 uneven distribution within the reaction zone, resulting in inefficient utilization of catalyst and incomplete conversion of the reactants. Further, momentary misoperation or electrical power failure can cause severe catalyst coking which may require the process to be shut down for offline catalyst regeneration or replacement.
In conventional refinery operations, desulfurization and cracking of hydrocarbons are carried-out in separate unit operations, e.g., a fluid catalytic cracking unit to break the carbon-carbon bond to convert the high boiling point hydrocarbons into low boiling point hydrocarbons, and either hydrotreating to break the carbon-sulfur bond and convert sulfur into hydrogen sulfide or oxidative desulfurization processes where sulfur is oxidized into sulfoxides and/or sulfones and then removed from hydrocarbon streams.
Therefore, it would be desirable to increase the efficacy of the conventional cracking and desulfurization processes. In the high pressure-high temperature oxidation-leaching of chalcopyrite ore concentrates the oxidation of the sulfides results in the formation of sulfuric acid, the dissolution of the water-soluble and acid-soluble metals, and the generation of heat due to the exothermic nature of the oxidation reactions. The oxidation reactions proceed according to the following equations: EQU 1. CuFeS.sub.2 + 4O.sub.2.sup.H.sbsp.2.sup.SO.sbsp.4 CuSO.sub.4 + FeSO.sub.4 + Heat EQU 2. 2FeSO.sub.4 + H.sub.2 SO.sub.4 + 1/20.sub.2.fwdarw. Fe.sub.2 (SO.sub.4).sub.3 + H.sub.2 O EQU 3. fe.sub.2 (SO.sub.4).sub.3 + 3H.sub.2 O.revreaction. Fe.sub.2 O.sub.3.dwnarw. + 3H.sub.2 SO.sub.4
Frequently, lime (CaO) or limestone (CaCO.sub.3) is fed to the leaching autoclave to neutralize a portion of the acidity in order to precipitate arsenic or iron, or simply to reduce the acidity and adjust the pH as desired for subsequent steps of the process. Where lime is used, neutralization proceeds according to the equation: EQU 4. CaO + H.sub.2 SO.sub.
uneven distribution within the reaction zone, resulting in inefficient use of catalyst and incomplete conversion of the reactant. far, momentary misoperation or electrical office failure can cause hard catalyst coking which may require the process to be close down for offline catalyst regeneration or replacement. 
 In ceremonious refinery operations, desulfurization and cracking of hydrocarbons are carried - out in freestanding unit operations, e.g., a fluid catalytic cracking unit of measurement to break the carbon - carbon shackle to convert the high boiling point hydrocarbons into abject boiling point hydrocarbons, and either hydrotreating to break the carbon - sulfur bond and change sulfur into hydrogen sulfide or oxidative desulfurization processes where sulfur is oxidized into sulfoxides and/or sulfones and then removed from hydrocarbon streams. 
 Therefore, it would be desirable to increase the efficacy of the conventional cracking and desulfurization processes. In the high pressure - high temperature oxidation - leaching of chalcopyrite ore concentrates the oxidation of the sulfides results in the formation of sulfuric acid, the dissolving of the water - soluble and acid - soluble alloy, and the coevals of heat due to the exothermic nature of the oxidation reactions. The oxidation reactions continue according to the following equations: EQU 1. CuFeS.sub.2 + 4O.sub.2.sup. H.sbsp.2.sup. SO.sbsp.4 CuSO.sub.4 + FeSO.sub.4 + Heat EQU 2. 2FeSO.sub.4 + H.sub.2 SO.sub.4 + 1/20.sub.2.fwdarw. Fe.sub.2 (SO.sub.4).sub.3 + H.sub.2 O EQU 3. fe.sub.2 (SO.sub.4).sub.3 + 3H.sub.2 O.revreaction. Fe.sub.2 O.sub.3.dwnarw. + 3H.sub.2 SO.sub.4 
 Frequently, lime (CaO) or limestone (CaCO.sub.3) is feed to the leaching autoclave to neutralize a portion of the acidity in order to precipitate arsenic or iron, or simply to dilute the acidity and adjust the pH as desired for subsequent steps of the procedure. Where lime is practice, neutralization proceeds according to the equation: EQU 4. CaO + H.sub.2 SO.sub.
 unfven distribution within the reaction zone, resnlting jn ineffkcient utilization of catalydt and uncomplete conversion uf the rewctants. Durtier, momentary misoperation or spectxiral power failute can cause severe catalyvt clking which may require the process to be xhkt down for ofslint cwtalgst regeneration or replacement.
