US3814681A - Control of asphaltic oil hydrode-sulfurization process - Google Patents

Abstract

ASPHALT-CONTAINING OILS ARE HYDRODESULFURIZED WITHOUT EXCESSIVELY CONVERTING THE ASPHALTENES AND RESINS PRESENT BY CONTROLLING THE EXTENT OF DESULFURIZATION OF THE ASPHALTIC PORTION OF THE OIL IN RESPONSE TO THE QUANTITY OF AROMATICS PRESENT. AS THE ASPHALTIC OIL PASSES THROUGH A HYDRODESULFURIZATION ZONE, THE AROMATIC CONTENT OF THE OIL INCREASES DUE TO IN SITU PRODCTION OF AROMATICS. THE OIL IS WITH-

DRAWN FROM THE HYDRODESULFURIZATION ZONE WHEN THE AROMATIC CONTENT NO LONGER INCREASES.

Description

June 4, 1974 MC E'TAL 3,814,68}

CONTROL OF ASPHALTIC OIL HYDRODESULFURIZATION PROCESS Filed Dec. 8, 1971 4 Sheets-Sheet 1 I O 01 cu j 2 a 5 Q 5 LI.

MAKE-UP HYDROGEN June 4, 1974 J. MCKINNEY ET AL 3,814,681

CONTROL OF ASPHALTIC OIL HYDRODESULFURIZATION PROCESS 4 Sheets-Sheet 2 Filed Dec. 8, 1971 750 AVERAGE REACTOR TEMPERATURE: F.

.5053 5 Q E; oowm FIG. 2

SATURATES mzommgome: +503 3 Emzthmzoo 6 .5653

I0 4O 5O 6O 7O I00 PERCENT DESULFURIZATION FIG. 3

June 4, 1974 J. D. MCKINNEY ET AL 3,814,681

CONTROL OF ASPHALTIC OIL HYDRODESULFURIZATION PROCESS Filed Dec.

FIG. 4

FIG. 6

VOL.9% 0F COMPONENTIN OVERHEAD o68 3883888 l 4 Sheet-Sheet 5 June 4, 1974 J. McKm Y ETAL 3,814,681

CONTROL OF ASPHALTIC OIL HYDRODESULFURIZATION PROCESS Filed Dec. 8, 1971 4 Sheets-Sheet 4 424 FIG. 7

United States Patent 3,814,681 CONTROL OF ASPHALTIC OIL HYDRODE- SULFURIZATION PROCESS Joel D. McKinney and John A. Paraskos, Pittsburgh, Pa.,

assiguors to Gulf Research & Development Company, Pittsburgh, Pa.

Filed Dec. 8, 1971, Ser. No. 206,078 The portion of the term of the patent subsequent to Nov. 27, 1990, has been disclaimed Int. Cl. Cg 23/02 US. Cl. 208210 9 Claims ABSTRACT OF THE DISCLOSURE Asphalt-containing oils are hydrodesulfurized without excessively converting the asphaltenes and resins present by controlling the extent of desulfurization of the asphaltic portion of the oil in response to the quantity of aromatics present. -As the asphaltic oil passes through a hydrodesulfurization zone, the aromatic content of the oil increases due to in situ production of aromatics. The oil is withdrawn from the hydrodesulfurization zone when the aromatic content no longer increases.

This invention relates to a process for the production of crude or residual oils having an especially low sulfur content. More particularly, this invention relates to a hydrodesulfurization process for producing an asphaltic fuel oil having a low sulfur content.

Various processes have been proposed for the desulfurization of petroleum hydrocarbons, and such processes have been highly effective in the removal of sulfur from the relatively lighter distillate fractions that are obtained from the distillation of crude oil. However, crude oil and reduced crude oil fractions contain a heavy, residue fraction boiling above 1040 F. commonly referred to as asphalt, which renders the oil much more difiicult to desulfurize. Asphalt is a generally low-grade material that has been isolated from the crude oil and utilized in road construction. In addition, it has been proposed to treat the asphaltic fraction of crude oil in some manner so as to upgrade this material into a more valuable product such as a fuel oil. However, asphalt, when isolated, is highly viscous and is difficult to process over a catalyst. Moreover, it consists of large molecules of fused, aromatic rings and contains the greatest amount of the total sulfur content of the full range crude on a relative basis. A further problem is that some of the sulfur content of the asphalt is tied up in the interior of the large molecules thereof, rendering the asphalt especially difiicult to desulfurize. In addition, asphalt contains metals, principally nickel and vanadium, which readily deposit on desulfurization catalysts tending to deactivate the catalyst. The cumulative effect of such factors is that much more severe conditions in the form of higher temperatures and pressures are required as well as a different type of catalyst in order to remove the sulfur from heavy, asphaltic oils as compared with desulfurization of a distillate oil.

Sulfur is a major contributor to air pollution. Accordingly, certain municipalities, both local and foreign, have placed an upper limit on the sulfur content of fuel oils. In the past, such locales have placed a one percent by weight sulfur limit on heavy fuel oils, but the trend has been to a lower maximum sulfur content, such as 0.5 percent. Such limitations have provided a major impediment to the use of heavy asphaltic hydrocarbon oil fractions as fuel oil, since an asphaltic fuel oil having an 0.5 percent sulfur content is not easily obtained from some high sulfur crudes merely by passing the crude oil over a desulfurization catalyst.

For reasons previously unappreciated, the sulfur conice tent of a particular asphaltic crude or reduced oil could be reduced to one percent sulfur in a hydrodesulfurization zone, but if the sulfur level was to be reduced below one percent, the desulfurization temperature had to be increased to a point at which excessive hydrocracking to lower boiling materials resulted. Thus, while it had been relatively easy to reduce the sulfur level of such residual oils from 4 to 1 percent by weight of sulfur without incurring excessive cracking of the feed, it is substantially more difficult for a majority of typical feeds to remove more than about percent of the sulfur without excessive hydrocracking. Excessive hydrocracking is undesirable since it unnecessarily consumes hydrogen and produces undesired light products and coke on the desulfurization catalyst. Furthermore, the nature of the resulting product can be altered to the extent that it is not a heavy fuel oil whereas heavy oils generally have a higher heating value than lighter oils.

Alternatives to attempted in-depth desulfurization of such asphaltic fractions have included blending of the I asphaltic hydrocarbon oil with essentially sulfur-free middle distillate oils in order to provide a low sulfur-containing fuel oil. Other proposals have involved hydrofining asphaltenic oils, under conditions wherein the asphaltic material is hydrocracked to extinction to produce lower boiling hydrocarbon products.

It woulde be highly desirable to provide a process for desulfurizing asphalt-containing hydrocarbon oils so as to render them suitable for use as heavy fuel oils without the need for either blending such materials with lighter oils or converting the asphalt content of such oils to lower-boiling products of a completely different nature which would prematurely deactivate the catalyst.

A relatively simple process for controlling the hydro desulfurization of an asphaltic oil without subjecting the oil to excessive hydrocracking has now been found, which process comprises passing a residual oil, for example, which oil contains an asphaltic fraction, through a hydrodesulfurization zone in the presence of hydrogen. The asphaltic oil increases in aromatics content as it passes through the hydrodesulfurization zone due to in situ aromatics production. The asphaltic oil having a substantially reduced sulfur content is withdrawn from the hydrode sulfurization zone at substantially the point at which the aromatic content of the oil no longer increases.

