NL1019328C2 - Preparation of lubricants from Fischer-Tropsch syncrude. - Google Patents

Description

Preparation of lubricants from Fischer-Tropsch substance

This invention relates generally to the field of Fischer-Trospch synthesis and more particularly relates to an efficient process for preparing lubricants from Fischer-Tropsch syncrude.

The conversion of natural gas into marketable products requires a large amount of capital.

The Fischer-Tropsch synthesis, in which methane is converted into higher molecular weight hydrocarbons, is now considered one of the most economical processes. However, natural gas feed is often located in remote locations, where it is more expensive to build commercial factories than in industrialized countries. It is therefore desirable to invest as little capital as possible at remote locations. One way to keep costs down is to hydrotreat the Fischer-Tropsch products in commercial refineries that are far removed from the location where the Fischer-Tropsch synthesis is being conducted.

The products of the Fischer-Tropsch synthesis are mostly linear hydrocarbons that often include wax with a high melting point. A C5 + product stream that is solid at room temperature, which is commonly referred to as "syncrude," can be isolated. In the Mossgas plant in South Africa and the Shell 20 plant in Malaysia (both developed plants with low to medium capital costs), methane is converted into Fischer-Tropsch syncrude, which is refined locally into ready-to-sell salable products. The syncrude can be transported to commercial refineries for hydroprocessing, for example, by hydrocracking, hydroisomerization, and hydrotreatment, to provide products with the desired properties.

Means for transporting Fischer-Tropsch-obtained syncrude from a remote location to a commercial refinery are well known in the art (see, for example, U.S. Patent Nos. 5,968,991; 5945459; 5856261; 5856260 and 5863856). An approach was to isolate a C20-36 syn-30 crude and to transport this composition as a solid. A limitation of this approach is that it is difficult and expensive to transport solids, because it requires expensive forming, loading and unloading installations.

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Other approaches have focused on conveying syncrude, or a syncrude that is partially refined at the remote location to convert a portion of the linear hydrocarbons to isoparaffins and thus form a syncrude that is fluid near ambient temperature. An approach to conveying syncrude in the liquid state includes partial dewaxing of the syncrude to form a pumpable liquid (see, for example, U.S. Patent No. 5292989). However, this dewaxing may require the construction of installations that are expensive and difficult to operate at remote locations.

Another approach involves transporting the syncrude as molten wax. This method of transport does not require any forming, loading and unloading equipment required for the transport of solids, or the dewaxing equipment required for converting the syncrude into a product that is liquid at room temperature. A limitation of this approach is that Fischer-Tropsch syncrude includes a sufficient amount of volatile hydrocarbons that cause the syn-crude to exceed the usual vapor pressure specifications if the syncrude were shipped at a temperature at which it was melted.

Regardless of the method of transport, the costs of constructing factories for converting methane and transporting the syncrude are relatively high. It is therefore desirable to generate products that are valuable enough to justify the costs. The Fischer-Tropsch products are generally linear hydrocarbons that can be converted into a variety of commercial products, such as jet fuel, diesel fuel and basic lubricant products. Lubricant base products are the most valuable of these products. Therefore, it would be desirable to develop cost-efficient processes for converting natural gas into lubricant base products via Fischer-Tropsch synthesis. U.S. Pat. No. 4,965,475 describes a process for converting natural gas into Fischer-Tropsch wax, transporting the wax to a developed location (as a solid), and refining the wax into a lubricant base product. However, there are several commercial considerations associated with converting methane to lubricant base products that are not discussed in U.S. Patent No. 4,965,475.

The service life of the natural gas reserves must be taken into account. Gas stocks are usually classified as either dry gas or associated gas. Dry gas is gas from a reservoir that usually does not contain crude oil or natural gas condensate. Associated gas is gas from a reservoir that also contains crude oil. The gas reserves can quickly become exhausted compared to the capital write-off time for the gas processing plant. This applies in particular to associated gas, which usually has a half-life of 5-10 years. If the factories are built on site to process the gas, the gas field can become exhausted before the invested capital is recouped with the installation. Furthermore, the current Fischer-Tropsch plants are usually small (about 10,000 BPD) and with most cost-efficient lubricant plants much more power is used because the production costs decrease as the plant gets larger. Also, lubricant base products obtained from Fischer-Tropsch syncrudes have different physical and chemical properties than current lubricant base products.

It would be desirable to develop processes that are economically viable given the short lifespan of conventional gas supplies that can handle more than 10,000 BPD feed, preferably more than 25,000 BPD feed and most preferably more than 50,000 BPD feed and where the production over time can be increased with a minimum of additional capital investments. The present invention provides such a process.

US patent 5866751 relates to a method for transporting a Fischer-Tropsch product in a solid, non-volatile form. Hereby it is required that the long chain hydrocarbons of the Fischer-Tropsch process (i.e., a molten wax) be cooled to form a solid wax. When arrived at the desired location, the solid wax must then be heated again to return it to the molten state so that processing is possible. The method according to U.S. Patent No. 5,666,751 is therefore not efficient with regard to energy consumption.

A process for the preparation of a lubricant base stock and the lubricant base stock produced according to the process are described. The method comprises converting a light hydrocarbon feed into syngas, converting the syngas into hydrocarbon products via Fischer-Tropsch synthesis and isolating a fraction containing substantially 650 ° F (343.33 ° C) preferably substantially C5-20 hydrocarbons) and a fraction containing substantially 650 ° F + (343.33 ° C +), either derived from or, preferably, directly from the 4

Fischer-Tropsch product stream, The fraction comprising substantially C5.20 hydrocarbons (and the fraction of essentially C5.20) is a fraction containing at least 80% by weight, preferably at least 85% by weight and more preferably comprises more than 90% by weight of products boiling in the range between 50 and 700 ° F. The fraction containing 650 ° F (343.33 ° C) can be converted into distillate fuels, either at the location where the Fischer-Tropsch synthesis takes place or at another location. The fraction containing 650 ° F + (343.33 ° C +) is converted into lubricant base products, preferably at a location different from where Fischer-Tropsch synthesis takes place via transport to and reception at the other location. The fractions can be converted at the same location or at different locations into distillate fuels and lubricant base products. Fractions from multiple places can be combined for conversion.

The fractions are preferably transported according to the methods described in the co-pending patent application entitled "Method for Transporting Fischer-Tropsch Products", filed simultaneously therewith and to be incorporated herein in its entirety. In particular, when transported for hydroprocessing, the fractions have actual vapor pressures at the transport temperature that are lower than about 15 psia, preferably lower than 11 psia. The fractions are both preferably at least partially liquid at the temperature of the transport. The fractions can be transported using all commonly used means of transport, including maritime tankers, railway carriages, pipelines, trucks, ships and combinations thereof. A preferred means of transport is a maritime tanker and, more preferably, each transportable fraction is transported either in a separate maritime tanker or in separate zones in the same tanker. In the case of transport by train, truck or ship, each fraction is preferably transported either in a separate wagon, truck or ship or in separate zones for each fraction in the same wagon, truck or ship.

The conversion of the fraction containing 650 ° C + into lubricant base products comprises dewaxing, which may include catalytic dewaxing, solvent dewaxing or combinations thereof. The conversion of both fractions to end products can also include, for example, hydrogenation steps, hydroisomerization steps, hydrocracking steps and combinations thereof.

