US20110180453A1 - Catalytic Dewaxing Process - Google Patents
Catalytic Dewaxing Process Download PDFInfo
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- US20110180453A1 US20110180453A1 US12/974,517 US97451710A US2011180453A1 US 20110180453 A1 US20110180453 A1 US 20110180453A1 US 97451710 A US97451710 A US 97451710A US 2011180453 A1 US2011180453 A1 US 2011180453A1
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- catalyst
- dewaxing
- silica
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- wax
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- 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
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
- C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
- C10G45/64—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
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- 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
- C10G73/00—Recovery or refining of mineral waxes, e.g. montan wax
- C10G73/02—Recovery of petroleum waxes from hydrocarbon oils; Dewaxing of hydrocarbon oils
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- 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
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
- C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
- C10G45/62—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used containing platinum group metals or compounds thereof
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- 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
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
- C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
- C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
- C10G47/12—Inorganic carriers
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- 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
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
- C10G65/043—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a change in the structural skeleton
-
- 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
- C10G2300/20—Characteristics of the feedstock or the products
-
- 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
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
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- 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
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4018—Spatial velocity, e.g. LHSV, WHSV
Definitions
- the present disclosure relates to a process for catalytically dewaxing feeds having a variety of wax contents.
- Waxy feedstocks may be used to prepare basestocks having a high viscosity index (VI).
- VI viscosity index
- Dewaxing may be accomplished by means of a solvent or catalytically.
- Solvent dewaxing is a physical process whereby waxes are removed by contacting with a solvent, such as methyl ethyl ketone, followed by chilling to crystallize the wax and filtration to remove the wax.
- Catalytic dewaxing involves chemically converting the less desirable molecules to produce a basestock with more favorable low temperature properties.
- Catalytic dewaxing is a process for converting these long chain normal paraffins and slightly branched paraffins to improve the low temperature properties of the feed.
- Catalytic dewaxing may be accomplished using catalysts that function primarily by cracking waxes to lower boiling products, or by catalysts that primarily isomerize waxes to more highly branched products. Catalysts that dewax by cracking decrease the yield of lubricating oils while increasing the yield of lower boiling distillates. Catalysts that isomerize do not normally result in significant boiling point conversion. Catalysts that dewax primarily by cracking are exemplified by the zeolites ZSM-5, ZSM-11, ZSM-12, and offretite. Catalysts that dewax primarily by isomerization are exemplified by the zeolites ZSM-22, ZSM-23, SSZ-32, ZSM-35, and ZSM-48.
- United States Published Patent Application No. 2007/0131581 discloses ZSM-48 having a silica to alumina molar ratio of 110 or less that is free of non-ZSM-48 seed crystals and free of ZSM-50.
- the low silica ZSM-48 is shown to have improved activity in the dewaxing of slack wax.
- the catalyst contains a low level of hydrogenation metal and, even using high wax feeds, is sufficiently active to allow the dewaxing to be effected at commercially acceptable throughput rates and at temperatures which minimize the undesirable dry gas (C 4 ) make.
- the catalyst is also able to process feeds containing higher levels of nitrogen and sulfur than a lower activity catalyst could handle.
- the disclosure resides in a catalytic dewaxing process comprising:
- the catalyst comprises from 50 to 70 wt % of ZSM-48 having a silica to alumina molar ratio of less than 200:1.
- the ZSM-48 has a silica to alumina molar ratio of 100:1 or less.
- the catalyst comprises from 0.3 to 0.8 wt % of a metal or metal compound from Groups 8 to 10 of the Periodic Table of the Elements, especially platinum.
- the catalyst further comprises an inorganic oxide binder, such as silica, a silicate, or an aluminosilicate.
- an inorganic oxide binder such as silica, a silicate, or an aluminosilicate.
- said dewaxing conditions include a temperature of 365° C. or less, such as from 290° C. to 365° C., and a liquid hourly space velocity on the hydrocarbon feed of at least 0.4 hr ⁇ 1 , such as from 0.95 to 3 hr ⁇ 1 .
- FIG. 1 is a graph comparing the average reaction temperature required to achieve different final pour points with high and low sulfur hydrotreated slack wax feeds using the dewaxing process of Example 3.
- FIG. 2 is a graph comparing the 370° C.+ conversion required to achieve different final pour points with high and low sulfur feeds hydrotreated slack wax feeds using the dewaxing process of Example 3.
- FIG. 3 is a graph comparing the average reaction temperature required to achieve different final pour points with different feeds using the dewaxing catalyst of Example 1 and using a similar process but with a higher silica to alumina ZSM-48 catalyst.
