AU2023279401B2 - Method for producing hydrocarbons - Google Patents

Abstract

The method for producing hydrocarbons according to the present disclosure includes a step in which a feed oil is cracked by fluid catalytic cracking with a fluid catalytic cracker comprising a reaction column and a regeneration column, wherein the feed oil includes an FT synthesis oil and wherein the feed temperature x (unit: °C) of the feed oil, the feed rate y1 (unit: ton/h) of the feed oil, the feed rate y2 (unit: ton/h) of a fuel oil to be supplied to the regeneration column, and the circulation rate z1 (unit: ton/h) of a catalyst to be circulated through the reaction column and the regeneration column satisfy a specific inequality.

Description

METHOD FOR PRODUCING HYDROCARBONS Field of the Invention

[0001] The present disclosure relates to a method for producing a hydrocarbon. 5 Background of the Invention 2023279401

[0002] In domestic refineries in Japan, fluid catalytic cracking (FCC) units play a central role in the production of hydrocarbons (for example, Patent Literature 1).

[0003] FIG. 1 is a flow chart illustrating an example of a conventional 10 method for producing hydrocarbons from crude oil. In the conventional method for producing hydrocarbons, as shown in FIG. 1, for example, hydrocarbons are produced by using a desulfurized atmospheric residue and a desulfurized vacuum gas oil, which are obtained by treating an atmospheric residue in a residue desulfurization unit, as feedstocks and 15 treating the feedstocks in a fluid catalytic cracking unit.

[0004] Furthermore, as environmental awareness is increasing, attention has been paid to FT synthetic oil having lower sulfur content and nitrogen content as compared with petroleum. FT synthetic oil is produced by Fischer-Tropsch synthesis from synthesis gas, which is a gas mixture of 20 hydrogen gas and carbon monoxide gas. For example, Patent Literature 2 discloses a technology for producing hydrocarbons by treating the FT synthetic oil as a feedstock in a fluid catalytic cracking unit. Citation List Patent Literature 25

[0005] Patent Literature 1: Japanese Unexamined Patent Publication No. 2020-186384 Patent Literature 2: Japanese Unexamined Patent Publication No. 2007-503503 5 Summary of Invention 2023279401

[0006] Coke produced from feedstocks in the course of fluid catalytic cracking adheres to the surface of catalysts. The fluid catalytic cracking unit regenerates catalysts and also utilizes the coke as its own heat source by sending coke-attached catalysts to a regenerator and combusting coke 10 within the regenerator.

[0007] However, as a result of studies conducted by the inventors of the present invention, it was found that when FT synthetic oil is treated in a fluid catalytic cracking unit, the amount of coke produced during fluid catalytic cracking is small, and there is a possibility that the heat source of 15 the fluid catalytic cracking unit may be insufficient as compared to the case of treating oil derived from petroleum. That is, it is difficult to maintain the heat balance of the fluid catalytic cracking unit, and there is room for improvement from the viewpoint of stable operation of the fluid catalytic cracking unit. When a fluid catalytic cracking unit cannot 20 operate stably, the utilization rate of the fluid catalytic cracking unit decreases, which leads to an increase in the production cost for hydrocarbons.

[0008] Thus, an aspect of the present disclosure provides a method for producing a hydrocarbon, which method uses FT synthetic oil as a 25 feedstock and allows stable operation.

[0009] An aspect of the present disclosure relates to a method for producing a hydrocarbon, the method including a step of subjecting a feedstock to fluid catalytic cracking by using a fluid catalytic cracking unit including a reactor and a regenerator, in which the feedstock includes FT 5 synthetic oil, and a feed temperature x (unit: C) of the feedstock, a feed 2023279401

rate y1 (unit: ton/h) of the feedstock, a feed rate y2 (unit: ton/h) of a fuel oil to be fed into the regenerator, and a circulation rate z1 (unit: ton/h) of a catalyst circulating through the reactor and the regenerator, satisfy the following Inequality Expression (1).

10

y = (y2/y1)  100 z = (z1/y1)

[0010] According to an embodiment, the feedstock may further include a hydrocarbon oil having a higher %CA than the FT synthetic oil. According 15 to an embodiment, the hydrocarbon oil may include a desulfurized atmospheric residue.

[0011] According to an embodiment, the above-described method for producing a hydrocarbon may further include: a step of mixing FT synthetic oil and a hydrocarbon oil having a higher %CA than the FT 20 synthetic oil to obtain a feedstock; and a step of feeding the feedstock into the reactor of the fluid catalytic cracking unit. According to an embodiment, the hydrocarbon oil may include clarified oil.

[0012] According to an aspect of the present disclosure, there is provided

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a method a forproducing method for producing a hydrocarbon, a hydrocarbon, which which method method uses uses FT FT synthetic synthetic

oil as a feedstock and enables stable operation. oil as a feedstock and enables stable operation.

Brief Description Brief Description of ofDrawings Drawings

[0013] [FIG. 1]

[0013] [FIG. 1] FIG. FIG. 11isis a aflowchart flowchartillustrating illustrating an an example of aa example of

conventionalmethod conventional method forproducing for producing a hydrocarbon a hydrocarbon fromfrom crudecrude oil. oil.

[FIG. 2]

[FIG. 2] FIG. FIG.22isis aa schematic schematicview view illustratingananexample illustrating exampleof of a a fluid catalytic fluid catalytic cracking cracking unit unit used for aamethod used for method forfor producing producing a a hydrocarbonaccording hydrocarbon according to to anan embodiment. embodiment.

[FIG. 3] FIG. 3(a) is a graph plotting set values of x and y, while

[FIG. 3] FIG. 3(a) is a graph plotting set values of X x and y, while

plotting Xxx on plotting onthe theaxis axisofofabscissa abscissa andand y ony the on axis the axis of ordinate, of ordinate, for for Examplesand Examples and Comparative Comparative Examples Examples in which in which z isFIG. Z is 4. 4. FIG. 3(b) 3(b) is aisgraph a graph plotting set values of x and y, while plotting x on the axis of abscissa and plotting set values of X x and y, while plotting X x on the axis of abscissa and

y on y on the the axis axis of of ordinate, ordinate,forfor Examples Examplesand andComparative Comparative Examples in Examples in

whichZ zisis 8. which 8. FIG. FIG.3(c) 3(c)isisa agraph graphplotting plottingsetsetvalues valuesofofXx xandand y, y, while while

plotting Xxx on plotting onthe theaxis axisofofabscissa abscissa andand y ony the on axis the axis of ordinate, of ordinate, for for Examplesandand Examples Comparative Comparative Examples Examples in which in which z is Z is 12. 12. Description of Description of Embodiments Embodiments

[0014] Embodiments

[0014] Embodiments of the of the present present disclosure disclosure will will be described be described below below

with reference with referencetoto the the drawings. drawings.However, However, the present the present disclosure disclosure is is not not

limited to limited to the the following followingembodiments embodimentsand and is indicated is indicated by scope by the the scope of of claims, and claims, and it it is is intended intended that that all allchanges in the changes in the meaning andthethescope meaning and scope equivalent to equivalent to the the scope scope of of claims claims are are included. In each included. In each of of the the drawings, drawings, aa

portion of portion of the the configuration configuration may be shown may be shownininananexaggerated exaggeratedororsimplified simplified mannerfor manner forthe theconvenience convenienceof of explanation. explanation. In In addition, addition, thethe dimensional dimensional

ratio of ratio of each each part part may be different may be different inin each each of of the the drawings. In the drawings. In the followingdescription following descriptionofofthe the drawings, drawings,the thesame sameor or similar similar partsmaymay parts be be

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assigned with assigned withthe the same sameororsimilar similarreference referencenumerals. numerals.

[0015] Inthe

[0015] In the present presentspecification, specification, aa synthetic synthetic oil oil produced byFischer- produced by Fischer- Tropschsynthesis Tropsch synthesisisisreferred referredtotoasas"FT"FT synthetic synthetic oil". oil". In present In the the present specification, a wax component included in the FT synthetic oil is referred specification, a wax component included in the FT synthetic oil is referred

to as to as "FT "FT wax". Inthe wax". In the present present specification, specification, an an FT synthetic oil FT synthetic oil produced produced

by Fischer-Tropsch by Fischer-Tropschsynthesis synthesisandand notnot subjected subjected to to distillationisis referred distillation referred to as "FT crude oil". In the present specification, with regard to "ton", not to as "FT crude oil". In the present specification, with regard to "ton", not

the yard-pound the system yard-pound system butthethemetric but metricsystem system is is adopted. adopted. That That is, is, 1 tonisis 1 ton

1000 kg. 1000 kg.

[0016] Inthe

[0016] In the present present specification, specification,the theterm term%C meansanann-d-m %CAA means n-d-m method method

value (aromatic value (aromatic content). content). Specifically, Specifically, %C is calculated %CA Ais calculated by the following by the following

70 70 procedure. That is, the specific gravity (d4 ) and the refractive index (nd ) procedure. procedure.That Thatis, thethe is, specific gravity specific (d470)(d) gravity andand the the refractive index index refractive (nd 70) (nd)

of the of the feedstock feedstock at at 70C are measured. 70°C are isis measured. a is calculatedbybyby calculated calculated substitutingthe substituting substituting the the

measured values measured values into into the the following following Formula (a1). With Formula (al). Withregard regard to to the the

calculated calculated , calculateda,, aaa value valuedetermined value determined determined by substituting by by substituting substituting  into a into into the following following the following the

Formula(a2) Formula (a2)inina acase casewhere where a ismore is is more more than than 0, than 0,into 0, and and and the into into the following the following following

Formula (a3) in a case where  is less than 0, is the %C of the feedstock. Formula Formula(a3) (a3)inin a case where a case a is is where lessless thanthan 0, is0,the is%CA theof%CA the feedstock. Aof the feedstock.

