Method for = withdrawing particulate solid from a high pressure vessel

Method for withdrawing = particulate=20 solid from a high pressure vessel

United States Patent = 4664782=20

The particulate solid = is=20 maintained in a bed in contact with a liquid within a high pressure = vessel. The=20 particulate solid is supported in the vessel in a cone-like = configuration. A=20 discharge tube is provided communicating with the particulate solid = running from=20 the bottom of the cone externally of said vessel and pressure on the = supported=20 particulate is produced to discharge said particulate out of said vessel = via the=20 discharge tube.

US Patent References:
Process and = device for=20 withdrawing solid particles and introducing a liquid charge at the lower = part of=20 a contact zone
Euzen et al. - April, 1984 - 4444653

Process and = device for=20 withdrawing solid particles and introducing a liquid charge at the lower = portion=20 of a contact zone
Euzen et al. - July, 1983 - 4392943

Moving-bed = reactor with=20 withdrawal of catalyst and effluent through the same = conduit
Youngman -=20 May, 1975 - 3883312

Catalyst transfer = method=20 for moving-bed reactors
Jones - March, 1975 -=20 3873441

N/A
Pegels et al. - July, 1974 - = 3826737

Inventors:

Galiasso, Roberto E. (San Antonio de Los = Altos, VE)=20
Belandria, Jose I. (Merida, VE)
Caprioli, Pasquale L. (Caracas, = VE)=20

Application Number:

06/817404

Publication Date:

05/12/1987

Filing Date:

01/09/1986

Export Citation:

Click for automatic=20 bibliography generation

Assignee:

Intevep, S.A. (Caracas, VE) =

Primary Class:

208/143=20

Other Classes:

208/168, 208/166, 208/171, 208/173 =

International Classes:

B01J3/02; = C10G49/00;=20 C10G35/10; C10B31/02

Field of Search:

208/143, 208/146, 208/152, 208/165, 208/166, = 208/168,=20 208/171, 208/173, 208/107, 422/143, 422/311, 34/57A

View Patent Images:

Download PDF=20 4664782 3Dpdf

=20 PDF = help=20

US Patent References:

2897138	Contacting = solids and=20 gases	July, 1959	Ardern	208/171
RE23942	N/A	February, 1955	Shabaker	208/171

Primary Examiner:

Caldarola, Glenn

Attorney, Agent or Firm:

Bachman & LaPointe

Claims:

What is claimed is:

1. A method for withdrawing particulate = solid maintained=20 in a bed in contact with a liquid within a high presssure vessel during = a=20 hydrogenation reaction which comprises: providing a high pressure vessel = having=20 a bottom and a top with a bed of particulate solid within said vessel in = contact=20 with a liquid, said particulate solid being a hydrogenation catalyst; = supporting=20 the particulate solid in the vessel in a cone-like configuration spaced = from the=20 bottom of the vessel; providing a discharge tube communicating with the=20 particulate running from the cone externally of said vessel; introducing = feed=20 comprising liquid hydrocarbon and hydrogen into the bottom of the vessel = through=20 a first inlet at a first linear velocity; passing the feed upwardly = through the=20 vessel and particulate solid to perform a hydrogenation reaction and = removing=20 liquid and gaseous reactor effluent from the top of the vessel; and = selectively=20 introducing through a secon inlet at a second linear velocity greater = than said=20 first linear velocity additional liquid hydrocarbon feed into said bed = of=20 particulate solid at the cone at a point adjacent said discharge tube so = as to=20 produce pressure on the supported particulate to discharge said = particulate out=20 of said vessel via said discharge tube.

2. A method=20 according to claim 1 including the step of periodically removing at = least a=20 portion of the particulate solid during the course of the reaction.
3. A method according to claim 1 wherein = said feed is=20 passed through baffles beneath said cone to distribute said feed through = said=20 vessel.

4. A method according to claim 1 = including=20 transferring the discharged particulate to a separator to remove solid = from=20 liquid and gas.

5. A method according to = claim 4=20 including providing a differential pressure between said separator and = vessel to=20 assist in removal of the particulate.

Description:

BACKGROUND OF THE INVENTION

The present invention relates to an improved method and apparatus for = discharging particulate solids maintained in contact with fluid within a = high=20 pressure vessel.

