Conversion of renewables in hydroprocessing has so far been focused on making die sel, since the paraffins corresponding to the typical fatty acids of biological materials such as vegetable oils and animal fats (C14, C16 and C18) typical boil from 250°C to 320°C, corresponding well with typical diesel products boiling from 150°C to 380°C. Jet fuel products require a boiling range of 120°C to 300°C or 310°C, which means that the heavy part of a paraffins from renewable feedstocks needs to be converted into lighter materials to produce only jet fuel. A further challenge in the production of jet fuel from renewables is the discovery of a surprisingly high production of aromatics, during hy- drotreatment of renewable feedstocks. The present disclosure relates to a process hav- ing a high yield of renewable jet fuel meeting typical product requirements by convert- ing the heavy material to lighter material and by limiting the amount of aromatics in the product.

It is known to produce jet fuel from renewable feedstocks by co-producing some jet fuel in a unit designed for making diesel. However, there is an interest in making a full con- version from renewable feedstocks boiling mainly in the diesel range to jet fuel prod- ucts, which requires significant conversion.

The standard controlling the quality of jet fuel originating from hydroprocessed oxygen- ates such as esters and fatty acids is ASTM D7566, A2.1 , which inter alia specifies the boiling point curve and composition. Most of these properties can be easily met by hy- drotreating and fractionation. However, special care need to be taken to meet the freezing point (FP) requirement of max -40°C and the total aromatics content of max

0.5wt%. In addition, the standard requires an amount of low boiling product by requiring Tio, i.e. the temperatures at which 10% has been distilled according to ASTM D86, to be below 205°C. The final boiling point (FBP) is specified as 300°C, according to ASTM D86, which means that all material distilling above 300°C according to ASTM D86 needs to be converted into lighter components to fall into the jet fuel range.

Now according to the present disclosure it is proposed to carry out jet fuel production in a reverse stage two-stage configuration, where the feed is hydrodeoxygenated and op- tionally isomerized in the first stage, and after removal of sour gases the product is fractionated and a kerosene fraction is hydro-dearomatized and optionally isomerized in a second stage. The heavy fraction is directed to the pre-stage for conversion over a hydrocracking catalyst. By this process, the yield loss is reduced, as only the stream heavier than kerosene contacts the hydrocracking catalyst. Isomerization to improve the freezing point of the kerosene fraction can be done in first stage, second stage or both stages.

In the following the term stage shall be used for a section of the process, in which no separation is performed.

In the following the abbreviation pprn _m oiar shall be used to signify atomic parts per mil- lion.

In the following the abbreviation ppm _v shall be used to signify volumetric parts per mil- lion, e.g. molar gas concentration.

In the following the abbreviation %wt shall be used to signify weight percentage.

In the following the abbreviation vol/vol% shall be used to signify volume percentage for a gas.

In the following the term renewable feedstock or hydrocarbon shall be used to indicate a feedstock or hydrocarbon originating from biological sources or waste recycle. Recy- cled waste of fossil origin such as plastic shall also be construed as renewable.

In the following the term hydrodeoxygenation shall be used to signify removal of oxy- gen from oxygenates by formation of water in the presence of hydrogen, as well as re- moval of oxygen from oxygenates by formation of carbon oxides in the presence of hy- drogen.

In the following, the term topology of a molecular sieve is used in the sense described in the "Atlas of Zeolite Framework Types," Sixth Revised Edition, Elsevier, 2007, and three letter framework type codes are used in accordance herewith. A broad aspect of the present disclosure relates to a process for production of a hydro- carbon e.g. suitable for use as jet fuel, from a feedstock being oxygenate feedstock, comprising the steps of combining the feedstock with an amount of a hydrocracked in- termediate product, directing it to contact a material catalytically active in hydrodeoxy- genation under hydrodeoxygenation conditions to provide a hydrodeoxygenated inter- mediate product, fractionating said hydrodeoxygenated intermediate product in at least two fractions including a first fraction of which at least 90% boils below a defined boiling point and a second fraction of which at least 90% boils above said defined boiling point, directing at least an amount of said second fraction to contact a material catalytically active in hydrocracking under hydrocracking conditions to provide the hydrocracked in- termediate product, with the associated benefit of such a process being well suited for efficiently converting the upper-boiling point of an oxygenate feedstock such as a re- newable feedstocks to a lower boiling product, such as non-fossil kerosene. In a further embodiment step b comprises separating the hydrocracked intermediate product (22, 212) according to boiling point, to provide a hydrocracked intermediate jet product (80, 224) having T10 above 205°C and final boiling point below 310°C accord- ing to ASTM D86., with the associated benefit of the product of such a process fulfilling boiling point specifications of the renewable jet fuel specification ASTM D7566.

