WO2005037748A2

WO2005037748A2 - Preparation of branched aliphatic alcohols using combined process streams from a dimerization unit and an isomerization unit

Info

Publication number: WO2005037748A2
Application number: PCT/US2004/034036
Authority: WO
Inventors: Paul Marie Ayoub; Hendrik Dirkzwager; Brendan Dermot Murray; Steven Clois Sumrow
Original assignee: Shell Internationale Research Maatshappij B.V.
Priority date: 2003-10-15
Filing date: 2004-10-14
Publication date: 2005-04-28
Also published as: WO2005037748A3

Abstract

Systems and methods to produced branched aliphatic alcohols are described. Systems may include an olefin dimerization unit, an olefin isomerization unit, a hydroformylation unit and/or combinations thereof. Methods for producing branched aliphatic alcohols may include isomerization of olefins in a process stream. The isomerized olefins may be hydroformylated to produce aliphatic alcohols. After hydroformylation of the aliphatic alcohols, unreacted components from the hydroformylation process may be separated from the aliphatic alcohols products. The unreacted components from the hydroformylation process may be recycled back into the main process stream or sent to other processing units. Addition of multiple streams to the units may be performed to control reaction conditions in the units.

Description

PREPARATION OF BRANCHED ALIPHATIC ALCOHOLS USING COMBINED PROCESS STREAMS FROM A DIMERrZATION UNIT AND AN ISOMERIZATION UNIT

Background of the Invention

Cross Reference to Related Application This application claims the benefit of U.S. Provisional Application Serial No. 60/511,423 filed October 15, 2003. Field of Invention The present invention generally relates to systems and methods for preparing aliphatic alcohols. More particularly, embodiments described herein relate to systems and methods for preparing branched aliphatic alcohols using a dimerization unit and an isomerization unit. Description of Related Art Aliphatic alcohols are important compounds that may be used in a variety of applications or converted to other chemical compounds (e.g., surfactants, sulfates). Surfactants may be used in a variety of applications (e.g., detergents, soaps, oil recovery). The structural composition of the aliphatic alcohol may influence the properties of the surfactant and/or detergent (e.g., water solubility, biodegradability and cold water detergency) produced from the aliphatic alcohol. For example, water solubility may be affected by the linearity of the aliphatic portion of the aliphatic alcohol. As the linearity of the aliphatic portion increases, the hydrophilicity (i.e., affinity for water) of the aliphatic alcohol surfactant may decrease. Thus, the water solubility and/or detergency performance of the aliphatic alcohol surfactant may decrease. Incorporating branches into the aliphatic portion of the aliphatic alcohol surfactant may increase the cold-water solubility and/or detergency of the aliphatic alcohol surfactant. Biodegradability, however, of the aliphatic alcohol surfactants may be reduced if the branches in the aliphatic portion of the alcohol surfactant include a high number of quaternary carbons. Incorporation of branches with a minimum number of quaternary carbon atoms into the aliphatic portion of the aliphatic alcohol surfactant may increase cold-water solubility and/or detergency of the alcohol surfactants while maintaining the biodegradability properties of the detergents. The aliphatic portion of an aliphatic alcohol used to manufacture a surfactant may include one or more aliphatic alkyl groups as branches. Aliphatic alkyl groups that may form branches in the aliphatic portion may include methyl, ethyl, propyl or higher alkyl groups. Quaternary and tertiary carbons may be present when the aliphatic portion is branched. The number of quaternary and tertiary carbons may result from the branching pattern in the aliphatic portion. As used herein, the phrase "aliphatic quaternary carbon atom" refers to a carbon atom that is not bound to any hydrogen atoms. The manufacture of a surfactant by oligomerizing C and C₄ olefins is described in U.S. Patent No. 5,112,519 to Giacobbe et al., entitled "Process for Production of Biodegradable Surfactants and Compositions Thereof." A process to manufacture linear alcohols by dimerizing an olefin feed comprising C₆-Cιo linear olefins to obtain C₁₂-C ₀ olefins is described in U. S. Patent No. 6,222,077 to Singleton et al, entitled "Dimerized Alcohol Compositions and Biodegradable Surfactants Made Therefrom Having Cold Water Detergency." The dimerized olefins may be converted to alcohols by hydroformylation. Processes to manufacture branched primary alcohol compositions are described in

