Carbo-metallic oil conversion with liquid water containing H2 S

Claim 2

A process for economically converting carbo-metallic oils to lighter products, comprising: I. providing a converter feed containing 650° F.+ material, said 650° F.+ material being characterized by a carbon residue on pyrolysis of at least about 1 and by containing at least about 5 parts per million of nickel and vanadium combined; II. bringing said converter feed together with cracking catalyst having an equilibrium microactivity test conversion activity level of at least about 40 and bearing an accumulation of at least about 1,000 ppm combined of nickel and vanadium expressed as weight of metal(s) on regenerated equilibrium catalyst; III. bringing said converter feed together with liquid water in a weight ratio relative to feed in the range of about 0.04 to about 0.15, said liquid water containing at least 100 ppm hydrogen sulfide, less than 100 ppm sodium and less than 500 ppm each of calcium and magnesium; IV. forming a stream containing a mixture of said converter feed, said catalyst and steam resulting from the vaporization of said liquid water and causing the resultant stream to flow through a progressive flow type reactor having an elongated reaction chamber which is at least in part vertical or inclined for a vapor residence time in the range of about 0.5 to about 10 seconds at a reaction chamber outlet temperature of about 900° to about 1400° F. and under a pressure of about 10 to about 50 pounds per square inch absolute sufficient for causing a conversion per pass in the range of about 50% to about 90% while producing coke in amounts greater than about 6% by weight based on fresh feed, and laying down coke on the catalyst in amounts greater than about 0.3 percent by weight based on catalyst; V. separating said catalyst from the resultant cracking products; VI. stripping said separated catalyst; VII. regenerating said catalyst; and, VIII. recycling the regenerated catalyst to the reactor for contact with fresh feed.

Claim 3

A process accordingly to claim 1 in which said 650° F.+ material contains at least about 4.0 ppm of Nickel Equivalents of heavy metal(s).

Claim 4

A process according to claim 2 in which the equilibrium microactivity test conversion level of said catalyst is at least about 60.

Claim 5

A process according to claim 3 in which said catalyst has an accumulation of at least about 3,000 ppm by weight of Nickel Equivalents of heavy metal(s) expressed as metal(s) on regenerated equilibrium catalyst.

Claim 6

A process according to claim 4 in which said catalyst is regenerated with oxygen-containing combustion-supporting gas under conditions of time, temperature and atmosphere sufficient to reduce the carbon on the catalyst to about 0.25% by weight or less while forming gaseous combustion products comprising carbon monoxide and/or carbon dioxide.

Claim 7

A process according to claim 5 in which said resultant stream flows through said reactor at a lineal velocity of at least about 25 feet per second.

Claim 8

A process according to claim 6 in which said reaction chamber outlet temperature is in the range of about 985° to about 1200° F.

Claim 9

A process according to claim 7 in which said resultant stream flows through said reactor under a pressure of about 15 to about 35 pounds per square inch absolute.

Claim 10

A process according to claim 8 in which said conversion per pass is in the range of about 60% to about 90%.

Claim 11

A process according to claim 9 in which said coke is produced in amounts in the range of about 6 to about 14% by weight based on fresh feed, and coke is laid down on said catalyst in amounts in the range of about 0.3 to about 3% by weight based on catalyst.

Claim 12

A process according to claim 10 in which said converter feed has had substantially no hydrotreatment and comprises at least about 70% by volume of said 650° F.+ material.

Claim 13

A process according to claim 11 in which the ratio of the partial pressure of added gaseous and/or vaporized material, including steam, relative to the partial pressure of the feed in said resultant stream is in the range of about 0.25 to about 4.0.

Claim 14

A process according to claim 12 in which said vapor residence time is less than about 3 seconds.

Claim 15

A process according to claim 13 in which said catalyst regenerating step reduces the carbon on the catalyst to about 0.1% by weight or less.

Claim 16

A process according to claim 1 in which the step of separating said catalyst from the resultant cracking products includes abruptly separating catalyst from product vapors at the downstream end of said elongated reaction chamber, discharging the catalyst thus separated into a catalyst collection chamber, and preventing at least about 80% by volume of the total converter feed and product vapors which have passed through said elongated reaction chamber from having further contact with the thus separated catalyst in said catalyst collection chamber.

