WO2004033587A2 - Procede integre de deparaffinage catalytique - Google Patents

Procede integre de deparaffinage catalytique Download PDF

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WO2004033587A2
WO2004033587A2 PCT/US2003/033324 US0333324W WO2004033587A2 WO 2004033587 A2 WO2004033587 A2 WO 2004033587A2 US 0333324 W US0333324 W US 0333324W WO 2004033587 A2 WO2004033587 A2 WO 2004033587A2
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zsm
dewaxing
group
feedstock
hydrodewaxing
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PCT/US2003/033324
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English (en)
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WO2004033587A3 (fr
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William J. Murphy
Ian A. Cody
Jacob B. Angelo
Zhaozhong Jiang
Jeffery C. Trewella
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Exxonmobil Research And Engineering Company
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Priority to JP2005501188A priority Critical patent/JP2006502307A/ja
Priority to CA002500455A priority patent/CA2500455A1/fr
Priority to AU2003286540A priority patent/AU2003286540A1/en
Priority to EP03777742A priority patent/EP1549725A2/fr
Publication of WO2004033587A2 publication Critical patent/WO2004033587A2/fr
Publication of WO2004033587A3 publication Critical patent/WO2004033587A3/fr

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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
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
    • 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
    • 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

Definitions

  • This invention related to an integrated catalytic hydrodewaxing process for hydrocarbon feeds. More particularly, a feedstock containing sulfur and nitrogen contaminants is subject to a process including hydrotreating, hydrodewaxing and/or hydrofinishing without disengagement between the process steps.
  • Dewaxing of hydrocarbon feedstocks is conventionally used to improve the flow properties of the feed, typically by lowering the pour point.
  • Dewaxing catalysts remove waxy components of feeds by either selective hydrocracking or isomerization.
  • the selectivity of dewaxing catalysts may be improved by employing constrained intermediate pore molecular sieves.
  • the activity of such selective catalysts may be improved by employing a metal hydrogenation/dehydrogenation component.
  • dewaxing catalysts are sensitive to environments containing sulfur and/or nitrogen contaminants. Such contaminants negatively impact catalyst activity, catalyst aging and catalyst selectivity.
  • a hydrotreating and/or hydrocracking step prior to the dewaxing step to convert nitrogen and sulfur containing contaminants to ammonia and hydrogen sulf ⁇ de and to remove these gaseous contaminants from the process prior to the dewaxing step.
  • the present invention relates to an integrated dewaxing process capable of operating with highly contaminated feedstocks.
  • the integrated process for dewaxing a raffmate feedstock containing up to 20,000 ppmw sulfur and up to 1000 ppmw nitrogen comprises: (a) contacting the feedstock with a hydrotreating catalyst under hydrotreating conditions to produce a hydrotreated feedstock and gaseous nitrogen- and sulfur-containing contaminants, and (b) passing at least a portion of the hydrotreated feedstock and gaseous components from step (a) without disengagement to a hydrodewaxing zone containing a dewaxing catalyst including at least one of ZSM-48, ZSM-22, ZSM-23, ZSM-5, ZSM-35, Beta, SSZ- 31.SAPO-11, SAPO-31, SAPO-41, MAPO-11, ECR-42, synthetic ferrierites, mordenite, offretite, erionite, and chabazite and hydrodewaxing the hydrotreated feedstock
  • Another embodiment relates to an integrated process for dewaxing a raffmate feedstock containing up to 20,000 ppmw sulfur and up to 1000 ppmw nitrogen which comprises: (a) contacting the feedstock with a hydrotreating catalyst under hydrotreating conditions to produce a hydrotreated feedstock and gaseous nitrogen- and sulfur-containing contaminants, (b) passing at least a portion of the hydrotreated feedstock and gaseous sulfur- and nitrogen-containing contaminants from step (a) without disengagement to a hydrodewaxing zone containing a dewaxing catalyst including at least one of ZSM-48, ZSM-22, ZSM- 23, ZSM-5, ZSM-35, Beta, SSZ- 31,SAPO-ll, SAPO-31, SAPO-41, MAPO-11, ECR- 42, synthetic ferrierites, mordenite, offretite, erionite, and chabazite and hydrodewaxing the hydrotreated feedstock under hydrodewaxing conditions, said dewaxing
