Partial oxidation process

Claim 2

A process for the production of gaseous mixtures comprising H 2 +CO by the partial oxidation of a feedstock comprising a heavy liquid hydrocarbonaceous fuel having a nickel and vanadium-containing ash or petroleum coke having a nickel and vanadium-containing ash, or mixtures thereof; and said feedstock includes a minimum of 0.5 wt. % of sulfur; and said ash includes a minimum of 5.0 wt. % vanadium, a minimum of 2.0 wt. % of nickel and less than about 350 parts per million of silicon; said process comprising: (1) mixing together an iron-containing additive comprising at least one iron compound with said feedstock; wherein the weight ratio of iron-containing additive to ash in the reaction zone in (2) is in the range of about 1.0-10.0 to 1.0, and there is at least 10 parts by weight of iron for each part by weight of vanadium; (2) reacting said mixture from (1) at a temperature the range of 2200° F. to 3000° F. and a pressure in the range of about 5 to 250 atmospheres in a free-flow refractory lined partial oxidation reaction zone with a free-oxygen containing gas in the presence of a temperature moderator and in a reducing atmosphere to produce a hot raw effluent gas stream comprising H 2 +CO and entrained molten slag; and where in said reaction zone said iron-containing additive combines with at least a portion of said nickel constituents and sulfur found in the feedstock to produce a liquid phase washing agent that collects and transports at least a portion of the vanadium-containing oxide laths and spinels and other ash components and refractory out of the reaction zone; and (3) separating nongaseous materials from said hot raw effluent gas stream.

Claim 3

The process of claim 1 wherein said iron-containing additive contains iron compounds selected from the group consisting of oxides, sulfides, sulfates, carbonates, cyanides, chlorides, nitrates, and mixtures thereof.

Claim 4

The process of claim 1 wherein the iron containing portion of said iron-containing additive is a ferro or ferri organic compound selected from the group consisting of naphthenates, oxalates, acetates, citrates, benzoates, oleates, tartrates, and mixtures thereof.

Claim 5

The process of claim 1 wherein the iron containing portion of said iron-containing additive is a water soluble iron salt.

Claim 6

The process of claim 1 wherein said heavy liquid hydrocarbonaceous fuel having a nickel and vanadium-containing ash feedstock is selected from the group consisting of crude residue from petroleum distillation and cracking process operations, petroleum distillate, reduced crude, whole crude, asphalt, coal tar, coal derived oil, shale oil, tar sand oil, and mixtures thereof.

Claim 7

The process of claim 1 wherein said heavy liquid hydrocarbonaceous fuel having a nickel and vanadium-containing ash is a pumpable slurry of petroleum coke in water, liquid hydrocarbon fuel or mixtures thereof.

Claim 8

The process of claim 1 where in (1) said iron-containing additive is introduced into the feed to or the bottoms from a vacuum distillation unit.

Claim 9

The process of claim 1 wherein said mixture of iron-containing additive and feedstock from (1) has a particle size of ASTM E-11 Standard Sieve Designation in the range of about 210 microns to 37 microns, or below.

Claim 10

The process of claim 1 wherein said iron-containing additive comprises about 30.0 to 100.0 wt. % of an iron compound.

Claim 11

The process of claim 1 wherein substantially all of the sulfur in said feedstock is converted into the sulfides of iron and nickel and leaves the reaction zone in the slag.

Claim 12

The process of claim 1 wherein a calcium compound in the amount of about 2.0 to below 8.0 wt. % of said iron-containing addition agent is only introduced into the reaction zone of the partial oxidation reaction zone at start-up to reduce the softening temperature of the iron-containing addition agent, and then discontinued.

Claim 13

The process of claim 1 wherein said iron-containing additive is iron oxide; and said iron oxide is in admixture with calcium oxide.

Claim 14

The process of claim 1 where included in the iron-containing additive in (1) is an additional material compound selected from the group of elements consisting of magnesium, chromium and mixtures thereof.

Claim 15

The process of claim 13 wherein said additional material comprises magnesium and/or chromium which are provided as compounds in the total amount of about 1.0 to 10.0 wt. % of said iron-containing additive.

Claim 16

The process of claim 14 wherein said magnesium and chromium compounds are oxides.

Claim 17

The process of claim 1 wherein said liquid phase washing agent substantially comprises in wt. %: iron sulfide about 75 to 95, nickel sulfide about 0.5 to 3.0, and iron oxide about 2 to 9.

Claim 18

In a process for coking a heavy liquid hydrocarbonaceous fuel having a nickel and vanadium containing ash to produce petroleum coke and gasifying said petroleum coke to produce gaseous mixtures comprising H 2 and CO, the improvement comprising: (1) mixing together said heavy liquid hydrocarbonaceous fuel with an iron-containing additive comprising at least one iron compound; wherein said heavy liquid hydrocarbonaceous fuel includes a minimum of 0.5 wt. % sulfur and has an ash which contains a minimum of 5.0 wt. % vanadium, a minimum of 2.0 wt. % nickel, and less than about 350 parts per million of silicon; and wherein the weight ratio of iron-containing additive to ash in the reaction zone in (4) is in the range of about 1.0-10.0 to 1.0, and there is at least 10 parts by weight of iron for each part by weight of vanadium; (2) coking said mixture from (1) to produce petroleum coke having a nickel and vanadium-containing ash and having dispersed therein said iron-containing additive; (3) introducing the petroleum coke from (2) into the partial oxidation reaction zone in (4) as a pumpable slurry of petroleum coke in water, liquid hydrocarbonaceous fluid or mixtures thereof, or as substantially dry petroleum coke entrained in a gaseous transport medium; (4) reacting said petroleum coke from (3) at a temperature in the range of 2200° F. to 3000° F. and a pressure in the range of about 5 to 250 atmospheres in said free-flow refractory lined partial oxidation reaction zone with a free-oxygen containing gas in the presence of a temperature moderator and in a reducing atmosphere to produce a hot raw effluent gas stream comprising H 2 +CO and entrained molten slag; and where in said reaction zone said iron-containing additive combined with at least a portion of said nickel constituents and sulfur found in the feedstock to produce a liquid phase washing carrier that collects and transports a portion of the vanadium-containing oxide laths and spinels and other ash components and refractory out of the reaction zone; and (5) separating nongaseous materials from said hot raw effluent gas stream.