Thefollowing The followingFormulas Formulas (al)(a1) to (a3) to (a3) are are defined defined with with reference reference to theto the standard "ASTM standard D3238". "ASTM D3238". In In Formulas Formulas (a2) (a2) andand (a3),M M (a3), representsthe represents the

averagemolecular average molecularweight. weight. ==2.42(nd 2.42(nd70- -1.4600) (d470 1.4600) -- (d - -0.8280)  (a1) 0.8280) (al) %C %CAA=== 410a %CA 410 3660/M  410 ++ 3660/M 3660/M (a2) (a2) (a2)

%C = - %CAA=== 720a %CA

[0017]

[0017] A 720 A method

embodimentwill embodiment 3660/M  720 ++ 3660/M 3660/M

method for (a3) (a3) (a3) for producing producing a ahydrocarbon willbebedescribed describedbelow. hydrocarbonaccording below.TheThe accordingtotoanan method method for producing for producing a a

hydrocarbonofofthethepresent hydrocarbon presentembodiment embodiment includes includes a of a step stepsubjecting of subjecting a a

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feedstock feedstock totofluid fluidcatalytic catalyticcracking crackingby by using using a fluid a fluid catalytic catalytic cracking cracking unit unit

including aa reactor including reactor and and aa regenerator. regenerator. The The feedstock feedstock includes includes FT synthetic FT synthetic

oil. The oil. feedtemperature The feed temperatureXx x(unit: C)ofofthe (unit:°C) thefeedstock, feedstock,the thefeed feedrate ratey1y1 (unit: ton/h) of the feedstock, the feed rate y2 (unit: ton/h) of the fuel oil (unit: ton/h) of the feedstock, the feed rate y2 (unit: ton/h) of the fuel oil

to be fed into the regenerator, and the circulation rate z1 (unit: ton/h) of to be fed into the regenerator, and the circulation rate zl (unit: ton/h) of

the catalyst circulating through the reactor and the regenerator, satisfy the the catalyst circulating through the reactor and the regenerator, satisfy the

following Inequality following Inequality Expression Expression(1). (1). The Thefollowing followingInequality InequalityExpression Expression (1) is derived based on the simulation results of the Examples that will be (1) is derived based on the simulation results of the Examples that will be

described below. described below. AAspecific specific method methodfor forderivation derivation will will be be described described

below. It has been revealed by the studies of the present inventors that in below. It has been revealed by the studies of the present inventors that in

the following the Inequality Expression following Inequality Expression(1), (1),factors factors other other than than y1, y1, y2, y2, and z1 and zl

do not do not affect affect stable stable operation operation of of the themethod for producing method for producing aahydrocarbon hydrocarbon according to the according to the present present embodiment. embodiment.

[0018]

[0018]

(1) (1)

y := y (y2/y1) xX 100 = (y2/y1) 100 zZ == (z1/y1) (z1/y1)

[0019] <Methodforfor producing FT synthetic oil>oil>

3

[0019] <Method producing FT synthetic

First, an outline of a method for producing FT synthetic oil that is First, an outline of a method for producing FT synthetic oil that is

used in used in the the method forproducing method for producinga ahydrocarbon hydrocarbon according according to the to the present present

embodiment embodiment will will be be described. described. FT synthetic FT synthetic oil oil is produced is produced by Fischer- by Fischer-

Tropschsynthesis, Tropsch synthesis, for for example, usingcarbon example, using carbonmonoxide monoxideandand hydrogen hydrogen gas gas as feedstocks. as The method feedstocks. The methodfor forproducing producingthe theFTFTsynthetic syntheticoil oil is is not not particularly limited, particularly limited,and and aaknown methodcancanbebe known method employed. employed. The The reaction reaction

unit for unit for producing the FT producing the FTsynthetic syntheticoil oil is is preferably a fixed preferably a fixed bed reaction bed reaction

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unit or a slurry fluidized bed reaction unit. In addition, it is preferable to unit or a slurry fluidized bed reaction unit. In addition, it is preferable to

performthe perform thereaction reaction under underthe theconditions conditionsininwhich whichthe theconversion conversion rateofof rate

carbonmonoxide, carbon monoxide, which which is is a a feedstock,isisset feedstock, set to to be be 50% or more, 50% or more,and andeven even morepreferably more preferablyininthe the range rangeof of 70 70 to to 90%. 90%.

[0020] Asthe

[0020] As theslurry slurryfluidized fluidized bed bedreaction reactionunit, unit, for for example, example, aa bubbling bubbling columntype column typefluidized fluidizedbed bedreaction reactionunit unitcan canbebeused. used.A A bubbling bubbling column column

type fluidized type fluidized bed bedreaction reactionunit unit hashas a reactor a reactor thatthat performs performs Fischer- Fischer-

Tropsch synthesis. Tropsch synthesis. Inside Inside the the reactor reactor of of the the bubbling bubbling column columntype type fluidized bed fluidized bed reaction reactionunit, unit,liquid liquidhydrocarbons hydrocarbonsthatthat are are liquid liquid at the at the

reaction temperature reaction temperatureare areaccommodated. accommodated. A catalyst A catalyst forsynthesis for FT FT synthesis is is dispersed in dispersed in the the liquid liquid hydrocarbons, and the hydrocarbons, and the liquid liquid hydrocarbons areinin aa hydrocarbons are

slurry state. slurry state. Synthesis gas, which Synthesis gas, whichisisaagas gasmixture mixtureofofcarbon carbon monoxide monoxide

gas and gas and hydrogen hydrogengas, gas,isis introduced introducedinto into the the liquid liquid hydrocarbons fromthe hydrocarbons from the lower part lower partofofthe thereactor. reactor.TheThe synthesis synthesis gas dissolves gas dissolves in thein the liquid liquid

hydrocarbons while hydrocarbons while rising rising in in the the liquid liquid hydrocarbons hydrocarbons after after becoming becoming

bubbles, and bubbles, andcomes comes intocontact into contactwith with thethe catalystfor catalyst forFTFT synthesis.TheThe synthesis.

FTsynthetic FT synthetic oil oil is is produced fromthe produced from thesynthesis synthesisgas gasby bythe thefunction functionofof the the catalyst for FT synthesis. catalyst for FT synthesis.

[0021] The reaction

[0021] The reaction temperature temperature can be determined can be determined depending dependingononthe the

target carbon target monoxide conversion carbon monoxide conversion rate; rate; however, however, the the reaction reaction temperature is temperature is preferably preferably 150 150 to to 300C, and more 300°C, and morepreferably preferably 170 170toto 250C. 250°C.

[0022] The reaction

[0022] The reaction pressure pressure is is preferably preferably0.5 0.5toto5.0 MPa, 5.0 MPa,and and more more

preferably 2.0 preferably 2.0 to to 4.0 4.0MPa. Whenthethereaction MPa. When reactionpressure pressureisis 0.5 0.5 MPa ormore, MPa or more,

there is there is aa tendency that the tendency that the carbon monoxide carbon monoxide conversion conversion rate rate is is likelytoto likely

be 50% be 50%ororhigher, higher,and andwhen when thereaction the reactionpressure pressureisis5.0 5.0 MPa MPaororless, less,there there

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is aa tendency is tendency that that the the occurrence occurrence ofoflocal local heat heatgeneration generationcan canbebe suppressed. suppressed.

[0023] Synthesis gas

[0023] Synthesis gas isis obtained obtainedby,by,forfor example, example, reforming reforming of of hydrocarbonssuch hydrocarbons such as as natural natural gas. gas. Synthesis Synthesis gas gas only only needsneeds to include to include

carbonmonoxide carbon monoxidegasgas andand hydrogen hydrogen gas gas and and may may be be aother a gas gas other than than a gasa gas obtained by reforming of natural gas or the like. obtained by reforming of natural gas or the like.

[0024] The

[0024] Thehydrogen/carbon hydrogen/carbon monoxide monoxide ratioratio (molar (molar ratio) ratio) in the in the synthesis synthesis

gas is gas is preferably 0.5 to preferably 0.5 to 4.0, 4.0, and morepreferably and more preferably1.0 1.0toto2.5. 2.5.When When thisthis

molar ratio is 0.5 or higher, the reaction temperature does not increase too molar ratio is 0.5 or higher, the reaction temperature does not increase too

high while high whiledeactivation deactivationofofthe the catalyst catalyst tends tends to to be suppressed, and be suppressed, andwhen when the molar the molarratio ratio isis 4.0 4.0 ororlower, lower,there thereisisa atendency tendency that that production production of of methane,which methane, whichisisananundesirable undesirablebyproduct, byproduct, can can be be suppressed. suppressed.

[0025] Thegas

[0025] The gasspace space velocity velocity of of thethe synthesis synthesis gasgas is is preferably preferably 500500 to to

5000 h-1, and and more more 5000 h-superscript(1), 5000 h¹, preferably 10001000 to to 2500 2500h¹. h-1. When When and more preferably 1000 to 2500 h-superscript(1). preferably thisgasgasspace space When this gas space this

-1 or more,

velocity is 500 h or more, higher productivity is obtained with the same velocity velocity is is 500 500 h-superscript(1) h-¹ or more, higher higher productivity is productivity isobtained with with obtained same the same the

amount of catalyst, and when the gas space velocity is 5000 h or less, amount amountofof catalyst, and when catalyst, andthe gas space when velocity the gas is 5000 space h-superscript(1) velocity is 5000 or or-1less, h¹ less,

there is there is aa tendency that the tendency that the conversion rate of conversion rate of carbon monoxide carbon monoxide is is likely likely

to be to be 50% orhigher. 50% or higher.

[0026]

[0026] AsAs thethe catalyst catalyst forfor FT FT synthesis, synthesis, a catalyst a catalyst in which in which an active an active metal metal

is supported is onananinorganic supported on inorganiccarrier carrierisis used. used. Examples Examples of the of the inorganic inorganic

carrier include carrier include porous oxidessuch porous oxides suchasassilica, silica, alumina, alumina,titania, titania, magnesia, magnesia, and zirconia. and zirconia. Examples Examples of the of the active active metal metal include include cobalt, cobalt, ruthenium, ruthenium,

iron, and iron, nickel. Furthermore, and nickel. Furthermore,in inthethecatalyst, catalyst,a acompound compound including including a a metal element metal elementsuch suchasaszirconium, zirconium, titanium, titanium, hafnium, hafnium, sodium, sodium, lithium, lithium, or or

magnesiummay magnesium may alsobebe also supported,ininaddition supported, addition to to the the above-described above-described active metals. active These components metals. These componentsimprove improve thethe catalyticactivity catalytic activity and and

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contribute to contribute to the control of the control the number of the numberofofcarbon carbon atoms atoms and and the the distribution thereof in the FT synthetic oil. distribution thereof in the FT synthetic oil.

