CA1126188A - Two-stage integrated coking for chemicals and coke gasification process - Google Patents
Two-stage integrated coking for chemicals and coke gasification processInfo
- Publication number
- CA1126188A CA1126188A CA293,001A CA293001A CA1126188A CA 1126188 A CA1126188 A CA 1126188A CA 293001 A CA293001 A CA 293001A CA 1126188 A CA1126188 A CA 1126188A
- Authority
- CA
- Canada
- Prior art keywords
- zone
- solids
- coking
- gas
- gasification
- 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
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Coke Industry (AREA)
Abstract
ABSTRACT OF THE DISCLOSURE
Unsaturated light hydrocarbons are produced by coking a heavy hydrocarbonaceous oil in a conventional fluid coking zone and subsequently heating the vaporous coker product to a higher temperature in a gas-solids separation zone, such as the coking reactor's cyclone separator, with hot solids derived from a coke gasification zone.
Unsaturated light hydrocarbons are produced by coking a heavy hydrocarbonaceous oil in a conventional fluid coking zone and subsequently heating the vaporous coker product to a higher temperature in a gas-solids separation zone, such as the coking reactor's cyclone separator, with hot solids derived from a coke gasification zone.
Description
BACKGE~OIJND OF THE INVENlION
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2 1~ Field of the Inven_on -
3 T~e present invention rela~ces to an improvement
4 ln an lntegrated fluid coking and coke gasifieatlon prvce~s S for the production of unsaturated light hydros::arbons and 6 aroma~cics useful as chemicals and chemical intermed~a~ces.
7 2. ~9~
8 The fluid coking process for the produc~ion of 9 fuels, such as gas oil and naph~ha is a weil known process, Integrated fluid coking and co~e gasification processes are `
ll also known.
12 - -Fluid coking processes for the production of 13 chemicals and chemical intermediates are also known.
14 Generally9 when it is desired to produce chemicals rather 'chan fuel oils" heretofore, ~he fluid coklng process usually 16 ~ncluded a high temperature transferline coking zone and a l7 j f~uidized bed coking zone 18 It is also known to introduce a small amount of 1~ Ihot solids in~o a gas-solids separation zone, such as the Icyclone separator, used to separate entrained solids from 21 the vaporous coker product so as to prevent coke deposition 22 on the wall~ o~ the cyclone separator.
~3 ~ It ha~ now been ~ound ~at cok~ng for the produc-2~ tion of chemicals and chemical in~ermediates c~n be p~o~med by coking a carbon~ceou~ material in a convention~l 1uid coking zone and subsequen~l~ hea~ing the resul~ing 27 vaporous product to a te~npera~ure su~ficient to crack the 28 coke~ vaporous product to unsaturated hydrocarbons in a ~ c~nventional gas-solids separation zone used to remove ~ntrained sol~ds from the coker vaporous product. The heat 31 ial the gas-~olids separation zone is provided by passing a 32 po~ion of ho~ solids from a gasification zone ~o ~he gas-1 olids separation zone.
__ 3 In accordance with the invention ~here is provided 4 in an integrated coking and gasification process oomprising the steps of (a) reacting a carbonaceous material having a 6 Conradson carbon content of at least l0 weight percent in 7 a coking zone conta~ning a bed o~ fluidized ~olids maintained 8 a~ fluid co~ing conditions to form a vsporous coking zone 9 conversion product and coke, said coke deposi~ing on said fluidized solids; (b) introducing at least a por~ivn of 11 said solids with the cske deposltion thereon .into a hea~ing 12 zone operated at a temperature greater than said coking zone 13 temperature to heat said por~ion of solids, (c) recycling a 14 irst portion of hea~ed solids from said heating zone to said coking zone and introduGing a second portion of said 16 heated solids to a fluid bed gasifica~ion zone main~ained 17 at a temperature greater than ~he tempera~ure of said 18~ heating zone; (d) passing said vaporous eoker conversion 19 product with entrained solids to a gaæ~soLids separation ~one, the lmprovement which compriseso withdrawing a pvr~
~1 tion of solids ~rom said gasification zone and introducing 22 sald portion of solids into said g~s-solids separation zone 23 in an amo~nt sufficient to maintai~ said g~s-solids separa~
24 tion zone at a temperature in the range of about 1200 to about 1700 degr0es Fahrenheit~wh~reby at least a portlon ~f 26 said vaporous coking zone product is conver~ed ~o unsaturated 27 hydrocarbons.