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A C1.2 fraction can also be isolated from the Fischer-Tropsch synthesis and recycled upstream of a syngas generation process, flared, used to produce hydrogen and / or used as fuel. A fraction enriched in C3 comprising more than 5% by weight of C3, preferably more than 20% by weight of C3 and most preferably more than 40% by weight of C3 can also be obtained. This fraction can be recycled upstream of a syngas generation process, flared, used as fuel, transported in pressurized tankers and / or transported in refrigerated tankers.

In one embodiment, petroleum products such as crude oil fractions with boiling points in the 650 ° F (343.33 ° C) or 650 ° F + (343.33 ° C +) ranges can be mixed with the corresponding 650 ° F ( 343.33 ° C +) or 650 ° F + (343.33 ° C +) containing fractions. The mixing can take place at any location - the remote Fischer-Tropsch location, the location of the lubricant production, the location of the distillation refinery or another location.

In preferred embodiments of a process and business process, at least some parts of the syngas generator, the Fischer-Tropsch synthesis reactor, and / or the equipment used to isolate the 650 ° F (343.33) ° C-) or 650 ° F + (343.33 ° C +) containing fractions are disassembled, transported to another location and applied to the other location for carrying out the process described herein. Ideally, the parts can either be reassembled at the other location or combined with other parts and assembled into a syngas generator, a Fischer-Tropsch synthesis reactor and / or equipment for isolating different product fractions. This embodiment is commercially relevant when considering the commercial life of remote gas sources.

Preferred embodiments are now described as non-limiting illustrations of the claimed invention. A process for preparing a lubricant base product and the lubricant base product produced with the process are described. The process involves converting a light hydrocarbon feed into syngas, converting the syngas into hydrocarbon products via Fischer-Tropsch synthesis, and isolating a fraction containing substantially 650 ° F (343.33 ° C). preferably substantially C5.20 hydrocarbons) and a fraction containing substantially 650 ° F + (343.33 ° C +), either derived from or, preferably, directly from the Fischer-Tropsch product stream. The 650 ° F (343.33 ° C) containing fraction can be converted to distillate fuels, either at the location where the Fischer-Tropsch synthesis takes place or at another location. The fraction containing 650 ° F + 5 (343.33 ° C +) is transported, received and converted into lubricant base products at a location different from where Fischer-Tropsch synthesis takes place. The fractions can be converted at the same location or at different locations into distillate fuels and lubricant base products. Fractions from multiple places can be combined for conversion.

The following definitions are helpful in understanding the compositions and methods described herein.

Linear hydrocarbon: the class of compounds that includes linear paraffins, linear olefins (internal and alpha), linear alcohols and linear acids. A substantially linear hydrocarbon fraction, i.e. product, contains more than about 50% by weight of linear hydrocarbons. Members of this class of compounds higher than C20, either individually or in mixtures, are usually solid or waxy at ambient temperature (20 ° C). The content of linear paraffins in materials lighter than about C20 can be determined by, for example, gas chromatography. Because heavy linear paraffins are mostly solid materials, the content of linear hydrocarbons heavier than about C20 can be determined by measuring the wax precipitated in the presence of methyl ethyl ketone and toluene. An acceptable method comprises the following: a 300 g portion of a sample is dissolved in 1200 ml of a 1: 1 toluene MEK solvent. Heating may be necessary to achieve complete dissolution. The solution is then cooled to -15 to -20 ° F overnight to crystallize the wax. The wax crystals formed are filtered off and recovered. The filtrate is subjected to vacuum distillation to separate the toluene MEK solvent from the dewaxed oil. Solvent trapped in the wax is removed by heating the wax on a hotplate, blowing nitrogen over the surface. The weights of the oil and wax recovered are divided by the original weight of the sample to obtain the percentage of oil and wax.

Transport temperature: For materials that are liquid at ambient temperature (20 ° C) or lower, the temperature of transport is 20 ° C.

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For materials that are solid at conventional ambient temperature, the temperature of transport is 5 ° C higher than the pour point, preferably 10 ° C higher than the pour point, and most preferably 20 ° C higher than the pour point, as measured according to ASTM D- 97.

5 Remote location: A remote location is a location that is far away from a refinery or market and where the costs of construction are higher than the costs of construction at the refinery or market. In quantitative terms, the distance between the remote location and the refinery or market (the distance for transportation) is at least 100 miles, preferably more than 500 miles and most preferably more than 10 1000 miles.

Transport in liquid form: this means that at least a part of the product is liquid, while the rest can be solid. The portion that is liquid is at least 10%, preferably more than 25% and most preferably more than 50%. It is within the scope of the processes described herein that wax-like products are completely liquid (or are at least a pumpable suspension) upon initial loading into a transport vessel and upon unloading of the vessel, but at least a portion can solidify during transport when the product cools down. This solid can easily be melted at the receiving end, for example by using steam heaters. However, it is highly desirable that the compositions be pumpable when loaded and unloaded, and that the product does not become completely solid during transportation.

Light hydrocarbon feed: these feeds may include methane, ethane, propane, butane and mixtures thereof. In addition, carbon dioxide, carbon monoxide, ethylene, propylene, and butenes may be present.

Syncrude: a mixture obtained from a Fischer-Tropsch process that does not meet all specifications for a ready-to-sell product, such as jet fuel, diesel fuel, lubricant base product, fully refined wax, gasoline and the like, without further processing. Although prior art syncrude has been described as a C5 + containing material, syncrude, as used herein, refers to a stream containing 650 ° F + (343.33 ° C +), which preferably comprises a relatively large amount of C36 + hydrocarbons (ie preferably more than 10% by weight, more preferably more than 20% by weight and most preferably more than 30% by weight). The C36 + hydrocarbons form δ lubricant base products with a relatively high viscosity, i.e. clear products.

Mode of transport: the mode of transport may vary, but preferably includes the use of a closed vessel with no significant exposure to air during transport. At the temperature at which the compositions are transported, the pressure in the vessel should not exceed about 14.9 psia.

Maritime tanker: a ship that is used for transporting hydrocarbons, usually but not limited to, crude oil, waxes and refined products.

Direct liquid product from a Fischer-Tropsch reactor: the direct liquid product is a liquid effluent from a Fischer-Tropsch reactor at reactor conditions. It usually solidifies on cooling to 20 ° C.

Direct vaporous product from a Fischer-Tropsch reactor: The direct vaporous product is a vaporous effluent from a Fischer-Tropsch reactor at reactor conditions.

650 ° F + (343.33 ° C +) containing product stream (eg fraction): a product stream that contains more than 25% by weight of 650 ° F + (343.33 ° C +) material, preferably more than 50% by weight of 650 ° F + ( 343.33 ° C +) material and most preferably more than 75% by weight of 650 ° F + (343.33 ° C +) material, as determined by ASTM D2887 or other suitable methods. The product stream containing 650 ° F (343.33 ° C) is defined accordingly.

Paraffin: a hydrocarbon with the formula C „H2n + 2 ·

Alkene: a hydrocarbon with at least a carbon-carbon double bond.

Oxygenation product: a hydrocarbonaceous compound that contains at least one oxygen atom.