  • Yet another embodiment relates to an integrated process for dewaxing a raffmate feedstock containing up to 20,000 ppmw sulfur and up to 1000 ppmw nitrogen which comprises: (a) contacting the feedstock with a dewaxing catalyst including at least one of ZSM-48, ZSM-22, ZSM-23, ZSM-5, ZSM-35, Beta, SSZ- 31.SAPO-11, SAPO-31, SAPO-41, MAPO-11, ECR-42, synthetic ferrierites, mordenite, offretite, erionite, and chabazite under hydrodewaxing conditions, said dewaxing catalyst including a metal hydrogenation component which is at least one Group 6 metal, at least one Group 8-10 metal, or mixtures of Group 6 and Group 8- 10 metals, to form a hydrodewaxed product, and (b) passing at least a portion of the hydrodewaxed product and gaseous components from step (b) to a hydrofinishing zone and hydro
  • a still further embodiment relates to an integrated process for dewaxing a raffmate feed which comprises: (a) solvent dewaxing the raffinate to form a raffmate and a slack wax, (b) deoiling the slack wax to produce a foots oil, (c) contacting the foots oil with a hydrotreating catalyst under hydrotreating conditions to produce a hydrotreated foots oil and gaseous nitrogen- and sulfur-containing contaminants and (d) passing at least a portion of the hydrotreated foots oil and gaseous sulfur- and nitrogen-containing contaminants from step (c) without disengagement to a hydrodewaxing zone containing a dewaxing catalyst including at least one of ZSM-48, ZSM-22, ZSM-23, ZSM-5, ZSM-35, Beta, SSZ-31.SAPO- 11, SAPO-31, SAPO-41, MAPO-11, ECR-42, synthetic ferrierites, mordenite, offretite, eri
  • Figure 1 is a graph showing average reactor temperature at given pour point .
  • Figure 2 is a graph showing polar tolerance of the catalyst.
  • Figure 3 is a graph showing lube yields for dewaxing a medium neutral foots oil over a Crosfield hydrotreating catalyst followed by a Pt/ZSM-48 dewaxing catalyst.
  • Figure 4 is a graph showing viscosity of the dewaxed medium neutral foots oil.
  • Figure 5 is a graph showing VI of the dewaxed medium neutral foots oil.
  • Figure 6 is a graph showing cloud points of the dewaxed medium neutral foots oil.
  • the steps are integrated, i.e., a process that incorporates a sequence of steps which are interrelated and dependent on either earlier or later steps, said steps occurring without disengagement between the sequence of steps.
  • Dewaxing catalysts which are isomerization catalysts are normally shape selective intermediate pore molecular sieves loaded with a hydrogenation metal, particularly noble metals.
  • a hydrogenation metal particularly noble metals.
  • isomerization dewaxing catalysts are considered susceptible to poisoning by sulfur- and nitrogen-containing contaminants such as NH 3 and H 2 S. They are thus normally protected by a preceding treatment to remove such poisons.
  • An example of such pre-treatment is conversion of sulfur- and nitrogen-containing contaminants to H 2 S and NH 3 , respectively, by hydrotreatment.
  • hydrotreatement is followed by disengagement to remove (strip) the sulfur- and nitrogen-containing contaminants prior to dewaxing so as not to poison the catalyst.
  • Feeds for the present integrated dewaxing process include raffmates.
  • Raffmates are obtained from solvent extraction processes that selectively dissolve the aromatic components in an extract phase while leaving the more paraffmic components in a raffmate phase. Naphthenes are distributed between the extract and raffmate phases.
  • Typical solvents for solvent extraction include phenol, furfural and N-methyl pyrrolidone.
  • the raffmates from solvent extraction may be further subject to solvent dewaxing to separate a lube oil fraction and a slack wax.
  • Solvent dewaxing may be accomplished by treating the raffmates with a solvent such as propane, ketones and mixtures of ketones with aromatics such as benzene, toluene and/or xylene and chilling to crystallize and separate wax molecules.
  • the resulting slack wax is then deoiled to separate a foots oil (soft wax) from microcrystalline wax (hard wax).
  • the slack wax or foots oil may be blended with a raffmate to form a blended feedstock.
  • the ratio of raffmate to slack wax or foots oil in the blended feedstock may range from 99: 1 to 1 : 99.
