Abstract:
An effective, economical catalytic cracking process is provided to produce quality gasoline and other hydrocarbons from whole crude oil. The catalytic cracking process is operable and particularly useful during maintenance or shutdown of associated pipestills, vacuum tower, and/or atmospheric tower.

Description:
BACKGROUND OF THE INVENTION 
     This invention pertains to refining of petroleum and, more particularly, to catalytic cracking of oil. 
     Catalytic cracking of oil is an important refinery process which is used to produce gasoline and other hydrocarbons. During catalytic cracking, the feedstock, which is generally a cut or fraction of crude oil, is cracked in a reactor under catalytic cracking temperatures and pressures in the presence of a catalytic to produce more valuable, lower molecular weight hydrocarbons. Gas oil is usually used as the feedstock in catalytic cracking. Gas oil feedstocks typically contain from 55% to 80% gas oil by volume having a boiling range from 650° F. to 1000° F. and less than 1% RAMS carbon by weight. Gas oil feedstocks also typically contain less than 5% by volume naphtha and lighter hydrocarbons having a boiling temperature below 430° F., from 10% to 30% by volume diesel and kerosene having a boiling range from 430° F. to 650° F., and less than 10% by volume resid having a boiling temperature above 1000° F. 
     In conventional catalytic cracking, whole crude oil is separated in a primary pipestill (crude oil unit) or atmospheric tower into fractions of 200° F. and lighter material, naphtha, diesel oil, atmospheric gas oil, and atmospheric bottoms. The atmospheric bottoms are heated in a furnace and separated in a secondary pipestill or vacuum tower into fractions of vacuum naphtha, light vacuum gas oil, heavy vacuum gas oil, and resid. The atmospheric gas oil from the atmospheric tower and the light and heavy gas oils from the vacuum tower and subsequently pumped into the catalytic cracker as a blended composite gas oil feedstock, where it is contacted with fine solid catalyst particles under cracking conditions to crack the gas oil. During cracking, the catalyst becomes coked and deactivated and has to be regenerated in a regeneration vessel. Fresh catalyst is conventionally replaced in the catalytic cracker at a rate of 0.25 pounds per barrel of reactor feed. 
     Catalytic cracking is an important source of gasoline. From time to time, however, it is necessary to shut down the catalytic cracking unit for days, weeks, or even months to clean, unplug, maintain, uncoke, revamp, and/or repair the pipestill (crude unit) vacuum tower and/or atmospheric tower. When the crude unit is down for maintenance or repair, there is no gas oil feed for the catalytic cracking unit. The catalytic cracking unit would normally be shutdown if gas oil cannot be obtained from another source. Such shutdown deprives the refinery and the consumer of substantial amounts of gasoline. It is also very expensive. Revamp costs and revenue loss to the refinery during shutdown can add up to millions of dollars. Shutdown of the catalytic cracker was, heretofore, required when the pipestills (crude unit), vacuum tower, and/or atmospheric tower were taken offstream for maintenance, revamp, or other work since there was no longer any production of gas oil feedstock from the pipestills (crude unit) and towers. It was generally believed that the catalytic cracking unit could not be operated nor the required heat balance maintained when using unrefined whole crude oil as the feedstock. 
     Typifying some to the many prior art catalytic cracking units, regenerators, and other refinery equipment and processes are those shown in U.S. Patents: 2,382,382; 2,398,739; 2,398,759; 2,414,002; 2,425,849; 2,436,927; 2,884,303; 2,981,676; 2,985,584; 3,004,926; 3,039,953; 3,351,548; 3,364,136; 3,513,087; 3,563,911; 3,661,800; 3,838,036; 3,844,973; 3,909,392; 4,331,533; 4,332,674; 4,341,623; 4,341,660; 4,332,674; and 4,695,370. 
     It is, therefore, desirable to provide an improved catalytic cracking process which is operable when the upstream pipestills (crude unit) or towers are taken off line for revamp, maintenance, or to shutdown permanently to consolidate operations. 
     SUMMARY OF THE INVENTION 
     An effective catalytic cracking process is provided to produce gasoline and other hydrocarbons. The novel catalytic cracking process is efficient, economical, and safe. It provides an excellent source of good quality gasoline to consumers and is very profitable for the refinery. Advantageously, the novel process is fully operable and is particularly useful when the upstream pipestills (crude unit) or towers are shut down and/or taken off line for revamp, repair, cleaning, decoking, maintenance, etc. 
     To this end, the novel cataytic cracking process comprises feeding petroleum to a catalytic cracking unit without previously fractionating the petroleum in a pipestill (crude unit), atmospheric tower, or vacuum tower. The petroleum can comprise: raw, uncut, whole crude oil; flashed crude oil; or petroleum containing less than about 50% gas by volume. In the catalytic cracking unit, the petroleum is cracked in the presence of a catalyst in a riser reactor and/or a fluidized bed reactor to more valuable, lower molecular weight hydrocarbons. For enhanced demetallization (removal of metals) of the oil, fresh catalyst can be fed and replaced in the regenerator at an increased rate of up to about 2 pounds per barrel of reactor feed. Coked catalyst is conveyed to a regenerator where it is regenerated and then recycled to the reactor. In order to enhance the environment and minimize pollution, carbon monoxide emitted during regeneration is essentially completely combusted in the regenerator. 
     Preferably, the composition of the petroleum feed comprises by volume: (a) less than about 35% hydrocarbons comprising naphtha and light hydrocarbons having a boiling temperature less than about 430° F.; preferably less than 400° F.; (b) from about 20% to about 50% hydrocarbons comprising diesel oil and kerosene having a boiling temperature ranging from greater than about 430° F. to less than about 650° F.; (c) from about 20% to less than about 50% hydrocarbons comprising gas oil having a boiling tempreature ranging from greater than about 650° F. to less than about 1000° F.; (d) less than about 20% hydrocarbons comprising resid having a boiling temperature greater than about 1000° F.; and (e) preferably less than 2% RAMS carbon by weight in the petroleum feed. Most perferably, a low resid crude is used with the RAMS carbon content of the resid ranging from about 0.5% to about 10% by weight. 
     One particularly useful petroleum feedstock is Trinidad crude from the Island of Trinidad. Other useful petroleum feedstocks can comprise: Brass River crude from Nigeria, HIPS crude from Galveston Bay, Texas, Florence Canal crude from Louisiana, St. Gabriel crude from Louisiana, and Louisiana Light crude from Louisiana. 
     As used in this patent application, the abbreviation &#34;FCCU&#34; means fluid catalytic cracking unit. 
     A more detailed explanation of the invention is provided in the following description and appended claims, taken in conjunction with the accompanying drawing. 
    
    
     BRIEF DESCRIPTION OF THE DRAWING 
     The FIGURE is a schematic flow diagram of a catalytic cracking process in accordance with principles of the present invention. 
    
