PROCESS FOR PREPARING HYDROCRACKING CATALYST

Abstract

Disclosed herein is a process for preparing a hydrocracking catalyst, comprising (i) combining a zeolite, a binder, water and a hydrogenating metal compound which is a complex or a salt of a hydrogenating metal to obtain a mixture, wherein the zeolite has not been treated with a phosphorus-containing compound and the zeolite has a silica to alumina molar ratio of 5-200; (ii) forming the mixture into a shaped body; and (iii) calcining the shaped body to form the catalyst.

Claims

1. A process for preparing a hydrocracking catalyst, comprising: (i) combining a zeolite, a binder, water and a hydrogenating metal compound which is a complex or a salt of a hydrogenating metal to obtain a mixture, wherein the zeolite has not been treated by a phosphorus-containing compound and the zeolite has a silica to alumina molar ratio of 5-200; (ii) forming the mixture into a shaped body; and (iii) calcining the shaped body at 250- to less than 300 C., for 2-8 hours to form the catalyst.

2. The process according to claim 1, wherein the catalyst has an average hydrogenating metal particle size of less than or equal to 5 nm, as determined using TEM.

3. The process according to claim 1, wherein the mixture is can extrudable paste.

4. A process for preparing a hydrocracking catalyst, comprising: (i) combining a zeolite, a binder, and a hydrogenating metal compound which is a complex or a salt of a hydrogenating metal, with water to form a paste, wherein the zeolite has not been treated by a phosphorus-containing compound; (ii) forming the paste into a shaped body; and (iii) calcining the shaped body at 250-295 C. to form the catalyst; wherein the catalyst has an average hydrogenating metal particle size of less than or equal to 5 nm, as determined using TEM.

5. The process according to claim 1, wherein the shaped body is calcined at 250-295 C.

6. The process according to claim 1, the preceding claims, wherein the catalyst comprises less than 0.01 parts tin, less than 0.02 parts lead, and less than 0.01 parts bismuth, on the basis of 100 parts by weight of the catalyst.

7. The process according to claim 1, wherein step (i) involves combining the zeolite and the hydrogenating metal compound and subsequently adding the binder to the combination of the zeolite and the hydrogenating metal compound; or combining the hydrogenating metal compound and the binder and subsequently adding the zeolite to the combination of the binder and the hydrogenating metal compound.

8. The process according to claim 1, wherein the zeolite is selected from the group consisting of ZSM-5, MCM-22, ZSM-11, beta zeolite, EU-1 zeolite, faujasite (zeolite Y), ferrierite and mordenite.

9. The process according to claim 1, wherein the silica to alumina molar ratio is 25-75.

10. The process according to claim 1, wherein the zeolite is an H.sup.+-form or NH.sub.4.sup.+-form.

11. The process according to claim 1, wherein the binder is selected from the group consisting of alumina, clay, silica-alumina, aluminum phosphate and combinations thereof.

12. The process according to claim 1, wherein the binder has been treated with a mineral acid such as nitric acid, hydrochloric acid, phosphoric acid or sulfuric acid.

13. The process according to claim 1, wherein the hydrogenating metal is at least one of palladium and platinum.

14. The process according to claim 1, wherein the hydrogenating metal compound is selected from the group consisting of H.sub.2PtCl.sub.6, (NH.sub.3).sub.4Pt(NO.sub.3).sub.2, (NH.sub.3).sub.4Pt(OH).sub.2 and (NH.sub.3).sub.4PtCl.sub.2.

15. The process according to claim 1, wherein the amount of the hydrogenating metal is 0.010-0.30 wt %, with respect to the total catalyst.

16. The process according to claim 1, wherein the shaped body is an extrudate having an average diameter of 0.5-5 mm.

17. The process according to claim 1, wherein the only metal in the catalyst is the hydrogenating metal and binder, and wherein the hydrogenating metal is at least one element selected from Group 10 of the periodic table of elements, rhodium, and iridium.

18. The hydrocracking catalyst obtained by the process according to claim 1.

19. A process for hydrocracking a feed stream comprising hydrocarbons comprising: contacting the feed stream in the presence of hydrogen with the hydrocracking catalyst according to claim 18 under process conditions including a temperature of 400-580 C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 0.1-30 hr.sup.1 to produce a hydrocracking product stream comprising benzene, toluene and xylene, wherein the hydrocracking feed stream comprises C.sub.5-C.sub.12 hydrocarbons; and separating the benzene, toluene, and xylene from the hydrocracking product stream.