  • the raffmate, slack wax or foots oil feeds are characterized in that they may contain high levels up to 20,000 ppmw of sulfur containing contaminants and up to 1,000 ppmw of nitrogen containing contaminants.
  • An important purpose of hydrotreating is to reduce the sulfur and nitrogen content of a feed. Hydrotreating for the present process is not primarily concerned with boiling point conversion of the feed. Hydrotreating catalysts usually contain at least one of Group 6 and Group 8-10 metal (Groups based on the IUPAC Periodic Table format having groups from 1 to 18), on a less acidic support such as alumina or silica. Catalysts may also be bulk metal catalysts wherein the amount of metal may be 30 wt.% or more.
  • hydrotreating catalysts are low acidity, high metals content catalysts such as KF-848 (Akzo Nobel), DN 190 (Criterion catalysts) and RT 721 (Akzo Nobel).
  • the amount of metal is from 0.1 to 95 wt.%, based on catalyst.
  • Hydrotreating conditions include temperatures of 315 - 425°C, pressures of 2170 - 20786 kPa (300 - 3000 psig), liquid hourly space velocities (LHSV) of 0.1 - 10 and hydrogen treat rates of 89 - 1780 m 3 /m 3 (500 - 10,000 scf/bbl).
  • dewaxing catalysts can function in a sour environment.
  • the present dewaxing catalysts include ZSM-48, ZSM-22, ZSM-23, ZSM-5, ZSM-35, Beta, SSZ- 31,SAPO-l l, SAPO-31, SAPO-41, MAPO-11, ECR-42, synthetic ferrierites, mordenite, offretite, erionite, and chabazite, with ZSM-48, ZSM-22, ZSM-5, ZSM-23 and ZSM-35 being preferred while ZSM-48 is a more preferred embodiment.
  • ZSM-48 is a unidimensional intermediate pore 10 ring zeolite having a pore size of 5.3 A x 5.6 A.
  • ZSM-48 is commercially available and its preparation is described in U.S. patents 4,397,827, 4,448,675 and 5,075,269.
  • ZSM-22 is described in U.S. Patent 4,556,477, ZSM-23 in U.S. patent 4,076,342 and ZSM-35 in U.S. patent 4,016,245.
  • the dewaxing catalysts are bifunctional, i.e., they are loaded with a metal hydrogenation component, which is at least one Group 6 metal, at least one Group 8 - 10 metal, or mixtures thereof.
  • Preferred metals are Groups 9 -10 metals.
  • Groups 9 - 10 noble metals such as Pt, Pd or mixtures thereof (based on the IUPAC Periodic Table format having Groups from 1 to 18). These metals are loaded at the rate of 0.1 to 30 wt.%, based on catalyst.
  • Catalyst preparation and metal loading methods are described for example in U.S. Patent No. 6,294,077, and include for example ion exchange and impregnation using decomposable metal salts.
  • Metal dispersion techniques and catalyst particle size control are described in U.S. Patent No. 5,282,958. Catalysts with small particle size and well-dispersed metal are preferred.
  • the dewaxing catalysts are typically composited with binder materials which are resistant to high temperatures which may be employed under dewaxing conditions to form a finished dewaxing catalyst or may be binderless (self-bound).
  • the binder materials are usually inorganic oxides such as silica, alumina, silica- aluminas, binary combinations of silicas with other metal oxides such as titania, magnesia, thoria, zirconia and the like and tertiary combinations of these oxides such as silica-alumina -thoria and silica-alumina magnesia.
  • the amount of molecular sieve in the finished dewaxing catalyst is from 10 to 100, preferably 35 to 100 wt.%), based on catalyst.
  • Such catalysts are formed by methods such spray drying, extrusion and the like.
  • the dewaxing catalyst may be used in the sulfided or unsulfided form, and is preferably in the sulfided form.
  • the temperature for the present dewaxing process is in the range from 360 to 425°C . Due to the catalyst structure, these temperatures may be higher than the temperatures normally used for catalytic dewaxing without the cracking that might otherwise be expected from such higher temperatures.
  • Other process conditions include hydrogen pressures of from 2859 - 20786 kPa (400 to 3000 psig), liquid hourly space velocities of 0.1 to 10 LHSV and hydrogen treat gas rates of from 53.4 - 1780 m 3 /m 3 (300 to 10,000 scf/bbl).