U.S. Patent No. 5,849,960 to Singleton et al. entitled "Highly Branched Primary Alcohol Compositions, and Biodegradable Detergents Made Therefrom" and U.S. Patent No. 6,150,322 to Singleton et al., entitled "Highly Branched Primary Alcohol Compositions, and Biodegradable Detergents Made Therefrom." Summary of the Invention In an embodiment, aliphatic alcohols may be produced by a method that includes dimerization of olefins in a dimerization unit. A process feed stream entering a dimerization unit may include linear olefins and paraffins having an average carbon number from 4 to 9. As used herein, the phrase "carbon number" refers to the total number of carbon atoms in a molecule. A process feed stream entering a dimerization unit is derived, in some embodiments, from a Fischer-Tropsch process. At least a portion of the olefins in the process feed stream may be dimerized to form dimerized olefins. The produced dimerized olefins may include branched dimerized olefins. In an embodiment, produced dimerized olefins may be separated from the unreacted components after leaving the dimerization unit. The unreacted components, in some embodiments, may be recycled back into the dimerization unit. The produced dimerized olefins may be converted to aliphatic alcohols. Process conditions in the dimerization unit may be such that the resulting branched olefins have an average number of branches per olefin molecule from about 0.7 to about 2.5. The branched olefins may include, but are not limited to, methyl and/or ethyl branched olefins. A dimerization unit may produce branched olefins that include less than about 0.5 percent of quaternary carbon atoms. The branched olefins produced from the dimerization of alpha-olefins having an average carbon number from 4 to 9 will have an average carbon number from 8 to 18. In some embodiments, dimerized olefins may be hydroformylated to produce aliphatic alcohols. After hydroformylation of the dimerized olefins, at least a portion of unreacted components from the hydroformylation process may be separated from the produced aliphatic alcohol products. At least a portion of the unreacted components maybe separated after leaving the hydroformylation unit to produce an unreacted hydrocarbon stream and a produced dimerized olefins stream. At least a portion of the unreacted hydrocarbon stream may be recycled to the dimerization unit. h an embodiment, at least a portion of the product stream exiting a dimerization unit maybe combined with at least a portion of the product stream exiting an isomerization unit and the combined stream directed to a hydroformylation unit. At least a portion of the olefins in the combined stream may be hydroformylated in the hydroformylation unit to produce aliphatic alcohols. After hydroformylation of the olefins, at least a portion of unreacted components from the hydroformylation process may be separated from the aliphatic alcohol products. At least a portion of the unreacted components may be separated. Isomerization of olefins in a process stream may occur in an isomerization unit. In certain embodiments, a process feed stream entering an isomerization unit is derived from a Fischer-Tropsch process. At least a portion of the linear olefins in a process feed stream may be isomerized to branched olefins in the isomerization unit. The resulting branched olefins may have an average number of branches per olefin molecule from about 0.7 to about 2.5. The branched olefins may include, but are not limited to, methyl and/or ethyl branched olefins. The isomerization process may produce branched olefins that include less than about 0.5 percent of aliphatic quaternary carbon atoms. In an embodiment, one or more hydrocarbon streams may be combined with the feed stream entering an isomerization unit and/or hydroformylation unit. The hydrocarbon stream may be mixed with the feed stream to alter the concentration of the olefins entering the isomerization unit and/or hydroformylation unit. h certain embodiments, at least a portion of the aliphatic alcohols maybe sulfated to form aliphatic sulfates. hi some embodiments, aliphatic sulfates may include branched alkyl groups, h certain embodiments, at least a portion of the produced aliphatic alcohols maybe oxyalkylated to form oxyalkyl alcohols, h some embodiments, oxyalkyl alcohols may include branched alkyl groups, h some embodiments, at least a portion of the produced branched aliphatic alcohols may be ethoxylated to form branched ethoxyalkyl alcohols. At least a portion of the oxyalkyl alcohols may be sulfated to from oxyalkyl sulfates. h some embodiments, oxyalkyl sulfates may include branched alkyl groups. Brief Description of the Drawings Advantages of the present invention will become apparent to those skilled in the art with the benefit of the following detailed description of embodiments and upon reference to the accompanying drawings, in which: FIG. 1 depicts a schematic diagram of an embodiment of a system for producing branched aliphatic alcohols using a dimerization unit and an isomerization unit. FIG. 2 depicts a schematic diagram of an embodiment of a separation unit to separate produced dimerized olefins from a reaction mixture. While the invention is susceptible to various modifications and alternative forms, specific embodiments thereof are shown by way of example in the drawing and will herein be described in detail. It should be understood that the drawings and detailed description thereto are not intended to limit the invention to the particular form disclosed, but on the contrary, the intention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the present invention as defined by the appended claims. Detailed Description of the Embodiment Hydrocarbon products may be synthesized from synthesis gas (i.e., a mixture of hydrogen and carbon monoxide) using a Fischer-Tropsch process. Synthesis gas may be derived by partial combustion of petroleum (e.g., coal, hydrocarbons), by reforming of natural gas or by partial oxidation of natural gas. The Fischer-Tropsch process catalytically converts synthesis gas into a mixture of products that includes saturated hydrocarbons, unsaturated hydrocarbons and a minor amount of oxygen-containing products. The products from a Fischer-Tropsch process may be used for the production of fuels (e.g., gasoline, diesel oil), lubricating oils and waxes. Fischer-Tropsch process streams may also be used to prepare commodity products, which have economic value. For example, linear olefins are commodity products that are useful for the production of surfactants. Using a portion of the process stream to produce linear olefins may increase the economic value of a Fischer-Tropsch process stream. Surfactants derived from branched olefins may have different properties than surfactants derived from linear olefins. For example, surfactants derived from branched olefins may have increased water solubility and/or improved detergency properties compared to surfactants derived from linear olefins. Biodegradable properties of the surfactant, however, may be affected by the presence of quaternary carbon atoms in the branched portion of the surfactant. Surfactants made from branched olefins with a minimum number of quaternary carbon atoms may have similar biodegradable properties to surfactants derived from linear olefins. Production of branched olefins from a Fischer- Tropsch process stream may increase the economic value of the stream. In some embodiments, linear olefins may be converted into branched olefins with a minimum number of quaternary carbon atoms using an isomerization catalyst. Increasing the amount of branched olefins derived from a Fischer-Tropsch process stream may increase the economic value of the process streams. Methods are described for increasing the amount of branched olefins derived from a process stream that includes certain amount of olefins, thus increasing the economic value of the process stream. Such methods are useful for both Fischer-Tropsch process streams and product streams from other sources that include hydrocarbons. A hydrocarbon feed stream composition may include paraffins and olefins. At least a portion of the hydrocarbon stream maybe made up of linear paraffins and olefins having at least 4 carbon atoms and up to 18 carbon atoms. A hydrocarbon feed stream may be obtained from a Fischer-Tropsch process or from an ethylene oligomerization process. Fischer-Tropsch catalysts and reaction conditions may be selected to provide a particular mix of products in the reaction product stream. For example, a Fischer-Tropsch catalyst and reaction conditions maybe selected to increase the amount of olefins and decrease the amount of paraffins and oxygenates in the stream. Alternatively, the catalyst and reaction conditions may be selected to increase the amount of paraffins and decrease the amount of olefins and oxygenates in the stream. The catalyst used in a Fischer-Tropsch process may be Mo, W, Group NUI compounds or combinations thereof. Group NUI compounds include, but are not limited to, iron, cobalt, ruthenium, rhodium, platinum, palladium, iridium and osmium. Combinations of Mo, W and Group NUI compounds may be prepared in the free metal form. In an embodiment, combinations of Mo, W and Group NIH compounds may be formed as alloys. Combinations of Mo, W and Group NUT compounds may be formed, in some embodiments, as oxides, carbides or other compounds, h other embodiments, combinations of Mo, W and Group NUI compounds may be formed as salts. Iron based and cobalt based catalysts have been used commercially as Fischer-Tropsch catalysts. Ruthenium catalysts tend to favor the formation of high melting waxy species under high- pressure conditions. Synthetic Fischer-Tropsch catalysts may include fused iron. In some embodiments, a fused iron Fischer-Tropsch catalyst may include a promoter (e.g., potassium or oxides on a silica support, alumina support or silica-alumina support). Cobalt metal may also be used in a Fischer-Tropsch catalyst. With the proper selection of supports, promoters and other metal combinations, a cobalt catalyst may be tuned to manufacture a composition enriched in the desired hydrocarbon species. Other catalysts, such as iron-cobalt alloy catalysts, are known for their selectivity toward the production of olefins. Catalysts and combinations for manufacture of hydrocarbon species by a Fischer- Tropsch process are generally known. While reference is made to a Fischer-Tropsch stream, any stream of olefins and saturated hydrocarbons may be suitable. Many Fischer-Tropsch streams may contain from 5 percent to 80 percent olefins, the remainder being saturated hydrocarbons comprising paraffins and other compounds. The Fischer-Tropsch stream may be separated into several streams. For example, one stream may include hydrocarbons with an average carbon number from 4 to 9 for streams used in a dimerization unit. A second stream may include hydrocarbons with an average carbon number from 7 to 18 for processes that involve an isomerization unit. In some embodiments, feed streams containing olefins and paraffins are obtained through cracking of paraffin wax or the oligomerization