- FIG. 4 is a graph comparing the 370° C.+ conversion required to achieve different final pour points with different feeds using the dewaxing catalyst of Example 1 and using a similar process but with a higher silica to alumina ZSM-48 catalyst.
- Described herein is a process for dewaxing hydrocarbon feedstocks that contain widely varying levels of wax, for example from slack waxes containing in excess of 90 wt % wax to a hydrocrackate containing less than 20 wt % wax, using a single catalyst in a single reactor in blocked operation.
- blocked operation means that, in dewaxing a first hydrocarbon feedstock having a wax content of less than 50 wt % and a second hydrocarbon feedstock having a wax content of 50 wt % or more, the first feedstock would, for example, be contacted with the catalyst under dewaxing conditions for a certain period of time. The supply of the first feedstock to the reactor would then be terminated or blocked, and the second feedstock would be supplied to the reactor without change-out of the catalyst but normally with the dewaxing conditions being changed to deal with the higher wax content of the feed.
- the present process employs a dewaxing catalyst comprising from 40 to 80 wt %, such as from 50 to 70 wt %, of ZSM-48 zeolite having a silica to alumina molar ratio of less than 200:1, typically 100:1 or less, and from 0.3 to 1.5 wt %, such as from 0.3 to 0.8 wt %, of a hydrogenation metal or metal compound from Groups 8 to 10 of the Periodic Table of the Elements.
- the metal or metal compound from Groups 8 to 10 is platinum or a compound thereof and is incorporated in the catalyst by impregnation or ion exchange.
- ZSM-48 is a zeolite having 10-ring unidirectional pores.
- ZSM-48, its X-ray diffraction pattern and a method for its preparation are described in each of U.S. Pat. Nos. 4,375,573, 4,397,827, 4,448,675 and 4,423,021.
- ZSM-48 has a silica/alumina molar ratio in excess of 200:1.
- the low silica/alumina ZSM-48 employed in the present process can be prepared by crystallizing a reaction mixture comprising silica, alumina, base, water and a directing agent (R) comprising a hexamethonium (N,N,N,N′,N′,N′-hexamethyl-1,6-hexanediammonium) salt, particularly hexamethonium dichloride or dihydroxide.
- the reaction mixture has the following composition.
- SiO 2 :Al 2 O 3 70 to 110 H 2 O:SiO 2 1 to 500 OH ⁇ :SiO 2 0.1 to 0.3, preferably 0.14 to 0.18 R:SiO 2 0.01-0.05, preferably 0.015 to 0.025
- the crystallization is generally conducted by stirring the reaction mixture at a temperature of 100 to 250° C. and produces ZSM-48 crystals having a silica:alumina molar ratio of 70 to 110 and a crystal size in the range of 0.01 to 1 ⁇ m. More information on this process for producing low silica/alumina ZSM-48 can be found in U.S. Published Patent Application No. 2007/0131581, the entire contents of which are incorporated herein by reference.
- the catalyst employed in the present process typically also contains from 20 to 60 wt % of a binder or matrix material. Binders are attrition resistant and resistant to the temperatures experienced by the catalyst in use. Binders may be catalytically active or inactive and include other zeolites, other inorganic materials such as clays and metal oxides, such as alumina, titania, silica and silica-alumina. Clays may be kaolin, bentonite and montmorillonite and are commercially available.
- suitable porous matrix materials in addition to silica-aluminas include other binary materials such as silica-magnesia, silica-thoria, silica-zirconia, silica-beryllia and silica-titania as well as ternary materials such as silica-alumina-magnesia, silica-alumina-thoria and silica-alumina-zirconia.
- the present process can be employed in the isomerization dewaxing of a wide variety of lube oil feedstocks.
- feedstocks are generally wax-containing feeds that boil in the lubricating oil range, typically having a 10% distillation point greater than 650° F. (343° C.), measured by ASTM D 86 or ASTM D2887.
- feeds may be derived from a number of sources such as oils derived from solvent refining processes such as raffinates, partially solvent dewaxed oils, deasphalted oils, distillates, hydrocracker bottoms, vacuum gas oils, coker gas oils, slack waxes, foots oils and the like, and Fischer-Tropsch waxes.
- Slack waxes are typically derived from hydrocarbon feeds by solvent or propane dewaxing. Slack waxes contain some residual oil and are typically deoiled. Foots oils are derived from deoiled slack waxes. Fischer-Tropsch waxes are prepared by the Fischer-Tropsch synthetic process.
