PROCESS FOR PRODUCING RENEWABLE PRODUCT STREAMS

Abstract

A renewable feed that is concentrated linear C10-C13 paraffins is produced by hydrodeoxygenating a renewable feedstock is produced by first hydrotreating the feedstock to remove heteroatoms followed by use of a Group VI or VIII catalyst producing a 10-13 carbon atom product having a high level of linearity. Normal paraffins in the range desired by the detergents industry can be produced.

Claims

1. A process for converting a renewable feedstream derived from a biological source, hydrocarbons derived from carbon dioxide or a Fischer-Tropsch liquid to a C.sub.10 normal to C.sub.13 normal paraffin stream by first treating said renewable feedstream to remove heteroatoms to produce a heteroatom-free feedstream and contacting said heteroatom-free feedstream in a cracking reactor with a catalyst comprising a metal selected from Group VIB and Group VIII metals or mixtures of two or more Group VIB and Group VIII metals and a neutral support material and mixtures thereof.

2. The process of claim 1 wherein said catalyst comprises 0.1-10 wt % RuZrO.sub.2.

3. The process of claim 1 wherein said catalyst comprises about 5-30 wt % Mo on alumina.

4. The process of claim 3 wherein said catalyst further comprises about 0.05-5.0 wt % Ni.

5. The process of claim 1 wherein said renewable feedstream comprises carbon chains comprising C.sub.10 to C.sub.57 carbons.

6. The process of claim 1 wherein said biorenewable feedstream comprises carbon chains comprising C.sub.10 to C.sub.18 carbons.

7. The process of claim 1 wherein said renewable feedstream is selected from triglycerides, fatty acids, fats, oils, greases and Fisher-Tropsch liquids.

8. The process of claim 1 wherein the biorenewable feedstream undergoes an additional conversion process to an intermediate stream comprising normal paraffins and wherein at least a portion of the intermediate stream comprising normal paraffins is converted to the C.sub.10 normal to C.sub.13 normal paraffin stream.

9. The process of claim 1 wherein said C.sub.10 to C.sub.13 normal paraffin stream has over 90% linearity.

10. The process of claim 1 wherein said C.sub.10 to C.sub.13 paraffin stream has over 98% linearity.

11. The process of claim 1 further comprising treating said C10 normal to C13 normal paraffin stream to remove branched C10 to C13 hydrocarbons.

12. The process of claim 1 wherein said process produces less than 25 wt % methane.

13. The process of claim 1 wherein said process produces less than 5% methane.

14. The process of claim 1 wherein said feedstream is first sent to a hydrotreating reactor and then sent to a reactor to produce the C.sub.10-C.sub.13 normal paraffin feed stream and then said C.sub.10-C.sub.13 normal paraffin feed stream is sent to be converted to a linear alkyl benzene.

15. The process of claim 1 wherein said catalyst is reduced or partially reduced.

16. The process of claim 1 wherein said cracking reactor is a combination of a hydrotreating stage and a hydrocracking stage.

17. A process for converting a feedstream to nC10 to nC13 linear hydrocarbons comprising sending a hydrocarbon liquid feedstream to a hydrotreating reactor to remove heteroatoms to produce an effluent stream, separating said effluent stream in a separation column into a C9? stream, a C10-C13 product stream and a C14+ stream, sending said C14+ stream to a linear cracking reactor to produce a second C10-C13 stream and other hydrocarbons and sending said second C10-C13 stream and other hydrocarbons to said separation column.

18. The process of claim 17 wherein said feedstream comprises palm kernel oil, coconut oil or babassu oil.

19. The process of claim 18 further comprising separating gas from said effluent stream upstream of said separation column.

20. A process for converting a renewable hydrocarbons to a C10 normal to C13 normal paraffin stream comprising reacting synthesis gas over a Fischer-Tropsch catalyst to provide a Fischer-Tropsch stream; treating said Fischer-Tropsch stream to remove heteroatoms to produce a heteroatom-free feedstream and contacting said heteroatom-free feedstream in a cracking reactor with a catalyst comprising a metal selected from one or more Group VIB and Group VIII metals or mixtures thereof and a neutral support material.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0010] FIG. 1 is a schematic view of a conversion unit of the present disclosure;

[0011] FIG. 2 is a schematic view of an alternate conversion unit of FIG. 1; and

[0012] FIG. 3 is a schematic view of a benzene alkylation unit useful with the conversion unit of either FIG. 1 or FIG. 2.