20. (canceled)

21. The process according to claim 1, wherein the shaped body is calcined at 260-290 C.

Description

EXAMPLES

[0084] The invention is now elucidated by way of the following examples, without however being limited thereto.

Materials Used for Catalyst Synthesis:

[0085] 1. Alumina powder (HiQ alumina, #Q-1665 obtained from Alcoa; or Catapal D alumina obtained from Zeolyst) [0086] 2. ZSM-5 zeolite powder (CBV 5524G, Zeolyst International). The ZSM-5 was in NH.sub.4-form having silica to alumina ratio of 56-58. Unless stated otherwise the zeolite powder was used as-obtained from the source without further treatment. The zeolite powder contained less than 0.04 wt % Na. The as-obtained ZSM-5 zeolite powder was calcined at 550 C. for 10 hours (hr) in air prior to use for making Catalyst A-E [0087] 3. HNO.sub.3 (Sigma-Aldrich, 70%, lot #70296CK) [0088] 4. Chloroplatinic acid, H.sub.2PtCl.sub.6.6H.sub.2O (Sigma-Aldrich, lot #MKBR5059V) [0089] 5. Tetraamine platinum nitrate, (NH.sub.3).sub.4Pt(NO.sub.3).sub.2 (Aldrich, LOT #MKBJ1197V) [0090] 6. ZSM-5 extrudates (CBV 5524G CY1.6, Zeolyst International). The as-obtained extrudates contained about 80 w % ZSM-5 (silica to alumina ratio 56-58) and 20 wt % alumina binder; the as-obtained zeolite extrudates were calcined and the zeolite present in the extrudates were in H-form. The zeolite contained less than 0.04 wt % Na. [0091] 7. Water used is deionized water.

Example Catalysts

Catalyst A

[0092] 10 grams (g) of alumina powder (HiQ) was treated with 1.6 g of HNO.sub.3 by adding slowly while mixing them in a ceramic dish.

[0093] A chloroplatinic acid solution was made by dissolving 0.1062 g of H.sub.2PtCl.sub.6.6H.sub.2O in 8 g water. The chloroplatinic acid solution was thereafter added (drop wise) to 40 g of the precalcined ZSM-5 powder and they were mixed well.

[0094] As described above the treated zeolite and alumina were combined together, mixed well and then water (22.5 g) was added to make a paste. Paste was formed into shape of beads. Beads were dried at 90 C. for 3 hours, then calcination was continued at temperature ramp 3 C./min up to 300 C. and was kept for 2 hours.

Catalyst B

[0095] 10 g of alumina powder (HiQ) was treated with 1.6 g of HNO.sub.3 by adding slowly while mixing them in a ceramic dish.

[0096] A solution of tetraammineplatinum nitrate was made by dissolving 0.0796 g of (NH.sub.3).sub.4Pt(NO.sub.3).sub.2 in 8 g of water, and the Pt-solution was added (drop wise) to 40 g of ZSM-5 powder (precalcined) mixing them well.

[0097] The treated zeolite and alumina were combined together, mixed well and then water (25 g) was added to make a paste. Paste was formed into shape of beads. Beads were dried at 90 C. for 3 hours, then calcination was continued at temperature ramp 3 C./min up to 300 C. and was kept for 2 hours.

Catalyst C

[0098] 10 g of alumina powder (HiQ) was treated with 1.6 g of HNO.sub.3 by adding slowly while mixing them in a ceramic dish. A solution of 0.1072 g of H.sub.2PtCl.sub.6.6H.sub.2O in 2 g of water was added (drop wise) to the alumina while mixing. White color of alumina changed to yellowish.

[0099] 40 g of ZSM-5 powder (precalcined) was combined with the alumina, mixed well and about 37-38 g of water was added to make a paste. The paste was formed into shape of beads. Beads were dried at 90 C. overnight, then calcination was continued at temperature ramp 3 C./min at 300 C. and was kept for 2 hours.

Catalyst D

[0100] 10 g of alumina powder (HiQ) was treated with 1.6 g of HNO.sub.3 by adding slowly while mixing them in a ceramic dish.