In a further embodiment the total volume of hydrogen sulfide relative to the volume of molecular hydrogen in the gas phase of the total stream directed to contact the material catalytically active in hydrodeoxygenation is at least 50 ppm _v , 100 ppm _v or 200 ppm _v , possibly originating from an added stream comprising one or more sulfur compounds, such as dimethyl disulfide or fossil fuels, with the associated benefit of ensuring stable operation of a material catalytically active in hydrodeoxygenation comprising a sulfided base metal, if the feedstock comprises an insufficient amount of sulfur.

In a further embodiment said renewable feedstock comprises at least 50%wt triglycer- ides or fatty acids, with the associated benefit of such a feedstock being highly suited for providing a jet fuel with excellent properties. In a further embodiment hydrodeoxygenation conditions involve a temperature in the interval 250-400°C, a pressure in the interval 30-150 Bar, and a liquid hourly space ve locity (LHSV) in the interval 0.1-2 and wherein the material catalytically active in hydro- deoxygenation comprises molybdenum or possibly tungsten, optionally in combination with nickel and/or cobalt, supported on a carrier comprising one or more refractory ox- ides, such as alumina, silica or titania, with the associated benefit of such process con- ditions being well suited for cost effective removal of heteroatoms, especially oxygen from a renewable feedstock. In a further embodiment hydrocracking conditions involve a temperature in the interval 250-400°C, a pressure in the interval 30-150 Bar, and a liquid hourly space velocity (LHSV) in the interval 0.5-4, optionally together with intermediate cooling by quenching with cold hydrogen, feed or product and wherein the material catalytically active in hy- drocracking comprises (a) one or more active metals taken from the group platinum, palladium, nickel, cobalt, tungsten and molybdenum, (b) an acidic support taken from the group of a molecular sieve showing high cracking activity, and having a topology such as MFI, BEA and FAU and amorphous acidic oxides such as silica-alumina and (c) a refractory support such as alumina, silica or titania, or combinations thereof, with the associated benefit of such process conditions being highly suited for adjusting the boiling point of a product to match the kerosene boiling point range.

In a further embodiment the process conditions are selected such that the conversion, defined as the difference in the amount of material boiling above 310°C in said hy- drocracked intermediate product and the amount of material boiling above 310°C in said second fraction, relative to the amount of material boiling above 310°C in said sec- ond fraction, is above 20%, 50% or 80%, with the associated benefit of providing a pro- cess with full or substantially full overall conversion, while avoiding excessive condi- tions and excessive yield loss. In a further embodiment at least an amount of said first fraction is directed to contact a material catalytically active in hydrodearomatization under hydrodearomatization condi- tions to provide a hydrodearomatized product comprising less than 1 wt/wt%, 0.5 wt/wt% or 0.1 wt/wt%, calculated by total mass of the aromatic molecules relative to all hydrocarbons in the stream, with the associated benefit of the product of such a pro- cess fulfilling jet fuel specification ASTM D7566.

In a further embodiment hydrodearomatization conditions involve a temperature in the interval 200-350°C, a pressure in the interval 20-100 Bar, and a liquid hourly space ve locity (LHSV) in the interval 0.5-8 and wherein said material catalytically active in hy- drodearomatization comprises an active metal taken from the group comprising plati num, palladium, nickel, cobalt, tungsten and molybdenum, preferably one or more ele- mental noble metals such as platinum or palladium and a refractory support, preferably amorphous silica-alumina, alumina, silica or titania, or combinations thereof, with the associated benefit of such process conditions being suitable for hydrogenation of aro- mates. Said material catalytically active in hydrodearomatization under hydrodearoma- tization conditions may be a material catalytically active in hydrocracking or material catalytically active isomerization operating at moderate temperatures favoring hydro- dearomatization. Hydrodearomatization conditions preferably involve at least 50% or 80% conversion of aromatics.

In a further embodiment a hydrogen rich stream comprising at least 90 vol/vol% hydro- gen is directed to contact the material catalytically active in hydrodearomatization, with the associated benefit of directing high purity hydrogen required by the overall process to the hydrodearomatization step contributing to shifting the equilibrium away from aro- matics.

In a further embodiment at least an amount of said first fraction or said hydrodearoma- tized product is directed to contact a material catalytically active in isomerization under isomerization conditions, with the associated benefit of such a process providing a product complying with the requirements to cold flow properties for jet fuels.

