WO1994025157A1 - A method of treating spontaneously combustible catalysts - Google Patents

Abstract

Self-heating characteristics of a spontaneously combustible catalyst are reduced by treating the catalyst with an oxygen-containing hydrocarbon having at least 12 carbon atoms. The treatment is particularly suitable for reducing the self-heating characteristics of sulfidable metal oxide(s)-containing catalysts, presulfurized catalysts, presulfided catalysts or reduced catalysts. When applied to sulfur-containing catalysts, the treatment gives a catalyst that has suppressed self-heating properties without substantially compromising sulfur retention or activity. Further hydrocracking catalysts treated by the oxygen-containing hydrocarbons give improved product yield. Further, a method of safely unloading a catalyst from a reactor is provided where the catalyst in the reactor is treated with a liquid mixture containing the oxygen-containing hydrocarbon to wet the catalyst.

Description

A METHOD OF TREATING SPONTANEOUSLY COMBUSTIBLE CATALYSTS

This invention relates to a method of treating spontaneously combustible catalysts and catalyst compositions resulting from such treatment. In one aspect, the invention relates to a process for preparing catalysts that produces catalyst compositions with reduced self-heating characteristics. In another aspect, the invention relates to hydrotreating and/or hydrocracking processes.

A spontaneously combustible catalyst is any catalyst composition which has a tendency to self-heat or combust in the presence of air or oxygen at a temperature of 200°C or lower. Particularly, many hydrocarbon processing catalysts, such as hydrotreating, hydrocracking and tail-gas treating catalysts which typically contain sulfur and reduced catalysts such as hydrogenation catalysts can be classified as spontaneously combustible catalysts. Some of the hydrocarbon processing catalysts can also be reduced catalysts.

A hydrotreating catalyst is used to catalyze the hydrogenation of hydrocarbon feedstocks, and most particularly to hydrogenate particular components of the feedstock, such as sulfur-, nitrogen- and metals-containing organo-compounds and unsaturates. A hydrocracking catalyst is used to crack large and complex petroleum derived molecules to attain smaller molecules with the concomitant addition of hydrogen to the molecules. Such hydrocracking catalyst includes catalysts used for residue conversion units. A tail gas catalyst is used to catalyze the conversion of hazardous effluent gas streams to less harmful products, and most particularly to convert oxides of sulfur to hydrogen sulfide which can be recovered and readily converted to elemental sulfur. A reduced catalyst is any catalyst that contains a metal in the reduced state such as an olefin hydrogenation catalyst. Such metals are typically reduced with a reducing agent such as hydrogen or formic acid. The metals on these reduced catalyst may be fully reduced or partially reduced. Hydrogenation catalysts are well known and several are commercially available. Typically, the active phase of the catalyst is based on at least one metal of group VIII, VIB, IVB, IIB or IB of the periodic table, typically Pt, Pd, Ru, Ir, Rh, Os, Fe, Co, Ni, Cu, Mo, , Ti Hg, Ag or Au, usually supported on a support such as alumina, silica, silica-alumina or carbon. Such reduced catalysts can be spon-taneously combustible.

Catalyst compositions for hydrotreating and/or hydrocracking or tail gas treating are well known and several are commercially available, in particular metal oxide catalysts including cobalt-molybdenum, nickel-tungsten, and nickel- molybdenum, usually supported on alumina, silica and/or silica- alumina, including zeolites and carriers. Other transition metal element catalysts may be employed for these purposes, including those containing at least one of V, Cr, Mn, Re, Co, Ni, Cu, Zn, Mo, W, Rh, Ru, Os, Ir, Pd, Pt, Ag, Au, Cd, Sn, Sb, Bi and Te.

For maximum effectiveness the metal oxide catalysts are converted at least in part to metal sulfides. The metal oxide catalysts can be sulfided in the reactor by contact at elevated temperatures with hydrogen sulfide or a sulfur-containing oil or feed stock ("in-situ") . However, it is advantageous to the user to be supplied with metal oxide catalysts having sulfur, as an element or in the form of an organo-sulfur compound, incor-porated therein. These presulfurized catalysts can be loaded into a reactor and brought up to reaction conditions in the presence of hydrogen causing the sulfur or sulfur compound to react with hydrogen and the metal oxides thereby con-verting them into sulfides without any additional process steps. These presulfurized catalysts provide an economic advantage and avoid many of the hazards such as flammability and toxicity, which the plant operator encounter when using hydrogen sulfide, liquid sulfides, polysulfides and/or mercaptans to sulfide the catalysts. Several methods of presulfurizing metal oxide catalysts are known. Hydrotreating catalysts have been presulfurized by incorporating sulfur compounds into a porous catalyst prior to hydrotreating a hydrocarbon feedstock, using, for example, organic polysulfides, or elemental sulfur in which case hydro¬ gen is used as a reducing agent to convert the elemental sulfur to hydrogen sulfide in situ. U.S.-A-4,943,547 discloses sub¬ liming elemental sulfur into the pores of the catalyst then heating the sulfur-catalyst mixture to a temperature above the melting point of sulfur in the presence of hydrogen which activates the catalyst. WO-A-93/02793 discloses a method where elemental sulfur is incorporated in a porous catalyst and at the same time or subsequently the catalyst is treated with a liquid olefinic hydrocarbon. However, these ex-situ presulfurized catalysts, which are spontaneously combustible and may be pyrophoric or self-heating, these two groups differing in the degree of spontaneous combustion, must be transported to the user or plant operator. Pyrophoric substances ignite, even in small quantities, within five minutes of coming into contact with air whereas self- heating substances ignite in air only when in large quantities and after long periods of time. Pyrophoric substances are typically classified as Division 4.2 Packing Group I and self- heating substances are classified in either Packing Group II or Packing Group III according to the test procedures recommended in the Dangerous Goods Special Bulletin, April 1987, published by TDG Ottawa, Transport Canada for Class 4, Division 4.2. These spontaneously combustible substances must be packaged in a United Nations designated 250 kg metal drum or in a smaller package of 100 kg plastic fiber drum or even smaller.

It is clearly desirable to transport these presulfurized catalysts in larger quantities such as in flow bins or super- sacks but they must pass the test for spontaneously combustible substances. Further, some of the prior art ex-situ methods of presul¬ furizing supported metal oxide catalysts have suffered from excessive stripping of sulfur upon start-up of a hydrotreating reactor in the presence of a hydrocarbon feedstock. As a result a decrease in catalyst activity or stability is observed and there can be fouling of downstream equipment.

Therefore, it is an object of the present invention to treat spontaneously combustible catalysts in a manner to suppress their self-heating properties.

The present invention provides a composition comprising a spontaneously combustible catalyst at least a portion of which has been coated with a substance comprising at least one oxygen- containing hydrocarbon having at least 12 carbon atoms; this can be achieved by contacting the catalyst with the oxygen- containing hydrocarbon at a temperature of at least 0°C. Such composition has a reduced self-heating characteristic when compared to the spontaneously combustible catalyst which has not been coated. Further, the present invention also provides an improved method of presulfurizing a sulfidable metal or metal oxide(s)- containing catalyst which suppresses self-heating characteristics, which comprises :

(a) contacting said catalyst with elemental sulfur, a sulfur compound or a mixture thereof at a temperature such that at least a portion of said sulfur or sulfur compound is incorporated in the pores of said catalyst by impregnation, sublimation and/or melting; and

(b) prior to, at the same time or subsequently contacting said catalyst particles in the presence of an oxygen-containing hydrocarbon having at least 12 carbon atoms.

The method is particularly suitable for application to hydrotreating and/or hydrocracking or tail gas treating catalysts, for hydrocracking hydrocarbon streams. Furthermore, the present invention provides a method of unloading a catalyst during a halt in the operation of the reactor wherein the catalyst in the reactor is contacted with a mixture comprising an oxygen-containing hydrocarbon having at least 12 carbon atoms prior to unloading. It has been found that by treating a spontaneously combustible catalyst by contacting with an oxygen-containing hydrocarbon having at least 12 carbon atoms, the resulting catalyst has suppressed self-heating characteristics, in general, such that it is no longer classified as spontaneously combustible. Thus, the process allows an otherwise spontaneously combus-tible catalyst to be transported or shipped in any suitable packaging such as flow-bins, super-sacks, or sling-bins for example.

As used herein, a "spontaneously combustible catalyst(s)" is any heterogeneous or solid metal(s)-, metal oxide(s)-, metal sulfide(s)- or other metal compound(s)- containing catalyst, optionally on a support which can be classified as a spontaneously combustible substance according to the test procedures recommended in the Dangerous Goods Special Bulletin, April 1987, published by TDG Ottawa, Transport Canada for Class 4, Division 4.2 or has a onset of exotherm below 200°C as measured by the self-heating ramp test des-cribed below. The terms "metal(s)τ", "metal oxide(s)-" and "metal sulfide(s)-" containing catalysts include catalyst precursors that can be used as catalysts after further treatment or activation. Further, the term "metal(s)" includes metal(s) in partially oxidized form. The term "metal oxide(s)" includes metal oxide(s) in partially reduced form. The term "metal sulfide(s)" includes metal sulfide(s) that are partially sulfided as well as totally sulfided metals.