The improvements provided in accordance with the present invention = are=20 broadly applicable to the discharge of particulate solids maintained in = contact=20 with fluids, i.e., liquid and/or gases, from vessels in which various = types of=20 reactions, conversions or the like operations are carried out at=20 super-atmospheric pressure. However, the present invention is = particularly=20 useful in the withdrawal of particulate solids as for example catalyst = material=20 from a liquid hydrocarbon treatment zone. For example, the present = invention has=20 particular application in the removal of spent catalyst material from a=20 treatment zone in which a heavy hydrocarbon oil is contacted with = gaseous=20 hydrogen at high temperatures as for example between about 200=C2=B0 and = 850=C2=B0 C. and=20 high pressures as for example between about 1000 and 5000 psig for the = purpose=20 of effecting hydrocracking, hydrodesulfurization or the like = hydrogenation=20 reactions. To effect hydrogenation reactions of this type, it has been = found=20 advantageous to pass the hydrocarbon material and hydrogen upwardly

bed of particulate catalyst material under conditions such that the = catalyst=20 particles are maintained in random motion to become a so-called = "ebullated" bed.=20

It is an object of the present invention to provide an efficient, = expeditious=20 and effective method and apparatus for discharging particulate solid in=20 admixture with fluid from a high pressure vessel.

It is a further object of the present invention to provide a method = and=20 apparatus as aforesaid whereby the fluid may be efficiently and = economically=20 separated from the particulate solid.

It is a still further object of the present invention to provide an = improved=20 process and apparatus as aforesaid for removing particulate solid in = admixture=20 with liquid hydrocarbon and hydrogen from a high pressure hydrogenation = zone.=20

The foregoing and further objects and advantages of the present = invention=20 will appear from a consideration of the following specification.=20

SUMMARY OF THE INVENTION

In accordance with the present invention it has been found that the = foregoing=20 objects and advantages of the present invention may be readily obtained. =

Thus, the method of the present invention relates to particulate = solid=20 maintained in a bed in contact with a liquid within a high pressure = vessel. The=20 method comprises providing a high pressure vessel having a bottom and a = top and=20 containing therein a bed of particulate solid in contact with a liquid,=20 supporting the particulate solid in the vessel in a cone-like = configuration=20 spaced from the bottom of the vessel, providing a discharge tube = communicating=20 with the particulate solid running from the base of the cone externally = of said=20 vessel, and producing pressure on the supported particulate to discharge = said=20 particulate out of the vessel via said discharge tube. The particulate = solid is=20 preferably a hydrogenation catalyst. In the preferred embodiment liquid=20 hydrocarbon and hydrogen feed is introduced into the reaction vessel, = the feed=20 is passed upwardly through the reaction vessel and particulate solid to = perform=20 a hydrogenation reaction, and liquid and gaseous reactor effluent is = removed=20 from the top of the reactor. It is preferred to introduce additional = liquid=20 hydrocarbon feed into the base of the bed at a point adjacent the = discharge tube=20 to produce pressure on the supported particulate and discharge same out = of the=20 vessel via the discharge tube. It is a significant advantage of the = process of=20 the present invention that one can remove at least a portion of the = particulate=20 solid during the course of the hydrogenation reaction. It has been found = that=20 such a procedure gives optimum results.

The apparatus of the present invention is a device for withdrawing=20 particulate solid maintained in a bed in contact with a liquid within a = high=20 pressure vessel. The device comprises a high pressure vessel having a = bottom and=20 a top, a bed of particulate solid within said vessel in contact with a = liquid,=20 means for supporting the bed in the vessel in a cone-like configuration = spaced=20 from the bottom of the vessel, a discharge tube communicating with the=20 particulate solid running from the support means externally of said = vessel, and=20 means for producing pressure on the supported particulate to discharge = said=20 particulate out of said vessel via said discharge tube. As indicated=20 hereinabove, the particulate solid is preferably a hydrogenation = catalyst. Inlet=20 means is preferably provided at the bottom of the vessel for = introduction of=20 feed comprising hydrocarbon and hydrogen material, and outlet means is=20 preferably provided at the top of the vessel for removal of liquid and = gaseous=20 reactor effluent. Distribution baffles are preferably provided at the = bottom of=20 the vessel between the inlet means and the particulate solid to provide = even=20 distribution of the feed throughout the vessel. A second inlet is = preferably=20 provided for the introduction of additional liquid hydrocarbon feed = beneath the=20 bed. Tube means are provided passing from the second inlet to the bed at = a point=20 adjacent to the discharge tube to produce pressure on the supported = particulate=20 to separate the particulate into a free-flowing form and discharge the=20 particulate out of the vessel via the discharge tube.

