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US3830728A - Hydrocracking and hydrodesulfurization process - Google Patents

Hydrocracking and hydrodesulfurization process Download PDF

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Publication number
US3830728A
US3830728A US00237955A US23795572A US3830728A US 3830728 A US3830728 A US 3830728A US 00237955 A US00237955 A US 00237955A US 23795572 A US23795572 A US 23795572A US 3830728 A US3830728 A US 3830728A
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hydrocracking
hydrodesulfurization
catalyst
conversion
hydrogen
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W Mounce
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Cities Service Research and Development Co
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Cities Service Research and Development Co
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/85—Chromium, molybdenum or tungsten
    • B01J23/88—Molybdenum
    • B01J23/882—Molybdenum and cobalt
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
    • B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/61—Surface area
    • B01J35/615—100-500 m2/g
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/63—Pore volume
    • B01J35/635—0.5-1.0 ml/g
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/64—Pore diameter
    • B01J35/647—2-50 nm
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/64—Pore diameter
    • B01J35/651—50-500 nm
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/107—Atmospheric residues having a boiling point of at least about 538 °C

Definitions

  • this invention consists of a process for the hydrocracking and hydrodesulfurization of a heavy hydrocarbon oil comprising the steps:
  • a heavy hydrocarbon oil may be hydrocracked to high conversion while achieving a high level of hydrodesulfurization.
  • hydrocracking-hydrodesulfurization process is commonly carried out by subjecting a heavy hydrocarbon oil and hydrogen to elevated temperature and pressure in the presence of a particulate hydrodesulfurization catalyst.
  • the heavy hydrocarbon oils that are contemplated for charge stocks in hydrocrackinghydrodesulfurization processes generally are atmospheric or vacuum distillation tower residual petroleum streams containing at least about 25% by volume of hydrocarbons boiling about 975 F.
  • Such hydrocarbon oils also contain sulfur present in the form of refractory compounds. Removal of as much sulfur as possible from the hydrocracked products of such hydrocarbon oils is desirable since the presence of sulfur in said hydrocracked products yields air polluting oxides of sulfur when said products are burned.
  • cobalt molybdate deposited on alumina is cobalt molybdate deposited on alumina.
  • my invention involves a two step process employing an active cobalt molybdate on alumina hydrodesulfurization catalyst in the first step and a less active cobalt molybdate on alumina hydrodesulfurization catalyst in the second step.
  • I employ as the active hydrodesulfurization catalyst a relatively nonporous, particulate cobalt molybdate deposited on alumina.
  • the less active hydrodesulfurization catalyst I employ a relatively porous, particulate cobalt molybdate reposited on alumina.
  • Both catalysts are particulate, the particle sizes being within the ability of one skilled in the art to determine. Generally, the catalyst particles are about 0.1-0.25 inch long and about 0.03-0.04 inch in diameter. However, particle size is not especially critical.
  • the active hydrodesulfurization catalyst is cobalt molybdate deposited on alumina.
  • the catalyst contains about 3.0-4.0% by weight of C00 and about 13.5- 15.0% by weight of M00
  • the surface area of the catalyst is about 200 M. /g. minimum.
  • the pore volume of the catalyst is about 0.50-0.60 cc./g.
  • the pore size distribution is defined as follows:
  • Pore Size Distribution Pore Volume, cc./g. 40 A. diameter 0.25-0.50 A. diameter (maximum) 0.05
  • the active hydrodesulfurization catalyst has small pores, most being in the range of about 40-125 A. diameter.
  • the less active hydrodesulfurization catalyst is also cobalt molybdate deposited on alumina.
  • the catalyst contains about 35-40% by weight of C00 and about 14.5- 15.5% by weight of M00
  • the surface area of the catalyst is about 250 Mfi/g. minimum.
  • the pore volume of the catalyst is about 0.75-0.85 cc./g.
  • the pore size distribution is defined as follows:
  • Pore Size Distribution Pore Volume, cc./g.
  • the hydrocracking-hydrodesulfurization process of this invention is carried out at a temperature that is within the range of about 750-900 F. and preferably within the range of about 800-850 F.
  • the process is carried out at a pressure that is broadly within the range of about 500-5000 p.s.i.g. and preferably Within the range of about 1500-3000 p.s.i.g.
