HYDROPROCESSING BLOCK METHODS FOR MAKING RENEWABLE FUELS

Description

FIELD OF THE DISCLOSURE

The present disclosure relates to methods and systems for alternating the making of renewable fuels, such as renewable diesel, and the making of hydrocracked products, wherein substantially the same equipment and catalysts are used to make the renewable diesel and hydrocracked products.

BACKGROUND AND SUMMARY

The production of renewable fuels, such as renewable diesel, and sustainable aviation fuel is becoming increasingly important. Unfortunately, the required process conditions, catalysts, and/or equipment for making renewable fuels are often very different from those required for producing hydrocracked products.

What is needed are new methods and systems wherein similar process conditions, catalysts, and/or equipment may be employed for producing both renewable diesel, sustainable aviation fuel, and hydrocracked products. It would be further advantageous if such methods and processes could be alternately employed to make desired products without requiring significant (or any) catalyst changes, equipment reconfiguration, and/or major process disruptions. It would further be advantageous if such new methods and systems for alternating product production could be undertaken in the same or similar unit. Advantageously, the methods and systems described here accomplish one or more up to all of the aforementioned advantages.

In one embodiment the application pertains to an alternating hydroprocessing process comprising reacting a lipid or a mixture of lipid and petroleum feedstock with hydrogen in the presence of a catalyst in a vessel under conditions suitable to form a renewable product. The formed renewable product is removed from the vessel. A petroleum feedstock is then reacted with hydrogen in the presence of the catalyst in the vessel under conditions suitable to form a hydrocracked product.

In another embodiment the application pertains to a system for alternating forming a renewable product and a hydrocracked petroleum-derived or fossil product. The system comprises a reactor, a catalyst, a lipid feed, a petroleum feedstock feed, a hydrogen feed, a catalyst, and process control equipment. The process control equipment are configured to provide alternating conditions suitable to form a renewable diesel product and a hydrocracked product.

DETAILED DESCRIPTION

Although illustrative embodiments of one or more aspects are provided herein, the disclosed processes may be implemented using any number of techniques. The disclosure is not limited to the illustrative or specific embodiments, drawings, and techniques illustrated herein, including any exemplary designs and embodiments illustrated and described herein, and may be modified within the scope of the appended claims along with their full scope of equivalents.

Definitions

Unless otherwise indicated, the following terms, terminology, and definitions are applicable to this disclosure. If a term is used in this disclosure but is not specifically defined herein, the definition from the IUPAC Compendium of Chemical Terminology, 2nd ed (1997), may be applied, provided that definition does not conflict with any other disclosure or definition applied herein, or render indefinite or non-enabled any claim to which that definition is applied. To the extent that any definition or usage provided by any document incorporated herein by reference conflicts with the definition or usage provided herein, the definition or usage provided herein is to be understood to apply.

“API gravity” refers to the gravity of a petroleum feedstock or product relative to water, as determined by ASTM D4052-11.

“Viscosity index” (VI) represents the temperature dependency of a lubricant, as determined by ASTM D2270-10 (E2011).

“Vacuum gas oil” (VGO) is a byproduct of crude oil vacuum distillation that can be sent to a hydroprocessing unit or to an aromatic extraction for upgrading into base oils. VGO generally comprises hydrocarbons with a boiling range distribution between 343° C. (649° F.) and 593° C. (1100° F.) at 0.101 MPa.

“Treatment,” “treated,” “upgrade,” “upgrading” and “upgraded,” when used in conjunction with an oil feedstock, describes a feedstock that is being or has been subjected to hydroprocessing, or a resulting material or crude product, having a reduction in the molecular weight of the feedstock, a reduction in the boiling point range of the feedstock, a reduction in the concentration of asphaltenes, a reduction in the concentration of hydrocarbon free radicals, and/or a reduction in the quantity of impurities, such as sulfur, nitrogen, oxygen, halides, and metals.

“Hydrocarbon” refers to any compound which comprises hydrogen and carbon and “hydrocarbon feedstock” refers to any charge stock which contains greater than about 90 wt. % carbon and hydrogen.