It is understood that while the normal catalyst prepara¬ tive techniques will produce metal oxide(s), it is possible to utilize special preparative techniques to produce the catalytic metals in a reduced form, such as the zero valent state. Since metals in the zero valent state will be sulfided as well as the oxides when subjected to sulfiding conditions, catalysts containing such sulfidable metals even in reduced or zero valent states will be considered as "sulfidable metal oxide catalyst(s)". Also the process of the instant invention can be applied to regenerated catalysts which may have the metal sulfide not completely converted to the oxides.

Other components such as carbides, borides, nitrides, oxyhalides, alkoxides and alcoholates can also be present.

In one embodiment of the present invention, a spontane¬ ously combustible catalyst is contacted with at least one oxygen-containing hydrocarbon at a temperature of at least about 0°C, preferably at least 15°C to 350°C, and more preferably 20°C to 150°C. Upon contact, the oxygen-containing hydrocarbon is impregnated into the spontaneously combustible catalyst so that the surface of the catalyst is coated with the oxygen-containing hydrocarbon. For the purpose of definition, the surface of the catalyst includes the external surface of the catalyst as well as the internal pore surfaces of the catalyst. The word "coating" does not rule out some reaction as defined below. The mechanism by which the oxygen-containing hydrocarbon suppresses the self-heating characteristics of the spontane¬ ously combustible catalysts is not known and will be referred to, for convenience as "reaction" or "reacts". The suppressed self-heating result can be readily determined without undue experimentation by measuring the exothermic onset temperatures for a specific rising temperature profile of catalysts sub¬ jected to differing temperature/time treatments with and with¬ out the oxygen-containing hydrocarbon, as shown below.

When sulfur-containing catalysts are treated their sulfur retention or activity is not substantially compromised. The sulfided catalysts can be catalysts sulfided by an in-situ presulfiding method or an ex-situ presulfiding or presulfuri- zing method. Such catalysts can be fresh or oxy-regenerated, for example, those disclosed in U.S.-A-4,530,917; 4,177,136; 4,089,930; 5,153,163; 5,139,983; 5,169,819; 4,530,917 or 4,943,547 or WO-A-93/02793, or reduced hydrogenation catalyst such as disclosed in U.S. Patent No. 5,032,565.

The treatment can also be applied prior to, at the same time or subsequent to presulfurizing a presulfidable metal or metal oxide catalyst. Preferably the catalyst is heated after contacting with elemental sulfur or a sulfur compound at an elevated temperature and time sufficient to fix the sulfur onto the catalyst. Such heating process can be before or after treatment with the oxygen-containing hydrocarbon. Generally, the catalysts of the present invention also have enhanced resistance to sulfur stripping during startup in a hydrotreating and/or hydrocracking reactor in the presence of a hydrocarbon feedstock. The mechanism by which this occurs is not known and will be referred to for convenience as "reaction" or "reacts". A suitable method for determining sulfur stripping resistance is described below wherein toluene is used as stripping agent.

Further, for reasons unknown for elemental sulfur- incorporated catalysts, the percent retention of sulfur is generally improved by the treatment, particularly for some high- pore volume catalysts.

There are three general methods for carrying out the presulfurising process.

In the first method porous catalyst particles are contac¬ ted with elemental sulfur or sulfur compounds or mixtures thereof so as to cause the sulfur or sulfur compounds to be incorporated into the pores of the catalyst by impregnation, by sublimation, by melting or by a combination thereof to produce "sulfur-incorporated catalysts."

The sulfur-incorporated catalyst particles are contacted with the oxygen-containing hydrocarbon at temperatures and times sufficient to cause the catalyst particles to exhibit suppressed self-heating properties.

When using elemental sulfur, the catalyst is contacted at a temperature such that the elemental sulfur is substantially incorporated in the pores of the catalyst by sublimation and/or melting. While the catalyst particles can be contacted with sulfur in the molten state, it is preferred to first admix the catalyst particles with powdered elemental sulfur and then heat the mixture to above the temperature at which sublimation of the sulfur occurs.

Generally the catalyst particles are heated in the presence of the powdered elemental sulfur at a temperature greater than about 80°C. Typically the catalyst and powdered sulfur are placed in a vibratory or rotary mixer and heated to the desired temperature for sufficient time, typically 0.1 to 10 hours or more, to allow for the incorporation. Preferably the sulfur impregnation step is carried out at 90°C to 130°C or higher, up to the boiling point of sulfur (about 445°C) . The lower temperature limit is fixed by the sublimation/melting characteristics of sulfur under the specific conditions of impregnation, whereas the upper temperature limit is fixed primarily by economics, higher temperatures being more costly to produce as well as more difficult to work with.

The sulfur-incorporated catalyst is then treated with the oxygen-containing hydrocarbon, as discussed below. The sulfur-incorporated catalyst may be further heated before and/or after the oxygen-containing hydrocarbon treatment at a temperature greater than about 150°C, preferably from 175°C to 350°C and more preferably from 200°C to 325°C, to fix the incorporated-sulfur onto the catalyst. Preferred sulfur compounds include, for example, ammonium sulfide, organic mono-, di- and poly-sulfides, dialkyl sulf- oxides and compounds derived from these upon heating or reduc¬ tion in the presence of the sulfidable metal oxide and mixtures thereof. Examples of organic sulfides include poly-sulfides of general formula R-S(n)-R' or HO-R-S(n)-R-OH wherein n is an integer from 3 to 20 and R and R' are independently organic radicals of 1 to 50 carbon atoms such as ditert dodecyl polysulfide and diethanol disulfide; mercaptoalcohols such as 2-mercaptoethanol; . alkylmercaptans such as n-butyl mercaptan; thioglycols such as dithiopropyleneglycol; dialkyl or diary1 sulfides such as di-n-butyl sulfides and diphenyl sulfides; dialkylsulfoxides such as dimethyl sulfoxide; and mixtures thereof.

Before use, the sulfur compounds are typically impregnated with an aqueous or organic solution such as a hydrocarbon or non-hydrocarbon equivalent to light gasoline, hexane or gasoline of white spirit type, for example as described in U.S.-A- 5,153,163; 5,139,983; 5,169,819; and 4,530,917. The resulting catalysts are typically reduced by hydrogen, or other organic reducing agent such as formic acid, methyl formate, ethyl formate, acetaldehyde or methyl alcohol. The sulfur compound- incorporated catalyst can be treated with the oxygen-containing hydrocarbon before and/or after the reduction step under conditions described above for the elemental sulfur-incorporated catalyst.

In the second method, a porous sulfidable metal oxide- containing catalyst is contacted with a mixture of powdered elemental sulfur and/or a sulfur compound and the oxygen- containing hydrocarbon, preferably while heating the resultant mixture to a temperature above about 80°C.

In this embodiment, the catalyst particles are contacted with the elemental sulfur, preferably powdered, and/or at least one sulfur compound and the oxygen-containing hydro-carbon simultaneously. Other hydrocarbons such as olefins can be optionally added simultaneously. A mixture of powdered ele¬ mental sulfur and/or sulfur compound and oxygen-containing hy- drocarbon is first produced. When elemental sulfur is used, the ratio of hydrocarbon to sulfur by weight is typically from 1:2 to 30:1, preferably from 1:1 to 6:1. The mixture may be heated to promote homogeneity, particularly if the hydrocarbon is not liquid at ambient conditions or the mixture may be a suspension. Toluene or other light weight hydrocarbon solvents may be added to decrease the viscosity of the mixture. Increased heat will achieve the same effect. When a sulfur compound is used as the source of sulfur, the ratio of hydrocarbon to sulfur compound by weight is typically from 1:2 to 30:1. The mixture is then added to a preweighed catalyst sample and mixed. When a mixture of elemental sulfur and sulfur compound is used as the source of sulfur, a ratio of hydrocarbon to total sulfur and by weight from 1:2 to 30:1 is suitable.

When, elemental sulfur is at least partially used, the mixture is then heated to incorporate sulfur at a temperature of above about 80°C. The times and temperature can be the same as in for the first embodiment. When sulfur compounds are used the catalyst can be reduced as above for the first embodiment.

In the third method, a porous sulfidable metal oxide- containing catalyst is first contacted with the oxygen- containing hydrocarbon before the presulfurization step. The resultant mixture can be optionally heated to a temperature above about room temperature (i.e. about 25°C) for a solid or semi-solid hydrocarbon to allow it to impregnate the catalyst. The catalyst and/or oxygen-containing hydrocarbon is preferably heated to at least a temperature where the hydrocarbon becomes liquid or semi-fluid. The hydrocarbon treated catalyst is then presulfurized by contacting with elemental sulfur and/or sulfur compound as described for the first method. Optionally, the hydrocarbon-treated presulfurized catalyst can be heated during the εulfurization step or after impregnation of sulfur compounds regardless of prior heat-treatment. The catalyst should preferably be heated at some point after contacting with the sulfur at a temperature above about 150°C so as to fix the sulfur on the catalyst.

The catalyst is preferably treated with the oxygen- containing hydrocarbon after sulfur and/or sulfur compound incorporation for superior suppression of self-heating characteristics. If the sulfur and/or sulfur compound and the hydrocarbon are contacted with the metal or metal oxide(s) catalyst simultaneously, it is preferable that the catalyst is contacted in such a manner which allows the sulfur and/or sulfur compounds to be incorporated or impregnated into the pores of the catalyst prior to the catalyst reacting or being coated with the hydrocarbon at a temperature of above 80°C.

