Ebullated bed platform for the processing of renewable and circular feedstocks

Abstract

Provided is a process for processing circular feedstocks, renewable feedstocks, or a mix of both renewable and circular feedstocks in an ebullated bed (EB) reactor. At least a portion of the renewable and / or circular feedstocks is added to the EB reactor above its catalyst grid, while a sufficient amount of the feedstocks is injected at the bottom of the EB reactor to create the fluidized bed.

Description

Attorney Docket No. 70205.0696WOU1 (T-12449-P2-WO01)EBULLATED BED PLATFORM FOR THE PROCESSING OF RENEWABLE AND CIRCULAR FEEDSTOCKSCROSS-REFERENCE TO THE RELATED APPLICATION

[0001] This application claims the benefit of U.S. Provisional Patent Application No. 63 / 725,847, filed November 27, 2024, the disclosure of which is hereby incorporated in its entirety.TECHNICAL FIELD

[0002] The present process relates to efficiently using an EB reactor platform in producing fuels from circular and renewable feedstocks.BACKGROUND

[0003] The production of fuels from non-fossil feedstock is becoming more and more important in reducing the fossil carbon footprint and tackling climate change. The industry is in need of new, useful, and more efficient processes for addressing the treatment of circular and renewable feedstocks. Ebullated Bed (EB) reactor platforms, such as LC-FINING, are widely used to hydrocrack heavy fossil oil feedstock, but have never been applied to the processing of renewable and circular feedstocks. To provide novel and more efficient processes for processing renewable and circular feedstocks to produce transportation fuels would be of great interest to the industry.SUMMARY OF THE INVENTION

[0004] Against this backdrop the present invention was developed. The present process provides a new, useful, and efficient process of transforming circular, renewable, or a mix of circular and renewable feedstock into fuel. The process utilizes an EB reactor where a circular, renewable, or a mix of circular and renewable feedstock is added to the reactor for hydrotreatment. The feedstock is injected at both the bottom of the EB reactor, below the catalyst grid, and above the catalyst grid.

[0005] Among other factors, it has been found that feeding 100% circular or renewable feedstocks, or a mixture thereof, to an EB reactor can result in effective, efficient, and complete conversion of the circular or renewable feedstocks into hydrocarbon products. The key is the use of an EB reactor, and the points of injection of the feedstocks. By injecting at least some of the renewable and / or circular feedstockAttorney Docket No. 70205.0696WOU1 (T-12449-P2-WO01) above the catalyst grid in the EB rector, while still injecting sufficient renewable and / or circular feedstock at the bottom of the EB reactor, the process can proceed smoothly and efficiently. The hydrocarbon products can then be separated into various cuts of different fuels or further refined to a finished fuel. Products such as base oils, gasoline, diesel fuel, and jet fuel can ultimately be obtained via the EB reactor. Surprisingly it has been discovered that no petroleum feed needs to accompany the circular or renewable feedstocks to the EB reactor. This results in expedient conversion of the circular and / or renewable sources, which is beneficial to the industry.

[0006] The present process offers a new efficient method of addressing the need to produce fuel from non-fossil feedstocks.BRIEF DESCRIPTION OF THE FIGURE

[0007] The Figure depicts one embodiment of the present process.DETAILED DESCRIPTION

[0008] Before the present processes for producing fuel from non-fossil feedstocks are disclosed and described, it is to be understood that this disclosure is not limited to the particular structures, process steps, or materials disclosed herein, but is extended to equivalents thereof as would be recognized by those ordinarily skilled in the relevant arts. It should also be understood that terminology employed herein is used for the purpose of describing particular embodiments only and is not intended to be limiting. It must be noted that, as used in this specification, the singular forms "a," "an," and "the" include plural referents unless the context clearly dictates otherwise. Thus, for example, reference to "a step" may include multiple steps, reference to "producing" or "products" of a reaction or treatment should not be taken to be all of the products of a reaction / treatment, and reference to "treating" may include reference to one or more of such treatment steps. As such, the step of treating can include multiple or repeated treatment of similar materials / streams to produce identified treatment products.