[0013] FIG. 4 is a schematic view of a unit to produce the desired nC10 to nC13 hydrocarbons.

[0014] FIG. 5 is a schematic view of a linear cracking process using Fischer Tropsch liquid hydrocarbons.

DETAILED DESCRIPTION

[0015] The present disclosure endeavors to produce alkylbenzenes for detergent production and jet fuel and/or diesel from renewable sources. The raw materials for the generation of linear alkyl benzenes are normal C.sub.10 to C.sub.13 olefins, which can be generated by dehydrogenation of normal C1.sub.0-C.sub.13 paraffins. Normal paraffins with 10 to 13 carbons are the desired number of carbons that detergent producers desire for the addition of the alkyl group on the alkylbenzenes used in detergents. While current processes generally use fossil sources of normal paraffins such as kerosene, there is a need for bio-renewable sources of normal paraffins. The most available source of bio-renewable n-paraffins is to subject a stream containing triglycerides or fatty acids to a deoxygenation process such as hydrodeoxygenation to generate an intermediate stream of normal paraffins. However, most triglyceride and fatty acid containing feedstocks produce normal paraffins with 16 to 18 carbons, and in some cases 22 carbons, when deoxygenated. These normal paraffins are of longer chain length than desired by detergent producers. Some renewable sources such as palm kernel oil (PKO), coconut oil and babassu oil have fatty acids that produce normal paraffins with 10 to 13 carbons when deoxygenated, so one path to generate C.sub.10 to C.sub.13 normal paraffins is to use one of these triglyceride containing feeds. In a broad description, it has been found desirable to be able to take an intermediate stream containing broad range of C.sub.16-C.sub.22 normal paraffins that was generated from readily available fats, oils and greases (FOGS) to produce a desired product stream of normal C.sub.10-C.sub.13 by a hydrocracking-like process. The intermediate feed stream is treated as necessary to remove sulfur which deactivates the catalyst. A difference between the catalysts typically used for hydrotreating and for instant the hydrocracking-like step is that the hydrocracking catalysts have been reduced rather than sulfided.

[0016] The hydrocarbons that are subjected to linear cracking reactions may be Fischer Tropsch liquids that are the product of a pretreated biomass that is subjected to gasification to produce a bio-syngas that is subjected to a Fischer Tropsch reaction. The Fischer-Tropsch process is a collection of chemical reactions that converts a mixture of carbon monoxide and hydrogen, known as syngas, into liquid hydrocarbons. These reactions occur in the presence of metal catalysts, typically at temperatures of 150-300? C. (302-572? F.) and pressures of one to several tens of atmospheres.

[0017] In its usual implementation, carbon monoxide and hydrogen, the feedstocks for Fischer Tropsch, are produced from coal, natural gas, or biomass in a process known as gasification. In the present embodiment a plant or animal source is used. The process then converts these gases into synthetic lubrication oil and synthetic fuel.

[0018] We have found that the selection of particular metal catalysts can produce a much higher yield of normal paraffins with 10-13 carbons from a stream containing normal paraffins of 14 to 22 carbons than in previous processes. Compared to the traditional LAB process where the feed is from petroleum, the feed for this process starts with nC.sub.10-nC.sub.57 hydrocarbons that are from renewable sources such as soybean oil, corn oil and other fats, oils, and greases from biological sources. This renewable n-paraffin feed is generally obtained by hydrodeoxygenation of triglycerides in a process such as Ecofining by UOP LLC, Des Plaines, IL. With the catalyst that is used herein, it has been found that the nC.sub.16-C.sub.18 intermediate stream is able to generate linear cracking products with low amounts of branched isomer production.