[0027] TheFTFT

[0027] The syntheticoil synthetic oilis, is, for for example, example, aa mixture of straight-chained mixture of straight-chained hydrocarbons(normal hydrocarbons (normal paraffins) paraffins) having having 5 to 5 to 100100 carbon carbon atoms. atoms. The The FT FT

synthetic synthetic oil oilmay may be be aa synthetic syntheticoil oilproduced produced by by Fischer-Tropsch synthesis Fischer-Tropsch synthesis

and may and mayinclude includestraight-chained straight-chained hydrocarbons hydrocarbons having more than having more than 100 100 carbon atoms. carbon atoms. The TheFTFTsynthetic syntheticoil oil includes includes almost almost none of aromatic none of aromatic hydrocarbons,naphthene, hydrocarbons, naphthene,andand isoparaffin. isoparaffin. TheThe FT synthetic FT synthetic oil has, oil has, for for example,aa%CA example, %Cof A of 0. 0. Incidentally,the Incidentally, theFTFT syntheticoiloilmay synthetic may have have a %CA a %CA

of more of than0,0,for more than for example, example,inina acase casewhere where aromatic aromatic hydrocarbons hydrocarbons are are included. included.

[0028] TheFTFTsynthetic

[0028] The syntheticoil oilmay mayinclude includeananFTFT wax wax having having a boiling a boiling point point

of higher of higher than than 330C. The 330°C. The FTFT waxwax is, is, forfor example, example, a mixture a mixture of straight- of straight-

chainedhydrocarbons chained hydrocarbons (normal (normal paraffins)having paraffins) having 17 17 or or more more carbon carbon atoms. atoms.

Thepercentage The percentagecontent contentofofthe theFTFTwax waxin in theFTFT the syntheticoil synthetic oilmay maybebe 30% 30%

by mass by mass or or more, more, 50% bymass 50% by massoror more, more, 70% 70%bybymass massorormore, more,90% 90%byby

mass or mass or more, more, or or 95% by mass 95% by or more mass or and may more and be 100% may be 100%bybymass. mass.The The percentagecontent percentage contentofofthe theFTFT waxwax in the in the FT synthetic FT synthetic oil can oil can be easily be easily

controlled by controlled appropriately adjusting by appropriately adjusting the the above-described above-describedreaction reaction

conditions. conditions.

[0029] <Methodfor

[0029] <Method for producing producing hydrocarbon> hydrocarbon> Next, an Next, an outline outline of of the the method methodfor for producing producinga ahydrocarbon hydrocarbon according to according to the the present presentembodiment embodiment will will be be described. described. Hydrocarbons Hydrocarbons

can be can be produced producedbyby treatinga feedstock treating a feedstock including including FT synthetic FT synthetic oil ain oil in a

fluid catalytic cracking unit. fluid catalytic cracking unit.

[0030] The %CA

[0030] The %CAofofthe thefeedstock feedstock may maybe, be, for for example, example, 0, 0, may be 11 or may be or

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more,may more, maybebe5 5orormore, more,may maybebe 6 6 orormore, more,orormay maybebe 7 7 oror more.TheThe more. %CA%CA

of the feedstock may be 23 or less, may be 22 or less, or may be 21 or less. of the feedstock may be 23 or less, may be 22 or less, or may be 21 or less.

[0031] The FT

[0031] The FTsynthetic synthetic oil oil included included in in the the feedstock feedstock may be an may be an oil oil producedbybyFischer-Tropsch produced Fischer-Tropsch synthesis synthesis andnotis particularly and is not particularly limited. limited.

TheFT The FTsynthetic syntheticoil oil included included in in the the feedstock feedstock may be, for may be, for example, anFT example, an FT crude oil, crude oil, may be an may be an oil oil obtained obtained by distilling FT by distilling FT crude crude oil, oil,may may be be an an FT FT

wax,or wax, or may maybebea amixture mixtureofofthese. these.

[0032] The feedstock

[0032] The feedstock may mayfurther further include include aa hydrocarbon oil having hydrocarbon oil a having a

higher %C than the FT synthetic oil. In this case, in the step of treating higher %CA than A the FT synthetic oil. In this case, in the step of treating

the feedstock the byusing feedstock by usingaafluid fluid catalytic catalytic cracking unit, the cracking unit, the feedstock may feedstock may

be obtained be obtainedby bymixing mixingthetheFTFT synthetic synthetic oiland oil anda ahydrocarbon hydrocarbon oil oil having having

a higher %C than the FT synthetic oil before the feedstock is fed into the a higher %CA than A the FT synthetic oil before the feedstock is fed into the

reactor of the fluid catalytic cracking unit. As the FT synthetic oil and the reactor of the fluid catalytic cracking unit. As the FT synthetic oil and the

hydrocarbonoiloilare hydrocarbon aremixed mixed before before thethe feedstock feedstock is is fedfed intothethereactor into reactorofof

the fluid catalytic cracking unit, the oil constituting the feedstock becomes the fluid catalytic cracking unit, the oil constituting the feedstock becomes

moreuniform more uniformasascompared compared to the to the case case where where the the FT synthetic FT synthetic oil oil and and the the

hydrocarbonoiloilare hydrocarbon aremixed mixedin in thethe reactor.Therefore, reactor. Therefore, the the fluid fluid catalytic catalytic

cracking reaction cracking reaction in in thethe reactor reactor tends tends tomore to be be more stable. stable.

[0033] The above-described

[0033] The above-describedhydrocarbon hydrocarbonoiloilis isobtained obtained from, from, for for

example, refining. example, refining. Examples Examplesofofthe theabove-described above-describedhydrocarbon hydrocarbonoil oil include RDS-BTM, include DS-VGO, RDS-BTM, DS-VGO, and and CLO. CLO. As shown As shown in FIG. in FIG. 1, RDS-BTM 1, RDS-BTM

is aadesulfurized is desulfurized atmospheric residue obtained atmospheric residue obtainedby bytreating treating an an atmospheric atmospheric residue in residue in aa residue residuedesulfurization desulfurizationunit. unit.TheThe atmospheric atmospheric residue residue is is obtained bybytreating obtained treatingcrude crudeoiloilininanan atmospheric atmospheric distillation distillation unit. unit. As As

shownininFIG. shown FIG.1,1,DS-VGO DS-VGOis, is, forfor example, example, a desulfurized a desulfurized vacuum vacuum gas gas oil oil obtained by treating obtained by treating an an atmospheric atmosphericresidue residueinina avacuum vacuum gas oil gas oil

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desulfurization unit. desulfurization unit. RDS-BTM RDS-BTM maymay or not or may mayinclude not include a solvent a solvent

deasphaltedvacuum deasphalted vacuum residual residual oilasasaafeedstock oil feedstockthereof. thereof. As Asshown shownin in FIG. FIG.

1, 1, CLO (CLarifiedOil) CLO (CLarified Oil)is, is, for for example, example, aa product product obtained obtainedbybyremoving removinga a

catalyst from a slurry oil, which is a residual oil obtained by treating RDS- catalyst from a slurry oil, which is a residual oil obtained by treating RDS-

BTM BTM or or DS-VGO DS-VGO in a fluid in a fluid catalytic catalytic cracking cracking unit unit to to obtain obtain an oilanand oil and further treating further treating the theobtained obtained oil oilininan anatmospheric atmospheric distillation distillationunit. unit.CLO CLO

mayorormay may maynotnotinclude includeFTFT synthetic synthetic oilasasa afeedstock oil feedstockthereof. thereof.

[0034] Inaa case

[0034] In case where wherethe thefeedstock feedstockincludes includesRDS-BTM, RDS-BTM, the proportion the proportion

occupied occupied by by RDS-BTM RDS-BTM in in RDS-BTM RDS-BTM andsynthetic and FT FT synthetic oil oil isis1% 1%byby mass mass

or more or basedononthethetotal more based totalmass massofofRDS-BTM RDS-BTM and FTand FT synthetic synthetic oil, oil, and and the proportion the proportion may may be be 15% bymass 15% by massorormore, more,may maybebe30% 30% by by mass mass or or more, or more, or may may be be 45% by mass 45% by mass or or more. more.

[0035]

[0035] The The proportion proportionoccupied by by occupied RDS-BTM RDS-BTM in in RDS-BTM andFTFT RDS-BTM and

synthetic synthetic oil oilisis98% 98% by by mass or less mass or less based based on on the the total totalmass mass of of RDS-BTM RDS-BTM

and FT and FTsynthetic syntheticoil, oil, and and the the proportion proportionmay maybebe75%75% by mass by mass or less, or less, or or maybebe50% may 50%by by mass mass or less. or less.

[0036] The %CA

[0036] The %CAofofRDS-BTM RDS-BTMis 5isor5 more or more andand may may be or be 10 10 more, or more, or or

maybe may be 20 20 or or more. The %CA more. The %CAofofRDS-BTM RDS-BTM is or is 99 99 less or lessand andmay maybebe 8080

or less, or may be 60 or less. or less, or may be 60 or less.

[0037] Inaacase

[0037] In casewhere wherethethefeedstock feedstock includes includes DS-VGO, DS-VGO, the proportion the proportion

occupied by occupied by DS-VGO DS-VGO ininDS-VGO DS-VGOand and FT synthetic FT synthetic oiloil isis1% 1%bybymass massoror morebased more basedonon thetotal the totalmass massof of DS-VGO DS-VGO and FTand FT synthetic synthetic oil,theand oil, and the proportion may proportion may be be 15% by mass 15% by massor or more, more, may maybe be 30% 30%bybymass massorormore, more, or may or may be be 45% by mass 45% by massor or more. more.

[0038]

[0038] The The proportion proportionoccupied occupiedbyby DS-VGO DS-VGO inin DS-VGO DS-VGOand and FT FT

synthetic oil synthetic oil is is98% by mass 98% by massororless less based basedononthe thetotal total mass massofofDS-VGO DS-VGO

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and FT and FTsynthetic syntheticoil, oil, and and the the proportion proportionmay maybe be 75%75% by mass by mass or less or less or or maybebe50% may 50%by by mass mass or less. or less.

[0039] The %CA

[0039] The %CAofofDS-VGO DS-VGOis,is, forforexample, example,11 or or more and may more and maybe be 55 or or more, or more, or may may be be 10 10 or ormore. more. The The %C of DS-VGO %CAA of DS-VGO isis99 99oror less less and and may may

be 80 or less, or may be 60 or less. be 80 or less, or may be 60 or less.