Claim 17

A process according to claim 1 in which said catalyst is a regenerated equilibrium catalyst bearing an accumulation of at least about 3,000 ppm by weight of Nickel Equivalents expressed as heavy metal(s) on regenerated equilibrium catalyst.

Claim 18

A process according to claim 1 in which the 650° F.+ material includes at least about 10% by volume of material which will not boil below about 1,000° F.

Claim 19

A process according to claim 1 in which the 650° F.+ material includes at least about 10% by volume of material which will not boil below about 1,025° F.

Claim 20

A process according to claim 1 wherein said carbon residue corresponds with a Ramsbottom carbon value in the range of about 2 to about 12.

Claim 21

A process according to claim 1 wherein the carbon residue of the feed as a whole corresponds with a Ramsbottom carbon value of at least about 1.

Claim 22

A process according to claim 20 wherein said Ramsbottom carbon value is in the range of about 2 to about 12.

Claim 23

A process according to claim 1 wherein the feed as a whole contains at least about 4 ppm by weight of Nickel Equivalents expressed as heavy metal(s) on regenerated equilibrium catalyst, of which at least about 2 ppm is nickel.

Claim 24

A process according to claim 1 wherein at least about 85% by volume of the feed is oil which has not previously been contacted with cracking catalyst under cracking conditions.

Claim 25

A process according to claim 1 wherein said feed comprises about 15% or less by volume of recycled oil.

Claim 26

A process according to claim 1 wherein said feed is processed in a substantially once-through or single pass mode with no substantial amount of recycled oil in the feed.

Claim 27

A process according to claim 1 wherein said catalyst is contact with said converter feed in said elongated reaction zone in a weight ratio of catalyst to converter feed in the range of about 3 to about 18.

Claim 28

A process according to claim 1 in which said 650° F.+ material represents at least about 70% by volume of said feed.

Claim 29

A process according to claim 27 in which said reaction chamber outlet temperature is in the range of about 985° to about 1200° F., said resultant stream flows through said reactor at a lineal velocity of at least about 25 feet per second, and said conversion per pass is in the range of about 60 to about 90 volume percent.

Claim 30

A process according to claim 1 wherein catalyst is added to the process at a rate in the range of about 0.1 to about 5 pounds of catalyst per barrel of feed.

Claim 31

A process according to claim 1 wherein said catalyst as introduced into the process has a microactivity of at least about 60 volume percent.

Claim 32

A process according to claim 1 wherein said catalyst has an equilibrium microactivity of at least about 60 volume percent.

Claim 33

A process according to claim 1 wherein said catalyst is equilibrium cracking catalyst which has previously been used in a fluid catalytic cracking unit in which said catalyst was used for the cracking of feed characterized by a carbon residue on pyrolysis of less than 1 and by containing less than about 4 ppm by weight of Nickel Equivalents expressed as heavy metal(s).

Claim 34

A process according to claim 1 wherein there is an accumulation of heavy metal(s) on said catalyst in the range of about 3,000 ppm to about 70,000 ppm by weight of Nickel Equivalents expressed as metal(s) on regenerated equilibrium catalyst.

Claim 35

A process according to claim 1 wherein there is an accumulation of heavy metal(s) on said catalyst in the range of about 4,000 ppm to about 50,000 ppm by weight of Nickel Equivalents expressed as metal(s) on regenerated equilibrium catalyst.

Claim 36

A process according to claim 1 wherein there is an accumulation of heavy metal(s) on said catalyst in the range of about 5,000 ppm to about 30,000 ppm by weight of Nickel Equivalents expressed as metal(s) on regenerated equilibrium catalyst.

Claim 37

A process according to claim 1 wherein said catalyst is characterized by a pore structure for absorbing hydrocarbon molecules and by reactive sites within or adjacent the pores.

Claim 38

A process according to claim 36 wherein said catalyst is a zeolite containing catalyst.

Claim 39

A process according to claim 37 wherein said zeolite containing catalyst is a molecular sieve catalyst which includes at least about 5% by weight of sieve.

Claim 40

A process according to claim 1 wherein the total amount of gaseous and/or vaporized material other than converter feed and resultant products which is present in said reaction zone is in a weight ratio of up to about 0.4 relative to converter feed.

Claim 41

A process according to claim 1 wherein the total amount of gaseous and/or vaporized material other than converter feed and resultant products which is present in said reaction zone is in a weight ratio in the range of about 0.02 to about 0.4 relative to converter feed.