The foregoing and other features of the present invention will appear = hereinbelow.=20

BRIEF DESCRIPTION OF THE DRAWINGS

The process and apparatus of the present invention will be more = readily=20 understandable from a consideration of the following illustrative = drawings=20 wherein:

FIG. 1 is a partially schematic flow-sheet of the overall process and = apparatus of the present invention;

FIG. 2 is a detailed sectional view of the top of the reactor of FIG. = 1;

FIG. 3 is a detailed sectional view of the bottom of the reactor of = FIG. 1;=20

FIG. 4 is a sectional view of the top of the reactor of FIG. 1 = showing the=20 introduction of particulate material into the reactor;

FIG. 5 is a graph of comparative data showing the rise in temperature = as a=20 function of time on stream;

FIG. 6 is a graph of comparative data showing carbon and vanadium as = a=20 function of length of reactor;

FIGS. 7a, 7b and 7c show vanadium distribution in the catalyst = particle by=20 microprobe x-ray analysis for comparative data;

FIG. 8 is a chart of the process of the present invention showing the = change=20 in demetallization during the time on stream;

FIG. 9 is a chart of the process of the present invention showing = carbon and=20 vanadium as a function of the length of the reactor; and

FIGS. 10a and 10b show vanadium distribution in the catalyst particle = by=20 microprobe x-ray analysis in the process of the present invention.=20

DETAILED DESCRIPTION

The present invention relates to an improved method and apparatus for = removing particulate catalyst from a fixed bed, up-flow type reactor = which=20 operates at a high pressure using dynamic pressure without disturbing = operation=20 of the reactor and without damage to the catalyst.

The catalyst and reactor operates at a high pressure and temperature. = The=20 catalyst is maintained in the reactor as a fixed bed and operates in the = up-flow=20 mode in a hydrogenation reaction with the liquid hydrocarbon and = hydrogen feed=20 passing upwardly through the catalyst bed. In accordance with the = present=20 invention the catalyst is supported in the reactor in the configuration = of a=20 fixed cone and the catalyst is withdrawn from the reactor either = continuously or=20 discontinuously in order to increase the performance of the bed. The = withdrawal=20 of the catalyst is accomplished with the use of a high linear velocity = in the=20 bottom of the cone where the catalyst is supported in order to separate = the=20 catalyst into a free-flowing form. A dynamic pressure is produced which = breaks=20 up the supported catalyst and starts movement of the particulate to a = transfer=20 line out of the reactor to a separator for separating catalyst from = liquid and=20 gaseous products. A controlled differential pressure is preferably = provided=20 between the bottom of the cone and the separator to help the = transportation of=20 the solid in the transfer line with the pressure differential preferably = controlled to assure the minimum linear velocity in the transfer line = and to=20 maintain the catalyst in suspension in the transfer line.

Preferably liquid hydrocarbon feed is introduced at a high linear = velocity at=20 the bottom of the cone to produce the dynamic pressure and separate the = catalyst=20 into a free-flowing form. The excess of liquid pumped into the reactor = for this=20 purpose is discharged with the catalyst via the transfer line to the = separator=20 without changing the conditions in the reactor. The fixed bed is not = fluidized=20 or disrupted because the action of the liquid stream is restricted only = to the=20 bottom of the catalyst supporting cone. During the catalyst withdrawal,=20 therefore, the reactor continues to operate as an up-flow, fixed bed = reactor=20 with the fixed bed moving downwardly to accommodate the area vacated by = catalyst=20 removal.

When the desired amount of catalyst is removed, fresh catalyst is = added from=20 a pressurized vessel with appropriate means, as a valve or using higher = pressure=20 than the reactor itself.

The liquid and gaseous products are separated from the catalyst in = the=20 separator with the liquid and gaseous products leaving the top of the = separator=20 to a secondary high temperature, low pressure separator. Gas is removed = from the=20 top of the secondary separator and liquid from the bottom, both for = recycling.=20 Catalyst material is removed from the bottom of the separator for = recycling.=20

The reactor of the present invention is used for the hydrogenation of = hydrocarbons, as heavy oils or its residuum, such as demetallization of = heavy=20 Tia Juana crude. Preferably a portion of the catalyst is periodically = removed=20 during the operation of the reactor, as for example 10% catalyst removal = each=20 week. The withdrawal operation takes less than one hour and does not = disturb=20 operations.

