# US 11,111,143 B2 · Chemical looping syngas production from carbonaceous fuels

> Agents: this data is available as JSON from the patentgrep API and MCP server — see https://patentgrep.com/llms.txt

- Number: US 11,111,143 B2
- Document ID: US11111143B2
- Status: Granted
- Kind: B2
- Application number: 16/091,253
- Filed: 2017-04-12
- Published: 2019-05-23
- Granted: 2021-09-07
- Earliest claimed: 2016-04-12
- Assignees: Ohio State Innovation Foundation
- Applicants: Ohio State Innovation Foundation
- Inventors: Liang-shih Fan; Abbey Empfield; Mandar Kathe; Charles Fryer; Elena Blair
- Web page: https://patentgrep.com/patent/US11111143B2

## CPC

- C01B 3/42: using moving solid particles, e.g. fluidised bed technique
- B01J 8/12: moved by gravity in a downward flow
- B01J 8/32: with introduction into the fluidised bed of more than one kind of moving particles
- B01J 8/388: {externally, i.e. the particles leaving the vessel and subsequently re-entering it}
- B01J 19/1837: {Loop-type reactors}
- C01B 3/344: {using non-catalytic solid particles}
- C01B 3/56: by contacting with solids; Regeneration of used solids
- C10J 3/26: downwardly
- C10J 3/57: Gasification using molten salts or metals (C10J3/02, C10J3/46 take precedence)
- C10J 3/721: {Multistage gasification, e.g. plural parallel or serial gasification stages}
- C10J 3/725: {Redox processes}
- B01J 2208/0038: Solids
- C01B 2203/0216: containing a non-catalytic steam reforming step
- C01B 2203/0222: containing a non-catalytic carbon dioxide reforming step
- C01B 2203/0255: containing a non-catalytic partial oxidation step
- C01B 2203/0475: the impurity being carbon dioxide
- C01B 2203/1241: Natural gas or methane
- C01B 2203/141: At least two reforming, decomposition or partial oxidation steps in parallel
- C01B 2203/148: involving a recycle stream to the feed of the process for making hydrogen or synthesis gas
- C01B 2203/1614: Controlling the temperature
- C01B 2203/1628: Controlling the pressure
- C10J 2300/1612: CO2-separation and sequestration, i.e. long time storage
- C10J 2300/1815: for carbon dioxide
- C10J 2300/1823: for synthesis gas
- Y02P 30/00: Technologies relating to oil refining and petrochemical industry
- C01B: NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; {METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C}
- B01J: CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- C10J: PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES (synthesis gas from liquid or gaseous hydrocarbons C01B; underground gasification of minerals E21B43/295); CARBURETTING AIR OR OTHER GASES
- Y02P: CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS

## Abstract

A reactor configuration is proposed for selectively converting gaseous, liquid or solid fuels to a syngas specification which is flexible in terms of H2/CO ratio. This reactor and system configuration can be used with a specific oxygen carrier to hydro-carbon fuel molar ratio, a specific range of operating temperatures and pressures, and a co-current downward moving bed system. The concept of a CO2 stream injected in-conjunction with the specified operating parameters for a moving bed reducer is claimed, wherein the injection location in the reactor system is flexible for both steam and CO2 such that, carbon efficiency of the system is maximized.

## Claims

### Claim 1

A system for converting a fuel, the system comprising:
a first moving bed reactor comprising a metal oxide particles having a primary component and a secondary component, wherein fuel, CO2 and steam are added to the first moving bed reactor in a co-current flow pattern relative to the metal oxide particles, wherein the first moving bed reactor is configured to reduce at least a portion of the metal oxide particles with the fuel to produce a first reduced metal oxide, and is further configured to produce a first syngas stream comprising H2, CO, CO2 and steam;
a second moving bed reactor, operating in parallel with the first moving bed reactor and comprising metal oxide particles having a primary component and a secondary component, wherein fuel, CO2 and steam are added to the second moving bed reactor in a co-current flow pattern relative to the metal oxide particles, wherein the second moving bed reactor is configured to reduce at least a portion of the metal oxide particles with the fuel to produce a second reduced metal oxide, and is further configured to produce a second syngas stream comprising H2, CO, CO2 and steam;
a separation unit, in communication with the first moving bed reactor and the second moving bed reactor, and configured to remove the CO2 from the first syngas stream and the second syngas stream, wherein the H2/CO ratios of the first and second syngas streams are controlled by recycling substantially all of the CO2 from the separation unit to the first moving bed reactor and the second moving bed reactor; and
a third co-current fluidized bed reactor in communication with the first moving bed reactor and the second moving bed reactor and configured to oxidize the first reduced metal oxide and the second reduced metal oxide with an oxidizing agent to produce oxidized metal oxide particles and recycle the oxidized metal oxide particles to the first moving bed reactor and the second moving bed reactor for subsequent reduction reactions.

### Claim 2 (depends on 1)

The system of claim 1, wherein the primary component is Fe2O3.

### Claim 3 (depends on 1)

The system of claim 1, wherein the secondary component comprises a metal-oxide selected from the group consisting of oxides of Ti, Al, Co, Cu, Mg, Mn, Zn, and combinations thereof.

### Claim 4 (depends on 1)

The system of claim 1, wherein the secondary component is titanium oxide.

### Claim 5 (depends on 1)

The system of claim 1, wherein the fuel is methane.

### Claim 6 (depends on 1)

The system of claim 1, wherein the H2/CO ratio of the first syngas stream is about 2.9 to about 3.1.

### Claim 7 (depends on 1)

The system of claim 1, wherein the H2/CO ratio of the second syngas stream is about 1.0 to about 1.5.

### Claim 8 (depends on 1)

The system of claim 1, wherein a combination of the syngas from the first moving bed reactor and the second moving bed reactor results in a total syngas H2/CO ratio of about 1 to about 3.

### Claim 9 (depends on 1)

The system of claim 1, wherein the first reduced metal oxides and the second reduced metal oxides are oxidized by introducing steam into the third co-current fluidized bed reactor.

### Claim 10 (depends on 1)

The system of claim 1, wherein the system consumes more CO2 than it produces.