In any of the above methods the amounts of sulfur or sulfur compounds used will depend upon the amounts of catalytic metal present in the catalyst. Typically the amount used is determined on the basis of the stoichiometric amount of sulfur or sulfur compounds required to convert all of the metal on the catalyst to the sulfide form. For example a catalyst containing molybdenum would require two moles of sulfur or mono-sulfur compounds to convert each mole of molybdenum to molybdenum disulfide. On regenerated catalysts, existing sulfur levels may be factored into the calculations for the amounts of elemental sulfur required. It has been found that the addition of presulfurizing sulfur in amounts down to about 50 percent of the stoichiometric requirement results in catalysts having enhanced hydrode- nitrification activity, which is an important property of hydrotreating and first stage hydrocracking catalysts. Thus, the amount of presulfurizing sulfur used for incorporation into the catalyst will typically be from 0.2 to 1.5 times, and preferably from about 0.4 to about 1.2 times the stoichiometric amount.

For hydrotreating/hydrocracking and tail gas treating catalysts containing Group VIB and/or Group VIII metals the amount of presulfurizing sulfur employed is typically 2% to 15%, and most preferably, 6% to 12%, by weight of the catalyst charged. It is preferred not to add so much sulfur or sulfur compound to the catalyst that the pores are completely filled up. By leaving residual pore volume, the oxygen-containing hydrocarbon can penetrate the pores and react therein. The key step in the present invention is to contact the catalyst with an oxygen-containing hydrocarbon having at least 12 carbon atoms for a sufficient time such that the hydrocarbon impregnates (or reacts) with the catalyst and provides a catalyst that is less spontaneously combustible and, for a sulfurised catalyst, is more resistant to sulfur leaching than one not contacted with the hydrocarbon. Typically the contact temperature is greater than about 0°C, desirably from 15°C to

350°C, preferably from 20°C to about 150°C. The contact temperature will vary depending on the melting point or sublimation temperature of the hydrocarbon. For example, when the oxygen-containing hydrocarbon is a solid or a semi-solid such as lard, the temperature should preferably be at least as high as the melting point for a time sufficient for the catalyst to flow freely (appear "dry" and not stick or clump) , i.e. it is liquid or semi-fluid, to enable the hydrocarbon to coat and/or impregnate the catalyst. Lard, for example, is preferably contacted at a initial temperature of about 80°C. The process temperature can be readily determined by the melting point of the solid or semi-solid at a given pressure environment or visually by checking if the oxygen-containing hydrocarbon flows. Contact times will depend on temperature and the viscosity of the oxygen-containing hydrocarbon, higher temperatures requiring shorter times and higher viscosity requiring longer times. In general times will range from 2 minutes to 2 hours or more.

Preferably the oxygen-containing hydrocarbon is suffi- ciently flowable or sublimable to give sufficient contact with the catalyst. A hydrocarbon which is liquid at the elevated temperature of contact is more preferred for ease of handling. It is preferred that the hydrocarbon is a higher hydrocarbon, i.e., one having greater than twelve, preferably greater than sixteen, and more preferably greater than twenty carbon atoms. The upper carbon number is determined by the melting point, solidification point, or smoke point of the hydrocarbon in question. While solid fatty oxygen-containing hydrocarbon having carbon numbers greater than 100 can be used, they are inconven- ient since they must be heated to such a high temperature in order to be converted into a liquid, although they can be used with a solvent. Hydrocarbons with carbon numbers from 12 to 100, preferably from 16 to 80 are found most useful.

The term "oxygen-containing hydrocarbon" as used herein refers to hydrocarbon molecules containing at least one oxygen atom, which includes, for example, acids, acid esters, alcohols, aldehydes, ketones and ethers. Mixtures may be used such as acid esters and alcohols, and different acid esters. It can be primary, secondary or tertiary, straight or branched chain, cyclic, acyclic or aromatic, saturated or unsaturated. Preferably, the hydrocarbon moiety contains at least some unsaturation for superior activity as a hydrotreating, hydrocracking or tail gas treating catalyst, typically an unsaturated fatty acid ester. The term "unsaturated" as used herein refers to hydrocarbon molecules containing at least one carbon-carbon double bond or compound(s) containing some carbon- carbon double bond and will have an iodine value of at least 60 measured by standard iodine measuring techniques such as American Oil Chemist Society (AOCS) Official Method Cd 1-25 or IUPAC Method 2.205 described in International Union of Pure and Applied Chemistry, 7th ed. , Blackwell Scientific Publications 1987 or any other standard iodine measuring techniques. The term "saturated" as used herein refers to oxygen-containing hydrocarbon compounds containing no carbon-carbon double bonds or compound(s) containing minimal carbon-carbon double bonds and have a iodine value of less than 60 measured by AOCS Official Method Cd 1-25, IUPAC Method 2.205 or any other standard iodine measuring techniques.

Preferred hydrocarbons include those having at least 12, preferably 16, more preferably 20 carbon atoms for example, higher alcohols such as dodecanol, hexadecanol, farnesol, hexe- strol, oleyl alcohol, cetyl alcohol, hexacosanol, triacontanol, cocceryl alcohol and octacosanol; higher ethers such as dicetyl ether; higher ketones such as palmitone, 10-hydroxypalmitone and 3-octadecanone; higher aldehydes such as palmitaldehyde and olealdehyde; higher acids such as saturated acids such as lauric, myristic, palmitic, stearic, and docosanoic acids or unsaturated higher acids such as palmitoleic, oleic, linoleic, linolenic, eleostearic, ricinoleic, eicosenoic, docosenoic, eicosatetraenoic, eicosapentaenoic, decosapentaenoic and docosahexaenoic; higher acid esters including mono-, di-, tri- and poly-fatty acid esters including alkyl and aryl esters of the above acids (e.g. benzyl oleate and butyl oleate) and esters of the above acids with mono-glyceride, di-glycerides and triglycerides and mixtures thereof. Glyceride fatty acid esters having from 16 to 100, more preferably 18 to 90, most preferably 20 to 80 carbon atoms are preferred.

Examples of commercial glyceride fatty acid esters include soybean oil, linseed oil, safflower oil, corn oil, sunflower oil, cottonseed oil, olive oil, tung oil, castor oil, rapeseed oil, tall oil, peanut oil, coconut oil, palm oil, canbra oil, perilla oil, lard, tallow, marine fat or oil such as fish fat or oil (e.g. herring and sardine) , vegetable residues and mix¬ tures thereof. Some examples of commercial higher alcohols in¬ cludes alkanol mixtures such as NEODOL alcohols (Shell Chemical Company), including mixtures of C₉,C₁₀ and C_u alkanols (NEODOL 91) , mixtures of Cι₂ and C₁₃ alkanols (NEODOL 23) , mixtures of C₁₂, C₁₃, C₁₄ and C₁₅ alkanols (NEODOL 25) , and mixtures of C_M and C₁₅ alkanols (NEODOL 45) ; the ALFOL Alcohols (Vista Chemical Company) , including mixtures of C_ι0 and C₁₂ alkanols (ALFOL 1012) , mixtures of C₁₂ and Cj₄ alkanols (ALFOL 1214) , mixtures of C₁₆ and C₁ alkanols (ALFOL 1618) and mixtures of Cι₆, C_lg, and C₂₀ alkanols (ALFOL 1620) ; the EPAL Alcohols (Ethyl Chemical Company) , including mixtures of C₁₀ and C₁₂ alkanols (EPAL 1012) , mixtures of Cι₂ and C₁₄ alkanols (EPAL 1214) and mixtures of C₁₄, C₁₆, and C₁₈ alkanols (EPAL 1418) ; and the TERGITOL-L Alcohols (from Union Carbide Corporation) , including mixtures of C_π, C₁₃, C_M and C₁₅ alkanols (TERGITOL-L 125) . Suitable commercially available alkanols prepared by the reduction of naturally occurring fatty acid esters include, for example, the CO and TA products of Procter and Gamble Company and the TA alcohols of Ashland Oil Company. Higher oligomers and polymers of polyols such as alkylene glycols are also suitable as higher alcohols. Optionally, the oxygen-containing hydrocarbon treated catalyst can be further treated with or simultaneously treated with, or treated prior to the hydrocarbon treatment with olefins to enhance catalytic activity in hydrocracking, hydrotreating or tail gas treating. The term "olefin" as used herein refers to hydrocarbons containing at least one carbon-carbon double bond. The olefins may be onoolefins or polyolefins, cyclic or acyclic, linear or branched. Suitable monoolefins include decene, undecene, dodecene, tridecene, tetradecene, pentadecene, hexadecene, heptadecene, octadecene, nonadecene and eicosene, whether branched, linear or cyclic, alpha or internal olefin. Similar materials in the form of di-, tri- and polyolefins may be used. Polycyclic olefins and polyolefins may also be used. Dicyclopentadiene is found useful. The oxygen-containing hydrocarbons may also be mixed with other hydrocarbons, such as alkanes or aromatic solvents.