Any of the conventional hydrogenation catalysts can be used, for = example,=20 cobalt, iron, nickel, tungsten, molybdenum, etc., as well as their = sulfides and=20 oxides alone or together with other suitable catalysts or on supports. = Generally=20 speaking the catalyst particles can be extrudates or spheres or other = irregular=20 shapes and can have an average equivalent diameter between 1/32 and 1/5 = inch,=20 although other sizes or shapes can be readily accommodated.

As indicated hereinabove, the reactor operates at high pressure and = high=20 temperature. The linear liquid velocity used in the particulate bed is = between=20 0.1 and 0.7 cm/sec. The gas (hydrogen) to liquid ratio may be readily = varied as=20 between 300 to 10000 cc/liter. The feedstock could be partially = vaporized in the=20 reactor under the operating conditions; however, in all cases the liquid = content=20 of the feedstock in the reactor must be higher than 10% in order to = maintain=20 proper operation of the particulate bed and also in order to perform = catalyst=20 withdrawal by liquid with minimal differential pressure in the transfer = line.=20 Normally, heavier feedstocks are preferred.

Referring specifically to the drawings, FIG. 1 represents a partially = schematic flow sheet of the overall reaction and apparatus of the = present=20 invention. High pressure vessel or reactor 10 having a top 11 and bottom = 12 is=20 provided with a bed of particulate solid catalyst material 13, see FIGS. = 2=20 through 4 wherein the particulate material is partially shown in the = reactor.=20 The particulate material is supported in reactor 10 in a cone-like = configuration=20 as clearly shown in FIG. 3 by a supporting means 14 which may be a = bubble tray=20 or the like permitting flow of liquids and gases therethrough arranged = in a=20 cone-like configuration disposed at the lower portion of the reactor = spaced from=20 the bottom of the reactor. In the top 11 of the reactor a disengaging = plate 15=20 prevents expansion of the catalyst bed during the process. In addition, = baffles=20 16 are provided at the bottom 12 of the reactor in order to properly = distribute=20 the feedstock throughout the reactor. The reactor itself can be a = conventional=20 hydrogenation reactor as for example a conventional hydrodesulfurization = reactor=20 providing that the length to diameter ratio is preferably higher than 5 = in order=20 to have a large hydrostatic pressure on the bottom cone. The baffles and = the=20 disengaging plate assist in proper catalyst distribution and appropriate = liquid=20 and gas distribution to prevent channeling. This is especially = significant after=20 fresh catalyst is loaded into the reactor since short circuiting could = occur in=20 the reactor. Naturally, it is desired to have proper catalyst and = feedstock=20 distribution throughout the reactor. Thus, as shown the bed of = particulate=20 catalyst fills the reactor from supporting means 14 to or below = disengaging=20 plate 15.

Inlet means 20 are provided in the bottom of the reactor for = introduction of=20 feedstock from feedstock storage means shown schematically as reference = numeral=20 23 via line 24. The feedstock flows upwardly in the reactor contacting = baffles=20 16 for proper distribution throughout the reactor. A discharge tube 21 = is=20 provided communicating with the particulate solid 13 and running from = the=20 support means externally of said vessel. In addition, means 22 are = provided for=20 producing pressure on the supported particles 13 to discharge said = particles out=20 of reactor 10 via discharge tube 21. As shown in FIG. 3 the means 22 is = a second=20 inlet for introducing feedstock beneath the bed adjacent discharge tube = 21. The=20 introduction of additional feedstock via second inlet 22 creates a high = linear=20 velocity at the base of the cone. Normally, the particulate is supported = on the=20 cone. However, the high linear velocity of the feedstock from second = inlet 22=20 creates a dynamic pressure, breaks up the supported particulate and = causes flow=20 of particulate and feedstock out of the reactor via discharge tube 21. =

Thus, in accordance with the operation of the reactor, liquid and gas = feedstock enters reactor 10 from bottom inlet 20, is distributed = throughout the=20 reactor 10 via baffles 16 so as to be progressively distributed under = cone 14=20 which supports the catalyst. Reactor effluent passes out of the top of = the=20 reactor via outlet 23. When it is desired to remove particulate from the = reactor=20 additional liquid feedstock is introduced via second inlet 22 at the = bottom of=20 the cone where the catalyst is supported in a solid mass-like arch. = Normally=20 unconverted liquid feedstock is pumped in through second inlet 22 in = order to=20 provide dynamic pressure on the supported arch of catalyst and break up = the arch=20 and force the catalyst out discharge tube 21 in a flow pattern shown by = the=20 arrows in FIG. 3. When the arch of catalyst is destroyed by the dynamic = pressure=20 of the additional feedstock via second inlet 22, catalyst and liquid is = removed=20 via discharge tube 21. This procedure is operative even when the = catalyst is=20 adhered together by for example vanadium and carbon material in view of = the=20 liquid pressure which breaks up the lumps of catalyst. This procedure = has been=20 found to be particularly effective and represents a significant = advantage over=20 procedures employed heretofore.