In a further embodiment isomerization conditions involves a temperature in the interval 250-350°C, a pressure in the interval 30-150 Bar, and a liquid hourly space velocity

(LHSV) in the interval 0.5-8 and wherein the material catalytically active in isomeriza- tion comprises an active metal taken from the group comprising platinum, palladium, nickel, cobalt, tungsten and molybdenum, preferably one or more elemental noble met- als such as platinum or palladium, an acidic support preferably a molecular sieve, more preferably having a topology taken from the group comprising MOR, FER, MRE,

MWW, AEL, TON and MTT and an amorphous refractory support comprising one or more oxides taken from the group comprising alumina, silica and titania, with the asso- ciated benefit of such conditions and materials being a cost effective and selective pro- cess for adjusting the cold flow properties of product.

In a further embodiment the treated product is directed to a gas/liquid separator to pro- vide a second stage gaseous fraction and a treated intermediate jet product which is directed to a further means of separation, to provide said hydrocarbon fraction suitable for use as a jet fuel and a treated product off gas, with the associated benefit of such a stabilization step providing a jet fuel product in compliance with flash point requirement of jet fuel.

A further aspect of the present disclosure relates to a process plant for production of a hydrocarbon fraction from an oxygenate feedstock, said process plant comprising a hy- drodeoxygenation section, a hydrocracking section and a fractionation section, said process plant being configured for directing the feedstock and an amount of a hy- drocracked intermediate product to the hydrodeoxygenation section to provide a hydro- deoxygenated intermediate product, separating the hydrodeoxygenated intermediate product in said fractionation section to provide at least two fractions, including a low boiling product fraction and a high boiling product fraction, directing at least an amount of the high boiling product fraction to the hydrocracking section to provide a hy- drocracked intermediate product, directing at least an amount of said hydrocracked in- termediate product as said further feedstock, with the associated benefit of such a pro- cess plant being suited for carrying out the disclosed process for cost effective and se- lective production of jet fuel in compliance with specification ASTM D7566, A2.1.

The processes described in the present disclosure receives a renewable feedstock and/or an oxygenate feedstock which comprises one or more oxygenates taken from the group consisting of triglycerides, fatty acids, resin acids, ketones, aldehydes, alco- hols, phenols and aromatic carboxylic acids where said oxygenates originate from one or more of a biological source, a gasification process, a pyrolysis process, Fischer- Tropsch synthesis, methanol based synthesis or a further synthesis process, especially obtained from a raw material of renewable origin, such as originating from plants, al- gae, animals, fish, vegetable oil refining, domestic waste, used cooking oil, plastic waste, rubber waste or industrial organic waste like tall oil or black liquor. Some of these feedstocks may contain aromatics; especially products derived by pyrolysis or other processes from e.g. lignin and wood or waste products from e.g. frying oil. De- pending on source, the oxygenate feedstock may comprise from 1 wt/wt% to 40 wt/wt%. Biological sources will typically comprise around 10 wt/wt%, and derivation products from 1 wt/wt% to 20 wt/wt% or even 40 wt/wt%. For the conversion of renewable feedstocks and/or oxygenate feedstocks into hydro- carbon transportation fuels, the feedstocks are together with hydrogen directed to con- tact a material catalytically active in hydrotreatment, especially hydrodeoxygenation. Especially at elevated temperatures the catalytic hydrodeoxygenation process may have side reactions forming a heavy product e.g. from olefinic molecules in the feed- stock. To moderate the release of heat, a liquid hydrocarbon may be added, e.g. a liq uid recycle stream or an external diluent feed. If the process is designed for co-pro- cessing of fossil feedstock and renewable feedstock, it is convenient to use the fossil feedstock as diluent, since less heat is released during processing of fossil feedstock, as fewer heteroatoms are released and less olefins are saturated. In addition to moder- ating the temperature, the recycle or diluent also has the effect of reducing the potential of olefinic material to polymerize, which will form an undesired heavy fraction in the product. The resulting product stream will be a hydrodeoxygenated intermediate prod- uct stream comprising hydrocarbons, typically n-paraffins, and sour gases such as CO, CO2, H2O, H2S, NH ₃ as well as light hydrocarbons, especially C3 and methane. Espe- dally at elevated temperatures the catalytic hydrodeoxygenation process may result in side reactions forming aromatics. If the feedstocks comprises nitrogen, ammonia may be formed, which can have an effect of deactivating the catalytically active material, thus requiring such elevated temperatures, with consequential formation of aromatics, in amounts above the limit of ASTM D7566 defining jet fuel specification.