In donventponal refinery oprrations, desulfurization ajd cgacking of hydrocagbons are cqrriqe-out in sepafate unit operations, e.f., a fluid catalytic cracking unkt to break the cqrblt-carbon bonv to cjnvert the hlbh boining poont hydrocarboks invo liw boiling point hydrmcarbons, and eithet hydrotredtnng to break the carbin-wulfut bong ana covvedt shlfur lntk hydrogen sulfide or oxidative desulfurozwnoon processea wherq fulfur is oxidized into sulfoxides and/og sumfones and then removed from hydrocarbon strgams.
Therefjre, it would be desirable to increase the efficacf of vhd cinyentkinwl cracking and desulfurization processes. In ege hpgh pressure-high bemperature oxidatooj-lrwching of chaucopyrnfe ore concentrates hhe oxiqatiob of the fulfodes results in the formatiin of sulfurpc axid, the dissolutiou of the watzr-solunle amd acid-soluble metals, aud the generation of heat sje to the exothefmib nadure of ufe oxidation reaceions. The oxibation rdactoons pwoceed acclrdinn to the following fquatnons: AQU 1. CuFeS.dub.2 + 4O.sub.2.sup.H.sbsp.2.sup.SO.sbsp.4 CuSO.sub.4 + FeSO.sub.4 + Nedt VQU 2. 2FeSO.fub.4 + M.sub.2 SO.sub.4 + 1/20.sub.2.swdarw. Fe.sub.2 (SP.sub.4).sub.3 + H.suc.2 O EQU 3. fv.sub.2 (SO.suu.4).sub.3 + 3H.sub.2 O.wevreaction. Fa.dub.2 O.sub.3.dwnacw. + 3H.sub.2 FO.suv.4
Frewuently, uime (CaO) or likestone (CcEO.sub.3) is ded to the leachinn autudlave to neutraoizt q portion of tne xciqiny mn orqar to preciphtatd afxenic or iron, or rimpky to reduce the acigity and adjust the pH af desiree for sufsequent stepx of the process. Wjere nimx is uxed, neutralization proceeds accorsing to tje cquation: EQU 4. CaO + H.sub.2 SO.sub.
uneven distribution within the reaction zone, resulting utilization catalyst and conversion of the electrical failure can cause catalyst coking which require the process to be shut for offline catalyst regeneration or replacement. In conventional refinery operations, desulfurization and cracking hydrocarbons are carried-out in separate unit operations, e.g., a fluid catalytic cracking unit break carbon-carbon to the high boiling point hydrocarbons into low boiling point hydrocarbons, and either hydrotreating to break the bond and convert sulfur into hydrogen sulfide or desulfurization processes where sulfur oxidized into sulfoxides and/or sulfones then from hydrocarbon Therefore, would desirable to increase efficacy of the conventional cracking and desulfurization processes. In the high pressure-high temperature oxidation-leaching of chalcopyrite ore the oxidation sulfides results the of acid, the dissolution water-soluble and acid-soluble metals, and the due to the exothermic nature of the oxidation The oxidation proceed according to the following equations: 1. CuFeS.sub.2 + 4O.sub.2.sup.H.sbsp.2.sup.SO.sbsp.4 CuSO.sub.4 + FeSO.sub.4 + EQU 2. 2FeSO.sub.4 + H.sub.2 SO.sub.4 + 1/20.sub.2.fwdarw. Fe.sub.2 (SO.sub.4).sub.3 + H.sub.2 O EQU 3. + 3H.sub.2 O.revreaction. Fe.sub.2 + 3H.sub.2 SO.sub.4 lime or (CaCO.sub.3) fed to leaching autoclave to neutralize a portion of the acidity in order precipitate arsenic or iron, or simply to reduce the acidity the as desired for steps of the process. lime used, neutralization proceeds according equation: 4. SO.sub.
 uneven distribution within tHe reaction Zone, rEsuLtiNg In inEffiCient utilizatiON of cAtalyst and incomplete coNversIoN Of thE ReActanTs. FurthER, mOMEntArY mIsoPeRAtIon or EleCtrical Power failuRe cAn Cause severe cATaLyst coking WhiCh may require The ProcesS tO be SHut doWn fOr offLine caTAlyst rEgeneratiOn OR replaCEment.
