GB2142551A - Catalyst for use in the fluid catalytic cracking of sulphur-containing hydrocarbons - Google Patents

Catalyst for use in the fluid catalytic cracking of sulphur-containing hydrocarbons Download PDF

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Publication number
GB2142551A
GB2142551A GB08417699A GB8417699A GB2142551A GB 2142551 A GB2142551 A GB 2142551A GB 08417699 A GB08417699 A GB 08417699A GB 8417699 A GB8417699 A GB 8417699A GB 2142551 A GB2142551 A GB 2142551A
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Prior art keywords
composition
sulfur
promoter
catalyst
palladium
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GB08417699A
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GB2142551B (en
GB8417699D0 (en
Inventor
Alan W Klaassen
Richard D Bezman
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Chevron USA Inc
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Chevron Research and Technology Co
Chevron Research Co
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Publication of GB8417699D0 publication Critical patent/GB8417699D0/en
Publication of GB2142551A publication Critical patent/GB2142551A/en
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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00Catalysts comprising molecular sieves
    • B01J29/04Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/70Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86Catalytic processes
    • B01D53/8603Removing sulfur compounds
    • B01D53/8609Sulfur oxides
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/40Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
    • B01J23/44Palladium
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/40Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
    • B01J23/46Ruthenium, rhodium, osmium or iridium
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/54Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/56Platinum group metals
    • B01J23/64Platinum group metals with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/656Manganese, technetium or rhenium
    • B01J23/6567Rhenium
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00Catalysts comprising molecular sieves
    • B01J29/04Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/70Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
    • B01J29/72Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65 containing iron group metals, noble metals or copper
    • B01J29/74Noble metals
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING 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
    • C10G11/00Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/02Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
    • C10G11/04Oxides
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING 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
    • C10G11/00Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique

Abstract

In a fluid catalytic cracking process for cracking a sulfur-containing hydrocarbon in which the amount of sulfur oxides present in the combustion gases formed in the catalyst regeneration zone is controlled by including a sulfur sorbent such as alumina in the cycled particulate solids, there is employed an improved oxidation promoter for converting SO2 present in the combustion gases to SO3 comprising an intimate association of palladium or a compound thereof and at least one other metal or compound thereof selected from platinum, osmium, iridium, rhenium and rhodium.