As will be hereinafter demonstrated, it has been discovered that as the asphaltic oil passes through the hydrodesulfurization zone, aromatic fragments of the difiiculty desulfurizable asphaltic portion of the oil are separated from the periphery of the complex, asphaltic molecules. These aromatics act as a solvent for the asphaltic material and enable this material to be desulfurized without its being excessively converted. By controlling the desulfurization process such that the asphaltic oil is hydrodesulfurized in the presence of a continually increasing percentage by weight of aromatics, or at least under conditions such that the percent by weight of aromatics present does not decrease, excessive hydrocracking of the asphaltic fraction is avoided, while desulfurization of the asphaltic fraction is optimized under the conditions employed.

Thus, for example, a particular fuel oil containing an asphaltic fraction may be produced having a sulfur content below one percent by weight by means of the present invention, by subjecting an asphalt-containing or asphaltic, hydrocarbon oil, such as a crude oil or residual oil (a reduced crude) containing more than about one percent sulfur to a hydrodesulfurization zone in the presence of hydrogen and withdrawing a first effluent having a reduced sulfur content relative to the feedstock from the hydrodesulfurization zone when the aromatic content of the oil no longer increases. -The efiiuent comprises hydrogen sulfide, a light gas fraction, an oil fraction containing aromatics and saturates, and a higher boiling, asphaltic fraction. The oil fraction is referred to as light oil" to contrast it with the higher boiling asphaltic fraction. Next, the hydrogen sulfide, the light gas fraction, and a low boiling portion of the light oil fraction are separated from the effluent, and the remaining portion of the effluent comprising the asphaltic fraction and a higher boiling portion of the oil fraction may be passed to a second hydrodesulfurization zone in the presence of hydrogen. Each hydrodesulfurization zone is provided with a hydrodesulfurization catalyst that is disposed on a non-cracking support. An asphaltic hydrocarbon oil is withdrawn from the second hydrodesulfurization zone which oil provides a heavy, asphaltic fuel oil containing less than one percent by weight sulfur. The sulfur content of the resulting heavy fuel oil can be reduced to below one percent, for example, to below 0.5 and 0.3 percent by weight sulfur.

As will be hereinafter described, the asphaltic, hydrocarbon oil containing more than about one percent sulfur which is obtained, for example, from the first desulfurization zone may be passed to a second hydrodesulfurization zone in the presence of hydrogen and a light oil fraction comprising aromatics and saturates having a boiling point below the asphaltic portion of the feedstock to the second hydrodesulfurization zone, and controlling the amount of light oil present in the zone, and thus the amount of aromatics and saturates that are passed to the hydrodesulfurization zone to increase the desulfurization rate and permit the recovery of a heavy, asphaltic fuel oil containing less than about one percent sulfur.

Thus, the present invention can provide an asphaltcontaining heavy fuel oil, which is practically sulfur free, without the need for blending the asphaltic fuel oil with a sulfur-free middle distillate oil in order to obtain an oil having a low sulfur content, although such blending is not precluded in accordance With the present invention.

The term asphalt or asphaltic as employed in the present specification is intended to include the resins and asphaltenes present in crude oil. Asphalt can constitute approximately to 30 percent by volume or more of crude oil and has an initial boiling point of about 1040 F. It is obtained in refineries by a propane deasphalting process (solvent extraction), or from the residues obtained from distillation. Asphaltenes are highly aromatic and consist of large molecules of fused aromatics rings and normally contain the greatest sulfur concentration of any constituent of the full range crude. Unlike other crude fractions, asphalt also contains metals, principally nickel and vanadium. Thus, the asphaltenes and resins may be distinguished from the remainder of the crude oil, which material comprises saturates and aromatics, by virtue of the solubility of these aromatics and saturates in propane and the insolubility of the asphaltenes and resins in propane.

The propane-soluble aromatics include benzenes, naphthalenes, thiophenes, benzothiophenes, and dibenzothiophenes as the predominant molecular species, while the saturates include the non-aromatic, propane-soluble species, such as the naphthenes, e.g., cyclohexanes, and the paraflins, e.g., dodecane, and sulfur-containing compounds, such as s-butyl mercaptan. Thus, the material commonly referred to as asphalt comprises the residue of a propane extraction. On the other hand, resins and asphaltenes are themselves separable by a pentane extraction, by virtue of the fact that asphaltenes are insoluble in pentane, while both resins and oils are soluble in pentane.

It has been proposed to subject crude oil or a reduced crude containing the asphaltene fraction to a hydrodesulfurization reaction in order to reduce the sulfur content of the crude. The crude oil or reduced crude is passed over Group VI and Group VIII metals on a noncracking support, such as alumina, in the presence of hydrogen and the sulfur level is relatively easily reduced from about 4 to about 1 percent by weight, i.e., a 75 percent sulfur removal. However, after about 75 percent sulfur removal is effected with a particular feed, such as a Kuwait crude for example, the sulfur content of the feed suddenly becomes quite refractory and a great deal of hydrocracking is experienced in order to accomplish additional sulfur removal thereby consuming a great deal of hydrogen and changing the nature of the product. Thus, the point at which the sulfur remaining in the crude oil becomes refractory may vary with the nature of the particular type of crude oil. This point may be easily determined experimentally. As previously mentioned, the asphaltenes consist of large molecules of fused aromatic rings and contain sulfur in the interior of the large molecules, thereby rendering the sulfur extremely difficult to remove. In addition, the asphalt contains all of the metals, such as nickel and vanadium that are present in the crude, and these metals readily deposit on the catalyst tending to deactivate the catalyst and reduce its effectiveness. For these reasons, more severe conditions in the form of higher temperatures and pressures are required to remove more than 75 percent of the sulfur from the asphaltic oil and such severe conditions result in hydrocracking, i.e., a severing of the carboncarbon bonds of the asphaltene molecule resulting in lower molecular weight materials, rather than desul furization by splitting carbon-sulfur bonds.

In order to more fully understand the process of the present invention, reference is made to the drawings wherein:

FIG. 1 is a flow diagram illustrating the desulfurization of an asphaltic, reduced crude in two stages;

FIG. 2 illustrates graphically the percent yield of materials boiling above the initial boiling point of the feed to a desulfurization reactor as the average reactor temperature increases;

FIG. 3 graphically illustrates the change in concentration of the aromatic, saturate, asphaltene and resin fractions of an asphalt-containing reduced crude as the degree of desulfurization increases;

FIG. 4 graphically illustrates volume percentages of aromatics and saturates that are removed at various interstages flash points; and

FIGS. 5 to 9 are diagrammatic schemes for obtaining a low sulfur, light aromatic-rich fraction from one portion of the feedstock to solubilize and reduce the viscosity of the solution of asphaltenes and resins present in the residual portion of the feed prior to desulfurization of the asphaltenes and resins.