of olefins. Commercial olefin products manufactured by ethylene oligomerization are marketed in the United States by Chevron Phillips Chemical Company, Shell Chemical Company (as NEODENE^®) and by British Petroleum. Cracking of paraffin wax to produce alpha-olefin and paraffin feed streams is described in U.S. Patent No. 4,579,986 to Sie, entitled "Process For The Preparation Of Hydrocarbons" and U.S. Patent Application Serial No. 10/153,955 of Ansorge et al., entitled "Process For The Preparation of linear Olefins and Use Thereof To Prepare Linear Alcohols." Specific procedures for preparing linear olefins from ethylene are described in U.S. Patent No. 3,676,523 to Mason, entitled "Alpha-Olefm Production;" U.S. Patent No. 3,686,351 to Mason, entitled "Alpha-Olefm Production;" U.S. Patent No. 3,737,475 to Mason, entitled "Alpha-Olefm Production" and U.S. Patent No. 4,020,121 to Kister et al, entitled "Oligomerization Reaction System." Most of the above-mentioned processes produce alpha-olefins. Higher linear internal olefins may be commercially produced (e.g., chlorination-dehydrochlorination of paraffins, paraffin dehydrogenation, isomerization of alpha-olefins). In an embodiment, a feed stream is processed to produce a hydrocarbon stream that includes branched olefins. These branched olefins may be converted to branched aliphatic alcohols using various techniques. The feed stream may have a paraffin content range between about 50 percent by weight to about 90 percent by weight of the feed stream, h certain embodiments, a feed stream may have a paraffin content greater than about 90 percent by weight paraffins. The feed stream may also include olefins. The olefin content of the feed stream may be between about 10 percent by weight to about 50 percent by weight, hi other embodiments, a feed stream may have an olefin content greater than 90 percent by weight olefins. The composition of the feed stream may include hydrocarbons having an average carbon number ranging from 4 to 30. h an embodiment, an average carbon number of the hydrocarbons in a feed stream may range from 4 to 24. other embodiments, an average carbon number of the feed stream may range from 4 to 18. An average carbon number of the hydrocarbons in a feed stream may range from 7 to 18 for processes that involve an isomerization unit, hi certain embodiments, an average carbon number of the hydrocarbons in a feed stream may range from 10 to 17 for processes that involve an isomerization unit, hi some embodiments, an average carbon number of hydrocarbons in a feed stream may range from 10 to 13 for processes that involve an isomerization unit. In other embodiments, an average carbon number of hydrocarbons in a feed stream may range from 14 to 17 for processes that involve an isomerization unit. The average carbon number of the hydrocarbons in a feed stream may range from 4 to 9 for processes that involve a dimerization unit, h certain embodiments, an average carbon number of the hydrocarbons in a feed stream ranges from 5 to 8. In some embodiments, an average carbon number of hydrocarbons in a feed stream may range from 5 to 7. In other embodiments, an average carbon number of hydrocarbons in a feed stream may range from 7 to 9. A feed stream may include minor amounts of hydrocarbons having a carbon number that is higher or lower than the desired carbon number range, h some embodiments, a feed stream may be derived from distillation of a process stream that includes a broader range of carbon numbers. In an embodiment, a feed stream for a dimerization unit and/or an isomerization unit includes mono-olefms and/or paraffins. The mono-olefms may be of a linear or branched structure. The mono-olefms may have an alpha or internal double bond position. The feed stream may include olefins in which 50 percent or more of the olefin molecules present may be alpha-olefins of a linear (straight chain) carbon skeletal structure. In certain embodiments, at least about 70 percent of the olefins are alpha-olefins of a linear carbon skeletal structure. A hydrocarbon stream in which greater than about 70 percent of all of the olefin molecules are alpha-olefins of a linear carbon skeletal structure may be used in certain embodiments to convert olefins to aliphatic alcohols. Such a stream may be derived from a Fischer-Tropsch process. In some embodiments, a feed stream includes olefins in which at least about 50 percent of the olefin molecules present are internal olefins. Branched chain olefins maybe converted to branched aliphatic alcohols (e.g., branched primary alcohols) by a hydroformylation process. "Hydroformylation," as used herein, refers to the production of alcohols from olefins via a carbonylation and a hydrogenation process. Other processes may be used to produce aliphatic alcohols from olefins. Examples of other processes to produce aliphatic alcohols from olefins include, but are not limited to, hydration, oxidation and hydrolysis, sulfation and hydration, and epoxidation and hydration. The composition of an alcohol product stream may include aliphatic alcohols having an average carbon number ranging from 5 to 31. hi an embodiment, an average carbon number of the aliphatic alcohols in an alcohol product stream may range from 7 to 19. In certain embodiments, an average carbon number of the aliphatic alcohols in an alcohol product stream may range from 11 to 18. In some embodiments, an average carbon number of aliphatic alcohols in an alcohol product stream may range from 11 to 14. In other embodiments, an average carbon number of aliphatic alcohols in an alcohol product stream may range from 15 to 18. hi certain embodiments, a Fischer-Tropsch feed stream may contain olefins and paraffins of low carbon number (e.g., 4, 5, 6, 7, 8, 9). Typically, a low carbon number feed stream may be sold as fuel, sent to waste and/or recycled to other processing units. The low carbon number feed stream may be less useful in the production of detergents. Typically detergents are made from olefins having a carbon number greater than 7. Conversion of the olefins in the feed stream to branched olefins with higher average carbon number (e.g., 7 to 18) may result in a more commercially valuable use of a low carbon number feed stream (e.g., processed to produce detergents and/or surfactants). The amount and type of branching of the alkyl group may increase the value of the feed stream, h certain embodiments, a hydrocarbon stream from a dimerization unit maybe combined with a hydrocarbon stream from an isomerization unit to produce a combined stream. The combined stream may be introduced into a hydroformylation unit. Combining streams from the two units may result in a more economically valuable process to produce aliphatic alcohols. A first hydrocarbon stream, that includes paraffins and olefins may enter dimerization unit 110 via first conduit 112 as depicted for System 100, in FIG. 1. In dimerization unit 110, at least a portion of the olefins may be dimerized. At least a portion of the dimerized olefins may exit dimerization unit 110 as a second hydrocarbon stream via second conduit 114. In certain embodiments, dimerization unit 110 may have several points of entry to accommodate process streams that vary in composition. Process streams may be from other processing units and/or storage units. Examples of process streams include a diluent hydrocarbon stream, and/or other hydrocarbon streams that include olefins and paraffins derived from other processes. Examples of other processes may include Shell Higher Olefins Process or wax cracking process. As used herein, "entry into the dimerization unit" refers to entry of process streams into the dimerization unit through one or more entry points. A dimerization catalyst used in dimerization unit 110 may be a homogeneous or heterogeneous catalyst, hi certain embodiments, a dimerization catalyst used in dimerization unit 110 may be a catalyst that includes oxides of Group HI, Group IN A, Group rVB, Group NILIA, or combinations thereof. Examples of such oxides include, but are not limited to, nickel oxide, silicon dioxide, titanium dioxide, aluminum oxide or zirconium dioxide. The dimerization catalyst may include an amorphous nickel oxide (ΝiO) present as a dispersed substantial monolayer on the surfaces of a silica (SiO₂) support. The silica support may also include on the surface minor amounts of an oxide of aluminum, gallium or indium such that the ratio of nickel oxide to metal oxide present in the catalyst is within the range from about 4:1 to about 100:1. The dimerization catalyst may be prepared by precipitating a water insoluble nickel salt onto the surface of a silica support. The silica support may be impregnated with a metal oxide. In other embodiments, a dimerization catalyst may be prepared by precipitating a water insoluble nickel salt onto a silica-alumina support. The silica-alumina support may be dealuminized such that the resulting nickel oxide/alumina ratio falls within the range from about 4: 1 to about 100:1. The catalyst may be activated by calcination in the presence of oxygen at a temperature with a temperature range from about 300 °C to about 700 °C. hi some embodiments, the catalyst may be activated by calcination in the presence of oxygen at a temperature with a temperature range from about 500 °C to about 600 °C. Silica useful as a support material may have a surface area within a range from about 100 m²/g to about 450 m²/g. hi an embodiment, a silica surface area may be within the range from about 200 m²/g to about 400 m²/g. A range of nickel oxide content may be from about 7 percent to about 70 percent by weight. In certain embodiments, a nickel oxide content may be from about 20 percent to about 50 percent by weight, depending on the surface area of the particular support utilized in preparing the catalyst. For a silica support having a surface area of about 300 m²/g, a nickel oxide content may, in some embodiments, range from about 21 percent to about 35 percent by weight. A nickel oxide content may, in other embodiments, be about 28 percent by weight. The silica support may be in dry granular form or in a hydrogel form prior to precipitation of the nickel oxide precursor compound on the surfaces thereof. Silica hydrogel may be prepared by mixing a water-soluble silicate, (e.g., a sodium or potassium silicate) with a mineral acid. The water-soluble silicate may be washed with water to remove water-soluble ions. The resulting silica hydrogel may be partially dried. In some embodiments, a silica hydrogel may be completely dried. A nickel oxide precursor may include a water-insoluble nickel salt, such as nickel carbonate, nickel phosphate, nickel nitrate or nickel hydroxide. A water-insoluble nickel salt may be generated in-situ by forming an aqueous mixture of the silica gel and a water- soluble nickel salt. The nickel salt may include, but is not limited to, nickel nitrate, nickel sulfonate, nickel carbonylate, nickel halide. A base may be added to the aqueous mixture to induce precipitation of the water-insoluble nickel salt. The water-insoluble nickel salt may be precipitated in finely divided form within