2~ BRIEF ~ESCRI,PTION 01 T~E D~AWIYC
The figure is a schematic flow plan of one embodi~
~ ment o the invention.
31 DESCRIPTION OF THE P~EFERRED EMBODIMENT
.. . .. ~ ~ . .. .. .
32 Referrirlg ~o the flgure, a carbonaceous material 3 ~
.
l having a Conradson carbon resldue of about lS weigh~ percent 2 such as heavy residuum having a boillng point (a~ atmospheric '.
3 pressure) of about l,OSO~F. ~ ~s passed by line 10 into a 4 coking zone 12 in whi~h is ma~ntained a fluidized bed of solids (e~g~ coke particles of 40 ~o 1000 microns in size) 6 hav~ng an upper le~el indicated at 14. Carbonaceous feeds 7 uitable for the present in~ention include heavy hydrocarbon-8 aceous o~ls; heavy and re~uced petrolleum crudes; petroleum 9 atmospheric distillation bottoms; pe~roleum vac~m distilla-~ion bottoms; pitch~ asphaltg bitumen~ other hea~y hydro~
11 carbon residues3 coalg coal slurry~ liquid products derived 12 from coal liquefaction proeesses and mixtures thereof.
13 Typically such feeds have a Conradson carbon re~idue o at 14 least 10 weight percent~ generally ~rom about 10 to about lS 50 weight percent (as to Conradson carbon residue~ see 16 ASTM test D 189~65). A fluidiz;ng gas, e~g. ste~m3 ls 17 admit~ed at the base of coking reactor l throug~ line 16 ln l~ an amoun~ sufficient to obtain superficial 1uidizing gas 19 velocity in the range o 0-5 to 5 ~eet per second. Coke at a temperature above the coking temperature, or example, 21 the temperature from about 100 to abou~ 400 Fahr~nhelt 22 degrees in excess of the ac~ual operating temperature o~
23 ~he coking zone is admitted ~o reactor 1 by line 4~ in an 24 amo~mt su~ficient to maintain ~he coking ~emperature ln the range of abou~ 8S0 to abou~ 1400Fq The pressure in the ~ g 26 zone ls malntained in the range from about 5 ~o ak~ ~nds~
27 ~quare inch gauge (psig), pre~erably ln the r~ge o:e abcll~ 5~o 2B about 45 peig. The lower portion o~ ~he coklng reactor ~9 serves as a str:lpping zone to remove occluded hydrocarbons 3~ rom the coke. A s~ream of coke is withdrawn from the 31 s'cripping zone by Iine 18 and clrculated to heater 2. The 32 v~porous cokin~s zone conversion product i~ passed through ~ i l a ~as-solids separation zone sucb as cyclones 20 to remove 2 entrained solids w~ieh are returned ~o the coker zone throu~h 3 dipleg 24. The cyclone separator system may be one or more 4 cyclones. In accordan~e with the present invention, the temperature in the cyclone is maintained in `the range of 6 1200 to 1700 degrees Fahrenheit 9 preferably a~ a temperature :- .7 in the range of about 1300 to about 1500 degrees Fahrenheit, : 8 to convert at least a portion of the cokin~ zone conversion 9 product into unsaturated lower boillng hydrocarbons such as olefins and diolefins and into aromatics w~ich are useful ll as chemicals or chemical intermediates~ The temperature l2 in the cyclones is maintained at an elévated temperature by 13 introducing in~o thP cyclones a sufficier~t amoun~ of a 14 stream of hot solids withdrawn from the gasifier by line 58 lS and ~hen injected by line 60 above the dense 1uid bed in~o 16 the dilute phase in the region adj~cent to the inlets of : :17. ~he cyclones. The heated g~sifier solids may be discharged 18 into the vaporous coker product passing into the c~clones 19 via the inlets of the cyclones or ~he hot gasifier solids ~ m~y be ln~roduced directly into the cyclone separators.