- Referring to FIG. 1, a reduced crude such as a 50 percent reduced Kuwait crude which contains the entire asphalt content of the full crude and therefore also contains all of the nickel and vanadium and most refractory sulfur content of the full crude is charged to the process through line 10 and is pumped through line 14, preheater 16, line 18, solids filter 20 and line 22 and drum 24. From drum 24. is the liquid oil charge is passed through line 24 to feed pump 30.

Liquid from pump 30 is admixed with hydrogen from line 32 and passed through line 34, valve 36, line 38 and furnace 40. Liquid flow valve 36 is disposed in a nonfully preheated liquid hydrocarbon line. Recycled hydrogen along with make-up hydrogen (if desired) are introduced into the liquid charge to the reactor prior to the preheating thereof. Recycled hydrogen is passed through line 42 and valve 44, While make-up hydrogen may be charged through line 46, compressor 48 and valve 50. The recycled hydrogen and any makeup hydrogen are introduced to the relatively cool liquid charge through line 32.

A preheated mixture of liquid charge and hydrogen in line 54 may be passed through a guard reactor (not shown), if desired. An efiluent stream from the guard reactor is charged to the main reactor 60 containing catalyst beds 62, 64 and 66. This stream may have a 650 F.+ boiling range, for example.

The hydrodesulfurization catalyst employed in the process of the present invention is conventional and comprises, for example, Group VI and Group VIII metals on a non-cracking support. Thus, the catalyst may comprise nickel-cobalt-molybdenum or cobalt-molybdenum on an alumina support. The alumina may be stabilized with 1 to 5 percent by weight of silica. The preferred catalyst is a nickel-cobalt-molybdenum on alumina containing less than 1 percent silica which catalyst may or may not be sulfided. Magnesia is also a non-cracking support. An especially preferred catalyst comprises a particulate catalyst comprising particles between about and 4 inch in diameter, such as described in US. Pat. 3,562,800 to Carlson et al., which patent is hereby incorporated by reference. The same or a different hydrodesulfurization catalyst can be employed in each stage.

An essential feature of the present invention is that the catalyst is provided on a non-cracking support, since the process of the present invention is essentially a noncracking process in that very little material is produced having a boiling point below the initial boiling point of the feed. However, high boiling material in the feed may be cracked to produce lower boiling products still in the boiling range of the feed. Thus, whereas prior processes have employed techniques involving, for example, high silica-containing catalysts, e.g. percent or more silica, to hydrocrack the asphaltenes in the feedstock, the process of the present invention involves mainly the severance of carbon-sulfur bonds of the asphaltenes and resins in order to desulfurize the difficulty desulfurizable asphalt, rather than cracking carbon-carbon bonds, which results in lower molecular weight materials. Of course, sulfur is removed from oils during the present process, but this type of sulfur removal is relatively easy to accomplish. In other words, the cracking of carbon-carbon bonds as in prior processes employing cracking produces a material other than a heavy fuel oil and is outside the scope of the present invention. Thus, a relatively minor amount of material is produced having a boiling point below the initial boiling point of the feed to the hydrodesulfurization unit.

As previously mentioned, hydrogen is introduced along with the feedstock by means of line 32. Conventional reaction conditions in the hydrodesulfurization reactor are employed, for example, a hydrogen partial pressure of 1000 to 5000 pounds per square inch, preferably 1000 to 3000 pounds per square inch, is employed. A hydrogen partial pressure of 1500 to 2500 pounds per square inch is especially preferred. The gas circulation rate may be between about 200 and 20,000 standard cubic feet per barrel, generally, or preferably about 3000 to 10,000 standard cubic feet per barrel of feed, and preferably containing 85 percent or more of hydrogen. The mol ratio of hydrogen to oil may be between about 8:1 and 80:1.

It is an essential feature of the present invention that a hydrogen partial pressure of at least 1000 pounds per square inch is provided. This is necessary in order to desulfurize the asphaltic oil of the present invention to the necessary extent and in order to get the hydrogen to the reactive surface of the asphaltene molecule. It is the chemical activity as expressed by the partial pressure of hydrogen rather than total reactor pressure which determines hydrodesulfurization activity.

Hydrodesulfurization reactor temperatures may range between about 650 and about 900 F, and preferably between about 680 and 800 F.

Referring again to FIG. 1, each succeeding catalyst bed 62, 64 and 66, may have a larger volume than the bed just prior to it. If desired, there may be 4 to 6 catalyst beds in the reactor and, if desired, each reactor bed may have 25 percent, 50 percent, 100 percent or more catalyst than the bed just prior to it.

As previously mentioned, because there is no guard chamber line 54 will lead directly to the reactor. The eflluent in line 54 is joined by a hydrogen stream from line 67, valve 69, line 70 and valve 72 so that a hydrocarbon and hydrogen stream is charged to the top of the reactor through line 74. As previously mentioned, the reactor stream is passed through catalyst bed 62 and due to the exothermic nature of the hydrodesulfurization reaction, it becomes heated in passage therethrough. Temperatures between the various catalyst beds may be controlled by employing a hydrogen quench which may be introduced by means of line 76, valve 78, sparger 80, and line 82, valve 84 and sparger 86. Finally, the reaction mixture passes through catalyst bed 66 and then leaves the reactor with, for example, about a one percent by weight sulfur content.

Referring now to FIG. 2, it is seen that as an asphaltic hydrocarbon crude oil residue containing 4 percent sulfur is passed through a hydrodesulfurization zone, such as reactor 60 in FIG. 1, to produce a 1 percent sulfur-containing 660 F.+ product, Well over percent of the product boils at 660 F. or above (the initial boiling point of the feed) as the average reactor temperature is increased to compensate for catalyst aging. However, when the reaction temperature is raised to 800 F., excessive hydrocracking to lower boiling materials results. This causes a drop in the curve as to the materials boiling below the initial boiling point of the feed. At this point excessive hydrocracking occurs in order to produce a 1 percent sulfur-containing 660 F product.

As will be hereinafter demonstrated, the process of the present invention permits the efiicient removal of greater than 75 percent sulfur from an asphaltic oil and overcomes the refractory nature of such oils.

Reference is now made, once again to FIG. 1. Next, the eflluent in line 88 is passed to a high pressure flash chamber 90 wherein light hydrocarbon gases, hydrogen sulfide, hydrogen and a controlled portion of the relatively highly desulfurized saturates and aromatics are removed by means of line 92. The operation of this interstage flash chamber 90' constitutes a critical feature of the present invention. By carefully selecting the flash temperature at the process pressure, the proper amount of light oil, which is to be removed from the feedstock to the second hydrodesulfurization feed stream, is determined. The reason for the removal of an amount of light oil will be demonstrated by reference to FIG. 3.

Referring now to FIG. 3, the composition of a 650 F.+ hydrocarbon oil containing various proportions of aromatics, saturates, resins and asphaltenes is presented, as the oil is passed through a hydrodesulfurization reactor, such as reactor 60 of FIG. 1. As shown in FIG. 3, the resins and asphaltenes content of the feed steadily decreases with increasing sulfur removal due to the severing of carbon-sulfur bonds thereby breaking off molecular fragments. The accumulation of these molecular fragments is reflected in the build-up of lower molecular saturates and aromatics and particularly aromatics. This increase in aromatics content in the liquid is beneficial because the aromatics constitute a solvent for the highly viscous resins and asphaltenes, whereas the resins and asphaltenes are not solvated by saturates. The deulfurization of each fraction continues until about 75 percent sulfur removal, and at that point the resins and aromatics curves reach a plateau which indicates no further cracking of fragments therefrom. At the same time, the total aromatics and saturates content does not increase further, but an increase in saturates level is accompanied by a decrease in aromatics level. This indicates that at 75 percent sulfur removal the aromatics tend to become saturated, which represents not only a fruitless consumption of hydrogen, but deprives the remaining resins and asphaltenes of aromatic solvent, while merely increasing the amount of saturates, which is a mere dispersant.