the interstices and on the surface of the silica support. The treated silica support may then be recovered, washed several times and dried. A second component in the catalyst may be a trivalent metal oxide, which may include, but is not limited to, aluminum, gallium and indium or combinations thereof. Although a nickel oxide and/or silica catalyst may be active for olefin dimerization, it may deactivate quickly. Deactivation may be from formation of large oligomers that remain attached to the catalyst surface. Large oligomers may act as coke precursors, in some embodiments. A presence of a small amount of the trivalent metal oxide within the catalyst may form acid sites. Acidic sites may promote catalytic activity without promoting unwanted and/or excessive oligomer formation. A trivalent metal oxide maybe incorporated into the silica support by generally known techniques (e.g., precipitation, impregnation). In an embodiment, a trivalent metal oxide may be impregnated into the silica support as an aqueous solution by the addition of a water-soluble salt. The water-soluble metal salt may include, but is not limited to, metal nitrates, metal chlorides or metal sulfates. Once impregnated with a metal salt, the silica support may be dried and calcinated to reduce the metal salt to the oxide form. The silica- trivalent oxide support may further treated to incorporate a nickel oxide layer onto the silica-trivalent metal oxide support. h an embodiment, silica-trivalent metal oxide (e.g., silica/alumina, silica/gallia or silica india gel) may be utilized as support material. In certain embodiments, a content of metal oxide (e.g., alumina) present in the support may be low in comparison with the content of nickel oxide. Dealuminization of the silica/alumina gel of relatively high alumina content (e.g., above about 5 percent by weight) may be necessary to reduce the content of alumina. Dealuminization may be accomplished by known techniques (e.g., extraction of the aluminum with an organic or inorganic acid). Organic or inorganic acids may include, but are not limited to, nitric acid, sulfuric acid, hydrochloric acid, chloroacetic acid or ethylene diamine tetraacetic acid. Extraction may be accomplished by adding the acid to an aqueous dispersion of the alumino silicate followed by stirring, decantation and washing with water. The process may be repeated one or more times until the desired alumina content is achieved. The solids are then dried, calcined and further treated to incorporate the nickel oxide layer onto the silica/alumina support. A content of trivalent metal oxide with respect to the content of the nickel oxide present in the silica support may be significant, hi certain embodiments, when the content of trivalent metal oxide is too low (e.g., above a nickel oxide to trivalent metal oxide ratio of about 100 to 1) then the yield of dimer decreases and the catalyst may tend to deactivate quickly, h certain embodiments, a content of trivalent metal oxide may be high (e.g., below a nickel oxide to trivalent metal oxide ratio of about 4 to 1). A high trivalent metal oxide content may lower the yield of dimer. hi some embodiments, a high trivalent metal oxide content may raise an average content of methyl branching in the dimerized olefin product, hi certain embodiments, a content of trivalent metal oxide may be such that the ratio of nickel oxide to trivalent metal oxide falls within the range from about 4:1 to about 30:1. In other embodiments, a content of trivalent metal oxide maybe such that the ratio of nickel oxide to trivalent metal oxide is between about 5:1 to about 20: 1. In certain embodiments, a ratio of nickel oxide to trivalent metal oxide may be between about 8:1 to about 15:1. In certain embodiments, a dimerization catalyst may contain from about 21 percent to about 35 percent by weight of nickel oxide and about 1 percent to about 5 percent by weight of trivalent metal oxide, based on the total weight of nickel oxide, trivalent metal oxide and silica, h certain embodiments, a dimerization catalyst may include from about 1.5 percent to about 4 percent by weight trivalent metal oxide based on the total weight of nickel oxide, trivalent metal oxide and silica. Preparation of dimerization catalysts are described in U.S. Patent No. 5,849, 972 to Nicari et al., entitled "Oligomerization Of Olefins To Highly Linear Oligomers, and Catalyst For This Purpose," and U.S. Patent No., 5,169,824 to Saleh et al., entitled "Catalyst Comprising Amorphous NiO On Silica Alumina Support." Conversion of olefins in the first hydrocarbon feed stream to dimers in dimerization unit 110, may be carried out as a batch, continuous (e.g., using a fixed bed), semi-batch or multi-step process, hi a batch process, the catalyst may be slurried with the first hydrocarbon feed stream. Temperature conditions for the dimerization reaction may range from about 120 °C to about 200 °C. h an embodiment, a reaction temperature may range from about 150 °C to about 165 °C. Reaction temperatures may be controlled with evaporative cooling (e.g., the evaporation of lighter hydrocarbon fractions from the reaction mixture may control the reaction temperature). Depending on the choice of catalyst, the resulting dimer may be branched. Branches of the olefin produced in dimerization unit 110 may include methyl, ethyl and/or longer carbon chains, hi an embodiment, produced dimerized olefins may contain greater than about 50 percent methyl branches, hi an alternate embodiment, produced dimerized olefins may contain greater than about 90 percent methyl branches. The average carbon number of produced dimerized olefins may range from 8 to 18. In some embodiments, an average carbon number of produced dimerized olefins may range from 10 to 16. In certain embodiments, an average carbon number of produced dimerized olefins may range from 10 to 14. In other embodiments, an average carbon number of produced dimerized olefins may range from 14 to 18. Produced dimerized olefins may be separated from the reactor product using generally known techniques (e.g., fractional distillation). In an embodiment, produced dimerized olefins may be separated from the reaction mixture. 1H NMR analysis of the composition and determination of the branching of the dimerized olefins may be performed. The second hydrocarbon stream may be transferred to other processing units, (e.g., separation units, alkylation units, hydroformylation units) or to storage units through a conduit. h an embodiment, an average number of branches per olefin molecule present in the produced branched olefin composition may be greater than 0.7. h certain embodiments, an average number of branches per olefin molecule present in the branched olefin composition is from about 0.7 to about 2.5. In some embodiments, an average number of branches per olefin molecule present in the branched olefin composition is from about 0.7 to about 2.2. In certain embodiments, an average number of branches per olefin molecule present in the branched olefin composition is from about 1.0 to about 2.2. The degree of branching in the product may be controlled by controlling process conditions used in dimerization unit 110. For example, high reaction temperatures and lower feed rates may result in a higher degree of branching. Methyl branches may represent between about 20 percent to about 99 percent of the total number of branches present in the olefin molecules. In some embodiments, methyl branches may represent greater than about 50 percent of the total number of branches in the olefin molecules. The number of ethyl branches in the olefin molecules may represent, in certain embodiments, less than about 30 percent of the total number of branches. In other embodiments, a number of ethyl branches, if present, maybe between about 0.1 percent and about 2 percent of the total number of branches. Branches other than methyl or ethyl, if present, may be less than about 10 percent of the total number of branches. Aliphatic quaternary carbon atoms present in the branched olefin composition may be less than about 2 percent of the carbon atoms present, hi an embodiment, a number of aliphatic quaternary carbon atoms present is less than about 1 percent of the carbon atoms present. For applications in which biodegradability is important, the number of aliphatic quaternary carbon atoms may be less than about 0.5 percent of the carbon atoms present. In an embodiment, a number of aliphatic quaternary carbon atoms is less than about 0.3 percent of the carbon atoms present. In other embodiments, a number of aliphatic quaternary carbon atoms present in the branched olefin composition is between about 0.01 percent and about 0.3 percent of the aliphatic carbon atoms present. At least a portion of the produced dimerized olefins may be transported to other processing units (e.g., an alkylation unit and hydroformylation unit) via second conduit 114. Produced dimerized olefins may include olefins with an average carbon number from 8 to 18. hi certain embodiments, produced dimerized olefins may include olefins with an average carbon number from 10 to 16. some embodiments, produced dimerized olefins may include olefins with an average carbon number from 10 to 14. In other embodiments, produced dimerized olefins may include olefins with an average carbon number from 14 to 18. Produced dimerized olefins maybe separated, if desired, from the reaction mixture through techniques known in the art (e.g., distillation, adsorption/desorption or molecular sieves). Referring to FIG. 2, a second hydrocarbon stream may exit dimerization unit 110 and enter separation unit 116 via separation conduit 118. Separation unit 116 may produce at least two streams, a branched olefins stream and a linear olefins and paraffins stream, h separation unit 116, the second hydrocarbon stream may be contacted with organic and/or inorganic molecular sieves (e.g., zeolite or urea) with the correct pore size for branched olefins and/or linear olefins and paraffins. Subsequent desorption (e.g., solvent desorption) of at least a portion of the branched olefins and/or at least a portion of the linear olefins and paraffins from the molecular sieves may produce at least two streams (e.g., a branched olefins stream and a linear olefins and paraffins stream). Separation unit 116 may include a fixed bed containing adsorbent for separation of the second hydrocarbon stream to produce a branched olefin and paraffins stream and a linear olefins and paraffins stream. Separation temperatures in separation unit 116 may range from about 100 °C to about 400 °C. h some embodiments, separation temperatures may range from 180 °C to about 380 °C. Separation in separation unit 116 may be conducted at a pressure ranging from about 2 atmospheres (202 kPa) to about 7 atmospheres (710 kPa). In some embodiments, a pretreatment of a second hydrocarbon stream may be performed to prevent adsorbent poisoning. An example of an adsorption/desorption process is a Molex process using Sorbex® separations technology (UOP process, UOP, Des Plaines, IL). Adsorption/desorption processes are described in U.S. Patent No. 6,225,518 to Sohn