“Hydroprocessing” refers to a process in which a carbonaceous feedstock is brought into contact with hydrogen and a catalyst, at a higher temperature and pressure, for the purpose of removing undesirable impurities and/or converting the feedstock to a desired product. Examples of hydroprocessing processes include hydrocracking, hydrotreating, catalytic dewaxing, and hydrofinishing.

“Hydrocracking” refers to a process in which hydrogenation and dehydrogenation accompanies the cracking/fragmentation of hydrocarbons, e.g., converting heavier hydrocarbons into lighter hydrocarbons, or converting aromatics and/or cycloparaffins (naphthenes) into non-cyclic branched paraffins.

“Hydrotreating” refers to a process that converts sulfur and/or nitrogen-containing hydrocarbon feeds into hydrocarbon products with reduced heterogenous impurities such as reduced sulfur, oxygen, and/or nitrogen content, typically in conjunction with hydrocracking, and which generates hydrogen sulfide and/or ammonia (respectively) as byproducts. Such processes or steps performed in the presence of hydrogen include hydrodesulfurization, hydrodenitrogenation, hydrodemetallation, and/or hydrodearomatization of components (e.g., impurities) of a hydrocarbon feedstock, and/or for the hydrogenation of unsaturated compounds in the feedstock. Depending on the type of hydrotreating and the reaction conditions, products of hydrotreating processes may have improved viscosities, viscosity indices, saturates content, low temperature properties, volatilities and depolarization, for example. The terms “guard layer” and “guard bed” may be used herein synonymously and interchangeably to refer to a hydrotreating catalyst or hydrotreating catalyst layer. The guard layer may be a component of a catalyst system for hydrocarbon dewaxing, and may be disposed upstream from at least one hydroisomerization catalyst.

“Distillate” means that typical fuels of this type can be generated from vapor overhead streams from distilling petroleum crude. In contrast, residual fuels cannot be generated from vapor overhead streams by distilling petroleum crude, and are then non-vaporizable remaining portion. Within the broad category of distillate fuels are specific fuels that include: naphtha, jet fuel, diesel fuel, kerosene, aviation gas, fuel oil, and blends thereof. at a specified temperature. The term “middle distillate” refers to products boiling in the 250-700° F. (121-371° C.) range, including diesel fuel. Middle distillates can include jet, kerosene, and diesel. Some typical naphthas and middle distillates for the North American market include the following:

	TABLE 1
	Products	Typical Cut Points ° F. (° C.)

	Light Naphtha	C5-180	(C5-82)
	Heavy Naphtha	180-300	(82-149)
	Jet	300-380	(149-193)
	Kerosene	380-530	(193-277)
	Diesel	530-700	(277-371)

“TBP” refers to the boiling point of a hydrocarbonaceous feed or product, as determined by Simulated Distillation (SimDist) by ASTM D2887-13.

“Hydrocarbonaceous”, “hydrocarbon” and similar terms refer to a compound containing only carbon and hydrogen atoms. Other identifiers may be used to indicate the presence of particular groups, if any, in the hydrocarbon (e.g., halogenated hydrocarbon indicates the presence of one or more halogen atoms replacing an equivalent number of hydrogen atoms in the hydrocarbon).

The term “Periodic Table” refers to the version of the IUPAC Periodic Table of the Elements dated Jun. 22, 2007, and the numbering scheme for the Periodic Table Groups is as described in Chem. Eng. News, 63 (5), 26-27 (1985). “Group 2” refers to IUPAC Group 2 elements, e.g., magnesium, (Mg), Calcium (Ca), Strontium (Sr), Barium (Ba) and combinations thereof in any of elemental, compound, or ionic form. “Group 7” refers to IUPAC Group 7 elements, e.g., manganese (Mn), rhenium (Re) and combinations thereof in their elemental, compound, or ionic form. “Group 8” refers to IUPAC Group 8 elements, e.g., iron (Fe), ruthenium (Ru), osmium (Os) and combinations thereof in their elemental, compound, or ionic form. “Group 9” refers to IUPAC Group 9 elements, e.g., cobalt (Co), rhodium (Rh), iridium (Ir) and combinations thereof in any of elemental, compound, or ionic form. “Group 10” refers to IUPAC Group 10 elements, e.g., nickel (Ni), palladium (Pd), platinum (Pt) and combinations thereof in any of elemental, compound, or ionic form. “Group 14” refers to IUPAC Group 14 elements, e.g., germanium (Ge), tin (Sn), lead (Pb) and combinations thereof in any of elemental, compound, or ionic form.