[0101] 40 g of ZSM-5 powder (precalcined) was combined with the alumina and mixed well. About 25 g of water was added to the zeolite and alumina mixture to moisten. Solution of 0.1062 g of H.sub.2PtCl.sub.6.6H.sub.2O in 15 g of water was prepared and was added to the mixture by portions with careful mixing and finally paste formation. The paste was formed in shape of beads. Beads were dried at 90 C. overnight, then calcination was continued at temperature ramp 3 C./min at 300 C. for 2 hours.

Catalyst E

[0102] 10 g of alumina powder (HiQ) was treated with 1.6 g of HNO.sub.3 by adding the acid slowly to the alumina while mixing them in a ceramic dish.

[0103] A Pt-solution was made of 0.3717 g of H.sub.2PtCl.sub.6.6H.sub.2O in 8 g of water. 40 g of ZSM-5 powder (precalcined) was impregnated with the Pt-solution by drops with constant mixing. The zeolite was combined with the alumina and mixed them well. The zeolite and alumina mixture was made into a paste by slowly adding and mixing of about 22.5 g of water. Paste was formed in shape of 1/16-inch cylindrical extrudates. The extruded catalyst was dried/calcined by using a temperature profile: room temperature to 90 C. with ramp 5 C./min (held 3 hr), ramp 3 C./min to 300 C. (held 2 hr).

Catalyst F

[0104] 20 g of alumina powder (Catapal D) was treated with 3.2 g of HNO.sub.3 by adding the acid slowly to the alumina while mixing them in a ceramic dish.

[0105] 80 g of ZSM-5 zeolite powder was mixed with 38.58 g of 0.005 M solution of H.sub.2PtCl.sub.6. The zeolite powder was then combined with the acid treated alumina and mixed well, and an additional 16.26 g water added to the zeolite-alumina mixture to form an extruadable paste.

[0106] The paste was extruded as 1/16-inch cylindrical shaped extrudate. The extrudates were dried/calcined in air at 319 C. for 2 hr.

Catalyst G

[0107] 50 g of alumina powder (Catapal D) was treated with 8.0 g of HNO.sub.3 by adding the acid slowly to the alumina while mixing them in a ceramic dish.

[0108] A Pt-solution was made of 0.2657 g of H.sub.2PtCl.sub.6.6H.sub.2O in 21 g of water. 50 g of ZSM-5 powder was impregnated with the Pt-solution by drops with constant mixing. The zeolite powder was then combined with the acid treated alumina and mixed well, and an additional 37.24 g water added to the zeolite-alumina mixture to form an extruadable paste.

[0109] The paste was extruded as 1/16-inch cylindrical shaped extrudate. The extrudates were dried/calcined in air at 319 C. for 2 hr.

Comparative Catalyst H

[0110] 8.2017 g of 0.005M (NH.sub.3).sub.4Pt(NO.sub.3).sub.2 solution were diluted in 49.2 g water in a 500 milliliter (ml) conical glass flask.

[0111] 10 g of extrudates (which were predried at 300 C. for 5 h) were poured into solution. The mixture was stirred at 60 C. for 24 hours. Then solution was decanted and sample was rinsed with 500 ml water 5 times and then stirred in 300 ml of water for 10 min. Then water was decanted and sample was dried at 90 C. overnight and calcined at 280 C. for 6 hours at temperature ramp 3 C./min.

Comparative Catalyst I

[0112] 82.148 g of 0.005M H.sub.2PtCl.sub.6.6H.sub.2O solution were diluted in 204.97 g water in a 3.5 L glass beaker.

[0113] 100 g of extrudates (which were predried at 150 C. overnight) were poured into solution. The mixture was stirred at 60 C. for 24 hours. Then solution was decanted and sample was rinsed with 1 liter (L) water 5 times and then stirred in 1 L of water for 10 min. Then water was decanted and sample was dried at 90 C. overnight and calcined at 280 C. for 6 hours at temperature ramp 3 C./min.

Comparative Catalyst J

[0114] 10 g of extrudates were stirred in 28.678 g of 0.005M H.sub.2PtCl.sub.6.6H.sub.2O solution at 60 C. for 24 hours. Then solution was decanted and sample was rinsed several times with water and stirred in 500 ml of water for 25 min. Then water was decanted and sample was dried at 90 C. overnight and calcined at 280 C. for 3 hours at temperature ramp 3 C./min.