et al., entitled "Olefmic Hydrocarbon Separation Process;" U.S. Patent No. 5,292,990 to Kantner et al., entitled, "Zeolite Compositions For Use in Olefmic Separations" and U.S. Patent No. 5,276,246 to McCulloch et al, entitled "Process For Separating Normal Olefins From Non-Normal Olefins." At least a portion of the linear olefins and paraffins stream may be transported to other processing units and/or stored on site. The paraffins and unreacted olefins stream may contain hydrocarbons with a carbon number less than 9. hi an embodiment, at least a portion of the linear olefins and paraffins stream may be combined with the first hydrocarbon stream in first conduit 112 via linear olefin and paraffin recycle conduit 120. The combined stream may enter dimerization unit 110 via first conduit 112 to continue the process to produce aliphatic alcohols, hi some embodiments, a linear olefins and paraffins stream may be introduced directly into dimerization unit 110. At least a portion of the branched olefins stream may be transported and utilized in other processing streams and/or stored on site via branched olefins conduit 122. In some embodiments, at least a portion of a branched olefins stream may exit separation unit 116 and be introduced into second conduit 114 via branched olefins conduit 122. In other embodiments, at least a portion of a branched olefins stream may exit separation unit 116 and be introduced directly into a hydroformylation unit. At least a portion of the second hydrocarbon stream may exit dimerization unit 110 and enter hydroformylation unit 124 via second conduit 114. A fourth hydrocarbon stream may be introduced directly into hydroformylation unit 124 through one or more hydroformylation unit ports. As used herein, "entry into the hydroformylation unit" refers to entry of process streams into the hydroformylation unit through one or more entry points. At least a portion of a fourth hydrocarbon stream may be introduced into second conduit 114 via third conduit 126 upstream of hydroformylation unit 124 to produce a combined stream. The fourth hydrocarbon stream may be a stream exiting from isomerization unit 128. Isomerization unit 128 may be fed by a third hydrocarbon stream containing paraffins and unreacted olefins via fourth conduit 130. In isomerization unit 128, at least a portion of the olefins in the third hydrocarbon stream maybe isomerized to branched olefins to produce the fourth hydrocarbon stream. A third hydrocarbon stream may include hydrocarbons with an average carbon number from 7 to 18. In certain embodiments, a third hydrocarbon stream may include hydrocarbons with an average carbon number from 10 to 17. In some embodiments, a third hydrocarbon stream may include hydrocarbons with an average carbon number from 10 to 13. h other embodiments, a third hydrocarbon stream may include hydrocarbons with an average carbon number from 14 to 17. hi some embodiments, a third hydrocarbon stream includes alpha-olefins. In certain embodiments, a third hydrocarbon stream is a stream derived from a Fischer-Tropsch process. The alpha- olefin content of the third hydrocarbon stream may be greater than about 70 percent of the total amount of olefins in the third hydrocarbon stream. In isomerization unit 128, at least a portion of the olefins in the third hydrocarbon stream may be isomerized to branched olefins (e.g., isoolefms) to produce a fourth hydrocarbon stream. In certain embodiments, isomerization unit 128 may have several points of entry to accommodate process streams, which may vary in composition. Process streams may be from other processing units and/or storage units. Examples of process streams include, but are not limited to, a diluent hydrocarbon stream, and/or other hydrocarbon streams that include olefins and paraffins derived from other processes. As used herein, "entry into the isomerization unit" refers to entry of process streams into the isomerization unit through one or more entry points. Conditions for olefin isomerization in isomerization unit 128 may be controlled such that the number of carbon atoms in the olefins before and after the isomerization is substantially the same. Process conditions to skeletally isomerize linear olefins to branched olefins are described in U. S. Patent No. 5,648,584 to Murray, entitled "Process for Isomerizing Linear Olefins to Isoolefms" and U.S. Patent No. 5,648,585 to Murray et al., entitled "Process for Isomerizing Linear Olefins to Isoolefms." In an embodiment, linear olefins in a third hydrocarbon stream are isomerized in isomerization unit 128 by contacting at least a portion of the third hydrocarbon stream with a zeolite catalyst. The zeolite catalyst may have at least one channel with a crystallographic free channel diameter ranging from greater than 4.2 A and less than about 7 A. The zeolite catalyst may have an elliptical pore size large enough to permit entry of a linear olefin and diffusion, at least partially, of a branched olefin. The pore size of the zeolite catalyst may also be small enough to retard coke formation. Temperatures at which the olefin isomerization may be conducted in isomerization unit 128 range from about 200 °C to about 500 °C. Temperatures in isomerization unit 128 are, in some embodiments, kept below the temperature at which the olefin will crack extensively. As used herein, "cracking" refers to the process of thermally degrading molecules into smaller molecules. To inhibit cracking, low temperatures may be used at low feed rates. In certain embodiments, lower temperatures may be used when the amount of oxygenates present in the process stream is low. Higher feed rates may be desirable to increase the production rate of isomerised products. Higher feed rates may be used, in some embodiments, when operating at higher reaction temperatures. The reaction temperature, however, should be set such that cracking to lower boiling weight products is minimized. For example, greater than 90 percent of linear C₁₂-C₁ olefins may be converted to branched olefins at 230 °C at a feed rate of 60 grams per hour per 6 grams of catalyst with minimal cracking. Pressures maintained in isomerization unit 128 may be at a hydrocarbon partial pressure ranging from about 0.1 atmospheres (10 kPa) to about 20 atmospheres (2026 kPa). h an embodiment, a partial pressure may range from above about 0.5 atmospheres (51 kPa) to about 10 atmospheres (1013 kPa). h an embodiment, a fifth hydrocarbon stream may be introduced into hydroformylation unit 124 through one or more hydroformylation ports. In certain embodiments, at least a portion of a fifth hydrocarbon stream may be introduced into second conduit 114 upstream of hydroformylation unit 124 via fifth conduit 132 to produce a combined stream. The combined stream may enter hydroformylation unit 124 and at least a portion of the olefins in the combined stream may be hydroformylated to produce a hydroformylation reaction stream. In an embodiment, a paraffin content of the fifth hydrocarbon stream may be greater than about 50 percent and less than about 99 percent relative to the total hydrocarbon content. In certain embodiments, a paraffin content of the fifth hydrocarbon stream may be between about 60 percent and about 90 percent relative to the total hydrocarbon content. In an embodiment, an olefin content of a fifth hydrocarbon stream ranges between about 1 percent and about 99 percent relative to the total hydrocarbon content. In certain embodiments, an olefin content of a fifth hydrocarbon stream ranges between about 45 percent and about 95 percent, h other embodiments, an olefin content of a fifth hydrocarbon stream may be greater than 80 percent relative to the total hydrocarbon stream. hi certain embodiments, at least a portion of a sixth hydrocarbon stream may be introduced into fourth conduit 130 upstream of isomerization unit 128 via sixth conduit 134 to produce a combined stream. The combined stream may enter isomerization unit 136 and at least a portion of the olefins in the combined stream may be isomerized to produce a sixth hydrocarbon stream, hi an embodiment, a paraffin content of the sixth hydrocarbon stream may be greater than about 50 percent and less than about 99 percent relative to the total hydrocarbon content. In certain embodiments, a paraffin content of the sixth hydrocarbon stream may be between about 60 percent and about 90 percent relative to the total hydrocarbon content. In an embodiment, an olefin content of a sixth hydrocarbon stream ranges between about 1 percent and about 99 percent relative to the total hydrocarbon content. In certain embodiments, an olefin content of a sixth hydrocarbon stream ranges between about 45 percent and about 95 percent. In other embodiments, an olefin content of a sixth hydrocarbon stream may be greater than 80 percent relative to the total hydrocarbon stream. The fourth and fifth hydrocarbon streams may be used to regulate the olefin concentration in hydroformylation unit 124 at a concentration sufficient to maximize hydroformylation of the olefin. The fourth and fifth hydrocarbon streams may be, but are not limited to, a hydrocarbon stream containing olefin, paraffins and/or hydrocarbon solvents. A combined stream may include, but is not limited to, a second hydrocarbon stream, a fourth hydrocarbon stream, a fifth hydrocarbon stream and/or combinations thereof, may be introduced into hydroformylation unit 124 via second conduit 114. An advantage of combining the streams may be that overall production of aliphatic alcohols may be increased with fewer throughputs. At least a portion of the olefins in the combined stream may be hydroformylated to produce aliphatic alcohols. An average carbon number of the alcohols produced in hydroformylation unit 124 may be less than 20. hi certain embodiments, an average carbon number of alcohols produced in hydroformylation unit 124 may range from 7 to 19. In some embodiments, an average number of alcohols produced in hydroformylation unit 124 may range from 10 to 18. In other embodiments, an average number of alcohols produced in a hydroformylation unit 124 may range from 14 to 19. hi a hydroformylation process, olefins are converted to aldehydes, alcohols or a combination thereof by reaction of at least a portion of the olefins with carbon monoxide and hydrogen according to an Oxo process. As used herein, an "Oxo process" refers to the reaction of an olefin with carbon monoxide and hydrogen in the presence of a metal catalyst (e.g., a cobalt catalyst) to produce an alcohol containing one more carbon atom than the starting olefin. hi other hydroformylation processes, a "modified Oxo process" is used. As used herein, a "modified Oxo process" refers to an Oxo process that uses a phosphine, phosphite, arsine or pyridine ligand modified cobalt or rhodium catalyst. Preparation and use of modified Oxo catalysts are described in U.S. Patent No. 3,231, 621, to Slaugh, entitled "Reaction Rates hi Catalytic Hydroformylation"; U.S. Patent No. 3,239,566 to Slaugh et al., entitled "Hydroformylation Of Olefins;" U.S. Patent No. 3,239,569 to Slaugh et al., entitled "HydiOformylation Of Olefins;" U.S. Patent No.