The term “support”, particularly as used in the term “catalyst support”, refers to conventional materials that are typically a solid with a high surface area, to which catalyst materials are affixed. Support materials may be inert or participate in the catalytic reactions, and may be porous or non-porous. Typical catalyst supports include metal oxides, various kinds of carbon, alumina, silica, and silica-alumina, e.g., amorphous silica aluminates, zeolites, alumina-boria, silica-alumina-magnesia, silica-alumina-titania and materials obtained by adding other zeolites and other complex oxides thereto.

Properties of the materials described herein may be determined as follows:

“Cut point” refers to the temperature on a True Boiling Point (TBP) curve at which a predetermined degree of separation is reached.

“Pour point” refers to the temperature at which an oil will begin to flow under controlled conditions. The pour point may be determined by, for example, ASTM D5950.

“Cloud point” refers to the temperature at which a lube base oil sample begins to develop a haze as the oil is cooled under specified conditions. The cloud point of a lube base oil is complementary to its pour point. Cloud point may be determined by, for example, ASTM D5773.

“Viscosity index” (VI) is an empirical, unit-less number indicated the effect of temperature change on the kinematic viscosity of the oil. The higher the VI of a base oil, the lower its tendency to change viscosity with temperature. VI is determined according to ASTM D2270.

“Kinematic viscosity” at a specified temperature is determined according to ASTM D445.

For the purposes of this specification and appended claims, unless otherwise indicated, all numbers expressing quantities, percentages or proportions, and other numerical values used in the specification and claims, are to be understood as being modified in all instances by the term “about.” Accordingly, unless indicated to the contrary, the numerical parameters set forth in the following specification and attached claims are approximations that can vary depending upon the desired properties sought to be obtained. It is noted that, as used in this specification and the appended claims, the singular forms “a,” “an,” and “the,” include plural references unless expressly and unequivocally limited to one referent. As used herein, the term “include” and its grammatical variants are intended to be non-limiting, such that recitation of items in a list is not to the exclusion of other like items that can be substituted or added to the listed items. As used herein, the term “comprising” means including elements or steps that are identified following that term, but any such elements or steps are not exhaustive, and an embodiment can include other elements or steps.

Unless otherwise specified, the recitation of a genus of elements, materials or other components, from which an individual component or mixture of components can be selected, is intended to include all possible sub-generic combinations of the listed components and mixtures thereof. In addition, all number ranges presented herein are inclusive of their upper and lower limit values.

The patentable scope is defined by the claims, and can include other examples that occur to those skilled in the art. Such other examples are intended to be within the scope of the claims if they have structural elements that do not differ from the literal language of the claims, or if they include equivalent structural elements with insubstantial differences from the literal languages of the claims. To an extent not inconsistent herewith, all citations referred to herein are hereby incorporated by reference.

General Process and System

The application pertains to alternating hydroprocessing processes and systems wherein renewable lipid-derived products and hydrocracked petroleum-derived or fossil products may advantageously be produced using substantially the same equipment and catalysts. In this manner, the commercial plant has flexibility to change product mixes depending upon, for example, available feedstocks and/or commercial reasons such as prices of raw materials or products. This may be accomplished without catalyst changes, significant equipment reconfiguration, or major process disruptions.

