Chemical looping reforming (CLR) and gasification (CLG) are the operations that involve the use of gaseous carbonaceous feedstock and solid carbonaceous feedstock, respectively, in their conversion to syngas in the chemical looping scheme. The typical gaseous carbonaceous feedstocks used are natural gas and reducing tail gas, while the typical solid carbonaceous feedstocks used are coal and biomass. The feedstocks are partially oxidized to generate syngas using metal oxide oxygen carriers as the oxidant. The reduced metal oxide is then oxidized in the regeneration step using air. The syngas is an important intermediate for generation of such diverse products as electricity, chemicals, hydrogen, and liquid fuels. 
The motivation for developing the CLR and CLG processes lies in their advantages of being able to avoid the use of pure oxygen in the reaction, thereby circumventing the energy intensive air separation requirement in the conventional reforming and gasification processes. The energy conversion efficiency of the processes can, thus, be significantly increased. Steam and carbon dioxide can also be used as the oxidants. As the metal oxide also serves as the heat transfer medium in the chemical looping process, the exergy efficiency of the reforming and gasification processes like that for the combustion process is also higher as compared to the conventional processes.
Description.
The CLR and CLG processes use solid metal oxides as the oxygen carrier instead of pure oxygen as the oxidant. In one reactor, termed the reducer or fuel reactor, the carbonaceous feedstock is partially oxidized to syngas, while the metal oxide is reduced to a lower oxidation state as given by:
CH"a"O"b" + MeO"x" → CO + H2 + MeO"x"-"δ"
where Me is a metal. It is noted that the reaction in the reducer of the CLR and CLG processes differs from that in the chemical looping combustion (CLC) process in that, the feedstock in CLC process is fully oxidized to CO2 and H2O. In another reactor, termed the oxidizer, combustor or air reactor (when air is used as the regeneration agent), the reduced metal oxide from the reducer is re-oxidized by air or steam as given by:
 ;templatestyles src="Fraction/styles.css" / ;2⁄"δ" MeO"x"-"δ" + O2 (air) → ;templatestyles src="Fraction/styles.css" / ;2⁄"δ" MeOx + (O2 depleted air)
 ;templatestyles src="Fraction/styles.css" / ;1⁄"δ" MeO"x"-"δ" + H2O → ;templatestyles src="Fraction/styles.css" / ;1⁄"δ" MeOx + H2
The solid metal oxide oxygen carrier is then circulated between these two reactors. That is the reducer and the oxidizer/combustor are connected in a solids circulatory loop, while the gaseous reactants and products from each of the two reactors are isolated by the gas seals between the reactors. This streamlining configuration of the chemical looping system possesses a process intensification property with a smaller process footprint as compared to that for the traditional systems.
Oxygen carriers.
The Ellingham diagram that provides the Gibbs free energy formation of a variety of metal oxides is widely used in metallurgical processing for determining the relative reduction-oxidation potentials of metal oxides at different temperatures. It depicts the thermodynamic property of a variety of metal oxides to be used as potential oxygen carrier materials. It can be modified to provide the Gibbs free energy changes for metals and metal oxides under various oxidation states so that it can be directly used for the selection of metal oxide oxygen carrier materials based on their oxidation capabilities for specific chemical looping applications. The modified Ellingham diagram is given in Fig 1a. As shown in Fig 1b, the diagram can be divided into four different sections based on the following four key reactions:
Reaction line 1: 2CO + O2 → 2CO2
Reaction line 2: 2H2 + O2 → 2H2O
Reaction line 3: 2C + O2 → 2CO
Reaction line 4: 2CH4 + O2 → 2CO + 4H2
The sections identified in Fig 1b provide the information on metal oxide materials that can be selected as potential oxygen carriers for desired chemical looping applications. Specifically, highly oxidative metal oxides, such as NiO, CoO, CuO, Fe2O3 and Fe3O4 belong to the combustion section (Section A) and they all lie above the reaction lines 1 and 2. These metal oxides have a high oxidizing tendency and can be used as oxygen carriers for the chemical looping combustion, gasification or partial oxidation processes. The metal oxides in Section E, the small section between the reaction lines 1 and 2, can be used for CLR and CLG, although a significant amount of H2O may present in the syngas product. The section for syngas production lies between reaction lines 2 and 3 (Section B). Metal oxides lying in this region, such as CeO2, have moderate oxidation tendencies and are suitable for CLR and CLG but not for the complete oxidation reactions. Metal oxides below reaction line 3 (Sections C and D) are not thermodynamically favored for oxidizing the fuels to syngas. Thus, they cannot be used as oxygen carriers and are generally considered to be inert. These materials include Cr2O3 and SiO2. They can, however, be used as support materials along with active oxygen carrier materials. In addition to the relative redox potentials of metal oxide materials illustrated in Fig 1b, the development of desired oxygen carriers for chemical looping applications requires to consider such properties as oxygen carrying capacity, redox reactivity, reaction kinetics, recyclability, attrition resistance, heat carrying capacity, melting point, and production cost.
Process configurations.
The CLR and CLG processes can be configured based on the types of carbonaceous feedstocks given and desired products to be produced. Among a broad range of products, the CLG process can produce electricity through chemical looping IGCC. The syngas produced from the CLR and the CLG can be used to synthesize a variety of chemicals, liquid fuels and hydrogen. Given below are some specific examples of the CLR and CLG processes.