Referring to FIG. 1, particulate material 13 removed from reactor 10 = via=20 discharge tube 21 is transported to high temperature separator 30. From=20 separator 30 the particulate material is separated from the slurry and=20 discharged out the bottom of separator 30 via discharge line 31 and a = rotating=20 high pressure, high temperature valve 32 for recycling, reprocessing, or = storage. Liquid and gas are separated from the slurry via line 33 to = second=20 separator 34. Second separator 34 separates gas and discharges same from = the top=20 of the second separator via line 35 and valve 36 for storage or = recycling.=20 Liquid is discharged from the bottom of second separator 34 via line 37 = and high=20 temperature, high pressure pump 38. The bottom of second separator 34 = may be=20 provided with a filter system to avoid passing fines to pump 38. Pump 38 = may=20 transfer liquid to heater 39 and from heater 39 to second inlet 22 for=20 recycling. Alternatively, liquid may be transferred via valve 40 and = line 41 for=20 storage or recycling, or via line 42 to flush discharge line 31.

Microprocessor 50 is provided to control the various functions as = shown by=20 the dashed lines running from the microprocessor. Naturally, if desired = the=20 functions may be manually controlled. Thus, solid level detector or = detectors 51=20 and liquid level detector or detectors 52 may be provided in reactor 10=20 controlled by microprocessor 50 to insure proper solid and liquid levels = in=20 reactor 10. The microprocessor may also control solid level detectors 53 = in=20 separator 30 and valve 32 for discharge of particulate from separator = 30. The=20 microprocessor may also control valve 36 for discharge of gas from = second=20 separator 34. The microprocessor can also control valve 40 for discharge = of=20 liquid from second separator 34.

Catalyst feed is stored in high temperature, low pressure vessel 60 = connected=20 to low pressure, low temperature vessel 61 via line 62 and valve 63. = Vessel 60=20 is connected to reactor 10 via line 64 and valve 65. Solid level = detectors 66=20 are provided in veseel 60 to maintain particulate level in the vessel. = Detectors=20 66 and valves 63 and 65 are controlled by microprocessor 50.

Thus, in accordance with the present invention if it is desired to = remove=20 part or all of the catalyst from vessel 10, one would start to pump = heated=20 liquid via second inlet 22. Naturally, additional feedstock could be = used if=20 desired. The flow rate is gradually increased to break the solid arch of = particulate at the base of the cone, with the actual flow rate depending = on such=20 variables as particle size and shape and conditions in the veseel 10. = When solid=20 removal commences, the liquid flow rate is maintained in second inlet 22 = to=20 complete withdrawal of the desired amount of particulate.

Special attention should be paid to control of differential pressure = between=20 separator 30 and the particulate. Normally, the range of differential = pressure=20 is around 50-100 psig. This differential can be adjusted stage-by-stage = during=20 the particulate withdrawal procedure after particulate withdrawal = commences as=20 indicated by the solid level detector.

If solid is not removed, the flow rate in inlet 22 is increased = gradually=20 until the solid detector or detectors 51 indicates solid removal. = Normally, the=20 maximum velocity is about 5 cm/second. Then the flow rate could be = maintained or=20 decreased to the minimum flow rate for solid transfer. To assist solid = removal,=20 the differential pressure between reactor 10 and separator 30 could be = increased=20 to at or near the maximum value indicated above. Above this value it is = possible=20 that the catalyst could be damaged and some solid carry over to second = separator=20 34 take place.

In the preferred embodiment, during discharge the microprocessor 50 = starts=20 the catalyst introduction into vessel 10 from vessel 60 using solid = detector 51.=20 Alternatively, liquid could be injected into vessel 60 to start particle = flow=20 via pump 70 and line 71 (FIG. 4) in a manner after liquid injection in = vessel=20 10.

When the desired amount of catalyst is discharged and fresh catalyst = added,=20 the microprocessor reduces the flow rate and could wash the discharge = line 31 if=20 necessary to avoid particle sticking in the discharge line.