The process generally comprises reacting a lipid or a mixture of lipid and petroleum feedstock with hydrogen in the presence of a catalyst in a vessel under conditions suitable to form a renewable diesel product. The formed renewable diesel product is then removed from the vessel and a petroleum feedstock is reacted with hydrogen in the presence of the catalyst in the same vessel under conditions suitable to form a hydrocracked product.

The system generally comprises a reactor, a catalyst, a lipid feed, a petroleum feedstock feed, a hydrogen feed, and a catalyst. Appropriate process control equipment are employed to provide alternating conditions suitable to form a renewable diesel product and a hydrocracked product.

The process steps, reactants, catalysts, reaction conditions, and system components are described in additional detail below.

Lipid and Reaction Conditions

The lipid employed may vary depending on, for example, the properties desired for the renewable product and/or the specific catalyst or equipment to be employed. Generally, the specific lipid is not particularly critical so long as it is capable of being hydroprocessed to a renewable product using suitable catalyst and hydrocracking equipment. In some embodiments suitable renewable products are substantially free or free of O2 and/or other heteroatoms such that the renewable product may be upgraded to, for example, a diesel product in a subsequent processing step.

Suitable lipids that may be employed include, for example, a vegetable oil including, but not limited to, used cooking oil, seed oils, an animal fat, a waste oil, an algae oil, or any mixture thereof. In some embodiments a useful lipid comprises an oil selected from canola oil, soybean oil, or any mixture thereof. Other examples of suitable lipids comprise plant-based oils and fats that include vegetable oils and fats, such as rapeseed (canola) oil, soybean oil, coconut oil, sunflower oil, palm oil, palm kernel oil, peanut oil, linseed oil, colza oil, tall oil, corn oil, castor oil, jatropha oil, jojoba oil, olive oil, flaxseed oil, hempseed oil, cottonseed oil, camelina oil, safflower oil, mustard oil, carinata oil, cuphea oil, curcas oil, crambe oil, babassu oil, rapeseed oil, peanut oil, rice bran wax, carnauba wax, rice bran oil, or any mixture or combination thereof. Animal oils and fats, and other sources, include beef fat (tallow), hog fat (lard), turkey fat, fish fat/oil, and chicken fat), yellow and brown greases, including algae and fish fats/oils, fats in milk, sewage sludge, and the like may also be employed.

In some embodiments a useful lipid comprises a treated oil wherein the treatment is such that the catalyst employed is not substantially deactivated and/or is deactivated not substantially more than when the catalyst is employed for hydrotreating or hydrocracking petroleum products. Such treated oil may comprise an oil that is refined, bleached, deodorized, or any combination thereof. Thus, in some embodiments the oil comprises a treated oil with less than about 2 ppm phosphorus, less than about 1 ppm.

In some embodiments the lipid may further comprises a petroleum feedstock portion or hydrocracked product portion.

Generally, the equipment, e.g., reactor, and catalyst employed for forming the renewable product or products from the lipid are substantially the same as those described below in regard to the hydrocracking unit and catalyst.

The conditions for making the renewable product or products differ from those of making the hydrocracked products from petroleum feedstocks. The conditions may vary depending upon such factors as the lipid, catalyst, and equipment employed but generally suitable conditions to form a renewable diesel product comprise a lower temperature than the conditions used to form a hydrocracked product. That is, in some embodiments the conditions suitable to form a renewable product comprise a temperature at least about 50, or at least about 100, or at least about 125, or at least about 150° F. lower than the conditions suitable to form a hydrocracked product.

While the temperatures are generally lower, other reaction conditions for the lipid may be similar to hydrocracking petroleum. For example, in some embodiments, the conditions suitable to form the renewable product may comprise mixing (mechanical mixing, liquid recirculation, gas bubbling, and the like), a temperature range of from about 350-700° F. (lower than hydrocracking), a reactor pressure of about 500-4000 psig, an average residence time of from 10 min to 10 hrs, and/or a space velocity of about 0.2 to 10.0.