  • the hydrodewaxing catalyst may contain a second catalytic component which may be admixed with the ZSM-48 dewaxing catalyst or may be in a stacked (layered) configuration with the second component in the upper layer.
  • the second catalyst is tolerant of sulfur- and nitrogen-containing contaminants.
  • Typical catalysts that are tolerant of such contaminants include ZSM-5 and larger pore catalysts such as zeolite beta.
  • a convenient measure of the extent to which a dewaxing catalyst provides control molecules of varying sizes to its internal structure is the Constraint Index of the zeolite. Zeolites which provide a highly restricted access to and egress from its internal structure have a high value for the Constraint Index, and zeolites of this kind usually have pores of small size.
  • zeolites which provide relatively free access to the internal zeolite structure have a low value for the Constraint Index.
  • the method by which Constraint Index is determined is described fully in U.S. Pat. No.4,016,218, to which reference is made for details of the method.
  • Large pore zeolites having Constraint Indices less than 1 include TEA mordenite (0.4), dealuminized Y (0.5), ZSM-4 (0.5), ZSM-20 (0.5), mordenite (0.5), REY (0.4) and ultrastable Y.
  • Zeolite beta is also within the scope of large pore zeolites.
  • the second catalytic component may also be acidic porous amorphous materials, such as amorphous aluminosilicate, halogenated alumina, acidic clay, alumina or silica-alumina.
  • At least a portion of the products from the hydrodewaxing zone or step may then be passed to a hydrofinishing step again without the need of disengagement between the hydrodewaxing and hydrofinishing steps.
  • Catalysts for hydrofinishing can the same as those used for the preliminary hydrotreating step, if any, i.e., those containing at least one of Group 6 and Group 8-10 metal on a support such as alumina or silica. Examples include Ni/Mo, Co/Mo and Ni/W catalysts.
  • Preferred hydrotreating catalysts include catalyst such as KF-840, KF-848 (Akzo Nobel), DN 190 (Criterion catalysts) and RT 721 (Akzo Nobel).
  • the hydrofinishing catalyst may also be a crystalline mesoporous material belonging to the M41S class or family of catalysts.
  • the M41S family of catalysts are crystalline mesoporous materials having high silica contents whose preparation is further described in J. Amer. Chem. Soc, 1992, 114, 10834. Examples included MCM-41, MCM-48 and MCM-50.
  • a preferred member of this class is MCM-41 whose preparation is described in US Patent No. 5,098,684.
  • MCM-41 is characterized by having a hexagonal crystal structure with a unidimensional arrangement of pores having a cell diameter greater than 13 Angstroms.
  • MCM-41 The physical structure of MCM-41 is like a bundle of straws wherein the opening of the straws (the cell diameter of the pores) ranges from 13 to 100+ Angstroms.
  • MCM-48 has a cubic symmetry and is described for example is U.S. Patent No. 5,198,203 whereas MCM-50 has a lamellar structure and is described in US Patent No. 5,246,689.
  • the amount of metal is from 0.1 to 5 wt.%, preferably 0.2 to 2 wt.%, based on catalyst.
  • Hydrofinishing conditions include temperatures of 150 -350°C, preferably 180 - 300°C, pressures of 100 - 3000 psig (790 - 20786 kPa), preferably 50 - 2500 psig (1135 - 17339 kPa), LHSV of 0.1 - 20, preferably 0.2 - 15 and treat gas rates of 300 - 10000 scf/bbl (53 - 1780 m 3 /m 3 ), preferably 450 -5000 scf/B (80 - 890 m 3 /m 3 ).
  • dewaxed product from hydrodewaxing is passed to hydrofinishing without disengagement.
  • the preferred hydrofinishing conditions will include a temperature range of from 150 - 300°C.
  • the product from the hydrofinishing step is typically passed to a separator which may include stripping and /or fractionation.
  • a separator which may include stripping and /or fractionation.
  • sulfur- and nitrogen containing contaminants, especially hydrogen sulfide and ammonia are separated together with other gaseous components from liquid product.
  • the liquid product may be fractionated to obtain various cuts of lubricating oil products based on boiling range.
  • the process sequence may include the following steps in various combinations.
  • a waxy feed is first solvent extracted to separate a raffmate and an extract.
