WO2009088454A1 - Integrated two-stage desulfurization/dewaxing with stripping high-temperature separator - Google Patents
Integrated two-stage desulfurization/dewaxing with stripping high-temperature separator Download PDFInfo
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- WO2009088454A1 WO2009088454A1 PCT/US2008/014053 US2008014053W WO2009088454A1 WO 2009088454 A1 WO2009088454 A1 WO 2009088454A1 US 2008014053 W US2008014053 W US 2008014053W WO 2009088454 A1 WO2009088454 A1 WO 2009088454A1
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- temperature
- hydrotreatment
- catalytic dewaxing
- zone
- dewaxing
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Classifications
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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
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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
- C10G2300/10—Feedstock materials
- C10G2300/1011—Biomass
- C10G2300/1014—Biomass of vegetal origin
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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
- C10G2300/10—Feedstock materials
- C10G2300/1011—Biomass
- C10G2300/1018—Biomass of animal origin
-
- 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
- C10G2300/1022—Fischer-Tropsch products
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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
- C10G2300/20—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
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/304—Pour point, cloud point, cold flow properties
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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
- C10G2300/4006—Temperature
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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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
Definitions
- This invention relates to a two stage hydroprocessing process with interstage stripping. More particularly, the interstage stripping occurs at high pressure and temperature with recycle of high temperature gaseous effluent from the stripping stage.
- a common method to remove contaminants such as nitrogen and sulfur from a hydrocarbon feedstock in diesel fuel production is to use a hydrotreating step to convert the nitrogen and sulfur contaminants to hydrogen sulfide and ammonia.
- the hydrotreating step may then be followed by a catalytic dewaxing step to improve the flow properties of the diesel fuel, such as cloud point.
- the catalyst for such a dewaxing step is typically sensitive to the presence of sulfur and nitrogen contaminants.
- One conventional approach for producing a diesel fuel is to perform the hydrotreatment and dewaxing steps in a single reactor. In such a configuration, the output from the hydrotreatment step is cascaded to the dewaxing step.
- the processing temperatures for the hydrotreatment and dewaxing steps will be similar.
- the temperature of the system will typically be selected based on the hydrotreatment step, with the result that the dewaxing step operates at a higher temperature than necessary. This leads to overprocessing of the diesel fuel, which produces a lower cloud point than necessary, and a correspondingly lower yield. Additionally, this type of configuration tends to reduce the operating lifetime of the dewaxing catalyst.
- the dewaxing step may operate at a higher temperature than is needed for hydrotreatment, such as when a new hydrotreatment catalyst is loaded into a reactor, leading to similar reduction in operating lifetime for the hydrotreatment catalyst.
- the cascaded product can be passed through a high temperature separator prior to being introduced into the dewaxing stage, but sulfur and nitrogen containing gases are typically not fully removed, which results in faster aging of the dewaxing catalyst.
- U.S. Patent 6,635,170 provides a general system for catalytic treatment of a hydrocarbon feed.
- a feedstock is hydroprocessed to remove contaminants, undergoes a first stripping step at a pressure similar to the operating pressure of the hydrotreatment step, and then is subjected to a second hydroprocessing step.
- the product from the second hydroprocessing step is then stripped, and at least a portion of the gases from the second hydroprocessing step are recycled to serve as the stripping gas for the first stripping step.
- U.S. Patent 6,623,628 provides a system for processing of middle distillates to make products such as diesel fuel.
- the middle distillate is subjected to hydroprocessing in two separate reactors with stripping in between. A portion of the product from the second hydroprocessing step is then refluxed back to the start of the hydroprocessing train.
- U.S. Published Patent Application 2005/0269245 describes a method for producing diesel fuel from a gas oil feedstock.
- the method includes hydrotreatment, hydrofinishing, and catalytic dewaxing.
- the hydrofmishing and catalytic dewaxing treatments are performed using a counter-current flow of hydrogen.
- US 6,676,828 describes another method for producing a diesel fuel from a gas oil.