Petroleum Feedstock and Hydrocracking Conditions

The petroleum feedstock is not particularly limited and a broad variety of petroleum feedstocks, i.e., hydrocarbonaceous feedstocks, may be used. Suitable hydrocarbonaceous feeds generally include heavy gas oil, an FCC cycle oil, a deasphalted oil, a coker gas oil, or any mixture thereof. In addition, feedstocks suitable for light and middle distillate production may be employed, including, e.g., feeds comprising gasoline, kerosene, gas oils, vacuum gas oils, long residues, vacuum residues, atmospheric distillates, heavy fuels, oils, waxes and paraffins, used oils, deasphalted residues or crudes, charges resulting from thermal or catalytic conversion processes, or a combination thereof.

Typical physical properties for useful hydrocarbon feedstocks are shown in the table below.

	Property	Value Range
	API Gravity	10-35.0
	N, ppm	0.5-2,000
	S, ppm	0-100
	Polycyclic Index (PCI)	10-2000
	TBP Range, ° F. (° C.)	700-1200° F. (371-649° C.)

In some embodiments the petroleum feedstock may further comprises a lipid portion and/or a renewable portion

In some embodiments suitable liquid feedstock may comprise a heavy boiling point component having a boiling point of at least about 800° F. For example, while not limited thereto, the liquid feedstock may typically be selected from vacuum gas oil, atmospheric resid, vacuum resid, FCC heavy cycle oil or decanted oil, FCC medium cycle oil, hydrocracker unconverted oil, or a combination thereof. The heavy boiling point component having a boiling point of at least about 800° F. may be present in the liquid feedstock in an amount of up to about 50 wt. %, or 40 wt. %, or 30 wt. %, or 20 wt. %, or 10 wt. %, or in the range from about 10-50 wt. %, or 10-40 wt. %, or 10-30 wt. %, or 20-30 wt. %. The liquid feedstock may comprise one or more components having a high boiling point of at least about 650° F., or 675° F., or 700° F., or 725° F., or 750° F. The amount of the liquid feedstock component having a high boiling point present in the liquid feedstock may be at least about 10 wt. %, or 20 wt. %, or 30 wt. %, or 40 wt. %, or 50 wt. %, or 60 wt. %, or 70 wt. %, or 80 wt. %, or 90 wt. % of the liquid feedstock.

Useful hydrocracking process conditions are shown in the table below.

Process Condition	Value Range
Liquid Hourly Space Velocity	0.1-5

(LHSV), hr − 1
H2 partial pressure, psig (kPa)	800-3,500	(5516-24,132)

H2 Consumption Rate, SCF/B	200-2,000
H2 Recirculation Rate, SCF/B	50-8,000

Operating Temperature, ° F. (° C.)

392-842° F.

(200-450° C.)

Conversion (wt. %)	20-80

Conditions suitable to form the hydrocracked fossil product may comprise mixing, a temperature range of from about 650-950° F., a reactor pressure of about 300-3000 psig, an average residence time of from 10 min to 10 hrs, and a space velocity of about 0.1 to 5.0.

Catalyst

The catalyst used for both the lipid reaction and the petroleum feedstock reaction is generally the same catalyst and may in some embodiments be selected for the mix of hydrocracked products desired. The catalyst may be a hydrocracking or hydroprocessing catalyst. The catalyst usually comprises a support and one or more transitional metals. The support usually comprises alumina, a zeolite, an amorphous silica-alumina, a clay, or any combination thereof. The one or more transitional metals comprises iron, cobalt, nickel, ruthenium, rhodium, palladium, osmium, iridium, platinum, molybdenum, tungsten or any combination thereof. In some embodiments the one or more transitional metals comprises a combination of molybdenum and tungsten

The catalyst may also comprise additional components, including matrix materials, also referred to as supports, zeolites, promoters, and the like. Suitable matrix materials generally include silica, alumina, amorphous silica-alumina (ASA), ceria, titania, magnesia, thoria, zirconia, or a combination thereof. In more particular aspects, the matrix material may be selected from alumina, amorphous silica-alumina (ASA), or a combination thereof. Other examples of the support materials include alumina-boria, silica-alumina-magnesia, silica-alumina-titania and materials obtained by adding zeolites and other complex oxides thereto. In some cases, the support material may be porous, and comprise a natural clay or a synthetic oxide. The support material can also be selected to provide adequate mechanical strength and chemical stability at the reaction conditions under which the catalyst is used. In some cases, the support material may comprise a pseudo-boehmite alumina, such as CATAPAL® high purity aluminas (CATAPAL® is a registered trademark of SASOL), while suitable amorphous silica-aluminas include SIRAL® (SIRAL® is a registered trademark of SASOL).