[0115] The catalyst preparation methods with Pt content are summarized in Table 1.

TABLE-US-00001 TABLE 1 Catalyst Pt deposition.sup.1 Pt source Pt, wt % A Zeolite powder H.sub.2PtCl.sub.6 0.060 B Zeolite powder (NH.sub.3).sub.4Pt(NO.sub.3).sub.2 0.065 C Alumina powder H.sub.2PtCl.sub.6 0.067 D Zeolite-alumina H.sub.2PtCl.sub.6 0.072 powder E Zeolite powder H.sub.2PtCl.sub.6 0.256 F Zeolite powder H.sub.2PtCl.sub.6 0.070 G Zeolite powder H.sub.2PtCl.sub.6 0.070 H Extrudate (NH.sub.3).sub.4Pt(NO.sub.3).sub.2 0.07 I Extrudate H.sub.2PtCl.sub.6 0.07 J Extrudate H.sub.2PtCl.sub.6 0.25 .sup.1Pt was added either to zeolite or alumina during forming or deposited on formed extrudates

Catalyst Testing:

[0116] The catalysts A-J were tested for hydrocracking reaction using stainless steel tube reactor as described below. 0.10 g catalyst (sized 20-40 mesh) was diluted to 3 ml by premixing with SiC (30 grit) and was loaded in a reactor.

[0117] Reactor description: one quarter inch () tube, 0.028 wall thickness. 1/16 thermocouple with a spacer bar; 121 brass over-sleeve; reactor bed is approx. 5-6 inches () in length in center of sleeve.

[0118] The catalyst was pre-activated (drying, Pt reduction) by subjecting it to 40 standard cubic centimeters (sccm) of H.sub.2 per minute at 130 C. under 50 psig for 2 hours and subsequently 40 sccm of H.sub.2 (with 50 ppm of H.sub.2S) at 350 C. at 50 psig for 30 min.

[0119] The hydrocracking feed stream consisted of 70 wt % benzene, 15 wt % 3-methylpentane and 15 wt % methylcyclopentane. All components of the hydrocracking feed stream are Aldrich reagent grade chemicals dried under 4 A molecular sieves overnight.

[0120] The hydrocracking feed stream was introduced to the reactor at a temperature of 470 C. and a pressure of 200 psig. The liquid feed rate was adjusted to give WHSV of about 10/hr. The molar ratio of H.sub.2 to the hydrocarbons was 4 to 1, and the H.sub.2S content was 50 parts per million by mole (ppm) based on the total hydrocarbon and H.sub.2 feed.

[0121] To illustrate the invention Example Catalysts A-G were used in Experiments 1-7 whereas Comparative Catalysts H-J were used in Experiments 8-10. In all experiments the catalysts were tested under the same conditions as described in preceding paragraphs. The catalytic activity was measured by comparing benzene purity which was calculated by following formula:

% benzene purity=% benzene/(% benzene+% C.sub.6-nonaromatic hydrocarbons)

[0122] where % is as C % in product stream.

[0123] The catalyst activity is shown in Table 2 and illustrated in FIG. 1. The selectivity was calculated as % C basis. The catalyst activity and selectivity were averaged from data over a period of about 20 hours after the catalyst reached to steady-state conditions.

TABLE-US-00002 TABLE 2 Catalyst activity and selectivity Activity Selectivity (% C) WHSV/ (benzene Total Example Catalyst hr purity) Methane LPG Benzene Aromatics 1 A 10.01 99.90 1.37 29.72 63.48 67.91 2 B 10.01 99.88 1.32 30.74 62.43 67.61 3 C 10.01 99.86 1.28 31.51 61.24 66.87 4 D 10.01 99.86 1.32 31.34 61.16 67.00 5 E 10.01 99.84 1.34 38.24 54.77 60.05 6 F 10.01 99.88 1.35 26.45 65.74 71.90 7 G 10.01 99.62 1.00 31.87 61.58 66.46 Comp 8 H 9.72 99.63 1.29 29.99 62.42 69.76 Comp 9 I 9.91 99.80 1.20 31.97 61.81 66.39 Comp 10 J 9.91 99.71 1.30 44.03 48.71 53.52

[0124] Under these conditions, all catalysts were shown to crack the 3-methylpentane and methylcyclopentane.