Claim 19

In a process for coking a heavy liquid hydrocarbonaceous fuel having a nickel and vanadium containing ash to produce petroleum coke and gasifying said petroleum coke to produce gaseous mixtures comprising H 2 and CO, the improvement comprising: (1) mixing together said heavy liquid hydrocarbonaceous fuel with an iron-containing additive comprising at least one iron compound; wherein said heavy liquid hydrocarbonaceous fuel includes a minimum of 0.5 wt. % sulfur and has an ash which contains a minimum of 5.0 wt. % vanadium, a minimum of 2.0 wt. % nickel, and less than about 350 parts per million of silicon; and wherein the weight ratio of iron-containing additive to ash in the reaction zone in (4) is in the range of about 1.0-10.0 to 1.0, and there is at least 10 parts by weight of iron for each part by weight of vanadium; (2) coking said mixture from (1) to produce petroleum coke having a nickel and vanadium-containing ash and having dispersed therein said iron-containing additive; (3) introducing the petroleum coke from (2) into the partial oxidation reaction zone in (4) as a pumpable slurry of petroleum coke in water, liquid hydrocarbonaceous fluid or mixtures thereof, or as substantially dry petroleum coke entrained in a gaseous transport medium; (4) reacting said petroleum coke from (3) at a temperature in the range of 2200° F. to 3000° F. and a pressure in the range of about 5 to 250 atmospheres in said free-flow refractory lined partial oxidation reaction zone with a free-oxygen containing gas in the presence of a temperature moderator and in a reducing atmosphere to produce a hot raw effluent gas stream comprising H 2 +CO and entrained molten slag; and where in said reaction zone said iron-containing additive combined with at least a portion of said nickel constituents and sulfur found in the feedstock to produce a liquid phase washing carrier that collects and transports a portion of the vanadium-containing oxide laths and spinels and other ash components and refractory out of the reaction zone; and (5) separating nongaseous materials from said hot raw effluent gas stream.

Claim 20

The process of claim 17 wherein said iron-containing additive contains iron compounds selected from the group consisting of oxides, sulfides, sulfates, carbonates, cyanides, chlorides, nitrates, and mixtures thereof.

Claim 21

The process of claim 17 wherein said mixture of iron-containing additive and feedstock from (1) has a particle size of ASTME-11 Standard Sieve Designation in the range of about 210 microns to 37 microns or below.

Claim 22

The process of claim 17 wherein said iron-containing additive includes an inorganic or organic compound of iron.

Claim 23

The process of claim 17 wherein said ash-containing heavy liquid hydrocarbonaceous fuel is a high boiling liquid petroleum feed to or the bottoms from a vacuum tower or a fractionator.

Claim 24

The process of claim 17 where in (2) the mixture from (1) at a temperature in the range of about 650° F. to 930° F. is introduced into a delayed coking zone where at a temperature in the range of about 800° F. to 895° F. and a pressure in the range of about 20 to 60 psig, uncondensed hydrocarbon effluent vapor and steam are removed overhead and said petroleum coke having a nickel and vanadium-containing ash and having uniformly dispersed therein said iron-containing additive is removed from the bottom.

Claim 25

The process of claim 17 where in (2) the mixture from (1) at a temperature in the range of about 550° F. to 750° F. is introduced into a fluidized bed coking zone where at a temperature in the range of about 1000° F. to 1200° F. and a pressure in the range of about 10 to 20 psig, uncondensed hydrocarbon efflent vapor and steam are removed overhead and said petroleum coke is removed from the bottom.

Claim 26

The process of claim 17 where in (5) said nongaseous materials are separated from said hot effluent gas stream by contacting the gas stream from (4) with a water or oil scrubbing medium.

Claim 27

The process of claim 17 where included in the iron-containing additive in (1) is an additional material compound selected from the group of elements consisting of magnesium, chromium, and mixtures thereof.

Claim 28

The process of claim 25 wherein said additional material comprises magnesium and/or chromium which is provided as compounds in the total amount of about 1.0 to 10.0 wt. % of the iron-containing additive.

Claim 29

The process of claim 26 wherein said magnesium and chromium compounds are oxides.

Claim 30

The process of claim 17 wherein substantially all of the sulfur in said feedstock is converted into the sulfides of iron and nickel and leaves the reaction zone in the slag.

Claim 31

The process of claim 17 wherein a calcium compound in the amount of about 2.0 to below 8.0 wt. % of said iron-containing addition agent is temporarily introduced into the reaction zone of the partial oxidation reaction zone only at start-up to reduce the softening temperature of the iron-containing addition agent, and then the introduction of said calcium compound is discontinued.