Description

1 GB 2 142 551 A 1
SPECIFICATION
Catalyst for use in the fluid catalytic cracking of sulphur-containing hydrocarbons This invention relates to a catalyst for use in a f 1 uid catalytic cracking (FCC) process.
Fluid catalytic cracking involves the catalytic breakdown of heavy hydrocarbons to lighter fuels and petrochemical stocks. A typical catalytic cracking (FCC) unit has a hydrocarbon cracking zone and a catalyst regeneration zone. A particulate catalyst, generally containing a zeolite, is cycled between the cracking zone where the hydrocarbon feedstock is cracked and a regeneration zone where the coke formed on the catalyst in the cracking zone is burned off. The combustion gases formed in the regeneration zone will usually contain some noxious gases which are considered air pollutants. For example, carbon monoxide is generally formed during oxidation of the coke (see U.S. Patent No. 3,909,392). In addition, when the hydrocarbon feedstocks contain sulfur and/or nitrogen, the combustion gases will usually contain the oxides of these elements in various amounts.
The carbon monoxide present in the combustion gas may be controlled by adding small amounts of a carbon monoxide oxidation promoter, such as platinum (see U.S. Patent No. 4,072,600). The suifur oxides may be controlled by including a sulfur sorbent, such as alumina, in the circulating inventory, i.e. in admixture with the cracking catalyst (see U.S. Patent No. 4,071,436). It has also been found that inclusion of a sulfur dioxide oxidation promoter enhances the removal of the sulfur from the combustion gas by the sulfur sorbent (see U.S. Patent No. 4,115,250). Hitherto, one of the most effective sulfur dioxide oxidation promoters has been platinum. Although effective, this promoter has the disadvantage of increasing the amount of the oxides of nitrogen present in the flue gas. As noted above, platinum can also serve as a carbon monoxide oxidation promoter. It would be desirable to use an oxidation promoter in the regeneration process which retains the effectiveness of platinum in promoting the oxidation of carbon monoxide and sulfur dioxide without contributing to the formation of nitrogen oxides.
It has been found that certain mixtures of metals containing palladium and at least one other metal selected from the group consisting of platinum, osmium, iridium, rhodium, and rhenium can serve as an effective carbon monoxide and sulfur dioxide oxidation promoter while minimizing the formation of the oxides of nitrogen. Even more surprising is the discovery that the effectiveness of these mixtures in promoting the oxidation of sulfur dioxide is usually greater than the effectiveness of the individual metals 30 used in forming the mixture. Just as remarkable is the discovery that this increase in the ability to promote the oxidation of sulfur dioxide is usually accompanied by significant decreases in the amount of the oxides of nitrogen formed as compared with platinum alone.
Thus in accordance with the present invention, there is provided a catalyst composition for use in the fluid catalytic cracking of a sulfur-containing hydrocarbon, which comprises:
(a) a particulate cracking catalyst for cracking sulfur-containing hydrocarbons in the absence of hydrogen; (b) a sulfur sorbent capable of sorbing sulfur trioxide formed during the catalytic cracking process; and (c) a sulfur dioxide oxidation promoter comprising a particulate solid containing an inorganic oxide support having associated therewith a promoter mixture comprising palladium or a compound of palladium and at least one other metal or a compound thereof selected from platinum, osmium, iridium, rhenium and 40 rhodium.
An FCC process in which the catalyst composition of the invention is employed is described and claimed in our copending Application No. 8223991 (Serial No. 2104406).
In one embodiment of the invention, the sulfur sorbent is in the form of a particulate solid which is in physical admixture with the particulate cracking catalyst and the particu(ate oxidation promoter.
In another embodiment, the sulfur sorbent is present on the particu(ate cracking catalyst, for instance an aluminum compound capable of sorbing sulfur oxides can be impregnated into a silica-containing cracking catalyst.
The phrase "circulating inventory" refers to the particulate solids which are cycled between the cracking zone and regeneration zone. Thus, the phrase includes, but is not necessarily limited to, the cracking catalyst, 50 the particulate sulfur sorbent, and the promoter particles.
As used herein, the phrase---sulfur sorbent" refers to a material capable of forming a stable association with sulfur trioxide in the regenerator of an FCC unit and capable of dissociation in the hydrocarbon cracking zone. This association may be formed by absorption, adsorption, or by chemical reaction. Such sulfur sorbents include alumina and magnesia. Particularly preferred as a suffur sorbent is "reactive alumina" 55 which may be described as alumina having a surface area of at least 50m2/g, e.g., gamma- or eta-alumina.
Suitable reactive alumina is not in intimate combination with more than about 40% silica, and preferably is substantially free from admixture with silica. A full description of reactive alumina may be found in U.S.
Patent No. 4,071,436.
The present invention is directed to an improved class of oxidation promoters which are highly effective in 60 converting sulfur dioxide to sulfur trioxide. In most cases, the oxidation promoter also may serve as an oxidation promoter for the conversion of carbon monoxide to carbon dioxide. This class of promoters is particularly advantageous because the promoters described herein may be made selective for the promotion of sulfur dioxide to sulfur trioxide while minimizing the formation of the oxides of nitrogen. The relative ratio of palladium to the other metals will vary depending on the metals used and the selected mode of 2 GB 2 142 551 A 2 operation. In general, when only one other metal is present in association with the pal ladiu m, the relative weight ratios of the two metals will be in the range of from about 100:1 and 1:100, with weight ratios in the range off rom about 10:1 and 1:10 being preferred. Particularly preferred for promoting the oxidation of sulfur dioxide are promoters containing palladium and iridium (10:1); and palladium and platinum (10:1). It is important that the metals be placed on the support as a mixture of metals. It has been found that when the different metals are placed on separate particles from one another, the ability of the metals to promote sulfur dioxide oxidation is significantly reduced.