    
     DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT 
     Unrefined, raw, whole crude oil or petroleum, is pumped by a pump 10 from tankage, such as an above ground storage tank 12 at about 75° F. to about 80° F., through pipelines 14-17. The whole crude oil comprises by volume: (a) less than about 35% hydrocarbons comprising naphtha and light hydrocarbons having a boiling temperature less than about 430° F., preferably less than 400° F.; (b) from about 20% to about 50% hydrocarbons comprising diesel oil and kerosene having a boiling temperature ranging from greater than about 430° F. to less than about 650° F.; (c) from about 20% to less than about 50% hydrocarbons comprising gas oil having a boiling temperature ranging from greater than about 650° F. to less than about 1000° F.; (d) less than about 20% hydrocarbons comprising resid having a boiling temperature greater than about 1000° F.; and (e) preferably less than 2% RAMS carbon by weight in the whole crude oil. Most preferably, a low resid crude is used with the RAMS carbon content of the resid ranging from about 0.5% to about 10% by weight. For best results, the preferred petroleum (whole crude oil) is Trinidad crude. 
     Decanted oil can be injected, fed, mixed, or blended with the whole crude oil in line 14 through decanted oil line 18 and/or 19, via valves 20 and 21, to raise the temperature of the regenerator 22 in the fluid catalytic cracking unit (FCCU) 24 so as to enhance the complete combustion of carbon monoxide in the regenerator 22. Decanted oil can be obtained from a separate FCCU or from the decanted oil ouput line 26 of the main fractionator 30, downstream of the subject FCCU 24. In some circumstances it may be desirable to inject, feed, mix, or blend, the decanted oil with the reactor charge or crude oil anywhere before reaching the reactor. 
     Valve 32 can be provided to regulate the flow of oil through line 17. Water can be passed through water lines 34-37 and injected, fed, and dispersed into oil line 17 downstream of valve 32. The flow rate of the water can be regulated or stopped by one or more water control valves 38 and 40. 
     The oil in line 17 is partially preheated to about 125° F. in a heat exchanger 42. The partially preheated oil from heat exchanger 42 in line 44 is passed through exchanger lines 46 and 48 to parallel heat exchangers 50 and 52 where the oil is further partially preheated to about 220° F. The partially preheated oil from heat exchangers 50 and 52 in exchanger effluent line 54-56 is passed through an oil flow valve 58 to line 60. Water from water lines 34 and 35 can be passed through water lines 62 and 64 via water flow valve 66 to be injected, fed, and dispersed into the oil in oil line 60. Hydrochloric acid or other acids from a tank 68 can be pumped by pH control pump 70 through acid lines 72 and 74 into the water in lines 35 and 62 to maintain and control the pH of the water injected into the oil. The oil and water in line 76 are mixed by a mix valve 78 and passed through mixed oil and water line 80 into a desalter 82. About 5% to about 10% water by volume can be added to the oil. In the desalter 82, the oil is desalted and the water removed. The removed water is discharged through water discharge line 84. 
     The desalted oil from the desalter 82 in line 86 is passed through line 88, via a valve 90, into a heat exchanger 92 where it is preheated to about 315° F. The preheated oil from heat exchanger 92 in exchanger effluent line 94 is passed into another heat exchanger 96 where it is further preheated to about 372° F. The preheated oil from heat exchanger 96 is passed from line 98 to a furnace 100 where it is heated to about 520° F. The heated oil from the furnace 100 is passed through oil lines 102-104, via heated oil flow valve 106, into a flash drum 108. 
     In the flash drum 108, the oil is flashed so a substantial portion of the naphtha and light ends (light hydrocarbons) having a boiling temperature below 430° F. are vaporized and removed through an overhead flash line 110. About 20% to about 30% by volume of Trinidad crude can be flashed. The flashed vapors in overhead flash line 110 are passed through a flash vapor line 112, via a valve 114, to the main fractionator 30. 
     The remaining flashed liquid oil (flashed bottoms) in the flash drum 108 is discharged from the bottom portion of the flash drum 108 through liquid line 116 and pumped by pump 118 through lines 120-122, via liquid flow control valve 124, into the catalytic cracking reactor 126 of the FCCU 24. The reactor charge (reactor feed) comprising flashed liquid oil (flashed) bottoms fed to the reactor 126 comprises by volume: (a) from about 0.1% to about 20% hydrocarbons comprising naphtha and light hydrocarbons having a boiling temperature less than about 430° F., preferably less than about 400° F.; (b) from about 20% to about 50% hydrocarbons comprising diesel oil and kerosene having a boiling temperature ranging from greater than about 430° F. to less than about 650° F.; (c) from about 30% to about 70%, preferably less than 50%, hydrocarbons comprising gas oil having a boiling temperature ranging from greater than about 650° F. to less than about 1000° F.; (d) less than about  20% hydrocarbons comprising resid having a boiling temperature greater than 1000° F.; and (e) preferably from about 0.5% to about 10% by weight RAMS carbon in the resid. 
     In some circumstances, it may be desirable to bypass the flash drum 108 and feed whole crude oil through bypass lines 128 and 130 and oil line 122, via bypass regulator valve 132 into the FCCU 24. Bypass valve 132 can be opened for bypass operations or can be closed if feed is flashed in the flash drum 108. 
     The fluid catalytic cracking unit (FCCU) 24 includes a catalytic cracking (FCC) reactor 126, a stripper section 128, and a regenerator 22. The catalytic cracking reactor 126 preferably comprises a riser reactor. In some circumstances it may be desirable to use a fluid bed reactor or a fluidized catalytic cracking reactor. Fresh replacement catalyst (makeup catalyst) is fed through fresh catalyst line 134 into the regenerator 22 at a replacement rate of about 0.25 to about 2.0, preferably less than about 0.5, pounds per barrel to reactor feed (flashed bottoms) to control the effects of contaminant metals in the reactor feed. In the catalytic cracking reactor 126, the oil is contacted, mixed, and fluidized with the fresh catalyst and regenerated catalyst from regenerated catalyst line 136 at catalytic cracking temperatures and pressures to catalytically crack and volatilize the oil feed into more valuable, lower molecular weight hydrocarbons. The temperatures in the reactor 126 can range from about 900° F. to about 1025° F. at a pressure from about 5 psig to about 50 psig. The circulation rate (weight hourly space velocity) of the cracking catalyst in the reactor can range from about 5 to about 200 WHSV. The velocity of the oil vapors in the riser reactor can range from about 5 ft/sec to about 100 ft/sec. 
     Suitable cracking catalysts include, but are not limited to, those containing silica and/or alumina, including the acidic type. The cracking catalyst may contain other refractory metal oxides such as magnesia or zirconia. Preferred cracking catalysts are those containing crystalline aluminosilicates, zeolites, or molecular sieves in an amount sufficient to materially increase the cracking activity of the catalyst, e.g., between about 1 and about 25% by weight. The crystalline aluminosilicates can have silica-to-alumina mole ratios of at least about 2:1, such as from about 2 to about 12:1. The crystalline aluminosilicates are usually available or made in sodium form and this component is preferably reduced, for instance, to less than about 4 or even less than about 1% by weight through exchange with hydrogen ions, hydrogen-precursors such as ammonium ions, or polyvalent metal ions. Suitable polyvalent metals include calcium, strontium, barium, and the rare earth metals such as cerium, lanthanum, neodymium, and/or naturally-occuring mixtures of the rare earth metals. Such crystalline materials are able to maintain their pore structure under the high temperature conditions of catalyst manufacture, hydrocarbon processing, and catalyst regeneration. The crystalline aluminosilicates often have a uniform pore structure of exceedingly small size with the cross-sectional diameter of the pores being in a size range of about 6 to about 20 angstroms, preferably about 10 to about 15 angstroms. Silica-alumina based cracking catalysts having a major proportion of silica, e.g., about 60 to about 90 weight percent silica and about 10 to about 40 weight percent alumina, are suitable for admixture with the crystalline aluminosilicate or for use as such as the cracking catalyst. Other cracking catalysts and pore sizes can be used. The cracking catalyst can also contain or comprise a carbon monoxide (CO) burning promoter or catalyst, such as a platinum catalyst to enhance the combustion of carbon monoxide in the dense phase in the regenerator 22. 
     The catalytically cracked hydrocarbon vapors (volitilized oil) from the catalytic cracking reactor 126 are passed through an overhead product line 138 into the FCC main fractionator 30. In the main fractionator 30, the oil vapors and flashed vapors are fractionated (separated) into: (a) light hydrocarbons having a boiling temperature less than about 430° F., (b) light catalytic cycle oil (LCCO), and decanted oil (DCO). The light hydrocarbons are withdrawn from the fractionator 30 through an overhead line 140 and fed to a separator drum 142. In the separator drum 142, the light hydrocarbons are separated into (1) wet gas and (2) C 3  to 430-° F. light hydrocarbon material comprising propane, propylene, butane, butylene, and naphtha. The wet gas is withdrawn from the separator drum 142 through a wet gas line 144 and further processed in a vapor recovery unit (VRU). The C 3  to 430-° F. material is withdrawn from the separator drum 142 through a line 146 and passed to the vapor recovery unit (VRU) for further processing. LCCO is withdrawn from the fractionator 30 through an LCCO line 148 for further refining, processing, or marketing. DCO is withdrawn from the fractionator 30 through one or more DCO lines 26 for further use. Slurry recycle comprising DCO can be pumped from the bottom portion of the fractionator 30 by pump 150 through a slurry line 26 for recycle to the reactor 126. The remainder of the DCO is conveyed through line 28 for further use in the refinery. 
     Spent deactivated (used) coked catalyst is discharged from the catalytic cracking reactor 126 and stripped of volatilizable hydrocarbons in the stripper section 128 with a stripping gas, such as with light hydrocarbon gases or steam. The stripped coked catalyst is passed from the stripper 128 through spent catalyst line 146 into the regenerator 22. Air is injected through air injector line 148 into the regenerator 22 at a rate of about 0.2 ft/sec to about 4 ft/sec. Preferably, excess air is injected in the regenerator 22 to completely convert the coke on the catalyst to carbon dioxide and steam. The excess air can be from about 2.5% to about 25% greater than the stoichiometric amount of air necessary for the complete conversion of coke to carbon dioxide and steam. 
     In the regenerator 22, the coke on catalyst is combusted in the presence of air so that the catalyst contains less than about 0.1% coke by weight. The coked catalyst is contained in the lower dense phase section of the regenerator 22, below an upper dilute phase section of the regenerator 22. Carbon monoxide can be combusted in both the dense phase and the dilute phase although combustion of carbon monoxide predominantly occurs in the dense phase with promoted burning, i.e., the use of a CO burning promoter. The temperature in the dense phase can range from about 1150° F. to about 1400° F. The temperature in dilute phase can range from about 1200° F. to about 1510° F. The stack gas (combustion gases) exiting the regenerator 22 through overhead flue line 150 preferably contains less than about 0.2% CO by volume (2000 ppm). The major portion of the heat of combustion of carbon monoxide is preferably absorbed by the catalyst and transferred with the regenerated catalyst through a regenerated catalyst line 136 into the catalytic cracking reactor 126. 
     In a catalytic cracker (reactor) 126, some non-volatile carbonaceous material, or coke, is deposited on the catalyst particles. Coke comprises highly condensed aromatic hydrocarbons which generally contain 4-10 wt. % hydrogen. As coke builds up on the catalyst, the activity of the catalyst for cracking and the selectivity of the catalyst for producing gasoline blending stock diminish. The catalyst particles can recover a major proportion of their original capabilities by removal of most of the coke from the catalyst by a suitable regeneration process. 
     Catalyst regeneration is accomplished by burning the coke deposits from the catalyst surface with an oxygen-containing gas such as air. The burning of coke deposits from the catalyst requires a large volume of oxygen or air. Oxidation of coke may be characterized in a simplified manner as the oxidation of carbon and may be represented by the following chemical equations: 
     