- the feedstocks employed in the present process may have high contents of nitrogen and/or sulfur contaminants.
- feeds having a nitrogen content of up to 80 ppm, even up to 150 ppm, and/or a sulfur content of up to 250 ppm, even up 1000 ppm can be processed in the present process.
- Sulfur and nitrogen contents may be measured by standard ASTM methods D2622 and D4629, respectively.
- Suitable conditions for the present dewaxing process include temperatures of up to 426° C., preferably 365° C. or less, more preferably 290° C. to 365° C., pressures of from 791 to 20786 kPa (100 to 3000 psig), preferably 1480 to 17339 kPa (200 to 2500 psig), liquid hourly space velocities of from 0.1 to 10 hr ⁇ 1 , preferably at least 0.4 hr ⁇ 1 , more preferably from 0.95 to 3 hr ⁇ 1 , and hydrogen treat gas rates from 45 to 1780 m 3 /m 3 (250 to 10000 scf/B), preferably 89 to 890 m 3 /m 3 (500 to 5000 scf/B).
- Suitable hydrotreating catalysts contain Group 6 metals, Group 8-10 metals, and mixtures thereof.
- suitable metals include nickel, tungsten, molybdenum, cobalt and mixtures thereof. These metals are typically present as oxides or sulfides on refractory metal oxide supports.
- the mixture of metals may also be present as bulk metal catalysts wherein the amount of metal is 30 wt % or greater, based on catalyst.
- Suitable metal oxide supports include oxides such as silica, alumina, silica-aluminas or titania, preferably alumina.
- Preferred aluminas are porous aluminas such as gamma or eta.
- the amount of metal either individually or in mixtures, ranges from 0.5 to 35 wt %, based on the catalyst.
- Suitable hydrotreating conditions include temperatures of up to 426° C., such as from 150 to 400° C., for example from 200 to 350° C., a hydrogen partial pressure of from 1480 to 20786 kPa (200 to 3000 psig), such as from 2859 to 13891 kPa (400 to 2000 psig), a space velocity of from 0.1 to 10 hr 4 , such as from 0.1 to 5 hr ⁇ 1 , and a hydrogen to feed ratio of from 89 to 1780 m 3 /m 3 (500 to 10000 scf/B), preferably 178 to 890 m 3 /m 3 .
- the dewaxing catalyst employed in this Example comprised of 65 wt % of ZSM-48 having a silica to alumina molar ratio of 90/1 and 35 wt % alumina in the form of a 1.5 mm diameter by 3.25 mm length quadrulobe extrudate. This extrudate was steamed for 3 hours at 482° C. prior to impregnation with 0.3 wt % platinum (as tetraammine platinum nitrate salt). The catalyst was loaded into a vertical downflow reactor beneath a top bed of a hydrotreating catalyst comprising 15 wt % Pt/Pd on alumina.
- the above catalyst combination was used to consecutively hydrotreat and hydroisomerize four different feeds, a light neutral (LN) and a heavy neutral (HN) slack wax and an LN and an HN hydrocrackate having the properties listed in Table 1.
- the process was conducted at a liquid hourly space velocity (LHSV) 1 hr ⁇ 1 , a hydrogen circulation rate of 419 Nm 3 /m 3 , a pressure of 107 kg/cm 2 and an average reaction temperature adjusted to produce lube fractions having substantially the same pour point.
- LHSV liquid hourly space velocity
- Example 2 is a hypothetical example using the dewaxing catalyst and process conditions of Example 1 to process a similar set of feeds but having higher levels of sulfur and nitrogen impurities.
- the operating temperatures required to achieve the same 370° C.+ conversion as in Example 1 were calculated and the results are shown in Table 2.
- Table 2 shows that, depending on the wax content of the feed, high levels of sulfur and nitrogen that can be tolerated at nominal 365° C. dewaxing temperature with the catalyst of Example 1. Note that the conversion levels are the same in Example 2 as Example 1 thus leading to similar lube yields and properties.
- Example 2 the dewaxing catalyst of Example 1 was used to dewax two similar slack wax feeds that had undergone prior hydrotreatment with a conventional NiMo on alumina HDT catalyst under similar conditions as specified in Table 3 but with the temperature adjusted to result in hydrotreated products with different sulfur levels.
- the resultant hydrotrreated products were dewaxed to different pour points between ⁇ 10 and ⁇ 36° C. using the dewaxing catalyst specified in Example 1 and the results are summarized in FIGS. 1 and 2 .
- the feed properties for dewaxing are shown in Table 3 as “Product Properties” from the hydrotreating step.