Zeolites may also be included in the catalyst, including, e.g., Y, USY, beta zeolites, and any combination thereof. Promoters such as silicon, boron, phosphorus, fluorine, aluminum, zinc, manganese, or a combination thereof may be included in the catalyst as well. The amount of promoter in the catalyst can be from 0 wt. % to 10 wt. % based on the bulk dry weight of the catalyst. In some cases, the amount of promoter in the catalyst may be from 0.1 wt. % to 5 wt. % based on the bulk dry weight of the catalyst.

The catalyst is generally in the form of extruded pellets (extrudates) that have an extruded pellet diameter of 10 mm or less, such as from 1.0 to 5.0 mm. In some cases, the extruded pellet may have a length-to-diameter ratio of 10 to 1. Examples of other types and sizes of pellets used for the catalysts are 1 to 10 mm diameter spheres; 1 to 10 mm diameter cylinders with a length-to-diameter ratio of 4 to 1; 1 to 10 mm asymmetric shapes (including quadrilobes), and up to 10 mm diameter hollow cylinders or rings.

Hydrocracking Units, i.e., Reactors

As described above the processes and systems employ the same reactor, i.e., hydrocracking unit, for processing the lipids and the petroleum. In some cases, the hydrocracking unit comprised one or more fixed catalyst beds in a single stage hydrocracking unit, i.e., reactor, with or without recycle (once-through operation). Such a single-stage hydrocracking unit may employ multiple single-stage units operated in parallel. In other cases, the catalyst may be deployed in one or more beds or units in a two-stage hydrocracking unit, with and/or without intermediate stage separation, and with or without recycle. Two-stage hydrocracking units may be operated using a full conversion configuration (meaning all of the hydrotreating and hydrocracking is accomplished within the hydrocracking loop via recycle). One or more distillation units may also be used within the hydrocracking loop to strip off product prior to second stage hydrocracking or prior to recycle of the distillation bottoms back to the first and/or second stage.

Two stage hydrocracking units can also be operated in a partial conversion configuration, such that one or more distillation units may be positioned within a hydrocracking loop to strip off one or more streams that are then passed on for further hydroprocessing. Operation of the hydrocracking unit in this manner allows highly disadvantaged feedstocks to be hydroprocessed by allowing undesirable feed components such as the polynuclear aromatics, nitrogen and sulfur species to pass out of the hydrocracking loop for further processing under more suitable conditions.

These and other objects, features and advantages of the exemplary embodiments of the present disclosure will become apparent upon reading the following detailed description of the exemplary embodiments of the present disclosure, when taken in conjunction with the appended claims.

EXAMPLE 1—HYDROCRACKING CONVENTIONAL PETROLEUM FEED

A conventional petroleum feed is hydrocracked using the conditions described in the table below.

EXAMPLE 2—RENEWABLE DIESEL FROM SOYBEAN OIL IN THE SAME REACTOR WITH THE SAME CATALYST

After the hydrocracking product of Example 1 was removed from the reactor, soybean oil was fed into the same reactor with the same hydrocracking catalyst. The soybean oil was blended at 25% by volume with renewable diesel product to simulate product recycling for exotherm mitigation purposes. A reaction temperature of 559° F., clearly lower than that required for processing the petroleum derived feedstock, was employed to completely convert fresh soybean oil into a renewable hydrotreated product using the conditions described in the table below. Oxygen removal from the lipid can be considered complete, as evidenced by the absence of oxygen in the renewable hydrotreated product.