The support used in association with the promoter may be any inorganic oxide which does not adversely affect the activity of the promoter orthe operation of the FCC unit. Preferably, the support is a particulate solid which may be physically admixed and circulated with the cracking catalyst and sulfur sorbent. Such 10 materials include porous inorganic oxides, such as alumina and silica, or mixtures of two or more inorganic oxides, such as silica-alumina, natural and synthetic clays and the like, crystalline aluminosilicate zeolites, etc. A preferred support is a porous cracking catalyst which shows good attrition-resistance in the FCC unit to prevent loss of the promoter from the system. The catalyst base HEZ-55 supplied by Engelhard is suitable for use as a support for the promoter.
The metals may be added to the support in any suitable manner, as by impregnation or ion exchange, or can be added to a precursor of a preselected solid support, as by coprecipitation from an aqueous solution with an inorganic precursor. In the case of a particulate promotersupport, the particulate solid can be formed into particles of a size suitable for use in an FCC system by conventional means, such as spray-drying, crushing of larger particles to the desired size, etc.
When incorporating the promoter into the circulating inventory of the FCC unit, sufficient promoter should be present to promote the oxidation of sulfur dioxide to sulfur trioxide. In addition, if it is desired that the oxidation promoter also serve as a promoter for the conversion of carbon monoxide to carbon dioxide, sufficient promoter should be present to aid this reaction. Generally, the amount of promoter required to oxidize the carbon monoxide is less than that required to oxidize the sulfur dioxide, so this is not normally a 25 consideration. In general, the total metal content of the promoter will constitute from about 0.01 to about 2% byweight of the promoter-support association and from about 0.01 to about 100 parts per million by weight of the total circulating inventory.
The sulfur sorbent included in the circulating inventory is preferably reactive alumina. However, other sulfur sorbents have been described and could be used with the present invention. In general, a suitable sulfur sorbent should be capable of sorbing at least about 50 weight percent of the sulfur oxides present in the regeneration zone. In the case of reactive alumina, the particles of sulfur sorbent will usually contain at least 60% by weight of alumina. The alumina will have a surface area of at least 50 square meters per gram and contain from about 0.1 to 100% by weight reactive alumina. The sulfur sorbent will usually be in sufficient amount with the catalystto provide from about 0.1 to about 25% by weight of alumina with respect 35 to the total circulating inventory. Generally, the sulfur sorbent is included as a particulate solid physically admixed with the catalyst particles and the promoter particles. However, the sulfur sorbent may also be present on the catalyst particles as described in U.S. Patent No. 4,115, 249.
The catalyst employed in cracking the hydrocarbon feedstock may be any catalyst suitable for use in an FCC system. Such catalysts normally contain silica andlor alumina. Other refractory metal oxides, such as 40 magnesia and zirconia, have been suggested and could be employed if desired. Various types of naturally occurring and synthetic aluminosilicate molecular sieves are usually incorporated into the cracking catalyst.
The choice of catalyst is not critical to the invention. It is anticipated that the selection of catalystwill depend on the feedstock to be cracked and the mode of operation rather than on the oxidation promoter selected.
Thus, catalyst selection is well within the knowledge of one skilled in the art and should require no further explanation here.
Various othertypes of materials may be included in the circulating inventory of the FCC unit provided they do not interfere substantially with the activity of the metal promoters. Additional carbon monoxide oxidation promoters can be added such as copper or chromium. Sodium has also been employed in association with alumina in the sulfur sorbent. Moderate amounts of such materials are not detrimental to the operation of 50 the invention.
In controlling the formation of nitrogen oxides, oxidation promoters containing a mixture of palladium and iridium (10: 1) and of palladium and rhodium (10: 1) are especially desirable. Particularly preferred is the mixture of palladium and iridium (10:1) which has also demonstrated excellent promotion of sulfur dioxide to sulfur trioxide.
In orderto further clarify the invention described herein, attention is directed to the Table. Various oxidation promoters were placed on equilibrium catalyst HEZ-55 by impregnation, and the ability of the individual metals to oxidize sulfur dioxide to sulfur trioxide was determined indirectly by measuring the rate of sulfur trioxide adsorption onto alumina. The Table shows the activity of three selected metal catalysts when employed alone.
3 GB 2 142 551 A 3 TABLE
Metalpromoter 0.1% platinum 0.1% palladium 0.1% iridium Rate of SO3Adsorotion (ppmlmin) 599 497 318 From thetable, it should be noted that platinum is byfarthe best oxidation promoter of thethree metals. Iridium showsvery low abilityto promote oxidation.
Reference will now be made to the accompanying drawings, in which:
Figure 1 compares the ability of various metals and combinations of metals to promote the oxidation of 15 sulfur dioxide and the formation of the oxides of nitrogen; and Figure 2 demonstrates in graphic form the synergistic effect of various mixtures of palladium/platinum on the oxidation of sulfur dioxide.
As already noted, the ability of metal mixtures as described herein to promote the oxidation of sulfur dioxide selectively while minimizing the formation of the oxides of nitrogen offers a distinct advantage over 20 oxidation promoters described in the prior art. This is clearly illustrated by referring to Figure 1 which illustrates the activity of the individual metals shown in the Table and various mixtures of metals failing within the scope of the invention. Figure 1 shows that all of the mixtures of metals tested had improved activity as sulfur dioxide promoters as compared to the individual metals used to prepare the mixture. At the same time, it is also shown that the metal mixtures significantly reduced the amount of nitrogen oxides formed as compared to platinum when used alone. All data collected used 0. 1 % total metal by weight on the support.
Particularly active as sulfur dioxide oxidation promoters are mixtures of palladium with iridium (10: 1) and of palladium with platinum (10: 1).
Referring now to Figure 2, the effect of various ratios of palladium to platinum on sulfur dioxide oxidation 30 promotion are compared. It will be seen from the Figure that the various mixtures of platinum and palladium show a true synergistic effect, i.e., the mixture shows greater oxidation promotion than either of the metals used alone. Although the greatest oxidation promotion is achieved at about a 1: 1 ratio of palladium to platinum, it is usually desirable from an economic standpoint to operate with less platinum in the mixture than the optimum. This is due to the high cost of platinum as compared to palladium.