Distillate fuel: a material containing hydrocarbons with boiling points between approximately 60 and 1100 ° F. The term "distillate" means that conventional fuels of this type can be generated from vapor overhead streams from the distillation of crude petroleum. In contrast, residual fuels cannot be generated from vapor overhead streams by distilling crude petroleum, and are then a non-vaporizable residual portion. Within the broad category of distillate fuels there are specific fuels, including: naphtha, jet fuel, diesel fuel, kerosene, aviation gasoline, fuel oil and mixtures thereof.

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Diesel fuel: a material that is suitable for use in diesel engines and that meets at least one of the following specifications: • ASTM D 975 - "Standard Specification for Diesel Fuel Oils" • European quality CEN 90 5 · Japanese fuel standards JIS K 2204 • the guidelines from the United States National Conference on Weights and Measures (NCWM) from 1997 for first quality diesel fuel • the recommended guidelines from the United States Engine Manufacturers Association for first quality diesel fuel (FQP-1A) 10 Aircraft fuel: a material that is suitable for use in aircraft turbine engines or other applications that meets at least one of the following specifications: • ASTM D1655 • DEF STAN 91-91 / 3 (THIRD 2494), TURBINE FUEL, AVIATION, 15 KEROSINE TYPE, JET Al, NATO CODE: F-35 • International Air Transportation Association (IATA) "Guidance Material for Aviation Turbine Fuels Specifications", fourth edition, March 2000

Gasoline: a material suitable for use in internal combustion spark-ignition engines for cars and small trucks (engine gasoline) and 20 in aircraft with piston engines (aviation gasoline) that meets the current version of at least one of the following specifications:

Lubricant base product: a material that meets the definition in API 1509.

Fully refined wax: fully refined wax meets FDA requirements for food quality as defined in Title 21 of the Code of Federal Regulations, 25 sections 178.3710 and 172.886. Fully refined waxes have very little odor (ASTM D188), an oil content lower than 0.5% (ASTM D721) and a Saybolt color of +25 to +30 (ASTM D1 56).

Natural gas is an example of a light hydrocarbon feed. In addition to methane, natural gas comprises a few heavier hydrocarbons (in particular C2-5 paraffins) and other contaminants, e.g. mercaptans and other sulfur-containing compounds, carbon dioxide, nitrogen, helium, water and acid non-hydrocarbon gases. Natural gas fields also usually contain a significant amount of C5 + material, which is liquid at ambient conditions.

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The methane, and optionally ethane and / or other hydrocarbons, can be isolated and used to generate syngas. Various other contaminants can easily be separated. Inert contaminants such as nitrogen and helium can be tolerated. The methane in natural gas can be isolated, for example in a demethanizer, and can then be desulphurized and fed to a syngas generator.

Methane (and / or ethane and heavier hydrocarbons) can be passed through a conventional syngas generator to provide synthesis gas. Typically, synthesis gas contains hydrogen and carbon monoxide, and may include smaller amounts of carbon dioxide, water, unreacted light hydrocarbon feed, and / or various other impurities. The presence of sulfur, nitrogen, halogen, selenium, phosphorus and arsenic contaminants in the syngas is undesirable. Therefore, it is preferable to remove sulfur and other contaminants from the feed before the Fischer-Tropsch chemistry or other hydrocarbon synthesis is performed. Means for removing these contaminants are known to those skilled in the art. For example, ZnO protection beds are preferred for removing sulfur impurities. Means for removing other contaminants are known to those skilled in the art.

The Fischer-Tropsch reaction can be carried out in a fixed bed reactor, in a reactor with a suspension bed or in a fluid bed reactor. The conditions of the Fischer-Tropsch reaction may include the use of a reaction temperature between 190 ° C and 340 ° C, the actual reaction temperature being largely determined by the configuration of the reactor. Thus, if a fluidized bed reactor is used, the reaction temperature is preferably between 300 ° C and 340 ° C; if a fixed bed reactor is used, the reaction temperature is preferably between 200 ° C and 250 ° C; and if a slurry bed reactor is used, the reaction temperature is preferably between 190 ° C and 270 ° C.

A supply pressure of synthesis gas to the Fischer-Tropsch reactor between 1 and 50 bar, preferably between 15 and 50 bar, can be applied. The synthesis gas can have a H 2: CO mole ratio, in the fresh feed, of 1.5: 1 to 2.5: 1, preferably 1.8: 1 to 2.2: 1. The synthesis gas usually comprises 0.1 wppm of sulfur or less. Optionally, a gas recycle can be used in the reaction step, and the ratio of the gas recycling rate to the feed rate of fresh synthesis gas, on a molar basis, can be between 1: 1 and 3: 1, preferably between 1.5: 1 and 2.5: 1. A space velocity, in m3 (kg of catalyst) * 1 hour -1, from 1 to 20, preferably 8 to 12, can be used in the reaction step.

In principle, an iron-based, cobalt-based or iron-cobalt-based Fischer-Tropsch catalyst can be used during the Fischer-Tropsch reaction step, although Fischer-Tropsch catalysts operated with high chain growth probabilities (ie alpha values of 0.8 or higher, preferably 0.9 or higher and more preferably 0.925 or higher) are preferred. The reaction conditions are preferably chosen such that the formation of methane is minimized. As a result, product streams are obtained which are essentially wax and comprise heavy products, i.e. largely paraffinic C20 + linear hydrocarbons.

The iron-based Fischer-Tropsch catalyst can include iron and / or iron oxides that have been precipitated or fused. However, iron and / or iron oxides that have been sintered, cemented or impregnated on a suitable support can also be used. The iron should be reduced to metallic Fe for Fischer-Tropsch synthesis. The iron-based catalyst may contain various amounts of promoters, the role of which may be to change the activity, stability and / or selectivity of the final catalyst.

Preferred promoters are those that affect the surface of the reducing iron ("structural promoters") and these include oxides or metals of Mn, Ti, Mg, Cr, Ca, Si, Al or Cu or combinations thereof.

The products of Fischer-Tropsch reactions generally comprise a gaseous reaction product and a liquid reaction product. The gaseous reaction product 25 comprises hydrocarbons boiling at a temperature below about 650 ° F (e.g., methane up to middle distillates). The liquid reaction product comprises hydrocarbons boiling at a temperature higher than about 650 ° F (e.g., vacuum gas oil up to and including heavy paraffins).

When the Fischer-Tropsch unit is operated in the slurry mode, with a liquid product phase usually present in the reactor under the reaction conditions, both the direct vaporous and the direct liquid products can be produced. The direct liquid product can be a product containing 650 ° F + (343.33 ° C +). Similarly, the direct 12 vaporous product can be cooled so that a product containing 650 ° F + (343.3 ° C +) is condensed. In addition, the products of different types of Fischer-Tropsch units can be combined and separated, for example by distillation, whereby 650 ° F + (343.33 ° C +) and 650 ° F- (343.33 ° C-) products are obtained .

The product of a temperature below 650 ° F can be separated into a tail gas fraction and a condensate fraction, ie about C5-C20 normal paraffins and hydrocarbons with a higher boiling point, using for example a high pressure and / or low temperature vapor-liquid separator or low-pressure separators or a combination of detectors. The fraction boiling at a temperature higher than about 650 ° F contains C20-C50 linear paraffins with relatively small amounts of branched paraffins with a higher boiling point.