[0040] In

[0040] In aa case case where wherethe thefeedstock feedstockincludes includes CLO, CLO,thethe proportion proportion

occupied by occupied by CLO CLOininCLO CLOandand FT FT synthetic synthetic oilisis 1% oil 1%bybymass massorormore more based on based onthe thetotal total mass ofCLO mass of CLOandand FT FT synthetic synthetic oil,oil, andand thethe proportion proportion

maybe may be 15% 15%bybymass massorormore, more,may maybebe30% 30%by by mass mass or or more, more, orormay maybebe

45%bybymass 45% massoror more. more.

[0041] Theproportion

[0041] The proportionoccupied occupied by by CLO CLO inand in CLO CLOFT and FT synthetic synthetic oil is oil is

98%bybymass 98% massor or lessbased less basedononthethetotal totalmass massofofCLO CLOandand FT FT synthetic synthetic oil,oil,

and the and the proportion proportionmay may be be 75% 75% by by mass or less mass or lessorormay maybe be50% 50% by by mass mass

or less. or less.

[0042] The%CA

[0042] The %CofA of CLOCLO is, for is, for example, example, 1 or 1 or more more and and may may be 5 be or 5more, or more, maybebe1010orormore, may more,orormay maybe be 20 20 or or more. more. TheThe %CA %C A ofis of CLO CLO is 99 99 or or less less and may and maybebe8080ororless, less, or or may maybebe6060ororless. less.

[0043]

[0043] RDS-BTM, DS-VGO, RDS-BTM, DS-VGO, andCLO and CLO maymay be be used used inincombination combination of of two or two or more morekinds kindssuch suchthat thatthe the%CA %CofA of thethe feedstock feedstock is is within within therange the range

of the of the above-mentioned upper above-mentioned upper limitvalue limit valueandand lower lower limitvalue. limit value.

[0044] Thefluid

[0044] The fluidcatalytic catalytic cracking crackingunit unitused usedfor forfluid fluid catalytic catalytic cracking cracking

of the feedstock is not particularly limited. Regarding the fluid catalytic of the feedstock is not particularly limited. Regarding the fluid catalytic

cracking unit, a known fluid catalytic cracking unit can be used. FIG. 2 is cracking unit, a known fluid catalytic cracking unit can be used. FIG. 2 is

a schematic a schematicview viewillustrating illustratingananexample exampleof of thethe fluid fluid catalyticcracking catalytic cracking

unit used unit for the used for the method methodforforproducing producing a hydrocarbon a hydrocarbon according according to theto the present embodiment. present embodiment. A fluid A fluid catalyticcracking catalytic cracking unitA A unit includes:a areactor includes: reactor

12

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1; a regenerator 1; a regenerator3;3;a aline line1515 connecting connecting to reactor to the the reactor 1; a 17line 17 1; a line

connectingtotothe connecting the regenerator; regenerator; aa line line 11 11 connecting connectingthe thereactor reactor11and andthe the regenerator 3; regenerator 3; aa line line 23 23 connecting the reactor connecting the reactor 11 and andthe the regenerator regenerator3;3; aa line 27 line 27 connecting the regenerator connecting the regenerator 33 and a boiler and a boiler (not (not shown in the shown in the

drawing); a line 29 connecting the reactor 1 and a recovery unit (not shown drawing); a line 29 connecting the reactor 1 and a recovery unit (not shown

in the in the drawing); drawing); and a heating and a heating unit unit (not (not shown in the shown in the drawing) for heating drawing) for heating the reactor. the reactor.

[0045] The reactor 1 is a riser type. The reactor 1 includes a reaction zone

[0045] The reactor 1 is a riser type. The reactor 1 includes a reaction zone

55 and andaaseparation separationzone zone 7. 7. The The reactor reactor 1 is 1fed is with fed with a feedstock a feedstock and and

innumerablecatalyst innumerable catalystparticles particles (cracking (crackingcatalyst). catalyst). The Thefeedstock feedstock is is fedfed

into the reaction zone 5 through the line 15. In a case where the feedstock into the reaction zone 5 through the line 15. In a case where the feedstock

further includes further includesa ahydrocarbon hydrocarbon oil oilhaving having aa higher higher %C than the %CAA than the FT FT synthetic oil, synthetic oil, the thefeedstock feedstock may beobtained may be obtainedbybymixing mixing thethe FT FT synthetic synthetic

oil and oil and the the hydrocarbon oilininthe hydrocarbon oil the line line 15. 15. InInthis this case, case, the the line line 15 may 15 may

branchoff branch off from fromthe themiddle. middle.ByBy feeding feeding thethe FT FT synthetic synthetic oiloil through through oneone

branchedline branched lineof of the the line line 15 and feeding 15 and feedingthe thehydrocarbon hydrocarbonoiloil through through thethe

other line, other line, the the FT FT synthetic synthetic oil oil and and the the hydrocarbon oilare hydrocarbon oil are mixed mixedatatthe the confluence of confluence of the thebranched branchedlines, lines,andand thethe feedstock feedstock is obtained. is obtained.

Furthermore,inin aa case Furthermore, case where the feedstock where the feedstockfurther further includes includes aa hydrocarbon hydrocarbon

oil having oil a higher having a %CAthan higher %CA thanthetheFTFT synthetic synthetic oil,a amixture oil, mixtureobtained obtained byby

mixingthe mixing theFT FTsynthetic syntheticoil oil and and the the hydrocarbon oil in hydrocarbon oil in advance maybebefed advance may fed as the feedstock to the reaction zone 5 through the line 15. as the feedstock to the reaction zone 5 through the line 15.

[0046] The

[0046] The catalyst catalyst particles particles are are fed fed intointo the reaction the reaction zone 5zone 5 through through the the line 11. line In the 11. In the reaction reactionzone zone5,5,a afluidizing fluidizinggas gas13, 13,which which is is steam, steam, is is

blownfrom blown fromthe thelower lowerpart partofofaalayer layer formed formedofofthe thecatalyst catalyst particles. particles. The The

catalyst particles are fluidized by the fluidizing gas 13. The feedstock and catalyst particles are fluidized by the fluidizing gas 13. The feedstock and

13

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the fluidized the fluidized catalyst catalyst particles particles move moveup up through through the reaction the reaction zone 5zone 5 together with together with the the fluidizing fluidizinggas gas13. 13. When the feedstock When the feedstock comes comesinto into contact with the catalyst particles in the reaction zone 5, catalytic cracking contact with the catalyst particles in the reaction zone 5, catalytic cracking

occurs, occurs, and occurs, and hydrocarbons andhydrocarbons hydrocarbons are are produced produced are from from produced the the from the feedstock. feedstock. The feedstock. The The

hydrocarbonsobtained hydrocarbons obtainedbybycracking cracking thefeedstock the feedstock and and thecatalyst the catalystparticles particles used for catalytic cracking are separated in the separation zone 7. used for catalytic cracking are separated in the separation zone 7.

[0047] The

[0047] Theseparated separatedhydrocarbons hydrocarbons areare fedfed into into therecovery the recovery unitthrough unit through the line the line29. 29. The The hydrocarbons areseparated hydrocarbons are separatedinto into aa plurality pluralityofofcomponents components

and recovered and recoveredininthe therecovery recoveryunit. unit.TheThe recovery recovery unitunit may may include, include, for for

example,a aplurality example, pluralityof ofdistillation distillationcolumns, columns, absorbers, absorbers, compressors, compressors,

strippers, fractionators, strippers, fractionators,splitters, andand splitters, heatheat exchangers. The exchangers. Thehydrocarbons hydrocarbons

are fractionated are fractionated into, into,for forexample, example,gas gascomponents andhydrocarbon components and hydrocarbonoiloil inin

the distillation the distillation column column (atmospheric distillation column). (atmospheric distillation The gas column). The gas components include components include dry dry gas gas and and LP gas (LPG). LP gas (LPG). Examples Examplesofofthe the

hydrocarbonoiloilinclude hydrocarbon include a gasoline a gasoline fraction fraction (CCG), (CCG), a gas aoil gasfraction oil fraction (LCO), (LCO), aakerosene kerosenefraction, fraction,clarified clarified oil oil(CLO), (CLO), and coke. The and coke. Therecovered recovered clarified oil (CLO) may be fed into the reactor 1 as a feedstock. clarified oil (CLO) may be fed into the reactor 1 as a feedstock.

[0048] Theseparated

[0048] The separated catalyst catalyst particlesareare particles fedfed into into the the regenerator regenerator 3 3 throughthe through the line line 23. Cokegenerated 23. Coke generatedduring during catalyticcracking catalytic crackingisisattached attached

to the surface of the catalyst particles fed into the regenerator 3, and the to the surface of the catalyst particles fed into the regenerator 3, and the

catalyst particles have deteriorated catalytic activity. In the regenerator 3, catalyst particles have deteriorated catalytic activity. In the regenerator 3,

the catalyst particles used for catalytic cracking are regenerated. Air 25 is the catalyst particles used for catalytic cracking are regenerated. Air 25 is

supplied toto the supplied theregenerator regenerator3 for 3 for the the regeneration regeneration treatment. treatment. In the In the regenerator 3,3, bybycombusting regenerator combusting the the cokecoke attached attached to thetosurface the surface of the of the

catalyst particles, the amount of coke attached to the surface of the catalyst catalyst particles, the amount of coke attached to the surface of the catalyst

particles is reduced, and at the same time, the temperature of the catalyst particles is reduced, and at the same time, the temperature of the catalyst

14

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particles is increased. The catalyst particles after regeneration are fed into particles is increased. The catalyst particles after regeneration are fed into

the reaction zone 5 again through the line 11. That is, the catalyst particles the reaction zone 5 again through the line 11. That is, the catalyst particles

circulate between circulate the regenerator between the regenerator33and andthe thereactor reactor1.1.High-temperature High-temperature carbonmonoxide carbon monoxidegasgas andand carbon carbon dioxide dioxide gas generated gas generated in theincourse the course of of

the regeneration the regenerationtreatment treatmentarearesupplied supplied to,to, forfor example, example, a boiler a boiler (not (not

shownininthe shown thedrawing) drawing)or or a heat a heat exchanger exchanger (not(not shown shown in theindrawing) the drawing) throughthe through the line line 27. In aa case 27. In case where the carbon where the carbonmonoxide monoxidegasgas andand carbon carbon

dioxide gas dioxide gasgenerated generatedin in thethe course course of the of the regeneration regeneration treatment treatment are are supplied toto aaheat supplied heatexchanger, exchanger, forfor example, example, the gases the gases are utilized are utilized for for

increasing the temperature increasing the of the temperature of the feedstock. feedstock.