[0019] The catalysts are chosen from Group VI metals, Group VIII metals or mixtures of two or more Group VI and/or Group VIII metals. The preferred metals include molybdenum, tungsten, aluminum and nickel/aluminum. This catalyst metal is on a neutral support. Neutral support is meant to be a support material that is acidicly neutral, Of the preferred catalysts, the Ru catalyst exhibits much higher activity and per-pass nC.sub.10 to nC.sub.13 yield than the other catalysts. Under the optimized reaction conditions, it also produces very small amounts of methane and isomerized product. This has been found to be the best catalyst for such chemical transformation process. The PtAl.sub.2O.sub.3 catalyst can produce even lower methane yield than the Ru based catalyst with slightly less linear product yield. However, it was found that the Mo containing catalysts produced high yield of the desired nC.sub.10-nC.sub.13 with a high degree of linearity and low amounts of methane.

[0020] To limit catalyst deactivation and poisoning, the feed is treated to remove sulfur contamination for the supported catalysts. The feed has less than 1 wt ppm sulfur content but for the purposes of this disclosure, a feed with less than 100 wt, ppm is considered to be sulfur free. Without this treatment, sulfur accumulates on the catalyst and leads to deactivation. A high temperature hydrogen treatment is shown to recover some of the lost activity.

[0021] The bio-renewable triglyceride containing feed is subjected to hydrodeoxygenation to generate the intermediate normal paraffin feed. The hydrodeoxygenation reactor reacts the bio-renewable triglyceride containing feed with hydrogen and converts triglycerides and free fatty acids to propane, water, n-paraffins and small amounts of ammonia, carbon monoxide and carbon dioxide. Generally, the n-paraffins are separated from the water and gaseous products in a separator to generate the intermediate normal paraffin stream. Hydrodeoxygenation should be complete or nearly complete such that the intermediate feed stream contains less than about 1000 ppm of oxygen, preferably less than 10 ppm of oxygen. The hydrodeoxygenation reactor temperatures are kept low, less than 343? C. (650? F.) for typical biorenewable feedstocks and less than 304? C. (580? F.) for feedstocks with higher free fatty acid (FFA) concentration to avoid polymerization of olefins found in FFA. Generally, hydrodeoxygenation reactor pressure of about 700 kPa (100 psig) to about 21 MPa (3000 psig) are suitable.

[0022] As used herein, the term separator means a vessel which has an inlet and at least an overhead vapor outlet and a bottoms liquid outlet and may also have an aqueous stream outlet from a boot. A flash drum is a type of separator which may be in downstream communication with a separator which may be operated at higher pressure. The term communication means that fluid flow is operatively permitted between enumerated components, which may be characterized as fluid communication. The term downstream communication means that at least a portion of fluid flowing to the subject in downstream communication may operatively flow from the object with which it fluidly communicates.

[0023] The term column means a distillation column or columns for separating one or more components of different volatilities. Unless otherwise indicated, each column includes a condenser on an overhead of the column to condense and reflux a portion of an overhead stream back to the top of the column and a reboiler at a bottom of the column to vaporize and send a portion of a bottoms stream back to the bottom of the column. Feeds to the columns may be preheated. The top pressure is the pressure of the overhead vapor at the vapor outlet of the column. The bottom temperature is the liquid bottom outlet temperature. Unless indicated otherwise, overhead lines and bottoms lines refer to the net lines from the column downstream of any reflux or reboil take-off to the column. Stripper columns may omit a reboiler at a bottom of the column and instead provide heating requirements and separation impetus from a fluidized inert media such as steam.

[0024] As used herein, the term linearity is the mole percentage of hydrocarbons calculated by dividing the moles of normal hydrocarbons divided by the total moles of hydrocarbons.

[0025] The catalysts that are used in the hydrocracking reactions are selected from Group VIB and Group VIII metals with a neutral support. Unlike the catalyst supports in some other reactions, there is no acid functionality in these catalyst supports including no zeolites and no amorphous AI/Si in the support. Some more preferred catalysts include Ru on ZrO.sub.2 catalyst, a Pt on Al.sub.2O.sub.3 catalyst, a Ni on alumina catalyst, Ni on ZrO.sub.2 catalyst, NiO/clay catalyst, a NiMo on alumina catalyst and a Mo catalyst that may be on alumina. The catalyst may be RuZrO.sub.2 (0.1 wt %)