         a. C+O.sub.2 →CO.sub.2 
    
     
         b. 2C+O.sub.2 →2CO 
    
     
         c. 2CO+O.sub.2 →2CO.sub.2 
    
     Reactions (a) and (b) both occur at typical catalyst regeneration conditions wherein the catalyst temperature may range from about 1050° F. to about 1300° F. and are exemplary of gas-solid chemical interactions when regenerating catalyst at temperatures within this range. The effect of any increase in temperature is reflected in an increased rate of combustion of carbon and a more complete removal of carbon, or coke, from the catalyst particles. As the increased rate of combustion is accompanied by an increased evolution of heat whenever sufficient oxygen is present, the gas phase reaction (c) may occur. This latter reaction is initiated and propagated by free radicals. Further combustion of CO to CO 2  is an attractive source of heat energy because reaction (c) is highly exothermic. 
     EXAMPLES 
     The following examples serve to give specific illustration of the practice of this invention but are not intended in any way to limit the scope of this invention. 
     Whole crude oil consisting of Trinidad crude was fed, processed, and refined in a catalyst cracking process and system substantially similar to the process flow diagram of the Figure. Specifically, 51 days of test runs were conducted starting on Mar. 29, 1987 at FCCU No. 2 at the Amoco Oil Company Refinery at Texas City, Texas. The test runs produced unexpected surprisingly good results, since it was heretofore believed that Trinidad crude could not be catalytically cracked without prior fractionation of the Trinidad crude or similar light crude in a pipestill(s), vacuum tower, and/or atmospheric tower. The extent, amount, and quality of the products produced by the test runs were unexpected. Furthermore, the test runs later became a commercial success when the products produced during the tests runs were eventually sold for about a $5 million net profit. Such profit was mainly attributable to the unique process arrangement and sequence shown in the Figure and recited in the claims. 
     EXAMPLE 1 
     Totals for the test runs were as follows: 
     
         ______________________________________       VolumeFeed        BSD        °API                         Lb/Hr    Wt. %______________________________________Trinidad    31,800     32.3   400,345  98.5FCCU No. 3 DCO       370        -3.3   6,015    1.5       Total 32,170      Total 406,360______________________________________        VolumeProducts     BSD      °API                            Use______________________________________Absorber Offgas        220      22.6    MW   fuel        MSCFHPropane-Propylene        5        42.7    MW   fuel        MSCFHPropane-Propylene        2,600    144.5        alkylation feedButane-Butylene        3,910    109.5        alkylation feedLight CatalyticNaphtha      4,020    76.6         blendingHeavy CatalyticNaphtha      12,810   49.3         reformer feedLight CatalyticCycle Oil (LCCO)        10,190   26.4         fuel oilDecanted Oil (DCO)        280      -1.1         recycle, fuelCoke______________________________________Products     Lb/Hr    Wt %       Use______________________________________Absorber Offgas        13,230   3.26       fuelPropane-Propylene        540      0.13       fuelPropane-Propylene        19,370   4.77       alkylation feedButane-Butylene        33,450   8.23       alkylation feedLight CatalyticNaphtha      39,830   9.80       blendingHeavy CatalyticNaphtha      146,070  35.95      reformer feedLight CatalyticCycle Oil (LCCO)        133,050  32.74      fuel oilDecanted Oil (DCO)        4,440    1.09       recycle, fuelCoke         16,380   4.03Total        406,360  100.00______________________________________ 
    
     EXAMPLE 2 
     During the test runs on Apr. 13, 1987, the Trinidad whole crude had: an actual API gravity of 32.7°, a molecular weight of 231.98, an observed refractive index of 1.4612, and an average boiling point of 571.4° F. The Trinidad crude comprised by weight: 0.22% RAMS carbon, 0.25% sulfur, and 0.0230 total nitrogen. The Trinidad whole crude had the following characteristics at a normal pressure of 760 mm. 
     