Claim 42

A process according to claim 1 wherein the total amount of gaseous and/or vaporized material other than converter feed and resultant products which is present in said reaction zone is in a weight ratio in the range of about 0.03 to about 0.3 relative to converter feed.

Claim 43

A process according to claim 1 wherein the total amount of gaseous and/or vaporized material other than converter feed and resultant products which is present in said reaction zone is in a weight ratio in the range of about 0.05 to about 0.25 relative to converter feed.

Claim 44

A process according to claim 1 wherein said reactor is a riser type reactor.

Claim 45

A process according to claim 1 wherein said reactor is a vented riser type reactor.

Claim 46

A process according to claim 1 wherein said residence time of the converter feed and product vapors is in the range of about 0.5 to about 6 seconds.

Claim 47

A process according to claim 1 wherein said residence time of the converter feed and product vapors is in the range of about 1 to about 4 seconds.

Claim 48

A process according to claim 1 wherein said residence time of the conveter feed and product vapors is in the range of about 1.5 to about 3 seconds.

Claim 49

A process according to claim 1 wherein the ratio of average catalyst residence time to vapor residence time is in the range of about 1 to about 5.

Claim 50

A process according to claim 1 wherein the ratio of average catalyst residence time to vapor residence time is in the range of about 1 to about 4.

Claim 51

A process according to claim 1 wherein the ratio of average catalyst residence time to vapor residence time is in the range of about 1.2 to about 3.

Claim 52

A process according to claim 1 wherein the ratio of average catalyst residence time to vapor residence time is in the range of about 1.2 to about 2.

Claim 53

A process according to claim 1 wherein the reactor pressure is in the range of about 15 to about 35 psia.

Claim 54

A process according to claim 1 wherein the feed partial or total pressure is in the range of about 3 to about 30 psia.

Claim 55

A process according to claim 1 wherein the feed partial or total pressure is in the range of about 7 to about 25 psia.

Claim 56

A process according to claim 1 wherein the feed partial or total pressure is in the range of about 10 to about 17 psia.

Claim 57

A process according to claim 1 wherein said conversion is in the range of about 60 to about 90 volume percent.

Claim 58

A process according to claim 1 wherein the coke laydown on said catalyst is in the range of about 0.5 to about 3% by weight based on weight of catalyst.

Claim 59

A process according to claim 1 in which the liquid water is brought together with the converter feed prior to bringing said converter feed into contact with the cracking catalyst.

Claim 60

A process according to claim 1 in which the total amount of liquid water added to converter feed is in the range of about 5% to about 15% by weight of said carbonaceous portion of the feed.

Claim 61

A process according to claim 1 in which the weight ratio of liquid water to converter feed is about 0.05 to about 0.1.

Claim 62

A process according to claim 1 in which the liquid water and converter feed are mixed in an atomizing nozzle and sprayed into contact with the catalyst.

Claim 63

A process according to claim 1 in which at least a portion of said liquid water is recycle water condensed from a product stream of a previously converted hydrocarbon feed.

Claim 64

A process according to claim 1 in which said liquid water contains at least 120 ppm by weight of hydrogen sulfide, and in which said conversion per pass comprises a yield of C 5 -430° F. gasoline representing at least about 44% by volume of the total amount of fresh feed.

Claim 65

A process according to claim 1 in which the total amount of liquid water added to the feed is in the range of about 1% to about 25% by weight of said carbonaceous portion of the feed.

Claim 66

A process according to claim 64 in which said liquid water contains more than 1000 ppm dissolved H 2 S.

Claim 67

The process of claim 65 in which said liquid water contains less than 25 ppm sodium, and at least 2000 ppm combined of nickel and vanadium is deposited on the catalyst.

Claim 68

The process of claim 66 in which the conversion catalyst is a cracking catalyst containing zeolite.

Claim 69

The process of claim 1, claim 64, claim 65, claim 66 or claim 67 in which substantially all of the liquid water added to the feed is recycle water.

Claim 70

A process according to claim 1 in which said reaction chamber outlet temperature is in the range of about 975° to about 1300° F.

Claim 71

A process according to claim 1 in which the liquid water is brought together with the converter feed simultaneously with or subsequent to bringing said converter feed into contact with the cracking catalyst.