EXAMPLE 3—HYDROCRACKING CONVENTIONAL PETROLEUM FEED

Following the removal of the renewable diesel from the reactor in Example 2, another conventional petroleum feed is hydrocracked using the conditions described in the table below.

Example 1-3 Reaction Conditions and Results

The tables below show the reaction conditions and results for Examples 1-3. From experimental data, the normalized hydrocracking reaction temperature for a target conversion of 66% wt., was 760° F. for Example 1 and 762° F. for Example 3. The required temperature for Example 3 agrees well with the projected temperature using the experimental catalyst aging rate found on Example 1, and the product yields were the same before and after processing the lipid feedstock. Thus, the lipid hydroprocessing on Example 2 had no detrimental effects on the hydrocracking catalyst system and that the same catalyst system was effective for lipid hydroprocessing and petroleum hydrocracking when operating at the appropriate conditions.

Hydrocracker Yields Before (Example 1) and after (Example 3) Lipid Hydroprocessing

	Example 1 - On Petroleum Feed	Example 3 - On Petroleum Feed
FEED	BEFORE Processing Soy	AFTER Processing Soybean Oil

Hour	8133	8157	8181	8205	9813	9981	10005	10029	10053
Average Temp., ° F.	760	760	760	760	762	762	762	762	762
LHSV	0.55	0.55	0.55	0.55	0.55	0.55	0.55	0.55	0.55
Tot. Press., psig	1850	1850	1850	1850	1850	1850	1850	1850	1850
Gas Rate, SCFB	4401	4397	4397	4398	4410	4411	4411	4412	4409
Conversion (<683°
F.), Wt %	66.1	66	65.83	65.8	65.99	66.06	65.97	65.8	65.99
No Loss Yields,
Wt %
Methane	0.35	0.35	0.35	0.35	0.34	0.35	0.34	0.35	0.34
Ethane	0.46	0.45	0.44	0.48	0.43	0.44	0.44	0.45	0.45
Propane	1.04	1.01	0.99	1.11	0.97	0.99	1.01	1.01	1.03
i-Butane	0.97	0.91	0.92	0.97	0.88	0.9	0.94	0.93	0.96
n-Butane	1.23	1.14	1.17	1.16	1.11	1.13	1.21	1.16	1.2

C5-180°	F.	5.32	5.25	5.02	4.97	4.92	5.01	5.26	5.04	5.05
180-250°	F.	5.89	6.01	5.97	5.95	6.06	6.07	5.99	6	6.05
250-550°	F.	40.33	40.2	40.21	40.31	40.34	40.22	40.1	40.14	40.16
550-700°	F.	23.33	23.13	23.22	23.07	23.08	23.19	23.13	23.2	23.15
700°	F.+	28.48	28.62	28.64	28.72	28.33	28.37	28.56	28.56	28.47

EXAMPLE 2—SOYBEAN OIL HYDROPROCESSING DATA

	Run hour	8997	9045	9069
	Average Temp., ° F.	559	559	559
	overall LHSV	1	1	1
	Tot. Press., psig	2300	2300	2300
	Gas Rate, SCFB	6043	6040	6043
	No-loss yields, wt. %
	C1	0.25	0.26	0.26
	C2	0.11	0.11	0.11
	C3	4.77	4.96	4.64
	C4	0.05	0.04	0.07
	naphtha	0.06	0.06	0.08
	diesel	85.08	84.47	85.90
	C5+	85.14	84.53	85.98
	H2O	11.85	11.86	11.80
	H2 cons, SCFB	2311	2320	2339
	Renewable product
	API gravity	48	48.1	48
	oxygen, wt. %	0	0	0
	Simdist, wt. %	F	F	F
	0.5/5	520/550	519/549	520/550
	10/30	552/603	551/602	551/603
	50	604	605	605
	70/90	606/607	607/608	606/607
	95/99.5	607/775	609/788	607/718

These results show effective block operation in a hydrocracker, alternating the processing of petroleum and of renewable feeds without having to change catalysts, sacrifice yields or introduce additional catalyst deactivation.