  • the raffmate may then be sent directly to hydrotreating, may be hydrodewaxed directly or may be solvent dewaxed to produce a lubricating oil and a slack wax.
  • the slack wax yields a hard wax and foots oil which may then be sent to hydrotreating.
  • hydrotreating and hydrodewaxing steps may take place sequentially in separate reactors or may occur as stacked beds in a single reactor. Any hydrofinishing step will occur in a separate reactor. If the hydrodewaxing step involves more than one dewaxing catalyst, then the hydrodewaxing step may involve a mixture of dewaxing catalysts in a single reactor, stacked beds in a single reactor, or separate reactors in sequence each containing a dewaxing catalyst.
  • the process sequence involving foots oils may include hydrotreating, hydrodewaxing and optionally hydrotreating. As in the case of raffmates, the sequence may take place sequentially in separate reactors or may occur as stacked beds in a single reactor.
  • Table 1 compares three processing configurations for dewaxing a 260 Neutral raffmate containing 6680 wppm sulphur and 50.6 wppm nitrogen and a dry wax content of 16.75 wt.% on feed at -18 pour point.
  • Column A illustrates the properties of a dewaxed oil obtained by solvent dewaxing with methylisobutyl ketone at a feed to solvent ratio of 3:1, the 260 Neutral raffmate.
  • the raffmate Prior to solvent dewaxing, the raffmate had been hydrotreated over an Akzo KF-848 hydrotreated catalyst at an average reactor temperature of 350°C, 0.53 LHSV, at a treat gas rate of 2600 SCF H 2 /bbl of feed and 1800psig.
  • the sulphur and nitrogen contents of the hydrotreated raffmate were less than 2 wppm.
  • Column B illustrates the properties of the product made by hydrotreating the 260N raffmate over Akzo KF 848 at an average reactor temperature of 350°C, 0.53LHSV, 1800psig and at a treat gas rate of 2600SCF H 2 /bll of feed but followed by catalytic dewaxing over a hydrodewaxing catalyst containing ZSM-48.
  • the process conditions during hydrodewaxing were 0.76 LHSV, 1650SCF/B H 2 , and 1800psig.
  • the gas phase polar species e.g., ammonia and hydrogen sulphide
  • Column C illustrates the properties of the product made by hydrotreating the 260N raffmate over Akzo KF 848 at an average reactor temperature of 350°C, 0.53LHSV and at a treat gas rate of 2600SCF H 2 /bbl of feed but hydrodewaxing over a hydrodewaxing catalyst containing ZSM-48.
  • the process conditions in the hydrodewaxing stage were 0.76 LHSV, 1650SCF/B H 2 , and 1800psig.
  • the gas phase polar species generated during the hydrotreating stage were cascaded with the hydrogen over the hydrodewaxing stage which required that the temperature of the dewaxing stage was higher than that in column B.
  • Table 2 compares three processing configurations for dewaxing a 130 Neutral raffmate containing 2500wppm sulphur and 25 wppm nitrogen and a dry wax content of 16.44 wt.% on feed at -16°C pourpoint.
  • Column A illustrates the properties of a dewaxed oil obtained by solvent dewaxing with methylisobutyl ketone at a feed to solvent ratio of 3:1, the 130 Neutral raffmate.
  • the raffmate Prior to solvent dewaxing, the raffmate had been hydrotreated over an Akzo KF848 hydrotreated catalyst at an average reactor temperature of 350°C, 0.53LHSV, at a treat gas rate of 2600SCF H 2 /bll of feed and 1800psig.
  • the sulphur and nitrogen contents of the hydrotreated raffmate were less than 2wppm.
  • Column B illustrates the properties of the product made by hydrotreating the 130N raffmate over Akzo KF 848 at an average reactor temperature of 350°C, 0.53LHSV, 1800 ⁇ sig and at a treat gas rate of 2600SCF H 2 /bll of feed but followed by catalytic dewaxing over a hydrodewaxing catalyst containing ZSM-48.
  • the process conditions during hydrodewaxing were 0.76 LHSV, 1650SCF/B H 2 , and l ⁇ OOpsig.