         ______________________________________True Boiling Point           % Crude Vaporized°F.      (Boiled)______________________________________400             24.73430             28.78450             31.96475             36.43500             40.85525             45.08550             49.32575             53.44600             57.54625             61.27650             64.43675             67.59700             70.65725             73.37750             76.09800             81.01850             84.60900             88.20950             91.001000            93.001100            96.321200            98.95______________________________________ 
    
     EXAMPLE 3 
     During the test runs on Apr. 13, 1987, the flashed bottoms which were fed to the catalytic cracker had: an actual API gravity of 29°, a molecular weight of 290.94, an observed refractive index of 1.4702, and an average boiling point of 678.2° F. The flashed bottoms comprised by weight: 0.35% RAMS carbon, 0.37% sulfur, 0.0370 total nitrogen. The flashed bottoms had the following characteristics at a normal pressure of 760 mm. 
     
         ______________________________________           % FlashedTrue Boiling Point           Bottoms Vaporized°F.      (Boiled)______________________________________400             11.36430             15.06450             17.53475             20.68500             24.11525             27.53550             31.40575             36.40600             41.27625             45.82650             50.34675             54.58700             58.81725             62.50750             65.97800             72.36850             77.98900             81.95950             85.001000            88.051100            95.211200            98.63______________________________________ 
    
     EXAMPLE 4 
     During the test runs on Apr. 15, 1987, the Trinidad whole crude had: an actual API gravity of 33°, a molecular weight of 224, and an average boiling point of 571.63° F. The Trinidad crude had the following characteristics at a normal pressure of 760 mm. 
     
         ______________________________________True Boiling Point           % Crude Vaporized°F.      (Boiled)______________________________________400             18.38430             21.80450             24.62475             28.14500             32.21525             36.88550             41.55575             46.23600             50.81625             55.04650             59.27675             63.50700             67.73725             72.30750             77.28800             84.81850             90.65900             93.64950             95.701000            96.981100            99.541200            100.00______________________________________ 
    
     EXAMPLE 5 
     During the test runs on Apr. 15, 1987, the flash drum bottoms (flashed bottoms) which were fed to the FCCU had: an actual API gravity of 29.3°, a molecular weight of 265, and an average boiling point of 685.59° F. The flashed bottoms comprised by weight: 0.3% RAMS carbon and 0.25% total nitrogen. The flashed bottoms had the following characteristics at a normal pressure of 760 mm. 
     
         ______________________________________           % FlashedTrue Boiling Point           Bottoms Vaporized°F.      (Boiled)______________________________________400             8.69430             9.46450             9.96475             13.36500             16.91525             20.69550             26.01575             31.25600             36.25625             41.24650             46.23675             50.99700             55.06725             59.13750             63.20800             71.30850             79.27900             84.83950             90.341000            98.471100            100.001200            100.00______________________________________ 
    
     EXAMPLE 6 
     During the test runs on Apr. 28, 1987, the Trinidad whole crude had an API gravity of 32.9° and a RAMS carbon content of 0.31% by weight. The initial boiling point was 143° F. The whole crude had the following characteristics: 
     
         ______________________________________True Boiling Point           % Crude Vaporized°F.      (Boiled)______________________________________335             10420             20485             30531             40578             50629             60684             70699             75.5______________________________________ 
    
     EXAMPLE 7 
     During the test runs from Mar. 29, 1987 to May 18, 1987, 1.62 MM barrels of Trinidad crude were processed at a throughput rate of 31.8 MBCD. The catalytic cracking reactor charge rate averaged 23.8 MBCD, and 24.6% flashed off and processed with a riser. The volume recovery was 105.78%, and the weight balance was 99.3%. Gasoline production was 16.7 MBCD. Light catalytic naphtha production was 23.8%. Heavy catalytic naphtha production was 76.2%. 
     EXAMPLES 8-357 
     The feed rates, products, and other data taken for the tests run from Mar. 30, 1987 to May 19, 1987 were as follows: 
     
