Abstract: A process for catalytic multi-stage hydrogenation of heavy carbonaceous feedstocks using catalytic ebullated bed reactors is operated at selected flow and operating conditions so as to provide improved reactor operations and produce increased yield of lower boiling hydrocarbon liquid and gas products. The disclosed process advantageously takes advantage of an external gas/liquid separation unit associated with the first stage reactor to allow for a more efficient and effective catalytic hydrocracking process. The more efficient process is primarily a result of the increased catalyst loading and lower gas hold-up in the ebullated reactors.

Abstract: An integrated hydrotreating/hydrocracking process employs two hydrotreating catalysts of different relative activities in sequence to provide improved products. A more active second catalyst is employed after the first hydrotreating catalyst. The jet fuel fraction recovered from the effluent of the downstream hydrocracking reaction zone has a reduced aromatic hydrocarbon content compared to the prior art.

Abstract: Petroleum wax feeds are converted to high viscosity index lubricants by a two-step hydrocracking-hydroisomerization process in which the wax feed which exhibits branchingis initially subjected to hydrocracking under mild conditions with a conversion to non-lube range products of no more than about 30 weight percent of the feed. The hydrocracking is carried out at a hydrogen pressure of at least 1000 psig (7000 kPa) using an amorphous catalyst which preferentially removes the aromatic components present in the initial feed. The hydrocracked effluent is then subjected to hydroisomerization in a second step using a low acidity zeolite beta catalyst which effects a preferential isomerization on the paraffin components to less waxy, high VI isoparaffins. The second stage may be operated at high pressure by cascading the first stage product into the second stage or at a lower pressure, typically from 200 to 1000 psig.

Abstract: A process for hydrocracking heavy hydrocarbon feeds using a catalyst composition containing a hydrogenation/dehydrogenation component, such as a noble metal, and an acidic solid component including a Group IVB metal oxide modified with an oxyanion of a Group VIB metal. The hydrocracking product has high isoparaffin to normal paraffin ratios and with minimal ethane and methane byproducts at high conversions. The hydrocracking step is useful in processes for producing high quality lubricating oil basestocks, along with naphtha and distillate products.

Abstract: A two stage hydrocracking process is characterized by operation of the second hydrocracking zone at a reduced pressure, which is conducive to cracking the highly paraffinic effluent of the first hydrocracking zone. The process is also characterized by the passage of the partially compressed hydrogen makeup gas stream into the second hydrocracking zone followed by compressing the gas recovered from the second hydrocracking zone effluent to form the makeup gas to the first stage hydrocracking zone. There is no recycle gas stream for the second hydrocracking zone.

Abstract: A process for reverse gas flow to obtain high conversion, selective hydrotreating and product selectivity in hydroprocessing reactor systems is disclosed. In the integrated process, hydrogen recovered from a hydrotreating reactor is purified and used as a source of hydrogen for a hydrocracking reaction zone. Hydrogen recovered from the hydrocracking reaction zone is recovered without substantial cooling and used as a source of hydrogen for the hydrotreating reaction zone.

Abstract: Petroleum waxes are converted to high viscosity index lubricants by a hydroisomerization process in which the wax feed is subjected to hydroisomerization over a low acidity molecular sieve isomerization catalyst (the molecular sieve being preferably a zeolite) which effects a preferential isomerization on the paraffin components in the feed to less waxy, high VI isoparaffins. The hydroisomerization is operated at high pressure, at least 1000 psig hydrogen partial pressure (reactor inlet) using a zeolite catalyst, preferably a noble metal containing zeolite beta catalyst which contains boron as a framework component of the zeolite to give a low alpha value, typically below 10. The hydroisomerization is carried out at with a 650° F.+ conversion in the range of 10 to 40 weight percent of the feed. A final dewaxing step to target pour point may be used with relatively low loss, typically no more than 15 weight percent, during this dewaxing.