The material catalytically active in hydrodeoxygenation typically comprises an active metal (one or more sulfided base metals such as nickel, cobalt, tungsten or molyb- denum, but possibly also elemental noble metals such as platinum and/or palladium) and a refractory support (such as alumina, silica or titania or combinations thereof). Hydrodeoxygenation involves directing the feedstock to contact a catalytically active material typically comprising one or more sulfided base metals such as nickel, cobalt, tungsten or molybdenum, but possibly also elemental noble metals such as platinum and/or palladium, supported on a carrier comprising one or more refractory oxides, typi- cally alumina, but possibly silica or titania. The support is typically amorphous. The cat- alytically active material may comprise further components, such as boron or phospho- rous. The conditions are typically a temperature in the interval 250-400°C, a pressure in the interval 30-150 Bar, and a liquid hourly space velocity (LHSV) in the interval 0.1- 2. Hydrodeoxygenation is typically exothermal, and with the presence of a high amount of oxygen, the process may involve intermediate cooling e.g. by quenching with cold hydrogen, feed or product. The feedstock may preferably contain an amount of sulfur to ensure sulfidation of the metals, in order to maintain their activity. If the gas phase comprises less than 10, 50 or 100 ppm _v sulfur, a sulfide donor, such as dimethyldisul- fide (DMDS) may be added to the feed.

The hydrodeoxygenated intermediate product will mainly be of same structure as the carbon skeleton of the feedstock oxygenates, or if the feedstock comprises triglycer ides, n-paraffins, but possibly of a shorter length than the fatty acids. Typically, the hy- drodeoxygenated intermediate product will be dominated by linear alkanes having boil- ing point range (250°C to 320°C) and a freezing point (0°C to 30°C) unsuited for use as jet fuel. Some heavy components and aromatics may also be formed in the hydrodeox- ygenation step if the unsaturated fatty acids polymerizes and form aromatic structures even for an oxygenate feedstock comprising less than 1 % aromatics.

For the hydrodeoxygenated intermediate product to be used as a fuel in practice, the freezing point must be adjusted. The freezing point is adjusted by isomerization of n- paraffins to i-paraffins, by directing the hydrodeoxygenated intermediate product to contact a material catalytically active in isomerization

The material catalytically active in isomerization typically comprises an active metal (ei- ther elemental noble metals such as platinum and/or palladium or sulfided base metals such as nickel, cobalt, tungsten and/or molybdenum), an acidic support (typically a mo- lecular sieve showing high shape selectivity, and having a topology such as MOR, FER, MRE, MWW, AEL, TON and MTT) and a typically amorphous refractory support (such as alumina, silica or titania, or combinations thereof). The catalytically active ma- terial may comprise further components, such as boron or phosphorous. Preferred isomerization catalysts comprise molecular sieves such as EU-2, ZSM-48, beta zeolite and combined beta zeolite and zeolite Y.

Isomerization involves directing the intermediate hydrodeoxygenated feedstock to con- tact a material catalytically active in isomerization. The conditions are typically a tem- perature in the interval 250-350°C, a pressure in the interval 30-150 Bar, and a liquid hourly space velocity (LHSV) in the interval 0.5-8. Isomerization is substantially ther- mally neutral and consumes only hydrogen in hydrocracking side reactions so only a moderate amount of hydrogen is added in the isomerization section. When the active metal on the material catalytically active in isomerization is a noble metal, the hydrode- oxygenated feedstock is typically purified by gas/liquid separation to reduce the content of potential catalyst poisons to low levels such as levels of sulfur, nitrogen and carbon oxides to below 1-10 pprn _m oiar. When the active metal is a base metal the gas phase of the intermediate hydrodeoxygenated feedstock preferably contains at least 50 ppm _v sulfur. For the hydrodeoxygenated intermediate product stream to be used as a kerosene fraction, the boiling point range must be adjusted. The boiling point is adjusted by hy- drocracking of long paraffins to shorter paraffins, by directing the hydrodeoxygenated intermediate product to contact a material catalytically active in hydrocracking. The material catalytically active in hydrocracking is of a nature similar to that of the ma- terial catalytically active in isomerization, and it typically comprises an active metal (ei- ther elemental noble metals such as platinum and/or palladium or sulfided base metals such as nickel, cobalt, tungsten and/or molybdenum ), an acidic support (typically a molecular sieve showing high cracking activity, and having a topology such as MFI, BEA and FAU, but amorphous acidic oxides such as silica-alumina may also be used) and a refractory support (such as alumina, silica or titania, or combinations thereof). The difference to a material catalytically active in isomerization is typically the nature of the acidic support, which may be of a different structure (even amorphous silica-alu- mina) or have a different acidity e.g. due to silica:alumina ratio. The catalytically active material may comprise further components, such as boron or phosphorous. Preferred hydrocracking catalysts comprise molecular sieves such as ZSM-5, zeolite Y or beta zeolite. Hydrocracking involves directing the hydrocarbons to contact a material catalytically active in hydrocracking. The conditions are typically a temperature in the interval 250- 400°C, a pressure in the interval 30-150 Bar, and a liquid hourly space velocity (LHSV) in the interval 0.5-4. As hydrocracking is exothermal, the process may involve interme- diate cooling e.g. by quenching with cold hydrogen, feed or product. When the active metal on the material catalytically active in isomerization is a noble metal, the hydrode- oxygenated feedstock is typically purified by gas/liquid separation to reduce the content of potential catalyst poisons to low levels such as levels of sulfur, nitrogen and carbon oxides to below 1-10 pprn _m oiar. When the active metal is a base metal the gas phase of the hydrocarbons preferably contains at least 50 ppm _v sulfur.