At the 75 percent sulfur-removal level, the sulfur becomes refractory to further desulfurization so that further desulfurization is accompanied by a loss in aromatics and a sharp increase in saturates. Both of these factors are detrimental in regard to removing further sulfur and overcoming the refractory nature of the oil at this point, since at the 75 percent sulfur-removal level most of the unremoved sulfur is concentrated in the resins and asphaltenes. Thus, a loss of aromatics deprives the viscous resins and asphaltenes of some solvation, while the formation of saturates imparts an excessive dispersion to the system tending to excessively dilute the remaining sulfur and thereby lower the reaction rate.

Thus, while operating the first hydrodesulfurization reactor, the aromatic content of the oil can be measured as it passes through the reactor, and the oil should be withdrawn from the reactor when the aromatic content of the oil is no longer increased. This was the situation at 75 percent desulfurization in FIG. 3. The aromatic content can increase 25 to 40 percent by weight or more as it passes through the reactor. Even a small increase in aromatics concentration is beneficial, e.g. 2 to 5 or percent by weight. 'Of course, the aromatics concentration should not increase to such a great extent that it unduly dilutes the sulfur which is to be removed.

Without attempting to limit the present invention to any particular theory or mechanism, it is believed that up to the 75 percent sulfur removal there is a removal of fringe sulfur from the complex heterocyclic ring structure of the asphaltene molecule accompanied by an in situ production of aromatic hydrocarbons mainly due to a severing of the carbon-sulfur bonds on the fringe aromatic rings. This production of aromatics is important, since asphaltene molecules have a tendency to form colloidal crystallites or aggregates, if the molecules are poorly solubilized. Thus, up to the 75 percent sulfur removal level, there is suflicient in situ production of aromatics to solubilize the asphaltene particle and permit contact of the internal, heterocyclic sulfur with the hydrogen and catalyst necessary to desulfurize the asphaltene. However, at the 75 percent desulfurization level, the ratio of aromatics to saturates is sufliciently small that there is insufficient solvent and too much diluent to effect the removal of the refractory sulfur.

For this reason, it is necessary to control the aromatic content of the asphaltic feed to the second hydrodesulfurization zone. This may be accomplished by flashing or otherwise separating, e.g. by distillation or flashing followed by partial condensation of flashed hydrocarbon and recycle, a controlled portion of the normally liquid eflluent oil from the first desulfurization zone to provide the proper aromatics content to the stream.

Thus, it is essential to include sufficient aromatics in the feed to the second desulfurization reactor to solubilize the resins and asphaltenes in the oil and to deagglomerate any asphaltene aggregate which may be formed. At any given flash temperature, the removal of a particular quantity of aromatic hydrocarbons normally removes an even greater quantity of saturated hydrocarbons. With certain crudes the flash may remove more aromatics than saturates, in which case the benefit of the flash will be derived from removal of excess dispersent. A compromise must be reached wherein sufflcient aromatics are charged along with the feed to the second hydrodesulfurization stage so that the resins and asphaltenes are adequately solvated in order to permit proper desulfurization of the resins and asphaltenes, without the quantity of aromatics being so high that the total aromatics and saturates fed to the second stage will excessively dilute and disperse the sulfur to be removed and thereby reduce the reaction rate. The volume of aromatics and saturates, respectively, which may be removed at a given flash point is shown in FIG. 4.

Referring now to the solid lines of FIG. 4, an analysis of the saturate and aromatic content of the first sulfur removal stage effluent is shown for various flash points when measured at atmospheric pressure. Thus, if the interstage flash point is 500 F, all of the aromatics boiling above 500 F. will enter the second stage and will be available for solvating the resins and asphaltenes. However, at 500 F., the stream comprises about 81 percent by volume saturates and about 19 percent by volume aromatics. This amount of aromatics together with the even greater amount of saturates which necessarily accompany it, might excessively dilute the asphaltic compounds and thereby lower the reaction rate. On the other hand, if the interstage flash point is as high as 800 F., the oil fed to the second stage will have a higher ratio of aromatics to saturates which is desirable in order to accomplish high solvation with minimum diluent. However, at the 800 F. fiashpoint, the total amount of aromatics which enter the second stage may not be great enough to dissolve the resins and asphaltenes and to sufliciently lower their viscosity to permit desulfurization. Accordingly, a proper balance of aromatics to saturates must be employed in order to obtain optimum desulfurization. This point may be easily experimentally determined for a particular stream undergoing desulfurization. For example, employing as a feed the residue represented by the overhead designated by the solid lines of FIG. 4, the best results are obtained by flashing at the temperature which gives about a 650 F. separation regardless of the elevated pressure of the flash. This provides not only suflicient total amount of aromatics in the stream, but a ratio of about 72 percent saturates by volume to about 26 percent aromatics in the overhead. As will be hereinafter demonstrated, the employment of an excessive amount of aromatics in the desulfurization reaction can be as detrimental to sulfur removal as employing too little aromatics.

The dashed lines of FIG. 4 designate another possible overhead saturates and aromatics distribution in which aromatics begin to predominate in a 550 F. overhead fraction. However, since a 550 F. flash includes all the lighter material, the total overhead will still predominate in saturates over aromatics.

Referring again to FIG. 1, a predetermined amount of liquid is flashed and removed by means of line 92. Depending upon the nature of the feedstock employed and the conditions utilized in the desulfurization reaction, the flashed material in line 92 may contain, for example, between about 5 and about 60 percent by weight of the liquid effluent from the desulfurization reactor 60, preferably between about 10 and about 35 percent by weight. Suitable flash temperatures include, for example, between about 500 and about 800 F., preferably between about 600 and about 700 F. (These temperatures refer to atmospheric pressure and of course will be different at the process pressure.) An especially preferred flash point for the interstage flash is 650 F. The most desirable amount of liquid to be flashed or otherwise separated from the desulfurization eflluent stream may be easily determined experimentally. The flashed material in line 92 is passed to a high pressure flash chamber unit 94 wherein hydrogen, hydrogen sulfide and light hydrocarbon gases are separated from a liquid hydrocarbon fraction. The gases are withdrawn by means of line 96 and are subjected to purification and separation, including various scrubbing operations and the like, in recycle gas recovery unit 97. Substantially all of the hydrogen sulfide that is produced in reactor 60 is recovered by means of line 93. Hydrogen now free from hydrogen sulfide and light hydrocarbon gases is recovered from unit 97 and is passed by means of line 99 to recycle gas compressor 101 and recycled for utilization in the process by means of line 103. The nonflashed liquid fraction is discharged from flash unit 94 by means of line 98.