Abstract: A catalytic hydrocracking process wherein a denitrification and desulfurization reaction zone effluent is heat-exchanged with a hydrogen-rich gaseous stream and introduced into a hydrocracking zone. The resulting effluent from the hydrocracking zone is passed directly without cooling into a hot, high-pressure stripper utilizing a hot, hydrogen-rich gaseous stream at least a portion of which is heated during the heat exchange with the denitrification and desulfurization reaction zone effluent. The stripper overhead is partially condensed to produce a hydrogen-rich gaseous stream and a liquid stream containing hydrocracked hydrocarbon compounds. At least a portion of the stripper bottoms is recycled to the denitrification and desulfurization reaction zone.

Abstract: A hydroprocessing process includes a cocurrent flow liquid reaction stage, a countercurrent flow liquid reaction stage and a vapor reaction stage in which feed components are catalytically hydroprocessed by reacting with hydrogen. Both liquid stages both produce a liquid and a vapor effluent, with the cocurrent stage liquid effluent the feed for the countercurrent stage and the countercurrent stage liquid effluent the hydroprocessed product liquid. Both liquid stage vapor effluents are combined and catalytically reacted with hydrogen in a vapor reaction stage, to form a hydroprocessed vapor. This vapor is cooled to condense and recover a portion of the hydroprocessed hydrocarbonaceous vapor components as additional product liquid. The uncondensed vapor is rich in hydrogen and is cleaned up if necessary, to remove contaminants, and then recycled back into the cocurrent stage as hydrogen-containing treat gas.

Abstract: A gas conversion process including catalytic hydrocarbon synthesis from a synthesis gas comprising a mixture of H.sub.2 and CO, produces hydrogen from the synthesis gas and upgrades synthesized hydrocarbons by one or more hydroconversion operations which utilize this hydrogen. The hydroconversion also produces a hydrogen rich tail gas which is used in the process for at least one of (i) hydrocarbon synthesis catalyst rejuvenation, (ii) the hydrocarbon synthesis, and (iii) hydrogen production. In one embodiment the tail gas is used to hydrodesulfurize sulfur-containing hydrocarbon liquids recovered from the natural gas used to form the synthesis gas. The hydrogen production is accomplished by physical separation, such as PSA, with or without chemical means such as a water gas shift reaction.

Abstract: A process for converting a heavy hydrocarbon fraction comprises treating the hydrocarbon feed in a hydrodemetallization section, the section containing at least one fixed bed hydrodemetallization catalyst.

Abstract: A hydrocracking process wherein a hydrocarbonaceous feedstock and a hot hydrocracking zone effluent containing hydrogen is passed to a denitrification and desulfurization reaction zone to produce hydrogen sulfide and ammonia to thereby clean up the fresh feedstock. The resulting hot, uncooled effluent from the denitrification and desulfurization zone is hydrogen stripped in a stripping zone maintained at essentially the same pressure as the preceding reaction zone with a hydrogen-rich gaseous stream to produce a vapor stream comprising hydrogen, hydrocarbonaceous compounds boiling at a temperature below the boiling range of the fresh feedstock, hydrogen sulfide and ammonia, and a liquid hydrocarbonaceous stream.

Abstract: A process to provide a multiplicity of hydrocracking reaction zones containing hydrocracking catalyst wherein the catalyst is rejuvenated or reactivated while the process unit remains on-stream by the periodic exposure of partially spent catalyst to hot recycle gas containing hydrogen. The hydrocracking catalyst always operates at "near" fresh activity and selectivity thereby resulting in more stable temperature, yield and product quality performance.

Abstract: A process for hydroprocessing middle distillate petroleum streams in two temperature stages. The feedstream is hydroprocessed in two or more first temperature stages operated at a temperature from about 360.degree. C. to about 450.degree. C. The reaction product of the first temperature stage(s) is quenched to a temperature from about 260.degree. C. to about 350, stripped of H.sub.2 S, NH.sub.3 and other dissolved gases, then sent to the second temperature stage which is operated at said quenched temperature range. The product from the second temperature stage is also stripped of dissolved gases. Color bodies produced in the higher temperature first stage are hydrogenated in the last stage.

Abstract: A refinery stream such as a VGO is hydrocracking in a hydrocracking reaction zone within an integrated hydroconversion process. Effluent from the hydrocracking reaction zone is combined with a second refinery stream, and the blended stream hydrotreated in a hydrotreating reaction zone. The hydrocracked effluent serves as a heat sink for the hydrotreating reaction zone. The integrated reaction system provides a single hydrogen supply and recirculation system for use in two reaction systems.