21 ~reerably, the amount of hot gasifier solids in~roduced 22 into the cyclones is such as to convert a~ least 20 weight 23 per~ent o~ the coker vaporvus product to unsaturated 24 hydrocarbons having 1~85 than 6 carbon atoms. The resul~in~
vapors ~eave the cyclones ~hrough line 24 and pa~ lnto a 26 ~crubber 25 moun~ed on ~he coking reac~or. I desired, a 27 stream o~ heavy mate~ia~ condensed in the ~crubber may be 28 recycl~d to ~he coking reac~or via line 26. Furthermore, if desired a portion of the carbonaceous feed may be ~ in~ected into the scrubber to provlde an adequate volume to 31 c~rry coke fines back to the coking zone. The cyclone : 32 conversion products are removed from ~crubber 25 via line .. . ~
28 for fractionation in a conventional manner~ In hea~cer 29 2 stripped coke frvm coking reactor 1 (eommonly called cold 3 coke) is introduced by line 18 to a fluid bed of hot coke h~ving an upper level indica~e~ a~30. The bed is par~lally heated by passing a fuel gas into the heater by line 32.
6 Supplementary heat is applied to ~he heater by coke circu-~ 7 lat~ng in line 34. The gaseous effluent of the heater~
- 8 inc~uding entrained solids~ passes through a cyclone w~ich may be a first cyclone 36 and a second cyclone 38 wherein separation of the larger entrained solids occurs. The 11 se~arated l~rger solids are returned to the heater bed via l2 the respective cyclone diplegs. The heater gaseous effluent - l3 w~ich still contains entrained solids fines is removed from . 14 heater 2 via line 40.
Hot coke is removed from the fluidized bed in 16 heater 2 ~nd recycled to coking reactor by line 42 to supply 17 heat thereto~ Another portion of coke is removed from 18 heater 2 and passed by line 4~ to ~ gasific~tlon zone 46 in , : 19 gasifier 3 in which ~s main~ained a bed of 1uidized coke having a level indicated a~ 48. If deslred~ a purge s~ream 21 o coke may be removed ~rom heater 2 by line 50.
~2 The gasification zone is main~ained at a tempera-23 ture ranging from about 19500 to about 2~000F. and at a 2~ pr~ssure rangin~ rom about 5 to about 150 p8ig, pre~rably at a press1lre ranging from about lO to abou~ 60 psig and 26 more preerably at ~ pressure ranging from about 25 to abou~
27 45 ps:Lg. Steam by line 52 and Rll oxygen-con~aln$ng gas 28 such as air, commercial oxygen or air enriched wl~h oxygen by line 54 are passed via line 56 into gasifier 30 Reaetion ~ o the coke particles in the gasification zone with the 31 steam and the oxygen--~on~aining gas produces a hydrogen and 32 carbon monoxide-containin~ fuel ga~ The gas-lfier produc~.
,.Z~
1 fuel gas, which m~y further contain some entrained solids, 2 is removed o~erhead from gasifier 3 by line 32 and in~roduced 3 into heater ~ to provide a portion of the required heat~ as 4 previously described.
While the process has been described for simplicity 6 of description with respect to circulating coke as ~he 7 fluidized medium, it is tv be understood that the fluidized 8 seed particles on which the coke is deposited may be silica, 9 alumina, zirconiaa magnesia, calcium oxide, al~ndum, mullite, .
bauxite or the like. The fluidized solids may or may not 11 be catalytic in na~ure.
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.; . .
.
;
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7 2. ~9~
8 The fluid coking process for the produc~ion of 9 fuels, such as gas oil and naph~ha is a weil known process, Integrated fluid coking and co~e gasification processes are `
ll also known.
12 - -Fluid coking processes for the production of 13 chemicals and chemical intermediates are also known.
14 Generally9 when it is desired to produce chemicals rather 'chan fuel oils" heretofore, ~he fluid coklng process usually 16 ~ncluded a high temperature transferline coking zone and a l7 j f~uidized bed coking zone 18 It is also known to introduce a small amount of 1~ Ihot solids in~o a gas-solids separation zone, such as the Icyclone separator, used to separate entrained solids from 21 the vaporous coker product so as to prevent coke deposition 22 on the wall~ o~ the cyclone separator.