In general, for superior activity of the catalyst upon start-up in the plant, the weight percent of the unsaturated compounds of any hydrocarbon used in the process (including unsaturated oxygen-containing hydrocarbon and olefin) should be above about 5%wt., preferably above about 10%wt. , and most preferably above about 30%wt. Generally, a higher weight percent of unsaturation compounds is used, say above about 50%wt; most conveniently the weight percent of the unsaturated hydrocarbons is l00%wt (undiluted form and only unsaturated oxygen-containing hydrocarbon and/or olefins) . For example, when the catalyst is treated with olefins and oxygen-containing hydrocarbons, the unsaturation may be provided from olefin alone using saturated oxygen-containing hydrocarbons or from olefin and some unsaturated oxygen-containing hydrocarbon. Of course, unsaturated oxygen-containing hydrocarbon alone without olefins can also be used. It is to be understood that the oxygen- containing hydrocarbons may be provided as oxygen-containing hydrocarbon precursors which are converted to the oxgyen- containing hydrocarbon before or upon reaching the reaction temperature such as, reacting lower molecular weight acids (e.g. lower than C₁₂ acids) with glycerol to form a higher triglyceride acid ester.

The minimum amount of oxygen-containing hydrocarbon used should be such that the catalyst obtained that is less spontaneously combustible. The maximum amount of oxygen- containing hydrocarbon used is determined primarily by economics. In a preferred embodiment the amount of substance or mixtures containing the oxygen-containing hydrocarbon is used that will just fill the pore volume of the impregnated catalyst or just slightly less, down to about 50 percent, preferably down to about 70 percent of the pore volume. A general range is from 50 to 95, more preferably from 70 to 90, percent. A preferred target range is from 80 to 95 percent although greater than 100% hydrocarbon can be used. In this manner, the treated catalyst will be "dry" (flow freely) and is more convenient to handle.

The presulfurized catalyst obtained by the above presulfurization process may be converted to sulfided catalysts by contact with hydrogen at temperatures of at least about 200°C, preferably from 200°C to 425°C, or 450°C for, say, 0.5 hours to up to 3 days.

In preferred operation the presulfurized catalyst is loaded into a hydrotreating and/or hydrocracking reactor or tail gas reactor and hydrogen flow is started to the reactor and the reactor is heated up to operating (hydrotreating and/or hydrocracking or tail gas treating) conditions to cause activation of the catalyst the metal oxides and hydrogen react with substantially all of the sulfur incorporated into the catalyst pores, thus producing hydrogen sulfide, water and metal sulfides. In the hydrotreating and/or hydrocracking process, a hydrocarbon feedstock flow may be started simultaneously with the hydrogen or later.

The process of the present invention is further applicable to the sulfurizing of spent catalysts which have been oxy- regenerated. After a conventional oxy-regeneration process, an oxy-regenerated catalyst may be presulfurized as would fresh catalyst in the manner set forth above.

The instant invention also provides a method for stabilizing (less spontaneouly combustible or reducing the self- heating characteristics) a supported metal catalyst containing elemental sulfur, particularly a Group VIB and/or Group VIII metal catalyst, by contacting the catalyst with an oxygen- containing hydrocarbon at a temperature and time sufficient to impregnate and/or to react with the catalyst. In applying the oxygen-containing hydrocarbon to the catalyst, the oxygen-containing hydrocarbon can be added in batches and mixed or added continuously by spraying the catalyst with the oxygen-containing hydrocarbon.

The inventive process is particularly suitable for application to hydrotreating and/or hydrocracking or tail gas treating catalysts. These catalysts typically comprise Group VIB and/or Group VIII metals supported on porous supports such as alumina, silica, silica-alumina or zeolite; they can be prepared by techniques described in e.g. U.S.-A-4,530,911, 4,520,128 and 4,584,287. Preferred hydrotreating and/or hydrocracking or tail gas treating catalysts contain a group VIB metal selected from molybdenum, tungsten and mixtures thereof and a Group VIII metal selected from nickel, cobalt and mixtures thereof, supported on alumina. Versatile hydrotreating and/or hydrocracking catalysts which show good activity under various reactor conditions are alumina-supported nickel-molybdenum and cobalt-molybdenum catalysts

SUBSTITUTE SHEET (RULE 26} and zeolite-supported nickel-molybdenum and nickel-tungsten catalysts. Phosphorus is sometimes added as a promoter. A versatile tail gas treating catalyst which shows good activity under various reactor conditions is an alumina-supported cobalt- molybdenum catalyst.

Hydrotreating catalysts which are specifically designed for hydrodenitrification operations, such as alumina-supported nickel-molybdenum catalysts, presulfurized or presulfided as described have equal activities, particularly hydrodeni- trification activities, compared with catalysts without the oxygen-containinghydrocarbontreatment. Hydrocrackingcatalysts such as nickel-molybdenum or nickel-tungsten on a zeolite or silica-alumina support presulfurized as described provide increased liquid yield over catalysts without the oxygen- containing hydrocarbon treatment. Thus, the invention is also an improved hydrotreating and/or hydrocracking process which comprises contacting at hydrotreating and/or hydrocracking conditions a hydrocarbon feedstock and hydrogen with a catalyst which has been presulfurized as described and which has been heated to hydrotreating and/or hydrocracking temperature in the presence of hydrogen and optionally a hydrocarbon feedstock.

The ability to avoid instantaneous combusting provides the presulfurized catalysts with a significant commercial advantage.

The ex-situ presulfurization method of this invention allows the hydrotreating, hydrocracking and/or tail gas treating reactors to be started up more quickly compared with the in-situ operation by eliminating the presulfiding step. Further, the presulfurized catalysts of the invention can be handled more conveniently than the conventional ex-situ presulfurized catalysts. Thus, the instant invention provides a process for starting up a hydrotreating and/or hydrocracking reactor, which comprises loading the catalyst presulfurized as described herein into the reactor and activating the catalyst by heating the reactor to operating conditions in the presence of hydrogen and optionally a hydrocarbon feedstock. Further, it has been found that catalysts activated by heating the catalyst in the presence of hydrogen and at least one feedstock or hydrocarbon having a boiling point at least 35°C, preferably from 40°C, more preferably from 85°C, to 700°C, preferably to 500°C at atmospheric pressure, give increased yields compared to gas activated catalysts. Such hydrocarbons include, for example, jet fuels, kerosines, diesel fuels, gasolines, gas oils, residual gas oils and hydrocarbon feed streams (feedstocks) . The catalysts are suitably activated at a temperature from 25°C to 500°C, preferably to 450°C, and a hydrogen pressure of from 50, preferably 350, to 3000 psig. The hydrocarbon rate will typically have a liquid hourly space velocity ("LHSV") from 0.1, preferably from 0.2, to about 20, preferably 15, more preferably 10, hr^*1.

Hydrotreating conditions typically comprise temperatures from 100°C to 450^βC, preferably to 425°C, and pressures above 40 atmospheres. The total pressure will typically range from 400 to 2500 psig. The hydrogen partial pressure will typically range from 200 to 2200 psig. The hydrogen feed rate will typically range from 200 to 10000 standard cubic feet per barrel ("SCF/BBL") . The feedstock rate will typically have a liquid hourly space velocity ("LHSV") from 0.1 to 15.

Hydrocracking conditions typically comprise temperatures from 100°C, preferably from 150°C, more preferably from 200°C, to 500°C, preferably to 485°C, more preferably to 450°C, and pressures from 40 atmospheres. The total pressure will typically be from 100 to 3500 psig. The hydrogen partial pressure will typically range from 100, preferably from 300, more preferably from 600 psig, to 3500, preferably to 3000 psig. The hydrogen feed rate will typically range from 1000, more preferably from 2000, to 15,000, more preferably to 10,000, SCF/BBL. The feedstock rate will typically have a LHSV from 0.05, preferably from 0.1 to 20, preferably to about 15, more preferably to about 10. First stage hydrocrackers, which carry out considerable hydrotreating of the feedstock may operate at higher tempera¬ tures than hydrotreaters and at lower temperatures than second stage hydrocrackers.

Tail gas treatment reactors typically operate at temp¬ eratures ranging from 100°C, preferably from 200°C, to about 450°C, preferably 400°C and at atmospheric pressure. Typically 0.5 to 5% vol. of the tail gas fed to the reactor will comprise hydrogen. Standard gaseous hourly space velocities of the tail gas through the reactor will range from 500 to 10,000 hr Claus unit feed or tail gas can be used to start up the catalysts. Supplemental hydrogen, as required, may be provided by a gas burner operating at a substoichiometric ratio in order to produce hydrogen.