Claims (11)

1. A catalyst composition for use in the fluid catalytic cracking of a sulfur-containing hydrocarbon, which comprises:
(a)a particulate cracking catalyst for cracking sulfur-containing hydrocarbons in the absence of hydrogen; (b) a sulfur sorbent capable of sorbing sulfurtrioxide formed during the catalytic cracking process; and (c) sulfur dioxide oxidation promoter comprising a particulate solid containing an inorganic oxide support having associated therewith a promoter mixture comprising palladium or a compound of palladium and at least one other metal or a compound thereof selected from platinum, osmium, iridium, rhenium and 45 rhodium.
2. A composition as claimed in Claim 1, wherein the sulfur sorbent is in the form of a pa rticu late solid in physical admixture with the particulate cracking catalyst and the particulate oxidation promoter.
3. A composition as claimed in Claim 1, wherein the sulfursorbent is present on the particulate cracking catalyst.
4. A composition as claimed in Claim 2, wherein the particulate sulfur sorbent solid contains from 0,1 to 100% by weight of reactive alumina.
5. A composition as claimed in Claim 1, 2,3 or4, wherein the oxidation promoter has a total metal content in the range from 0.01 to 2% by weight and constitutes from 0.1 to 100 parts per million by weight of the catalyst composition.
6. A composition as claimed in Claim 5, wherein the promoter mixture contains palladium and platinum.
7. A composition as claimed in Claim 5, wherein the promoter mixture contains palladium and iridium
8. A composition as claimed in Claim 5, wherein the promoter mixture c ontains palladium and rhodium.
9. A composition as claimed in Claim 5,6,7 or8, wherein the metals are present in a weight ratio to one another within the range from 10 to 1 and 1 to 10.
10. A composition as claimed in any preceding claim, wherein the cracking catalyst contains silica and/or aiumina.
11. A composition as claimed in any preceding claim, wherein the su [fur sorbent is reactive al u mina.
Printed in the UK for HMSO, D8818935, 11184, 7102.
Published by The Patent Office, 25 Southampton Buildings, London, WC2A lAY, from which copies may be obtained.
GB08417699A 1981-08-27 1984-07-11 Catalyst for use in the fluid catalytic cracking of sulpur-containing hydrocarbons Expired GB2142551B (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US29661981A 1981-08-27 1981-08-27
US34491582A 1982-02-02 1982-02-02