         __________________________________________________________________________      PropaneFresh Propylene            Propane                  Butane                       Lt CatDate Feed  to-Fuel            Propylene                  Butylene                       Gasoline1987 B/D   SCFH  B/D   FR-313                       B/D__________________________________________________________________________0330 25947 6.7   2895  3010 61580331 29560 0.0   2538  3475 50740401 29338 6.2   2255  3331 47490402 29448 0.0   2617  3196 48280403 29900 0.0   2467  3675 41500404 29524 4.0   2282  3632 36220405 29570 0.5   2454  3706 36000406 28989 0.0   2363  4046 36300407 29378 0.0   2562  3658 42800408 34000 0.0   2432  4315 50980409 33378 0.4   2525  4127 46000410 33308 0.0   2707  3687 53910411 32405 1.4   2672  3588 54570412 32733 4.1   2660  4851 51230413 33361 10.3  2638  3754 51000414 33454 19.3  2663  3901 51540415 33034 9.5   2702  3984 50430416 32146 6.8   2690  4124 36380417 32004 4.5   2579  3868 32340418 31780 4.8   2263  3919 26500419 32404 0.7   2643  3729 26230420 32043 0.0   2724  4000 34660421 32930 0.0   2559  4372 40310422 32910 3.8   2565  4164 47460423 33243 0.0   2708  3843 44330424 33425 0.1   2828  3889 32160425 31915 0.3   2512  4319 29010426 29173 0.6   2314  4822 22880427 33780 0.6   2800  4528 27840428 33860 0.5   2873  3878 36910429 34522 0.4   2817  3945 36790430 33453 0.9   2487  4366 35270501 33365 1.1   2637  4304 39840502 33290 3.4   2776  4245 49320503 32936 0.0   2574  4228 50520504 32990 0.5   2764  3784 52800505 32964 1.9   3076  3581 54730506 33181 2.7   2751  3669 47510507 32930 4.7   2727  4006 40390508 33459 0.1   2494  4255 29990509 33232 0.0   2497  4287 23650510 33959 0.2   3130  3301 26290511 17116 45.7  1353  3434 18290512 27848 10.4  1940  3209 34000513 32513 0.0   2555  3782 29600514 32691 0.3   2691  4167 29500515 32650 0.1   2817  4071 30350516 33122 6.7   3032  3700 25300517 32932 11.0  2815  3633 31260518 33500 11.2  2529  3610 49420519 30158 19.7  2324  3888 5150Average31799 4.0   2594  3899 3988__________________________________________________________________________                      DCO                      from Heavy Cat           DCO   another                           ReactorDate Gasoline   HCCO LCCO                Recycle                      FCCU Charge1987 B/D        B/D  B/D B/D   B/D  B/D__________________________________________________________________________0330 7209       98   7502                0     125  150000331 10950      0    8667                0     300  240000401 11300      0    9009                0     335  220000402 11290      0    9193                0     0    220000403 12012      0    8910                0     0    225000404 12365      0    8500                0     0    225000405 12299      0    8661                0     0    225000406 11776      0    8342                0     0    225000407 11342      0    8999                0     0    220000408 12780      0    10400                0     0    220000409 12710      0    10500                0     0    250000410 12078      0    11231                0     420  252000411 11777      0    10631                316   400  250000412 11274      0    10851                245   500  245000413 12207      0    11330                288   730  247900414 12100      0    11466                439   745  250000415 11872      0    11091                401   685  243400416 12512      0    11267                338   700  237100417 12780      0    11203                261   685  243400418 12893      0    11659                227   440  240000419 13728      0    11264                343   480  242000420 13195      0    10646                311   546  240000421 12777      0    10666                405   760  255000422 12688      0    10739                304   700  255000423 12928      0    10920                185   642  254000424 13950      0    11503                160   597  250000425 13218      0    10512                301   100  253100426 12010      0    9550                275   100  261000427 13707      0    11928                482   538  255000428 13996      0    11083                338   530  253500429 14302      0    11311                375   514  254500430 13879      0    10817                262   300  255000501 13434      0    10399                319   395  250000502 12499      65   9931                418   376  246700503 12470      0    10136                311   421  250000504 12608      10   10171                308   343  250000505 12577      61   10385                199   198  252000506 13092      0    10295                150   412  252220507 13744      169  10353                156   597  253000508 14364      0    10768                294   600  252200509 15356      0    10615                263   590  252500510 15795      0    10902                386   193  84170511 9163       615  5109                696   667  143200512 11036      437  9326                393   1000 247900513 14991      0    10427                345   60   249700514 14638      6    9648                266   505  248300515 14748      0    9921                86    180  245500516 15640      0    10090                343   20   241700517 14432      0    10268                338   28   245000518 13079      0    10787                412   409  245200519 10780      0    9442                268   219  24500Average 12752      29   10183                239   374.2                           23747__________________________________________________________________________  Regen Regen  Flue  Flue  Gas   Gas Reactor Regen                        Feed  CO    O2  Feed    Temp                        PreheatDate   ppm   vol %            deg F   deg F                        deg F1987   AR-2  AR-1            II-1-31 II-1-12                        II-1-45__________________________________________________________________________0330   613   0.6 541     1251                        4140331   491   4.3 523     1257                        3750401   296   5.1 532     1246                        3910402   250   5.00403   250   5.00404   238   5.0 531     1249                        3900405   282   5.0 531     1243                        3950406   264   4.9 523     1245                        3950407   283   4.2 525     1251                        3920408   520   2.6 525     1253                        3850409   754   1.0 520     1259                        3860410   724   2.2 520     1264                        3880411   597   3.1 522     1258                        3800412   696   2.1 524     1266                        3810413   708   2.1 523     1266                        3840414   582   2.2 519     1272                        3860415   445   2.7 515     1278                        3820416   498   1.6 515     1279                        3840417   554   1.4 515     1281                        3870418   485   1.5 513     1291                        3910419   439   2.0 511     1285                        3880420   497   1.8 513     1286                        3880421   485   1.6 513     1290                        3810422   369   2.0 515     1290                        3760423   252   2.5 517     1293                        3780424   221   3.0 514     1291                        3780425   263   2.8 517     1292                        3830426   644   1.3 525     1282                        4020427   443   2.1 524     1292                        3800428   476   2.1 522     1283                        3670429   396   2.5 521     1284                        3640430   460   2.2 515     1283                        3680501   526   3.0 512     1274                        3640502   648   2.3 516     1264                        3590503   682   1.5 516     1267                        3580504   660   1.7 515     1266                        3560505   787   2.9 517     1268                        3580506   751   2.7 518     1259                        3570507   516   3.5 513     1275                        3690508   310   4.5 516     1273                        3680509   315   4.3 517     1276                        3670510   274   4.9 521     1277                        3640511   260   5.1 498     1185                        3880512   142   5.2 549     1298                        4030513   351   2.8 524     1307                        3840514   331   4.2 520     1285                        3680515   332   5.0 520     1286                        3670516   374   4.7 530     1283                        3670517   475   4.6 530     1272                        3640518   629   3.7 527     1276                        3700519   558   1.5 550     1276                        406Average  459   3.06            521     1272                        379__________________________________________________________________________ Fresh Feed DCO  HCCO LCCO Hvy CatDate  Deg  Deg  Deg  Deg  Gasoline                           LCN1987  API  API  API  API  Deg API                           Deg API__________________________________________________________________________0330  31.8 -1.5 14.4 28.3 47    74.70331  32.3 1.2  14.4 27.7 47    74.70401  31.6 1.3  24.4 27.2 50.4  73.30402  31.6 1.3  24.4 27.2 50.4  73.30403  31.6 1.3  24.4 27.2 50.4  73.30402  32.8 2.4  24.4 26.7 50.4  73.30405  33   2.2  24.4 26.6 50.4  73.30406  32.6 0.4  24.4 24.6 49.7  74.40407  33.1 1.1  24.4 27.3 49.7  74.40408  33.1 1.1  24.4 27.3 49.7  74.40409  32.5 1.9  24.4 27.2 49.3  76.40410  32.6 -0.5 24.4 