In another embodiment of the invention, catalysts in a refining or a chemical plant reactor such as hydrocracking, hydrotreating, tail gas treating, hydrogenation, dehydrogenation isomerization and de-waxing can be treated with the oxygen- containing hydrocarbon and optionally carrier oil including feed oil and/or fused-ring aromatic hydrocarbons before unloading from the reactor, typically when operation is suspended, stopped or halted by terminating the refining or chemical reaction, for example by terminating the feed or by lower temperature, the process provides a method of safely unloading the catalysts with minimal catalyst oxidation and deterioration. The oxygen- containing hydrocarbon-containing mixture (mixture can be undiluted oxygen-containing hydrocarbon) penetrates to the surface of the catalyst and diffuses into the pores of the catalysts at the temperature in the reactor after suspension (or stopping) of its operation, and "coats" the catalyst with a film. It is preferred that the temperature within the reactor column be lower than the smoke point or boiling point (at the reactor operation pressure) of the oxygen-containing hydrocarbon when the mixture is added to the catalyst in the reactor. Thus, after the operation of the reactor is stopped, the feed and/or catalyst can be cooled from the operating temperature by allowing the reactor to equilibrate with the ambient temperature, recycling or by passing feed through a cooling unit. The feed to the reactor can optionally be shut off. For many of the oxygen-containing hydrocarbons, the temperature of the reactor and/or catalyst is preferably less than about 175°C, more preferably less than about 125°C when the hydrocarbon is contacted with the catalyst at atmospheric pressure. If the hydrocarbon is contacted with the catalyst at elevated reactor pressures, the reactor and/or catalyst temperatures can be higher. The contact temperature can be as low as the unloading temperature or lower. The catalyst is typically unloaded at a temperature about room temperature to about 70°C.

The oxygen-containing hydrocarbon mixture can be introduced into a reactor column after suspension of reactor operation. The mixture can be added to a batch containing the catalysts or to a recycle stream. Optionally, heavy oil or any similar raw material from the reactor columns can be removed before adding the hydrocarbon. The catalyst is coated with the hydrocarbon upon contact and incorporation, thus enhancing the safety of the unloading operation by protecting the catalyst against oxidation and rendering the catalyst less spontaneously combustible. A mixture containing the oxygen-containing hydrocarbon preferably in an amount from 1 to 100 weight percent of the mixture is contacted with the catalyst in the reactor for a time effective to coat the catalyst and reduce the self-heating characteristics of the catalyst. Preferably the mixture should be used in an amount sufficient to coat the surface of the catalyst.

The oxygen-containing hydrocarbon may be applied in admixture with a fused-ring aromatic hydrocarbon and/or a carrier oil. Preferable fused-ring aromatic hydrocarbon include for example, any fused-ring aromatic hydrocarbon containing at least 2 rings, preferably 2 to 4 rings, such as naphthalenes such as alkylnaphthalene; anthracenes such as alkylanthracene; and pyrenes such as allylpyrene. Such fused-ring aromatic hydrocarbons may be unsubstituted or substituted for example with alkyl or aryl moieties. Carrier oil can be any hydrocarbon stream used in refining operations or a blend thereof having a flash point of above about 38°C. Preferably carrier oil includes straight-run heavy gas oil (HGO) , vacuum gas oil (VGO) , diesel oil and the like. The oxygen-containing hydrocarbon and optionally fused-ring aromatic hydrocarbon and/or carrier oil can be added through separate lines then mixed or added after being mixed. If desired, the mixture can be heated with any heating means such as a heating furnace, band heater, heating coil or a heat exchanger, to the desired temperature.

The invention will now be illustrated by the following non- limiting Examples. Example I:

This Example demonstrates the case where the catalyst is first presulfurized and then treated with oxygen-containing hydrocarbon.

Part A: Sulfur impregnation A commercial hydrotreating catalyst having the properties listed below was used.

Table 1: Catalyst Properties Nickel 3.0 %wt

Molybdenum 13.0 %wt Phosphorous 3.5 %wt

Support gamma alumina

2

Surface Area, m /g 162

Water Pore Vol., cc/g 0.47

Size 1/16 inch trilobes 250 Gram of the above sample was dried at 371°C for one hour and then cooled to ambient under vacuum. The sample was then placed in a flask and enough sulfur, in powdered form, was added at 85°C to produce a sulfur level of about 10% by weight. The sulfur was allowed to coat the catalyst and then the flask, which was provided with a slow nitrogen purge and placed in a heating mantle, was further heated to 120°C for 30 minutes. During this period the flask was vibrated continually to provide mixing of sulfur and catalyst. The final sulfur level was about 10% by weight of the total catalyst. The water pore volume of the sulfur-impregnated catalyst was determined to be about 0.37 cc/g.

Part B: Oxyσen-containinσ Hydrocarbon Reaction and Comparative Examples

The sulfur-impregnated catalyst from Part A was impregnated with the various oxygen-containing hydrocarbons listed in Table 2. Catalyst from Part A was also impregnated with Diesel and Neodene 14/16/18 alpha-olefins as comparative examples. Impregnation was sufficient to fill 80% of the pore volume calculated by:

(pore volume of catalyst from Part A) (80%) (adjusted weight of catalyst) (density of oxygen-containing hydrocarbon or compara- tive compounds)=grams of oxygen-containing hydrocarbon or com¬ parative compounds. The pore volume of the catalyst was deter¬ mined with water (mL/g) . "Adjusted weight" is the amount of sulfur/catalyst remaining after retains and pore volume analysis. The lard, vegetable residue and coconut oil, being solids or semi-solids at room temperature, were heated up to approxi¬ mately 80°C before being applied to the catalyst. All other hy¬ drocarbons were simply added to the catalyst at room tempera¬ ture. The catalyst was shaken with the hydrocarbon until the catalyst appeared dry and is free flowing. This took approximat¬ ely 10 minutes per sample. Once the hydrocarbon was absorbed the catalyst temperature was allowed to return to room temperature. 150 Grams of the catalyst were loaded into a 1 liter four- neck flask equipped with a thermocouple through one of the necks and placed in a heating mantle. Another neck of the flask was tubed to a another flask equipped with a condenser which was tubed to a silicone oil-filled container to prevent air back- diffusion (outlet) . Nitrogen flow was established to the flask through another neck of the flask (inlet) at 273 cc/min. The remaining neck was stoppered. The flask was attached to a vibratory table and vibrated for the duration of the heat treatment described below.

The reactor was heated to 260°C over ten to twenty minutes and held there typically for 30 minutes. After heat treatment was complete, the reactor contents were cooled to room tempera¬ ture under nitrogen purge. The samples were analyzed for sulfur content and the exothermic onset temperatures of the samples were tested.

Part C: Self-Heating Ramp Test Approximately a 12 gram aliquot of the test sample was placed in a 3.1 cm diameter, 4.6 cm height sample container, made of 250 mesh stainless steel net, covered with a 30 mesh stainless steel net, container cover which had a square bottom net with the corners bent to form four legs so as to raise the sample container 0.8 cm off platform.

The sample container was placed in a programmable furnace at ambient temperature with a stagnant atmosphere. A thermo- couple was placed in the center of the sample. Another thermo¬ couple was placed near the sample container to monitor oven temperature. The oven was ramped at 0.4°C/minute to 450°C. The temperature data was collected and plotted as described below.

A time-temperature profile was plotted with temperature in the Y-axis and time in the X-axis for catalyst temperature and oven temperature.

Exothermic onset temperatures of the temperature profile test were determined by drawing a 45 degree tangent on the sample's temperature trace at the onset of an exotherm. From the tangent point, a vertical line was drawn to the oven trace then from that point horizontal to the Y axis for temperature readings. The results of the self-heating ramp tests are shown in Table 2 below.

Table 2: Exothermic Onset Temperatures

Oxygen-containing hvdrocarbon Onset of Exotherm (°C)

Lard ^a) 262

Vegetable Residue ^b) 250

Distilled Methyl Esters ^c) 206

Linoleic Acid * 244

Fatty alcohol ^e) 212

Linseed Oil ° 273

Soybean Oil ^g 237

Coconut Oil ^h) 200 Comparative

Diesel ° 156

Neodene® 14/16/18 * 158 a) Lard from Armour Foods. b) A vegetable oil residue from Arista Industries, a mixture of glycerides, polyglycerides, polyglycerols, dimer acids, hydrocarbon and alcohols comprising 79%wt C,₈ fatty acids, and 17%wt Cι₆-fatty acids and having an iodine value of 95- 110. c) Distilled methyl esters from Arista Industries, Inc. having 100 %wt of composition of CAS Registry No. 68990-52-3. d) 99% purity linoleic Acid from Aldrich Chemical. e) Mixture of alcohols from Henkel Corporation 87-95%wt oleyl alcohol and 2-10%wt cetyl alcohol having 90-95 iodine value. f) Raw linseed oil from Anlor Oil Company. g) RBD soybean oil from Lou Ana Foods. h) Laxmi Brand distributed by House of Spices. i) No.2 fuel oil with cetane value of 43 from Exxon Refining and Marketing Company. j) An olefin product manufactured by Shell Chemical Co. 93.5%wt. minimum alpha-monoolefin comprising 15%wt. c_w alpha-monoolefin, 50%wt. Cι₆ alpha-monoolefin and 35%wt. C₁₈ alpha-monoolefin.