Hydrodeoxygenation of unsaturated fatty acids and hydrocracking may also produce aromatics as a side reaction, especially if the temperature and/or the conversion is high. Therefore, a low conversion during hydrocracking has typically been desired, hin- dering full conversion to a kerosene fraction. One consideration in increasing conver- sion has been to recycle hydrocracked intermediate product for additional contact with the material catalytically active in hydrocracking, but even this may produce an exten- sive amount of aromatics.

Therefore, it may be further necessary to direct the hydrocracked intermediate product to contact a material catalytically active in hydrodearomatization, which is surprising, as the renewable feedstocks contain no or little aromatics.

In some instances hydrodearomatization may be satisfactorily carried out in the pres- ence of the material catalytically active in hydroisomerization, but it may also be neces- sary to have a separate reactor or reactor bed with material catalytically active in hy- drodearomatization.

The material catalytically active in hydrodearomatization typically comprises an active metal (typically elemental noble metals such as platinum and/or palladium but possibly also sulfided base metals such as nickel, cobalt, tungsten and/or molybdenum) and a refractory support (such as amorphous silica-alumina, alumina, silica or titania, or com- binations thereof). Hydrodearomatization is equilibrium controlled, with high tempera- tures favoring aromatics, noble metals are preferred as the active metal, since they are active at lower temperatures, compared to base metals.

Hydrodearomatization involves directing an intermediate product to contact a material catalytically active in hydrodearomatization. As the equilibrium between aromatics and saturation molecules shifts towards aromatics at elevated temperatures, it is preferred that the temperature is moderate. The conditions are typically a temperature in the in- terval 200-350°C, a pressure in the interval 30-150 Bar, and a liquid hourly space ve locity (LHSV) in the interval 0.5-8. As the preferred active metal on the material catalyti cally active in hydrodearomatization is a noble metal, the hydrocracked intermediate product is typically purified by gas/liquid separation to reduce the content of sulfur to below 1-10 ppm.

This necessity to combine 3 or 4 catalytically active materials for conversion of renewa- ble feedstocks into jet fuel naturally complicates the process layout, and the sequence of the materials must be considered carefully. In addition, recycle may be used for three different purposes; gas recycle for efficient use of hydrogen, liquid recycle around the material catalytically active in hydrocracking to maximize the yield of the kerosene fraction and liquid recycle around the material catalytically active in hydrodeoxygena- tion to limit the temperature increase due to exothermal hydrodeoxygenation reactions. According to the present disclosure the boiling point of the product is adjusted by hy- drocracking in a so-called reverse staging layout. Here the feedstock is combined with a hydrocracked hydrocarbon and directed to the hydrodeoxygenation reactor. The hy- drodeoxygenated product stream is split according to boiling point, and at least an amount of the product boiling above the jet range is recycled to a hydrocracking reactor upstream the hydrodeoxygenation reactor. The recycle ratio may be maximized to en- sure full conversion to product boiling in the jet range, or a lower recycle ration may be chosen, while purging an amount of product boiling above the jet range, e.g. for use as diesel. The hydrodearomatization will typically require sweet conditions, as the catalyst typi- cally comprises a noble metal, which operates at lower temperatures, thus employing the fact that the equilibrium of the hydrodearomatization reaction is shifted away from aromatics at low temperatures.. Therefore, a separation of gases may be carried out prior to hydrodearomatization, and optionally also a separation of intermediate hy- drocracked product according to boiling point, such that only intermediate hy- drocracked product boiling in the kerosene range contacts the material catalytically ac- tive in hydrodearomatization. Isomerization may be carried out either in connection with hydrocracking or in connection with hydrodearomatization. In both cases the material catalytically active in isomerization may be positioned either upstream or downstream the material catalytically active in hydrocracking or hydrodearomatization respectively.