  • the amount of hydrogen used is broadly within the range of about 2,000-15,000 cubic feet at standard temperature and pressure (STP) per barrel of heavy hydrocarbon undergoing the hydrocracking-hydrodesulfurization process. However, it is preferred that about 3,000-10,000 cubic feet (STP) of hydrogen per barrel of heavy hydrocarbon be used.
  • STP standard temperature and pressure
  • the heavy hydrocarbon oil to be subjected to the hydrocracking-hydrodesulfurization process and a suitable amount of hydrogen are brought into contact with the active hydrodesulfurization catalyst in a first reaction zone and subjected to elevated temperature and pressure within the ranges set forth above until the degree of hydrocracking reaches about 40-50% conversion.
  • the percent conversion is the percent of hydrocarbons boiling above 975 F. that are hydrocracked to hydrocarbons boiling below 975 F.
  • the hydrocracking in the first stage of the process is not allowed to exceed about 50% conversion because, above this level, degradation products present in the reaction mixture cause agglomeration of the active hydrodesulfurization catalyst particles, thereby rendering the catalyst inoperable.
  • the reaction product including unreacted hydrogen, is then conducted from the first reaction zone to a second reaction zone containing the less reactive hydrodesulfurization catalyst, and the reaction mixture is subjected to elevated temperature and pressure within the ranges set forth above until the overall degree of hydrocracking reaches about 70-80% conversion.
  • the less active hydrodesulfurization catalyst is not agglomerated by the degradation products present in the reaction mixture and therefore is operable even when the hydrocracking reaches a high conversion.
  • the heavy hydrocarbon oil is hydrocracked to up to about 50% conversionand a major proportion of the sulfur contained therein is removed in the first stage of the process and, in the second stage of the process, hydrocracking is continued to an overall conversion of up to about 80% while additional sulfur is removed.
  • the overall two stage process of the instant invention therefore permits hydrocracking to high conversion while at the same time a high level of sulfur removal is achieved.
  • Both stages of the instant invention may advantageously be carried out using the so-called ebullated or expanded catalyst bed described in Re. 25,770.
  • a preferred embodiment of my invention may be carried out as follows.
  • a heavy distillation tower residual hydrocarbon oil containing sulfur and greater than 25% by volume of hydrocarbons boiling above 975 F. is mixed with hydrogen in the proportion of about 5000 cubic feet (STP) of hydrogen per barrel of hydrocarbon oil.
  • STP cubic feet
  • the mixture is passed upward through a bed of the catalyst contained in a first closed reactor at such a rate as to cause the catalyst bed to expand, giving a so-called ebullated catalyst bed.
  • the temperature within the reactor is maintained within the range of 800-850 F. and the pressure within the range of 1500-3000 p.s.i.g.
  • the reaction conditions are such as to permit no more than 50% of the hydrocarbons boiling above 975 'F. to be converted to hydrocarbons boiling below 975 F. Simultaneous partial hydrodesulfurization also occurs in the first reactor.
  • the partially hydrocracked and partially hydrodesulfurized hydrocarbon oil and unreacted hydrogen are then removed from the first closed reactor and conducted to a second closed reactor.
  • the hydrocarbon oil-hydrogen mixture is passed upward through a bed of the less active cobalt molybdate on alumina hydrodesulfurization catalyst contained in the second closed reactor at a rate sufiicient to cause the catalyst bed to expand to give an ebullated bed.
  • the temperature within the reactor is maintained Within the range of 800-850 F. and the pressure within the range of 1500-3000 p.s.i.g.
  • the reac tion conditions are such as to permit overall hydrocracking conversion to reach i.e., 80% of the hydrocarbons boiling above 975 F.
  • hydrocarbon oil charge stock that were present in the original residual hydrocarbon oil charge stock are converted to hydrocarbons boiling below 975 F.
  • the hydrocarbon oil simultaneously undergoes further hydrodesulfurization.
  • the final hydrocarbon oil product recovered from the second reactor has undergone overall hydrocracking to 80% conversion in addition to having the sulfur content markedly reduced. There is no appreciable agglomeration of the catalyst in either reactor.
  • a heavy hydrocarbon oil may be hydrocracked to high conversion while at the same time a high level of sulfur removal by hydrodesulfurization is achieved.
  • a highly active hydrodesulfurization catalyst may be successfully employed in a process where hydrocracking to high conversion is achieved.