A Ci.2 fraction can also be isolated and recycled upstream of a syngas generation process, flared, used to produce hydrogen and / or used as a fuel. A fraction enriched in C3 comprising more than 5% by weight of C3, preferably more than 20% by weight of C3 and most preferably more than 40% by weight of C3 can also be obtained. This fraction can be recycled upstream of a syngas generation process, flared, used as fuel, transported in pressurized tankers and / or transported in refrigerated tankers.

An LPG fraction can also be isolated. The LPG fractions preferably comprise mainly C3.5 hydrocarbons and, in general, include mainly propane, n-butane and isobutane. They may also contain small amounts of pentanes and, less preferably, C 3.5 olefins. In a preferred embodiment, the LPG is a primary propane-rich and / or butane-rich product stream such as the streams known in the art. It is suitable for all possible final applications, such as, for example, as an alternative source of fuel for automobiles. Most preferably, the composition falls within the strict specifications for LPG product streams in a conventional application of LPG fuel and in the field of alternative fuels. The LPG fraction can include a substantial amount of olefins and / or oxygenation products, which can be hydrotreated to form paraffins. In a preferred LPG product, the amount of ethane is less than about five percent by volume of the mixture, the amount of propylene is less than about a volume percent of the propane, and the amount of butene is less than about a volume percent of the butane. The C5 + hydrocarbons are preferably less than about twenty five volume percent of the mixture. The sulfur content is preferably lower than about 150 ppm.

The LPG fraction can be transported at a temperature at which the volatility does not exceed the commercial specifications (i.e., lower than about 15 psia, preferably lower than about 11 psia). LPG generally has a pressure of about 120 psia at ambient temperatures, so it must be cooled if it is transported so that it meets these specifications unless it is transported under pressure in commercial means of transport that do not have these specifications.

In one embodiment, separate propane and butane streams are isolated instead of LPG. This can be done, for example, by passing a mixture comprising Cm hydrocarbons through a demethanizer, a de-ethanizer, and a depropanizer.

Preferably, volatile hydrocarbons which would increase the pressure to higher than 15 psia, more preferably higher than 11 psia, at the transport temperature, are all removed from all fractions to be transported.

When the gaseous reaction product of the Fischer-Tropsch reaction step is cooled and different fractions are collected, the first fractions that are collected have higher average molecular weights than subsequent fractions. A C 14.20 fraction can be obtained, and combined with the liquid reaction products to form a C14 + syncrude, by isolating the fraction while cooling the gaseous reaction products. A G14-20 fraction can also be obtained by distilling the C5.13 hydrocarbons from the C14 + products after the mean distillate effect has been collected.

The vapor pressure of the composition can be measured by the techniques known to the person skilled in the art at the temperature of the transport. If the vapor pressure of the composition exceeds specifications at the transport temperature, lower boiling hydrocarbons can be removed from the composition, for example via vacuum distillation or other suitable means known to those skilled in the art.

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The 650 ° F + (343.33 ° C +) and the 650 ° F (343.33 ° C) containing fractions, products obtained from these fractions and mixtures of these and other fractions can be isolated and transported, e.g. to commercial refining lines for additional processing, such as solvent dewaxing, catalytic dewaxing, hydrotreating, hydroisomerization of light paraffins and / or hydrocracking. At least one of the products is a syncrude product. The products can be transported using commonly used means of transport, including maritime tankers, railroad cars, pipelines, trucks, ships and combinations thereof. A preferred means of transport is a maritime tanker and more preferably, each transportable product is transported either in a separate maritime tanker or in separate zones in the same tanker. With transport by rail, truck or ship, each transportable product is preferably transported either in a separate wagon, truck or ship, or in separate zones for each transportable product in the same wagon, truck or ship. It must be possible to control the temperature at each zone in a means of transport or at each individual means of transport, so that each product can meet the desired pressure specifications. Therefore, with the means of transport, the LPG fractions being transported must be able to be cooled (or else elevated pressures must be safe to handle), all fractions containing 650 ° F (343.33 ° C) must be able to be kept at or around room temperature and the fractions containing 650 ° F + (343.33 ° C +) can be kept at a temperature at which they are melted, at least while the product is being pumped in or out of the means of transport, the temperature generally being at least 5 ° C is higher than the pour point, preferably 10 ° C is higher than the pour point. If the materials are liquid at ambient temperature, the transport temperature is preferably around ambient temperature. The temperature of the transport is preferably not higher than 250 ° C, more preferably lower than 200 ° C and most preferably lower than 150 ° C.

The fractions containing 650 ° F + (343.33 ° C +) are dewaxed in a conventional solvent dewaxing step to remove high molecular weight n-paraffins. This dewaxing can take place before or after the fractions are transported to commercial refineries, but this is preferably done after transport because this reduces the construction of installations at remote locations. The recovered dewaxed product, or dewaxed oil, can be fractionated under vacuum to produce fractions of paraffinic lubricant base products with different grades of quality, or can be directly mixed with other lubricant base product fractions.

Solvent dewaxing for the preparation of lubricant base products has been used for more than 70 years and is described, for example, in Chemical Technology of Petroleum, third edition, William Gruse and Donald Stevens, McGraw-Hill Book Company, Ine., New York, 1960, pages 567 to 570. The basic process comprises • mixing a waxy hydrocarbon stream with a solvent, usually comprising a ketone (such as methyl ethyl ketone or methyl isobutyl ketone) and an aromatic compound (such as toluene), • cooling the mixture so that wax crystals precipitate, separating the wax by filtration, usually using rotary drum filters, recovering the solvent from the wax and the dewaxed oil filtrate.

Refinements have been made to solvent dewaxing since its inception. For example, the DILCHILL® dewaxing process of Exxon includes cooling a wax-like oil in an extended stirred vessel, preferably a vertical tower, with a precooled solvent in which at least a portion of the oil dissolves while promoting the precipitation of the wax . The wax-like oil is supplied to the extended cascading cooling zone or tower at a temperature higher than cloud point. Cold dewaxing solvent is supplied in increasing amount to the cooling zone along a plurality of points or steps while maintaining a high degree of stirring to effect almost instant mixing of the solvent and the wax / oil mixture. while passing through the cooling zone, precipitating at least a portion of the wax in the oil. DILCHILL® dewaxing is discussed in more detail in U.S. Patent Nos. 4477333, 3773650 and 3775288. Texaco has also developed refinements to the process. For example, US Pat. No. 4898674 30 describes why it is important to control the ratio of methyl ethyl ketone (MEK) to toluene and why it is necessary to be able to adjust this ratio because it allows the use of optimum concentrations for processing different basic products is possible. Usually a ratio of 0.7: 1 to 1: 1 16 can be used in the processing of clear products; and a ratio of 1.2: 1 to about 2: 1 can be used in processing light products.

The solvent dewaxed fraction may optionally be subjected to catalytic dewaxing, as described in more detail below.

The fractions containing 650 ° F + (343.33 ° C +) can also be dewaxed in a catalytic dewaxing step to remove high molecular weight n-paraffins, in addition to or instead of solvent dewaxing. This dewaxing can also take place before or after the fractions are transported to commercial refineries, but this is preferably done after transport because this reduces the construction of installations at remote locations.

