Direct reduction process with improved product quality and process gas efficiency

Patent metadata

Field	Value
Publication number	US-2016002744-A1
Application number	US-201414770366-A
Country	US
Kind code	A1
Filing date	Feb 27, 2014
Priority date	Feb 27, 2013
Publication date	Jan 7, 2016
Grant date	—

Abstract

A direct reduction process producing DRI from iron oxide particles by reduction at a about 750° C. with a reducing gas mainly H 2 and CO, that also includes CO 2 , H 2 0, and methane, a the reduction reactor and the top gas effluent from the reduction reaction after cooling/scrubbing is split. The resulting first top gas portion with a first hydrocarbon-containing make-up gas passes through a catalytic reformer yielding an improved hot reducing gas first effluent. The second top gas portion passes through a CO 2 removal unit and then with the second hydrocarbon-containing make-up gas passes through a heater yielding a hot CO 2 -lean recycle reducing gas second effluent. The first and second effluents are fed to the reducing zone of the reduction reactor as the reducing gas reactant. The flow rate of at least the second of the two make-up gases is regulated to control the carbon content of the DRI produced.

First claim

1 . A process producing direct reduced iron (DRI) from iron oxide particles reduced at a temperature of about 750° C. or above by means of a reducing gas mainly composed of H 2 and CO, that also includes CO 2 , H 2 0, and methane, in a direct reduction plant comprising
a reduction reactor producing a top gas;
a first top gas recycle circuit recycling a first portion of said top gas, comprising
a reduction zone in said reactor producing the top gas as an effluent from the reduction therein of said iron oxide particles,
a gas cooler/scrubber separating water from said top gas resulting in a cooled and dewatered top gas, and
a catalytic reformer reforming a mixture of a first hydrocarbon-containing make-up gas stream with oxidants present in the first portion of said cooled and dewatered top gas being fed thereto to yield an effluent mainly composed of H 2 and CO at a temperature on the order of 750° C. or above;

a second top gas recycle circuit recycling a second portion of said top gas, comprising
said reduction zone in the reactor producing the top gas as an effluent from the reduction therein of said iron oxide particles,
said gas cooler/scrubber separating water from said top gas resulting in said cooled and dewatered top gas,
a carbon dioxide removal unit stripping at least a portion of the carbon dioxide content of said second portion of said top gas and thus producing a CO 2 -lean recycle gas,
a process gas heating device raising the temperature of said CO 2 -lean recycle gas to yield an effluent at a temperature on the order of 750° C. or above, and

feeding, as said reducing gas, the effluent from said reformer and the effluent from said heating device into said reduction zone;

characterized by
feeding a second hydrocarbon-containing make-up gas stream to said second portion of said cooled and dewatered top gas; and
regulating the flow rate of the second make-up gas stream so that the carbon content of the DRI produced is regulated within predetermined values in response to the concentration of hydrocarbons in the hot gas effluent from said heating device.

2 . A process according to claim 1 , further characterized by combining the gas stream effluent from said reformer and the gas stream effluent from said heating device before feeding said combined hot gas stream to said reactor.

3 . A process according to claim 2 , further characterized by said hydrocarbon-containing gas is natural gas.

4 . A process according to claim 2 , further characterized by said hydrocarbon-containing gas is coke oven gas or a gas derived from coke oven gas.

5 . A process according to claim 2 , further characterized by said hydrocarbon-containing gas is a syngas derived from coal.

6 . A process according to claim 1 , further characterized by regulating the flow rate of the first make-up gas stream relative to the flow rate of the second make-up gas stream to regulate the amount of carbon content in the DRI; regulating the flow rate of said second make-up stream of hydrocarbon gas so that the concentration of hydrocarbon gas measured as equivalent to methane in said third gas stream of reducing gas effluent from said heating device is in the range between 15% and 25% by volume.

7 . A process according to claim 1 , further characterized by regulating the flow rate of said second make-up stream of hydrocarbon gas for producing DRI having a carbon content in the range of about 1 to about 4 weight percent.

8 . A process according to claim 6 , further characterized by regulating the flow rate of said second make-up stream of hydrocarbon gas for producing DRI having a carbon content in the range of about 2 to about 3 weight percent.

9 . A process according to claim 1 , further characterized by providing said second top gas recycle circuit as an addition to an existing direct reduction plant which initially has only said first top gas recycle circuit thereby increasing the DRI production capacity of the existing reduction plant without increasing the capacity of the existing reformer and providing the ability to better control and to broaden the range of the carbon content in the DRI.

10 . A method according to claim 1 , wherein said carbon dioxide removal unit is a chemical absorption unit.

11 . A method according to claim 1 , wherein said carbon dioxide removal unit is a PSA or VPSA unit.

12 . A method according to claim 1 , further comprising humidifying said CO 2 -lean recycle gas whereby gaseous hydrocarbons present in said reducing gas fed to the reduction zone are largely reformed within the reduction zone taking advantage of the catalytic action of the metallic iron within said reduction reactor.

13 . A method according to claim 1 , further comprising injecting oxygen or an oxygen enriched gas into said reducing gas prior to its introduction into the reduction zone to aid in increasing the reducing gas temperature with minimal lessening of its reducing potential.

14 . A method according to claim 1 , wherein said reducing gas is heated to a temperature in the range of about 750° C. to about 1120° C.

15 . A method according to claim 8 , wherein said reducing gas is heated by said heating device to above about 900° C. and is further heated by said oxygen or oxygen enriched gas injection to a range of about 100° C. to about 1100° C.

16 . A method according to claim 1 , wherein said heating device is a fired tubular heater.

17 . A method according to claim 1 , wherein said heating device is a set of heating tubes located in the convection zone of said reformer.

Assignees

• Hyl Technologies Sa De Cv
• Danieli & Co Ohg S P A
• Danieli Off Mecc

Inventors

• Becerra-Novoa Jorge Octavio
• Martinis Alessandro

Classifications

• C21B2100/22

  by reforming · CPC title

• C21B13/004

  in a continuous way by reduction from ores · CPC title

• C21B13/02 Primary

  in shaft furnaces · CPC title

• C21B2100/282

  of carbon dioxide · CPC title

• Y02P10/122

  by capturing or storing CO2 · CPC title