Abstract: An integrated process for treating pyrolysis gasolines by depentanizing the pyrolysis gasoline in a first distillation column reactor which also subjects the C.sub.5 fraction to selective hydrogenation of acetylenes and diolefins. The bottoms or C.sub.6 + material is then subjected to further distillation in a second distillation column reactor to remove either a C.sub.6 and lighter or C.sub.8 and lighter overheads which contains a benzene/toluene/xylene (BTX) concentrate while at the same time removing mercaptans and selectively hydrogenating the diolefins. The BTX concentrate is then subjected to hydrodesulfurization prior to aromatics extraction and separation of the benzene from the toluene and xylene. Concurrently with the benzene separation any remaining olef ins are saturated to remove the color bodies. Finally the heavy gasoline fraction is subjected to the concurrent catalytic removal of mercaptans and separation to remove the heaviest material.

Abstract: A process for catalytic hydrodewaxing of a wax-containing feed wherein the feed is subjected to hydrodewaxing conditions in a first reaction zone containing a wax-cracking catalyst, the effluent from the first reaction zone is charged to a second reaction zone containing a hydrotreating catalyst that produces an exothermic reaction and the effluent from the second reaction zone is charged to a third reaction zone containing a wax-cracking catalyst, the exothermic reaction in the second reaction zone effecting heating of the effluent, which is charged to the third reaction zone.

Abstract: Process for the preparation of lubricating base oils comprising the steps of(a) contacting a hydrocarbon oil feed in the presence of hydrogen in a first reaction zone with a catalyst comprising at least one Group VIB metal component and at least one non-noble Group VIII metal component supported on a refractory oxide carrier;(b) separating the effluent at elevated pressure into a gaseous fraction and a liquid fraction having a sulphur content of less than 1000 ppmw and a nitrogen content of less than 50 ppmw;(c) contacting the liquid fraction in the presence of hydrogen in a second reaction zone with at least a catalyst comprising a noble metal component supported on an amorphous refractory oxide carrier; and(d) recovering a lubricating base oil having a viscosity index of at least 80.

Abstract: A gas conversion process in which both hydrocarbons and hydrogen are produced from a synthesis gas feed which comprises a mixture of H.sub.2 and CO, uses hydrogen from a portion of the feed for one or more of (i) hydrocarbon synthesis catalyst rejuvenation and (ii) hydroconversion upgrading of at least a portion of the synthesized hydrocarbons. Hydrogen is produced from a slipstream of the synthesis gas fed into the hydrocarbon synthesis reactor by one or more of (i) physical separation means such as pressure swing adsorption and (ii) chemical means such as a water gas shift reactor. If a shift reactor is used due to insufficient capacity of the synthesis gas generator, physical separation means such as pressure swing adsorption will still be used to separate a pure stream of hydrogen from the shift reactor gas effluent.

Abstract: A method and reactor for catalytic hydroprocessing liquid hydrocarbon feedstock at elevated temperatures and pressures for producing a liquid hydrocarbon product involves introducing the feedstock into a reactor having upper and lower reaction zones, each reaction zone having a hydroprocessing catalyst bed therein, the feedstock being introduced at the top of the lower reaction zone for downward flow through and reaction within the catalyst bed therein; collecting a partially reacted liquid effluent from the lower reaction zone; pumping the partially reacted liquid effluent to and introducing it at the top of the upper reaction zone for downward flow through and reaction within the catalyst bed therein; introducing hydrogen gas at the top of the upper reaction zone for flow downwardly and sequentially through and over the catalyst beds in the upper and lower reaction zones in co-current contact with the liquid in the reaction zones, the hydrogen reacting with the liquid in the reaction zones whereby the liqui

Abstract: There is provided a hydrocracking process using a catalyst comprising a hydrogenation/dehydrogenation component, such as a noble metal, and an acidic solid component comprising a Group IVB metal oxide modified with an oxyanion of a Group VIB metal. An example of this catalyst is zirconia, modified with tungstate and platinum. This catalyst is used to selectively hydrocrack naphtha range hydrocarbons to reduce the endpoint of reformulated gasolines.