The bottoms fraction from the flash unit is discharged by means of line 100 and is admixed with makeup hydrogen, which is provided by means of line 102,

valve 105 and line 107. In addition, recycle hydrogen may be added to the make-up hydrogen in line 107 from line 103 by means of line 109, valve 115 and line 113. H desired, make-up hydrogen may be passed from line 103 directly to line 108 by appropriate valving (not shown). The combined stream may be charged to a furnace 106 in order to raise the temperature of this stream if desired. However, furnace 106 is optional, as the stream 104 may be already at the desired desulfurization temperature for introduction by means of line 108 to the second hydrodesulfurization reactor 110.

The temperatures and pressures employed in reactor 110 may be the same as those described for the hydrodesulfurization reactor 60. Likewise, the desulfurization catalyst which is employed in reactor 110 may be identical to that described previously for reactor 60. It is noted at this point that the hydrodesulfurization catalyst is even more active for removal of nickel and vanadium than it is for removal of sulfur. Most of these metals will be removed in the first hydrodesulfurization reactor 60. The heaviest laydown of such metals is at the inlet to reactor 60. The second desulfurization reactor 110 will act as a metals clean-up stage, and the catalyst therein will not collect as much metals as does the catalyst in reactor 60. Hence, the first stage catalyst will remove most of the metals and will become deactivated by metals much faster than the second stage catalyst.

The desulfurized eflluent from reactor 110 is discharged by means of line 114 and is passed to a flash unit 116 for removal of light gases including hydrogen, hydrogen sulfide and light hydrocarbons. This gaseous stream is sent by means of line 118 to high pressure flash unit 94. Meanwhile, a bottoms fraction including the asphaltic product stream of the present invention is passed by means of line 120 to distillation column 122. A sulfur containing stream comprising sour gas and sour water is removed from column 122 by means of line 124. This stream is passed to a gas treatment plant (by a means not shown) to recover sulfur therefrom. A naphtha fraction is withdrawn from the column 122 by means of line 132. This naphtha stream may be employed as a wash liquid for the separation of the light hydrocarbons from the hydrogen in line 96 (by a means not shown). A furnace oil or heavier fraction may be withdrawn through line 133 and be employed in a manner hereinafter described to provide additional aromatics to the second stage desulfurization reactor 110. A product stream 134 is discharged from the distillation column 122. This desulfurized oil stream contains asphaltenes and resins, and is especially useful, without further blending, as a fuel oil, particularly since less than one percent by weight sulfur is contained therein. Thus, this heavy, asphaltic fuel oil contains, for example, between about 0.3 and about 0.5 percent by weight sulfur or less, which is well within the requirements of even the strictest ordinances for sulfur content of heavy fuel oils.

The process of the present invention provides a percent yield of not less than 40 or 50 and up to 80 or 90 percent by Weight of material having a boiling point greater than the initial boiling point (I.B.P.) of the feed to the first desulfurization reactor. Therefore, very little hydrocracking occurs in accordance with the present invention and the hydrogen consumption will be generally in the range of only 150 to 1500 and preferably in the range of 300 to 1000 standard cubic feet per barrel of feed. The feed to the hydrodesulfurization reactor can have an I.B.P. of not less than 375 F., and will preferably have an I.B.P. of at least 620 or 650 F.

Thus, the amount of material obtained from the second hydrodesulfurization zone whose boiling point is lower than 375 F., or 650 P. will not exceed 50 or 60 percent,

generally, or preferably or 20 weight percent. A feed having an I.B.P. greater than 650 F., e.g. vacuum tower bottoms having an I.B.P. in the range of 750 F. to 900 F. or more may be employed in the process of the present invention. In that event, the amount of material obtained from the second hydrodesulfurization zone whose boiling point is below 650 F. will not exceed 10 or 20 weight percent. Accordingly, the process of this invention may be characterized as an essentially non-cracking process."

Likewise, the fuel oil product from each hydrodesulfurization unit has a total asphaltenes plus resins content of at least 10 or 20 and can have 30 or 40 up to percent by weight of that present in the feed to the first hydrodesulfurization unit. The fuel oil product from the second hydrodesulfurization unit has a preferred total content of resins plus asphaltenes of at least 40, 50 or 70 up to percent by weight of that present in the feed to the second hydrodesulfurization zone. This is a further indication that the resins, and particularly the asphaltenes may be desulfurized without their complete destruction, as was previously proposed.

A modification of the process shown in FIG. 1 is illustrated in FIG. 5, which is a simplified schematic diagram.

Referring now to FIG. 5, a reduced crude oil is introduced by means of line 220 to an atmospheric distillation unit 222 wherein a light asphalt-free distillate fraction having a 630650 F. end point (E.P.) is Withdrawn by means of line 224, while a heavy asphalt-containing 630- 650 F.+ fraction containing 4 percent sulfur is discharged by means of line 226 from the distillation column 222. The asphalt-containing bottoms fraction 226 is passed to a vacuum distillation unit 228 wherein additional light oil is discharged by means of line 230 and is admixed with the lighter fraction in line 224 and introduced along with hydrogen from line 233 into a hydrodesulfurization zone 232 by means of the line 234. Zone 232 may be operated with a conventional gas oil desulfurization catalyst at a temperature, for example, in the range of between about 400 and about 800 F., but at a lower hydrogen partial pressure (e.g., below 1000 p.s.i.), than is employed for the desulfurization of an asphaltic oil. The asphalt-free distillate is easily completely desulfurized in the zone 232 and is discharged by means of line 236 and passed to distillation unit 238 from which an overhead fraction containing hydrogen, hydrogen sulfide and light gases is removed by line 240 and processed as previously described to recover hydrogen and light hydrocarbons.

An aromatic-rich, furnace oil and higher fraction is discharged from the distillation unit 238 by means of line 244. Meanwhile, an asphalt-containing oil -is withdrawn from the vacuum distillation unit 228 by means of a line 246. This stream may have, for example, an initial boiling point of about 1000 F. and contain about 5.5 percent by weight sulfur. The stream 246 is passed through a blending zone 250 wherein the asphalt-containing stream is admixed with a controlled portion of the aromatic-rich fraction from the line 244 in order to obtain the desired viscosity and solvency for the asphaltenes and resins contained in the stream. Then hydrogen is added through line 248. The heaviest product from distillation unit 242 can be blended with the product 268, if desired.

Next, the asphaltic fraction containing solubilized resins and asphaltenes is passed by means of line 252 to a first hydrodesulfurization zone 254 and subjected to desulfurization under the conditions previously described in regard to the reactor 60 of FIG. 1. The eflluent from zone 254 has a reduced sulfur content and is passed by means of line 256 to an interstage flash unit 258 wherein hydrogen, hydrogen sulfide, light hydrocarbon gases, and a controlled portion of aromatics and saturates is discharged by means of line 260. As previously discussed, a flash point is selected so as to optimize the amount of aromatic solvent available for solubilizing the asphaltenes and resins in the feed to the second hydrodesulfurization zone. An efiiuent stream 262 is discharged from the flash unit 258 and is admixed with hydrodesulfurization unit 266 wherein the sulfur content of the asphaltic oil is reduced to below one percent by weight. The heavy oil product stream is discharged from the second hydrodesulfurization unit 266, which unit is operated in the manner described for unit 110 in FIG. 1, and is withdrawn by means of the line 268 and treated as previously described for separation of hydrogen sulfide, light gases and the like.