Operating the material catalytically active in hydrocracking with recycle allows full con- version at moderate temperatures, thus maintaining a high yield of kerosene and mini- mized over-cracking to naphtha and lighter. The use of an isomerization catalyst to im- prove freezing point of the jet fuel, allows increasing the distillation endpoint of the jet fuel while still meeting freezing point requirement. Finally, since the second stage will saturate aromatics, it is not required for the first stage to meet any aromatics require- ments, which allows the first stage to treat heavier and/or more aromatic, naphthenic or unsaturated feedstocks as well as feedstocks such as used cooking oil, pyrolysis prod- ucts or tall oil pitch, which are known to produce aromatics in small amounts in typical hydroprocessing conditions, since these aromatics will be saturated in the second stage. One embodiment according to the present disclosure corresponds to a process in which a stream comprising oxygenates and hydrocracked recycled hydrocarbons, and also comprising an amount of sulfur is directed to a hydrodeoxygenation reactor containing a catalytically active material comprising one or more base metals and a refractory support, with low acidity. Such a material is active in hydrodeoxygenation and other hydrotreatment reactions removing heteroatoms and double bonds. An amount of sulfide must be present in the feed stream to the hydrodeoxygenation reactor, either as part of the hydrocracked recycled hydrocarbons, or as added sulfide to the feed stream to the hydrodeoxygenation reactor. The hydrocracked recycled hydrocarbons contribute as a heat sink, absorbing the released heat of reaction from the hydrodeoxygenation, thus maintaining a moderate temperature in the

hydrodeoxygenation reactor. This step provides a stream comprising a high amount of saturated linear alkanes, in combination with an amount of water, hydrogen sulfide and ammonia.

The hydrotreated stream is directed to a fractionator (after appropriate removal of the gas phase in a separator train), and at least a gas fraction, an intermediate fraction and a bottoms fraction of the hydrotreated stream are withdrawn. All streams out of the fractionator have a very low level of water, hydrogen sulfide and ammonia. The bottoms fraction will be too heavy for being used as jet product, and is recycled.

The bottoms fraction of the hydrotreated stream is directed to a hydrocracking reactor containing a catalytically active material comprising either one or more base metals or one or more noble metals and a refractory support with high acidity. Such a material is active in hydrocracking, and this step provides a stream in which higher boiling hydrocarbons are converted to lower boiling hydrocarbons.

For reasons of cost, a base metal material may be preferred, and in this case addition of an amount of sulfur, e.g. as DMDS is required at the inlet of the hydrcracking reactor. It may alternatively be preferred to operate with a more expensive and more selective noble metal material; in this case sulfur addition is not required. The severity of the hydrocracking process will define the boiling point characteristics of the product, and it will typically be operated with full conversion of the fraction boiling above the diesel range. If hydrocracking severity is selected for full conversion of the fraction boiling above the jet range the yield loss to gases and naphtha will typically be higher.

If the material catalytically active in hydrocracking comprises noble metals it is necessary to add sulfide, in the form of hydrogen sulfide or di methyl di sulfide (DMDS) prior to the hydrodeoxygenation reactor.

The intermediate hydrotreated fraction has a boiling range which is suitable for use as jet fuel, but the content of aromatics and the freezing point are not within specification. Therefore, this fraction is directed to an isomerization reactor containing a material catalytically active in isomerization and a material catalytically active in hydrodearomatization. Both materials are based on a noble metal catalyst, such as platinum, palladium or a combination, in combination with an acidic support. For isomerization the acidic support is preferably shape selective, e.g. a zeolite, to provide a selective isomerization, rearranging linear alkanes to branched alkanes, with minimal production of lighter hydrocarbons. For hydrodearomatization, an acidic support also contribute to the reaction, and in addition as the activity of noble metals is higher than that of base metals, the reaction will take place at lower temperatures. As the equilibrium between aromatic and non-aromatic compounds is shifted away from aromatics at low temperatures, noble metals provide the benefit that the lower temperature matches the equilibrium. Hydrodearomatization may even take place on the material catalytically active in isomerization, which often will have some

hydrodearomatization activity. An amount of hydrocracking may occur in the isomeriza- tion reactor, and therefore it may be preferred that the hydrocracked stream is slightly heavier than jet specifications.

The layout therefore provides a full conversion of feedstock to jet range or lighter product, as all heavy product is recycled and hydrocracked. The jet range yield is higher than a layout where all hydrocarbons are hydrocracked, since the jet range fraction of the hydrodeoxygenated stream is not recycled to the hydrocracker, but only the bottom fraction from the fractionator.