- FIG. 1 shows that, although slightly higher temperatures (around 5° C.) were required to reached the desired pour point with the higher sulfur content feed, pour points as low as ⁇ 36° C. could still be achieved at reaction temperatures below 365° C.
- FIG. 2 shows that, in terms of conversion of 370° C.+ fraction, the impact of the higher sulfur content of feed B was a decreased lube yield of 6-10%.
- a dual catalyst comprising a top bed of a hydrotreating catalyst comprising 15 wt % Pt/Pd on alumina and a bottom bed of a dewaxing catalyst.
- the dewaxing catalyst comprised 65 wt % of ZSM-48 having a silica to alumina molar ratio of 90/1 and 35 wt % alumina in the form of a 1.5 mm diameter by 3.25 mm length quadrulobe extrudate.
- the extrudate was steamed for 3 hours at 482° C. prior to impregnation with 0.6 wt % platinum (as tetraammine platinum nitrate salt).
- the feed was treated at a 421 Nm 3 /m 3 hydrogen circulation rate, an LHSV of 1.33 hr ⁇ 1 , a pressure of 1600 psig (11133 kPa) and at the temperatures shown in Table 4.
- the results are also shown in Table 4 and demonstrate that the high activity catalyst, by allowing dewaxing to be effected at lower temperatures, permits higher sulfur content feeds to be processed while maintaining reasonable lube yields.
- Feed A a medium pressure hydrocrackate (MPHC) and Feed B: a lube hydrocrackate (LHDC), were investigated in this Example.
- the feeds had the properties shown in Table 5.
- the feeds were dewaxed using two different ZSM-48 catalysts.
- the first catalyst was the same dewaxing catalyst employed in Example 1.
- the second catalyst comprised 65 wt % of ZSM-48 having a silica to alumina molar ratio of 200/1 and 35 wt % alumina in the form of a 1.5 mm diameter by 3.25 mm length quadrulobe extrudate.
- the extrudate was steamed for 3 hours at 482° C. prior to impregnation with 0.6 wt % platinum (as tetraammine platinum nitrate salt).
- the feed was treated at a 421 Nm 3 /m 3 hydrogen circulation rate, an LHSV of 1.33 hr ⁇ 1 , a pressure of 2000 psig (13789 kPa).
- the results are shown in FIGS. 3 and 4 and demonstrate that the low silica/alumina ratio catalyst of Example 1 at a Pt content of only 0.3 wt % exhibits similar activity and selectivity (as measured by 370° C.+ conversion) to the higher silica/alumina ratio catalyst with a Pt content of 0.6 wt %.
- This example teaches that the higher zeolite activity can be compensated for by lowering the metal content.
- Feed B used in Example 5 is similar to the feed used in Example 4. Processing conditions are also similar between the two examples, although there is a 400 psig difference in pressure. If one compares the no sulfur result in Example 4 which used a catalyst comprised of 90/1 Si/Al2 crystal and 0.6 wt % Pt to the Feed B result processed with 0.3 wt % Pt and 90/1 Si/Al 2 ratio, one can see that increasing the metal content from 0.3 wt % to 0.6 wt % increases the catalyst activity.
- Example 4 required only 329° C. to achieve a ⁇ 25° C. pour point, while the catalyst from Example 5 with half the metal required approximately 340° C. to achieve a similar pour point.
- a catalytic dewaxing process comprising:
- the catalyst comprises from 50 to 70 wt % of ZSM-48 having a silica to alumina molar ratio of less than 200:1.
- the catalyst comprises from 0.3 to 0.8 wt % of a metal or metal compound from Groups 8 to 10 of the Periodic Table of the Elements.