[0009] Numerical values with "about" include typical experimental variances. As used herein, the term "about" means within a statistically meaningful range of a value, such as a stated particle size, concentration range, time frame, molecular weight, temperature, or pH. Such a range can be within an order of magnitude, typically within 10%, and more typically within 5% of the indicated value or range. Sometimes, such a range can be within the experimental error typical of standard methods used for theAttorney Docket No. 70205.0696WOU1 (T-12449-P2-WO01) measurement and / or determination of a given value or range. The allowable variation encompassed by the term "about" will depend upon the particular system under study, and can be readily appreciated by one of ordinary skill in the art. Whenever a range is recited within this application, every whole number integer within the range is also contemplated as an embodiment of the invention.

[0010] Central to the present process is the ebullated bed (EB) reactor. The functioning of the EB reactor, including the recycling of reactor liquids upwards through the stirred bed of catalyst, is generally well known. A mixture of feedstock and hydrogen is passed from the bottom upwards over a bed of catalytic particles at a flow rate such that the particles are subjected to a forced random motion whereas the liquid and gas pass through the bed from the bottom upwards. The movement of the catalytic bed is controlled by a flow of recycle liquid so that, in the steady state, the mass of the catalyst does not rise above a definable level in the reactor. Vapors and liquid being hydrogenated pass through the upper level of the bed of catalytic particles to reach a zone substantially free of catalyst, and they are then discharged from the upper part of the reactor. A fraction of the reactor liquids can be continuously recycled into the reactor.

[0011] EB reactor technologies use supported catalysts, generally in the form of extrudates or beads whose diameter is generally of the order of 1, or less than 1, mm. The catalysts are supported on a catalyst grid, which the feeds and gases flow upward. The catalysts remain inside the reactors and are not discharged with the products. The catalytic activity can be kept constant by online replacement of the catalyst. It is thus not necessary to shut down the unit in order to change the spent catalyst, or to increase the reaction temperatures along the cycle in order to compensate for deactivation. Furthermore, working under constant operating conditions makes it possible to obtain constant product yields and qualities along the cycle. Also, because the catalyst is kept in agitation by a significant recycling of liquid, the pressure drop on the reactor remains low and constant and the reaction exotherms are rapidly averaged over the catalytic bed.

[0012] In one embodiment the spent catalyst is partly replaced with fresh catalyst by withdrawal from the bottom of the reactor and introducing, either at the top of the reactor or at the bottom of the reactor, fresh or new catalyst at regular time intervals, for example in bursts or almost continuously.Attorney Docket No. 70205.0696WOU1 (T-12449-P2-WO01)

[0013] Fresh catalyst can be introduced, for example, every day. The rate of replacement of the spent catalyst with fresh catalyst will be based on the particular reaction run and catalyst used. The required rate can be easily monitored, as is known in the industry. This withdrawal and this replacement are performed using devices which enable continuous functioning of this hydro conversion step. The unit usually includes an internal recirculation pump for maintaining the catalyst in an ebullated bed by continuous recycling of at least a portion of the liquid withdrawn at the top of the reactor and reinjected into the bottom of the reactor. It is also possible to send the spent catalyst withdrawn from the reactor to a regeneration zone, in which the carbon and sulfur which it contains are removed, and then to return this regenerated catalyst into the hydro conversion step. It is also possible to send the regenerated catalyst to a rejuvenation zone in which a treatment is performed aimed at improving the activity of the catalyst (presulfurization, additivation, etc.), then to return this rejuvenated catalyst into the hydro conversion step.

[0014] A fluidized bed reactor, such as an ebullating bed reactor, is well-suited to handle many of the difficulties associated with processing a renewable and / or circular feedstocks. For example, renewable feeds typically contain a large amount of oxygen that may need to be removed in order to make a suitable fuel. Ebullating bed reactors can tend to have an advantage in that gases such as hydrogen are typically well mixed throughout the fluidized bed. This effective mixing may reduce the amount of excess hydrogen needed in order to achieve full reaction with the oxygen in the renewable feed. Removing oxygen from a renewable feed is also an exothermic reaction, which has the potential to overwhelm the temperature control systems of a standard hydrotreatment reactor. In addition to the mixing advantages of a fluidized bed, which should minimize hot spots within the bed, ebullating bed reactors also typically operate with a recycle loop. Recycling of the feed can tend to dampen any temperature increase due to reaction with a high oxygen content feedstock.