  • the gas phase polar species e.g., ammonia and hydrogen sulphide
  • Column C illustrates the properties of the product made by hydrotreating the 130N raffmate over Akzo KF 84 ⁇ at an average reactor temperature of 350°C, 0.53LHSV and at a treat gas rate of 2600SCF H 2 /bll of feed but hydrodewaxing over a hydrodewaxing catalyst containing ZSM-4 ⁇ .
  • the process conditions in the hydrodewaxing stage were 0.76 LHSV, 1650SCF/B H 2 , and l OOpsig.
  • the gas phase polar species generated during the hydrotreating stage were cascaded with the hydrogen over the hydrodewaxing stage which required that the temperature of the dewaxing stage was higher than that in column B.
  • This example illustrates the effect of treat gas rate on the hydrodewaxing stage operating in a sour gas environment.
  • the 13 ON raffmate was hydrotreated over Akzo KF ⁇ 4 ⁇ at an average reactor temperature of 350°C, 0.53LHSV and at a freat gas rate of 2600SCF H 2 /bll of feed and hydrodewaxing over a hydrodewaxing catalyst containing ZSM-4 ⁇ .
  • the process conditions in the hydrodewaxing stage were 0.76 LHSV, 1650 to 2500SCF/B H 2 , and 1800psig.
  • the gas phase polar species generated during the hydrotreating stage were cascaded with the hydrogen over the hydrodewaxing stage.
  • the hydrodewaxing catalyst is a ZSM-48 bound with alumina (35/65 wt ratio respectively) operating under a series of conditions shown in Figure 1.
  • Figure 1 illustrates that by increasing the treat gas rate from 1650SCFH 2 /B feed to 2100 and then to 2500SCFH 2 /B feed, the Average Reactor Temperature required to maintain a feed pour point of 10°F decreases from 690 to 680°F for a 13 ON raffmate.
  • This example illustrates the application of a hydrodewaxing catalyst catalyst, containing ZSM-4 ⁇ and alumina 65/35wt%, for hydrodewaxing a 130N waxy raffmate containing , 7270 wppm sulfur and 32.6 wppm of total nitrogen, and a dry wax content of 17wt% on feed at a pour point of -l ⁇ °Cat 400 psig H 2 and 2500SCF/B H 2 without pre-hydrofreating but having a hydrofinishing step.
  • Table 4 illustrates that hydrodewaxing the unhydrofreated waxy raffmate gives a 370°C+ product having an eight point higher VI than that produced by solvent dewaxing.
  • Figure 2 illustrates the polar tolerance of the catalyst given 50 days on stream with the unhydrofreated 13 ON Raffinate feedstock.
  • This Example illustrates the cascade dewaxing of a foots oil feed.
  • Two soft wax feeds a medium neutral Foots oil (MNFO) and light neutral Foots oil (LNFO), were used for the dewaxing study.
  • MNFO medium neutral Foots oil
  • LNFO light neutral Foots oil
  • Crosfield 599 was used as a pre-hydrotreating catalyst followed by Pt/ZSM-48 dewaxing catalyst.
  • Crosfield 599 is a commercial catalyst containing a mixture of NiO and M0O 3 supported on alumina. The properties and metal contents of the catalyst are shown below.
  • Crosfield 599 224 m 2 /g (surface area), 1.37 g/cc (particle density), 35% Al, 3. ⁇ % Ni, 17% Mo.
  • the dewaxing catalyst was alumina (35 wt.%) bound, ZSM-4 ⁇ crystals containing 0.6 wt.% platinum.
  • the dewaxing experiments were performed using a microunit equipped with two cascaded down-flow trickle bed tubular reactors and two three-zone furnaces. The unit was heat-traced to avoid freezing of the waxy feedstocks. To reduce feed bypassing and lower zeolite pore diffusion resistance, the catalyst extrudates were crushed and sized to 60- ⁇ O mesh. The first reactor was then loaded with a mixture of 7.5 cc of the sized Crosfield 599 and 3 cc of ⁇ 0-120 mesh sand. The second reactor was loaded with a mixture of 15 cc of the sized Pt/ZSM-4 ⁇ and 5 cc of 80-120 mesh sand.
  • the catalysts were dried and reduced at 204°C (400°F) for one hour under 1 atmosphere, 255 cc/min hydrogen flow. The catalysts were then sulfided at 371°C (700°F) for 12 h using 100 cc/min, 2% H 2 S in H 2 .