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GB2142551A true GB2142551A (en) 1985-01-23
GB2142551B GB2142551B (en) 1985-09-11

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GB08223991A Expired GB2104406B (en) 1981-08-27 1982-08-20 Improved fluid catalytic cracking process and catalyst for use therein
GB08417699A Expired GB2142551B (en) 1981-08-27 1984-07-11 Catalyst for use in the fluid catalytic cracking of sulpur-containing hydrocarbons

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CA (1) CA1179314A (en)
DE (1) DE3230908A1 (en)
FR (1) FR2512050B1 (en)
GB (2) GB2104406B (en)
NL (1) NL8203278A (en)

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EA001407B1 (en) * 1996-07-15 2001-02-26 Шеврон Ю.Эс.Эй. Инк. Process for hydrotreating lubricating oil
CA2260104C (en) * 1996-07-16 2003-12-30 Chevron U.S.A. Inc. Base stock lube oil manufacturing process
ES2190552T3 (en) * 1998-02-06 2003-08-01 Kataleuna Gmbh Catalysts CATALYST FOR THE HYDROGENATION OF AROMATIC SUBSTANCES IN HYDROCARBON FRACTIONS CONTAINING SULFUR.

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1587040A (en) * 1977-06-09 1981-03-25 Air Prod & Chem Method for promoting regeneration of a hydrocarbon conversion catalyst in a fluidized bed regenerator

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA1124224A (en) * 1977-04-11 1982-05-25 Chevron Research And Technology Company Process for removing pollutants from catalyst regenerator flue gas
US4252636A (en) * 1978-04-11 1981-02-24 Atlantic Richfield Company Catalyst and process for conversion of hydrocarbons
US4241033A (en) * 1979-02-01 1980-12-23 Uop Inc. Process for the separation of sulfur oxides from a gaseous mixture containing sulfur oxides and oxygen
US4238317A (en) * 1979-08-20 1980-12-09 Standard Oil Company (Indiana) Catalytic cracking with reduced emission of noxious gases
US4259176A (en) * 1979-09-13 1981-03-31 Chevron Research Company Restricting silica content of catalyst inventory to prevent alumina poisoning for SOx control
US4300997A (en) * 1979-10-12 1981-11-17 Standard Oil Company (Indiana) Catalytic cracking with reduced emission of noxious gas

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1587040A (en) * 1977-06-09 1981-03-25 Air Prod & Chem Method for promoting regeneration of a hydrocarbon conversion catalyst in a fluidized bed regenerator

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GB2142551B (en) 1985-09-11
GB2104406A (en) 1983-03-09
CA1179314A (en) 1984-12-11
GB2104406B (en) 1985-09-04
FR2512050B1 (en) 1985-08-23
GB8417699D0 (en) 1984-08-15
DE3230908A1 (en) 1983-03-17
NL8203278A (en) 1983-03-16
FR2512050A1 (en) 1983-03-04

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Effective date: 19930820