[0015] In the present process, renewable and / or circular feedstock is also injected above the catalyst grid. To facilitate use of lower quality feeds in the processes according to the invention, a modified ebullating bed reactor can be used. In a conventional ebullating bed reactor, both the feedstock and the treat gas (e.g., hydrogen) are typically introduced into the reactor from the bottom. A recycled feed containing a portion of the reactor effluent is also optionally but typically introduced into the bottom of the reactor. These streams typically flow upward into the reactor andAttorney Docket No. 70205.0696WOU1 (T-12449-P2-WO01) pass through a catalyst support grid. The catalyst support grid is designed to inhibit / prevent catalyst from entering the areas at the bottom of the reactor where the feed pumps are located. The catalyst in the ebullating bed reactor is generally located above the catalyst support grid.

[0016] When the feedstock and gas flows reach the catalyst bed, the bed typically becomes fluidized, leading to expansion of the size of the bed as well as to mixing within the bed. The feed(s) and treat gas (hydrogen) typically react within the bed to form products, typically including liquid phase products and gas phase products. The flow in the reactor generally continues upward until an effluent is drawn off the reactor at the top. This gas phase effluent can typically be a combination of desired products, unreacted treat gas (hydrogen), and byproduct gases, generally including contaminant gases such as H2S or NH3 that were formed during the reaction. All, or more usually a portion, of the liquid phase effluent can be recycled to the bottom of the reactor. If desired, the gases can be separated from the liquid portion of the effluent that is not recycled.

[0017] In the present process, at least a portion of the renewable and / or circular feed to the ebullating bed reactor can be introduced at a location that is downstream from the catalyst support grid, i.e., above the catalyst grid. In a conventional ebullating bed design, introducing feed downstream from the catalyst support grid is not desirable, as such a feed would be less effective in creating the fluidized bed and flow patterns that are desired for proper ebullating bed operation. However, a sufficient amount of renewable feed and / or recycled feed can be introduced at the bottom of the reactor to overcome any fluidization and / or flow issues.

[0018] Catalysts used in an EB reactor are widely marketed. These are granular catalysts whose size never reaches that of the catalysts used in an entrained bed. The catalyst is usually in the form of extrudates or beads. Typically, they contain at least one hydro-dehydrogenating element deposited on an amorphous support. Generally, the supported catalyst comprises a group VIII metal chosen from the group formed by Ni, Pd, Pt, Co, Rh, and / or Ru, optionally a group of VIB metal chosen from the group Mo and / or W, on an amorphous mineral support chosen from the group formed by alumina, silica, silica-aluminas, magnesia, clays and mixtures of at least two of these minerals. CoMo / alumina and NiMo / alumina catalysts are the most common.

[0019] In step a) of the process according to the invention a circular, renewable, or a mix of circular and renewable feedstock is added to the EB reactor. CircularAttorney Docket No. 70205.0696WOU1 (T-12449-P2-WO01) feedstock is understood as generally referring to any feedstock that is considered as a waste or processing residue that has not been energetically used. In various embodiments of the present invention circular feedstock comprises liquified waste plastic (LWP), plastic pyrolysis oil, tire-derived oil (TDO), waste plastics, and any combinations thereof. Renewable feedstock is understood generally as referring to any feedstock that replenishes itself during certain processes. In various embodiments of the present process the renewable feedstock comprises bio crudes such as fast-pyrolysis bio-oil (pyoil or FPBO) and hydrothermal liquefaction oil (HTL oil), lipids such as vegetable oils, used cooking oil, tallow, animal fats and greases, bio-residual oils from other conversion process, or any combinations thereof. A mix of circular and renewable feedstocks is understood generally as referring to any combination of circular and renewable feedstocks. In various embodiments the mix of circular and renewable feedstocks comprises a combination of at least one of any circular and at least one of any renewable feedstocks disclosed in any aforementioned embodiment. For a mixture of renewable and circular feedstocks, there is no ratio limitation.