Catalytic dewaxing consists of two main classes (conventional hydro dewaxing and hydroisomeristic dewaxing) and hydroisomeristic dewaxing can be further subdivided into partial and complete hydroisomerization dewaxing. All classes include passing a mixture of a wax-like hydrocarbon stream and hydrogen over a catalyst containing an acidic component to convert the normal and slightly branched isoparaffins in the feed into other non-wax-like species and thereby producing a lubricant base product with an acceptable pour point. Typical conditions for all classes include temperatures of about 400 to 800 ° F, pressures of about 200 to 3000 psig, and space velocities of about 0.2 to 5 hours. The method selected for dewaxing a feed usually depends on the quality of the product and the wash content of the feed, with conventional hydrodewashing generally being preferred for low wash feed. The dewaxing process can be influenced by the choice of the catalyst. The general topic is discussed by Avilino Sequeira, in Lubricant Base Stock and Wax Processing, Marcel Dekker, Ine., Pages 194-223. The determination of the class of dewaxing catalysts for conventional hydro-dewaxing, partial hydroisomerization dewaxing and full hydroisomerization dewaxing can be done by applying the n-hexadecane isomerization test, as described by Santilli et al. In U.S. Pat. 5282958. When measured at a 96% n-hexadecane conversion under the conditions described by Santilli et al., conventional hydro-dewaxing catalysts show a selectivity for isomerized hexadecans of less than 10%, hydroisomerization-dewaxing catalysts show a selectivity for iso 17 mercerized hexadecans of more than or equal to 10%, partial hydroisomerization dewaxing catalysts have a selectivity for isomerized hexadecans from more than 10% to less than 40% and complete hydroisomerization dewaxing catalysts have a selectivity for isomerized hexadecans of more than than or equal to 40%, preferably more than 60% and most preferably more than 80%.

Conventional hydro-dewaxing is defined for the purposes of this document as a catalytic dewaxing process using a conventional hydro-dewaxing catalyst. In conventional hydro-dewaxing, the pour point is lowered by selective cracking of the wax molecules, usually to smaller paraffins that boil between propane and about octane. Because the wax in this technique is converted into less valuable by-products, this technique is essentially useful for dewaxing oils that do not contain a large amount of wax. Wax-like oils of this type are often found in crude oil petroleum distillate with an average wax content (Arabian, North Slope, etc.). Catalysts useful for conventional hydro-dewaxing are usually 12-ring zeolites and 10-ring zeolites. Zeolites from this class include ZSM-5, ZSM-11, ZSM-22, ZSM-23, ZSM-35 and mordenite. Conventional hydro-dewaxing catalysts favor cracking in comparison with another method for converting paraffins. This is demonstrated by using the n-hexadecane isomerization test of San-20 tilli et al., With conventional hydro-dewaxing catalysts showing a selectivity for isomerized hexadecane products of less than 10%. In addition to the zeolites, metals can be added to the catalyst, primarily for reducing fouling. Representative process conditions, yields and product properties for conventional hydro-dewaxing are described, for example, in U.S. Patent Nos. 4176050 to Chen et al., 4181598 to Gillespie et al., 4222855 to Pelrine et al., 4229282 to Peters et al., 4211635 to Chen. , by Sequeira in the section entitled "The Mobil Lube Dewaxing Process", pages 198-204 and references therein, JD Hargrove, G.J. Elkes and A.H. Richardson, Oil and Gas J., p. 103, January 15, 1979; wherein the contents of each as a whole are incorporated herein by reference.

For the purposes of this document, hydroisomerization dewaxing is defined as a catalytic dewaxing process using a hydroisomerization dewaxing catalyst. In hydroisomerization dewaxing, at least a portion of the wax is converted by isomerization into non-wax-like isoparaffins, while at the same time reducing cracking conversion. When conventional hydro-dewaxing and hydroisomerization dewaxing are compared to the same feed, the conversion of wax to non-wax-like isoparaffins during hydroisomerization dewaxing gives the benefits of reducing the yield of less valuable by-products, increasing the yield. lubricating oil and producing an oil with a higher VI and more oxidation and a higher thermal stability. Hydrotomerization dewaxing uses a dual functionality catalyst consisting of an acid component and a metal component. Both components are required for carrying out the isomerization reaction. Common metal components are platinum or palladium, with platinum being the most commonly used. The choice of metal and the amount of metal in the catalyst are sufficient to achieve more than 10% isomerized hexadecane products in the test described by Santilli et al. If the selectivity to hexadecane isomers after Santilli's test is greater than 40 %, then the catalyst is a complete hydroisomerization dewaxing catalyst. Because in hydroisomerization dewaxing, wax is converted to isoparaffins boiling in the lubricant base product range, this is useful for dewaxing oils containing a large amount of wax. Wax-like oils of this type are obtained from slag waxes from solvent dewaxing processes, and high-oil crude distillates (Minas, Altamont, etc.) and Fischer-Tropsch process products.

For the purposes of this document, partial hydroisomerization dewaxing is defined as a catalytic dewaxing process using a partial hydroisomerization dewaxing catalyst. In partial hydroisomerization dewaxing, a portion of the wax is isomerized to isoparaffins using catalysts that can selectively isomerize paraffins, but only if the wax conversion is kept at relatively low values (usually below 50%). At higher conversions, the conversion of wax by cracking becomes significant and the loss of yield of the lubricant base product becomes uneconomical. The acid catalyst components useful for partial hydroisomerization dewaxing include amorphous silica-alumina, fluorinated alumina, and 12-ring zeolites (such as Beta, Y-zelite, L-zeolite). Because the conversion of wax is incomplete, the partial hydroisomerization dewaxing 19 must be supplemented with an additional dewaxing technique, usually solvent dewaxing, full hydroisomerization dewaxing or conventional hydro-dewaxing, in order to obtain a lubricant base product with an acceptable pour point (lower than about + 10 ° F or -12 ° C). The wax recovered from a solvent dewaxing operation after partial hydroisomerization dewaxing can be recycled to the partial hydroisomerization dewaxing step. Representative process conditions, yields and product properties for partial hydroisomerization dewaxing are described, for example, in U.S. Patent Nos. 50,495,336 to Belussi et al .; 4943672 from Hamner et al. And EP 0582347 from Perego et 10 al., EP 0668342 from Eilers et al., PCT WO 96/26993 from Apelian et al .; PCT WO 96/13563 to Apelian et al .; wherein the contents of each as a whole are incorporated herein by reference.

For the purposes of this document, complete hydroisomerization dewaxing is defined as a catalytic dewaxing process using a full hydroisomer dewaxing catalyst. In complete hydroisomerization dewaxing, complete hydroisomerization dewaxing catalysts are used with which high conversion levels of the wax can be achieved while maintaining acceptable isomerization selectivities. Since the conversion of the wax can be complete, or at least very high, this process usually does not need to be combined with additional dewaxing processes to produce a lubricant base product with an acceptable pour point. Representative process conditions, yields and product properties for complete hydroisomerization dewaxing are described, for example, in U.S. Patent Nos. 5,113,538 to Miller, 5,224,666 to Miller, 5,228,958 to Santilli et al., 50,82986 to Miller, 5,723,716 to Bmades et al., 25 with the contents of each as a whole must be regarded as inserted herein.

With solvent dewaxing and catalytic dewaxing, trace amounts of washing may still remain. The presence of unwanted wax can be detected by visual inspection or by applying analytical techniques, such as, for example, light scattering turbidity measurement, as described in U.S. Pat. No. 4,627,901.

Various methods have been developed for removing these trace amounts of impurities. For example, U.S. Pat. No. 4,950,382 describes the use of adsorbents for removing wax. U.S. Pat. Nos. 4,702,217 and 4,820,400 describe the performance of electrophoresis on the hydrocarbons during solvent dewaxing.