  • a process for the hydrocracking and hydrodesulfurization of a heavy hydrocarbon oil wherein the oil is a distillation tower residual petroleum oil containing at least about 25% by volume of hydrocarbons boiling above 975 F., comprising the steps:
  • step (a) contacting said heavy hydrocarbon oil and hydrogen at a pressure of from about 500 to about 5,000 p.s.i.g. and a temperature of about 7 50-900 F. with an active particulate cobalt molybdate on alumina hydrodesulfurization catalyst in a first reaction zone until the degree of hydrocracking approaches about 50% conversion, with the oil and hydrogen being passed upward through the catalyst bed at such a rate as to cause the bed to expand and to form an ebullated catalyst bed, and then (b) contacting said partially hydrocracked and partially desulfurized oil and hydrogen, at temperature and pressure similar to that found in step (a) with a less active particulate cobalt molybdate on alumina hydrodesulfurization catalyst in a second reaction zone until the overall degree of hydrocracking reaches up I to about 80% conversion, with the quantity of hydrogen employed ranging from about 2,000 to about 15,000 cubic feet (STP) per barrel of said oil in the hydrocracking-hydrodesulfurization process, wherein the improvement comprises using
  • Pore Size Distribution Pore Vol., cc./g. 40 A. diameter 0.25-0.50 125 A. diameter (maximum) 0.05
  • step (b) having a pore volume within the range of about 0.75-0.85 cc./ g. and the pore size distribution is Pore Size Distribution: Pore Vol., cc./g.
  • steps (a) and (b) are carried out at a temperature within the range of about 800-850 F. and a pressure within the range of about 1500-3000 p.s.i.g.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Materials Engineering (AREA)
  • Combustion & Propulsion (AREA)
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  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

AN IMPROVED PROCESS FOR THE HYDROCRACKING AND HYDRODESULFURIZATION OF HEAVY HYDROCARBON OILS SUCH AS RESIDUAL OILS WHICH IS CHARACTERIZED BY HIGH CONVERSION AND EFFICIENT SULFUR REMOVAL. THE PROCESS INVOLVES A FIRST STEP IN WHICH THE HYDROCARBON OIL AND HYDROGEN ARE REACTED AT ELEVATED TEMPERATURE AND PRESSURE IN THE PRESENCE OF AN ACTIVE PARTICULATE HYDRODESULFURIAZATION CATALYST WHEREIN HYDROCRACKING OCCURS UP TO ABOUT 50% CONVERSION. THE REACTION PRODUCT IS THEREAFTER REACTED IN A SECOND STEP WITH HYDROGEN AT ELEVATED TEMPERATURE AND PRESSURE IN THE PRESENCE OF A LESS ACTIVE PARTICULATE HYDRODESULFURIZATION CATALYST WHEREIN HYDROCRACKING IS CARRIED TO AN OVERALL CONVERSION OF UP TO ABOUT 80% AND SULFUR CONTENT IS REDUCED TO A LOW LEVEL.

Description

United States Patent O 3,830,728 HYDROCRACKING AND HYDRODESULFURIZA- TION PROCESS William Mounce, Cranbury, N.J., assignor to Cities Service Research and Development Company, New York, N.Y. No Drawing. Filed Mar. 24, 1972, Ser. No. 237,955
Int. Cl. C10g 13/02, 37/02 US. Cl. 208-59 Claims ABSTRACT OF THE DISCLOSURE An improved process for the hydrocracking and hydrodesulfurization of heavy hydrocarbon oils such as residual oils which is characterized by high conversion and eflicient sulfur removal. The process involves a first step in which the hydrocarbon oil and hydrogen are reacted at elevated temperature and pressure in the presence of an active particulate hydrodesulfurization catalyst wherein hydrocracking occurs up to about 50% conversion. The reaction product is thereafter reacted in a second step with hydrogen at elevated temperature and pressure in the presence of a less active particulate hydrodesulfurization catalyst wherein hydrocracking is carried to an overall conversion of up to about 80% and sulfur content is reduced to a low level.