3.239.570 to Slaugh et al., entitled "Hydroformylation Of Olefins;" U.S. Patent No.

3.239.571 to Slaugh et al., entitled "Hydroformylation Of Olefins;" U.S. Patent No. 3,400,163 to Mason et al., entitled "Bicyclic Heterocyclic Sec- And Tert-Phosphines;" U.S. Patent No. 3,420,898 to Nan Winkle et al, entitled "Single Stage Hydroformylation Of Olefins To Alcohols Single Stage Hydroformylation Of Olefins To Alcohols;" U.S. Patent No. 3,440,291 to Van Winkle et al., entitled "Single Stage Hydroformylation Of Olefins To Alcohols;" U.S. Patent No. 3,448,157 to Slaugh et al., entitled "Hydroformylation Of Olefins;" U.S. Patent No. 3,488,158 to Slaugh et al., entitled "Hydroformylation Of Olefins;" U.S. Patent No. 3,496,203 to Morris et al., entitled "Tertiary Organophosphine- Cobalt-Carbonyl Complexes;" U.S. Patent No. 3,496,204 to Morris et al., entitled "Tertiary Organophosphine-Cobalt-Carbonyl Complexes;" U.S. Patent No. 3,501,515 to Nan Winkle et al, entitled "Bicyclic Heterocyclic Terteriary Phosphine-Cobalt-Carbonyl Complexes"; U.S. Patent No. 3,527,818 to Mason et al., entitled "Oxo Alcohols Using Catalysts Comprising Ditertiary Phosphines;" U.S. Patent Application Serial No. 10/075682, entitled "A Process For Preparing A Branched Olefin, A Method Of Using The Branched Olefin For Making A Surfactant, and a Surfactant " and in U. S. Patent Application Serial No. 10/167209 entitled "Process for the Preparation Of A Highly Linear Alcohol Composition." Methods of alcohol production are also described by Othmer, in "Encyclopedia of Chemical Technology" 2000, Fourth Edition; and by Wickson, in "Monohydric Alcohols; Manufacture, Applications and Chemistry" Ed. Am. Chem. Soc. 1981. A hydroformylation catalyst used in hydroformylation unit 124 may include a metal from Group Nm of the Periodic Table. Examples of Groups NUI metals include cobalt, rhodium, nickel, palladium or platinum. The Group NUI metal may be used as a complex compound. A complex compound may be a Group NUI metal combined with a ligand. Examples of ligands include, but are not limited to, a phosphine, phosphite, arsine, stibine or pyridine ligand. Examples of hydroformylation catalysts include, but are not limited to, cobalt hydrocarbonyl catalyst, cobalt-phosphine ligand catalyst, rhodium-phosphine ligand catalyst or combinations thereof. In hydroformylation unit 124, olefins may be hydroformylated using a continuous, semi-continuous or batch process, hi case of a continuous mode of operation, the liquid hourly space velocities maybe in the range of about 0.1 h^"1 to about 10 h^"1. When operating hydroformylation unit 124 as a batch process, reaction times may vary from about 0.1 hours to about 10 hours or even longer. Reaction temperatures in hydroformylation unit 124 may range from about 100 °C to about 300 °C. In certain embodiments, reaction temperatures in the hydroformylation unit ranging from about 125 °C to about 250 °C may be used. Pressure in hydroformylation unit 124 may range from about 1 atmosphere (101 kPa) to about 300 atmospheres (30398 kPa). h an embodiment, a pressure from about 20 (2027 kPa) to about 150 atmospheres (15199 kPa) maybe used. An amount of catalyst relative to the amount of olefin to be hydroformylated may vary. Typical molar ratios of catalyst to olefin in the hydrocarbon stream may range from about 1 : 1000 to about 10:1. A ratio of between about 1:10 and about 5:1 maybe used in certain embodiments, hi an embodiment, a second stream may be added to hydroformylation unit 124 to control reaction conditions. The second stream may include solvents that do not interfere substantially with the desired reaction. Examples of such solvents include, but are not limited to, alcohols, ethers, acetonitrile, sulfolane and paraffins. Mono-alcohol selectivities of at least 90 percent and even of at least 92 percent may be achieved in hydroformylation unit 124. In addition, olefin conversions to aliphatic alcohols may range from about 50 percent by weight to greater than about 95 percent by weight. In certain embodiments, olefin conversion to aliphatic alcohols may be greater than 75 percent by weight, hi some embodiments, olefin conversion to aliphatic alcohols may be greater than about 99 percent by weight. Isolation of aliphatic alcohols produced from the hydroformylation reaction product stream may be achieved by generally known methods. In an embodiment, isolation of the aliphatic alcohols includes subjecting the produced aliphatic alcohols to a first distillation, a saponification, a water washing treatment and a second distillation. The hydroformylation reaction mixture stream may enter separator 136 via sixth conduit 138. In separator 136, the hydroformylation reaction product stream may be subjected to a first distillation step (e.g., flash distillation or a short path distillation), h an embodiment, a short path distillation may be used to produce at least two streams, a bottom stream and a top stream. At least a portion of the bottom stream may be recycled to hydroformylation unit 124 via bottom stream recycle conduit 140, in certain embodiments. The top stream may include, but is not limited to, paraffins, unreacted olefins and a crude aliphatic alcohol product. In an embodiment, a top stream may be subjected to a saponification treatment to remove any acids and esters present in the stream. Saponification may be performed by contacting the top stream with an aqueous solution of a hydroxide base (e.g., sodium hydroxide or potassium hydroxide) at elevated temperatures with agitation. The saponification may be carried out by contacting the top stream with an aqueous 0.5 percent to 10 percent hydroxide base solution at a crude alcohol/water ratio of 10: 1 to 1 : 1. The amount of hydroxide base used may depend on an estimated amount of esters and acids present. Saponification of the top stream may be carried out batch- wise or continuously. The top stream may be subjected to one or more saponification processes. Saponification reaction temperatures may be from about 40 °C to about 99 °C. In an embodiment, saponification temperatures may range from about 60 °C to about 95 °C. Mixing of the top stream with the basic water layer may be performed during the saponification reaction. Separation of the top stream from the basic water layer may be performed using known methods. The top stream may be subjected to a water wash after separation to remove any sodium salts present. The top stream may be separated using generally known techniques (e.g., fractional distillation) to produce at least two streams, a crude alcohol product stream and a paraffins and unreacted olefins stream. As used herein, "fractional distillation" refers to the distillation of liquids and subsequent collection of fractions of liquids determined by boiling point. At least a portion of the paraffins and unreacted olefins stream may exit separation unit 136 and be transported via seventh 144 to another processing unit, and/or storage vessel. In certain embodiments, a paraffins and unreacted olefins stream may be further separated into a hydrocarbons stream including paraffins and unreacted olefins with a carbon number less than 8. The hydrocarbon stream including paraffins and unreacted olefins with a carbon number less than 8 maybe introduced upstream of the dimerization unit and/or into the dimerization unit. hi certain embodiments, a crude aliphatic alcohol product stream may contain unwanted by-products (e.g., aldehydes, hemi-acetals). The by-products may be removed by subjecting the crude alcohol product stream to a hydrofmishing treatment step to produce an aliphatic alcohol product stream. "Hydrofinishing," as used herein, refers to a hydrogenation reaction carried out under relatively mild conditions. Hydrofinishing may be carried out using conventional hydrogenation processes. Conventional hydrogenation processes may include passing the crude alcohol feed together with a flow of hydrogen over a bed of a suitable hydrogenation catalyst. The aliphatic alcohol product stream may include greater than about 50 percent by weight of the produced aliphatic alcohols. In some embodiments, the aliphatic alcohol product stream may include greater than 80 percent by weight of the produced aliphatic alcohols. In other embodiments, the aliphatic alcohol product stream may include greater than 95 percent by weight of the produced aliphatic alcohols. The aliphatic alcohol product stream may include branched aliphatic primary alcohols. The resulting aliphatic alcohols in the aliphatic alcohol product stream may be sold commercially, transported off-site, stored on site and/or used in other processing units via product conduit 142. The composition of an aliphatic alcohol product stream may include hydrocarbons with an average carbon number ranging from 8 to 19. hi an embodiment, an average carbon number of the hydrocarbons in aliphatic alcohol product stream may range from 10 to 17. In certain embodiments, an average carbon number of the feed stream may range from 10 to 13. In other embodiments, an average carbon number of the feed stream may range from 14 to 17. The aliphatic alcohol product stream may include branched primary alcohols. The branched primary alcohol product may be suitable for the manufacture of anionic, nonionic and cationic surfactants, hi some embodiments, branched primary alcohol products may be used as the precursor for the manufacture of anionic sulfates, including aliphatic sulfates and oxyalkyl sulfates and oxyalkyl alcohols. Aliphatic alcohols may have slightly higher aliphatic branching and slightly higher number of quaternary carbons as the olefin precursor, hi some embodiments, aliphatic branching may include methyl and/or ethyl branches. In other embodiments, aliphatic branching may include methyl, ethyl and higher aliphatic branching, h certain embodiments, a number of quaternary carbon atoms in the aliphatic alcohol product may be less than 0.5 percent. In other embodiments, a number of quaternary carbon atoms in the aliphatic alcohol product may be less than 0.3 percent. Branching of the alcohol product may be determined by 1H NMR analysis. The number of quaternary carbon atoms may be determined by ^! C NMR. A ¹³C NMR method for determining quaternary carbon atoms for branched aliphatic alcohols is described in U.S. Patent No. 6, 150,322 to Singleton et al., entitled, "Highly Branched Primary Alcohol Compositions and Biodegradable Detergents Made Therefrom." x Aliphatic alcohols may be converted to oxy alcohols, sulfates or other commercial products. At least a portion of the aliphatic alcohols in the alcohol product stream may be reacted hi an oxyalkylation unit with an epoxide (e.g., ethylene oxide, propylene oxide, butylene oxide) in the presence of a base to produce an oxyalkyl alcohol. Condensation of an alcohol with an epoxide allows the alcohol functionality to be expanded by one or more oxy groups. The number of oxy groups may range from 3 to 12. For example, reaction of an alcohol with ethylene oxide may produce alcohol products having between 3 to 12 ethoxy groups. Reaction of an alcohol with ethylene oxide and propylene oxide may produce alcohols with an ethoxy/propoxy ratio of ethoxy to propoxy groups from about 4:1 to about 12:1. In some embodiments, a substantial proportion of alcohol moieties may become combined with more than three ethylene oxide moieties. In other embodiments, an approximately equal proportion may be combined with less than three ethylene oxide moieties, hi a typical oxyalkylation product mixture, a minor proportion of unreacted alcohol may be present in the product mixture. In an embodiment, at least a portion of the aliphatic alcohol product stream may be formed by condensing a C₅ to C₃₁ aliphatic alcohol with an epoxide. h certain embodiments, a C₅ to C₁₅ branched primary alcohol may be condensed with ethylene oxide and/or propylene oxide, hi other embodiments, a Cπ to C₁₇ branched primary alcohol may be condensed with ethylene oxide and/or propylene oxide. The resulting oxyalkyl alcohols may be sold commercially, transported off-site, stored on site and or used in other processing units. In some embodiments, an oxyalkyl alcohol may be sulfated to form an anionic surfactant. hi an embodiment, at least a portion of the alcohols in the aliphatic alcohol product stream may be added to a base. The base may be an alkali metal or alkaline earth metal hydroxide (e.g., sodium hydroxide or potassium hydroxide). The base may act as a catalyst for the oxyalkylation reaction. An amount from about 0.1 percent by weight to about 0.6 percent by weight of a base, based on the total weight of alcohol, may be used for oxyalkylation of an alcohol, hi an embodiment, a weight percent of a base may range from about 0.1 percent by weight to 0.4 percent by weight based on the total alcohol amount. The reaction of the alcohol with the base may result in formation of an alkoxide. The resulting alkoxide may be dried to remove any water present. The dried alkoxide may be reacted with an epoxide. An amount of epoxide used may be from about 1 mole to about 12 moles of epoxide per mole of alkoxide. A resulting alkoxide-epoxide mixture may be allowed to react until the epoxide is consumed. A decrease in overall reaction pressure may indicate that the reaction is complete. Reaction temperatures in an oxyalkylation unit may range from about 120 °C to about 220 °C. hi an embodiment, reaction temperatures may range from about 140 °C to about 160 °C. Reaction pressures may be achieved by introducing to the reaction vessel the required amount of epoxide. Epoxides have a high vapor pressure at the desired reaction temperature. For consideration of process safety, the partial pressure of the epoxide reactant may be limited, for example, to less than about 4 atmospheres (413 kPa). Other safety measures may include diluting the reactant with an inert gas such as nitrogen. For example, inert gas dilution may result in a vapor phase concentration of reactant of about 50 percent or less, hi some embodiments, an alcohol-epoxide reaction may be safely accomplished at a greater epoxide concentration, a greater total pressure and a greater partial pressure of epoxide if suitable, generally known, safety precautions are taken to manage the risks of explosion. With respect to ethylene oxide, a total pressure from about 3 atmospheres (304 kPa) to about 7 atmospheres (709 kPa) may be used. Total pressures of ethylene oxide from about 1 atmosphere (101 kPa) to about 4 atmospheres (415 kPa) may be used in certain embodiments. In an embodiment, total pressures from about 1.5 atmospheres (150 kPa) to about 3 atmospheres (304 kPa) with respect to ethylene oxide may be used. The pressure may serve as a measure of the degree of the reaction. The reaction may be considered substantially complete when the pressure no longer decreases with time. Aliphatic alcohols and oxyalkyl alcohols may be derivatized to form compositions (e.g., sulfonates, sulfates, phosphates) useful in commercial product formulations (e.g., detergents, surfactants, oil additives, lubricating oil formulations). For example, alcohols may be sulfurized with SO₃ to produce sulfates. The term "sulfurized" refers to a sulfur atom or sulfur containing functionality being added to a carbon or oxygen. Sulfurization processes are described in U.S. Patent No. 6,462,215 to Jacobson et al, entitled "Sulfonation, Sulfation and Sulfamation"; U.S. Patent No. 6,448,435 to Jacobson et al., entitled "Sulfonation, Sulfation and Sulfamation"; U.S. Patent No. 3,462,525 to Levinsky et al, entitled, "Dental Compositions Comprising Long-Chain Olefin Sulfonates;" U.S. Pat. No. 3,428,654 to Rubinfeld et al., entitled, "Alkene Sulfonation Process and Products;" U.S. Patent No. 3,420,875 to DiSalvo et al., entitled, "Olefin Sulfonates;" U.S. Patent No. 3,506,580 to Rubinfeld et al., entitled, "Heat-Treatment Of Sulfonated Olefin Products;" and U.S. Patent No. 3,579,537 to Rubinfeld, entitled, "Process For Separation Of Sultones From Alkenyl Sulfonic Acids." A general class of aliphatic alcohol sulfates may be characterized by the chemical formula: (R-O-(A)^-SO₃)„M. R' represents the aliphatic moiety. "A" represents a moiety of an alkylene oxide; x represents the average number of A moieties per R-O moiety and may range from 0 to 15; and n is a number depending on the valence of cation M. Examples of cation M include, but are not limited to, alkali metal ions, alkaline earth metal ions, ammonium ions and/or mixtures thereof. Examples of cations include, but are not limited to, magnesium, potassium, monoethanol amine, diethanol amine or triethanol a ine. Aliphatic and oxyalkyl alcohols may be sulfated in a sulfation unit. Sulfation procedures may include the reaction of sulfur trioxide (SO₃), chlorosulfonic acid (ClSO₃H), sulfamic acid (NH₂SO₃H) or sulfuric acid with an alcohol. In an embodiment, sulfur trioxide in concentrated (e.g., fuming) sulfuric acid may be used to sulfate alcohols. The concentrated sulfuric acid may have a concentration of about 75 percent by weight to about 100 percent by weight in water. In an embodiment, concentrated sulfuric acid may have a concentration of about 85 percent by weight to about 98 percent by weight in water. The amount of sulfur trioxide may range from about 0.3 mole to about 1.3 moles of sulfur trioxide per mole of alcohol, h certain embodiments, an amount of sulfur trioxide may range from about 0.4 moles to about 1.0 moles of sulfur trioxide per mole of alcohol. hi an embodiment, a sulfur trioxide sulfation procedure may include contacting a liquid alcohol or an oxyalkyl alcohol and gaseous sulfur trioxide in a falling film sulfator to produce a sulfuric acid ester of the alcohol. The reaction zone of the falling film sulfator may be operated at about atmospheric pressure and at a temperature in the range from about 25 °C to about 70 °C. The sulfuric acid ester of the alcohol may exit the falling film sulfator and enter a neutralization reactor. The sulfuric acid ester may be neutralized with an alkali metal solution to form the alkyl sulfate salt or the oxyalkyl sulfate salt. Examples of an alkali metal solution may include solutions of sodium or potassium hydroxide. The derivatized alcohols may be used in a wide variety of applications. An example of an application includes detergent formulations. Detergent formulations include, but are not limited to, granular laundry detergent formulation, liquid laundry detergent formulations, liquid dishwashing detergent formulations and miscellaneous formulations. Examples of miscellaneous formulations may include general purpose cleaning agents, liquid soaps, shampoos and liquid scouring agents. Granular laundry detergent formulations may include a number of components besides the derivatized alcohols (e.g., surfactants, builders, co-builders, bleaching agents, bleaching agent activators, foam controlling agents, enzymes, anti-graying agents, optical brighteners and stabilizers). Examples of other surfactants may include ionic, nonionic, amphoteric or cationic surfactants. Liquid laundry detergent formulations may include the same components as granular laundry detergent formulations. In certain embodiments, liquid laundry detergent formulations may include less of an inorganic builder component than granular laundry detergent formulations. Hydrotropes may be present in the liquid detergent formulations. General purpose cleaning agents may include other surfactants, builders, foam control agents, hydrotropes and solubilizer alcohols. The formulations may typically include one or more inert components. For example, the balance of liquid detergent formulations may typically be an inert solvent or diluent (e.g., water). Powdered or granular detergent formulations typically contain quantities of inert filler or carrier materials. EXAMPLES