[0020] In one embodiment, an optional pretreatment step can occur prior to step a). In this pretreatment step, the circular, renewable, or mix of circular and renewable feedstocks are pretreated physically or chemically via filtration, water washing, hydrothermal cleanup, or mild-hydrotreating. This enables the removal of large solids or contaminants from the circular, renewable, or mix of circular and renewable feedstocks and stabilizes said feedstocks by saturating the olefins.

[0021] In the present process the feed composition of the circular, renewable, or mix of circular and renewable feedstocks is not limited in the proportion of circular or renewable material in the feedstock. The total feedstock comprises circular and / or renewable materials. Thus, the process has been found to be quite effective in processing large amounts of circular and renewable materials into fuels. There is also no limit regarding the ratio of circular feedstock to renewable feedstock. The total feedstock can be circular feedstock, renewable feedstock, or a mix of the two in any ratio. As discussed above, however, the present process does inject at least a portion of the renewable and / or circular feed above the catalyst grid of the EB reactor.

[0022] In step b) of the present process a reaction step is performed in the EB reactor wherein the feedstocks from step a) are exposed to hydrogen and an EB reactor catalyst. In some embodiments the reaction in step b) comprises hydrogenation, hydrocracking, hydrodesulfurization, hydrodenitrogenization, hydrodemetallization,Attorney Docket No. 70205.0696WOU1 (T-12449-P2-WO01) hydrodeoxygenation, decarbonylation, or decarboxylation, depending on the catalyst used. Preferable processing conditions involve a liquid hourly space velocity of 0.1 to 1 hr-1, pressure in the range of 800 - 3000 psig, temperature of 650 to 850 °F, and a H2 to feed ratio in the range of 1000-8000 SCF / bbl.

[0023] In one embodiment, unreacted hydrogen can be recycled back to the frontend reactor. Such recycling of the hydrogen can greatly improve the overall efficiency of the process.

[0024] In step c) of the present process, a separation step is performed to separate the products of step b) into heavy and light hydrocarbon products. This is generally achieved by fractionation, as is known in the industry. The number of cuts of hydrocarbon products can vary and will depend on the ultimate product goal of the reaction.

[0025] In one embodiment a hydrotreatment step d) occurs. In this hydrotreatment step distillate and vacuum gas oil (VGO) products can be further hydrotreated in an integrated hydrotreater. Doing so further removes contaminates such as sulfur, nitrogen, and oxygen. In another embodiment after the optional hydrotreatment step d) occurs, hydrotreated VGO can be further hydrocracked in a hydrocracker or fluid catalytic cracking (FCC) process after separation. In some embodiments the separation process can be fractionation.

[0026] In some embodiments, isomerization may be subsequently needed. In one embodiment isomerization is used to produce jet and diesel products.

[0027] In some embodiments, the heavy product can be further refined by the separation of heavy liquid and solid in the heavy product. This can be achieved via filtration, centrifugation, and other similar processes.

[0028] In one embodiment of the present process, bio-oils containing conjugated diolefins and having a Maleic Diene value over 1.2 are added to a first stage reactor. Because bio-oils with conjugated diolefins tend to polymerize at elevated temperature and cause plugging issue when feeding to a reactor, it may be desirable to saturate them with H2 to remove most diolefins in a first stage reactor to form a stabilized bio-oil. This will remove the problematic diolefins. In one embodiment operating conditions for this first stage reactor are from about 120-300°C and from about 300-3000 psig.

[0029] From here, the bio-oil can be fed to the next stage EB reactor containing hydroprocessing catalyst with a Eb-rich gas. A lipid feedstock FOG (fat, oil and grease) can be co-fed to the same reactor to remove most of the oxygen in the feedstock at mildAttorney Docket No. 70205.0696WOU1 (T-12449-P2-WO01) operating condition. In one embodiment operating conditions for the EB reactor can comprise from about 250-400 °C, 500-3000 psig, LHSV at 0.1-3.0 hr- 1, Eb rate at 2500-10000 SCF / bbl. The process is efficient in contaminant removals, which can remove > 70% oxygen and >90% combined P and metal contaminants. Sulfiding agent can also be added in this stage to maintain a EbS / fccd ratio at 100 ppm or higher.