- the method involves at least two hydrotreatment steps, with a stripping and washing step between the hydrotreatment steps.
- the washing step includes injecting an additional hydrocarbon stream into the liquid product from the first hydrotreatment step.
- the additional hydrocarbon stream can be diesel, gasoline, or a light vacuum gas oil.
- a method for producing a diesel fuel product.
- the method includes passing a first hydrocarbon feedstock having a first initial cloud point to a hydrotreatment zone and hydrotreating the feedstock under effective hydrotreatment conditions to form a hydrotreated product having a sulfur content of 15 wppm or less, the hydrotreatment zone having a hydrotreatment temperature and pressure.
- the hydrotreated product is then passed to a stripping zone, where the hydrotreated product is stripped to form a gaseous effluent and a liquid effluent.
- the liquid effluent is then passed to a catalytic dewaxing zone and dewaxed under effective catalytic dewaxing conditions to form a dewaxed product having a cloud point at least 10 0 C lower than the first initial cloud point, the catalytic dewaxing conditions including a first average catalytic dewaxing temperature that is at least 15 0 C less than the hydrotreatment temperature.
- the temperature of the catalytic dewaxing zone is lowered to a second catalytic dewaxing temperature that is at least 5 0 C less than the first catalytic dewaxing temperature.
- a second hydrocarbon feedstock having a second initial cloud point is then passed to the hydrotreatment zone and the feedstock is hydrotreated at the hydrotreatment temperature to form a second hydrotreated product having a sulfur content of 15 wppm or less.
- the second hydrotreated product is passed to the stripping zone and stripped to form a second gaseous effluent and a second liquid effluent.
- the second liquid effluent is then passed to the catalytic dewaxing zone and dewaxed at the second catalytic dewaxing temperature to form a second dewaxed product, the second dewaxed product having a cloud point at least 10 0 C lower than the second initial cloud point.
- Figure 1 depicts a reaction system suitable for performing a process according to the invention. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS
- the invention provides a process that retains benefits of the two-stage configuration but at reduced capital cost.
- the process makes use of a stripping high-temperature separator between the hydrotreatment and catalytic dewaxing stages within a reactor.
- the desulfurization reactor effluent is sent to the stripping high-temperature separator and stripped with make-up hydrogen to remove and separate dissolved ammonia and hydrogen sulfide in the desulfurized liquid.
- only one common recycle compressor is required to serve both the desulfurization and dewaxing reactors. Both the hydrotreatment and dewaxing stages are operated in a co-current manner.
- a high pressure stripper is not needed after the dewaxing stage, in part because make-up gas is used for the stripping stage between the hydrotreatment and dewaxing stages. Additionally, no reflux of product is needed from any of the process stages. More generally, an additional hydrocarbon stream does not need to be introduced into the effluent from the hydrotreatment stage prior to passing the effluent to the catalytic dewaxing stage.
- Still another advantage of various embodiments of the invention is the ability to independently control the temperatures of the hydrotreatment and dewaxing stages. This flexibility provides many benefits with regard to diesel fuel production. For example, by adjusting only the temperature of the dewaxing stage while maintaining the temperature of the hydrotreatment stage, diesel fuels matching various specifications can be produced from a single feedstock while maximizing the diesel fuel yield at each specification.
- the present process involves a first hydroprocessing zone, a first separation zone following the first hydroprocessing zone, and a second hydroprocessing zone.
- the first separation zone is operated at the pressure of the preceding hydroprocessing zone. There is no disengagement, i.e., depressurization between first and second hydroprocessing zones. After the second hydroprocessing zone, the feedstock may be disengaged.
- Diesel boiling range feedstreams suitable for use in the present invention boil within the range of about 215 0 F to about 800 0 F.
- the diesel boiling range feedstream has an initial boiling point of at least 250 0 F, or at least 300 0 F, or at least 350 0 F, or at least 400 0 F, or at least 451 0 F.
- the diesel boiling range feedstream has a final boiling point of 800 0 F or less, or 775°F or less, or 750 0 F or less.