Example 1 : Isomerization of Olefins in a Fischer-Tropsch derived Hydrocarbon Stream. Carbon monoxide and hydrogen were reacted under Fischer-Tropsch process conditions to yield a hydrocarbon mixture of linear paraffins, linear olefins, a minor amount of dienes and a minor amount of oxygenates. The Fischer-Tropsch hydrocarbon stream was separated into different hydrocarbon streams using fractional distillation techniques. A hydrocarbon stream containing olefins and paraffins with an average number of carbon atoms from 8 to 10 was obtained. The composition of the resulting C₈-C ₀ hydrocarbon stream was analysed by gas chromatography and is tabulated in Table 1.

Table 1

A zeolite catalyst used for isomerization of linear olefins in the hydrocarbon stream was prepared in the following manner. Ammonium-ferrierite (645 grams) exhibiting a 5.4% loss on ignition and exhibiting the following properties: molar silica to alumina ratio of 62:1, surface area of 369 square meters per gram (P/Po=0.03), soda content of 480 ppm and n-hexane sorption capacity of 7.3 g per 100 g of ammonium-ferrierite was loaded into a Lancaster mix muller. CATAPAL® D alumina (91 grams) exhibiting a loss on ignition of 25.7% was added to the muller. During a five-minute mulling period, 152 milliliters of deionized water was added to the alumina/arnmonium-ferrierite mixture. Next, a mixture of 6.8 grains glacial acetic acid, 7.0 grams of citric acid and 152 milliliters of deionized water was slowly added to the alumina ammonium-ferrierite mixture in the muller to peptize the alumina. The resulting alumina/ammonium- ferrierite/acid mixture was mulled for 10 minutes. Over a period of 15 minutes, a mixture of 0.20 grams of tetraamine palladium nitrate in 153 grams of deionized water was slowly added to mulled alumina ammonium-ferrierite/acid mixture. The resulting mixture exhibited a 90: 10 ratio of zeolite to alumina and a loss on ignition of 43.5%. The zeolite/alumina mixture was shaped by extruding the mixture through a stainless steel die plate (1/16" holes) of a 2.25 inch Bonnot extruder. The moist zeolite/alumina extrudate was dried at 125°C for 16 hours. After drying, the zeolite/alumina extrudate was longsbroken manually. The zeolite/alumina extrudate was calcined in flowing air at 200°C for two hours. The temperature was raised to a maximum temperature of 500°C and the zeolite/alumina extrudate was calcined for an additional two hours to yield an isomerization catalyst. The isomerization catalyst was allowed to cool in a dessicator under a nitrogen atmosphere. Stainless steel tubing, 1 inch OD, 0.6 inch TD and 26 inches long, was used as an isomerization reactor. A thermowell extended 20 inches from the top of the stainless steel reactor tube. To load the reactor tube, the reactor tube was inverted and a piece of glass wool was transferred down the wall of the reactor tube, over the thermowell and positioned at the bottom of the reactor tube to serve as a plug for the reactor tube. Silicon carbide (20 mesh) was added to a depth of about 6 inches to the reactor tube. A second piece of glass wool was placed over the silicon carbide. A mixture of 6.0 grams of the isomerization catalyst particles (6-20 mesh) and 45 grams of fresh silicon carbide (60-80 mesh) was added to the reactor tube in two parts. The two-part addition distributed the isomerization catalyst evenly in the reactor tube and resulted in an isomerization catalyst bed of about 10 inches in length. A third piece of glass wool was added to the top of the catalyst in the reactor tube. Silicon carbide (20 mesh) was layered onto the third piece of glass wool. A fourth piece of glass wool was positioned over the silicon carbide to serve as a plug for the bottom of the reactor tube. To monitor the temperature of the reaction at various points in the reactor tube, a multipoint thermocouple was inserted into the thennowell of the reactor tube. The temperature above, below and at three different places in the catalyst bed was monitored. The reactor tube was inverted and installed in the furnace. The reactor tube was heated to the operating temperature of 280 °C over a four-hour period under flowing nitrogen. Once the temperature of 280 °C was obtained, the reactor tube was held at the operating temperature for an additional two hours to condition the isomerization catalyst. After conditioning the isomerization catalyst, the hydrocarbon stream was pumped through the reactor tube at a flow rate of 60 g/hr. Nitrogen, at a flow rate of 6 L/hr, was passed over the isomerization catalyst simultaneously with the hydrocarbon stream. The hydrocarbon stream was vaporized before contacting the isomerization catalyst. The reactor tube was operated at an outlet pressure of 20 kPa above atmospheric pressure. In Table 2, the weight percent of C₈-C₁₀ branched olefins, C₈-C₁₀ linear olefins and C₈-C₁₀ paraffins in the hydrocarbon stream at 0 hours and in the reactor tube effluent after 24 and 48 hours of isomerization is tabulated. Greater than 90%> of the linear olefins in the hydrocarbon stream were converted into branched olefins in the isomerization reactor. During the isomerization step, a small amount of material boiling below C₈ was generated from cracking side reactions, h addition, a portion of the C₉-Cπ alcohols present in the feed was dehydrated to yield additional olefins in the product. The average number of alkyl branches on the C₈-C₁₀ olefins in the product was found to be 1.0 as determined by 1H NMR analysis. Table 2

Example 2. Isomerization of 1-Dodecene. 1-Dodecene was obtained from Shell Chemical Co. The composition of 1-dodecene, as assayed by gas chromatography, is tabulated in Table 3.

Table 3

1-dodecene was isomerized using the same reactor tube design and isomerization catalyst preparation as described in Example 1. A stream of 1-dodecene was pumped through a reactor tube at a flow rate of 90 g/hr. Nitrogen, at a flow rate of 6 L/hr, was passed over the isomerization catalyst simultaneously with the stream of 1-dodecene. The stream of 1-dodecene was vaporised before contacting the isomerization catalyst. The reactor tube was operated at an outlet pressure of 20 kPa above atmospheric pressure and a temperature of 290°C. Table 4 is a tabulation of the weight percent of less than do, do-C₁ and greater than Cu molecules in 1-dodecene at 0 hours and the reactor tube effluent after 168 and 849 hours. Linear C₁₀-d₄ olefins were converted in a 94% yield to branched C₁₀-C₁₄ olefins after a 168 hr processing time. During the isomerization step, less than 3 weight percent of material boiling below C₁₀ was generated from cracking side reactions. The average number of alkyl branches on the C₁₀-C₁₄ olefins in the product was determined to be 1.3 by 1H NMR analysis.

Table 4

Example 3. Dimerization of 1-Hexene. A dimerization catalyst for the dimerization of a C₆ olefin stream was prepared by the method for Example 1 in U.S. Patent No. 5,169,824 to Saleh et al., entitled, "Catalyst Comprising Amorphous NiO On Silica/ Alumina Support." An aluminosilicate cogel (100 gram, 87% by weight SiO₂-13% by weight Al₂O₃) was dispersed in distilled water (2000 mL). Aluminosilicate cogel may be obtained from Ineos Silicas, Netherlands BV, as Synclist-13. Nitric acid (65%>) was added to the aluminosilicate/water dispersion with stirring until a pH of 2.7 was obtained. The resulting acidic mixture was filtered and the aluminosilicate solid washed with distilled water until the filtrate exhibited a pH of 5.7. The recovered aluminosilicate solid was dispersed again in distilled water and nitric acid (65%) was added until a pH of 2.7 was obtained. The resulting acidic mixture was filtered and the resulting aluminosilicate solid was washed with distilled water until the filtrate exhibited a pH of 5.7. The recovered aluminosilicate solid was dried for 16 hours at 110 °C in an air atmosphere and thereafter calcined at 500 °C for 16 hours under an air atmosphere. Ni(NO₃)₂-6 H₂O (67.38 gram) was dissolved in distilled water (700 mL) and heated to a temperature of 32 °C to result in a solution having a pH of 5.7. The aluminosilicate solid (35 gram) was added over time to the nickel solution resulting in a nickel/aluminosilicate slurry. The pH of the nickel/aluminosilicate slurry was approximately 3.9. The nickel/aluminosilicate slurry was neutralized by adding a solution of (NH₄)₂C0₃ (33.69 gram) in distilled water (200 mL) drop wise over 30 minutes until the pH of the slurry was approximately 6.9. The neutral slurry was stirred for 30 minutes at 32 °C and then filtered to obtain a solid. The recovered solid was slurried twice with water to the original volume of the nickel/aluminosilicate slurry, stirred for 5 minutes and then filtered to obtain a solid. The resulting solid was dried at 110 °C for 16 hours in an air atmosphere. Calcination of the solid was performed by heating the solid under an air atmosphere at increasing temperatures. Initially, the solid was heated to 232 °C for 1 hour. The temperature was raised to 371 °C and the solid heated for 2 hours. After 2 hours, the temperature was raised to 592 °C and the solid was heated for 16 hours. The resulting NiO catalyst dispersed on an aluminosilicate support was crushed and carefully sized to slightly greater than 60 mesh before testing. A 15 mL reactor tube of an autoclave unit was charged with the NiO catalyst (0.335 grams), 1-hexene (3.35 grams), and a gas chromatography standard (0.67 grams linear tefradecane). Autoclave units of the type "Endeavour" from Argonaut Technologies, United Kingdom, were used to perform the dimerization experiments. The gas cap of the reactor tube was flushed with nitrogen and the reactor tube was heated to 160 °C. Once the reaction temperature of 160 °C was obtained, the reaction temperature was maintained for 10 hours and then cooled to room temperature. The reaction mixture was filtered to remove the NiO catalyst and the filtrate was analysed by gas chromatography. The dimerization results are tabulated in Table 5. Table 5