Claim 72

A process for economically converting carbo-metallic oils to lighter products, comprising: I. providing a converter feed containing 650° F.+ material, said converter feed being characterized by a carbon residue on pyrolysis of at least about 1 and by containing at least about 4 ppm of Nickel Equivalents of heavy metal(s); II. bringing said converter feed together with liquid water in a weight ratio relative to converter feed in the range of about 0.04 to about 0.15, said liquid water containing at least 100 ppm by weight of hydrogen sulfide; III. bringing said converter feed together with cracking catalyst having an equilibrium MAT conversion activity level of at least about 60 volume percent and bearing an accumulation of at least about 3000 ppm by weight of nickel equivalents of heavy metal(s) expressed as metal(s) on regenerated equilibrium catalyst; IV. forming a stream containing a mixture of said converter feed, said catalyst and steam resulting from the vaporization of said liquid water and causing the resultant stream to flow through a progressive flow type reactor having an elongated reaction chamber which is at least in part vertical or inclined at a lineal velocity of at least about 35 feet per second for a vapor residence time in the range of about 0.5 to about 6 seconds at a reaction chamber outlet temperature of about 975° to about 1300° F. and under a pressure of about 10 to about 50 pounds per square inch absolute sufficient for causing a conversion per pass in the range of about 60% to about 90% while producing coke in amounts greater than about 6% by weight based on fresh feed, and laying down coke on the catalyst in amounts in the range of about 0.3 to about 3% by weight; V. separating said catalyst from at least a substantial portion of the stream comprising said catalyst, steam and resultant cracking products formed in the elongated reaction chamber; VI. stripping said separated catalyst; VII. regenerating said catalyst; and VIII. recycling the regenerated catalyst to the reactor for contact with fresh feed.

Claim 73

A process for economically converting carbo-metallic oils to lighter products, comprising: I. providing a converter feed containing 650° F.+ material, said converter feed being characterized by a carbon residue on pyrolysis of at least about 1 and by containing at least about 4 ppm of Nickel Equivalents of heavy metal(s); II. bringing said converter feed together with liquid water in a weight ratio relative to converter feed in the range of about 0.04 to about 0.15, said liquid water containing at least 100 ppm by weight of hydrogen sulfide; III. bringing said converter feed together with cracking catalyst having an equilibrium MAT conversion activity level of at least about 60 volume percent and bearing an accumulation of at least about 3000 ppm by weight of nickel equivalents of heavy metal(s) expressed as metal(s) on regenerated equilibrium catalyst; IV. forming a stream containing a mixture of said converter feed, said catalyst and steam resulting from the vaporization of said liquid water and causing the resultant stream to flow through a progressive flow type reactor having an elongated reaction chamber which is at least in part vertical or inclined at a lineal velocity of at least about 35 feet per second for a vapor residence time in the range of about 0.5 to about 6 seconds at a reaction chamber outlet temperature of about 975° to about 1300° F. and under a pressure of about 10 to about 50 pounds per square inch absolute sufficient for causing a conversion per pass in the range of about 60% to about 90% while producing coke in amounts greater than about 6% by weight based on fresh feed, and laying down coke on the catalyst in amounts in the range of about 0.3 to about 3% by weight; V. separating said catalyst from at least a substantial portion of the stream comprising said catalyst, steam and resultant cracking products formed in the elongated reaction chamber; VI. stripping said separated catalyst; VII. regenerating said catalyst; and VIII. recycling the regenerated catalyst to the reactor for contact with fresh feed.

Claim 74

A process according to claim 71 in which at least a portion of said liquid water is recycle water condensed from a product stream of a previously converted hydrocarbon feed.

Claim 75

A process according to claim 71 wherein said weight ratio of liquid water to converter feed is in the range of about 0.04 to about 0.1.

Claim 76

A process according to claim 71 wherein water is brought into contact with said converter feed in said stream and/or prior to formation of said stream in the form of steam in a weight ratio relative to feed in the range of about 0.01 to about 0.25 and in the form of said liquid water, the total water thus supplied not exceeding a weight ratio of about 0.3 relative to converter feed.

Claim 77

A process according to claim 71 wherein said accumulation of heavy metal(s) on said catalyst is at least about 4,000 ppm by weight of Nickel Equivalents expressed as metal(s) on regenerated equilibrium catalyst.