[0125] The catalysts according to the invention show an improved or at least the same hydrocracking activity giving the same or increased benzene purity as shown in table above.

Calcination Temperature Analysis

[0126] The effect of calcination temperature on the platinum (Pt) particle size was examined. The calcination was in air at the temperature set forth in Table 3. The particle size was determined using a Scanning Transmission Electron Microscopy (STEM) using a TECNAI-F20 microscope, measuring at least 6 particles. High Angular Annular Dark Field (HAADF) detector was used in the STEM mode to study the material.

TABLE-US-00003 TABLE 3 Calcination l Further Calcination Average Pt time (hr) at Calcination Temperature particle size Example Catalyst 280 C. time (hr).sup.2 ( C.) Pt wt % (nm) 11 I 6 280 0.070 (not detected).sup.1 12 I 6 3 600 0.070 14.7 13 E 2 280 0.256 0.9 14 E 2 3 500 0.256 25 15 E 2 2 600 0.256 99 .sup.1Below detection limit of 0.5 nm. .sup.2The catalyst was initially calcined at 280 C. and then further calcined at the higher temperature to determine the effect of calcining at a higher temperature. The ramp rate was 2 C./min.

[0127] As can be seen in Table 3, as the calcination temperature increases, the particle size increases. The change from 500 C. to 600 C. increased the particle size by nearly 300%. Changing the calcination temperature from 280 C. to 500 C. showed an increase of well over 500%. Actually, Table 3 shows that the average Pt particle size is less than or equal to 1 nm when the Pt containing catalyst was calcined at 280 C. in air, yet well over 10 nm when calcined at higher temperatures such as 500 C. Smaller particle sizes have greater surface area and greater activity. Clearly calcining at a higher temperature produces a different catalyst.

[0128] Set forth below are some embodiments of the catalyst, method of making the catalyst, and method of using the catalyst disclosed herein.

Embodiment 1

[0129] A process for preparing a hydrocracking catalyst, comprising: (i) combining a zeolite, a binder, water and a hydrogenating metal compound which is a complex or a salt of a hydrogenating metal to obtain a mixture, wherein the zeolite has not been treated by a phosphorus-containing compound and the zeolite has a silica to alumina molar ratio of 5-200; (ii) forming the mixture into a shaped body; and (iii) calcining the shaped body at 250-300 C., preferably 250-295 C., for 2-8 hours to form the catalyst.

Embodiment 2

[0130] The process according to any one of the preceding embodiments, wherein the catalyst has an average hydrogenating metal particle size of less than or equal to 5 nm, preferably less than or equal to 3 nm, or less than or equal to 2 nm, as determined using TEM.

Embodiment 3

[0131] The process according to any one of the preceding embodiments, wherein the mixture is a paste.

Embodiment 4

[0132] A process for preparing a hydrocracking catalyst, comprising: (i) combining a zeolite, a binder, and a hydrogenating metal compound which is a complex or a salt of a hydrogenating metal, with water to form a paste, wherein the zeolite has not been treated by a phosphorus-containing compound, and wherein the zeolite has a silica to alumina molar ratio of 5-200; (ii) forming the paste into a shaped body; and (iii) calcining the shaped body to form the catalyst; wherein the catalyst has an average hydrogenating metal particle size of less than or equal to 5 nm, preferably less than or equal to 3 nm, or less than or equal to 2 nm, as determined using TEM.

Embodiment 5

[0133] The process according to Embodiment 4, wherein the shaped body is calcined at 250-300 C., preferably 250-295 C., for 2-8 hours.

Embodiment 6

[0134] The process according to any one of Embodiments 3-5, wherein the paste is an extrudable paste.

Embodiment 7

[0135] The process according to any of the preceding embodiments, wherein step (i) involves: combining the zeolite and the hydrogenating metal compound and subsequently adding the binder to the combination of the zeolite and the hydrogenating metal compound; or combining the hydrogenating metal compound and the binder and subsequently adding the zeolite to the combination of the binder and the hydrogenating metal compound.

Embodiment 8

[0136] The process according to any one of the preceding embodiments, wherein the zeolite is selected from the group consisting of ZSM-5, MCM-22, ZSM-11, beta zeolite, EU-1 zeolite, faujasite (zeolite Y), ferrierite and mordenite and preferably the zeolite is ZSM-5.