[0030] The effluent from the EB reactor can then be separated in an overhead stream containing CO, CO2, water, C1-C4 and light hydrocarbons with boiling point< 370°C, and a heavy stream containing mainly 370°C+ oil. This heavy oil stream along with an Fb-rich gas can be sent to a third stage with a hydrocracking catalyst, where a heavy plastic pyrolysis oil stream can be injected. It may be desirable to operate the stage three reactor about at least 20°C hotter than the EB reactor. In one embodiment the operating condition comprise from about 350-450°C, 1000-3000 psig, LHSV at 0.1 -3.0 hr-I, H2 rate at 2500-10000 SCF / bbl. This stage can achieve >90% or near complete hydrodeoxygenation (HDO) and significant cracking, with >60% 370°C+ in the product. Here another sulfiding agent can be added to maintain a FbS / feed ratio at 100 ppm or higher. The effluent from this third stage reactor can be separated in an overhead stream containing CO, CO2, water, light hydrocarbons with boiling point< 370°C, and a heavy stream containing mainly 370°C+ oil.

[0031] In one embodiment the heavy stream from the third stage reactor can be recycled back to said third stage reactor to complete hydrocracking. In another embodiment this heavy stream can be further passed by a separator to separate the gas product (CO, CO2, H2O, C1-C4) with light oil (370°C+). In yet another embodiment the light oil (370°C) can be sent to a fixed-bed hydroprocessing reactor with two types of catalysts. A first layer (contacting liquid first) with 5-20% hydrotreating catalyst to eliminate contaminants such as oxygen and nitrogen completely or almost completely, and a second layer with an isomerization catalyst to convert n-paraffins into isoparaffins. In still another embodiment, a further separation and fraction step to separate the light oil into gaseous products and drop-in renewable fuels (gasoline, suitable aviation fuel (SAF), and renewable diesel) can occur.

[0032] Now discussing the drawing of the present application, the Figure of the Drawing depicts one embodiment of the present process. Unstable feedstocks 1001 are fed along with H2 1002 to a first stage reactor 1003, where they are stabilized. In one embodiment, the feedstocks comprise fast pyrolysis bio-oil (FPBO), HTL oil tall oils or tall oil pitch, etc., with bio-oils that are compatible and which may contain someAttorney Docket No. 70205.0696WOU1 (T-12449-P2-WO01) diolefins which tends to polymerize at elevated temperatures. In one embodiment, the feed comprises bio-oil, with di-olefin content > 0.5 wt%; O > 10 wt%; TAN (total acid number) > 20. The reactor is run at P:500-3000 psig and T: 120-300°C. The Stage 1 reactor 1003 provides stabilization of the unstable feedstocks 1001.

[0033] The stabilized products 1004 are passed to an ebullated bed reactor 1005, along with a FOG (fat, oil and grease) feedstock 1006. The Stage 2 reactor 1005 is generally an EB reactor run under mild conditions to perform HDO. In one embodiment, the pressure ranges from 500-3000 psig and the temperature ranges from 250-600°C, with the HDO > 80%.

[0034] The EB effluent is passed through a hot separator 1007, where it is separated into a heavy stream 1008 and light stream 1009. The heavy stream 1008 is fed to a third stage reactor 1010 along with H2 1011 and heavy plastic pyrolysis oil 1012. The Stage 3 reactor is generally an EB reactor run under severe conditions to favor hydrocracking. In one embodiment, the conditions are a pressure in the range of 1000-3000 psig and a temperature of 350-450°C. The product content can comprise greater than 60% 360°C+ product. The HDO after Stage 3 reaction is generally greater than 90%.

[0035] The third stage reactor effluent is passed through a hot separator 1013. The heavy stream 1014 of the hot separator 1013 can in some embodiments be fed back to the third stage reactor 1010. The light stream 1015 combines with light stream 1009 after separation, creating combined light stream 1016. Combined light stream 1016 undergoes a separation step 1017, producing CO, CO2, H2O, and light hydrocarbons 1018 and effluent stream 1019. Effluent stream 1019 is passed through hydrotreating (HDT) 1020 and isomerizing (ISO) 1021 producing gasoline, SAF, and renewable diesel 1022. In one embodiment combined light stream 1016 can be passed to HDT 1024 as combined light stream 1023, and subsequently passed to ISO 1025 producing gasoline, SAF, and renewable diesel 1026.