Claim 78

A process according to claim 71 wherein said accumulation of heavy metal(s) on said catalyst is at least about 5,000 ppm by weight of Nickel Equivalents expressed as metal(s) on regenerated equilibrium catalyst.

Claim 79

A process according to claim 71 wherein said elongated reaction chamber outlet temperatures is in the range of about 985° to about 1200° F.

Claim 80

A process according to claim 71 wherein said conversion is in the range of about 70% to about 85%.

Claim 81

A process for economically converting carbo-metallic oils to lighter products, comprising: I. providing a converter feed that has had substantially no prior hydrotreatment and contains at least about 70% by volume of 650° F.+ material and at least about 10% by volume of material which will not boil below about 1025° F., said converter feed being characterized by a carbon residue on pyrolysis of at least about 2 and by containing at least about 5.5 ppm of Nickel Equivalents of heavy metal(s); II. bringing said converter feed together with liquid water in a weight ratio relative to converter feed in the range of about 0.04 to about 0.15, said liquid water containing at least about 100 ppm by weight of hydrogen sulfide, less than 100 ppm sodium and less than 500 ppm each of calcium and magnesium, and at least a portion of said liquid water being recycle water condensed from a product stream of a previously converted hydrocarbon feed; III. bringing said converter feed together with hot cracking catalyst at a catalyst to fresh converter feed weight ratio of at least about 6, said catalyst having an equilibrium MAT conversion activity level of at least about 60 volume percent and bearing an accumulation of more than about 500 ppm by weight of Nickel Equivalents of heavy metal(s) expressed as metal(s) on regenerated equilibrium catalyst; IV. forming a stream containing fine droplets of said converter feed, said catalyst and steam resulting from the vaporization of said liquid water and causing the resultant stream to flow through a progressive flow type reactor having an elongated riser reaction chamber which is at least in part vertical or inclined at a lineal velocity of at least about 35 feed per second for a vapor residence time in the range of about 0.5 to about 3 seconds at a reaction chamber outlet temperature of about 985° to about 1200° F. and under a pressure of about 15 to about 35 pounds per square inch absolute sufficient for causing a conversion per pass in the range of about 60% to about 90% while producing coke in amounts greater than about 6% by weight based on fresh feed, and laying down coke on the catalyst in amounts in the range of about 0.3 to about 3% by weight, but insufficient for fully vaporizing the converter feed; V. separating said catalyst from at least a substantial portion of the stream comprising said catalyst, steam and resultant cracking products formed in the elongated reaction chamber; VI. stripping said separated catalyst; VII. regenerating said catalyst; and VIII. recycling the regenerated catalyst to the reactor for contact with fresh feed.

Claim 82

A process for economically converting carbo-metallic oils to lighter products, comprising: I. providing a converter feed that has had substantially no prior hydrotreatment and contains at least about 70% by volume of 650° F.+ material and at least about 10% by volume of material which will not boil below about 1025° F., said converter feed being characterized by a carbon residue on pyrolysis of at least about 2 and by containing at least about 5.5 ppm of Nickel Equivalents of heavy metal(s); II. bringing said converter feed together with liquid water in a weight ratio relative to converter feed in the range of about 0.04 to about 0.15, said liquid water containing at least about 100 ppm by weight of hydrogen sulfide, less than 100 ppm sodium and less than 500 ppm each of calcium and magnesium, and at least a portion of said liquid water being recycle water condensed from a product stream of a previously converted hydrocarbon feed; III. bringing said converter feed together with hot cracking catalyst at a catalyst to fresh converter feed weight ratio of at least about 6, said catalyst having an equilibrium MAT conversion activity level of at least about 60 volume percent and bearing an accumulation of more than about 500 ppm by weight of Nickel Equivalents of heavy metal(s) expressed as metal(s) on regenerated equilibrium catalyst; IV. forming a stream containing fine droplets of said converter feed, said catalyst and steam resulting from the vaporization of said liquid water and causing the resultant stream to flow through a progressive flow type reactor having an elongated riser reaction chamber which is at least in part vertical or inclined at a lineal velocity of at least about 35 feed per second for a vapor residence time in the range of about 0.5 to about 3 seconds at a reaction chamber outlet temperature of about 985° to about 1200° F. and under a pressure of about 15 to about 35 pounds per square inch absolute sufficient for causing a conversion per pass in the range of about 60% to about 90% while producing coke in amounts greater than about 6% by weight based on fresh feed, and laying down coke on the catalyst in amounts in the range of about 0.3 to about 3% by weight, but insufficient for fully vaporizing the converter feed; V. separating said catalyst from at least a substantial portion of the stream comprising said catalyst, steam and resultant cracking products formed in the elongated reaction chamber; VI. stripping said separated catalyst; VII. regenerating said catalyst; and VIII. recycling the regenerated catalyst to the reactor for contact with fresh feed.