Embodiment 9

[0137] The process according to any one of the preceding embodiments, wherein the silica to alumina molar ratio is 25-75, preferably 30-65, more preferably 35-60, more preferably 40-55.

Embodiment 10

[0138] The process according to any one of the preceding embodiments, wherein the zeolite is an H.sup.+-form or NH.sub.4.sup.+-form.

Embodiment 11

[0139] The process according to any one of the preceding embodiments, wherein the binder is an inorganic oxide material preferably selected from the group consisting of alumina, clay, silica-alumina, aluminum phosphate and combinations thereof, preferably alumina.

Embodiment 12

[0140] The process according to any one of the preceding embodiments, wherein the binder has been treated with a mineral acid such as nitric acid, hydrochloric acid, phosphoric acid or sulfuric acid, preferably nitric acid.

Embodiment 13

[0141] The process according to any one of the preceding embodiments, wherein the amount of binder is 10 to 90 wt % relative to the total weight of the catalyst.

Embodiment 14

[0142] The process according to any one of the preceding embodiments, wherein the hydrogenating metal is at least one element selected from Group 10 of the periodic table of elements or rhodium or iridium, preferably palladium or platinum, most preferably platinum.

Embodiment 15

[0143] The process according to any one of the preceding embodiments, wherein the hydrogenating metal compound is selected from the group consisting of H.sub.2PtCl.sub.6, (NH.sub.3).sub.4Pt(NO.sub.3).sub.2, (NH.sub.3).sub.4Pt(OH).sub.2 and (NH.sub.3).sub.4PtCl.sub.2.

Embodiment 16

[0144] The process according to any one of the preceding embodiments, wherein the amount of the hydrogenating metal is 0.010-0.30 wt %, preferably 0.015-0.095 wt %, more preferably 0.035-0.080 wt %, with respect to the total catalyst.

Embodiment 17

[0145] The process according to any one of the preceding embodiments, wherein the shaped body is an extrudate having an average diameter of 0.5-5 mm.

Embodiment 18

[0146] The process according to any one of the preceding embodiments, wherein the only metal in the catalyst is the hydrogenating metal.

Embodiment 19

[0147] The process according to any one of the preceding embodiments, wherein the hydrogenating metal consists of at least one element selected from Group 10 of the periodic table of elements, rhodium, and iridium, preferably the hydrogenating metal consists of at least one of palladium and platinum, most preferably the hydrogenating metal consists of platinum.

Embodiment 20

[0148] The process according to any one of the preceding embodiments, wherein the shaped body consists of the zeolite, the binder, the water, and the hydrogenating metal compound.

Embodiment 21

[0149] The process according to any one of the preceding embodiments, wherein the catalyst consists of the calcined shaped body.

Embodiment 22

[0150] The process according to any one of the preceding embodiments, wherein the shaped body is formed before the hydrogenating metal and binder are calcined.

Embodiment 23

[0151] The process according to any one of the preceding embodiments, wherein catalyst comprises platinum, and preferably comprises less than 0.01 wt % of the hydrogenating metals, based upon the total weight of the catalyst.

Embodiment 24

[0152] The process according to any one of the preceding embodiments, wherein the mixture is mixed for a period of time of less than or equal to 20 minutes, preferably less than or equal to 10 minutes, prior to forming into the shaped body.

Embodiment 25

[0153] The hydrocracking catalyst obtainable by the process according to any one of the preceding embodiments.

Embodiment 26

[0154] A process for hydrocracking a feed stream comprising hydrocarbons by contacting the feed stream in the presence of hydrogen with the hydrocracking catalyst according to Embodiment 25.

Embodiment 27

[0155] The process according to Embodiment 26, comprising: contacting a hydrocracking feed stream in the presence of hydrogen with a hydrocracking catalyst to produce a hydrocracking product stream comprising BTX, preferably the contacting is under process conditions including a temperature of 400-580 C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 0.1-30 hr.sup.1, wherein the hydrocracking feed stream comprises C.sub.5-C.sub.12 hydrocarbons; and (c) separating the BTX from the hydrocracking product stream.

[0156] The present application claims priority to EP Application No. 16182324.0 filed on Aug. 2, 2016, which is incorporated herein in its entirety.