In order to illustrate the process and apparatus of the present = invention a=20 comparative example (Test I) was run using a reactor as shown in FIG. 1 = using a=20 flat catalyst support and without changing catalyst during the course of = the run=20 compared to a test in accordance with the process and apparatus of the = present=20 invention (Test II). Both Tests I and II were for one (1) month = duration, and=20 Test II replaced 10% of the catalyst each 5 days of operation. Both = tests were=20 up-flow demetallization with a heavy crude feedstock as shown in Table I = with=20 hydrogen. In Test I the reactor temperature was increased progressively = from=20 370=C2=B0 C. (start-up temperature) to 400=C2=B0 C. (end of run = temperature). Test II was=20 run at a constant temperature. The total pressure in Tests I and II was = 1800=20 psig and the LHSV (ratio of volumetric feed rate of fresh feed to the = volume of=20 the reactor) was 0.3.

The level of demetallization in Test I was maintained at 75% and the = quality=20 of the product measured at different times. After one month in operation = the=20 product quality had changed. The results are shown in Table I and = indicate that=20 operating Test I results in quality changes and conversion increases = during the=20 course of the run. Considering that conversion is more remunerative than = quality, it is clear that income is higher at the end of the run where=20 conversion is higher.

FIG. 5 shows a plot of temperature as a function of time on stream = for Test=20 I. FIG. 6 shows the vanadium and carbon loading and FIG. 7 presents the = profile=20 of vanadium in the catalyst for the top, the middle and the bottom of = the=20 reactor.

In accordance with Test I, using constant demetallization level the = rate of=20 metal deposition on the catalyst is constant and metal loading on the = catalyst=20 increases linearly as a function of time. Vanadium on catalyst decreases = with=20 the length of the reactor. The rate of vanadium deposition on the = catalyst is=20 higher in the top of the reactor and lower in the bottom. Looking at the = carbon=20 profile the contrary held, there is a higher carbon content in the = outlet area=20 than the inlet. Vanadium distribution on the particle is inhomogeneous. = More=20 vanadium in the external part of the particle than in the center = according to=20 the microprobe analysis shown in FIG. 7.

Using the present invention (Test II) can be observed in Table I that = higher=20 conversion of residuum, demetallization and desulfurization occurred. At = the=20 same time the initial and final quality of the product is slightly = lower, but=20 the change is negligible compared with Test I. The amount of distillate = formed=20 in Test II is nearly constant which is a large advantage.

FIG. 8 shows the change in demetallization during the time on stream = for Test=20 II, and FIG. 9 shows the carbon and vanadium loading. The carbon and = vanadium=20 profile is completely different from Test I showing that up-flow = behavior=20 produces lower carbon accumulation and flat vanadium distribution along = the bed.=20

Vanadium distribution in the particle is also different showing that = a high=20 amount of vanadium is now accumulated in the center of the particle (see = FIG.=20 10) which teaches that the better behavior of the process and apparatus = of the=20 present invention.=20

TABLE I

______________________________________

PROPERTIES OF THE PRODUCTS TEST I TEST II INI- FI- INI- FI- = PROPERTIES=20 FEED TIAL NAL TIAL NAL

______________________________________

API=C2=B0 5.0 10.2 12.0 13.0 12.0

S % WT 3.4 2.0 = 1.8 1.4=20 1.6

V ppm 700 420 330 290 320

H % WT 9.85 10.1 = 10.3 10.5=20 10.2

C % WT 84.7 82.6 82.3 82.1 82.4

N % WT 0.63 = 0.45 0.41=20 0.40 0.41

CCR % WT 21.3 14.0 13.5 12.1 12.8

ASPH. = % WT=20 14.0 12.5 10.7 9.7 10.6

TEMPERATURE =3D

BOILING = POINT=20

C ₅- 200 -- 4 5 9 6

200-305 -- 9 11 14 = 12=20

350-500 12 23 24 24 23

500=C2=B0 C.+

88 64 = 60 53 59=20

H ₂

CONSUMP./BBL.

FT3/B 1000 = 1000 1000=20 1000

OPERATING

CONDITIONS

P (PSIG) 1800 = 1800 1800=20 1800

T (=C2=B0C.) 370 400 400 400

LHSV 0.3 0.3 0.3 = 0.3=20

H ₂HC LT/LT 1000 1000 1000 1000 =

______________________________________ =

This invention may be embodied in other forms or carried out in other = ways=20 without departing from the spirit or essential characteristics thereof. = The=20 present embodiment is therefore to be considered as in all respects = illustrative=20 and not restrictive, the scope of the invention being indicated by the = appended=20 claims, and all changes which come within the meaning and range of = equivalency=20 are intended to be embraced therein.

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