Example 4. Dimerization of Diluted 1-Hexene. A 15 mL reactor tube of the autoclave unit was charged with the NiO catalyst (0.335 grams) prepared according to the method for Example 7, 1-hexene (1.675 grams), hexane (1.675 grams) and a gas chromatography standard (0.67 grams linear tefradecane). The gas cap of the reactor tube was flushed with nitrogen and the reactor tube was heated to 160 °C. Once the reaction temperature of 160 °C was obtained, the reaction temperature was maintained for eight hours and then cooled to room temperature. The reaction mixture was filtered to remove the NiO catalyst and the filtrate was analyzed by gas chromatography. The dimerization results are tabulated in Table 6.

Table 6

Claims

C L A IM S

1. A method for the production of aliphatic alcohols, comprising: introducing a first hydrocarbon stream comprising olefins and paraffins into a dimerization unit, wherein the dimerization unit is configured to dimerize at least a portion of the olefins in the first hydrocarbon stream to produce dimerized olefins, and wherein at least a portion of the unreacted components of the first hydrocarbon stream and the produced dimerized olefins form a second hydrocarbon stream, and wherein at least a portion of the dimerized olefins are branched olefins; introducing at least a portion of the second hydrocarbon stream into a hydroformylation unit; introducing a third hydrocarbon stream comprising olefins and paraffins into an isomerization unit, wherein the isomerization unit is configured to isomerize at least a portion of linear olefins in the third hydrocarbon sfream to branched olefins, and wherein at least a portion of the unreacted components of the third hydrocarbon stream and the produced branched olefins form a fourth hydrocarbon sfream; and, introducing at least a portion of the fourth hydrocarbon stream into the hydroformylation unit, wherein the hydroformylation unit is configured to hydroformylate at least a portion of the olefins in the second hydrocarbon stream and the fourth hydrocarbon stream to produce aliphatic alcohols, wherein at least a portion of the produced aliphatic alcohols comprises a branched alkyl group.

2. The method of claim 1 , wherein the first hydrocarbon stream is produced from a /

Fischer-Tropsch process.

3. The method of any one of claims 1 to 2, wherein the first hydrocarbon stream comprises olefins.

4. The method of any one of claims 1 to 3, wherein the second hydrocarbon stream comprises olefins having a carbon number from 10 to 16.

5. The method of any one of claims 1 to 4, wherein a portion of the branched olefins comprises an average number of branches per total olefin molecules of at least 0.7.

6. The method of any one of claims 1 to 5, wherein a portion of the branched olefins comprises methyl and ethyl branches.

7. The method of any one of claims 1 to 6, wherein a portion of the branched olefins comprises an average number of branches per total olefin molecules of less than about 2.5.

8. The method of any one of claims 1 to 6 , wherein a portion of the branched olefins comprises an average number of branches per total olefin molecules from about 0.7 to about 2.2.

9. The method of any one of claims 1 to 6, wherein a portion of the branched olefins comprises an average number of branches per total olefin molecules from about 1.0 to about 2.2.

10. The method of any one of claims 1 to 9, wherein greater than about 50 percent of the branched groups on the branched olefins are methyl groups.

11. The method of any one of claims 1 to 10, wherein less than about 30 percent of the branched groups on the branched olefins are ethyl groups.

12. The method of any one of claims 1 to 11, wherein less than about 10 percent of the branched groups on the branched olefins are neither methyl or ethyl groups.

13. The method of any one of claims 1 to 12, wherein the branched olefins have less than about 0.5 percent aliphatic quaternary carbon atoms.

14. The method of any one of claims 1 to 12, wherein the branched olefins have less than about 0.3 percent aliphatic quaternary carbon atoms.

15. The method of any one of claims 1 to 14, further comprising: separating the produced dimerized olefins from the second hydrocarbon stream to form a produced dimerized olefins stream and a paraffins and unreacted olefins stream, wherein the paraffins and unreacted olefins stream comprises hydrocarbons of a carbon number less than 9; and, introducing at least a portion of the paraffins and unreacted olefins stream into the dimerization unit.

16. The method of any one of claims 1 to 15, wherein the hydroformylation unit is configured to produce greater than about 50 percent of aliphatic alcohols.

17. The method of any one of claims 1 to 15, wherein the hydroformylation unit is configured to produce greater than about 95 percent of aliphatic alcohols.

18. The method of any one of claims 1 to 17, wherein the hydroformylation unit is operated at a reaction temperature from about 100 °C to about 300 °C.

19. The method of any one of claims 1 to 18, wherein the branched alkyl groups of the branched aliphatic alcohols comprise 0.5 percent or less aliphatic quaternary carbon atoms, and an average number of branches per alkyl group of at least 0.7, the branches comprising methyl and ethyl branching.

20. The method of any one of claims 1 to 19, wherein introducing at least a portion of the fourth hydrocarbon stream into the hydroformylation unit comprises combining at least a portion of the fourth hydrocarbon stream with at least a portion of the second hydrocarbon stream to produce a combined stream upstream of the hydroformylation unit.

21. The method of any one of claims 1 to 20, further comprising adjusting a ratio of olefins to paraffins introduced into the hydroformylation unit by adding at least a portion of a fifth hydrocarbon stream into the hydroformylation unit.

22. The method of any one of claims 1 to 20, further comprising adjusting a ratio of olefins to paraffins introduced into the hydroformylation unit by adding at least a portion of a fifth hydrocarbon stream into the hydroformylation unit and wherein the fifth hydrocarbon stream comprises greater than about 80 percent olefins by weight.

23. The method of any one of claims 1 to 20, further comprising adjusting a ratio of olefins to paraffins introduced into the hydroformylation unit by adding at least a portion of a fifth hydrocarbon stream to at least a portion of the second hydrocarbon stream upstream of the hydroformylation unit.

24. The method of any one of claims 1 to 20, further comprising adjusting a ratio of olefins to paraffins introduced into the hydroformylation unit by adding at least a portion of a fifth hydrocarbon stream to at least a portion of the second hydrocarbon stream upstream of the hydroformylation unit and wherein the fifth hydrocarbon stream comprises greater than about 80 percent olefins by weight.

25. The method of any one of claims 1 to 24, further comprising introducing at least a portion of the aliphatic alcohol product stream into an oxyalkylation unit, wherein the oxyalkylation unit is configured to oxyalkylate at least a portion of the aliphatic alcohols in the aliphatic alcohol product stream to produce oxyalkyl alcohols, wherein at least a portion of the oxyalkyl alcohols produced comprises branched oxyalkyl alcohols.

26. The method of any one of claims 1 to 24, further comprising: introducing at least a portion of the aliphatic alcohol product stream into an oxyalkylation unit, wherein the oxyalkylation unit is configured to oxyalkylate at least a portion of the aliphatic alcohols in the aliphatic alcohol product sfream to produce an oxyalkyl alcohol stream, wherein at least a portion of the oxyalkyl alcohol produced comprises branched oxyalkyl alcohols; and, introducing at least a portion of the oxyalkyl alcohol stream into a sulfation unit, wherein the sulfation unit is configured to sulfate at least a portion of the oxyalkyl alcohols in the oxyalkyl alcohol stream to produce oxyalkyl sulfates, wherein at least a portion of the oxyalkyl sulfates produced comprises branched oxyalkyl sulfates.

27. The method of any one of claims 1 to 24, further comprising: forming a hydroformylation reaction stream wherein the hydroformylation reaction stream comprises at least a portion of the unreacted components of the second and fourth hydrocarbon streams, and at least a portion of the produced aliphatic alcohols; separating aliphatic alcohols from the hydroformylation reaction stream to produce a paraffins and unreacted olefins stream and an aliphatic alcohol product stream; and, introducing at least a portion of the paraffins and unreacted olefins stream into the isomerization unit.

28. The method of any one of claims 1 to 24, further comprising introducing at least a portion of the aliphatic alcohol product stream into a sulfation unit, wherein the sulfation unit is configured to sulfate at least a portion of the aliphatic alcohols in the aliphatic alcohol product stream to produce aliphatic sulfates and wherein at least a portion of the aliphatic sulfates produced comprises branched aliphatic sulfates.

29. The method of 28, further comprising separating the olefins from the paraffins and unreacted hydrocarbons stream to produce an olefmic stream, wherein the average carbon number of the olefins in the olefinic stream is less then 9 and introducing at least a portion of the olefinic stream into the dimerization unit.

30. A system for the production of aliphatic alcohols configured to perform the method according to any one of claims 1 to 29.