  • the MNFO was first processed over the cascaded Crosfield 599/Pt-ZSM-48, followed by switching feed to the LNFO.
  • TLPs Total liquid products
  • IBP initial boiling point
  • -330°F initial boiling point
  • 166-343°C 330-650°F
  • 343°C+ 650°F+
  • the 343°C+ (650°F+) lube fractions were again analyzed by simulated distillation (Simdis) to ensure accuracy of the actual distillation operations.
  • the pour point and cloud point of 343°C+ 650°F+ lubes were measured according to corresponding ASTM D97 and D2500 methods, and their viscosities were determined at both 40°C and 100°C according to ASTM D445-3 and D445-5 methods, respectively.
  • the dewaxing of the MNFO was carried out under 6996 kPa (1000 psig) H 2 at 2.0 If 1 LHSV based on Crosfield 599 and 1.0 h "1 LHSV based on Pt/ZSM-4 ⁇ . Hydrogen/feed ratio of 1015 m /m (5700 scf/bbl) was used. The temperature of both Reactor 1 (containing Crosfield 599) and Reactor 2 (containing Pt/ZSM-4 ⁇ ) was kept same.
  • the dewaxed oil yields and properties are summarized in Table 6. For further clarification, the dewaxing results are also illustrated in Figures 3-6.
  • This example shows the dewaxing of LNFO at 6996 kPa H 2 .
  • the process conditions used for dewaxing the LNFO were similar to those for the MNFO.
  • the experiments were carried out under 6996 kPa (1000 psig) H 2 at 2.0 h "1 LHSV based on Crosfield 599 and 1.0 h "1 LHSV based on Pt/ZSM-48. Hydrogen/feed ratio of 5700 scf/bbl (1015 m /m ) was employed.
  • the temperature of Reactor 1 (containing Crosfield 599) and Reactor 2 (containing Pt/ZSM-4 ⁇ ) was kept same.
  • the dewaxed oil yields and properties are summarized in Table ⁇ ; and for further clarification, the results are depicted in Figures 5- ⁇ .
  • Byproduct Yields for Dewaxing the MNFO and LNFO were determined as follows. The processes were carried out under 6996 kPa (1000 psig) H 2 at 2.0 h "1 LHSV based on Crosfield 599 and 1.0 h "1 LHSV based on Pt/ZSM-48. Hydrogen/feed ratio of 1015 m 3 /m 3 (5700 scf/bbl was employed. The temperature of Reactor 1 (containing Crosfield 599) and Reactor 2 (containing Pt/ZSM-4 ⁇ ) was kept same. The yields of dewaxed oil and lighter byproducts are summarized in Table 9. For both MNFO and LNFO dewaxing, the major byproducts were distillate and naphtha with relatively small amount ( ⁇ ⁇ %) of C 1 -C gases.

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Abstract

L'invention porte sur un procédé intégré de déparaffinage de charges fraîches d'hydrocarbures dans un environnement sulfureux. Ce procédé inclut l'hydrotraitement, le déparaffinage, l'hydrofinissage ou la combinaison de ces traitements, procédé au cours duquel les étapes sont liées.
PCT/US2003/033324 2002-10-08 2003-10-07 Procede integre de deparaffinage catalytique WO2004033587A2 (fr)

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JP2005501188A JP2006502307A (ja) 2002-10-08 2003-10-07 接触脱ロウのための総合的プロセス
CA002500455A CA2500455A1 (fr) 2002-10-08 2003-10-07 Procede integre de deparaffinage catalytique
AU2003286540A AU2003286540A1 (en) 2002-10-08 2003-10-07 Integrated process for catalytic dewaxing
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EP2516590A1 (fr) * 2009-12-23 2012-10-31 ExxonMobil Research and Engineering Company Déparaffinage catalytique de charges non sulfureuses ou sulfureuses suivant une configuration de mode en blocs
US20240010504A1 (en) * 2022-07-05 2024-01-11 Saudi Arabian Oil Company Hierarchically ordered crystalline microporous materials with long-range mesoporous order having lamellar symmetry

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JP2013515821A (ja) * 2009-12-24 2013-05-09 エクソンモービル リサーチ アンド エンジニアリング カンパニー 接触脱ロウプロセス
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WO2004033587A3 (fr) 2004-07-01
US20040108250A1 (en) 2004-06-10

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