Claim 83

In a method for the conversion of an oil feed containing a portion having a high level of coke-forming carbonaceous materials, which portion exhibits a Conradson carbon value of greater than 1 and/or a combined level of vanadium and nickel of greater than 5 ppm, by contacting in a continuous process such feed in the upstream end of a tubular reaction zone with heated particulate conversion catalyst in the presence of water, the improvement of introducing to the feed liquid water containing at least 100 ppm H 2 S, less than 100 ppm sodium and less than 500 ppm each of calcium and magnesium, and also introducing to the feed a conversion catalyst having at least 1000 ppm combined of nickel and vanadium deposited on the catalyst.

Claim 84

In a method for the conversion of an oil feed containing a portion having a high level of coke-forming carbonaceous materials, which portion exhibits a Conradson carbon value of greater than 1 and/or a combined level of vanadium and nickel of greater than 5 ppm, by contacting in a continuous process such feed in the upstream end of a tubular reaction zone with heated particulate conversion catalyst in the presence of water, the improvement of introducing to the feed liquid water containing at least 100 ppm H 2 S, less than 100 ppm sodium and less than 500 ppm each of calcium and magnesium, and also introducing to the feed a conversion catalyst having at least 1000 ppm combined of nickel and vanadium deposited on the catalyst.

Claim 85

The process of claim 80 wherein the total amount of liquid water added to the feed is in the range of about 1% to about 25% by weight of said carbonaceous portion of the feed, and said liquid water contains more than 1000 ppm dissolved H 2 S.

Claim 86

The process of claim 80 or claim 81 wherein the total amount of liquid water added to the feed is between 5 and 15% by weight of said carbonaceous portion of the feed.

Claim 87

The process of claim 80 or claim 81 wherein said liquid water contains less than 25 ppm sodium, and at least 2000 ppm combined of nickel and vanadium is deposited on the catalyst.

Claim 88

The process of claim 80 or claim 81 wherein the conversion catalyst is a cracking catalyst containing zeolite.

Claim 89

The process of claim 80 or claim 81 wherein at least a portion of said liquid water comprises recycle water condensed from the product stream of a previously converted oil feed.

Claim 90

The process of claim 80 or claim 81 wherein substantially all of said liquid water introduced to the feed is recycle water condensed from the product stream of a previously converted oil feed.

Claim 91

In a method for the conversion of an oil feed containing a portion having a high level of coke-forming carbonaceous materials, which portion exhibits a Conradson carbon value of greater than 1 and/or a combined level of vanadium and nickel of greater than 5 ppm, by contacting in a continuous process such feed in the upstream end of a tubular reaction zone with heated particulate conversion catalyst in the presence of water, the improvement of introducing to the feed liquid water containing at least about 100 ppm H 2 S, less than 100 ppm sodium and less than 500 ppm each of calcium and magnesium, and also introducing to the feed a conversion catalyst having at least 1000 ppm combined of nickel and vanadium deposited on the catalyst, at least a portion of said liquid water comprising recycle water condensed from the product stream of a previously converted oil feed.

Claim 92

In a method for the conversion of an oil feed containing a portion having a high level of coke-forming carbonaceous materials, which portion exhibits a Conradson carbon value of greater than 1 and/or a combined level of vanadium and nickel of greater than 5 ppm, by contacting in a continuous process such feed in the upstream end of a tubular reaction zone with heated particulate conversion catalyst in the presence of water, the improvement of introducing to the feed liquid water containing at least about 100 ppm H 2 S, less than 100 ppm sodium and less than 500 ppm each of calcium and magnesium, and also introducing to the feed a conversion catalyst having at least 1000 ppm combined of nickel and vanadium deposited on the catalyst, at least a portion of said liquid water comprising recycle water condensed from the product stream of a previously converted oil feed.