[0036] The following examples are provided to further illustrate the present process. The examples are meant to be illustrative, but not limiting.Attorney Docket No. 70205.0696WOU1 (T-12449-P2-WO01)Examples 1-2

[0037] Provided are examples of suitable renewable and circular feedstocks for the present process.Maleic Diene value, the number of grams of iodine equivalent to the amount of maleic anhydride that reacts with 100 g of sample (based on 2 atoms of iodine per mole of maleic anhydride) under the specified reaction conditions.

[0038] Among other factors, it has been found that feeding 100% circular or renewable feedstocks to an EB reactor can result in effective, efficient, and complete conversion of the circular or renewable feedstocks into hydrocarbon products. The hydrocarbon product can then be separated into various cuts of different fuels or further refined to a finished fuel. Fuels such as base oils, gasoline, diesel fuel, and jet fuel can ultimately be obtained via the present process, all by via non-fossil feedstocks. Surprisingly it has been discovered that no petroleum feed needs to accompany the circular or renewable feedstocks to the EB reactor. This results in expedient conversion of the circular and / or renewable sources, which is beneficial to the industry.Attorney Docket No. 70205.0696WOU1 (T-12449-P2-WO01)

[0039] As used in this disclosure the word "comprises" or "comprising" is intended as an open-ended transition meaning the inclusion of the named elements, but not necessarily excluding other unnamed elements. The phrase "consists essentially of or "consisting essentially of is intended to mean the exclusion of other elements of any essential significance to the composition. The phrase "consisting of or "consists of is intended as a transition meaning the exclusion of all but the recited elements with the exception of only minor traces of impurities.

[0040] All patents and publications referenced herein are hereby incorporated by reference to the extent not inconsistent herewith. It will be understood that certain of the above-described structures, functions, and operations of the above-described embodiments are not necessary to practice the present invention and are included in the description simply for completeness of an exemplary embodiment or embodiments. In addition, it will be understood that specific structures, functions, and operations set forth in the above-described referenced patents and publications can be practiced in conjunction with the present invention, but they are not essential to its practice. It is therefore to be understood that the invention may be practiced otherwise that as specifically described without actually departing from the spirit and scope of the present invention as defined by the appended claims.

Claims

Attorney Docket No. 70205.0696WOU1 (T-12449-P2-WO01)What is claimed is:

1. A process for processing circular feedstocks, renewable feedstocks, or a mix of both circular and renewable feedstocks in an ebullated bed (EB) reactor, comprising: a) Providing bio-oil(s) to a first stage reactor; b) Feeding the product of said first stage reactor to an EB reactor, wherein the EB reactor comprises a hydroprocessing catalyst with a Eb-rich gas; c) Co-Feeding a lipid feedstock to said EB reactor; d) Maintaining an EB reactor EbS / feed ratio at about 100 ppm or higher by adding a sulfiding agent to said EB reactor; e) Separating an effluent from said EB reactor in an overhead stream comprising CO, CO2, water, C1-C4 and light hydrocarbons with a boiling point of less than about 370°C, and a heavy stream comprising oil with a boiling point of greater than about 370°C; f) Sending said heavy stream to a third stage reactor comprising a hydrocracking catalyst; g) Maintaining a third stage reactor EbS / feed ratio at about 100 ppm or higher by adding another sulfiding agent to the third stage reactor; h) Injecting a heavy plastic pyrolysis oil stream into said third stage reactor; and i) Separating the effluent of said third stage reactor in an overhead stream comprising CO, CO2, water, C1-C4 and light hydrocarbons with a boiling point of less than about 370 °C, and a heavy stream comprising oil with a boiling point of greater than about 370 °C.

2. The process of claim 1 , wherein the heavy stream fraction of the effluent of the third stage reactor is recycled back to said third stage reactor to complete hydrocracking.