27.2 49.3  76.40411  32.9 -1   24.4 25.7 49.3  76.40412  32.7 -3.5 24.4 26.5 49.3  76.40413  33.1 -0.8 24.4 25.2 48.2  75.70414  32.3 -3   24.4 25.2 48.2  75.70415  32.8 -1.3 24.4 26.6 46.7  73.40416  27.6 -2.2 24.4 27.2 46.7  73.40417  32.8 -1.9 24.4 26.5 46.7  73.40418  32.9 -4.3 24.4 26.9 46.7  73.40419  31.6 -0.3 24.4 26.4 46.7  73.40420  34.2 -0.2 24.4 27.5 46.7  73.40421  32.5 -2.3 24.4 27.6 54.2  73.40422  32.1 -1.4 11.4 26.1 48.6  75.40423  32.6 -3.9 11.4 25.9 48.6  77.10424  32.7 -2.7 11.4 26.4 48.6  77.10425  30.7 1    11.4 26.4 48.6  77.10426  30.5 -6.3 11.4 23.1 48.6  77.10427  33   -4.1 11.4 24.2 50.6  71.40428  33.7 1.2  11.4 28   50.6  71.40492  33.4 -1.8 9.4  26   50.9  79.40430  32.9 1    9.4  26.3 50.9  79.40501  32.8 -0.8 9.4  27.1 50.9  79.40502  32   0.8  9.4  27   50.9  79.40503  34.8 1.1  9.4  27   50.9  79.40504  34   0    9.4  26.8 47.3  75.20505  32.9 -1.8 9.4  26.5 47.3  75.20506  32.7 0    9.4  26.5 48    76.70507  32.9 -3.7 9.4  27.1 48    76.70508  32.7 -2.9 9.4  26.2 48    76.70509  32.9 -3.9 9.4  25.1 48    76.70510  33.4 0.4  9.4  25.8 48    76.70511  32   -0.2 9.4  27.6 47.2  83.80512  27.4 -1.8 9.4  27.6 47.2  83.80513  32.3 -1.6 18.2 25.6 51.7  87.10514  32.9 -4.7 18.2 25.7 51.7  87.10515  33   -4.2 18.2 24.6 51.7  87.10516  32.8 -2.8 18.2 25.8 51.7  850517  32.8 -2.8 18.2 25.8 51.7  850518  32.8 -2.8 18.2 25.8 51.7  78.80519  36.4 0.5  18.2 26.8 51.7  78.8Average 32.3 -1.1 17.3 26.4 49.3  76.9__________________________________________________________________________           Heavy      LightDate  LCCO LCCO Catalytic Naphtha                      Catalytic Naphtha1987  90%  FBP  90%   FBP  RVP__________________________________________________________________________0330  513  562  344   413  18.60331  554  624  342   398  17.60401  561  616  340   402  15.30402  572  624  345   396  12.80403  592  652  352   392  15.90404  583  642  350   388  15.90405  570  633  329   371  15.90406  574  630  340   415  12.90407  579  632  349   409  13.30408  592  637  343   383  13.80409  590  635  344   375  15.10410  630  668  340   406  130411  604  670  356   400  13.10412  596  664  336   404  11.90413  600  654  341   381  15.30414  676  673  350   400  12.30415  592  654  342   386  15.30416  627  695  331   367  120417  596  662  338   374  13.50418  600  664  339   367  15.70419  575  633  352   389  15.90420  643  690  350   389  15.90421  576  639  347   387  11.20422  598  665  347   388  10.80423  600  673  349   395  13.40424  655  672  343   380  15.60425  607  636  352   420  15.60426  632  688  342   395  16.10427  603  682  326   384  13.70428  591  643  347   406  13.70429  618  676  361   472  13.10430  607  676  347   379  12.60501  595  652  338   395  12.30502  576  626  339   375  11.90503  595  650  339   399  11.10504  590  640  348   402  11.80505  598  660  348   4100506  601  667  355   382  120507  587  648  340   382  150508  619  676  345   389  14.50509  630  682  344   397  160510  610  667  348   385  16.40511  397  652  341   381  16.305120513  613  676  341   411  21.40514  601  696  331   360  20.70515  616  682  340   411  20.70516  609  665  349   376  20.70517  660  704  370   440  10.70518  587  646  352   411  14.90519  603  663  376   420  20.6Average 596  656  345   395  14.8__________________________________________________________________________  Feed  Feed            LCCO   DCO NaphthaDate   Sulfur        RAMS            Flash  Sulfur                       in LCCO1987   wt %  wt %            °F.                   wt %                       vol %__________________________________________________________________________0330   0.3   0.13            152        13.140331   0.29  0.13            158    1.37                       18.470401   0.33  0.26            158    1.38                       18.880402   0.28      168        13.930403                        18.980404   0.31  0.26            153    1.38                       140405   0.32  0.31            153    1.22                       17.750406   0.31  0.31            160    1.22                       16.870407   0.3   0.31            157    1.22                       17.360408   0.27  0.35           13.310409   0.27  0.35            171    1.16                       20.690410   0.27  0.35            171    1.16                       17.740411   0.58  0.35            164    1.16                       16.940412   0.58  0.35            161    1.25                       18.620413   0.28  0.35            165    1.25                       190414   0.3   0.35            166    1.25                       19.430415   0.25  0.21            161    1.17                       24.110416   0.25  0.21            141    1.17                       17.210417   0.26  0.21            156    1.17                       21.040418   0.28  0.21            154    1.17                       22.660419   0.28  0.33            157    1.35                       24.420420   0.29  0.33            165    1.35                       17.90421   0.27  0.33            166    1.35                       21.540422   0.26  0.23            166    1.27                       21.520423   0.29  0.23            160    1.27                       23.80424   0.29  0.23            156    1.27                       19.660425   0.3   0.23            154    1.27                       12.070426   0.37  0.25            166    1.27                       16.970427   0.29  0.25            158    1.27                       21.710428   0.29  0.25            156    1.27                       18.640429   0.29  0.25            160    1.27                       16.750430   0.22  0.25            158    1.27                       21.940501   0.25  0.25            154    1.27                       18.080502   0.27  0.25            157    1.27                       17.130503   0.25  0.3 151    1.35                       21.260504   0.22  0.3 157    1.35                       20.760505                        18.160506                        16.870507                        19.750508                        18.80509                        18.80510                        16.30511                        21.440512                        20.840513   0.28  0.26           19.870514                        19.870515   0.28      162    1.32                       19.410516   0.29      151    1.32                       17.940517   0.28      138    1.27                       19.220518   0.35      138    1.27                       190519   0.34      156    1.27                       18.7Average  0.30  0.27            158    1.27__________________________________________________________________________Propane-PropylenetoDate Fuel               Butane-Butylene1987 Wt %   Vol %           Wt %    Vol %                        Wt %__________________________________________________________________________0330 0.23   11.16           6.45    11.60                        7.910331 0.00   8.59           4.98    11.76                        8.040401 0.18   7.68           4.44    11.35                        7.730402 0.00   8.89           5.33    10.85                        8.600403 0.00   8.25           4.95    12.29                        9.740404 0.12   7.73           4.70    12.30                        8.450405 0.02   8.30           4.90    12.53                        8.670406 0.00   8.15           4.80    13.96                        9.630407 0.0    8.72           5.15    12.45                        8.630408 0.00   7.15           4.22    12.69                        8.790409 0.01   7.56           4.45    12.37                        8.550410 0.00   8.13           4.71    11.07                        7.550411 0.04   8.25           4.79    11.07                        7.560412 0.11   8.13           4.73    14.82                        10.150413 0.27   7.91           4.58    11.25                        7.670414 0.50   7.96           4.58    11.66                        7.900415 0.25   8.18           4.81    12.06                        8.120416 0.18   8.37           4.76    12.83                        8.360417 0.12   8.06           4.74    12.09                        8.130418 0.13   7.12           4.23    12.33                        8.380419 0.02   8.16           4.70    11.51                        7.780420 0.00   8.50           4.96    12.48                        8.550421 0.00   7.77           4.45    13.28                        8.930422 0.10   7.80           4.55    12.65                        8.480423 0.00   8.14           4.78    11.56                        7.790424 0.00   8.46           4.98    11.64                        7.860425 0.01   7.87           4.53    13.53                        9.200426 0.02   7.93           4.56    16.53                        11.230427 0.02   8.29           4.76    13.40                        9.100428 0.01   8.49           4.90    11.45                        7.820429 0.01   8.16           4.86    11.43                        7.760430 0.03   7.43           4.45    13.05                        8.910501 0.03   7.90           4.55    12.90                        8.740502 0.09   8.34           4.78    12.75                        8.610503 0.00   7.81           4.54    12.84                        8.810504 0.01   8.38           4.86    11.47                        7.860505 0.05   9.33           5.41    10.86                        7.440506 0.07   8.29           4.86    11.06                        7.510507 0.13   8.28           4.82    