~3 ~ It ha~ now been ~ound ~at cok~ng for the produc-2~ tion of chemicals and chemical in~ermediates c~n be p~o~med by coking a carbon~ceou~ material in a convention~l 1uid coking zone and subsequen~l~ hea~ing the resul~ing 27 vaporous product to a te~npera~ure su~ficient to crack the 28 coke~ vaporous product to unsaturated hydrocarbons in a ~ c~nventional gas-solids separation zone used to remove ~ntrained sol~ds from the coker vaporous product. The heat 31 ial the gas-~olids separation zone is provided by passing a 32 po~ion of ho~ solids from a gasification zone ~o ~he gas-1 olids separation zone.
__ 3 In accordance with the invention ~here is provided 4 in an integrated coking and gasification process oomprising the steps of (a) reacting a carbonaceous material having a 6 Conradson carbon content of at least l0 weight percent in 7 a coking zone conta~ning a bed o~ fluidized ~olids maintained 8 a~ fluid co~ing conditions to form a vsporous coking zone 9 conversion product and coke, said coke deposi~ing on said fluidized solids; (b) introducing at least a por~ivn of 11 said solids with the cske deposltion thereon .into a hea~ing 12 zone operated at a temperature greater than said coking zone 13 temperature to heat said por~ion of solids, (c) recycling a 14 irst portion of hea~ed solids from said heating zone to said coking zone and introduGing a second portion of said 16 heated solids to a fluid bed gasifica~ion zone main~ained 17 at a temperature greater than ~he tempera~ure of said 18~ heating zone; (d) passing said vaporous eoker conversion 19 product with entrained solids to a gaæ~soLids separation ~one, the lmprovement which compriseso withdrawing a pvr~
~1 tion of solids ~rom said gasification zone and introducing 22 sald portion of solids into said g~s-solids separation zone 23 in an amo~nt sufficient to maintai~ said g~s-solids separa~
24 tion zone at a temperature in the range of about 1200 to about 1700 degr0es Fahrenheit~wh~reby at least a portlon ~f 26 said vaporous coking zone product is conver~ed ~o unsaturated 27 hydrocarbons.
2~ BRIEF ~ESCRI,PTION 01 T~E D~AWIYC
The figure is a schematic flow plan of one embodi~
~ ment o the invention.
31 DESCRIPTION OF THE P~EFERRED EMBODIMENT
.. . .. ~ ~ . .. .. .
32 Referrirlg ~o the flgure, a carbonaceous material 3 ~
.
l having a Conradson carbon resldue of about lS weigh~ percent 2 such as heavy residuum having a boillng point (a~ atmospheric '.
3 pressure) of about l,OSO~F. ~ ~s passed by line 10 into a 4 coking zone 12 in whi~h is ma~ntained a fluidized bed of solids (e~g~ coke particles of 40 ~o 1000 microns in size) 6 hav~ng an upper le~el indicated at 14. Carbonaceous feeds 7 uitable for the present in~ention include heavy hydrocarbon-8 aceous o~ls; heavy and re~uced petrolleum crudes; petroleum 9 atmospheric distillation bottoms; pe~roleum vac~m distilla-~ion bottoms; pitch~ asphaltg bitumen~ other hea~y hydro~
11 carbon residues3 coalg coal slurry~ liquid products derived 12 from coal liquefaction proeesses and mixtures thereof.