- the diesel boiling range feedstream has a boiling range of from 451 0 F to about 800 0 F.
- the diesel boiling range feedstream also includes kerosene range compounds to provide a feedstream with a boiling range of from about 25O 0 F to about 800°F.
- These feedstreams can have a nitrogen content from about 50 to about 2000 wppm nitrogen, preferably about 50 to about 1500 wppm nitrogen, and more preferably about 75 to about 1000 wppm nitrogen.
- feedstreams suitable for use herein have a sulfur content from about 100 to about 40,000 wppm sulfur, preferably about 200 to about 30,000 wppm, and more preferably about 350 to about 25,000 wppm.
- the feedstreams suitable for use can include feedstreams derived from synthetic sources, such as Fischer-Tropsch hydrocarbons, or feedstreams derived from biocomponent sources, such as animal or vegetable oils, fats, or fatty acids.
- the primary purpose of hydrotreating is typically to reduce the sulfur, nitrogen, and aromatic content of a feed, and is not primarily concerned with boiling point conversion of the feed.
- Catalysts usually contain at least one of Group VIA and Group VIII metal on a support such as alumina or silica. Examples include Ni/Mo, Co/Mo and Ni/W catalysts.
- Hydrotreating conditions typically include temperatures of 315-425 0 C, pressures of 300-3000 psig, Liquid Hourly Space Velocities (LHSV) of 0.2-10 h "1 and hydrogen treat rates of 500- 10000 scf/bbl.
- the sulfur present in the diesel product must be below 15 wppm.
- Catalytic dewaxing relates to the removal and/or isomerization of long chain, paraffinic molecules from feeds. Hydrodewaxing can be accomplished by selective hydrocracking or by hydroisomerizing these long chain molecules. Hydrodewaxing catalysts are suitably molecular sieves such as crystalline aluminosilicates (zeolites) or silico-aluminophosphates (SAPOs), such as zeolite Beta.
- the molecular sieve can be a 10-ring sieve such as ZSM-5, ZSM-22, ZSM-23, ZSM-35, ZSM-48, SAPO-11, SAPO-41 and the like.
- These catalysts may also carry a metal hydrogenation component, preferably Group VIII metals, especially Group VIII noble metals.
- Hydrodewaxing conditions include temperatures of 280-380 0 C, pressures of 300-3000 psig, LHSV of 0.1-5.0 h "1 and treat gas rates of from 500-5000 scf/bbl.
- the dewaxing catalyst is selected to also provide additional desulfurization.
- the hydrotreating step can be used to reduce the sulfur in a feedstock to a first level, such as from about 12 wppm to about 25 wppm. Additional sulfur is then removed during the dewaxing step to guarantee that the sulfur level is below 15 wppm. By relaxing the sulfur requirement of the hydrotreatment step, the severity of conditions in the hydrotreatment step can be reduced, which allows for an improved yield.
- Suitable dewaxing catalysts can include bound molecular sieve catalysts containing ZSM-48, ZSM-23, zeolite Beta, and a Group VIII noble metal, such as Pt or Pd. Molecular sieves that are isostructural with ZSM-48, ZSM-23, or zeolite Beta, such as ZBM-30, EU-2, or EU-11, can also be used.
- Typical distillate feeds suitable for conversion into a diesel fuel product can have initial cloud points ranging from about -20 0 C to about 5°C.
- the catalytic dewaxing conditions can be selected to reduce the cloud point by at least about 10 0 C, or at least about 20 0 C, or at least about 30 0 C, or at least about 40 0 C, or at least about 50 0 C.
- the dewaxing temperature can be 15°C lower than the hydrotreatment temperature, or 20 0 C lower, or 25°C lower, or 30 0 C lower.