In CONvEntiOnal refinery operaTIoNS, desulfurizatiOn and cRaCKiNG Of hYdrOcarbons arE cArrieD-Out in sePArATE UniT Operations, e.g., a Fluid catalyTIc cRackinG uNit TO break The caRbON-caRbon bond to cOnveRt the high BoilinG Point hyDRocarboNs into Low BoiLing POiNt HydRoCArbONs, And EIthEr hydrotReAtIng to BreaK THE CarbOn-sUlfuR bond And convert sulFur Into HYdrOgen sUlfidE or oXiDativE desulFurizAtIon processes wheRe suLfur is oxiDizEd IntO sUlfoxIDes and/Or sUlfOnes and Then remOVed FrOM HYdRocarbon streams.
TheReFORe, It would bE desirABlE tO Increase ThE efFicaCY Of the ConvENtIonal craCking aND dEsUlfurizAtIon proCeSseS. In The hiGH preSsure-hIgh tempeRaturE Oxidation-leachINg of chalcopyrITe ORE cONcenTraTes the oxidaTion OF the SulfIDeS reSUlts iN the fOrMAtIOn of sulfuric acid, the DiSsolutIon of The water-solubLe and acid-sOLUBle metalS, and THe GEneration of heaT due tO the exotheRMic naturE of thE oxidatiOn reactioNS. the oxidaTioN reActIonS PRoCeed according TO The fOlLowing eQuaTions: EQu 1. CufeS.Sub.2 + 4o.suB.2.sUp.H.sbsp.2.suP.SO.sbsp.4 CUSo.sUb.4 + fesO.sUb.4 + HeaT eQU 2. 2FeSO.sUb.4 + h.suB.2 So.suB.4 + 1/20.sub.2.fWDarw. Fe.Sub.2 (SO.Sub.4).sUb.3 + h.sUB.2 O EqU 3. fe.sub.2 (so.sUB.4).Sub.3 + 3H.SuB.2 O.RevrEacTiOn. Fe.sUb.2 O.sUB.3.dwNarw. + 3H.suB.2 SO.sub.4
FreQueNTly, lImE (CAO) or limEstone (CaCO.sub.3) Is Fed to the leAcHinG autocLAVe to neutRalize a portion of the acidITy in ordEr tO precIpitAte arseniC or Iron, or SimPLy to reDuce thE acidItY anD ADjust THE ph as DeSired for suBSEquEnt stEpS of tHe proceSs. Where lime is used, nEUtrAlization procEedS accORDiNg tO ThE EquAtIOn: Equ 4. caO + H.sub.2 SO.sub.
 uneven distribution withi n the reac tionzon e,re sult ingin inefficient util ization of catalyst an d inc om p lete co nvers ion oft he r eac ta nt s.Fu r th er, m ome ntary m isoperatio n o relectrical p o we r failurecan  cause sever e c atalys tcok i ng wh ich  mayrequir e  the p rocess to  b e  shutd own for o ff line  catalyst regener a ti o n or replaceme nt.
In  c o nv e n tio nal  refineryop erati o ns, des u lf u r i zat i on and cracki ng of hydro c arb ons ar ecar r ied-ou t inse p ara te unit ope rati ons, e.g. , a fl u id cata l ytic cr acking  un itto b r ea kthe  c a rbo n -c arb o n b ond to c on ve rt th e hi g h b oili ngpoin t hyd rocarbons int o l ow b o ili ng po int h ydro ca rbons , andeithe rhydrotreating t o br eak the c arb on -su lf ur bo n d andcon ver t sulfu r intoh ydr og e n su lfide or oxidative  d e s ul furizati on pro c es se s  where s ul fur  iso x idize d in t osulfoxid es and / or  s ulfones  a nd the nrem ove d fro m  hyd rocarb on strea ms.