BACKGROUND OF THE INVENTION In the catalytic treatment of heavy hydrocarbon oils to affect hydrocracking and hydrodesulfurization, it is I desirable to achieve hydrocracking at high conversion while at the same time achieving as high a degree of sulfur removal as possible. However, solid catalysts having a high level of hydrodesulfurization activity are generally not usable in processes where hydrocracking is carried out at high conversion. For example, degradation products of the heavy hydrocarbon oil formed as a result of the hydrocracking and hydrodesulfurization processes may coat the catalyst particles to thereby render the catalyst inactive. Also, the degradation products may cause agglomeration of the catalyst particles to thereby reduce its surface area as well as to render it inoperable in a so-called ebullated catalyst process such as that described in Re. 25,770.
SUMMARY It is therefore an object of this invention to provide an improved process for the hydrocracking and hydrosulfurization of heavy hydrocarbon oils.
It is another object of this invention to provide a process for hydrocracking heavy hydrocarbon oils to high conversion while achieving a high level of hydrodesulfurization.
Yet other objects and advantages will be apparent to those skilled in the art from the description contained herein.
The foregoing objects are achieved according to the practice of this invention. Broadly, this invention consists of a process for the hydrocracking and hydrodesulfurization of a heavy hydrocarbon oil comprising the steps:
a. Contacting said heavy hydrocarbon oil and hydrogen at elevated temperature and pressure with an active particulate cobalt molybdate on alumina hydrodesulfurization catalyst in a first reaction zone until the degree of hydrocracking reaches up to about 50% conwersion; and
b. Contacting said partially hydrocracked and partially desulfurized oil and hydrogen at elevated temperature 3,830,728 Patented Aug. 20, 1974 and pressure with a less active particulate cobalt molybdate on alumina hydrodesulfurization catalyst in a second reaction zone until the overall degree of hydrocracking reaches up to about conversion.
By the practice of this invention, a heavy hydrocarbon oil may be hydrocracked to high conversion while achieving a high level of hydrodesulfurization.
DETAILED DESCRIPTION When heavy hydrocarbon oils are subjected to a hydrocracking-hydrodesulfurization process, it is desirable to achieve hydrocracking at high conversion while at the same time achieving as high a degree of sulfur removal as possible. A hydrocracking-hydrodesulfurization process is commonly carried out by subjecting a heavy hydrocarbon oil and hydrogen to elevated temperature and pressure in the presence of a particulate hydrodesulfurization catalyst. The heavy hydrocarbon oils that are contemplated for charge stocks in hydrocrackinghydrodesulfurization processes generally are atmospheric or vacuum distillation tower residual petroleum streams containing at least about 25% by volume of hydrocarbons boiling about 975 F. Such hydrocarbon oils also contain sulfur present in the form of refractory compounds. Removal of as much sulfur as possible from the hydrocracked products of such hydrocarbon oils is desirable since the presence of sulfur in said hydrocracked products yields air polluting oxides of sulfur when said products are burned.
Among the more prominent catalysts that may be used for hydrodesulfurization is cobalt molybdate deposited on alumina. As stated above, my invention involves a two step process employing an active cobalt molybdate on alumina hydrodesulfurization catalyst in the first step and a less active cobalt molybdate on alumina hydrodesulfurization catalyst in the second step. I employ as the active hydrodesulfurization catalyst a relatively nonporous, particulate cobalt molybdate deposited on alumina. As the less active hydrodesulfurization catalyst I employ a relatively porous, particulate cobalt molybdate reposited on alumina. I believe that the difference in hydrodesulfurization activity of the two catalysts is due to differences in the average pore sizes, but I do not limit myself thereto. Both catalysts are particulate, the particle sizes being within the ability of one skilled in the art to determine. Generally, the catalyst particles are about 0.1-0.25 inch long and about 0.03-0.04 inch in diameter. However, particle size is not especially critical.
The active hydrodesulfurization catalyst is cobalt molybdate deposited on alumina. The catalyst contains about 3.0-4.0% by weight of C00 and about 13.5- 15.0% by weight of M00 The surface area of the catalyst is about 200 M. /g. minimum. The pore volume of the catalyst is about 0.50-0.60 cc./g. The pore size distribution is defined as follows:
Pore Size Distribution: Pore Volume, cc./g. 40 A. diameter 0.25-0.50 A. diameter (maximum) 0.05
From the above table it is apparent that the active hydrodesulfurization catalyst has small pores, most being in the range of about 40-125 A. diameter.