13 Typically such feeds have a Conradson carbon re~idue o at 14 least 10 weight percent~ generally ~rom about 10 to about lS 50 weight percent (as to Conradson carbon residue~ see 16 ASTM test D 189~65). A fluidiz;ng gas, e~g. ste~m3 ls 17 admit~ed at the base of coking reactor l throug~ line 16 ln l~ an amoun~ sufficient to obtain superficial 1uidizing gas 19 velocity in the range o 0-5 to 5 ~eet per second. Coke at a temperature above the coking temperature, or example, 21 the temperature from about 100 to abou~ 400 Fahr~nhelt 22 degrees in excess of the ac~ual operating temperature o~
23 ~he coking zone is admitted ~o reactor 1 by line 4~ in an 24 amo~mt su~ficient to maintain ~he coking ~emperature ln the range of abou~ 8S0 to abou~ 1400Fq The pressure in the ~ g 26 zone ls malntained in the range from about 5 ~o ak~ ~nds~
27 ~quare inch gauge (psig), pre~erably ln the r~ge o:e abcll~ 5~o 2B about 45 peig. The lower portion o~ ~he coklng reactor ~9 serves as a str:lpping zone to remove occluded hydrocarbons 3~ rom the coke. A s~ream of coke is withdrawn from the 31 s'cripping zone by Iine 18 and clrculated to heater 2. The 32 v~porous cokin~s zone conversion product i~ passed through ~ i l a ~as-solids separation zone sucb as cyclones 20 to remove 2 entrained solids w~ieh are returned ~o the coker zone throu~h 3 dipleg 24. The cyclone separator system may be one or more 4 cyclones. In accordan~e with the present invention, the temperature in the cyclone is maintained in `the range of 6 1200 to 1700 degrees Fahrenheit 9 preferably a~ a temperature :- .7 in the range of about 1300 to about 1500 degrees Fahrenheit, : 8 to convert at least a portion of the cokin~ zone conversion 9 product into unsaturated lower boillng hydrocarbons such as olefins and diolefins and into aromatics w~ich are useful ll as chemicals or chemical intermediates~ The temperature l2 in the cyclones is maintained at an elévated temperature by 13 introducing in~o thP cyclones a sufficier~t amoun~ of a 14 stream of hot solids withdrawn from the gasifier by line 58 lS and ~hen injected by line 60 above the dense 1uid bed in~o 16 the dilute phase in the region adj~cent to the inlets of : :17. ~he cyclones. The heated g~sifier solids may be discharged 18 into the vaporous coker product passing into the c~clones 19 via the inlets of the cyclones or ~he hot gasifier solids ~ m~y be ln~roduced directly into the cyclone separators.
21 ~reerably, the amount of hot gasifier solids in~roduced 22 into the cyclones is such as to convert a~ least 20 weight 23 per~ent o~ the coker vaporvus product to unsaturated 24 hydrocarbons having 1~85 than 6 carbon atoms. The resul~in~
vapors ~eave the cyclones ~hrough line 24 and pa~ lnto a 26 ~crubber 25 moun~ed on ~he coking reac~or. I desired, a 27 stream o~ heavy mate~ia~ condensed in the ~crubber may be 28 recycl~d to ~he coking reac~or via line 26. Furthermore, if desired a portion of the carbonaceous feed may be ~ in~ected into the scrubber to provlde an adequate volume to 31 c~rry coke fines back to the coking zone. The cyclone : 32 conversion products are removed from ~crubber 25 via line .. . ~
28 for fractionation in a conventional manner~ In hea~cer 29 2 stripped coke frvm coking reactor 1 (eommonly called cold 3 coke) is introduced by line 18 to a fluid bed of hot coke h~ving an upper level indica~e~ a~30. The bed is par~lally heated by passing a fuel gas into the heater by line 32.
6 Supplementary heat is applied to ~he heater by coke circu-~ 7 lat~ng in line 34. The gaseous effluent of the heater~
- 8 inc~uding entrained solids~ passes through a cyclone w~ich may be a first cyclone 36 and a second cyclone 38 wherein separation of the larger entrained solids occurs. The 11 se~arated l~rger solids are returned to the heater bed via l2 the respective cyclone diplegs. The heater gaseous effluent - l3 w~ich still contains entrained solids fines is removed from . 14 heater 2 via line 40.
Hot coke is removed from the fluidized bed in 16 heater 2 ~nd recycled to coking reactor by line 42 to supply 17 heat thereto~ Another portion of coke is removed from 18 heater 2 and passed by line 4~ to ~ gasific~tlon zone 46 in , : 19 gasifier 3 in which ~s main~ained a bed of 1uidized coke having a level indicated a~ 48. If deslred~ a purge s~ream 21 o coke may be removed ~rom heater 2 by line 50.
~2 The gasification zone is main~ained at a tempera-23 ture ranging from about 19500 to about 2~000F. and at a 2~ pr~ssure rangin~ rom about 5 to about 150 p8ig, pre~rably at a press1lre ranging from about lO to abou~ 60 psig and 26 more preerably at ~ pressure ranging from about 25 to abou~
27 45 ps:Lg. Steam by line 52 and Rll oxygen-con~aln$ng gas 28 such as air, commercial oxygen or air enriched wl~h oxygen by line 54 are passed via line 56 into gasifier 30 Reaetion ~ o the coke particles in the gasification zone with the 31 steam and the oxygen--~on~aining gas produces a hydrogen and 32 carbon monoxide-containin~ fuel ga~ The gas-lfier produc~.
