cracking vessel 100.
  • a catalytic cracking vessel 100 Preferably this is a fraction boiling between about 430 and 1050 F.
  • the latter is preferably of the uidized solids type but other conventional types of cracking apparatus may be used in some cases.
  • Cracked products are returned t0 this fractionator 50 through a line 101 connecting With line 55, or independently if desired.
  • the operation of such a cracking system is well known and needs no detailed description.
  • the feed to the catalytic cracker may be recycled to extinction if desired.
  • the end point of this gas oil may be controlled by using proper temperature in the dash zone of the fractionator 59. In this manner the amount of contaminants in the catalytic cracker feed can be minimized and the Conradson carbon may be controlled.
  • the amount of recycling from catalytic cracker to fractionat-or and return can be adjusted to keep the desired heat balance in the catalytic cracking zone.
  • the cracking severity can be reduced and recycling increased to transfer more heat to the fractionator.
  • By reducing recycling and increasing severity of cracking less heat is transferred to the fractionator. Good fractionation is desirable between the gas oil and the fractionator bottoms and this can be accurately controlled in this system.
  • the amount of coke produced in catalytic cracking can also be controlled.
  • a wash stream of clean t gas oil can be used below the gas oil draw-off in the fractionator to reduce contamination by the fresh feed of the gas oil going to the catalytic cracking unit.
  • hot fresh or regenerated catalyst may be supplied to the catalytic cracker from a suitable source or from a regenerator through line 102.
  • the spent catalyst will be stripped in a stripping zone 103 by means ofl a stripping gas such as steam admitted through a line 105.
  • the spent catalyst is then returned to the conventional regenerator, not shown, through a line 107.
  • crude or preferably a topped crude feed may be fed either to the vacuum tower 11 or directly to the product fractionator 50 or both, as may be desirable, and that various other arrangements may be made as will be apparent to those skilled in the art.
  • fresh feed is brought into the fractionator, e. g. through line 90, it should be introduced substantially above the inlet of the hot vapors from line 55.
  • the vapors from coking and from cracking can be introduced at different heights to vary the temperature gradient in the fractionator as desired.
  • the liquid in the bottom of the fractionator is preferably quenched, by suitable conventional means not shown. to keep its temperature below about 700 F. and avoid coking in this vessel.
  • the fractionator bottoms may be steam stripped if desired.
  • each of the vessels 47 and 100 appropriate gas-solids separating means such as cyclones 111 and 112 are installed and operated in a conventional manner to remove solids from the exit gases or vapors.
  • the ue gases from the heater or burner vessel 47 are taken overhead through a suitable pressure control valve 114 and outlet 116 for suitable heat transfer andi/or other disposition.
  • a partial condenser 120 is inserted in line 101. Condensation is just sufficient to remove a purge stream, which may be withdrawn through a line 122.
  • a hydrocarbon conversion process which comprisesl in combination, the steps of: initially separating a crude feed in a fractionation zone to obtain a bottoms fraction, a gas oil fraction boiling immediately above said bottoms fraction within the limits of 430-1050 F. and lighter material which is withdrawn as product; converting said gas oil fraction by contact with a uid bed of cracking catalyst in a catalytic cracking zone to vaporous catalytic conversion products and coke which is deposited on said cracking catalyst; converting said bottoms fraction by contact with a uid bed of finely divided inert coke particles in a coking zone to vaporous Coker conversion products and coke which is deposited on said finely divided inert coke particles; maintaining the temperature of said catalytic cracking zone by circulating said cracking catalyst through an external regeneration zone wherein coke deposits on the catalyst are removed by combustion; mantaining the temperature of said coking zone by circulating said nely divided coke particles through an external heating zone wherein the coke particles are heated by partial combustion

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Dispersion Chemistry (AREA)
  • Materials Engineering (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US382977A 1953-09-29 1953-09-29 Integrated fractionation, fluid coking and catalytic cracking process for hydrocarbon oils Expired - Lifetime US2852439A (en)

Priority Applications (5)

Application Number Priority Date Filing Date Title
BE532013D BE532013A (en(2012)) 1953-09-29
US382977A US2852439A (en) 1953-09-29 1953-09-29 Integrated fractionation, fluid coking and catalytic cracking process for hydrocarbon oils
GB22611/54A GB757769A (en) 1953-09-29 1954-08-04 Improvements in or relating to cracking hydrocarbon oils
FR1111174D FR1111174A (fr) 1953-09-29 1954-08-25 Procédé et dispositif pour la conversion d'hydrocarbures
DEST8750A DE964086C (de) 1953-09-29 1954-09-18 Verfahren zur Umwandlung von schweren Kohlenwasserstoffoelen