Abstract: A process for upgrading a liquid petroleum or chemical stream wherein said stream flows countercurrent to the flow of a treat gas, such as a hydrogen-containing gas, in at least one reaction zone. The reaction vessel used in the practice of the present invention contains vapor and optionally liquid passageway means to bypass one or more catalyst beds. This permits more stable and efficient reaction vessel operation.

Abstract: A hydrocracking process wherein a hydrocarbonaceous feedstock and a hot hydrocracking zone effluent containing hydrogen is passed to a denitrification and desulfurization reaction zone to produce hydrogen sulfide and ammonia to thereby clean up the fresh feedstock. The resulting hot, uncooled effluent from the denitrification and desulfurization zone is hydrogen stripped in a stripping zone maintained at essentially the same pressure as the preceding reaction zone with a hydrogen-rich gaseous stream to produce a vapor stream comprising hydrogen, hydrocarbonaceous compounds boiling at a temperature below the boiling range of the fresh feedstock, hydrogen sulfide and ammonia, and a liquid hydrocarbonaceous stream.

Abstract: This invention discloses a process for producing a high Viscosity Index lubricant having a VI of at least 125 from a waxy hydrocarbon feed having a wax content of at least 40 wt %. The process comprises catalytically dewaxing waxy paraffins present in the feed by isomerization in the presence of hydrogen and in the presence of a low acidity large pore zeolite isomerization catalyst. This catalyst has a ratio of SiO.sub.2 /Al.sub.2 O.sub.3, as synthesized, of at least 50:1, and an alpha value of not greater than 20, wherein the catalyst is prepared in the absence of boron. The catalyst further comprises a noble metal hydrogenation component. The feed may be hydrocracked prior to dewaxing with the large pore zeolite. The feed may be solvent dewaxed prior to isomerization. The effluent of the isomerization step may also be further dewaxed by either solvent or catalytic means in order to achieve target pour point.

Abstract: The present invention relates to new crystalline zeolite SSZ-39 prepared using a cyclic or polycyclic quaternary ammonium cation templating agent.

Abstract: A process for producing normally gaseous olefins from two different process units sharing common downstream quench and fractionation facilities, wherein one of the process units is a short contact time mechanically fluidized vaporization unit for processing petroleum residual feedstocks and the other is a conventional steam cracking unit.

Abstract: Process for reducing the wax content of wax-containing hydrocarbon feedstocks to produce middle distillate products including low freeze point jet fuel and/or low pour point and low cloud point diesel fuel and heating oil. The process involves contacting the feedstock with a hydrocracking catalyst containing a carrier, at least one hydrogenation metal component of Group VIB and Group VIII metals, and a large pore zeolite such as a Y type zeolite, in a hydrocracking zone in the presence of hydrogen at elevated temperature and pressure, and contacting the entire effluent from the hydrocracking zone with a dewaxing catalyst containing a crystalline, intermediate pore size molecular sieve selected from metallosilicates and silicoaluminophosphates in a hydrodewaxing zone in the presence of hydrogen at elevated temperature and pressure.

Abstract: An apparatus for mixing vapor and liquid reactants within a column. The apparatus forms a first mixing zone into which a first reactant (e.g., vapor) is homogenized by swirl flow and flows vertically downward. The apparatus further forms a second mixing zone into which a second reactant (e.g., liquid) is homogenized by swirl flow and flows vertically downward. Additional amounts of either the first reactant, the second reactant or both may be added into or ahead of the first mixing zone or the second mixing zone as appropriate. The first reactant is directed radially to collide in crossflow with a thin sheet of the second reactant to provide intense mixing of the first and second reactants. Due to separate mixing zones for the two reactants, the mixing conditions for each can be tailored to best mix each reactant while minimizing pressure drop and minimizing the space and volume requirements for this mixing.

Abstract: The safety, convenience and environmental acceptability of starting a two-stage hydrocracking process unit is increased by employing aqueous ammonia as a selective catalyst poison. The aqueous ammonia is injected into the recycle gas system of the hydrocracking process. The invention eliminates the possibility of forming a large airborne cloud of ammonia gas upon an accidental release of the ammonia stream as is possible with the injection of anhydrous ammonia. The invention also stabilizes the operation of the unit through the use of a maintenance injection rate sufficient to maintain an inlet ammonia content above about 40 ppm.