12.16                        8.210508 0.00   7.45           4.34    12.72                        8.580509 0.00   7.51           4.37    12.90                        8.710510 0.00   9.22           5.61    9.72 4.110511 2.35   7.90           4.58    20.06                        8.070512 0.32   6.97           3.94    11.52                        4.530513 0.00   7.86           4.32    11.63                        7.450514 0.01   8.23           4.76    12.75                        8.570515 0.00   8.63           5.05    12.47                        8.500516 0.18   9.15           5.39    11.17                        7.650517 0.30   8.55           5.03    11.03                        7.550518 0.29   7.55           4.34    10.78                        7.300519 0.58   7.70           4.56    12.89                        8.98__________________________________________________________________________Date     Lt Cat Gasoline                 Hvy Cat Gasoline 1987    Vol %        Wt %     Vol %                      Wt %__________________________________________________________________________0330     23.73        18.80    27.78                      25.420331     17.17        13.64    37.04                      33.990401     16.19        12.9     38.52                      34.50402     16.40        13.1     38.34                      34.40403     13.88        11.1     40.17                      36.00404     12.27        9.8      41.8 37.80405     12.17        9.8      41.59                      37.60406     12.52        10.0     40.62                      36.80407     14.57        11.6     38.61                      35.10408     14.99        12.0     37.59                      34.10409     13.78        10.9     38.08                      34.50410     16.18        12.6     36.26                      32.40411     16.84        13.1     36.34                      32.50412     15.65        12.1     34.44                      30770413     15.29        11.8     36.59                      32.60414     15.41        11.8     36.17                      32.10415     15.27        11.9     35.94                      32.30416     11.32        8.6      38.92                      33.80417     10.10        7.9      39.93                      35.80418     8.34        6.6      40.57                      36.80419     8.10        6.3      42.37                      38.10420     10.82        8.6      41.18                      37.50421     12.24        9.5      38.80                      33.30422     14.42        11.1     38.55                      34.10423     13.33        10.2     38.89                      34.60424     9.62        7.4      41.74                      37.20425     9.09        7.0      41.42                      37.20426     7.84        6.1      41.17                      36.90427     8.24        6.5      40.58                      35.90428     10.90        8.7      41.33                      36.80429     10.66        8.2      41.43                      36.80430     10.54        8.1      41.49                      37.00501     11.94        9.2      40.26                      35.70502     14.81        11.3     37.55                      33.20503     15.34        11.9     37.86                      34.00504     16.01        12.6     38.22                      34.90505     16.60        13.1     38.15                      34.80506     14.32        11.1     39.46                      35.50507     12.26        9.5      41.74                      37.40508     8.96        6.9      42.93                      38.40509     7.12        5.5      46.21                      41.40510     7.74        6.1      46.51                      42.40511     10.68        7.7      53.53                      46.70512     12.21        8.6      39.63                      33.80513     9.11        6.4      46.11                      38.60514     9.02        6.7      44.78                      39.40515     9.30        6.9      45.17                      40.30516     7.64        5.8      47.22                      42.30517     9.49        7.2      43.82                      39.30518     14.75        11.3     39.04                      34.50519     17.08        13.5     35.75                      32.5__________________________________________________________________________Date  LCCO     LCCO  HCCO               HCCO  Decanted Oil1987  Vol %     Wt %  Vol %               Wt %  Vol %                         Wt %__________________________________________________________________________0330  28.91     29.55 0.38               0.42  0.00                         0.000331  29.32     30.17 0.00               0.00  0.00                         0.000401  30.71     31.6  0.00               0.00  0.00                         0.000402  31.22     32.1  0.00               0.00  0.00                         0.000403  29.80     30.6  0.00               0.00  0.00                         0.000404  28.79     29.9  0.00               0.00  0.00                         0.000405  29.29     30.5  0.00               0.00  0.00                         0.000406  28.78     30.3  0.00               0.00  0.00                         0.000407  30.63     31.8  0.00               0.00  0.00                         0.000408  30.59     31.7  0.00               0.00  0.00                         0.000409  31.46     32.5  0.00               0.00  0.00                         0.000410  33.72     34.3  0.00               0.00  0.00                         0.000411  32.81     33.8  0.00               0.00  0.97                         1.210412  33.15     33.8  0.00               0.00  0.75                         0.940413  33.96     34.7  0.00               0.00  0.86                         1.060414  34.27     34.8  0.00               0.00  1.31                         1.630415  33.57     34.0  0.00               0.00  1.21                         1.490416  35.05     34.2  0.00               0.00  1.05                         1.260417  35.00     35.4  0.00               0.00  0.82                         1.010418  36.69     37.4  0.00               0.00  0.72                         0.910419  34.76     35.3  0.00               0.00  1.06                         1.290420  33.22     33.9  0.00               0.00  0.97                         1.200421  32.39     32.4  0.00               0.00  1.23                         1.520422  32.63     33.0  0.00               0.00  0.92                         1.130423  32.85     33.4  0.00               0.00  0.56                         0.700424  34.41     35.0  0.00               0.00  0.48                         0.600425  32.94     33.7  0.00               0.00  0.94                         1.150426  32.74     34.2  0.00               0.00  0.94                         1.210427  35.31     36.6  0.00               0.00  1.43                         1.810428  32.73     33.3  0.00               0.00  1.00                         1.220429  32.76     33.7  0.00               0.00  1.09                         1.360430  32.33     33.3  0.00               0.00  0.78                         0.960501  31.17     31.8  0.00               0.00  0.96                         1.190502  29.83     30.4  0.19               0.22  1.25                         1.530503  30.77     31.8  0.00               0.00  0.94                         1.160504  30.83     31.8  0.03               0.04  0.93                         1.160505  31.50     32.5  0.18               0.21  0.60                         0.760506  31.03     31.8  0.00               0.00  0.45                         0.550507  31.44     31.8  0.51               0.59  0.47                         0.600508  32.18     32.8  0.00               0.00  0.88                         1.100509  31.94     32.8  0.00               0.00  0.79                         1.000510  32.10     33.4  0.00               0.00  1.14                         1.410511  29.85     29.3  3.60               3.98  4.07                         4.830512  33.49     32.0  1.57               1.69  1.41                         1.660513  32.07     31.3  0.00               0.00  1.06                         1.250514  29.51     30.3  0.02               0.02  0.81                         1.030515  30.39     31.8  0.0 0.00  0.26                         0.340516  30.46     31.8  0.00               0.00  1.04                         1.320517  31.18     32.5  0.00               0.00  1.03                         1.310518  32.20     33.1  0.00               0.00  1.23                         1.550519  31.31     32.9  0.00               0.00  0.89                         1.12__________________________________________________________________________Date  Regen Total Air                Coke Burn                      Coke1987  SCFH           lb/hr Wt %__________________________________________________________________________0330  3273640        16832 5.140331  3285700        13996 3.760401  3256780        13168 3.550402  3188480        12995 3.490403  3201780        13049 3.450404  3156080        12855 3.470405  3160880        12861 3.470406  3147740        12919 3.550407  3148440        13443 3.650408  3221640        15030 3.530409  3185420        16096 3.830410  3243520        15444 3.630411  3236900        14734 3.570412  3250500        15556 3.710413  3261240        15603 3.630414  3274580        15573 3.600415  3276320        15240 3.580416  3210660        15729 3.680417  3338440        16579 4.020418  3228340        15906 3.920419  3308900        15959 3.820420  3311200        16134 