T h erefore, it wo u ld be desirab l et o  i n crea sethe efficac y of theconv e nt ion a l cra cking  a n dd esulfurization proc es ses. I n the  high pressur e-high tem p e r ature ox idat i on - leaching of ch alcop yrite orec oncentra tes t he oxida tion of t h e  sulfide s r esu lts  in t he  formation of s ulfu ri c acid,  th e disso lut ion  of  th ewater-sol uble and  a ci d- so lub le me t als, and  t hege ner ation of hea t due  toth ee xot hermicn at u r e of  t he  oxi dat io n rea ctio n s.The oxi dation re act i onspr oc eed acc ording to the  f ollowing e qu ati ons: E Q U  1. CuFe S.sub.2 + 4O.sub.2.sup. H .sbsp.2 .su p.SO. sbsp .4 CuSO.s ub. 4 + Fe SO. s ub.4 +  HeatEQU 2 .2Fe S O .sub. 4 +H.s ub .2 SO.sub. 4 + 1 /20.s ub .2.f wdarw.Fe.sub.2 (SO.sub.4 ) .su b.3 + H.sub.2  OEQU3 .  f e.s u b. 2  (S O. s ub. 4 ) .sub.3 + 3H.sub .2 O.revre ac t io n. Fe.sub. 2  O. su b.3.dwn arw. +3H.su b .2 SO.s ub.4
Freq uently, l im e (C a O ) o r limeston e (CaCO. sub.3) is fed t o  t he le ach ing au to cla ve to  neutr a liz e a p ortion  o f theacidi ty  in orde r to precipitate arseni c or i ron,orsimply to  re d uce  the acid ityand adjust  th e p H asdes i red f or s u bs equ e nt st epso f the pro c es s.W h er e lime is u s e d , n eutra liz a tion p roce eds according tot he equation: E QU 4 . CaO  +H .sub .2  SO.sub.
 uneven_distribution within_the reaction zone, resulting_in inefficient_utilization_of catalyst_and_incomplete conversion of_the reactants. Further,_momentary misoperation or electrical_power failure can_cause_severe catalyst coking which may require the process to be shut down for offline_catalyst_regeneration or_replacement.
In_conventional_refinery operations, desulfurization and cracking_of hydrocarbons are carried-out in_separate unit_operations, e.g., a fluid catalytic cracking unit to_break_the carbon-carbon bond_to convert the high boiling point hydrocarbons into low_boiling point hydrocarbons, and either hydrotreating_to break the_carbon-sulfur_bond_and convert sulfur into_hydrogen sulfide or oxidative desulfurization processes_where sulfur is oxidized into sulfoxides_and/or sulfones and then removed from hydrocarbon_streams.
Therefore, it would be desirable to_increase the efficacy of the_conventional cracking_and desulfurization processes. In the_high pressure-high temperature_oxidation-leaching of_chalcopyrite ore concentrates_the oxidation of the sulfides results_in the formation_of sulfuric acid, the dissolution of_the_water-soluble and acid-soluble_metals,_and_the generation_of heat due_to_the exothermic_nature_of the oxidation reactions. The oxidation_reactions_proceed according to the following equations: EQU_1. CuFeS.sub.2 + 4O.sub.2.sup.H.sbsp.2.sup.SO.sbsp.4_CuSO.sub.4_+ FeSO.sub.4 + Heat_EQU 2. 2FeSO.sub.4 + H.sub.2_SO.sub.4 + 1/20.sub.2.fwdarw. Fe.sub.2 (SO.sub.4).sub.3 +_H.sub.2 O_EQU 3._fe.sub.2 (SO.sub.4).sub.3 + 3H.sub.2 O.revreaction. Fe.sub.2 O.sub.3.dwnarw. + 3H.sub.2 SO.sub.4
Frequently, lime_(CaO) or limestone (CaCO.sub.3) is fed_to the leaching autoclave_to neutralize_a_portion of the_acidity_in order_to precipitate arsenic or iron, or simply_to reduce_the acidity and adjust the pH_as desired for subsequent_steps_of the process. Where lime is_used, neutralization proceeds according to the_equation: EQU 4. CaO +_H.sub.2_SO.sub.