Abstract: A process for converting a Fischer-Tropsch light oil stream to jet fuel by reacting said stream with a hydroisomerization catalyst in a reaction zone where the stream flows countercurrent to upflowing hydrogen-containing treat gas.

Abstract: This invention discloses a process for producing a high Viscosity Index lubricant having a VI of at least 125 from a waxy hydrocarbon feed having a wax content of at least 40 wt %. The process comprises catalytically dewaxing waxy paraffins present in the feed by isomerization in the presence of hydrogen and in the presence of a low acidity large pore zeolite isomerization catalyst. This catalyst has a ratio of SiO.sub.2 /Al.sub.2 O.sub.3, as synthesized, of at least 50:1, wherein the catalyst is prepared in the absence of boron. The alpha value of the catalyst is no greater than 20. The catalyst comprises a noble metal hydroisomerization catalyst such as Pt. The feed may be hydrocracked prior to dewaxing with the large pore zeolite. The effluent of the process may also be further dewaxed by either solvent or catalytic means in order to achieve target pour point.

Abstract: A process for converting Fischer-Tropsch wax streams to lubricants by reacting said stream with a dewaxing catalyst in a reaction zone where the stream flows countercurrent to upflowing hydrogen-containing treat gas.

Abstract: The present invention relates to new crystalline zeolite SSZ-44 prepared by processes for preparing crystalline molecular sieves, particularly large pore zeolites, using a N,N-diethyl-cis-2,6-dimethyl piperidinium cation templating agent.

Abstract: A process for the production of diesel fuel with a high cetane number at a low cloud point, which involves hydrocracking highly aromatic fractions obtained from catalytic cracking operations. The fraction of hydrocracker effluent which boils between about 400.degree. F. (205.degree. C.) and 1000.degree. F. (538.degree. C.) is subsequently catalytically dewaxed in order to obtain a cloud point of no more than 41.degree. F. (5.degree. C.). The hydrocracker effluent fraction is preferably recycled to the hydrocracking step prior to dewaxing.

Abstract: The invention is a hydrocracking process which produces an increased amount of hydrocarbons useable as diesel fuel by isomerization of high boiling paraffins using a dewaxing catalyst. The process is characterized by the use of a dewaxing catalyst containing a very small amount of a non-noble metal hydrogenation component such as nickel on an intermediate pore nonzeolitic molecular sieve (NZMS) material. This dewaxing catalyst has been found to be very effective in reducing the pour point of a diesel boiling range distillates even in the presence of sulfur levels which adversely affect catalysts containing higher amounts of the same metal component.

Abstract: A tri-elemental catalyst on a support that includes a pentasil crystalline zeolite and is suitable for hydrocracking and hydrogenation of aromatics-containing petroleum hydrocarbon feedstocks such as hydrotreated cracked feedstock, virgin feedstock, vacuum distillate, middle distillate, mixtures thereof, and the like, is disclosed. The catalyst is suitable for hydrodesulfurization as well as hydrodenitrogenation, thus the feedstock can contain sulfur and nitrogen in addition to the aromatic components. Hydrocracking and aromatics hydrogenation of the petroleum hydrocarbon feedstocks is accomplished under a relatively wide range of process conditions in plural process zones using the tri-elemental catalyst that contains a catalytically active metal phase constituted by a Group VI-B element, a Group VIII first transition series element and a Group VIII second transition series element.

Abstract: A process for the joint production of middle distillates and oil bases (viscosity index between 95 and 150) particularly from vacuum distillates and/or deasphalted oils, comprises a first step in which the feedstock is brought into contact with an amorphous catalyst containing at least one metal or metallic compound with a hydro-dehydrogenating function, such as Ni, Mo, W or Co, at a temperature of between 350.degree. C. and 430.degree. C., a pressure of between 5 and 20 MPa, a space velocity of between 0.1 and 5 h.sup.-1 in the presence of hydrogen in a ratio H.sub.2 /HC of 150 to 2,000 by volume. The product from the first step is brought into contact in a second step with a second catalyst comprising a support, a Y zeolite, at least one group VIB element and at least one group VIII metal at a temperature of between 350.degree. C. and 430.degree. C., a pressure of between 5 and 20 MPa and a space velocity of between 0.1 and 5 h.sup.-1.