,.Z~
1 fuel gas, which m~y further contain some entrained solids, 2 is removed o~erhead from gasifier 3 by line 32 and in~roduced 3 into heater ~ to provide a portion of the required heat~ as 4 previously described.
While the process has been described for simplicity 6 of description with respect to circulating coke as ~he 7 fluidized medium, it is tv be understood that the fluidized 8 seed particles on which the coke is deposited may be silica, 9 alumina, zirconiaa magnesia, calcium oxide, al~ndum, mullite, .
bauxite or the like. The fluidized solids may or may not 11 be catalytic in na~ure.
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Claims (10)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. An integrated coking and gasification process comprising the steps of:
(a) reacting a carbonaceous material having a Conradson carbon content of at least 10 weight percent in a coking zone containing a bed of fluidized solids maintained at fluid coking conditions to form a vaporous coking zone conversion product and coke, said coke depositing on said fluidized solids;
(b) introducing a portion of said solids with the coke deposition thereon into a heating zone operated at a temperature greater than said coking zone temperature to heat said portion of solids;
(c) recycling a first portion of heated solids from said heating zone to said coking zone and introducing a second portion of said heated solids to a fluid bed gasification zone maintained at a temperature greater than the temperature of said heating zone, and (d) passing said vaporous coking zone conversion product with entrained solids to a gas-solids separation zone, characterized in that it comprises withdrawing a portion of solids from the gasification zone and introducing said portion of solids into said gas-solids separation zone in an amount sufficient to maintain said gas-solids separation zone at a temperature in the range of about 1200 to about 1700 degrees Fahrenheit, whereby at least a portion of said vaporous coking zone product is converted to unsaturated hydrocarbons.
(a) reacting a carbonaceous material having a Conradson carbon content of at least 10 weight percent in a coking zone containing a bed of fluidized solids maintained at fluid coking conditions to form a vaporous coking zone conversion product and coke, said coke depositing on said fluidized solids;
(b) introducing a portion of said solids with the coke deposition thereon into a heating zone operated at a temperature greater than said coking zone temperature to heat said portion of solids;
(c) recycling a first portion of heated solids from said heating zone to said coking zone and introducing a second portion of said heated solids to a fluid bed gasification zone maintained at a temperature greater than the temperature of said heating zone, and (d) passing said vaporous coking zone conversion product with entrained solids to a gas-solids separation zone, characterized in that it comprises withdrawing a portion of solids from the gasification zone and introducing said portion of solids into said gas-solids separation zone in an amount sufficient to maintain said gas-solids separation zone at a temperature in the range of about 1200 to about 1700 degrees Fahrenheit, whereby at least a portion of said vaporous coking zone product is converted to unsaturated hydrocarbons.
2. The process of claim 1 wherein said portion of gasification zone solids is introduced into said vaporous coking zone product passing into said gas-solids separation zone.
3. The process of claim 1 wherein said portion of gasification zone solids is introduced directly into said gas-solids separation zone.
4. The process of claim 1 wherein said coking zone is maintained at a temperature ranging from amount 850 to about 1,400°F.
5. The process of claim 1 wherein said gasifica-tion zone is maintained at a temperature ranging from about 1,500 to about 2,000°F.
6. The process of claim 1 wherein said coking zone and said gasification zone are each maintained at a pressure ranging from about 5 to about 150 psig.
7. The process of claim 1 wherein a sufficient amount of said solids is introduced into said gas-solids separation zone to convert at least 20 weight percent of the coking zone vaporous product to unsaturated hydrocarbons having less than 6 carbon atoms.