Thus, the system of FIG. provides a parallel mode of operation wherein an initially-separated lighter portion of the crude is desulfurized and is utilized to pro vide the desired viscosity and solvency for desulfurization of the heavy, asphaltic portion of the crude oil.

Another modification of the FIG. 1 process is illustrated in FIG. 6. Referring now to FIG. 6, an asphaltic oil is introduced by means of line 320 to a distillation unit 322 for separation into an aromatic-poor fraction on which is withdrawn from unit 322 by means of line 324 and an aromatic-rich fraction containing 4 percent sulfur. An aromatic-rich asphaltic oil is discharged from unit 322 by means of a line 326. For example, distillation unit 322 may be operated to provide an asphaltic fraction having an initial boiling point of about 650 F.

The asphaltic stream in line 326 is admixed with hydrogen which is introduced by means of line 328 and the combined stream is passed by means of line 330 into a hydrodesulfurization unit 332 which is operated in the manner previously described. The effiuent from zone 332 is withdrawn by means of line 334 and is introduced into a high pressure flash unit 336 where, for example, material boiling below 800 F. is discharged by means of line 338. Accordingly, an asphaltic oil having a boiling point of 800 F.+ is discharged from the flash unit 336 by means of the line 340.

Referring momentarily to FIG. 4, it is seen that at an 800 F. flash point there is a relatively high aromatic to saturate ratio. However, the total aromatic content of the oil at this point may be less than desired. Accordingly, a controlled amount of an aromatic-rich fraction is introduced into the stream in line 340 by means of line 342 in order to provide the resins and asphaltenes with a proper degree of solvency. The combined stream is then admixed with hydrogen, which is introduced by means of line 344 and introduced into hydrodesulfurization reactor 346 where the sulfur level of the asphaltic fuel oil is reduced to below one percent by weight.

The eflluent from zone 346 is removed by means of line 348 and is introduced into distillation unit 350 where an aromatic-rich fraction is separated and recovered by means of line 352. A controlled portion of the material in stream 352 is recycled by means of line 342 for admixture with the asphaltic stream in line 340 as previously described. The light gases are discharged from distillation unit 350 by means of line 354, While a substantially sulfurfree, asphaltic, heavy fuel oil is recovered from line 356. Substantially all of the asphaltenes and resins fed to distillation unit 350 are recovered in line 356 with the asphaltic fuel oil. The recycle stream 342 is devoid of asphaltenes. The asphaltenes are not recycled to the first hydrodesulfurization zone, since they would deactivate the catalyst prematurely. They are not recycled to the second hydrodesulfurization zone, since they have already been desulfurized, and such recycle would serve no useful purpose.

In the foregoing manner depicted in FIG. 6, a light, desulfurized, aromatics-rich solvent for the asphaltic material is obtained from the product stream.

Still another modification of the present invention is shown in FIG. 7, wherein an asphaltic feed stream is introduced by means of a line 420 to a distillation unit 422 to reduce the feed and prepare a hydrodesulfurization feed for passage through line 426. The asphaltic fraction is discharged by means of the line 426 from unit 422 and is admixed with a controlled portion of an aromatic-rich stream which is introduced by means of line 428. The stream in line 428 can be an aromatic-rich fraction boiling within the range of between about 400 and about 1050 F., preferably between about 650 F. and about 900 F. The combined stream is admixed with hydrogen, which is introduced by means of line 430, and a stream having a boiling point of about 650 F.+ and containing about 4 percent by weight sulfur is introduced by means of line 432 into hydrodesulfurization zone 434. This unit may be operated at a temperature of 690790 or 800 F. An eflluent stream having a sulfur content of about one percent by weight sulfur is introduced by means of line 436 into flash unit 438. A light oil and gas fraction containing substantially all of the hydrogen sulfide produced is flashed from the unit 438 and discharged by means of the line 440, which stream may have, for example, a 650 F. E.P.

An asphaltic stream having a boiling point of, for example, 650 F.+ is admixed with hydrogen which is introduced by means of line 442 and introduced by means of line 444 into second hydrodesulfurization zone 446, which may be also operated at about 690 to 790 or 800 F. The effluent from the second desulfurization zone 446 has a sulfur content of less than one percent and is passed by means of line 448 to distillation unit 450. An aromatics-rich, asphaltene-free fraction is withdrawn from unit 450 by means of line 452 and is recycled by means of line 428 for admixture to the asphaltic oil feedstock to the first desulfurization zone 434. Hydrogen sulfide and light gases are withdrawn from the distillation unit 450 by means of line 454, while a low sulfur asphaltic fuel oil is recovered by means of line 456. Excess from stream 452 not recycled can be blended with product in line 456 to reduce the sulfur content of the product.

Thus, the arrangement of FIG. 7 utilized a low sulfur aromatic-rich product stream for solubilizing the asphaltenes and resins in a heavy desulfurization feedstock having a relatively high I.B.P.

A modification of the system of FIG. 7 is shown in FIG. 8.

The process of FIG. 8 is similar to FIG. 7, however, as shown in FIG. 8, the eflluent from flash unit 438 that is withdrawn by means of line 440 is passed to a flash unit which is provided with cooling coils. Hydrogen sulfide and light gases are withdrawn by means of line 443. Theremaining heavier eflluent is withdrawn from the flash unit 441 by means of the line 445 and is passed by means of pump 447 for admixture with stream 444 for introduction into the second stage desulfurization unit 446.

The mode of operation of FIG. 8 permits the employment of a flash temperature for unit 438, which temperature may be the same as that employed in the hydrodesulfurization units 434 and 446. At the same time the lower temperature flash unit 441 which is provided with cooling coils permits the separation of hydrogen sulfide and light gases and the reintroduction of a material having the optimum aromatics content and initial boiling point. l

Thus, for example, if it were determined that the optimum interstage flash temperature corresponded to 650 F. at atmospheric pressure and the desulfurization units 434 and 446 are being operated at about 700 F., the flash unit 438 may also be operated at 700 F. However, the lower temperature flash unit 441 is operated at 650 F. and thus permits the return by means of the 650 F.+ material by means of line 449.

Thus, the modification of FIG. 8 avoids the need for reducing the temperature of the stream in line 436 and the reheating of stream 444.

Referring now to FIG. 9, an asphaltic, sulfur-containing, hydrocarbon oil is introduced by means of line 520 to distillation unit 522 for separation of the feed into light gases, which are withdrawn by means of line 524, and an aromatic-rich fraction, which is discharged by line 526, which is to be employed in a manner hereinafter described. This aromatic-rich fraction may have a 650 F. E.P.