[0049]

[0049] A A fuel fuel oiloil is is fed fed into into thethe regenerator regenerator 3 through 3 through the17. the line line As 17. the As the

fuel oil fed fuel oil fed into intothe theregenerator regenerator 3 combusted 3 is is combusted in thein the regenerator regenerator 3, heat 3, heat

is generated. is Theheat generated. The heatgenerated generatedbybycombustion combustion of the of the fuel fuel oiloil isisutilized utilized for increasing the temperature of the catalyst particles in the regenerator for increasing the temperature of the catalyst particles in the regenerator

3. The 3. Thecatalyst catalystparticles particles heated heatedbybythethefuel fueloil oilcan cansuppress, suppress,when when fed fed

again into again into the thereaction reactionzone zone 5, 5, a decrease a decrease in temperature in the the temperature of the of the feedstock as compared feedstock as comparedto to thethe case case where where the catalyst the catalyst particles particles are not are not

heated by the fuel oil. heated by the fuel oil.

[0050] Asthethefuel

[0050] As fueloiloilfedfedinto intothetheregenerator regenerator 3 combusted 3 is is combusted in thein the

regenerator 3, regenerator 3, high-temperature carbonmonoxide high-temperature carbon monoxide gas, gas, carbon carbon dioxide dioxide gas, gas,

and the and the like like are are also also generated. Thehigh-temperature generated. The high-temperature carbon carbon monoxide monoxide

gas, carbon gas, dioxidegas, carbon dioxide gas, and andthe the like like generated by combustion generated by combustionof of thefuel the fuel oil are fed into, for example, a boiler (not shown in the drawing) or a heat oil are fed into, for example, a boiler (not shown in the drawing) or a heat

exchanger(not exchanger (notshown shownin in thethe diagram) diagram) through through the the lineline 27 and 27 and serves serves as as

one of one of heat heat sources sources for for the the fluid fluid catalytic catalyticcracking cracking unit. unit. In In aa case case where where

the carbon the monoxide carbon monoxide gasgas andand carbon carbon dioxide dioxide gas gas generated generated in course in the the course

15

FP23-0372-00 FP23-0372-00

of the of the regeneration regeneration treatment treatment are are supplied supplied to to a heat exchanger, a heat exchanger, for for example,the example, thegases gases areare utilized utilized forfor increasing increasing the the temperature temperature of of the the feedstock. feedstock.

[0051] Therefore,not

[0051] Therefore, notonly onlythe thecoke coke attached attached to to thecatalyst the catalystfed fedinto intothe the

regenerator 33through regenerator through thethe line line 23 also 23 but but also the oil the fuel fuelfed oilinto fedthe into the regenerator 3 through the line 17 may be heat sources for the fluid catalytic regenerator 3 through the line 17 may be heat sources for the fluid catalytic

cracking unit A. Accordingly, by feeding the fuel oil to the regenerator 3, cracking unit A. Accordingly, by feeding the fuel oil to the regenerator 3,

the number the numberof of heat heat sources sources for for the fluid the fluid catalytic catalytic cracking cracking unit unit A is A is increased as increased as compared comparedto to thethe case case where where onlyonly the coke the coke attached attached to theto the

catalyst fed into the regenerator 3 through the line 23 is combusted inside catalyst fed into the regenerator 3 through the line 23 is combusted inside

the regenerator the regenerator3.3.Since Since the fluid the fluid catalytic catalytic cracking cracking reaction reaction is an is an endothermic reaction, it is easier to maintain the heat balance of the fluid endothermic endothermic reaction, reaction, it it is is easier easier to to maintain maintain the the heat heat balance balance of of the the fluid fluid

catalytic cracking catalytic unitA,A,andand cracking unit stable stable operation operation of fluid of the the fluid catalytic catalytic

cracking unit cracking unit A can be A can be more moreeasily easilyrealized. realized.

[0052] The

[0052] The feed feed raterate y1the y1 of of feedstock the feedstock is the is theofrate rate the of the feedstock feedstock to be to be fed into fed into the the reaction reaction zone 5 through zone 5 throughthe the line line 15. 15. The Thefeed feedrate ratey1y1ofofthe the feedstock is, feedstock is, for for example, 0.1[ton/h] example, 0.1 [ton/h]orormore moreandand maymay be 1be 1 [ton/h]

[ton/h] or or more,or more, or may maybebe1010[ton/h]

[ton/h]orormore. more.TheThe feed feed rate rate y1 y1 of of thethefeedstock feedstock is,is,

for example, for 3000[ton/h] example, 3000 [ton/h]oror less less and maybebe2000 and may 2000 [ton/h]ororless,

[ton/h] less, or or may may

be 1000 [ton/h] or less. be 1000 [ton/h] or less.

[0053] Thefeed

[0053] The feedtemperature temperature X x of x of thethe feedstock feedstock is is thetemperature the temperature of of thethe

feedstock feedstock atatthe thetime timewhen when the the feedstock feedstock is fedisinto fed the intoreactor the reactor 1. The1.feed The feed temperatureXxxofofthe temperature the feedstock feedstockis, is, for for example, 150Cororhigher example, 150°C higherandand maymay

be 200°C be 200Cororhigher, higher,orormay maybebe 250C 250°C or higher. or higher. The The feed feed temperature temperature X x x

of the of the feedstock feedstock is, is, for for example, 450C example, 450°C or or lower lower andand may may be 400C be 400°C or or lower, or lower, or may be350°C may be 350Coror lower. lower.

16

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[0054] Thefuel

[0054] The fueloil oiltotobebefedfedinto intothetheregenerator regenerator 3 is 3 is notnot particularly particularly

limited as long as it is an oil that can be combusted in the regenerator 3. limited as long as it is an oil that can be combusted in the regenerator 3.

Examplesof of Examples thethe fuel fuel oiloil to to be be fed fed intointo the the regenerator regenerator 3 include 3 include FT FT synthetic syntheticoil, oil,RDS-BTM, RDS-BTM, DS-VGO, andCLO. DS-VGO, and CLO.

[0055] The

[0055] The value value y obtained y obtained by dividing by dividing the feedthe feed rate ratethey2fuel y2 of of the oil fuel to oil to be fed be fed into into the the regenerator regenerator3 3bybythethefeed feed rate rate y1 y1 of of thethe feedstock feedstock and and multiplyingthe multiplying the resultant resultant by by 100, 100, is, is,for forexample, example, 0.1 0.1 or ormore more and maybebe and may

1.5 1.5 or or more, or may more, or be3 3orormore. may be more.y is, y is,for forexample, example,1010 or or lessand less andmaymay be 8 or less, or may be 6 or less. be 8 or less, or may be 6 or less.

[0056]

[0056] A A value value obtained obtained by dividing by dividing the circulation the circulation z1 rate rate zl z1catalyst of the of the catalyst circulating between the reactor 1 and the regenerator 3 by the feed rate y1 circulating between the reactor 1 and the regenerator 3 by the feed rate y1

of the of the feedstock feedstockisisa acatalyst/oil catalyst/oil ratio ratio (z). (z). The Thecatalyst/oil catalyst/oilratio ratioisis3 3

[mass/mass] or more

[mass/mass] or moreand andmay maybe be 4 [mass/mass] 4 [mass/mass] or more, or more, may may be 5 be 5

[mass/mass] ormore,

[mass/mass] or more,orormay maybebe7.5 7.5[mass/mass]

[mass/mass]or or more. more. TheThe catalyst/oil catalyst/oil

ratio isis5050[mass/mass] ratio [mass/mass] or or less lessand and may be 13 may be 13 [mass/mass]

[mass/mass]ororless, less, may maybebe 12 [mass/mass]ororless, 12 [mass/mass] less, 11 11 [mass/mass]

[mass/mass]ororless, less,oror may maybebe9 9[mass/mass]

[mass/mass] or less. or less.

[0057] Theleft-hand

[0057] The left-handside sideofofthe theabove-described above-described Inequality Inequality Expression Expression

(1) may (1) be, for may be, for example, example, 11or or more moreorormay maybebe 2 ormore. 2 or more.

[0058] The cracking

[0058] The cracking catalyst catalyst used used for for fluid fluid catalytic catalytic cracking may cracking may

include, for include, for example, an inorganic example, an inorganicoxide oxide(matrix (matrixcomponent) component)andand zeolite. zeolite.

Theinorganic The inorganicoxide oxidemay may be,be, forfor example, example, at least at least oneone selected selected from from the the

groupconsisting group consistingofofkaolin, kaolin, montmorinite, montmorinite,halloysite, halloysite,bentonite, bentonite,alumina, alumina, silica, boria, chromia, magnesia, zirconia, titania, and silica-alumina. The silica, boria, chromia, magnesia, zirconia, titania, and silica-alumina. The

zeolite may zeolite be, for may be, for example, example,atatleast least any anyofof natural natural zeolite zeolite and synthetic and synthetic

zeolite. The zeolite. natural zeolite The natural zeolite may maybebeatatleast least one oneselected selectedfrom fromthethegroup group

17

FP23-0372-00 FP23-0372-00

consisting of gmelinite, chabazite, dachiardite, clinoptilolite, faujasite, consisting of gmelinite, chabazite, dachiardite, clinoptilolite, faujasite,

keyite, heulandite, keyite, heulandite, levynite, levynite,erionite, erionite,sodalite, sodalite,cancrinite, cancrinite, ferrierite, ferrierite,

brewsterite, offretite, natrolite, and mordenite. The synthetic zeolite may brewsterite, offretite, natrolite, and mordenite. The synthetic zeolite may

be at least one selected from the group consisting of X-type zeolite, Y-type be at least one selected from the group consisting of X-type zeolite, Y-type

zeolite, USY-type zeolite, zeolite,A-type USY-type zeolite, A-type zeolite, zeolite, L-type L-type zeolite, zeolite, ZK-4-type ZK-4-type

zeolite, B-type zeolite, E-type zeolite, F-type zeolite, H-type zeolite, J- zeolite, B-type zeolite, E-type zeolite, F-type zeolite, H-type zeolite, J-

type zeolite, M-type zeolite, Q-type zeolite, T-type zeolite, W-type zeolite, type zeolite, M-type zeolite, Q-type zeolite, T-type zeolite, W-type zeolite,

Z-type zeolite, -type Z-type zeolite, a-type zeolite, -type zeolite, -type zeolite, zeolite,-type zeolite, B-type zeolite, ß-type w-typezeolite, w-type zeolite, zeolite, ZSM-5-type ZSM-5-type ZSM-5-type

zeolite, SAPO-5-type zeolite, zeolite,SAPO-11-type SAPO-5-type zeolite, SAPO-11-type zeolite, zeolite, andand SAPO-34-type SAPO-34-type

zeolite. zeolite.