8. In an integrated coking and gasification process comprising the steps of:
(a) reacting a carbonaceous material having a Conradson carbon content of at least 10 weight percent in a coking zone containing a bed of fluidized solids maintained at a temperature ranging from about 850 to about 1,400°F.
to form a vaporous coking zone product and coke, said coke depositing on said fluidized solids;
(b) introducing a portion of said solids with the coke deposition thereon into a heating zone operated at a temperature greater than said coking zone temperature to heat said portion of solids;
(c) recycling a first portion of heated solids from said heating zone to said coking zone;
(d) introducing a second portion of heated solids to a fluid bed gasification zone maintained at a temperature ranging from about 1,500 to about 2,000°F.;
(e) reacting said portion of heated solids in said gasification zone with steam and an oxygen-containing gas to produce a hot gaseous stream containing hydrogen and carbon monoxide;
(f) introducing said hot gaseous stream and entrained solids into said heating zone;
(g) passing an additional stream of solids from said gasification zone to said heating zone, and (h) passing said vaporous coking zone conversion product with entrained solids to a gas-solids separation zone, the improvement which comprises passing a portion of solids from said gasification zone to said gas-solids separation zone in an amount sufficient to maintain said gas-solids separation zone at a temperature in the range of about 1200 to about 1700 degrees Fahrenheit, whereby at least a portion of said vaporous coking zone product is converted to unsaturated light hydrocarbons.
(a) reacting a carbonaceous material having a Conradson carbon content of at least 10 weight percent in a coking zone containing a bed of fluidized solids maintained at a temperature ranging from about 850 to about 1,400°F.
to form a vaporous coking zone product and coke, said coke depositing on said fluidized solids;
(b) introducing a portion of said solids with the coke deposition thereon into a heating zone operated at a temperature greater than said coking zone temperature to heat said portion of solids;
(c) recycling a first portion of heated solids from said heating zone to said coking zone;
(d) introducing a second portion of heated solids to a fluid bed gasification zone maintained at a temperature ranging from about 1,500 to about 2,000°F.;
(e) reacting said portion of heated solids in said gasification zone with steam and an oxygen-containing gas to produce a hot gaseous stream containing hydrogen and carbon monoxide;
(f) introducing said hot gaseous stream and entrained solids into said heating zone;
(g) passing an additional stream of solids from said gasification zone to said heating zone, and (h) passing said vaporous coking zone conversion product with entrained solids to a gas-solids separation zone, the improvement which comprises passing a portion of solids from said gasification zone to said gas-solids separation zone in an amount sufficient to maintain said gas-solids separation zone at a temperature in the range of about 1200 to about 1700 degrees Fahrenheit, whereby at least a portion of said vaporous coking zone product is converted to unsaturated light hydrocarbons.
9. The process of claim 8 wherein at least 20 weight percent of said vaporous coking zone product is converted to unsaturated hydrocarbons having less than 6 carbon atoms.
10. The process of claim 8 wherein said portion of solids from said gasification zone is passed to said gas-solids separation zone in an amount sufficient to maintain said gas-solids separation zone at a temperature in the range of about 1300 to about 1500 degrees Fahrenheit.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US78956977A | 1977-04-21 | 1977-04-21 | |
| US789,569 | 1977-04-21 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1126188A true CA1126188A (en) | 1982-06-22 |
Family
ID=25148020
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA293,001A Expired CA1126188A (en) | 1977-04-21 | 1977-12-13 | Two-stage integrated coking for chemicals and coke gasification process |
Country Status (2)
| Country | Link |
|---|---|
| JP (1) | JPS53132003A (en) |
| CA (1) | CA1126188A (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4325815A (en) * | 1980-09-02 | 1982-04-20 | Exxon Research & Engineering Co. | Catalytic fluid coking and gasification process |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5833278B2 (en) * | 1974-10-25 | 1983-07-19 | 株式会社日立製作所 | Calcination strengthening method for catalyst in fluidized bed catalytic cracking system |
| JPS51107282A (en) * | 1975-03-18 | 1976-09-22 | Chiyoda Chem Eng Construct Co | RYUSHIJUNKANGATARYUDOSONETSUBUNKAIHANNOSOCHINIOKERU ANZENSEIGYOHOHO |
-
1977
- 1977-12-13 CA CA293,001A patent/CA1126188A/en not_active Expired
-
1978
- 1978-04-17 JP JP4431578A patent/JPS53132003A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6323237B2 (en) | 1988-05-16 |
| JPS53132003A (en) | 1978-11-17 |
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