The contents of each of these patents are hereby incorporated by reference herein in its entirety.

The fractions described above may optionally be combined with hydrocarbons from other streams, although such hydrocarbons should not increase the pressure of the composition at the transport temperature by more than about 14.7 psia. For example, LPG can be supplemented with LPG obtained from a natural gas field. Both fractions can be combined with a corresponding fraction obtained from the fractional distillation of crude oil or products obtained therefrom. For example, the 650 ° F + (343.33 ° C +) containing fraction can be combined with waxy crude oils and / or slag waxes from petroleum dewaxing and dewaxing operations.

The fractions containing 650 ° F + (343.33 ° C +) and 650 ° F- (343.33 ° C-), products obtained from these fractions and mixtures of these and other fractions can be subjected to hydroprocessing conditions. The hydroprocessing conditions include, for example, hydrotreatment, hydroisomerization dewaxing and / or hydrocracking. Alkenes and oxygenation products are hydrotreated to form paraffins. ParafFines in the C4.20 range, preferably the C4.6 range, are subjected to light paraffin hydroisomerization conditions to form isoparaffins. Hydrocarbons with chain lengths greater than a desired value, such as, for example, C40, are hydrocracked. For example, a C5.20 product stream comprising a mixture of paraffins and isoparaffins can be isolated from the fractions containing 650 ° F + and / or 650 ° F (343.33 ° C), although the 650 ° F + ( 343.33 ° C +) containing fractions preferably being substantially converted into lubricant base products.

As used herein, "hydrotreating" and "hydrotreating" have their usual meaning and describe processes known to those skilled in the art. Hydrotreating refers to a catalytic process, usually carried out in the presence of free hydrogen, the primary purpose being the desulfurization and / or the denitrification of the feed. Sulfur is generally converted to hydrogen sulfide and nitrogen is generally converted to ammonia, and these 21 can be removed from the product stream by using methods known to those skilled in the art, including stripping and distillation. When hydrotreating is performed on Fischer-Tropsch products, the primary objective is usually the saturation of olefins and the deoxygenation of the feed. Oxygen in the oxygenation products is converted to water, which can be removed from the product stream by means known to those skilled in the art, including stripping and distillation. Conventional hydrotreating conditions for petroleum and Fischer-Tropsch feeds vary over a wide range. In general, the total hourly liquid space velocity (LHSV) is about 0.25 to 5.0, preferably about 0.5 to 2.0. The hydrogen partial pressure is higher than 200 psia and preferably ranges from about 500 psia to about 2000 psia. The hydrogen recycling rates are usually higher than 50 SCF / Bbl and are preferably between 300 and 5000 SCF / Bbl. Temperatures range from about 300 ° F to about 750 ° F and preferably range from 450 ° F to 750 ° F.

As used herein, "hydroisomerization of light paraffins" refers to processes in which at least a portion of the light normal paraffins are isomerized to isoparaffins. This differs from hydroisomerization dewaxing. This process is usually used to increase the octane number of light naphthas or to prepare isobutane for alkylation. Conventional conditions for the hydroisomerization of light paraffins are known from the literature and can vary widely. Isomerization processes are usually carried out at a temperature between 200 ° F and 700 ° F, preferably 300 ° F to 550 ° F, with an LHSV between 0.1 and 2, preferably between 0.25 and 0.50. Hydrogen is used in such an amount that the molar ratio of hydrogen to hydrocarbon is between 1: 1 and 5: 1. Catalysts useful for isomerization processes are generally bifunctional catalysts comprising a dehydrogenation / hydrogenation component and an acid component. These are preferably combinations of zeolites and noble metals.

As used herein, "hydrocracking" refers to cracking of hydrocarbon chains to form smaller hydrocarbons. This is usually done by contacting the hydrocarbon chains with hydrogen under elevated temperature and / or pressure in the presence of a suitable hydrocracking catalyst. Hydrocracking catalysts with high selectivity for medium distillate products are known.

More than one type of catalyst can be used in the hydroprocessing step. The different types of catalysts can be separated into layers or can be mixed. The hydroprocessing conditions can be varied depending on the fractions obtained from the hydrocarbon synthesis step. For example, if the fractions comprise substantially C20 + hydrocarbons, the hydroprocessing conditions may be adjusted such that the fraction is hydrocracked and substantially C5-20 hydrocarbons are provided. A substantially C20 + hydrocarbon or fraction is a fraction comprising at least 80% by weight, preferably at least 85% by weight and more preferably more than 90% by weight of products with a boiling point higher than 650 ° F. There is probably some degree of overlap between the groups. If the fractions comprise substantially C5-20 hydrocarbons, the hydroprocessing conditions can be adjusted such that hydrotherapy is minimized. The person skilled in the art knows how to modify the reaction conditions in order to adjust the degree of hydrotreatment, hydroisomerization and hydrocracking.

Suitable catalysts and conditions are described, for example, in U.S. Pat. No. 60,75061, the contents of which are incorporated herein by reference in their entirety. Other catalysts are described below.

Hydrotreating can also be used as a final step in the production process of a lubricant base product. In this final step, commonly referred to as hydrofinishes, trace amounts of aromatics, olefins, color bodies and solvents are removed. Treating with clay to remove these contaminants is a possible additional or alternative final process step.

Examples of hydrotreating catalysts that can be used in this embodiment are known in the art. See, for example, U.S. Pat. Nos. 4347121 and 4810357 for general descriptions of hydrotreating and conventional catalysts used in hydrotreating processes.

Suitable catalysts include Group VIIIA noble metals, such as platinum or palladium on an aluminum oxide or silicon-containing matrix, and Group VIIIA and Group VIB unsulfurized metals such as nickel-molybdenum or nickel-tin on an aluminum oxide or silicon-containing matrix. A suitable noble metal catalyst and reaction conditions are described in U.S. Pat. No. 3,852,207.

Other suitable catalysts are described, for example, in U.S. Pat. Nos. 4157294 and 3904513. Non-noble metals (such as nickel-molybdenum) are usually present in the final catalyst composition as oxides, or possibly as sulfides, if such compounds are readily formed from the metal in question. Preferred non-noble metal catalyst compositions contain more than about 5 weight percent, preferably about 5 to about 40 weight percent molybdenum and / or tungsten, and at least about 0.5, 10 and generally about 1 to about 15 weight percent nickel and / or cobalt, determined as the corresponding oxides. The noble metal (such as platinum) catalysts comprise more than 0.01 percent metal, preferably 0.1 to 1.0 percent metal. Combinations of precious metals, such as mixtures of platinum and palladium, may also

are applied. J

The hydrogenation components can be included in the total catalyst composition by various processes. The hydrogenation components can be added to the matrix component by co-milling, impregnation or ion exchange, and the Group VI components, i.e., molybdenum and tungsten, can be combined with the refractory oxide by impregnation, co-milling or coprecipitation. The matrix component can be one of many types, including some that have acid catalytic activity. Those possessing activity include amorphous silica-alumina or may be a zeolietic or non-zeolite crystalline molecular sieve. Examples of suitable matrix molecular sieves include zeolite Y, zeolite X and the so-called ultrastable zeolite Y and zeolite Y with a high structural ratio of silica: alumina, such as that described in U.S. Pat. Nos. 440,156, 4,820,402 and 50,59567. Zeolite Y with a small crystal size, as described in U.S. Patent No. 5073530, can also be used. Non-zeolietic molecular sieves that can be used include, for example, silicoaluminophosphates (SAPO), ferroaluminophosphate, titanium aluminophosphate, and the various ELAPO molecular sieves described in U.S. Patent No. 4,913,799 and the references cited therein. Details regarding the preparation of the various non-zeolietic molecular sieves can be found in U.S. Patent Nos. 51145623 (SAPO); No. 4,913,799 and the various references cited in U.S. Patent No. 4,913,799. Mesoporous molecular sieves can also be used, such as, for example, the M41S family of materials (J. Am. Chem. Soc. 1992, 114, 10834-10843), MCM- 41 (U.S. Patent Nos. 5246689, 5198203 and 5334368) and MCM-48 (Kresge et al., Nature 359 (1992) 710).