Abstract: A process is provided for converting a hydrocarbon feedstock comprising the steps of introducing the hydrocarbon feedstock to a first hydroconversion zone at superatmospheric pressure and at a temperature between about 450.degree. F. and about 850.degree. F. in the presence of hydrogen, the hydrogen flowing in a countercurrent relationship to the hydrocarbon feedstock, to form a hydrogen-rich vapor effluent and a hydrocarbon-rich liquid effluent; reacting the hydrogen-rich vapor effluent in a second hydroconversion zone to form a converted vapor effluent; and introducing a portion of the hydrocarbon-rich liquid effluent to the second hydroconversion zone in countercurrent relationship to the hydrogen-rich vapor effluent. By recycling to the second hydroconversion zone a stream having sufficiently high boiling range that it remains a liquid, a greater range of operating conditions are possible in the second hydroconversion zone, thus allowing for higher conversions and product yields.

Abstract: A process for the simultaneous replacement of a first catalyst by a second catalyst which first catalyst is circulating as a moving bed of solid particles in a hydrocarbon treating unit, which unit comprises at least one processing reactor. The first catalyst is withdrawn downstream of the reactor, or of each reactor, in the direction of catalyst circulation. The second catalyst is simultaneously injected upstream of the reactor or of each reactor. The bulk density of the material withdrawn downstream of the reactor, or of each reactor, is measured continuously. The withdrawal of the first catalyst and the injection of the second catalyst into the reactor concerned are interrupted when the bulk density so measured is equal to that of the second catalyst.

Abstract: This invention relates to a process for cracking waste polymers in a fluidized bed reactor to produce vaporous products comprising primary products which can be further processed, eg in a steam cracker to produce olefins, characterized in that the vaporous products are treated to generate a primary product substantially free of a high molecular weight tail having molecular weights >700 prior to further processing. The removal of the high molecular weight tail minimizes fouling and prolongs the lifetime of the reactors used for further processing.

Abstract: A diesel or jet fuel distillate product is recovered from a hydrocracking process in an integrated flowscheme wherein the distillate is removed from the hydrocracking zone product column and then passed into a catalytic dewaxing zone. The once-through hydrogen provided in the catalytic dewaxing zone is the makeup hydrogen for the hydrocracking zone. Large economies are realized in terms or reduced capital costs compared to the conventional flowscheme. In addition the severity of the hydrocracking operation is reduced thus extending the life of the hydrocracking catalyst.

Abstract: Charge waxy hydrocarbon is converted to lube oil base stock by hydrotreating in the presence of catalyst characterized by its ability to convert a waxy hydrocarbon distillate of high pour point to a hydrocarbon product of reduced pour point and high viscosity index, suitable for use as a lube oil base stock, which comprises a support containing about 2-50 w % silica and 50-98 w % alumina, bearing 2-10 w % of a non-noble Group VIII metal, as metal, metal oxide, or metal sulfide, about 8-20 w % of a Group VI-B metal, as metal, metal oxide, or metal sulfide, less than 0.5% halogen; and 0-2 w % of phosphorus, the atom ratio of Group VIII metal to Group VI-B metal being about 0.3-2:1, said catalyst being characterized by a micropore mode of about 60-130 .ANG. diameter, a Total Surface Area of about 150-300 m.sup.2 /g, a Total Pore Volume of about 0.45-0.9 cc/g and a Pore Volume of pores with pore diameter >500 .ANG. of about 0.02-0.25 cc/g.

Abstract: Heavy oils are advantageously preconditioned by heat soaking prior to hydrotreating with a dispersed metal catalyst to reduce coking in a two stage hydrotreating process. The effluent of a hydrotreating process is filtered to recover catalytically active coke which is recovered by backflushing and recycled to the feed stream. A mild solvent deasphalting step isolates metals in a reduced volume asphaltene fraction.