3. The process of claim 2, wherein the heavy stream fraction of the effluent of the third stage reactor further passes a separator to separate a gas product comprising CO, CO2, water, and C1-C4 hydrocarbons with a light oil product having a boiling point of about 370 °C.Attorney Docket No. 70205.0696WOU1 (T-12449-P2-WO01)4. The process of claim 3, wherein the light oil product is sent to a fixed bed hydroprocessor comprising a first layer with from about 5-20% hydrotreating catalyst and a second layer comprising an isomerization catalyst.

5. The process of claim 4, wherein a further separation and fraction step is used to separate the product of said fixed bed hydroprocessor into gaseous products and drop-in renewable fuels such as gasoline, sustainable aviation fuel, and renewable diesel.

6. The process of claim 1, wherein the bio-oils comprise conjugated diolefins and a maleic diene value greater than about 1.2.

7. The process of claim 1, wherein the first stage reactor is operated at a temperature of from about 120 - 130°C and a pressure from about 300-3000 psig.

8. The process of claim 1, wherein the EB reactor is operated at a temperature from about 250-400°C, a pressure from about 500-3000 psig, a LHSV at from about 0.1 -3.0 hr-1, and Hz rate at from about 2500 - 10000 SCF / bbl.

9. The process of claim 1, wherein the third stage reactor is operated at a temperature at least 20°C higher than said EB reactor but preferably from about 350- 450°C, a pressure of from about 1000-3000 psig, a LHSV of from about 0.1-3.0 hr-1, and an Hz rate of from about 2500-10000 SCF / bbl.

10. A process for processing circular feedstocks, renewable feedstocks, or a mix of both renewable and circular feedstocks in an ebullated bed (EB) reactor, comprising: a) adding one or more of the circular, renewable, or mix of circular and renewable feedstocks to an EB reactor, with at least a portion of the feedstock added above a catalyst grid in the reactor; b) performing a catalytic reaction in said EB reactor wherein the feedstocks from step a) are exposed to hydrogen and an EB catalyst; and c) separating products of step b) into heavy and light hydrocarbon products.Attorney Docket No. 70205.0696WOU1 (T-12449-P2-WO01)11. The process of claim 10, wherein before step a) the circular, renewable, or mix of circular and renewable feedstocks are pretreated physically or chemically.

12. The process of claim 10, wherein the circular feedstock comprises liquified waste plastic (LWP), plastic pyrolysis oil, tire-derived oil (TDO), or waste plastics.

13. The process of claim 10, wherein the renewable feedstock comprises bio crudes, lipids, or bio-residual oils from other conversion process.

14. The process of claim 13, wherein bio crudes comprise fast-pyrolysis bio-oil (pyoil or FPBO), or hydrothermal liquefaction oil (HTL oil).

15. The process of claim 13, wherein lipids comprise vegetable oils, used cooking oil, tallow, animal fats, or greases.

16. The process of claim 10, wherein the mix of circular and renewable feedstocks comprises a combination of liquified waste plastic (LWP), plastic pyrolysis oil, tire- derived oil (TDO), or waste plastics, and bio crudes, lipids, or bio-residual oils from other conversion process.

17. The process of claim 10, wherein unreacted hydrogen is recycled back to the front end of the reactor.

18. The process of claim 10, wherein a hydrotreatment step d) occurs, wherein the distillate and vacuum gas oil (VGO) products are further hydrotreated in an integrated hydrotreater.

19. The process of claim 18, wherein, the hydrotreated VGO is further hydrocracked in a hydrocracker or fluid catalytic cracking (FCC) process after separation.

20. The process of claim 10, wherein the products are subjected to an isomerization step to produce jet and diesel products.Attorney Docket No. 70205.0696WOU1 (T-12449-P2-WO01)21. The process of claim 10, wherein a heavy product is recycled back to the EB reactor.

22. The process of claim 21, wherein heavy liquid and solid in the heavy product are separated via filtration, or centrifugation.

23. The process of claim 1, wherein the bio-oils provided to the first stage reactor comprises conjugated diolefins and have a Maleic Diene value over 1.2.

24. The process of claim 23, wherein the bio-oils are saturated with H2 in the first stage reactor.

25. The process of claim 10, wherein the feedstock comprises bio-oils containing conjugated diolefins having a Maleic Diene value over 1.2, and the feedstock is saturated with H2 in a reactor prior to being fed to the EB reactor.

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