[0059] Thereaction

[0059] The reactiontemperature temperature for for the the fluid fluid catalytic catalytic cracking cracking of the of the

feedstock may feedstock maybebe500 500toto700°C. 700C.In In a case a case where where thethe reaction reaction temperature temperature

is 500C or higher, there is a tendency that the cracking ratio is likely to is 500°C or higher, there is a tendency that the cracking ratio is likely to

be improved, and the yield of the gasoline fraction is likely to be improved. be improved, and the yield of the gasoline fraction is likely to be improved.

In aa case In case where wherethethereaction reactiontemperature temperature is 700C is 700°C or lower, or lower, therethere is a is a tendencythat tendency that excessive excessive cracking crackingreaction reaction can can be be suppressed, suppressed,and andthe theyield yield of the gasoline fraction is likely to be improved. of the gasoline fraction is likely to be improved.

[0060] Thereaction

[0060] The reactiontime time(contact (contacttime) time)ofof fluid fluid catalytic catalyticcracking cracking may be may be

0.5 to 0.5 to 10 10 seconds. seconds.In Ina case a case where where the the reaction reaction timetime of fluid of fluid catalytic catalytic

cracking is 0.5 seconds or more, there is a tendency that the cracking ratio cracking is 0.5 seconds or more, there is a tendency that the cracking ratio

is likely to be improved, and the yield of the gasoline fraction is likely to is likely to be improved, and the yield of the gasoline fraction is likely to

be improved. be improved.In In a case a case where where the the reaction reaction time time (contact (contact time)time) of fluid of fluid

catalytic cracking is 10 seconds or less, there is a tendency that excessive catalytic cracking is 10 seconds or less, there is a tendency that excessive

cracking reaction can be suppressed, and the yield of the gasoline fraction cracking reaction can be suppressed, and the yield of the gasoline fraction

is likely to be improved. is likely to be improved.

[0061] Themass

[0061] The mass of of steam steam supplied supplied to the to the fluid fluid catalyticcracking catalytic cracking unitA A unit

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as aa fluidizing as fluidizing gas gas 13 maybebe2 2toto5050parts 13 may partsbybymass mass with with respect respect to to 100100

parts by parts massofofthe by mass thefeedstock. feedstock.InIna acase case where where the the mass mass of steam of steam is 2 is 2 parts by parts by mass or more, mass or more,the thefeedstock feedstockisis sufficiently sufficiently dispersed, dispersed, and and coking coking

tends to tends to be be suppressed. Inaacase suppressed. In casewhere wherethe themass massof of steam steam is is 50 50 parts parts byby

massororless, mass less, the the contact contact time time can can be be prevented frombecoming prevented from becomingtootoo short, short,

and there is a tendency that the yield of the gasoline fraction is likely to be and there is a tendency that the yield of the gasoline fraction is likely to be

improved. improved.

[0062] Thepressure

[0062] The pressureinside insidethe thereactor reactor11where wherefluid fluidcatalytic catalytic cracking crackingisis 5In a performed performed may performedmay may be bebe 101325 101325 to3x10 to to 101325 310 3x105 Pa.Pa.Pa.Incase In a a casewhere where case where thepressure pressure the pressure the is is is

101325 101325 PaPa (standard (standard pressure) pressure) or higher, or higher, the pressure the pressure of gases of gases after after

cracking does cracking doesnot not drop droptoo toomuch, much,and andoperation operationofofthe therecovery recoveryunit unittends tends 5 or to be to stabilized. In be stabilized. In aa case case where wherethe thepressure pressureisis3x105 310 3x10 Pa Pa Pa or lower, or lower, lower, thethe the

hydrocarbon partial hydrocarbon partial pressure pressure in in the the reactor reactor1 1can can be be prevented prevented from from

becomingtoo becoming toohigh, high,and andthethecracking cracking ratiocancan ratio be be prevented prevented fromfrom

becomingtoo becoming toohigh. high.Therefore, Therefore, excessive excessive cracking cracking reaction reaction cancan be be suppressed, and there is a tendency that the yield of the gasoline fraction suppressed, and there is a tendency that the yield of the gasoline fraction

is likely to be improved. is likely to be improved.

Examples Examples

[0063] Hereinafter,

[0063] Hereinafter, thethe present present disclosure disclosure will will be be described described in more in more detail detail

by way by wayofofExamples; Examples; however, however, thethe present present disclosure disclosure is is notintended not intendedtotobebe limited to limited to these these Examples. Examples.

[0064] <Simulation

[0064] <Simulationof of hydrocarbon hydrocarbon production> production>

(Examples (Examples 1 1toto21 21and andComparative Comparative Examples Examples 1 to 1 8)to 8)

Whether stableoperation Whether stable operationofofhydrocarbon hydrocarbon production production by fluid by the the fluid

catalytic cracking catalytic cracking unit unit A is possible A is possible was wasverified verifiedbyby simulation. simulation.

Specifically, simulation Specifically, of feeding simulation of feedinga afeedstock feedstock into into thethe reactor reactor 1 1 and and

19

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subjecting the subjecting the feedstock feedstock totofluid fluidcatalytic catalyticcracking cracking to produce to produce

hydrocarbons was hydrocarbons wasperformed. performed.TheThe simulation simulation was was performed performed using using TM 6.2" (trade name) manufactured by KBC Corporation. "FCC-SIM "FCC-SIM ver ver 6.2" (trade name) manufactured by KBC Corporation. In the In the above-described InequalityExpression above-described Inequality Expression (1),X, (1), x,x,y,y,and andZ zwere weresetsetasas

showninin Tables shown Tables 11 to to 3. 3. For For Examples Examplesand andComparative Comparative Examples Examples in in which z is 4, a graph plotting the set values of x and y, with x being plotted which Z is 4, a graph plotting the set values of X x and y, with X x being plotted

on the axis of abscissa and y being plotted on the axis of ordinate, is shown on the axis of abscissa and y being plotted on the axis of ordinate, is shown

in FIG. in 3(a). Also, FIG. 3(a). Also, for for Examples Examplesandand Comparative Comparative Examples Examples in which in which Z z is 8, is 8, and and Examples andComparative Examples and Comparative Examples Examples in which in which z isgraphs Z is 12, 12, graphs

similar to similar to the the case whereZ zisis44are case where areshown shownin in FIG. FIG. 3(b)3(b) and and FIG. FIG. 3(c),3(c),

respectively. respectively.

[0065] Simulation

[0065] Simulationwas was performed performed for for feedstocks feedstocks having having the the compositions compositions

shown in Tables 1 to 3. The density at 15C, the sulfur content, the carbon shown in Tables 1 to 3. The density at 15°C, the sulfur content, the carbon

residue content, the distillation characteristics, the aromatic content, the residue content, the distillation characteristics, the aromatic content, the

naphthenecontent, naphthene content,andand the the paraffin paraffin content content for material for the the material of of each each feedstock were feedstock wereassumed assumedto to have have thethe values values shown shown in Table in Table 4. Regarding 4. Regarding

the distillation the distillation characteristics characteristicsof of the the material of the material of the feedstock, feedstock,the the1-1- volume%distillation volume% distillation temperature temperature (T1), (T1), the the 10-volume% 10-volume% distillation distillation

temperature(T10), temperature (T10),the the 30-volume% 30-volume% distillationtemperature distillation temperature(T30), (T30),the the50- 50-

volume% volume% distillationtemperature distillation temperature(T50), (T50),andand thethe 70-volume% 70-volume% distillation distillation

temperature(T70) temperature (T70)are areshown shownin in Table Table 4.4.

[0066] The carbon residue content of the material of a feedstock is a value

[0066] The carbon residue content of the material of a feedstock is a value

measured by measured bythe the method methodofofJIS JISK K2270-2. 2270-2.TheThe sulfur sulfur content content of of thethe

material of material of the the feedstock feedstock is isa a value measured value measured by by the themethod of JIS method of JIS K K 2541- 2541-

4. The 4. Thedistillation distillationcharacteristics characteristics of of the thematerial materialofofthe thefeedstock feedstock areare

values measured values measured by by ASTM D2887. ASTM D2887. TheThe aromatic aromatic content,the content, thenaphthene naphthene

20

FP23-0372-00 FP23-0372-00

content, and the paraffin content of the material of the feedstock are values content, and the paraffin content of the material of the feedstock are values

measured by measured by an an n-d-m method. n-d-m method.