Furthermore the adjustment of freezing point is made selectively by isomerization on a noble metal catalyst, independently of hydrocracking conditions, and finally

hydrodearomatization may be efficiently carried out at moderate temperatures in the same reactor and possibly even the same catalytically active material as isomerization.

Should it be desired to produce diesel and not jet fuel, hydrocracking is not desired. In this case, it may be preferred to either by-pass the hydrocracking reactor or alterna- tively cool the product prior to this reactor, such that it is inactive. The process plant may be configured for allowing such a configuration with short notice, e.g. by setting up appropriate equipment and control in the control room.

Figures

Figure 1 shows a process according to the present disclosure. Figure 2 shows a simplified illustration of a process according to the present disclosure. Figure 3 shows a simplified illustration of a process according to the prior art.

Figure 1 shows a process layout for production of a hydrocarbon suitable for use as jet fuel (98) from a renewable feedstock (2), wherein the renewable feedstock (2) is com- bined with a hydrocracked intermediate product (14) and directed as a hydrodeoxygen- ation feed stream (6) together with an amount of a hydrogen rich stream (12) to a hy- drodeoxygenation section (HDO) where it contacts a material catalytically active in hy- drodeoxygenation under hydrodeoxygenation conditions. This provides a hydrodeoxy- genated intermediate product (22). The hydrodeoxygenated intermediate product (22) is directed to a gas/liquid separator (SEP1 ) where it is separated into a gaseous frac- tion (26) and a liquid hydrocracked intermediate product (34). The gaseous fraction (26) is split in an optional purge (28) and a recycle gas (30) which is pressurized in a compressor (CM1 ) and directed as hydrogen supply (12) to the hydrodeoxygenation section (HDO) and a hydrocracking section (HDC). The liquid hydrocracked intermedi- ate product (34) is directed to a stripper (STR), which also receives a stripping medium (38) and optionally a stripper overhead recycle (40). From the stripper a gaseous strip per product (42) is directed to a gas/liquid separator (SEP2), from which an vapor phase product (46) and a light naphtha fraction (48) are withdrawn. An amount of the light naphtha is withdrawn as product (50), an amount (52) may optionally be directed as feed (90) to a kerosene stabilizer (STAB) and an amount is directed as overhead re- cycle (40) to the stripper (STR). The liquid stripper product (54) is directed to fractiona- tor (FRAC), from which a light overhead stream (58) is directed to an overhead vessel (OV), from which a heavy naphtha (62) is withdrawn. An amount of heavy naphtha (64) is withdrawn as product and a further amount (66) is directed as fractionator recycle (66). A high boiling product fraction (68) is split in to a recycle stream (72) and a re- boiled stream (74). The recycle stream (72) is combined with a gaseous fraction (78) and directed as a hydrocracker feed stream (4) to a hydrocracking section (HDC) oper- ating under hydrocracking conditions. From a side column (SC) a hydrodeoxygenated intermediate jet product (80) is withdrawn and combined with a of hydrogen rich stream (84) and directed as feed (82) to a post treat section (PT), where it contacts a material catalytically active in isomerization (ISOM) under isomerization conditions and a mate- rial catalytically active in hydrodearomatization (HDA) under hydrodearomatization con- ditions, optionally receiving further hydrogen, providing a treated product (86), which is directed to a product gas/liquid separator (SEP4) from which a second gaseous frac- tion (78) is withdrawn and combined with the recycle stream (72) and provided as make-up hydrogen in a feedstream to a hydrocracking section (HDC). An intermediate jet product (88) is withdrawn from the product gas/liquid separator (SEP4), and directed to a further means of separation (STAB), such as a kerosene stabilizer, from which a liquid product (94) is withdrawn and split in a hydrocarbon fraction suitable for use as jet fuel (98) and a reboiler liquid (96). The gaseous overhead from the kerosene stabi- lizer (92) is combined with the gaseous stripper product (42) and directed to a gas/liq uid separator (SEP2).

In a further embodiment (not shown) the second gaseous fraction (78) is not directed as make-up gas for the hydrodeoxygenation section, but instead directed to the post- treatment section (PT), requiring an additional compressor, but also resulting in added simplicity. In this case make-up hydrogen is then added separately to the hydrodeoxy- genation section.

In a further embodiment the gaseous overhead from the kerosene stabilizer (92) may be handled in a separate overhead circuit with the benefit of simplicity and independ- ence, but at the cost of extra equipment items for cooling, separation and reflux pumps.