[0026] Preferred cracking reaction conditions for the hydrocracking-like process include a temperature from about 230? C. (446? F.) to about 455? C. (850? F.), suitably 316? C. (600? F.) to about 427? C. (800? F.) and preferably 343? C. (650? F.) to about 399? C. (750? F.). For the RuZrO2 catalyst, being the most active, suitable temperatures are lower than for the other catalysts; generally, about 230? C. (446? F.) to about 300? C. (572? F.). Suitable reaction pressure is from about 2.8 MPa (gauge) (400 psig) to about 17.5 MPa (gauge) (2500 psig), a liquid hourly space velocity of the fresh hydrocarbonaceous intermediate feed stream from about 0.1 hr.sup.?1, suitably 0.5 hr.sup.?1, to about 5 hr.sup.?1, preferably from about 1.5 to about 4 hr.sup.?1, and a hydrogen rate of about 84 Nm.sup.3/m.sup.3 (500 scf/bbl), to about 1,011 Nm.sup.3/m.sup.3 oil (6,000 scf/bbl), preferably about 168 Nm.sup.3/m.sup.3 oil (1,000 scf/bbl) to about 2,016 Nm.sup.3/m.sup.3 oil (12,000 scf/bbl). The cracking reactor is generally downstream of a reactor containing hydrotreating catalyst or a combination of hydrotreating catalysts.

[0027] As used herein, the term a component-rich stream or a component stream means that the stream coming out of a vessel has a greater concentration of the component than the feed to the vessel. As used herein, the term a component-lean stream means that the lean stream coming out of a vessel has a smaller concentration of the component than the feed to the vessel.

[0028] A basic process design showing a hydrotreating reactor and hydrocracking-like cracking reactor with the hydrocracking-like process in back-stage configuration is shown in FIG. 1 in which a feed 40 of a sustainable feedstock such as a soybean oil or corn oil that is rich in nC.sub.16 to nC.sub.22 are sent to be combined with a back stage effluent 35 from a hydrocracking-like cracking reactor 30 (henceforth referred to has hydrocracking reactor), containing one of the catalysts of the present invention, to be sent to a hydrotreating rector 45. The effluent 50 from the hydrotreating reactor 45 is sent to a separator 55 in which a liquid hydrocarbon stream 57 is split into a stream 56 to be combined with feed 40 and a stream 58 which is combined with a hydrogen stream 10 to be sent in stream 20 to hydrocracking reactor 30. An aqueous product 54 is collected in separator 55. An upper stream 60 is sent to vessel 65 to stream 67 and a 3-phase separator 70 to be split into stream 75 sent through compressor 85 to stream 90 which is combined with stream 96 to be sent to the hydrotreating reactor 45. A hydrocarbon product stream 72 is shown. An aqueous stream 74 is shown to be disposed of.

[0029] FIG. 2 shows an embodiment using a hydrotreating reactor and hydrocracking reactor in series using the catalysts of the present invention to produce a higher level of the desired C.sub.10-C.sub.13 carbons for use in making more linear alkyl benzene. A vegetable oil stream 100 is sent to a hydrotreating reactor 105 which contains hydrodeoxygenation catalysts. A stream of the hydrotreated hydrocarbon 110 is sent to separator 115 to produce a stream 130 to be recycled to vegetable oil stream 100, a stream 120 to be sent to a hydrocracking reactor 145, an aqueous stream 118, and a gas stream 125 to be split, a portion of which is compressed to form stream 190 and recycled to combine with vegetable oil stream 100. The normal paraffin containing intermediate stream 120 is optionally combined with recycle product stream 175 and hydrogen stream 140 to hydrocracking reactor 145. Stream 135 is passed to the hydrocracking reactor containing a reduced or partially reduced Ru, Pt, Ni or Mo containing catalyst in which the hydrocarbons are cracked into a hydrocarbon mixture 150 including normal paraffins. These hydrocarbons are sent to column 165 to be separated into an off-gas 170, a lighter hydrocarbon stream 185 to be sent to a steam cracker or otherwise utilized to make further products or fuels, and a stream 180 of C.sub.10 to C.sub.13 hydrocarbons which are then sent to be reacted to produce linear alkyl benzene product. Optionally, a stream 175 is sent to an isomerization reactor (not shown) to produce renewable fuels and a portion of stream 175 is recycled to be sent back through hydrocracking reactor 145.