The less active hydrodesulfurization catalyst is also cobalt molybdate deposited on alumina. The catalyst contains about 35-40% by weight of C00 and about 14.5- 15.5% by weight of M00 The surface area of the catalyst is about 250 Mfi/g. minimum. The pore volume of the catalyst is about 0.75-0.85 cc./g. The pore size distribution is defined as follows:
Pore Size Distribution: Pore Volume, cc./g.
250 A. diameter 0.22-0.31 500 A. diameter 0.18-0.28 1500 A. diameter 0.12-0.24 4000 A. diameter 0.06-0.16
It is apparent from the foregoing table that the less active hydrodesulfurization catalyst has greater pore volume and larger average pore diameter than does the active hydrodesulfurization catalyst.
The hydrocracking-hydrodesulfurization process of this invention is carried out at a temperature that is within the range of about 750-900 F. and preferably within the range of about 800-850 F. The process is carried out at a pressure that is broadly within the range of about 500-5000 p.s.i.g. and preferably Within the range of about 1500-3000 p.s.i.g. The amount of hydrogen used is broadly within the range of about 2,000-15,000 cubic feet at standard temperature and pressure (STP) per barrel of heavy hydrocarbon undergoing the hydrocracking-hydrodesulfurization process. However, it is preferred that about 3,000-10,000 cubic feet (STP) of hydrogen per barrel of heavy hydrocarbon be used. The foregoing temperature and pressure parameters apply to both the first and the second stages of the hydrocracking-hydrodesulfurization process.
In the practice of my invention, the heavy hydrocarbon oil to be subjected to the hydrocracking-hydrodesulfurization process and a suitable amount of hydrogen are brought into contact with the active hydrodesulfurization catalyst in a first reaction zone and subjected to elevated temperature and pressure within the ranges set forth above until the degree of hydrocracking reaches about 40-50% conversion. By definition, the percent conversion is the percent of hydrocarbons boiling above 975 F. that are hydrocracked to hydrocarbons boiling below 975 F. The hydrocracking in the first stage of the process is not allowed to exceed about 50% conversion because, above this level, degradation products present in the reaction mixture cause agglomeration of the active hydrodesulfurization catalyst particles, thereby rendering the catalyst inoperable.
The reaction product, including unreacted hydrogen, is then conducted from the first reaction zone to a second reaction zone containing the less reactive hydrodesulfurization catalyst, and the reaction mixture is subjected to elevated temperature and pressure within the ranges set forth above until the overall degree of hydrocracking reaches about 70-80% conversion. The less active hydrodesulfurization catalyst is not agglomerated by the degradation products present in the reaction mixture and therefore is operable even when the hydrocracking reaches a high conversion.
Thus, by the practice of my invention the heavy hydrocarbon oil is hydrocracked to up to about 50% conversionand a major proportion of the sulfur contained therein is removed in the first stage of the process and, in the second stage of the process, hydrocracking is continued to an overall conversion of up to about 80% while additional sulfur is removed. The overall two stage process of the instant invention therefore permits hydrocracking to high conversion while at the same time a high level of sulfur removal is achieved. Both stages of the instant invention may advantageously be carried out using the so-called ebullated or expanded catalyst bed described in Re. 25,770.
A preferred embodiment of my invention may be carried out as follows. A heavy distillation tower residual hydrocarbon oil containing sulfur and greater than 25% by volume of hydrocarbons boiling above 975 F. is mixed with hydrogen in the proportion of about 5000 cubic feet (STP) of hydrogen per barrel of hydrocarbon oil. The mixture is passed upward through a bed of the catalyst contained in a first closed reactor at such a rate as to cause the catalyst bed to expand, giving a so-called ebullated catalyst bed. The temperature within the reactor is maintained within the range of 800-850 F. and the pressure within the range of 1500-3000 p.s.i.g. The reaction conditions are such as to permit no more than 50% of the hydrocarbons boiling above 975 'F. to be converted to hydrocarbons boiling below 975 F. Simultaneous partial hydrodesulfurization also occurs in the first reactor.