- the dewaxing temperature selected can also be influenced by the diesel fuel product specification that is being matched. Because the temperatures of the hydrotreatment and dewaxing steps can be separately controlled, it is feasible to adjust the dewaxing temperature to match a desired specification. For example, it may be desirable to make some diesel fuel at a first cloud point specification, and then a second batch of diesel fuel intended for different winter climate that has a corresponding change in the specified cloud point. Since the dewaxing temperature is not dictated by the hydrotreatment temperature, the dewaxing temperature for producing the diesel fuel at the first cloud point specification can be optimized.
- the dewaxing temperature can be increased by at least about 5°C, or at least about 10 0 C, or at least about 15°C.
- the dewaxing temperature can be decreased by at least about 5°C, or at least about 10 0 C, or at least about 15 0 C.
- the change in dewaxing temperature does not correspond to simply turning off the dewaxing stage.
- the decrease in the temperature of the dewaxing stage is less than 100 0 C. This modification of the dewaxing temperature allows for an improved yield at diesel product specifications with a less severe cloud point requirement, while still allowing for production of diesel fuels with lower cloud points when necessary.
- a common practice in the art is to disengage, i.e., depressurize between hydroprocessing steps.
- the reason for such disengagement is to strip the effluent from the first hydroprocessing step (or zone) before passing the effluent to a second hydroprocessing step.
- An interstage stripping zone is employed to remove gaseous contaminants created in the first hydroprocessing step such as H 2 S and NH 3 and may also be used to strip light (low boiling) products from the effluent. Such gaseous contaminants may adversely impact the performance of catalysts in the second hydroprocessing step or zone.
- High pressure separators are known in the art. They may include flash drums, pressure strippers which include pressure separators for separating liquids and gases at high temperatures, or combinations thereof. These units are designed to operate at high temperatures such as the temperature of the preceding hydroprocessing zone. High pressure strippers may operate in either the co-current or countercurrent mode with regard to the stripping gas.
- Fresh feed is fed through line 15 to hydrotreater 20 to produce a hydrotreated product, hydrogen sulfide, ammonia and light hydrocarbon gases.
- the hydrogen for the first hydroprocessing zone is provided from recycle apparatus 70 via line 35.
- the products from the hydrotreater are passed through to a first separation zone 30 which is a stripping separator operated at a temperature and pressure similar to the output temperature and pressure of the hydrotreater.
- the liquid hydrotreated product is stripped with make-up hydrogen gas that is passed to first separation zone 30 via line 25.
- Light hydrocarbons, hydrogen sulfide and ammonia are separated from the hydrotreated product and sent to a second separation zone 40.
- This separation zone can be a conventional separator at a cooler temperature.
- the gas phase products from second separation zone 40 are sent to recycle apparatus 70.
- the stripped hydrotreated product is sent to the second catalytic dewaxer 50.
- catalytic dewaxer 50 may be operated at a pressure similar to hydrotreater 20, although slightly higher or lower pressures are also acceptable.
- the catalytic dewaxer removes and/or modifies waxy paraffins from the hydrotreated product by selective hydrocracking, isomerization or some combination thereof.
- the hydrogen for catalytic dewaxer 50 is provided by the make-up hydrogen flow used in first separation zone 30 and additional hydrogen from the recycle apparatus.
- the resulting dewaxed product and any gases are then passed to separation zone 60.
- the separator that comprises separation zone 60 separates liquid product from gases.
- the liquid product (the dewaxed product) is passed through line 65 for use as a diesel fuel product.
- the gaseous product from separator 60 is passed to the same recycle loop used for the gas phase product from separator 40.
- a common recycle apparatus can be used for all hydrogen in the system.
- the temperatures of the hydrotreatment and dewaxing steps can be controlled independently. In particular, this allows the temperature of each reactor to be independently modified to achieve a desired specification. As a result, the reaction conditions can be readily modified in response to a change in product specification or a change in the type of available feedstock.
- the process of the invention could be used for production of diesel fuels intended for a variety of locations.
- the cloud point requirement for a diesel fuel varies significantly by month and region, as shown in the specification maps provided in ASTM D975 and/or regulations in other countries. It is most economic for a user to be able to vary the dewaxing severity to meet a specific cloud point requirement. For a given feedstock, the hydrotreatment severity will not need to change, as the sulfur specification is uniform.