[0030] FIG. 3 shows an embodiment in which the hydrotreating and hydrocracking occur in sections within the same reactor. A feed 200 that has been treated to remove sulfur is combined with a supply of make-up hydrogen 205 to enter an upper portion of reactor 210 which has a low temperature catalyst in the upper portion of the reactor and a high temperature catalyst in the lower part of the reactor. The resultant stream 215 is sent to a separator 220 with a light hydrocarbon portion 260 returned to be combined with feed 200. A water stream 223 is shown exiting separator 220. A portion that contains the heavier hydrocarbons is sent in line 222 to column 235 to be separated into off gas stream 240, LPG stream 245 and LNAP stream 250 containing the linear C.sub.10-C.sub.13 products to be further reacted to make linear alkyl benzene. A stream 270 is sent to an isomerization reactor.

[0031] FIG. 4 shows a flowscheme in which the hydrocarbon oils 300 are from palm kernal oil or coconut oil. A stream 310 of the hydrocarbon oils is sent to a hydrotreating reactor 330 along with make-up hydrogen gas 320. Heteroatoms are removed from the hydrocarbon oils in the hydrotreating reactor with the liquid effluent 335 going to a separator 326 with a gas portion 325 being added to make-up hydrogen 320, a waste water stream 328 exiting and a recycle portion of hydrocarbons 327 returning to stream 310. The remaining hydrocarbon goes to separation column 340 which produces a lighter hydrocarbon stream 342, a product stream 344 of normal C10 to C13 hydrocarbons and a heavier hydrocarbon stream 346 of C14+ which is sent to linear cracking reactor 350 to which is added make up hydrogen stream 348. Stream 360 contains normal C10 to C13 hydrocarbons which are sent to the separator 242 to be made part of product stream 344.

[0032] FIG. 5 shows a flowscheme for providing a linear cracked hydrocarbon product from a Fischer Tropsch liquid stream. Pretreated biomass 500 with supply of oxygen 502 is subject to gasification reactor 505 which becomes a biosyngas 510 that is subjected to a Fischer-Tropsch reaction in reactor 515 to produce Fischer-Tropsch liquids 516 which are a mixture of C7+ hydrocarbons. The C7+ hydrocarbons are sent to hydrotreating reactor 530 so that heteroatoms such as oxygenates can be removed. The C7+ hydrocarbons are treated in purification section 520 to produce a treated Fisher-Tropsch liquid stream 525 to be sent to hydrotreating reactor 530. A treated stream 535 is sent through separator 540 to stream 537 to linear cracking reactor 560 which has make-up hydrogen 562 added. Waste water 539 is removed at separator 540. Effluent 565 is sent through separator 570 to separator column 580. Off gases 582 pass from the top of separator 580. A light hydrocarbon stream 586 of C2-C9 hydrocarbons is sent to a steam cracker 590 which is not shown. The product stream 588 of normal C10-C13 hydrocarbons is sent through stream 592 to a unit to produce linear alkyl benzenes. The bottom stream 584 may be sent to an isomerization reactor (not shown). A portion of bottom stream 584 may be sent back through linear cracking reactor 560. Recycle streams 555 and 545 may be returned to hydrotreating reactor 530.

[0033] The following are several examples of the use of different catalysts to crack a paraffin into the desired C.sub.10-C.sub.13 paraffins.

Example 1

[0034] A normal pentadecane (n-C15) feed was contacted with a 0.75% wt Pt on ?-alumina catalyst, with 0.75% wt Cl at conditions of 350? C., 500 psig, 1 h?1 WHSV, 10 H2/HC, 1 g catalyst. The reaction generated 40% n-C15 conversion. On carbon basis, selectivities were as follows: 0.79% methane, 39.50% C2-C8 normal paraffins, 38.08% C9-C12 normal paraffins, 10.91% C13 and C14 normal paraffins and 10.74% isomerized pentadecanes. The advantages seen were a low degree of methane production but there was low activity and high feed isomerization levels that may limit recycling.