Specific Embodiments

Specific embodiments are described in the numbered embodiments below.

1. An alternating hydroprocessing process comprising:

• • reacting a lipid with hydrogen in the presence of a catalyst in a vessel under conditions suitable to form a renewable hydrocarbonaceous product; and
  • removing the formed renewable hydrocarbonaceous product from the vessel; and reacting a petroleum feedstock with hydrogen in the presence of the catalyst in the vessel under conditions suitable to form a hydrocracked fossil product.

2. The process of embodiment 1 wherein the lipid comprises a vegetable oil, an animal fat, an algae oil, or any mixture thereof.

3. The process of embodiment 1 wherein the lipid comprises an oil selected from canola oil, soybean oil, or any mixture thereof.

4. The process of embodiment 1 wherein the petroleum feedstock comprises a heavy gas oil, an FCC cycle oil, a deasphalted oil, a coke gas oil, or any mixture thereof.

5. The process of embodiment 1 wherein the conditions suitable to form a renewable diesel product comprise a lower temperature than the conditions suitable to form a hydrocracked product.

6. The process of embodiment 1 wherein the conditions suitable to form a renewable diesel product comprise a temperature at least about 100 F lower than the conditions suitable to form a hydrocracked product.

7. The process of embodiment 1 wherein the catalyst comprises a hydroprocessing catalyst.

8. The process of embodiment 1 wherein the catalyst comprises a hydrocracking catalyst.

9. The process of embodiment 1 wherein the catalyst comprises a support and one or more transitional metals.

10. The process of embodiment 9 wherein the support comprises alumina, a zeolite, an amorphous silica-alumina, a clay, a metal oxide or any combination thereof.

11. The process of embodiment 9 wherein the one or more transitional metals comprises iron, cobalt, nickel, ruthenium, rhodium, palladium, osmium, iridium, platinum, molybdenum, tungsten or any combination thereof.

12. The process of embodiment 11 wherein the one or more transitional metals comprises a combination of molybdenum and tungsten.

12. The process of embodiment 1 wherein the hydrocracked product comprises gasoline, jet fuel, light gas oil, diesel, base oils or any combination thereof.

13. The process of embodiment 1 wherein the lipid further comprises a petroleum feedstock.

14. The process of embodiment 1 wherein the petroleum feedstock further comprises a lipid.

15. The process of embodiment 1 wherein the conditions suitable to form the hydrocracked fossil product comprise mixing, a temperature range of from about 650-950° F., a reactor pressure of about 300-3000 psig, an average residence time of from 10 min to 10 hrs, and a space velocity of about 0.1 to 5.0.

16. The process of embodiment 1 wherein the conditions suitable to form the renewable product comprise mixing, a temperature range of from about 350-700° F., a reactor pressure of about 500-4000 psig, an average residence time of from 10 min to 10 hrs, and a space velocity of about 0.2 to 10.0.

17. A system comprising a reactor, a catalyst, a lipid feed, a petroleum feedstock feed, a hydrogen feed, a catalyst, and process control equipment to provide alternating conditions suitable to form a renewable product and a hydrocracked product.

18. The system of embodiment 17 wherein the process control equipment provide conditions suitable to form a hydrocracked fossil product comprise mixing, a temperature range of from about 650-950° F., a reactor pressure of about 300-3000 psig, an average residence time of from 10 min to 10 hrs, and a space velocity of about 0.1 to 5.0.

19. The system of embodiment 17 wherein the process control equipment provide conditions suitable to form a renewable product comprise mixing, a temperature range of from about 350-700° F., a reactor pressure of about 500-4000 psig, an average residence time of from 10 min to 10 hrs, and a space velocity of about 0.2 to 10.0.

In the preceding specification, various embodiments have been described with references to the accompanying drawings. It will, however, be evident that various modifications and changes may be made thereto, and additional embodiments may be implemented, without departing from the broader scope of the invention as set forth in the claims that follow. The specification and drawings are accordingly to be regarded as an illustrative rather than restrictive sense.