Applications Claiming Priority (1)

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US382977A US2852439A (en) 1953-09-29 1953-09-29 Integrated fractionation, fluid coking and catalytic cracking process for hydrocarbon oils

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BE (1) BE532013A (en(2012))
DE (1) DE964086C (en(2012))
FR (1) FR1111174A (en(2012))
GB (1) GB757769A (en(2012))

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3878088A (en) * 1974-03-04 1975-04-15 Robert S Nahas Integrated production of olefins and coke
US3907664A (en) * 1971-06-04 1975-09-23 Continental Oil Co Integrated delayed coking and thermal cracking refinery process
US20080230440A1 (en) * 2007-03-12 2008-09-25 Robert Graham Methods and Systems for Producing Reduced Resid and Bottomless Products from Heavy Hydrocarbon Feedstocks

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB803104A (en) * 1956-04-25 1958-10-15 Exxon Research Engineering Co Process for cracking hydrocarbons and a combination fluid solids reactor and thermal cracking unit

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2312230A (en) * 1940-06-29 1943-02-23 Kellogg M W Co Catalytic conversion of hydrocarbons
US2338020A (en) * 1941-02-25 1943-12-28 Texas Co Conversion of hydrocarbon oils
US2388055A (en) * 1942-06-13 1945-10-30 Standard Oil Dev Co Petroleum conversion process
US2636844A (en) * 1950-08-29 1953-04-28 Standard Oil Dev Co Process for the conversion of reduced crudes in the presence of an added naphtha
US2644785A (en) * 1950-06-03 1953-07-07 Standard Oil Dev Co Combination crude distillation and cracking process
US2717862A (en) * 1951-05-29 1955-09-13 Exxon Research Engineering Co Coking of hydrocarbon oils
US2766184A (en) * 1952-02-01 1956-10-09 Exxon Research Engineering Co Combination oil refining process

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2198557A (en) * 1938-09-13 1940-04-23 Florez Engineering Co Inc De Cracking hydrocarbon oils

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2312230A (en) * 1940-06-29 1943-02-23 Kellogg M W Co Catalytic conversion of hydrocarbons
US2338020A (en) * 1941-02-25 1943-12-28 Texas Co Conversion of hydrocarbon oils
US2388055A (en) * 1942-06-13 1945-10-30 Standard Oil Dev Co Petroleum conversion process
US2644785A (en) * 1950-06-03 1953-07-07 Standard Oil Dev Co Combination crude distillation and cracking process
US2636844A (en) * 1950-08-29 1953-04-28 Standard Oil Dev Co Process for the conversion of reduced crudes in the presence of an added naphtha
US2717862A (en) * 1951-05-29 1955-09-13 Exxon Research Engineering Co Coking of hydrocarbon oils
US2766184A (en) * 1952-02-01 1956-10-09 Exxon Research Engineering Co Combination oil refining process

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3907664A (en) * 1971-06-04 1975-09-23 Continental Oil Co Integrated delayed coking and thermal cracking refinery process
US3878088A (en) * 1974-03-04 1975-04-15 Robert S Nahas Integrated production of olefins and coke
US20080230440A1 (en) * 2007-03-12 2008-09-25 Robert Graham Methods and Systems for Producing Reduced Resid and Bottomless Products from Heavy Hydrocarbon Feedstocks
EP1970427A3 (en) * 2007-03-12 2012-05-09 Ivanhoe Energy Inc. Methods and systems for producing reduced resid and bottomless products from heavy hydrocarbon feedstocks
US8377287B2 (en) 2007-03-12 2013-02-19 Ivanhoe Energy, Inc. Methods and systems for producing reduced resid and bottomless products from heavy hydrocarbon feedstocks
US8808632B2 (en) 2007-03-12 2014-08-19 Ivanhoe Energy Inc. Methods and systems for producing reduced resid and bottomless products from hydrocarbon feedstocks
US9434888B2 (en) 2007-03-12 2016-09-06 Ivanhoe Htl Petroleum Ltd. Methods and systems for producing reduced resid and bottomless products from heavy hydrocarbon feedstocks

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DE964086C (de) 1957-05-16
GB757769A (en) 1956-09-26
BE532013A (en(2012))
FR1111174A (fr) 1956-02-23

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