Suitable matrix materials may also include synthetic or natural substances, as well as inorganic materials such as clay, silica and / or metal oxides such as silica-alumina, silica-magnesium oxide, silica-zirconia, silica-thorium oxide, silica-berylium oxide, silica titanium oxide, as well as temary compositions, such as silica-alumina-thorium oxide, silica-alumina-zirconia, silica-alumina-magnesium oxide and silica-magnesium-oxide-zirconia. The latter may either occur naturally or may be in the form of gelatinous precipitates or gels, including mixtures of silica and metal oxides. Naturally occurring clays that can be formulated with the catalyst include those from the montmorrillonite and kaolin families. These clays can be used in the raw state as originally mined, or they can be subjected to calibration, acid treatment or chemical modification.

Catalysts useful for isomerization processes are generally bifunctional catalysts comprising a dehydrogenation / hydrogenation component, an acid component, and optionally, but preferably, a hydrocracking suppressor. Preferably, the light paraffin hydroisomerization catalysts used herein are not sensitive to sulfur, but instead promote activity by the presence of sulfur.

The light paraffin hydroisomerization catalyst (s) can be prepared using well-known methods such as e.g. impregnation with an aqueous salt, the technique of incipient humidification, followed by drying at about 125-150 ° C for 1-24 hours, calcining at about 300-500 ° C for about 1-6 hours, reduction by treatment with hydrogen or a hydrogen-containing gas and, if desired, sulfurization by treatment with a sulfur-containing gas, e.g. H2S, at elevated temperatures. The catalyst then contains about 0.01 to 10% by weight sulfur. The metals may be formulated or added to the catalyst either sequentially, in any order, or by co-impregnating two or more metals. Additional details regarding preferred components of the light paraffin hydroisomerization catalysts are described below.

The dehydrogenation / hydrogenation component is preferably a Group VIII metal, more preferably a Group VIII non-noble metal, or a Group VI metal. Preferred metals include nickel, platinum, palladium, cobalt, and mixtures thereof. The Group VIII metal is usually present in catalytically effective amounts, i.e. ranging from 0.5 to 20% by weight. Preferably, a metal from VI, e.g. molybdenum, in amounts of 1-20% by weight, included in the catalyst.

Examples of suitable acid components include crystalline zeolites, molecular sieves, catalyst supports such as halogenated alumina components or silica-alumina components and amorphous metal oxides. The same paraffinic isomerization catalysts are known in the art. The acid component can be a catalyst support with which the catalytic metal is or the catalytic metals are composed. Preferably, the acid component is a zeolite or a silica-alumina support, wherein the silica / alumina ratio (SAR) is less than 1 (w / w).

Preferred carriers include silica, alumina, silica-alumina, silica-alumina phosphates, titanium oxide, zirconia, vanadium oxide, and other oxides of Group III, IV, V, or VI oxides, as well as Y-seven, such as ultra-stable Y-seven. Preferred carriers include alumina and silica-alumina, more preferably silica-alumina, wherein the silica concentration of the bulk support is less than about 50% by weight, preferably less than about 35% by weight. % and more preferably 15-30% by weight. When alumina is used as a carrier, small amounts of chlorine or fluorine can be included in the carrier to provide the acid functionality.

A preferred supported catalyst has a surface area in the 0 Λ range of about 180-400 m / g, preferably 230-350 m / g, and a pore volume of 0.3 to 26 1.0 ml / g , preferably 0.35 to 0.75 ml / g, a bulk density of about 0.5-1.0 g / ml and a side buckling strength of about 0.8 to 3.5 kg / mm.

The preparation of preferred amorphous silica-alumina microspheres for use as carriers is described in Ryland, Lloyd B., Tamele, M.W. and Wilson, J. N., Cracking Catalysts, Catalysis; part VII, Ed. Paul H. Emmet, Reinhold Publishing Corporation, New York, 1960.

Hydrocracking catalysts are known to those skilled in the art and include the catalysts described above that are not sensitive to the presence of sulfur. In the absence of sulfur, significant Cm fractions can be produced with such hydrocracking catalysts which are undesirable. Suppression of these fractions can be promoted by the use of a hydrocracking suppressor. Suitable hydrocracking suppressors include metals from group IB, e.g. preferably copper, more preferably, in amounts of about 0.1-10% by weight of the total catalyst, sulfur-containing organic compounds and presulfurized catalysts.

Some acidic components also act as hydrocracking suppressors, in particular if they are pre-sulphurized catalysts. The catalysts can be pre-sulphurized using known methods, such as, for example, by treatment with hydrogen sulphide until breakthrough occurs. Catalysts containing sulfur-20 sheet usually contain at least about 0.01% by weight of sulfur, preferably about 0.01 to 20% by weight of sulfur, and more preferably 0.1 to 10% by weight of sulfur.

In the hydroprocessing step (s) one or more additional hydrocracking suppressors can be used. Examples of suitable hydrocracking suppressors include Group IB metals, sulfur, and mixtures thereof. Pre-sulphurized catalysts are preferred as hydrocracking suppressors.

If the feeds to the catalytic dewaxing process, the light paraffin hydroisomerization process and other sulfur-sensitive processes include sulfur-containing compounds, the sulfur must be removed for the efficiency of the process. Because the syngas for a Fischer-Tropsch process is usually essentially sulfur-free, it is unlikely that a considerable amount of sulfur will come off the Fi-sharper-Tropsch products, although oxygenation products are often formed. However, sulfur and other heteroatoms can be introduced by mixing 27 with other feed streams, or during the hydroprocessing steps, if, for example, pre-sulfurized catalysts are used. Methods for removing heteroatom contaminants are known to those skilled in the art and include, for example, extractive Merox, hydrotreating, adsorption, etc. Hydrotreating is the preferred method for removing these and other contaminants.

Preferably, the equipment used in syngas generation, Fischer-Tropsch synthesis and / or product isolation can be transported, in whole or in parts, from remote location to remote location, thereby saving money as a a natural gas source becomes exhausted.

Moving a GTL (gas-to-liquid) installation from one location to another can be accomplished, for example, by simply dismantling the GTL installation at its original location, isolating the equipment and then moving it . The most expensive parts will probably be moved to the new location. These components include compressors, reactors, large pumps, high-pressure vessels, control systems, software for control systems, and other expensive components.