Example 2

[0035] A n-C15 feed was contacted with a catalyst consisting of 0.5% wt Ru on ZrO.sub.2 at 245? C., 200 psig, 2 h.sup.?1 WHSV, 25 H.sub.2/HC (by moles), 0.5 g catalyst. The reaction generated 75% n-C.sub.15 conversion. The selectivities on a carbon basis were C1 8.36%, C2 to C8 normal paraffins 34.65%, C.sub.9 to C.sub.12 normal paraffins 34.60%, C.sub.13 and C.sub.14 normal paraffins 21.94% and iC.sub.15 0.44%. The advantages found were high activity and low level of isomerization but there was higher production of methane than with the Pt-based catalyst.

Example 3

[0036] A n-C.sub.15 feed was contacted with a catalyst consisting of 0.1% wt Ru on ZrO.sub.2 at 285? C., 500 psig, 1 hr.sup.?1 WHSV, 25 H.sub.2/HC (by moles), 1 g catalyst. The reaction generated 98% n-C.sub.15 conversion. The selectivities on a carbon basis were C1 3.08%, C.sub.2-C.sub.8 normal paraffins 58%, C.sub.9-C.sub.12 normal paraffins 34.57%, C.sub.13-C.sub.14 normal paraffins 4.33% and no detectable isomerized C.sub.15 or heavier products.

[0037] The Ru-based catalyst is sensitive to sulfur in the feed. In the examples, all clean parts were used in the testing. Previous testing with sulfur contaminated reactor yielded very low activity. Therefore, use of Ru based catalyst requires very low levels of sulfur ?<0.1 ppm, preferably <0.03 ppm S in feed to maintain activity.

Example 4

[0038] Table 1 shows the experimental results from a feed containing 10 wt % n-C16 and 90 wt % nC.sub.18 contacted with a number of different catalysts including catalysts containing Pt on alumina, Ni on alumina, NiO on clay, Ni on alumina dispersed on an inert core, NiMo on alumina and Mo on alumina. Each individual catalyst testing was carried out in a 0.46 ID once through plant having a Gas, Liquid Feed, Rx, Stripper and Product collection section. Reactor was loaded with the catalyst/SiC ratio 3. A sulfur adsorbent was placed in the pre-heat zone of the reactor to ensure the feed that enters the reactor has no sulfur in it. All catalysts were in-situ reduced in hydrogen at temperatures ?400? C. followed by inducting the catalyst with 90/10 nC.sub.18/nC.sub.16 blend. Using the same feed, under conditions outlined in Table 1 catalyst activity measurements were taken. In general, it preferred to maximize yield of normal C10-C13, maximize linearity and minimize methane byproduct level.

TABLE-US-00001 TABLE 1 Ni/alumina NiMo on Mo on Cat comp. Pt/alumina Ni/alumina NiO/clay on inert core alumina alumina Temp., ? C. 325 315 350 315 400 370 Pressure, bars 35.41 7 35.72 7 34.5 7 H.sub.2/oil 10400 5000 10000 5000 3170 5000 C.sub.14 + 5% 24% 54% 33% 31% 53% conversion H.sub.2 ?0.1 ?1.8 ?4.09 ?3.2 ?1.82 ?0.986 consumption Total C10-13 4.23 23.57 22.8 49.3 29.3 79 KMTA produced nC10-nC13 1.13 23 20.65 48 22 72 KMTA Linearity 26 97.61 90.54 97.52 75 91 (nC.sub.10-C.sub.13) 0.08 37 14.82 40.6 36.6 57 Selectivity Byproduct 0.206 31.82 68.757 60.43 0.6 0.87 CH.sub.4 KMTA

[0039] While the following is described in conjunction with specific embodiments, it will be understood that this description is intended to illustrate and not limit the scope of the preceding description and the appended claims.

[0040] Without further elaboration, it is believed that using the preceding description that one skilled in the art can utilize the present disclosure to its fullest extent and easily ascertain the essential characteristics of this disclosure, without departing from the spirit and scope thereof, to make various changes and modifications of the disclosure and to adapt it to various usages and conditions. The preceding preferred specific embodiments are, therefore, to be construed as merely illustrative, and not limiting the remainder of the disclosure in any way whatsoever, and that it is intended to cover various modifications and equivalent arrangements included within the scope of the appended claims.