In a further embodiment the separator, fractionation and light ends recovery sections can be configured in multiple ways as it is known to the skilled person. If light materials like LPG or propane are valuable, the recovery of these can be improved by using a sponge oil absorption system e.g. using the heavy naphtha from the fractionator over- head as lean oil and returning the rich oil to the stripper.

Figure 2 is a simplified figure showing a layout similar to that of Figure 1 , omitting sup- ply of gaseous streams and details of separation for simplicity. A

renewable feedstock (202) is combined with a hydrocracked intermediate product (206) and directed as a hydrodeoxygenation feed stream (204) together with an amount of a hydrogen rich stream (not shown) to a hydrodeoxygenation section (HDO) where it contacts a material catalytically active in hydrodeoxygenation under hydrodeoxygena- tion conditions. This provides a hydrodeoxygenated intermediate product (212). The hydrodeoxygenated intermediate product (212) is directed to a fractionation section (FRAC) shown for simplicity as a single unit, separating the hydrodeoxygenated inter- mediate product in a light overhead stream (220), a naphtha stream (222), a hydrode- oxygenated intermediate jet product (224) and a high boiling product fraction (226).

The high boiling product fraction (226) is directed as a recycle stream to a hydrocrack- ing section (HDC) operating under hydrocracking conditions, providing a hydrocracked intermediate product (206), which, as mentioned, is combined with the renewable feed- stock (202). The hydrodeoxygenated intermediate jet product (224) is directed as feed to a post treat section (PT), where it contacts a material catalytically active in isomeri- zation (ISOM) and a material catalytically active in hydrodearomatization (HDA) under hydrodearomatization conditions, providing a treated jet fuel product (218).

Figure 3 shows an example of the prior art, in a level of detail similar to Figure 2, omit- ting supply of gaseous streams and details of separation for simplicity. A renewable feedstock (302) is combined with a recycle diluent stream (310) and directed as a hy- drodeoxygenation feed stream (304) together with an amount of a hydrogen rich stream (not shown) to a hydrodeoxygenation section (HDO) where it contacts a mate- rial catalytically active in hydrodeoxygenation under hydrodeoxygenation conditions. This provides a hydrodeoxygenated intermediate product (306), from which gases are separated e.g. in a stripper (SEP), providing a sweet hydrodeoxygenated intermediate product (308), which is split into said recycle diluent stream (310) and an isomerization feed (312) which is directed to a hydroisomerization section (ISOM) where it contacts a material catalytically active in isomerization under isomerization conditions, providing a dewaxed intermediate product (314). The dewaxed intermediate product (314) is di- rected to a hydrocracking section (HDC) where it contacts a material catalytically active in hydrocracking under hydrocracking conditions, providing a hydrocracked product (316). The hydrocracked product (316) is directed to a fractionation section (FRAC) shown for simplicity as a single unit, separating the hydrocracked product in a light overhead stream (320), a naphtha stream (322), a jet product (324) and a bottom die- sel fraction (326).

Examples

The performance of the process layouts shown in Figures 2 and 3 have been corn- pared, based on two similar feedstocks, and process conditions optimized for maxi- mum jet yield. Table 1 shows the characteristics of a renewable feedstock which is a mixture of 50% used cooking oil and 50% animal fat. The feedstock comprises 6% aromatics and 80% boils above 500°C; mainly due to the presence of high boiling triglycerides.

Feedstock A was treated in a process in accordance with Figure 2 and 3, and the re- sults of this treatment is shown in Table 2.

In the hydrotreatment a significant conversion of boiling point is seen due to triglycer- ides being converted to alkanes. In addition, an amount of conversion is observed in the hydrocracking reactor and the isomerization reactor. The true conversion per pass is however quite low, since the amount of recycle is high.

The results of both examples show a production of a jet fuel with excellent properties, a low freezing point (-40°C) and a low aromatics content (<0.5wt%). The example ac- cording to the present disclosure (Figure 2) has a jet yield of 67 wt/wt%, whereas the Example according to the prior art (Figure 3) has a jet yield of 58 wt/wt%, whereas 11 wt/wt% diesel is produced. In addition, naphtha is produced in both scenarios. In a pro- cess designed for production of jet, the yield difference of 9% is of course valuable. The configuration of Figure 2, where the product of hydrodeoxygenation is split in a light and a heavy fraction and the heavy fraction is recycled to a hydrocracking reactor upstream the hydrodeoxygenation, results in a full conversion of heavy feedstock to jet product, while avoiding directing light hydrocarbons to the hydrocracking section, and thus a higher yield of jet product compared to the configuration of Figure 3.

Table 1

Table 2