- the process of the invention overcomes the above problem by allowing the hydrotreatment and dewaxing temperatures to be set separately. This allows a first, higher temperature to be selected for the hydrotreatment step.
- the temperature of the dewaxing step can then be set to be at least 10°C lower, or at least 15°C, or at least 20 0 C, or at least 25°C lower in order to match a desired cloud point specification.
- the higher temperature may be in the dewaxing step, in which case the temperature of the dewaxing step can be at least 1O 0 C higher, or at least 15°C, or at least 20 0 C, or at least 25°C higher in order to match a desired cloud point specification.
- the yield of diesel fuel from the process can be increased.
- temperatures herein refer to average temperatures. Average temperatures are used as the catalyst beds (or reaction stages) will typically have some variation in temperature from the top to the bottom of a catalyst bed/reaction stage.
- the process of the invention allows a further advantage in that multiple types of product specifications can be accommodated. For example, during the transition from summer to winter, it would be desirable to continue making summer type diesel for any locations which permit the fuel for as long as possible, as the yield is improved. However, other locations may switch earlier to a lower cloud point requirement.
- the process of the invention allows the dewaxing temperature to be varied in order to produce multiple diesel product types, thus maximizing yield while still meeting desired product specifications.
- the change in cloud point between locations can be at least 5°C, or at least 10 0 C, or at least 15°C, or at least 20 0 C.
- Another example of the process flexibility provided by the invention relates to the types of initial feedstocks available for use. Depending on the original source of the feedstock, it may be desirable to perform hydrotreatment at more or less severe conditions. For example, a Fischer-Tropsch type feed might require little processing, while a feed including biocomponent might require additional severity to meet the desired sulfur target. Alternatively, one mineral feed may be similar in overall profile to a second feed, except for a change in the sulfur or nitrogen content. The process according to the invention allows the hydrotreatment severity to be modified without harming the ability to meet a desired cloud point specification.
Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP08869977.2A EP2238219A4 (en) | 2007-12-31 | 2008-12-24 | Integrated two-stage desulfurization/dewaxing with stripping high-temperature separator |
AU2008347111A AU2008347111B2 (en) | 2007-12-31 | 2008-12-24 | Integrated two-stage desulfurization/dewaxing with stripping high-temperature separator |
CA2709975A CA2709975C (en) | 2007-12-31 | 2008-12-24 | Integrated two-stage desulfurization/dewaxing with stripping high-temperature separator |
CN2008801236442A CN101970608A (en) | 2007-12-31 | 2008-12-24 | Integrated two-stage desulfurization/dewaxing with stripping high-temperature separator |
JP2010540669A JP5783724B2 (en) | 2007-12-31 | 2008-12-24 | Integrated two-stage desulfurization / dewaxing using high temperature separator for stripping |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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US968907P | 2007-12-31 | 2007-12-31 | |
US61/009,689 | 2007-12-31 |
Publications (1)
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WO2009088454A1 true WO2009088454A1 (en) | 2009-07-16 |
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PCT/US2008/014053 WO2009088454A1 (en) | 2007-12-31 | 2008-12-24 | Integrated two-stage desulfurization/dewaxing with stripping high-temperature separator |
Country Status (7)
Country | Link |
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EP (1) | EP2238219A4 (en) |
JP (1) | JP5783724B2 (en) |
CN (2) | CN101970608A (en) |