[0041] In the foregoing, all temperatures are set forth in degrees Celsius and, all parts and percentages are by weight, unless otherwise indicated. A first embodiment of the disclosure is a process for converting a renewable feedstream to a C.sub.10 normal to C.sub.13 normal paraffin stream by first treating the renewable feedstream to remove heteroatoms such as sulfur, oxygen and nitrogen to produce a heteroatom-free feedstream and contacting said heteroatom-free feedstream in a cracking reactor with a catalyst selected from Group VIB or Group VIII metals or mixtures of two or more Group VIB and Group VIII metals and a neutral support. An embodiment of the disclosure is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the catalyst comprises a RuZrO.sub.2, PtAl.sub.2O.sub.3, NiZrO.sub.2, tungsten-containing catalyst or a Mo-containing catalyst or mixtures thereof. An embodiment of the disclosure is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the catalyst comprises RuZrO.sub.2 (0.1-10 wt %). An embodiment of the disclosure is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the catalyst comprises about 5-30 wt % Mo on alumina. An embodiment of the disclosure is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the Mo containing catalyst further comprises about 0.05-5.0 wt % Ni. An embodiment of the disclosure is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein said biorenewable feedstream comprises carbon chains comprising C.sub.10 to C.sub.57 carbons. An embodiment of the disclosure is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph process of claim 1 wherein said biorenewable feedstream comprises carbon chains comprising C.sub.10 to C.sub.18 carbons An embodiment of the disclosure is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the biorenewable feedstream is selected from triglycerides, fats, oils or greases. An embodiment of the disclosure is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the biorenewable feedstream undergoes an additional conversion process to an intermediate stream comprising normal paraffins and where at least a port of the intermediate stream comprising normal paraffins is converted to the C.sub.10 normal to C.sub.13 normal paraffin stream. An embodiment of the disclosure is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the C.sub.10 to C.sub.13 normal paraffin stream has over 90% linearity. An embodiment of the disclosure is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the C.sub.10 to C.sub.13 normal paraffin stream has over 95% linearity. An embodiment of the disclosure is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the normal paraffin stream has over 98% linearity An embodiment of the disclosure is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph further comprising treating the C.sub.10 normal to C.sub.13 normal paraffin stream to remove isomerized C.sub.10 to C.sub.13 hydrocarbons. An embodiment of the disclosure is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the sulfur is removed from the biorenewable feed stream by sending the biorenewable feedstream through an adsorption bed before being sent to be contacted with said catalyst. An embodiment of the disclosure is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the process produces less than 25 wt % methane. An embodiment of the disclosure is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein said process produces less than 5% methane. An embodiment of the disclosure is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the feedstream is first sent to a hydrotreating reactor and then sent to a reactor and then the C.sub.10-C.sub.13 stream is sent to be converted to a linear alkyl benzene. An embodiment of the disclosure is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein said catalyst in said hydrocracking reactor is partially reduced. An embodiment of the disclosure is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the cracking reactor is a combination of a hydrotreating and hydrocracking reactor.

[0042] A second embodiment of the disclosure is a process for converting a feedstream to nC10 to nC13 linear hydrocarbons comprising sending a Fischer Tropsch liquid feedstream to a hydrocracking reactor to remove heteroatoms to produce an effluent stream, separating said effluent stream in a separation column into a C9? stream, a C10-C13 product stream and a C14+ stream, sending said C14=stream to a linear cracking reactor to produce a second C10-C13 stream and other hydrocarbons and sending said second C10-C13 stream and other hydrocarbons through said separation column.

[0043] A third embodiment of the disclosure is a process for converting a feedstream to nC10 to nC13 linear hydrocarbons comprising sending a hydrocarbon liquid feedstream to a hydrotreating reactor to remove heteroatoms to produce an effluent stream, separating said effluent stream in a separation column into a C9? stream, a C10-C13 product stream and a C14+ stream, sending said C14+ stream to a linear cracking reactor to produce a second C10-C13 stream and other hydrocarbons and sending said second C10-C13 stream and other hydrocarbons to said separation column. An embodiment of the disclosure is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the feedstream comprises palm kernel oil, coconut oil or babassu oil. An embodiment of the disclosure is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein gas is separated from the effluent upstream of the separation column.