Part D: Sulfur Leaching Tests

Toluene was used as a extractive solvent for measuring the ability of the catalysts to resist sulfur leaching. Generally, the samples were subjected to a hot toluene extraction then washed with petroleum ether and dried for analysis. Sulfur analyses before and following the extraction are used to calculate percent sulfur retention. A thorough drying of the sample is necessary to prevent artificially high carbon and sulfur readings during analysis. A Soxhlet extractor (200ml) equipped with a boiling flask (500ml) and Allihn condenser was used. The cotton thimble of the extractor was filled with approximately 10 grams of catalyst to be analyzed and loaded into the Soxhlet extractor. The boiling flask was filled about 3/4 full (about 350ml) with toluene. Toluene was brought to rapid boiling so a cycle of filling and emptying of thimble occurs approximately every 7-9 minutes. The catalyst sample was extracted for a minimum of 4 hours to a maximum of 18 hours. Extraction was stopped when extract in siphon tube was water clear. Catalyst was cooled and placed on a filter in a Buchner funnel and washed with 50 mL of petroleum ether to displace toluene and then dried in a 100°C oven for 1 hour. Prolonged drying may compromise results by loss of sulfur from sample. An alternate drying method is to purge the sample with nitrogen for 2 to 3 hours. The extracted catalysts were analyzed for carbon and sulfur content (wt.% and) with a LECO corporation CS-244 carbon-sulfur analyzer. The percent of sulfur retained after extraction is shown in Table 3 below. This percent of retained sulfur is calculated as the amount of sulfur on the catalyst after the extraction of Part D (Fresh Basis after) divided by the sulfur in the catalyst after the oxygen- containing hydrocarbon treatment of Part B (Fresh Basis before) times 100%. Fresh basis was calculated using the following equation:

Fresh Basis Sulfur = Sulfur wt.% / (100-(Carbon wt.% + Sulfur wt.%)) * 100%.

Table 3: Sulfur Leaching Results

"Reactant" Hydrocarbon Amount of Sulfur After Extraction Oxygen-containing hydrocarbon Sulfur Extractability f%)

Lard ^•* >95

Vegetable Residue ^b) 85

Distilled Methyl Esters ^c) >95

Linoleic Acid ^d) 86 Fatty alcohol ^e) 66

Linseed Oil ° 85 Soybean Oil ⁸⁾ 88

Coconut Oil ^h) 96 Comparative

Diesel '^"> 77 Neodene® 14/16/18 ^Λ 95 a)-j) as described in Table 2.

Part E: Sulfur Retention Tests

A commercial hydrotreating catalyst having the properties listed below was used to prepare the sulfurized catalysts: Table 4: Catalyst Properties

Nickel 2.24 %wt

Molybdenum 7.54 %wt

Phosphorus 3.5 %wt

Support gamma alumina

2 Surface Area, m /g 309

Water Pore Vol., cc/g 1

Size 1/16 inch trilobes

Sulfur was impregnated according to the method of Part A using 5.9wt% of sulfur and soybean oil and Neodene 14/16/18 were impregnated according to the method of Part B. Carbon and sulfur content of the catalyst were analyzed using LECO corporation CS- 244 carbon-sulfur analyzer. Fresh Basis Sulfur was calculated using the equation shown in Part D. Percent Stoichiometric sulfur was calculated by dividing (the Fresh Basis Sulfur) over (the amount of sulfur added) times 100 percent.

Table 5: Sulfur Retention

Carbon Sulfur Fresh Basis Percent

Sample wt.% wt.% Sulfur wt.% Stoichiometric

Neodene®¹⁰ 26.7 3.0 4.3 73 Soybean^b) 33.5 3.5 5.6 95 a) and b) as described in Table 2 as j) and g) respectively.

As can be seen from the Table the percent retention of sulfur is significantly improved by using a glyceride fatty acid ester. Example II: This Example demonstrates the embodiment where the presulfided or sulfurized catalyst is coated with oxygen- containing hydrocarbon.

A commercial sulfurized hydrotreating catalyst having the properties listed below was used.

Table 6: Catalyst Properties Nickel 3.0 %wt

Molybdenum 13.0 %wt

Phosphorus 3.5 %wt Sulfur 8 %wt

Support gamma alumina

Size 1/16 inch trilobes

The oxygen-containing hydrocarbon listed in Table 7 was added to the sulfurized catalyst in an amount listed. The hydrocarbon was added to the catalyst at ambient temperature and allowed to absorb into the pores. The treated catalyst may take some time to absorb the substances so that it is not tacky and flows freely. The self-heating ramp test was measured in a similar manner to Example I, part C.

Table 7: Post-coating

Oxygen-containing Hydrocarbon Amountfwt%. Onset of Exotherm f°C) 1:1 wt ratio soybean:linseed 8 280

1:3 wt ratio soybean:linseed 10 260

Example III: A presulfurized catalyst prepared in a similar manner to Example I was used in a hydrotreating process. 7 types of catalysts, (1 comparative) were used. These were:

1) COMP Catalyst - the commercial hydrotreating catalyst listed in Table 1 which has been sulfided by an industry accepted sulfiding method using hydrogen and hydrogen sulfide as described below.

2) A Catalyst - a catalyst prepared as described in Illustrative Embodiment I with 100% stoichiometric sulfur and using the lard described in Table 2.

3) B Catalyst - a catalyst prepared as described in Illustrative Embodiment I with 100% stoichiometric sulfur and using the vegetable residue described in Table 2. 4) C Catalyst - a catalyst prepared as described in Illustrative Embodiment I with 100% stoichiometric sulfur and using the coconut oil described in Table in Table 2.

5) D Catalyst - a catalyst prepared as described in Illustrative Embodiment I with 100% stoichiometric sulfur and using the methyl esters described in Table 2.

6) E Catalyst - a catalyst prepared as described in Illustrative Embodiment I with 100% stoichiometric sulfur and using the vegetable oil described in Table 2 and Neodene 14/16/18 alpha-olefin described in Table 2 in a weight ratio of 1:1.

The catalysts were loaded into the reactor as follows: 48cc of catalyst (basis compacted bulk density) was divided into 3 aliquots. The first aliquot contained 4 cc of catalyst and was diluted with 10 to 14 mesh alundum at a ratio of alundum to catalyst of 10:1. The remaining two aliquots contained 22 cc of catalyst each and were diluted 1:1 with alundum. These aliquots were loaded into the reactor tube with the dilute one on top (the inlet end) .

Activity Tests A blend of 50 wt% vacuum gas oil, 25 wt% light cycle oil and 25 wt% CC heavy gas oil (VGO/LCO) was used as feedstock having the following properties:

%wt Sulfur 1.93 ppm Nitrogen 1420 Refractive Index 1.5377 (25°C)

API Gravity 17.8°

1) COMP Catalyst Activation

The Catalyst was dried at 400°C for one hour in air, cooled in a desiccator and loaded into the reactor. It was sulfided in a flow of 60 Nl/hr of 95%vol hydrogen/5%vol hydrogen sulfide according to the following schedule: a. ambient to 218°C in one hour b. hold at 218°C for one hour c. heat from 218°C to 329°C in one hour d. heat from 229°C to 343°C in one hour e. hold at 343°C for one hour f. cool reactor and hold at 246°C

2) Diesel Activation

This method was used to activate catalysts using a diesel refined for cars and trucks and was as follows: a. Unit was pressurized to 700 psig and hydrogen circulation was established at 1000 SCF/BBL ( Nl/hr) . b. Diesel feed was started to the catalyst bed at 1.5 LHSV and ambient temperature. c. The reactor temperature was raised to 121°C in one hour, then increased to 343°C at rate of 27.8°C/hour.

Temperatures were held at 343°C for 30 minutes. d. The reactor was then cooled over 2 hours to 246°C.

3) Activity Testing

For activity testing the unit was pressured up to 700 psig and heated to 246°C with a hydrogen gas rate of 220 SCF/bbl (13.2 Nl/hr). The VGO/LCO feed was started to the unit at 1.5 LHSV (66 gm/hr) . After the feed had wetted the entire bed (and product was noted in the separator) , the temperature was raised to 329°C at 22.2°C/hr. After the reactor was at 329°C, a 12 hour break-in period was begun. The product from this period was not analyzed. The run was continued with additional weight periods of 12 hours and the products of third weight period (37-48 hours) were analyzed for nitrogen and sulfur. From these values rate constants were calculated for the hydrodenitrification ("HDN") reaction and the hydrodesulfurization ("HDS") reaction. These provide an indication of how active the catalyst is, the higher the rate constant, the faster the reaction process, and the higher the conversion of sulfur and nitrogen at a given space velocity (feed rate) . For HDN the reaction order is 1.0 and the k value is calculated by the equation

J = ( space veloci ty) *_ln I cone . of N in feed

\ cone, of N in product}

For HDS the reaction is not first order and many values are used, but 1.7 is the value most used and is used herein to calculate as follows:

_R _ ( apace velocity ( 1 _ 1 1

I 1.7-1 ] \ [conc. of S in product) ⁰-¹ (con , of S in feed) ⁰-¹ j

The relative rate constants are provided in Table 8, normalized against the values for the third weight period for the COMP Catalyst.

Table 8: Activity Tests Weight Period

Catalyst Activation DS Rel.K Value HDN Rel. K Value

COMP 1) Standard 1.00 1.00

A 2) Diesel 0.94 0.88

B 2) Diesel 1.04 0.94

C 2) Diesel 0.87 0.87

D 2) Diesel 0.94 1.02

E 2) Diesel 1.00 1.01 As can be seen the catalysts of this invention show a comparable hydrodenitrification activity (without significant decrease in activity) to a traditional hydrotreating catalyst. Further, catalysts containing unsaturated hydrocarbons show advantage over catalyst with only saturated hydrocarbons with regard to the hydrodenitrification activity.