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Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
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US12/974,517 US20110180453A1 (en) | 2009-12-24 | 2010-12-21 | Catalytic Dewaxing Process |
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US28483509P | 2009-12-24 | 2009-12-24 | |
US12/974,517 US20110180453A1 (en) | 2009-12-24 | 2010-12-21 | Catalytic Dewaxing Process |
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US12/974,517 Abandoned US20110180453A1 (en) | 2009-12-24 | 2010-12-21 | Catalytic Dewaxing Process |
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US (1) | US20110180453A1 (de) |
EP (1) | EP2516597A1 (de) |
JP (1) | JP2013515821A (de) |
KR (1) | KR20120114321A (de) |
CN (1) | CN102686709A (de) |
CA (1) | CA2784146A1 (de) |
IN (1) | IN2012DN05208A (de) |
RU (1) | RU2012128049A (de) |
SG (1) | SG181451A1 (de) |
WO (1) | WO2011079116A1 (de) |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2017116754A1 (en) * | 2015-12-28 | 2017-07-06 | Exxonmobil Research And Engineering Company | Dewaxing catalyst with improved aromatic saturation activity |
US10780430B2 (en) | 2015-12-28 | 2020-09-22 | Exxonmobil Research And Engineering Company | Sequential impregnation for noble metal alloy formation |
WO2023015168A1 (en) | 2021-08-06 | 2023-02-09 | ExxonMobil Technology and Engineering Company | Hydro-dealkylation process to generate high quality fuels, base stocks and waxes |
Citations (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4375573A (en) * | 1979-08-03 | 1983-03-01 | Mobil Oil Corporation | Selective production and reaction of p-Disubstituted aromatics over zeolite ZSM-48 |
US4397827A (en) * | 1979-07-12 | 1983-08-09 | Mobil Oil Corporation | Silico-crystal method of preparing same and catalytic conversion therewith |
US4423021A (en) * | 1979-08-08 | 1983-12-27 | Mobil Oil Corporation | Method of preparing silico-crystal ZSM-48 |
US4448675A (en) * | 1981-09-17 | 1984-05-15 | Mobil Oil Corporation | Silico-crystal ZSM-48 method of preparing same and catalytic conversion therewith |
US20040065588A1 (en) * | 2002-10-08 | 2004-04-08 | Genetti William Berlin | Production of fuels and lube oils from fischer-tropsch wax |
US20040108250A1 (en) * | 2002-10-08 | 2004-06-10 | Murphy William J. | Integrated process for catalytic dewaxing |
US20060252632A1 (en) * | 2002-10-08 | 2006-11-09 | Cody Ian A | Catalyst for wax isomerate yield enhancement by oxygenate pretreatment |
US20070131582A1 (en) * | 2005-12-13 | 2007-06-14 | Lai Wenyih F | Hydroprocessing with blended ZSM-48 catalysts |
US20070131581A1 (en) * | 2005-12-13 | 2007-06-14 | Lai Wenyih F | High activity ZSM-48 and methods for dewaxing |
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2010
- 2010-12-21 JP JP2012546148A patent/JP2013515821A/ja active Pending
- 2010-12-21 EP EP10840062A patent/EP2516597A1/de not_active Withdrawn
- 2010-12-21 RU RU2012128049/04A patent/RU2012128049A/ru not_active Application Discontinuation
- 2010-12-21 IN IN5208DEN2012 patent/IN2012DN05208A/en unknown
- 2010-12-21 SG SG2012039863A patent/SG181451A1/en unknown
- 2010-12-21 CA CA2784146A patent/CA2784146A1/en not_active Abandoned
- 2010-12-21 KR KR1020127019403A patent/KR20120114321A/ko not_active Application Discontinuation
- 2010-12-21 CN CN2010800586499A patent/CN102686709A/zh active Pending
- 2010-12-21 US US12/974,517 patent/US20110180453A1/en not_active Abandoned
- 2010-12-21 WO PCT/US2010/061542 patent/WO2011079116A1/en active Application Filing
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Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2017116754A1 (en) * | 2015-12-28 | 2017-07-06 | Exxonmobil Research And Engineering Company | Dewaxing catalyst with improved aromatic saturation activity |
US9944865B2 (en) | 2015-12-28 | 2018-04-17 | Exxonmobil Research And Engineering Company | Dewaxing catalyst with improved aromatic saturation activity |
US10780430B2 (en) | 2015-12-28 | 2020-09-22 | Exxonmobil Research And Engineering Company | Sequential impregnation for noble metal alloy formation |
US11198115B2 (en) | 2015-12-28 | 2021-12-14 | Exxonmobil Research And Engineering Company | Sequential impregnation for noble metal alloy formation |
WO2023015168A1 (en) | 2021-08-06 | 2023-02-09 | ExxonMobil Technology and Engineering Company | Hydro-dealkylation process to generate high quality fuels, base stocks and waxes |
Also Published As
Publication number | Publication date |
---|---|
IN2012DN05208A (de) | 2015-10-23 |
WO2011079116A1 (en) | 2011-06-30 |
RU2012128049A (ru) | 2014-01-27 |
SG181451A1 (en) | 2012-07-30 |
KR20120114321A (ko) | 2012-10-16 |
CA2784146A1 (en) | 2011-06-30 |
EP2516597A1 (de) | 2012-10-31 |
CN102686709A (zh) | 2012-09-19 |
JP2013515821A (ja) | 2013-05-09 |
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