US4400263A — H-Coal process and plant design

Claim 1

Independent Claim 165 words

A process for converting coal and/or other hydrocarbonaceous materials to more valuable liquid products, said process comprising: (a) feeding coal and/or other hydrocarbonaceous materials with a hydrogen-containing gas into an ebullated catalyst bed reactor; (b) passing the reaction products from the reactor to a separator where vaporous and distillate products are separated from the residuals of said reacted products; (c) introducing the vaporous and distillate products directly from the separator to a fixed catalyst bed hydrotreater where said products are further hydrogenated; (d) passing the residuals from said separator successively through flash vessels at reduced pressures where distillates are flashed off and combined with the vaporous and distillate products to be hydrogenated; (e) transferring the unseparated residuals to a solids concentrating and removal means to remove a substantial portion of solids therefrom and recycling the residual oil to the reactor; and (f) passing the hydrogenated distillate products from said hydrotreater to a low pressure fractionator where the combined products are fractionated into separate liquid products.

Claim 2

Dependent Claim 165 words

A process for converting coal and/or other hydrocarbonaceous materials to more valuable liquid products, said process comprising: (a) feeding coal and/or other hydrocarbonaceous materials with a hydrogen-containing gas into an ebullated catalyst bed reactor; (b) passing the reaction products from the reactor to a separator where vaporous and distillate products are separated from the residuals of said reacted products; (c) introducing the vaporous and distillate products directly from the separator to a fixed catalyst bed hydrotreater where said products are further hydrogenated; (d) passing the residuals from said separator successively through flash vessels at reduced pressures where distillates are flashed off and combined with the vaporous and distillate products to be hydrogenated; (e) transferring the unseparated residuals to a solids concentrating and removal means to remove a substantial portion of solids therefrom and recycling the residual oil to the reactor; and (f) passing the hydrogenated distillate products from said hydrotreater to a low pressure fractionator where the combined products are fractionated into separate liquid products.

Claim 3

Dependent Claim 20 words

The process of claim 1, wherein the reactor and hydrotreater operate under similar conditions of temperature and hydrogen partial pressure.

Claim 4

Dependent Claim 32 words

The process of claim 2, wherein the reactor and hydrotreater operate under a temperature ranging from about 750° F. to about 850° F. and a pressure of between 2,000 and 3,200 psi.

Claim 5

Dependent Claim 20 words

The process of claim 1, wherein the coal and/or other hydrocarbonaceous materials and the recycled residual oil are separately preheated.

Claim 6

Dependent Claim 30 words

The process of claim 4, wherein the coal is preheated to a temperature of about 350° F. before being mixed with the recycled residual oil and fed into said reactor.

Claim 7

Dependent Claim 28 words

The process of claim 1, wherein at least about 90% of the solids are removed from said residuals prior to said residual oil being recycled to said reactor.

Claim 8

Dependent Claim 15 words

The process of claim 1, wherein the solids concentrating and removal means is a centrifuge.

Claim 9

Dependent Claim 15 words

The process of claim 1, wherein said hydrogen-containing gas is generated from within the process.

Claim 10

Dependent Claim 29 words

The process of claim 8, wherein said hydrogen-containing gas is generated from naphtha in a catalytic reformer and from C 1 -C 4 hydrocarbon gases in a steam reformer.

Claim 11

Dependent Claim 24 words

The process of claim 6, wherein the residual underflow portion containing at least about 50W % solids is used as fuel for said process.

Claim 12

Dependent Claim 15 words

The process of claim 1, wherein said flash vessels operate at atmospheric and vacuum pressures.

Claim 13

Dependent Claim 18 words

The process of claim 1, wherein said fractionator operates within pressure range of about atmospheric to 50 psi.

Claim 14

Dependent Claim 175 words

A process for converting coal and/or other hydrocarbonaceous materials to more valuable liquid products, said processing comprising: (a) feeding coal and/or other hydrocarbonaceous materials with a residual oil and a hydrogen-containing gas generated from within the process into an ebullated catalyst bed reactor; (b) passing the reaction products from the reactor to a separator where vaporous and distillate products are separated from the residuals of said reacted products; (c) introducing the vaporous and distillate products directly from the separator to a fixed catalyst bed hydrotreater where said products are further hydrogenated; (d) passing the residuals from said separator successively through atmospheric and vacuum flash vessels where distillates are flashed off and combined with the vaporous and distillate products to be hydrogenated; (e) transferring the unseparated residuals to a solids concentrating and removal means to remove a substantial portion of solids therefrom and recycling the residual oil to the reactor; and (f) passing the hydrogenated vaporous and distillate products from said hydrotreater to an atmospheric fractionator where the combined products are fractionated into separate liquid products.

Claim 15

Dependent Claim 175 words

A process for converting coal and/or other hydrocarbonaceous materials to more valuable liquid products, said processing comprising: (a) feeding coal and/or other hydrocarbonaceous materials with a residual oil and a hydrogen-containing gas generated from within the process into an ebullated catalyst bed reactor; (b) passing the reaction products from the reactor to a separator where vaporous and distillate products are separated from the residuals of said reacted products; (c) introducing the vaporous and distillate products directly from the separator to a fixed catalyst bed hydrotreater where said products are further hydrogenated; (d) passing the residuals from said separator successively through atmospheric and vacuum flash vessels where distillates are flashed off and combined with the vaporous and distillate products to be hydrogenated; (e) transferring the unseparated residuals to a solids concentrating and removal means to remove a substantial portion of solids therefrom and recycling the residual oil to the reactor; and (f) passing the hydrogenated vaporous and distillate products from said hydrotreater to an atmospheric fractionator where the combined products are fractionated into separate liquid products.

Claim 16

Dependent Claim 20 words

The process of claim 13, wherein the reactor and hydrotreater operate under similar conditions of temperature and hydrogen partial pressure.

Claim 17

Dependent Claim 55 words

The process of claim 14, wherein the reactor operates under a temperature ranging from about 800° F. to about 850° F. and the hydrotreater operate under a temperature ranging from about 750° F. to about 825° F. and both said reactor and hydrotreater operate under a pressure of between about 2,000 and about 3,200 psig.

Claim 18

Dependent Claim 20 words

The process of claim 13, wherein the coal and/or other hydrocarbonaceous materials and the recycled residual oil are separately preheated.

Claim 19

Dependent Claim 30 words

The process of claim 16, wherein the coal is preheated to a temperature of about 350° F. before being mixed with the recycled residual oil and fed into said reactor.

Claim 20

Dependent Claim 28 words

The process of claim 13, wherein at least about 90% of the solids are removed from said residuals prior to said residual oil being recycled to said reactor.

Claim 21

Dependent Claim 15 words

The process of claim 13, wherein the solids concentrating and removal means in a centrifuge.

Claim 22

Dependent Claim 27 words

The process of claim 13, wherein said hydrogen-containing gas is generated from naphtha by catalytic reforming and from C 1 -C 4 hydrocarbon gases by steam reforming.

Annuity Stage	Window Opens	Payment Deadline	Surcharge Period Until	Estimated Fee	Status
3.5 Years (Year 4)	1986-08-22	1987-02-21	1987-08-23	$2000.00	Window Closed / Lapsed
7.5 Years (Year 8)	1990-08-22	1991-02-21	1991-08-23	$3760.00	Window Closed / Lapsed
11.5 Years (Year 12)	1994-08-22	1995-02-21	1995-08-23	$7700.00	Window Closed / Lapsed

H-Coal process and plant design

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