[0067]

[0067] AAmethod methodforfor measuring measuring the naphthene the naphthene content content and and the the paraffin paraffin

content of the material of the feedstock will be described in detail. First, content of the material of the feedstock will be described in detail. First,

(d), 70 the specific gravity (d470), thethe refractive refractive index index (nd), 70the the specific gravity (d4 ), the refractive index (nd ), and the sulfur content (nd and 70), and the sulfur sulfur content content

(SC) (SC) ofthe (SC) of of the feedstock thefeedstock at at feedstock 70C 70°C at are are 70°C measured. measured. are  is calculated ß is calculated measured. is byby substituting by substituting calculated substituting

the measured values of the specific gravity and the refractive index of the the measured values of the specific gravity and the refractive index of the

feedstock at 70°C feedstock at 70Cinto intothe thefollowing followingFormula Formula (b1). (b1). With With regardregard to theto the

calculated calculated , %C B,%CR calculated ß, is R is %CRis calculated calculated calculated by substituting by substituting by substituting into ß into intothe the thefollowing following following

Formula Formula (b2)inin (b2) Formula (b2) ina aacase case case where where where ismore ß is ismore more than than than 0, 0,0,and and andinto into into the following the the following following

Formula (b3) Formula (b3) in in aa case case where ß is where is is lessthan less less than0.0. than %C %Cp 0. %Cp is calculated isPis calculatedbyby calculated by

substituting the substituting the %C into the %CR Rinto the following followingFormula Formula (b4).%CN%C (b4). is calculated is Ncalculated

by substituting by substituting the the %CR %Cand R and thethe %CA%C for material forA the the material offeedstock of the the feedstock measured by measured byan ann-d-m n-d-mmethod method(ASTM (ASTM D3228-equivalent D3228-equivalent method) method) into into

the following the following Formula (b5). The Formula (b5). Thefollowing following Formulas Formulas(b1) (b1)toto (b5) (b5) are are defined with defined with reference referenceto to the the standard standard "ASTM "ASTM D3238". D3238". In Formula In Formula (b2) (b2) and Formula and Formula(b3), (b3),MM representsthetheaverage represents average molecular molecular weight. weight.

 ß=== (n 70 d -- 0.8280) -0.8280) (nd --1.11 - 1.11 0.8280)  (d X1.11 (d470 70 X 4(d 1.460)(b1) - -1.460)...(b1) -1.460) (b1) %C %CR 775- -- 333x XSC %CR R===775B 775ß SCSC 11500/M(b2) ++ 11500/M +11500/M (b2) (b2)

%C %CR 1400- --333XXSC %CR R===1400B 1400ß 12100/M(b3) SCSC++ 12100/M +12100/M (b3) (b3)

%CP == 100 %Cp 100 --%C R %CR (b4) (b4)

%C %CNN == %CN = %C %CR %CRR --%CA %C %CA  (b5) A (b5) (b5)

[0068] Thefeasibility

[0068] The feasibility of of the the simulation simulationisis shown shownininTables Tables1 to 1 to3.3.TheThe fact that fact that simulation simulation is is possible possible means that ROT means that ROT is is calculatedforforthetheset calculated set

values (a values (a solution solution is is obtained obtained by by executing the simulation). executing the simulation). The Thefact factthat that simulation isis impossible simulation impossiblemeans means thatthat ROTROT is notis calculated not calculated forset for the the set

21

FP23-0372-00 FP23-0372-00

values (a values (a solution solution isis not not obtained obtainedbybyexecuting executing the the simulation). simulation). ROT ROT (Riser Outlet Temperature) is the temperature of hydrocarbons at the outlet (Riser Outlet Temperature) is the temperature of hydrocarbons at the outlet

of the of the reactor reactor1, 1,through throughwhich which the the hydrocarbons headingfrom hydrocarbons heading from thereactor the reactor 11 to to the recoveryunit the recovery unitpass. pass.

[0069] <Evaluation

[0069] <Evaluation ofof stableoperation> stable operation> (Examples1 1toto2121and (Examples andComparative Comparative Examples Examples 1 to 1 8)to 8) Theresults The results of of the the simulation simulationwere wereevaluated evaluated on on thethe basis basis of of thethe

followingcriteria. following criteria. The The results results are areshown in Tables shown in Tables 1 1 to to 3. 3. When the ROT When the ROT is 480C or higher, it is considered that the unit can be stably operated by is 480°C or higher, it is considered that the unit can be stably operated by

suppressing solidification of the produced oil or the catalyst (bogging). suppressing solidification of the produced oil or the catalyst (bogging).

(Criteria) (Criteria)

A: The A: Thesimulation simulationisis possible, possible, and and the the ROT ROTisis480°C 480Cor or higher. higher.

B: The B: Thesimulation simulationis isimpossible, impossible, or or although although the simulation the simulation is is possible, the possible, the ROT is lower ROT is lowerthan than480°C. 480C.

[0070] [Table1]1]

[0070] [Table

22

FP23-0372-00 FP23-0372-00

Example Example Possible Possible

100 100 200 200 542 542 10 8 3 A Example Example Possible Possible

100 100 200 200 495 495

9 8 2 A Example Example Possible Possible

100 100 350 350 543 543

8 4 3 A Example Example Possible Possible

100 100 350 350 1.5 494 494

7 4 A Example Example Possible Possible

100 100 300 300 519 519

6 4 3 A Possible Example Example Possible

100 100 300 300 2.2 2.2 490 490

5 4 A Example Example Possible Possible

100 100 250 250 4.5 4.5 526 526

4 4 A Example Example Possible Possible

100 100 250 250 2.8 2.8 486 486

3 4 A Example Example Possible Possible

100 100 200 200 4.5 4.5 508 508

2 4 A Example Example Possible Possible

100 100 200 200 3.5 3.5 482 482

1 4 A stable operation stable operation

Evaluation Evaluation of of Feasibility of of Feasibility

simulation simulation

ROT ROT(C) (°C) FT wax FT wax

XX (°C) (C)

Z y

composition composition (% (% by by mass) mass)

Feedstock Feedstock Simulation Simulation conditions conditions operation operation

results results

FCC FCC

23

FP23-0372-00 FP23-0372-00

[0071] [Table 2]

[0071] [Table 2]

Example Possible Possible Example

100 100 250 250 492 492 20 20 12 0 A

Example Example Possible Possible

237.5 237.5

100 100 484 484 19 12 0 A

Example Example Possible Possible

100 100 200 200 1.5 1.5 540 540 18 18 12 A

Example Example Possible Possible

100 100 200 200 0.5 0.5 490 490 17 17 12 12 A

Example Example Possible Possible

100 100 350 350 1.5 1.5 563 563 16 16 8 A

Example Example Possible Possible

100 100 350 350 485 485 15 8 0 A

Example Example Possible Possible

100 100 300 300 1.5 1.5 532 532 14 14 8 A

Example Possible Possible Example

100 100 300 300 0.7 0.7 488 488 13 8 A

Example Example Possible Possible

100 100 250 250 566 566 12 8 3 A

Example Possible Example Possible

100 100 250 250 1.3 1.3 524 524 11 8 A of Evaluation Evaluation of of Feasibility Feasibility of

simulation simulation ROT ROT (°C) (°C) operation operation

FT wax FT wax stable stable

XX (°C) (°C)

Z y

FCCFCC operation operation

composition composition (%(% byby mass) mass)

Feedstock Feedstock Simulation Simulation conditions conditions

results results

24

FP23-0372-00 FP23-0372-00

[0072] [Table 3]

[0072] [Table 3] Comparative Comparative

Example 8 Example 8 Possible Possible

100 100 200 200 460 460 12 12 0 B

Comparative Comparative

Example 7 Impossible Impossible Example 7 454°C 454°C or or

lower lower

100 100 300 300

8 0 B B

Comparative Comparative

Impossible Impossible Example Example 6 6 454°C 454°C or or

lower lower

100 100 250 250

8 0 B B

Comparative Comparative

Example 5 Example 5 Possible Possible

100 100 200 200 1.5 1.5 469 469

8 B

Comparative Comparative

Example 4 Impossible Example 4 Impossible 454°C or or 454°C

lower lower

100 100 350 350

4 0 B B

Comparative Comparative

Example3 Example 3

Possible Possible

100 100 300 300 1.5 1.5 458 458

4 B

Comparative Comparative

Impossible Impossible Example Example 2 2 454°C or or 454°C

lower lower

100 100 250 250 1.5 1.5

4 B

Comparative Comparative

Example 1 Example 1 Possible Possible

100 100 200 200 464 464

4 3 B B

Example21 Example 21

Possible Possible

100 100 250 250 1.5 540 540 12 1.5 12 A

Feasibility Feasibility of of

simulation simulation ROT (°C) Evaluation Evaluation ROT (C) operation operation ofof stable stable

FT wax FT wax

XX (°C) (°C)

Z y

FCC operation FCC operation

composition composition (% (% byby mass) mass) Feedstock Feedstock conditions conditions Simulation Simulation

results results

25

FP23-0372-00 FP23-0372-00

[0073] [Table 4]

[0073] [Table 4] FT wax FT wax Densityat Density at 15°C (g/cm3) 15C(g/cm³ (g/cm³) 0.82 0.82

Sulfur Sulfur content (%by content (% bymass) mass) 0.01 0.01 Carbonresidue Carbon residuecontent content(%(%byby mass) mass) 0.01 0.01 Aromatic content Aromatic content (%C A) (%CA) 0 0 Naphthenecontent Naphthene content (%C (%CN)N) 0 0 Paraffin content Paraffin content (%C (%Cp)P) 100 100 T1 T1 249 249 Distillation Distillation T10 T10 330 330 characteristics characteristics T30 T30 391 391 (C) (°C) (C) T50 T50 438 438 T70 T70 450 450

[0074] Theabove-described

[0074] The above-described Inequality Inequality Expression Expression (1)derived (1) was was derived as as follows. That follows. Thatis, is, for for Examples and Examples and Comparative Comparative Examples Examples in which in which the the catalyst/oil ratio was 4, a first straight line was derived as a boundary line catalyst/oil ratio was 4, a first straight line was derived as a boundary line

that distinguished that betweenExamples distinguished between Examples1 to1 8, to in 8, which in which the evaluation the evaluation of of stable operation stable wasA, operation was A,and andComparative Comparative Examples Examples 1 toin4,which 1 to 4, in which the the sameevaluation same evaluationwas was B. B. The The firstfirst straight straight line line is is a a straightline straight linepassing passing through Xxx (feed through (feed temperature temperature of of feedstock) feedstock) and and yy (value (value obtained obtained byby dividing feed rate y2 by feed rate y1 and multiplying the resultant by 100) dividing feed rate y2 by feed rate y1 and multiplying the resultant by 100)

of Examples of Examples1,1,3,3,5,5,and and7.7.TheThe firststraight first straightline lineisis represented representedbybythe the followingFormula following Formula(A1). (A1).