AU (1) | AU2008347111B2 (en) |
CA (1) | CA2709975C (en) |
SG (1) | SG186668A1 (en) |
WO (1) | WO2009088454A1 (en) |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
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WO2011133829A1 (en) | 2010-04-23 | 2011-10-27 | Exxonmobil Research And Engineering Company | Low pressure production of low cloud point diesel |
WO2011143397A3 (en) * | 2010-05-14 | 2012-02-16 | Exxonmobil Research And Engineering Company | Hydroprocessing of pyrolysis oil and its use as a fuel |
WO2018004924A1 (en) * | 2016-06-29 | 2018-01-04 | Exxonmobil Research And Engineering Company | Production of low cloud point distillate fuels |
WO2022173422A1 (en) * | 2021-02-09 | 2022-08-18 | ExxonMobil Technology and Engineering Company | Renewable arctic diesel production |
RU2793029C1 (en) * | 2022-07-06 | 2023-03-28 | Мнушкин Игорь Анатольевич | Method for producing diesel fuel with low-temperature properties |
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IL164591A0 (en) | 2004-10-14 | 2005-12-18 | Hernia repair device |
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US20040232045A1 (en) * | 2003-02-18 | 2004-11-25 | Chevron U.S.A. Inc. | Process for producing premium fischer-tropsch diesel and lube base oils |
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- 2008-12-24 SG SG2012093092A patent/SG186668A1/en unknown
- 2008-12-24 CA CA2709975A patent/CA2709975C/en active Active
- 2008-12-24 CN CN2008801236442A patent/CN101970608A/en active Pending
- 2008-12-24 EP EP08869977.2A patent/EP2238219A4/en not_active Withdrawn
- 2008-12-24 CN CN201510378913.1A patent/CN105062546A/en active Pending
- 2008-12-24 JP JP2010540669A patent/JP5783724B2/en not_active Expired - Fee Related
- 2008-12-24 WO PCT/US2008/014053 patent/WO2009088454A1/en active Application Filing
- 2008-12-24 AU AU2008347111A patent/AU2008347111B2/en not_active Ceased
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Cited By (10)
Publication number | Priority date | Publication date | Assignee | Title |
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WO2011133829A1 (en) | 2010-04-23 | 2011-10-27 | Exxonmobil Research And Engineering Company | Low pressure production of low cloud point diesel |
US9290703B2 (en) | 2010-04-23 | 2016-03-22 | Exxonmobil Research And Engineering Company | Low pressure production of low cloud point diesel |
AU2011242608B2 (en) * | 2010-04-23 | 2016-10-20 | Exxonmobil Research And Engineering Company | Low pressure production of low cloud point diesel |
WO2011143397A3 (en) * | 2010-05-14 | 2012-02-16 | Exxonmobil Research And Engineering Company | Hydroprocessing of pyrolysis oil and its use as a fuel |
CN102884159A (en) * | 2010-05-14 | 2013-01-16 | 埃克森美孚研究工程公司 | Hydroprocessing of pyrolysis oil and its use as a fuel |
WO2018004924A1 (en) * | 2016-06-29 | 2018-01-04 | Exxonmobil Research And Engineering Company | Production of low cloud point distillate fuels |
US10208260B2 (en) | 2016-06-29 | 2019-02-19 | Exxonmobil Research And Engineering Company | Production of low cloud point distillate fuels |
CN109415637A (en) * | 2016-06-29 | 2019-03-01 | 埃克森美孚研究工程公司 | The production of low cloud point distillate fuel |
WO2022173422A1 (en) * | 2021-02-09 | 2022-08-18 | ExxonMobil Technology and Engineering Company | Renewable arctic diesel production |
RU2793029C1 (en) * | 2022-07-06 | 2023-03-28 | Мнушкин Игорь Анатольевич | Method for producing diesel fuel with low-temperature properties |
Also Published As
Publication number | Publication date |
---|---|
CN105062546A (en) | 2015-11-18 |
CN101970608A (en) | 2011-02-09 |
EP2238219A1 (en) | 2010-10-13 |
CA2709975A1 (en) | 2009-07-16 |
EP2238219A4 (en) | 2013-11-27 |
SG186668A1 (en) | 2013-01-30 |
AU2008347111B2 (en) | 2013-04-18 |
AU2008347111A1 (en) | 2009-07-16 |
CA2709975C (en) | 2016-10-11 |
JP2011508051A (en) | 2011-03-10 |
JP5783724B2 (en) | 2015-09-24 |
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