An asphaltic bottoms fraction having an initial boiling respectively, while the resins and asphaltenes have lost point of, for example, about 650 F. is discharged by sulfur to the least extent, viz., 2.37 and 4.95 percent by means of line 528 and is admixed with hydrogen from weight sulfur, respectively. Finally, even after the second line 530 prior to introduction into first desulfurization stage desulfurization, the only significant sulfur remaining zone 532. The desulfurized effluent from zone 532 is inis present in the resins and asphaltenes. troduced by means of line 534 into flash unit 536. As be- In addition, 1t 1s seen from Table I, that the aromatlc fore, the optimum flash point has been previously detercontent of the feed has gone from 55.45 weight percent to mined and a light oil fraction containing saturates and 60.45 Weight percent after the first stage flashing, and finalaromatics is flashed off along with light gases and hydro- 1y up to 61 91 weight percent aromatics in the product. At gen lfid b means f lin 538, the same t1me the weight who of aromatlcs to resins plus Th asphaltic il i passed f th fl h nit 536 nd asphaltenes increases from about 2 to 1 to about 4 to 1. mixed with hydrogen from line 540 and introduced by Thus, Table I clearly illustrates the criticality Of providing means of line 542 to the second stage desulfurization zone Sufficient aromatics in the asphaltic stream in order to 546, I ddi i h h l i feed to h Zone 546 i solubilize the resins and asphaltenes and to deagglomerate admixed with the aromatic-rich stream 526. Thus, the y asphaltene aggregates so as to Permit desulfurization distillation operation unit 522 is conducted under condit Likewise, this table Shows the eiitieaiitY of avoid tions so that the stream 526 has a selected boiling range g an excess of liquid including aromatics, especially and aromatics content which provides maximum sol vation e i j beyond What is required to contribute a 80infor the asphaltenes present in the feed to the second dehlhllng effect, Since Such an excess of low-Sulfur liquid sulfurization zone 546. The effluent from zone 546 is disy t to i p and dilute t e sulfur-containing. charged by means of the line 548 and is passed to 11 mresins, resms and asphaltenes and dlminish their chance lation unit 550 for separation of the asphaltic fuel oil proof Contact With the catalyst It Should be further noted duced therefrom by means of line 552. Light gas stream t t the fnomatie Pontent of the teed t0 the Second Stage 554 and naphtha stream 556 are recovered and treated as 15 rlchet 1n aromatics, 60-45 Weight Percent than is the usuaL feed to the first stage, i.e., 55.45 weight percent. This is The following examples are presented to further illusdue, In P to the age flashing Which retrate h i i moves saturates in much greater proportion relative to EXAMPLE 1 the aromatics present in the flashed, light oil stream. In

each stage, the weight ratio of aromatics to resins plus asphaltenes to accomplish solvation should be at least 1 to 1 and is preferably 1.5 or 2 to 1, and can be 4 or 5 to 1. The aromatics can be present in the feed, can be introduced by recycle or can be produced in situ.

It is further interesting to note that Table I reveals that the saturates, which are flashed 01f, are the most highly desulfurized fraction and therefore have the least need for passage through the second stage of desulfurization.

The following example illustrates the refractory nature of an asphaltic feedstock when it is attempted to remove more than one percent sulfur without employing the process of the present invention.

An asphalt-containing, reduced crude oil containing about 4.09 weight percent sulfur and hydrogen are intro- 30 duced into a hydrodesulfurization zone containing a nickel-cobalt-molybdenum catalyst disposed on a noncracking, alumina support. The hydrodesulfurization operation is conducted at temperatures of about 650-820 F. and a hydrogen partial pressure of 2000 p.s.i.g., and the resulting asphaltic material is flashed at a temperature corresponding to 650 F. at one atmosphere so as to optimize the amount of aromatics and saturates present in the efiiuent. The 650 F.+ asphaltic fraction that is withdrawn from the flashing unit has a sulfur content of about 1.09 weight percent sulfur and is introduced into a second hydrodesulfurization zone where the desulfurization is EXAMPLE 2 also conducted at about 650 F. to 820 F. while employ- A 22 percent reduced Kuwait crude containing an asing the same catalyst that is employed in the first stage. phalt fraction and 5.43 percent by Weight sulfur is sub- A heavy fuel oil is obtained having a sulfur content of jected to desulfurization. The initial boiling point of the 0.58 weight percent sulfur. The distribution of sulfur in crude is 556 and the boiling range extends to 1400 F.+. each of the various fractions of the oil undergoing de- After the sulfur content is reduced to 4.77, the I.B.P. is

sulfurization is set forth in Table I, below: 514 and the boiling range extends to 1400 F.+.

TABLE I Feed to first HDS Feed to second HDS Zone zone Fuel oil product Sulfur in Sulfur in Sulfur in Fraction traction Fraction fraction Fraction fraction (percent (percent (percent (percent (percent (percent by wt.) by wt.) by wt.) by wt.) by wt.) by wt.)

Saturatcs 17. 9s 3. 42 22. 24 0. so 22. 34 0. 49 Aromatics 55.45 5. 04 60. 45 1.12 61.91 0.56 Resins 16.73 5. 59 13.76 2. 31 12. 72 1. 56 Asphaltcnes- 9. 84 6. 99 3. 4. 95 3. O3 3. l3

As seen from Table I, it is apparent that in an asphaltic As desulfurization continues, and the sulfur content is feed containing a total of about 4.09 weight percent sulreduced to 1.41, the I.B.P. is 509 with the boiling range fur, the sulfur content of such feed is relatively evenly extending to 1400" F.+. However, when the sulfur condistributed between the saturates, aromatics, resins and tent is reduced to 0.83, the I.B.P. drops 90 F. to 466 asphaltenes. However, after the feed is passed through the F. with the boiling range extending to l400 F.+.

first desulfurization zone and the 650 F. E.P. fraction is The results of this run are shown in Table H, below:

TABLE II Reduction in sulfur content during Feedstock desulfurization Sulfur, percent by wt 5. 48 4. 77 1. 41 0.80 Boiling range, F 566-1, 400+ 514-1,400+ 509-1,400| 466-1,400+ Desulfun'zation, percent 12. 2 74. 0 85. 3 API 6. 5 8. 7 17. 7 20. 3

removed, i.e., at 1.09 weight percent total sulfur, the satu- The foregoing data shows that the sulfur content of the rates and aromatics have lost sulfur to the greatest extent, feed becomes very refractory at about 74 percent deviz., they are down to 0.80 and 1.12 weight percent sulfur sulfurization. At 12 percent sulfur removal the I.B.P. is

Feedstock Composition change during (percent desulfurization (percent by wt.) by wt.)

Desulmrizatlon, percent 12. 2 74 85 saturates-.. 11 16. 7 26. 1 33. 2 Aromatics 39 41. 2 56. 6 49. 9 Resins 82 25. 7 15. 1 15. 3 Asphaltenes 18 16. 4 2. 2 1. 6

The foregoing data show that as the depth of sulfur removal increases, resins and asphaltenes diminish and are converted to saturates and aromatics.

The following Table IV gives a molecular weight comparison of the aromatics, saturates and residuals during the course of desulfurization.

TABLE IV Feed- Molecular weight change stock during desulfurization Desulfurization, percent 12.2 74 85 saturates, M.W- 430. 400 410 Aromatics, M.W 490. 0 530 400 Total Residuals, M.W 1,080 590. 0 490 420 The data in Table IV show that as the depth of desulfurization increases, the molecular weight of the total residuals decrease, but not significantly below the molecular weight of the initially formed saturates and aromatics. This molecular weight pattern further illustrates that during the breaking of carbon-sulfur bonds in the resins and asphaltenes, hydrocarbon fragments are produced which are about in the same molecular weight range as are the feed saturates and aromatics.