[0075] ForExamples

[0075] For Examplesandand Comparative Comparative Examples Examples in which in which the catalyst/oil the catalyst/oil

ratio was ratio 8, aa second was 8, secondstraight straightline line was wasderived derived as as a boundary a boundary line line thatthat

distinguished between distinguished betweenExamples Examples 9 to 9 to 16, 16, inin which which thethe evaluation evaluation ofof stable stable

operation operation was was A, A, and and Comparative Examples55toto 7, Comparative Examples 7, in in which which the the same same

evaluation was evaluation wasB.B.The The second second straight straight linea straight line is is a straight line passing line passing

throughXxxand through andy yofofExamples Examples9, 9, 11,11, 13,13, andand 15.15. TheThe second second straight straight lineline

26

FP23-0372-00 FP23-0372-00

is is represented represented by by the the following Formula(A2). following Formula (A2).

[0076] ForExamples

[0076] For Examplesandand Comparative Comparative Examples Examples in which in which the catalyst/oil the catalyst/oil

ratio was ratio 12, aathird was 12, third straight straight line line was wasderived derivedasasa boundary a boundary lineline thatthat

distinguished between distinguished between Examples 17toto 21, Examples 17 21, in in which whichthe the evaluation evaluation of of

stable operation stable wasA, operation was A,and andComparative Comparative Example Example 8, in8, in which which the the same same evaluation was B. The third straight line is a straight line passing through evaluation was B. The third straight line is a straight line passing through

xx and X and yy of of Examples Examples 1717 andand 19.19. The The third third straight straight line line is is represented represented byby

the following the Formula(A3). following Formula (A3).TheThe firsttotothird first thirdstraight straight lines lines are are shown in shown in

FIGS. 3(a) to 3(c), respectively. FIGS. 3(a) to 3(c), respectively.

[0077]

[0077]

(A1)

[in

[in Formula (A1),X1X1represents Formula (A1), representsthethefeed feedtemperature temperature of of thethe feedstock feedstock at at

a catalyst/oil ratio of 4; and Y1 represents a value obtained by dividing the a catalyst/oil ratio of 4; and Y1 represents a value obtained by dividing the

feed rate of the fuel oil to be fed into the regenerator by the feed rate of feed rate of the fuel oil to be fed into the regenerator by the feed rate of

the feedstock and multiplying the resultant by 100, at the catalyst/oil ratio the feedstock and multiplying the resultant by 100, at the catalyst/oil ratio

of 4.] of 4.]

[0078]

[0078]

(A2)

[in

[in Formula (A2),X2X2represents Formula (A2), representsthethefeed feedtemperature temperature of of thethe feedstock feedstock at at

a catalyst/oil ratio of 8; and Y2 represents a value obtained by dividing the a catalyst/oil ratio of 8; and Y2 represents a value obtained by dividing the

feed rateofofthe feed rate thefuel fueloiloiltotobebe fedfed into into the the regenerator regenerator by theby therate feed feedof rate of the feedstock and multiplying the resultant by 100, at the catalyst/oil ratio the feedstock and multiplying the resultant by 100, at the catalyst/oil ratio

of 8.] of 8.]

[0079]

[0079]

27

FP23-0372-00 FP23-0372-00

Y3 = (A3)

[in Formula

[in (A3),X3X3represents Formula (A3), representsthethefeed feedtemperature temperature of of thethe feedstock feedstock at at a catalyst/oil a catalyst/oilratio ratioofof12;12;and andY3 Y3 represents represents aavalue value obtained obtained by dividing by dividing

the feed rate of the fuel oil to be fed into the regenerator by the feed rate the feed rate of the fuel oil to be fed into the regenerator by the feed rate

of the of the feedstock andmultiplying feedstock and multiplyingthe theresultant resultantbyby100, 100,atatthe thecatalyst/oil catalyst/oil ratio of 12.] ratio of 12.]

[0080] It can

[0080] It canbebeverified verified that that anyany fourfour points points on theonstraight the straight lines lines

represented by represented bythe theabove-described above-described Formulas Formulas (A1) (A1) to (A3) to (A3) exist exist on on the the sameplane. same plane.TheThe feed feed temperature temperature of feedstock of the the feedstock at point at any any point on on the the

straight line straight line represented represented by the above-described by the above-described Formula Formula(A1) (A1) is is designated as X11, designated as X11,and anda avalue valueobtained obtained by by dividing dividing thethe feed feed rate rate of of thethe

fuel oil to be fed into the regenerator by the feed rate of the feedstock and fuel oil to be fed into the regenerator by the feed rate of the feedstock and

multiplying the multiplying the resultant resultant by 100 isis designated by 100 designated asas Y11. Y11.The The feed feed

temperatureofofthe temperature the feedstock feedstockatat any anypoint pointononthe thestraight straight line line represented represented

by the by the above-described above-describedFormula Formula (A2) (A2) is designated is designated as X12, as X12, and aand a value value

obtained bydividing obtained by dividingthethe feed feed raterate of the of the fuelfuel oil betofed oil to be into fed the into the regenerator by the feed rate of the feedstock and multiplying the resultant regenerator by the feed rate of the feedstock and multiplying the resultant

by 100 by 100is is designated as Y12. designated as Thefeed Y12. The feedtemperature temperatureofof thefeedstock the feedstockatatany any point on point on the the straight straightline represented line bybythethe represented above-described above-describedFormula Formula (A3) (A3)

is designated as X13, and a value obtained by dividing the feed rate of the is designated as X13, and a value obtained by dividing the feed rate of the

fuel oil to fuel oil to be fed into be fed intothe theregenerator regeneratorby by the the feedfeed raterate of the of the feedstock feedstock and and multiplyingthe multiplying the resultant resultant by by 100 is designated 100 is designated as as Y13. Bysimultaneously Y13. By simultaneously solving the solving the following following Formulas (A11)toto(A13) Formulas (A11) (A13)represented represented byby X11 X11 to to X13X13

and Y11 and Y11totoY13 Y13forfora,a,b,b, and andc,c, aa conditional expression(A21) conditional expression (A21)serving servingasas

a boundary a boundaryline line that that distinguishes distinguishes between Examples,ininwhich between Examples, whichthethe

28

evaluation of stable operation is A, and Comparative Examples, in which the same evaluation is B, is derived. Based on the conditional expression (A21), the above-described Inequality Expression (1) is derived as the ranges of the feed temperature of the feedstock allowing stable operation 5 of the fluid catalytic cracking unit, the feed temperature of the fuel oil to 2023279401

be fed into the regenerator, and the catalyst/oil ratio.

[0081] X11a + Y11b + 4c + d = 0 (A11) X12a + Y12b + 8c + d = 0 (A12) X13a + Y13b + 12c + d = 0 (A13)

10

[0082] Examples 1 to 21 satisfy the above-described Inequality Expression (1) (left-hand side is 0 or greater). On the other hand, Comparative Examples 1 to 8 do not satisfy the above-described Inequality Expression (1) (left-hand side is less than 0). From this, it could 15 be verified that when the above-described Inequality Expression (1) is satisfied, the unit can be stably operated. Reference Signs List

[0083] 1: reactor, 3: regenerator, A: fluid catalytic cracking unit.

[0084] Throughout this specification and the claims which follow, 20 unless the context requires otherwise, the word "comprise", and variations such as "comprises" and "comprising", will be understood to imply the inclusion of a stated integer or step or group of integers or steps but not the exclusion of any other integer or step or group of integers or steps.

[0085] The reference in this specification to any prior publication (or information derived from it), or to any matter which is known, is not, and should not be taken as an acknowledgment or admission or any form of suggestion that that prior publication (or information derived from it) or 5 known matter forms part of the common general knowledge in the field 2023279401

of endeavour to which this specification relates.

29a

Claims (5)

1. THE CLAIMS DEFINING THE INVENTION ARE AS FOLLOWS

   [Claim 1] A method for producing a hydrocarbon, the method comprising: a step of subjecting a feedstock to fluid catalytic cracking by using 5 a fluid catalytic cracking unit including a reactor and a regenerator, 2023279401

   wherein the feedstock to be fed into the reactor includes FT synthetic oil, a feed temperature x (unit: C) of the feedstock, a feed rate y1 (unit: ton/h) of the feedstock, a feed rate y2 (unit: ton/h) of a fuel oil to be 10 fed into the regenerator, and a circulation rate z1 (unit: ton/h) of a catalyst circulating through the reactor and the regenerator satisfy the following Inequality Expression (1).

   y = (y2/y1)  100 15 z = (z1/y1)
2. [Claim 2] The method for producing a hydrocarbon according to claim 1, wherein the feedstock further includes a hydrocarbon oil having a higher %CA than the FT synthetic oil.
3. [Claim 3] The method for producing a hydrocarbon according to 20 claim 2, wherein the hydrocarbon oil includes a desulfurized atmospheric residue.
4. [Claim 4] The method for producing a hydrocarbon according to claim 1, wherein in the step, the feedstock is obtained by mixing the FT synthetic oil and a hydrocarbon oil having a higher %CA than the FT 25 synthetic oil before the feedstock is fed into the reactor of the fluid

   catalytic cracking unit.
5. [Claim 5] The method for producing a hydrocarbon according to claim 4, wherein the hydrocarbon oil includes clarified oil. 2023279401

   1 /3 1/3 KEROSENE KEROSENE LUBRICANT LUBRICANT OIL OIL HEAVY OIL NAPHTHA-BTX NAPHTHA-BTX HEAVY OIL GASOLINE GASOLINE

   GAS OIL GAS OIL

   PITCH PITCH

   ATMOSPHERIC ATMOSPHERIC

   DISTILLATION DISTILLATION

   CLO CLO

   CRACKING (FCC) CRACKING (FCC)

   CATALYTIC CATALYTIC

   FLUID FLUID

   RDS-BTM RDS-BTM

   HYDROGENATION HYDROGENATION

   REFORMING REFORMING

   CATALYTIC CATALYTIC CRACKING CRACKING

   DESULFURIZATION DESULFURIZATION

   DS-VGO DS-VGO RESIDUAL OILOIL RESIDUAL

   DESULFURIZATION DESULFURIZATION DESULFURIZATION DESULFURIZATION DESULFURIZATION DESULFURIZATION DESULFURIZATION DESULFURIZATION

   KEROSENE KEROSENE

   NAPHTHA NAPHTHA DEASPHALTING DEASPHALTING VACUUM VACUUM GAS GAS OIL OIL GAS OIL GAS OIL

   SOLVENT SOLVENT

   (SDA) (SDA)

   VGO VGO

   DISTILLATION VACUUM

   HOUNTHING DISTILLATION ATMOSPHERIC Fig. Fig. 11

   CRUDE CRUDE OIL OIL