3.960421  3425760        16798 3.940422  3235520        15571 3.660423  3456740        16191 3.780424  3414380        15620 3.640425  3425300        15846 3.890426  3062300        15271 4.090427  3309740        15830 3.660428  3358260        16066 3.730429  3381200        15824 3.600430  3429500        16333 3.850501  3395280        17120 4.030502  3325800        17320 4.070503  3296800        17884 4.310504  3292020        17710 4.250505  3308060        16722 4.010506  3356300        17123 4.050507  3513240        17172 4.060508  3491840        16147 3.760509  3476840        16254 3.810510  3102360        13978 3.270511  3206520        14272 6.300512  3308320        14653 3.880513  3160660        16027 3.670514  3406840        15977 3.820515  3278620        14710 3.570516  3261480        14886 3.580517  3286340        15150 3.660518  3236680        15697 3.680519  3245480        17648 4.72__________________________________________________________________________ Total      ConvertedDate  Gasoline      Barrels Total Products1987  B/D  B/D     B/D                 lb/hr                      vol %                          wt %__________________________________________________________________________0330  13367      17128   26872                 320013                      103.6                          97.70331  16024      20139   30704                 362631                      103.9                          97.40401  16049      19594   30643                 362142                      104.4                          97.60402  16118      18898   31124                 369966                      105.7                          99.40403  16162      20275   31214                 372781                      104.4                          98.60404  15987      19778   30400                 360207                      103.0                          97.20405  15899      20072   30720                 361991                      103.9                          97.60406  15406      19743   30157                 356165                      104.0                          97.80407  15622      19462   30841                 363068                      105.0                          98.60408  17878      21979   35025                 411669                      103.0                          96.60409  17310      22275   34462                 408789                      103.2                          97.40410  17469      20990   35093                 416222                      105.4                          97.90411  17234      20211   34441                 409904                      106.3                          99.30412  16397      20632   35005                 417006                      106.9                          99.50413  17307      20741   35316                 426958                      105.9                          99.40414  17254      20551   35723                 432944                      106.8                          100.00415  16915      21276   35094                 421607                      106.2                          99.10416  16150      19258   34568                 416605                      107.5                          97.40417  16014      19861   33925                 411527                      106.0                          99.70418  15543      19454   33611                 411071                      105.8                          101.30419  16351      20596   34330                 416807                      105.9                          99.90420  16661      19975   34341                 413336                      107.2                          101.50421  16808      21232   34809                 413253                      105.7                          97.00422  17434      21267   35207                 425925                      107.0                          100.00423  17361      21902   35016                 426571                      105.3                          99.60424  17166      20890   35546                 431039                      106.3                          100.40425  16119      19189   33763                 409443                      105.8                          100.50426  14298      18233   31259                 384769                      107.2                          103.10427  16491      20686   36229                 443603                      107.2                          102.60428  17687      21386   35860                 431825                      105.9                          100.20429  17981      21466   36430                 439814                      105.5                          100.00430  17406      21846   35337                 426705                      105.6                          100.60501  17418      21581   35077                 419518                      105.1                          98.70502  17431      21673   34866                 414844                      104.7                          97.40503  17522      21880   34770                 415321                      105.6                          100.10504  17888      21820   34926                 420638                      105.9                          101.00505  18050      21286   35352                 424052                      107.2                          101.80506  17843      21570   34707                 418308                      104.6                          98.80507  17783      24149   35193                 425006                      106.9                          100.50508  17363      21409   35174                 426911                      105.1                          99.30509  17721      21389   35382                 431540                      106.5                          101.20510  18424      21278   36143                 426546                      106.4                          99.70511  10992        22281                 2670060512  14436      16898   29785                 354140                      107.0                          93.90513  17951      20913   35061                 421863                      107.8                          96.60514  17588      22021   34365                 410009                      105.1                          98.00515  17783      21874   34678                 411592                      106.2                          99.80516  18170      21624   35335                 420672                      106.7                          101.10517  17558      21423   34611                 413877                      105.1                          100.00518  18021      21300   35359                 423672                      105.5                          99.20519  15930      19566   31851                 384495                      105.6                          102.8Average 16740      20638   33686                 404046                      105.7                          99.3__________________________________________________________________________              Through-              putDate    Conv       Ratio                   Energy Index1987    vol %      (TPR)                   MBTU/bbl__________________________________________________________________________0330    66.0       1.14 3620331    68.1       1.12 3030401    66.8       1.10 2890402    64.2       1.10 2810403    67.8       1.09 2770404    67.0       1.10 2810405    67.9       1.08 2770406    68.1       1.09 2810407    66.2       1.09 2870408    64.6       1.08 2720409    66.7       1.11 2900410    63.0       1.09 2840411    62.4       1.06 2820412    63.0       1.07 2840413    62.2       1.06 2800414    61.4       1.06 2830415    64.4       1.06 2840416    59.9       1.06 2920417    62.1       1.07 3010418    61.2       1.08 2940419    63.6       1.08 2930420    62.3       1.08 2990421    64.5       1.08 3000422    64.6       1.07 2890423    65.9       1.06 2950424    62.5       1.06 2870425    60.1       1.07 3010426    62.5       1.06 3160427    61.2       1.0  2860428    63.2       1.07 2890429    62.2       1.06 2810430    65.3       1.07 2890501    64.7       1.06 3020502    65.1       1.11 3040503    66.4       1.07 3140504    66.1       1.13 3130505    64.6       1.09 3020506    65.0       1.07 3120507    65.0       1.07 3120508    64.0       1.06 3000509    64.4       1.06 2980510    62.7       1.07 2720511               1.07 5450512    60.7       1.12 3130513    64.3       1.08 2960514    67.4       1.04 2970515    67.0       1.05 2810516    65.3       1.06 2810517    65.1       1.04 2870518    63.6       1.07 2900519    64.9       1.08 342Average 64.3       1.08 299__________________________________________________________________________ 
    
     Among the many advantages of the novel catalytic cracking process are: 
     1. Outstanding ability to refine petroleum and produce gasoline without the use of a pipestill(s), atmospheric tower, and/or vacuum tower. 
     2. Superior processing of whole crude oil. 
     3. Excellent production of gasoline and other hydrocarbons. 
     4. Enhanced catalytic cracking of petroleum. 
     5. Good throughput. 
     6. Cost effective. 
     7. Convenient. 
     8. Safe. 
     9. Efficient. 
     10. Effective. 
     Although embodiments of the invention have been shown and described, it is to be understood that various modifications, additions, and substitutions, as well as rearrangements of process steps, can be made by those skilled in the art without departing from the novel spirit and scope of this invention.