The partially hydrocracked and partially hydrodesulfurized hydrocarbon oil and unreacted hydrogen are then removed from the first closed reactor and conducted to a second closed reactor. The hydrocarbon oil-hydrogen mixture is passed upward through a bed of the less active cobalt molybdate on alumina hydrodesulfurization catalyst contained in the second closed reactor at a rate sufiicient to cause the catalyst bed to expand to give an ebullated bed. The temperature within the reactor is maintained Within the range of 800-850 F. and the pressure within the range of 1500-3000 p.s.i.g. The reac tion conditions are such as to permit overall hydrocracking conversion to reach i.e., 80% of the hydrocarbons boiling above 975 F. that were present in the original residual hydrocarbon oil charge stock are converted to hydrocarbons boiling below 975 F. The hydrocarbon oil simultaneously undergoes further hydrodesulfurization. The final hydrocarbon oil product recovered from the second reactor has undergone overall hydrocracking to 80% conversion in addition to having the sulfur content markedly reduced. There is no appreciable agglomeration of the catalyst in either reactor.
Thus, by the practice of my invention a heavy hydrocarbon oil may be hydrocracked to high conversion while at the same time a high level of sulfur removal by hydrodesulfurization is achieved. In the practice of this invention, a highly active hydrodesulfurization catalyst may be successfully employed in a process where hydrocracking to high conversion is achieved.
While this invention has been illustrated by the presentation of a specific example, it will be understood that the scope of the invention is limited only by the appended claims.
I claim:
1. A process for the hydrocracking and hydrodesulfurization of a heavy hydrocarbon oil, wherein the oil is a distillation tower residual petroleum oil containing at least about 25% by volume of hydrocarbons boiling above 975 F., comprising the steps:
(a) contacting said heavy hydrocarbon oil and hydrogen at a pressure of from about 500 to about 5,000 p.s.i.g. and a temperature of about 7 50-900 F. with an active particulate cobalt molybdate on alumina hydrodesulfurization catalyst in a first reaction zone until the degree of hydrocracking approaches about 50% conversion, with the oil and hydrogen being passed upward through the catalyst bed at such a rate as to cause the bed to expand and to form an ebullated catalyst bed, and then (b) contacting said partially hydrocracked and partially desulfurized oil and hydrogen, at temperature and pressure similar to that found in step (a) with a less active particulate cobalt molybdate on alumina hydrodesulfurization catalyst in a second reaction zone until the overall degree of hydrocracking reaches up I to about 80% conversion, with the quantity of hydrogen employed ranging from about 2,000 to about 15,000 cubic feet (STP) per barrel of said oil in the hydrocracking-hydrodesulfurization process, wherein the improvement comprises using a catalyst in step (a) having a pore volume within the range of about 0.50-0.60 cc./g. and
the pore size distribution is Pore Size Distribution: Pore Vol., cc./g. 40 A. diameter 0.25-0.50 125 A. diameter (maximum) 0.05
and using a catalyst in step (b) having a pore volume within the range of about 0.75-0.85 cc./ g. and the pore size distribution is Pore Size Distribution: Pore Vol., cc./g.
250 A. diameter 0.22-0.31 500 A. diameter 0.18-0.28 1500 A. diameter 0.12-0.24 4000 A. diameter 0.06-0.16
2. The process of Claim 1 wherein steps (a) and (b) are carried out at a temperature within the range of about 800-850 F. and a pressure within the range of about 1500-3000 p.s.i.g.
3. The process of Claim 1 wherein the quantity of hydrogen employed is within the range of about 3,000- 10,000 cubic feet (STP) per barrel of said hydrocarbon oil.
4. The process of Claim 1 wherein the active hydrodesulfurization catalyst of (a) contains about 3.04.0% by weight of C00 and about 13.5-15.0% by weight of M00 and the less active hydrodesulfurization catalyst of (b) contains about 3.5-4.0% by weight of C00 and about 14.5-15.5% by weight of M00 6 S. The process of Claim 4 wherein the surface area of the active hydrodesulfurization catalyst of (a) is at least about 200 M. /g. and the surface area of the less active hydrodesulfurization catalyst of (b) is at least about 250 MF/g.
References Cited UNITED STATES PATENTS DELBERT E. GANTZ, Primary Examiner G. E. SCHMITKONS, Assistant Examiner US. Cl. X.R.