Example IV:

Z-753 Ni-W/Ultrastable Y zeolite based hydrocracking catalyst, (from Zeolyst International Inc.), was presulfurized according to the procedure outlined in Example I.

Sulfur was incorporated according to the method of Part A using 5.5 wt% of sulfur. Soybean oil and Neodene were impregnated on the catalyst according to the method of Part B. Carbon and sulfur content of the catalyst were analyzed using LECO corporation CS-244 carbon-sulfur analyzer. Fresh Basis Sulfur was calculated using the equation shown in Part D. Percent Stoichiometric sulfur was calculated by dividing the Fresh Basis Sulfur percent by the percent sulfur calculated for complete conversion of the oxidic nickel and tungsten to the corresponding Ni₃S₂ and WS₂ phases.

Table 10: Sulfur Retention

Carbon Sulfur Fresh Basis Percent

Sample wt.% wt.% Sulfur wt.% Stoichiometric Neodene" 11.1 1.4 1.6 43

Soybean¹* 20.5 2.4 3.1 84 a) as described in Table 2 as j) b) as described in Table 2 as g)

As can be seen from Table 10, the percent retention of sulfur is significantly improved by using a glyceride fatty acid ester such as soybean oil.

Performance Tests

A blend of 75 vol% hydrotreated cracked heavy gas oil, and 25 vol% hydrocracker bottoms stream was used as feedstock for performance testing of the zeolitic hydrocracking catalysts obtained from Example IV and the fresh Z-753 (Reference Catalyst) . Some of the feedstock properties are listed in Table 11. DMDS and n-amylamine were added to the feedstock to generate the requisite levels of H₂S and NH₃, respectively. Table 11: Performance Testing Feedstock Properties

ppm Sulfur 14 ppm Nitrogen 25 wt% Carbon 87 .334 wt% Hydrogen 12 .69

API Gravity 26 .1° 338+ ^βC (wt%) 71 .4

DMDS (wt%) o.: L33 n-amylamine (wt%) 0.1 D79

Simulated Distillation of Feedstock

WT% TEMP °C

IBP 181

5% 248

25% 330 50% 382

75% 434

90% 481

98% 537

FBP 572

Performance Testing Conditions

The conditions employed for the performance testing e zeolitic catalysts above are given in Table 12. Table 12: Performance Testing Conditions

Hydrogen Pressure (psig) 1800

Hydrogen Circulation (scf H₂/bbl feed) 8935

LHSV (hr^"1) 1.5 Cut Point for converison calculation (°C) 338°

Conversion Target (Single Pass, wt%) 80.0

Catalyst Activation Procedures

1) Zeolite Reference Catalyst: Gas Phase Activation The fresh Z-753 catalyst was dried at 482°C for one hour in air, cooled in a desiccator and loaded into the reactor. It was sulfided in a flow of 95% vol hydrogen/5% vol hydrogen sulfide at a GHSV of 1500 hr^"1, according to the following gas phase schedule:

a. ambient to 149°C, hold 1 hour a. 149°C to 371°C in six hours b. hold at 371°C for two hours c. cool reactor to 149°C and hold d. switch to pure hydrogen flow

lb) Zeolite Reference Catalyst: Licuid Phase Activation To activate the zeolite catalyst, after loading it dried, the reactor was brought to 1800 psig pure hydrogen, at a circulation rate of 8935 scf hydrogen/bbl feed. The acti¬ vation feedstock employed consisted of the performance testing feedstock containing sufficient dimethyldisulfide (DMDS) to produce 2.5 vol% H₂S, and n-amylamine to produce 150 ppm NH₃ in the gas phase, respectively. The procedure for the activation was as follows:

a. reactor brought to operating pressure and hydrogen rate b. activation feedstock introduced at 149°C c. 149°C to 232°C in 3 hours d. 232°C to 302°C in 18 hours e. 302 °C to 315 °C in 8 hours f. hold 315 °C for 8 hours g. switch to activity testing feedstock and adjust temperature to maintain 80 wt% conversion of feed.

During steps c-f, H₂S and i-butane were continuously monitored in the exit gas stream of the reactor. Temperature was ramped as long as H₂S remained above 2000 ppmv, and isobutane concentration remained below 0.4 vol%. Otherwise, the ramp was discontinued until these levels were realized.

2) Zeolitic Catalyst:

Gas Phase Activation with 5.0% vol H₇S.

The zeolitic hydrocracking catalyst from Example IV was dried at 482°C for one hour in air, cooled in a desiccator and loaded into the reactor. It was activated in the same manner as the catalyst in case 1) of this Example.

2a) Zeolitic Catalyst:

Gas Phase Activation with 0.5% vol H--.S. After reactor loading 25 cc of the zeolitic hydrocracking catalyst from Example IV and pressure testing, the following procedure was used for a gas phase activation that simulates 0.5% H₂S in the recycle gas: a. pressurize reactor to 450 psig with pure H₂ and establish a GHSV of 320 hr^'1. b. ramp temperature at 14°C/hr to 120°C; begin sampling the reactor off-gas for H₂S each 0.5 hr. c. switch to 0.5% H₂S/95.5% H₂ mixture d. ramp temperature to 205°C at 14°/hr. e. at 205°C, increase pressure to 1500 psig and establish a GHSV Of 850 hr^"1. f. ramp temperature to 370°C at 14°c/hr, interrupt ramp if H₂S in reactor off-gas drops below 2000 ppmv. g. hold at 370° for 4 hours h. cool to 149°C i. switch to pure H₂ and set pressure and flow rates for performance testing

2b) Zeolitic Catalyst: Liguid Feed Activation

The same method as for reference catalyst liquid activation was used to activate zeolitic catalyst from Example IV. The same activity testing feed was used with sufficient dimethyldisulfide (DMDS) and n-amylamine added to produce 2000 ppm H₂S and 150 ppm NH₃ in the gas phase, respectively. DMDS was added to the feed in order to simulate a minimum level of H₂S that could be tolerated during activation in the gas recycle loop of commercial units.

All gas phase activated catalysts (1), (2), (2a): After activation with the hydrogen sulfide/hydrogen mixture, the reactor was cooled to 149°C and the following startup procedure was implemented:

a. introduce activity testing feed at 149°C b. 149°C to 260°C in 5 hours c. 22°C/day for 4 days d. 5.5°C/day for 5 days e. adjust reactor temperature to maintain 80 wt% conversion of 338+ °C in feed.

Conversion (wt%) is defined as follows:

100 x tWt% 338+ °C in feed - Wt% 338+ °C in product)

(Wt% 338+ °C in Feed)

In this conversion definition, gaseous products are included. Performance Testing Results

Liquid and gas product streams were both analyzed and mass balanced yields based on feed oil and hydrogen were calculated. Representative weight period results from testing of the three zeolite catalysts are found in Table 13. Values for product cuts are reported as mass balanced wt% based on feed.

Table 13. Representative performance measures for zeolitic hydrocracking catalysts.* Values reported are calculated for 80% conversion.

PRODUCT CUTS (°C)

Catalvst^b Temp C,^ C<-82° 82-190° 190-288° 288-338° 338°+

1 378 15.0 23.0 37.8 9.1 2.7 14.5

lb 381 17.1 23.5 35.4 8.0 3.3 14.5

2 378 12.1 18.5 40.6 12.3 3.6 14.5

2a 381 14.4 19.3 39.7 11.5 3.7 14.4

2b 377 11.8 19.1 42.0 10.9 3.2 14.5

Catalyst" Tem -C, C_τ-82 82-190 190-288 288-338 338+ 1 384 17.7 25.4 34.9 7.3 2.3 14.6

2a 387 17.3 22.9 35.1 8.8 3.3 14.5

2b 381 13.2 19.9 40.9 10.4 2.9 14.5

(a) Absence of a letter following the catalyst reference number denotes gas phase activation with 5% H₂S/95% H₂, "a" following the catalyst number denotes gas phase activation with 0.5% H₂S/99.5% H₂, and "b" denotes liquid phase activation. (b) Values reported are for 700 hours on feed, (c) Values reported are for 1400 hours on feed. As can be seen from Table 13, the zeolitic catalysts of this invention (2,2a,2b) show a significant improvement in liquid yield relative to the reference catalysts (1 and lb) . This improvement occurs regardless of whether the reference catalyst was activated in liquid phase or gas phase, but the more appropriate comparison of the two liquid phase activations reveals the greatest advantage for the invention catalyst. In this case, the catalyst also exhibits an advantage in activity, with a 3°C lower temperature requirement at 80 wt% conversion.

Table 14. Yield stability data on selected cuts for reference and invention catalysts.