Abstract: High quality lubricating oil base stocks are produced from crude oils that contain significant concentrations of aromatic compounds in their higher boiling fractions. First, the crude is fractionated. After the residua fraction has been deasphalted, it is combined with the gas oil fraction. The resultant combined fraction is hydrocracked. The hydrocrackate is separated into a light fraction and a heavy fraction. The heavy fraction is hydrodewaxed, then hydrofinished. The hydrofinished product is combined with the light fraction and distilled into products including middle distillate fuel products and lubricating oil base stocks. The lubricating oil base stocks have high VI.

Abstract: A reactivated catalyst having optimum activity for hydrocracking and other acid catalyzed chemical conversion processes is prepared by contacting its deactivated counterpart, which contains a crystalline molecular sieve, a Group VIII noble metal hydrogenation component and carbonaceous deposits, with a gas containing molecular oxygen, preferably air, at a temperature between 950.degree. and 1200.degree. F., preferably between about 1050.degree. and 1150.degree. F., for a time sufficient to remove at least a portion of the carbonaceous deposits. When the reactivated catalyst contains a dealuminated Y zeolite that has been ion-exchanged with both noble metal and rare earth metal cations, its activity for hydrocracking in an ammonia-deficient atmosphere can be further increased by a rejuvenation procedure in which the reactivated catalyst is contacted with an aqueous ammonia solution in which an ammonium salt has been dissolved.

Abstract: The present invention provides a process for hydrodelayed thermal cracking in combination with hydrostripping, which comprises feeding crude oil from a surge tank to a crude oil stripper via a feed line; separating the crude oil into a lighter fraction and a heavier fraction in the crude oil stripper; subjecting the lighter fraction to hydrodesulfurization; feeding the heavier fraction from the crude oil stripper to a first storage tank; hydrothermally cracking the heavier fraction for at least 10 minutes under a hydrogen pressure in the first storage tank; introducing a bottom residue of the first storage tank into a second storage tank or the feed line, and subjecting a cracked and vaporized fraction of the first storage tank to hydrodesulfurization; hydrothermally cracking the residue introduced into the second storage tank under a higher hydrogen pressure than the hydrogen pressure of the first storage tank; subjecting a portion of a bottom residue of the second storage tank to hydrodemetallization, hydro

Abstract: Low sulfur gasoline of relatively high octane number is produced from a catalytically cracked, sulfur-containing naphtha by hydrodesulfurization followed by treatment over an acidic catalyst, modified to reduce surface acidity, and preferably an intermediate pore size zeolite such as ZSM-5. The treatment over the acidic catalyst in the second step restores the octane loss which takes place as a result of the hydrogenative treatment and results in a low sulfur gasoline product with an octane number comparable to that of the feed naphtha. In favorable cases, using feeds of extended end point such as heavy naphthas with 95 percent points above about 380.degree. F. (about 193.degree. C.), improvements in both product octane and yield relative to the feed may be obtained.

Abstract: Hydrocarbon lube boiling range stock of high Pour Point may be catalytically hydrotreated to yield a product of high viscosity index and reduced Pour Point which is suitable as a lube base oil.

Abstract: Heavy oils are simultaneously subjected to hydrocracking and dewaxing using a catalyst based on zeolite beta together with a hydrogenation component. The process is able to effect a bulk conversion of the oil while, at the same time, yielding a low pour point product.

Abstract: A process for making a lubricant oil of low pour point and improved oxidation stability by catalytically hydro-dewaxing a lube chargestock containing paraffin wax in a vertical column reactor having a cascade series of fixed downflow catalyst beds over dewaxing catalyst comprising acid medium pore size zeolite. The treatment is carried out by selectively hydrodewaxing paraffinic wax contained in the liquid petroleum in a first serial catalyst bed under adiabatic cracking temperature conditions while controlling adiabatic exothermal heat of reaction within a 30.degree. C. maximum excursion from the initial reaction temperature, thereby producing lighter olefinic components, recovering partially hydrodewaxed liquid petroleum from a bottom portion of the first serial catalyst bed, and redistributing said partially hydrodewaxed liquid petroleum for contact with said catalyst in at least one downstream fixed catalyst bed.