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US3905893A (en) * 1973-08-22 1975-09-16 Gulf Research Development Co Plural stage residue hydrodesulfurization process
US3907667A (en) * 1973-08-22 1975-09-23 Gulf Research Development Co Process for producing a lubricating oil from a residue feed
US3926784A (en) * 1973-08-22 1975-12-16 Gulf Research Development Co Plural stage residue hydrodesulfurization process with hydrogen sulfide addition and removal
US3936370A (en) * 1973-08-22 1976-02-03 Gulf Research & Development Company Process for producing a zeolite riser cracker feed from a residual oil
US3998722A (en) * 1975-12-31 1976-12-21 Mayer Francis X High temperature hydroconversion without incompatibles formation
US4073718A (en) * 1976-05-12 1978-02-14 Exxon Research & Engineering Co. Process for the hydroconversion and hydrodesulfurization of heavy feeds and residua
EP0021495A1 (en) * 1979-06-21 1981-01-07 Shell Internationale Researchmaatschappij B.V. Process for the catalytic hydrodesulphurization of a residual fraction of a hydrocarbon oil
US4451354A (en) * 1983-01-03 1984-05-29 Exxon Research And Engineering Co. Process for upgrading hydrocarbonaceous oils
US4456700A (en) * 1976-08-13 1984-06-26 Mobil Oil Corporation Catalyst for residua demetalation and desulfurization
US4657664A (en) * 1985-12-20 1987-04-14 Amoco Corporation Process for demetallation and desulfurization of heavy hydrocarbons
US4744888A (en) * 1986-10-06 1988-05-17 Chevron Research Company Process for the removal of sodium from a hydrocarbon feedstock employing a catalyst system
US6274029B1 (en) 1995-10-17 2001-08-14 Exxon Research And Engineering Company Synthetic diesel fuel and process for its production
US6309432B1 (en) 1997-02-07 2001-10-30 Exxon Research And Engineering Company Synthetic jet fuel and process for its production
US6822131B1 (en) 1995-10-17 2004-11-23 Exxonmobil Reasearch And Engineering Company Synthetic diesel fuel and process for its production

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JPS6147935U (en) * 1984-08-29 1986-03-31 勇 加藤 Filter for coffee, tea, etc.

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3905893A (en) * 1973-08-22 1975-09-16 Gulf Research Development Co Plural stage residue hydrodesulfurization process
US3907667A (en) * 1973-08-22 1975-09-23 Gulf Research Development Co Process for producing a lubricating oil from a residue feed
US3926784A (en) * 1973-08-22 1975-12-16 Gulf Research Development Co Plural stage residue hydrodesulfurization process with hydrogen sulfide addition and removal
US3936370A (en) * 1973-08-22 1976-02-03 Gulf Research & Development Company Process for producing a zeolite riser cracker feed from a residual oil
US3998722A (en) * 1975-12-31 1976-12-21 Mayer Francis X High temperature hydroconversion without incompatibles formation
US4073718A (en) * 1976-05-12 1978-02-14 Exxon Research & Engineering Co. Process for the hydroconversion and hydrodesulfurization of heavy feeds and residua
US4456700A (en) * 1976-08-13 1984-06-26 Mobil Oil Corporation Catalyst for residua demetalation and desulfurization
EP0021495A1 (en) * 1979-06-21 1981-01-07 Shell Internationale Researchmaatschappij B.V. Process for the catalytic hydrodesulphurization of a residual fraction of a hydrocarbon oil
US4451354A (en) * 1983-01-03 1984-05-29 Exxon Research And Engineering Co. Process for upgrading hydrocarbonaceous oils
US4657664A (en) * 1985-12-20 1987-04-14 Amoco Corporation Process for demetallation and desulfurization of heavy hydrocarbons
US4744888A (en) * 1986-10-06 1988-05-17 Chevron Research Company Process for the removal of sodium from a hydrocarbon feedstock employing a catalyst system
US6274029B1 (en) 1995-10-17 2001-08-14 Exxon Research And Engineering Company Synthetic diesel fuel and process for its production
US6296757B1 (en) 1995-10-17 2001-10-02 Exxon Research And Engineering Company Synthetic diesel fuel and process for its production
US6607568B2 (en) 1995-10-17 2003-08-19 Exxonmobil Research And Engineering Company Synthetic diesel fuel and process for its production (law3 1 1)
US6822131B1 (en) 1995-10-17 2004-11-23 Exxonmobil Reasearch And Engineering Company Synthetic diesel fuel and process for its production
US6309432B1 (en) 1997-02-07 2001-10-30 Exxon Research And Engineering Company Synthetic jet fuel and process for its production
US6669743B2 (en) 1997-02-07 2003-12-30 Exxonmobil Research And Engineering Company Synthetic jet fuel and process for its production (law724)

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