EXAMPLE 3 In order to illustrate the effect of both dilution and concentration of the resins and asphaltenes in the second stage feed upon the second stage desulfurization rate, a 650 F. flash temperature is employed on a feedstock that had been subjected to a single stage of hydrodesulfurization. The asphaltic, flash residue is subjected to a second stage hydrodesulfurization, and it exhibits a desulfurization reaction rate constant of about 85. The desulfurization reaction rate constant is calculated in a conventional manner, i.e.

( Lb. oil lb. oil 1b. sulfur hr.-lb. catalyst This reaction rate constant can also be expressed as 1 1 R-( LHSV where S is pounds of sulfur per pound of oil in the product; S is pounds of sulfur per pound of oil in the feed; and LHSV is volume of oil per hour per volume of catalyst.

For comparative purposes, a desulfurized furnace oil having a boiling point in the range of 400 to 650 F. and containing 0.07 weight percent sulfur is added to the residue of the 650 F. flash operation. The furnace oil is comprised of about one-half saturates and one-half aromatics. Upon passing this asphaltic feed through a second stage desulfurization, the desulfurization reaction rate drops to 75. Thus, excessive dilution of the feed to the second stage actually reduces the desulfurization reaction rate, even though aromatics are being added.

For further comparison, 30 percent by weight of a light portion of the second desulfurization stage feed is removed making the feed equivalent to about the residue of an 800 F. flash. In this instance, the reaction rate for desulfurization in the second stage falls to 40 thereby illustrating the effect of the inadequate solvation for the resins and asphaltenes. It is clearly evident that the amount of saturates plus aromatics which accompanies the resins and asphaltenes into the second stage has a distinct effect upon the second stage reaction rate, and that too much diluent can have a detrimental effect upon desulfurization reaction rate, just as does too little aromatic solvent.

EXAMPLE 4 In order to determine the effect of adequate, as contrasted to excessive solubilization of an asphalt-containing feed, a residual, high-boiling feed having an initial boiling point of about 800 F. is charged to a hydrodesulfurization process, and 76.2 percent by weight desulfurization is accomplished. Next, a second sample of the feed is diluted with 30 volume percent of a lower boiling gas oil which had been previously desulfurized to the extent of to percent by weight. The addition of the gas oil, which comprises a high proportion of aromatics, increases the desulfurization to 80.3 percent by weight.

For comparative purposes, a further sample of the feed is diluted with 40 percent by volume of a gas oil and is subjected to desulfurization as before. In this instance, there is a loss in desulfurization activity and the desulfurization drops to 76.3 percent by weight. The employment of 64 percent by volume of gas oil reduces the degree of desulfurization even lower to 69.4 percent by weight. The results of these tests are illustrated in Table V below:

TABLE V Effect of gas oil dilution Gas Oil, percent by vol 0 30.0 40. 0 64. 0 Desulfurization, percent by wt"..- 76. 2 80. 3 76. 3 69. 4 Vanadium removal, percent by wt 83. 5 78. 6 74. 6 77. 8

EXAMPLE 5 A test is performed utilizing in the first and second stages a one-thirty-second inch nickel-cobalt-molybdenum on alumina catalyst. In the first stage the catalyst exhibits a six month life with a start-of-run temperature of 690 F. and an end-of-run temperature of about 790 F. in hydrodesulfurizing a Kuwait reduced crude from 4 to 1 weight percent sulfur at a LHSV of about 0.8. The catalyst life in the second stage is even longer. The one weight percent sulfur eflluent from the first stage is flashed to remove 650 F. end point material based on atmospheric pressure and is charged to the second stage with hydrogen to reduce the sulfur level to 0.5 weight percent. The second stage start-of-run temperature is 690 F. and the temperature at days is only 763 F. The test can continue until the temperature is 790 F. Therefore, the first and second stages of this invention can operate for 3, 4, 5, 6 or even 7, 8 or 12 months at a LHSV generally ranging between 0.1 and 10 or preferably between 0.3 and 1 7 1.25. The life of the second stage catalyst is longer than the life of the first stage catalyst.

Although the invention has been described in considerable detail with particular reference to certain preferred embodiments thereof, variations and modifications can be effected within the spirit and scope of the invention as described hereinbefore, and as defined in the appended claims.

We claim:

1. A process for the hydrodesulfurization at a hydrogen partial pressure from 1,000 up to 5,000 psi. of a sulfurcontaining heavy feed oil containing high boiling asphaltenes and resins and lower boiling saturates and aromatics to produce a product of reduced sulfur content, said process comprising charging said feed oil downfiow in a first hydrodesulfurization zone in the presence of hydrogen in a reaction zone containing catalyst particles to inch in diameter at a temperature in the range between 680 to 800 F., said temperature being increased within said range to compensate for loss in hydrodesulfurization rate due to catalyst aging, said catalyst comprising both Group VI and Group VIII metal on alumina, operating said first zone at a liquid hourly space velocity between 0.1 and 10, the catalyst and process conditions pro viding at least about 75 percent sulfur removed and in situ production of aromatics in said first zone to increase the aromatics concentration in the oil at least 5 weight percent in said first zone, withdrawing an efiiuent from said first zone containing asphaltenes in the presence of said increased aromatics concentration, flashing said efiluent to separate hydrogen, hydrogen sulfide, light hydrocarbon gases and a low-boiling liquid fraction containing a major amount of saturates and a minor amount of aromatics from a flash residue having a further increase in the concentration of aromatics relative to said efliuent, charging said flash residue to a second hydrodesulfurization zone and continuing hydrodesulfurization of the oil in said second zone.

2. The process of claim 1 wherein the aromatics concentration in the oil increases at least 10 weight percent in said first zone.

3. The process of claim 1 wherein the aromatics concentration in the oil increases at least 25 weight percent in said first zone.

4. The process of claim 1 wherein the aromatics concentration increases 25 to weight percent in said first zone.

5. In the process of claim 1 recovering an eflluent from the second zone of which not more than 20 weight percent has a boiling point lower than 375 F.

6. In the process of claim 1 recovering an eflluent from the second zone of which not more than 10 weight percent has a boiling point lower than 375 F.

7. The process of claim 1 which produces an oil wherein at least weight percent boils above the initial boiling point of the feed oil.

8. The process of claim 1 wherein the catalyst contains nickel, cobalt and molybdenum.

9. The process of claim 1 wherein the catalyst age ex tends to at least five months of operation.

References Cited UNITED STATES PATENTS 3,392,112 7/1968 Bercik et a1. 208216 3,563,886 2/1971 Carlson et a1. 208210 3,481,860 12/1969 Borst, Jr. 208213 3,617,525 11/1971 Moritz et al 208211 2,723,943 11/1955 McAfee 208213 3,483,118 12/ 1969 Gleim et al 208209 3,649,526 3/1972 Pollitzer 208210 3,429,801 2/ 1969 Gleim et a1 208210 3,714,031 1/ 1973 Van der Toorn et a1. 208216 DELBERT E. GANTZ, Primary Examiner G. I. CRASANAKIS, Assistant Examiner

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