A preferred approach, however, is not to build a large integrated GTL installation for the production of lubricant syncrudes, but instead to build the GTL installation in easily transportable modules. These modules can be built at a development site where the construction costs are relatively low, transported to the remote gas source, assembled and operated to produce the syncrude. When the gas source is exhausted, at least some of the modules can be moved to another remote gas source. The modules can be arranged on sliding tracks, which means that they are transported with a floating vessel and are unloaded to shore and brought to the business location. If the gas source is near a bank or river or other accessible location, the modules can be further built on ships and transported to the location near the bank. The vessels are mounted with piles or in another manner, assembled and operated to produce syncrude. Combinations of integrated installations, vessels mounted on slide rails and attached vessels can also be used.

28

The person skilled in the art recognizes many equivalents of the specific embodiments of the invention described herein, or can determine them using routine experiments only. Such equivalents are intended to be encompassed by the following claims.

In addition, it is part of the claimed invention that the process sites that are far apart may be located in different countries and this still falls within the scope and coverage of the embodiments claimed by the invention.

1019328

Claims (22)

A process for preparing a lubricant base product, comprising: (a) converting a light hydrocarbon feed into syngas, (b) subjecting the syngas to a Fischer-Tropsch synthesis to form a substantially linear hydrocarbon product, (c) isolating a fraction containing 650 ° F (343.33 ° C) and a fraction containing 650 ° F + (343.33 ° C +) with an actual vapor pressure of less than 15 psia at the transport temperature, (D) transporting the 650 ° F + (343.33 ° C +) containing fraction to a refinery and (e) converting the 650 ° F + (343.33 ° C +) containing fraction into a lubricant base product. The process of claim 1, wherein at least a portion of the fraction containing 650 ° F (343.33 ° C) is converted into a distillate fuel composition. The process of claim 1 or claim 2, wherein at least a portion of the fraction containing 650 ° F (343.33 ° C) is transported to a refinery and converted into a distillate fuel composition. The process according to any of claims 1 to 3, wherein the fraction containing 650 ° F + (343.33 ° C +) used in step (d) and / or (e) is isolated by condensing the direct vaporous product from a Fischer-Tropsch reactor. 5. Process according to any of claims 1-4, wherein the fraction containing 650 ° F + (343.33 ° C +) used in step (d) and / or (e) is the direct liquid product of a Fischer-Tropsch reactor. The process according to any of claims 1 to 6, wherein the fraction containing 650 ° F + (343.33 ° C +) used in step (d) and / or (e) is obtained from the direct liquid product of a Fischer product Tropsch reactor. The process of any one of claims 1-7, wherein the conversion in step (e) comprises dewaxing selected from the group consisting of: solvent dewaxing, catalytic dewaxing and combinations thereof. 1019328 The process according to any of claims 1 to 8, wherein the conversion in step (e) comprises a hydrotreating step. The process according to any of claims 1 to 9, wherein the conversion in step (e) is carried out at a plurality of fractions obtained from a plurality of 5 different locations. A process for preparing a lubricant base product comprising at least a first location and at least a second location that are far apart from one another, a product being formed at one or a plurality of first locations being applied to the second location (s), wherein the lubricant base product is formed at the second location (s), the process comprising: (a) receiving at the second location a fraction containing 650 ° F + (343.33 ° C +) prepared by : (i) converting a light hydrocarbon feed into syngas, (ii) subjecting the syngas to a Fischer-Tropsch synthesis to form a substantially linear hydrocarbon product and (iii) isolating a 650 ° F (343.33 ° C-) containing fraction and a 650 ° F + (343.33 ° C +) containing fraction from the product of the 11. The process of claim 10, further comprising receiving at least a portion of the fraction containing 650 ° F (343.33 ° C) and converting a portion of the fraction into a distillate fuel composition. The process of claim 10 or claim 11, wherein the fraction containing 650 ° F + (343.33 ° C +) used in step (iii) and / or (iv) is isolated by condensing the direct vaporous product of a Fischer-Tropsch reactor. The process of any one of claims 10 to 12, wherein the 650 ° F + (343.33 ° C +); containing fraction used in step (iii) and / or (iv) is the direct liquid product of a Fischer-Tropsch reactor. The process according to any of claims 10-13, wherein the fraction containing 650 ° F + (343.33 ° C +) used in step (iii) and / or (iv) is obtained from the direct liquid product of a Fischer Tropsch reactor. The process according to any of claims 10-14, wherein the conversion in step (b) comprises dewaxing selected from the group consisting of: solvent dewaxing, catalytic dewaxing and combinations thereof. The process of any one of claims 10 to 15, wherein the conversion in step (b) comprises a hydrotreating step. The process of any one of claims 10-16, wherein the fraction of step (a) containing 650 ° F + (343.33 ° C +) is prepared according to a process further comprising: (a ') establishing the Fischer Tropsch synthesis plant at a first remote location, wherein the plant comprises a syngas generator, a Fischer-Tropsch reactor and equipment for isolating the different products from the Fischer-Tropsch reactor, and wherein the first remote location is a natural gas source has, (b ') converting natural gas into syngas at the first remote location, (c') converting the syngas into fraction (s) containing 650 ° F + (343.33 ° C +) via Fischer-Tropsch synthesis, (d ') disassembling at least a portion of the equipment from step 20 (a'), (e ') transporting at least a portion of those components from d') to a second remote natural gas field and ( f) assembling a Fischer-Tropsch synthesis plant at the second remote natural gas field that has at least one part of the parts of step (e '). The process of claim 17, wherein the Fischer-Tropsch synthesis plant comprises of (a ') components that can be easily dismantled and reassembled. 19. Process for receiving a Fischer-Tropsch product from converted natural gas, wherein the Fischer-Tropsch conversion takes place at several remote locations, the process comprising: (a) receiving a product produced by: ( i) establishing a factory at a first remote location, the factory comprising a syngas generator, a Fischer-Tropsch reactor and equipment for isolating the different products from the Fischer-Tropsch reactor, and wherein the first remote location location 5 has a natural gas source, (ii) converting natural gas into syngas at the first remote location, (iii) converting the syngas into products via Fischer-Tropsch synthesis, (iv) dismantling at least a portion of the 10 step equipment, (v) transporting the dismantled equipment to a second remote location, (vi) establishing a factory at the second remote location, using the dismantled equipment and (vii) repeating steps (ii) and (iii) and (b) refining the received product. 20. Method for preparing hydrocarbon products from remote natural gas fields, comprising: (a) establishing a factory at a first remote natural gas field, wherein the factory comprises components that can be easily disassembled and re-assembled, and wherein natural gas in the factory hydrocarbon products can be converted, (b) converting natural gas into hydrocarbon products at the first remote natural gas field until the natural gas supply is nearly exhausted, (c) dismantling those parts of the plant that can be easily dismantled, (d) transporting at least a portion of those portions from (c) to a second remote natural gas field and (e) assembling a plant at the second remote natural gas field, which comprises at least a portion of the parts from step (d). Fischer-Tropsch synthesis, (b) converting the 650 ° F + (343.33 ° C +) containing fraction into a lubricant base product. The process of any one of claims 1-19, wherein the fractions containing 650 ° F + (343.33 ° C +) have an actual vapor pressure of less than 11 psia at the transport temperature. The process of any one of claims 1 to 19, wherein the fractions containing 650 ° F (343.33 ° C) have an actual vapor pressure of less than 15 psia at the transport temperature. 1 0 19 328