C,-C₄ Yields 82-190°C Yields HOURS ==> 500 1000 1600 500 1000 1600 Catalyst

1 13.8 16.6 18.3 38.6 36.4 34.5

lb 15.4 19.5 37.3 32.8

11.1 14.2 41.4 39.0

2a 11.6 14.8 16.8 40.6 37.8 35.5

2b 10.1 12.7 13.2 43.0 41.0 40.7

Table 14 illustrates the additional benefit of yield stability associated with the process of liquid phase activation of the catalysts prepared according to Example IV. Both the gas phase activated reference catalyst (1) and the liquid phase activated invention catalyst (2b) have an initial C1-C4 yield decline rate of 5.6 wt%/1000 hrs. However, in the case of (2b), the yield decline rate between 1000 and 1600 hours on feed has dropped to 0.8 wt%/1000 hrs, while that of (1) is 2.8 wt%/1000 hrs. The case is even more dramatic when examining the naphtha range (82-190°C) liquid yields. The 1000-1600 hours yield decline rate for (1) is 3.2 wt%/1000 hrs, while that of (2b) is only 0.5 wt%/1000 hrs. This yield stability can translate into significant improvement in output of valuable products for the refiner, at the same time decreasing the production of the less valuable C1-C4 stream.

Example V In this Example a spontaneously combustible or self-heating catalyst is unloaded from a reactor after treatment with oxygen- containing hydrocarbon.

A highly self-heating, spent, hydrotreating catalyst listed below (obtained from a hydrotreating reactor) was treated with 1.5 Wt. % soybean oil in a carrier oil (feed stream) and a second sample of same material was treated with 100% soybean oil. The mixtures were heated to 140°C under nitrogen for one hour and then cooled and drained. The material was tested for self-heating properties according to Appendix E of 49 CFR 173 (Test for Class 4, Division 4.2 Substances in Code of Federal Regulations), which requires a 2.5 cm cube size sample and a 10 cm cube size sample.

The samples were further analyzed for exothermic onset by a Differential Scanning Calorimetry, Mettler's TA 4000 using a DSC27HP DSC measuring cell. For the purposes of this test the onset and half the distance along the trace to the first peak were entered to calculate the onset temperature and slop of the curve. The sample was heated from 30°C to 500°C at 10°C per minute. A 500 cc/min of air purge the DSC measuring during the test.

Catalyst Properties: Cobalt/Molybdenum on activated alumina Size 1/20 inch

Shape Quadralobe Form Spent

Carbon 12.9 Wt. %

Sulfur 7.9 Wt. % Both samples treated with soybean oil (at 1.5 and 100%) passed the Large Basket Test as described in Appendix E of 49 CFR 173. The untreated sample failed the Large Basket Test.

Exothermic Onset temperatures for the samples determined by DSC are as follows:

Table 15

* samp es integra e rom onset to 500°C

Samples treated with soybean oil have reduced self-heating. The sample treated with 100% soybean oil have a smaller overall exotherm than the 1.5 Wt.% treated sample as shown by the integration values for each sample.

Claims

1 . A composition comprising a spontaneously combustible catalyst at

least a part of which has been coated and/or impregnated with at least one

oxygen-containing hydrocarbon having at least 12 carbon atoms, thereby

reducing the self-heating characteristics of said catalyst.

2. A composition according to claim 1 wherein the oxygen-

containing hydrocarbon is an acid, acid ester, alcohol, ketone, aldehyde or ether,

having at least 1 2 carbon atoms.

3. A composition according to claim 2 wherein the acid ester is a

glyceride fatty acid ester having from 16 to 100 carbon atoms.

4. A composition according to any one of claims 1 to 3 wherein the

oxygen-containing hydrocarbon has from 1 6 to 80 carbon atoms.

5. A composition according to claim 3 or 4 wherein the acid ester is

an unsaturated fatty acid ester.

6. A composition according to claim 5 wherein the ester is derived

from palmitoleic, oleic, linoleic, linolenic, eleostearic, ricinoleic, eicosenoic,

docosenoic, eicosatetraenoic, eicosapentaenoic, decosapentaenoic or

docosahexaenoic acid or a mixture thereof.

7. A composition according to claim 5 or 6 wherein the ester is

derived from soybean oil, linseed oil, safflower oil, sunflower oil, corn oil,

cottonseed oil, olive oil, tung oil, castor oil, rapeseed oil, tall oil, peanut oil,

canbra oil, perilla oil, vegetable residue, marine oil or a mixture thereof.

8. A composition according to claim 3 or 4 wherein the ester is a

saturated fatty acid ester.

9. A composition according to claim 8 wherein the saturated fatty acid ester is derived from coconut oil, palm oil, lard or tallow or a mixture thereof.

10. A composition according to any one of the preceding claims

wherein the catalyst comprises at least one metal, metal sulfide or metal oxide

of a metal of Group VIB or Group VIII of the Periodic Table.

1 1 . A composition according to claim 10 wherein the catalyst is

supported on alumina, silica, silica-alumina, zeolite or a mixture thereof.

1 2. A composition according to any one of the preceding claims

wherein the catalyst is a presulfurized or a sulfided catalyst.

1 3. A composition according to any one of claims 1 to 1 1 wherein

the catalyst is a reduced catalyst.

14. A composition according to any one of claims 1 to 1 1 wherein

the catalyst is a hydrocracking catalyst.

15. A composition according to any one of claims 1 to 1 1 wherein

the catalyst is a hydrotreating catalyst.

1 6. A method of reducing the self-heating characteristics of a

spontaneously combustible catalyst contacting said spontaneously combustible

catalyst with at least one oxygen-containing hydrocarbon having at least 12

carbon atoms.

17. A method according to claim 1 6 wherein the hydrocarbon is one

defined in any one of claims 1 to 9.

1 8. A method according to claim 1 6 or 1 7 wherein the catalyst is

one defined in any one of claims 10 to 1 5..

1 9. A process for preparing catalyst suitable for hydrotreating and/or

hydrocracking a hydrocarbon stream or tail gas treating a sulfur-containing gas stream, which comprises heating a presulfurized composition as claimed in claim

1 2 to 200oC to 500oC in the presence of hydrogen to produce metal sulfide.

20. A process according to claim 19 wherein the catalyst is activated

by heating the treated presulfurized catalyst in the presence of hydrogen and at

least one hydrocarbon having a boiling point of at least about 35°C at

atmospheric pressure at a temperature from 25°C to 430°C, a hydrogen partial

pressure from 50 psig to 3000 psig and a Liquid Hourly Space Velocity from 0.1

to 20 hr¹.

21 . A process according to claim 20 wherein the hydrocarbon has a

boiling point of 40°C to 700°C.

22. A process according to claim 20 and 21 wherein the hydrocarbon

has a boiling point from 85°C to 500°C.

23. A process according to any one of claims 20 to 22 wherein the

hydrocarbon is jet fuel, kerosine, diesel fuel, gasoline, gas oil, residual gas oil or

hydrocarbon feed stream.

24. A method of presulfurizing porous particles of a sulfidable

catalyst containing at least one metal or metal oxide, which comprises:

(a) contacting said catalyst with elemental sulfur at a

temperature such that at least a portion of said sulfur is incorporating in the

pores of said catalyst by sublimation and/or melting; and

(b) prior to, at the same time or subsequently contacting said

catalyst particles with at least one oxygen-containing hydrocarbon having at

least 1 2 carbon atoms.

25. A method of presulfurizing porous particles of a sulfidable

catalyst containing at least one metal or metal oxide, which comprises; (a) contacting said catalyst with at least one sulfur compound under conditions so as to incorporate at least a portion of said sulfur compound

in the pores of said catalyst by impregnation; and

(b) prior to, concurrently or subsequently contacting said

catalyst particles with at least one oxygen-containing hydrocarbon having at

least 20 carbon atoms.

26. A method according to claim 24 or 25 wherein the hydrocarbon

is one defined in any one of claims 3 and 5 to 8.

27. A method of presulfurizing porous particles of a sulfidable

catalyst containing at least one metal or metal oxide, which comprises:

(a) contacting said catalyst with at least one sulfur compound

under conditions so as to incorporate at least a portion of said sulfur compound

in the pores of said catalyst by impregnation; and

(b) prior to, concurrently or subsequently contacting said catalyst particles with at least one glyceride fatty acid ester having at least 12

carbon atoms.

28. A method according to any one of claims 24 to 27 wherein the

hydrocarbon is one defined in any one of claims 2, 4 and 9 to 1 5.

29. A process for hydrotreating and/or hydrocracking a hydrocarbon

stream or tail gas treating sulfur-containing gas stream which comprises

contacting the stream in the presence of hydrogen with a sulfided catalyst as

claimed in claim 14 or 1 5 or one prepared by a process as claimed in claim 19.

30. A process according to claim 29 wherein the stream is contacted

with the hydrocracking catalyst at a temperature from 100°C to 450°C.

31. A method nf transporting a spontaneously combustible catalyst which comprises contacting the catalyst with at least one oxygen-containing hydrocarbon having at least 12 carbon atoms, placing the treated catalyst in a container and then transporting the container.

32. A method according to claim 31 wherein at least 100 kg of catalyst Is placed in εaid container.

33. A method according to claim 32 wherein at least 250 kg of catalyst is placed In said container.

34. A method of unloading a catalyst from a reactor in operation which comprising stopping reactor operation, contacting εaid catalyst In the reactor with at least one oxygen-containing hydrocarbon having at least 2 carbon atoms and then reπioving the oxygen-containing hydrocarbon treated catalyst from the reactor.

35. A method according to any of claims 29 to 34 wherein the hydrocarbon is as defined in any one of claims 2 to 9.