Steam methane reforming with chemical looping combustion (CLC-SMR).
Hydrogen and syngas are currently produced largely by steam methane reforming (SMR). The main reaction in SMR is:
CH4 + H2O → CO + 3H2
Steam can be further used to convert CO to H2 via the water-gas shift reaction (WGS): 
H2O + CO → CO2 + H2
The SMR reaction is endothermic, which requires heat input. The state-of-art SMR system places the tubular catalytic reactors in a furnace, in which fuel gas is burned to provide the required heat.
In the SMR with chemical looping combustion (CLC-SMR) concepts shown in Fig 2, the syngas production is carried out by the SMR in a tubular catalytic reactor while the chemical looping combustion system is used to provide the heat for the catalytic reaction. Depending on which chemical looping reactor is used to provide the SMR reaction heat, two CLC-SMR schemes can be configured. In Scheme 1 (Fig 2a), the reaction heat is provided by the reducer (fuel reactor). In Scheme 2 (Fig 2b), the reaction heat is provided by the combustor (air reactor). In either scheme, the combustion of metal oxide by air in the chemical looping system provides the heat source that sustains the endothermic SMR reactions. In the chemical looping system, natural gas and the recycled off-gas from the pressure swing adsorption (PSA) of the SMR process system are used as the feedstock for the CLC fuel reactor operation with CO2 and the steam as the reaction products. The CLC-SMR concepts have mainly been studied from the perspective of the process simulation. It is seen that both schemes do not engage directly the chemical looping system as a means for syngas production.
Chemical looping reforming (CLR).
Chemical looping systems can directly be engaged as an effective means for syngas production. Compared to the conventional partial oxidation (POX) or autothermal reforming (ATR) processes, the key advantage of the chemical looping reforming (CLR) process is the elimination of the air separation unit (ASU) for oxygen production. The gaseous fuel, typically natural gas, is fed to the fuel reactor, in which a solid metal oxide oxygen carrier partially oxidizes the fuel to generate syngas: 
CH4 + ;templatestyles src="Fraction/styles.css" / ;1⁄"δ" MeOx → CO + 2H2 + ;templatestyles src="Fraction/styles.css" / ;1⁄"δ" MeO"x"-"δ"
Steam can be added to the reaction in order to increase the generation of H2, via the water-gas shift reaction (WGS) and/or steam methane reforming.
The CLR process can produce a syngas with a H2:CO molar ratio of 2:1 or higher, which is suitable for Fischer–Tropsch synthesis, methanol synthesis, or hydrogen production. The reduced oxygen carrier from the reducer is oxidized by air in the combustor: 
 ;templatestyles src="Fraction/styles.css" / ;2⁄"δ" MeO"x-δ" + O2 (air) → ;templatestyles src="Fraction/styles.css" / ;2⁄"δ" MeO"x"
The overall reaction in the CLR system is a combination of the partial oxidation reaction of the fuel and the WGS reaction:
CH4 + O2 + "a" H2O → CO + (2+"a") H2
It is noted that the actual reaction products for such reactions as those given above can vary depending on the actual operating conditions. For example, the CLR reactions can also produce CO2 when highly oxidative oxygen carriers such as NiO and Fe2O3 are used. The carbon deposition occurs particularly when the oxygen carrier is highly reduced. Reduced oxygen carrier species, such as Ni and Fe, catalyze the hydrocarbon pyrolysis reactions.
Fig 3 shows a CLR system that has been studied experimentally by Vienna University of Technology. The system consists of a fluidized bed reducer and a fluidized bed combustor, connected by loop seals and cyclones. Commonly used oxygen carriers are based on NiO or Fe2O3. The NiO-based oxygen carriers exhibit excellent reactivity, as shown by the high conversion of natural gas. The Fe2O3-based oxygen carriers have a lower material cost while their reactivity is lower than that of the NiO-based ones. Operating variables such as temperature, pressure, type of metal oxide, and molar ratio of metal oxide to gaseous fuel will influence the fuel conversion and product compositions. However, with the effects of the back mixing and distributed residence time for the metal oxide particles in the fluidized bed, the oxidation state of the metal oxide particles in the fluidized bed varies that prevents a high purity of the syngas to be produced from the reactor. 
The moving bed reactor that does not have the effects of back mixing of the metal oxide particles is another gas-solid contact configuration for CLR/CLG operation. This reactor system developed by Ohio State University is characterized by a co-current gas-solid moving bed reducer as given in Fig 4. The moving bed reducer can maintain the uniform oxidation state of the exit metal oxide particles from the reactor. thereby synchronizing the process operation to achieve the thermodynamic equilibrium conditions. The CLR moving bed process applied to the methane to syngas (MTS) reactions has the flexibility of co-feeding CO2 as a feedstock with such gaseous fuels as natural gas, shale gas, and reducing tail gases, yielding a CO2 negative process system. The CLR-MTS system can yield a higher energy efficiency and cost benefits over the conventional syngas technologies. In a benchmark study for production of 50,000 barrels per day of liquid fuels using the natural gas as the feedstock, the CLR - MTS system for syngas production can reduce the natural gas usage by 20% over the conventional systems involving the Fischer–Tropsch technology.
Chemical looping gasification (CLG).
Chemical looping gasification (CLG) differs from the CLR in that it uses solid fuels such as coal and biomass instead of gaseous fuels as feedstocks. The operating principles for the CLG is similar to CLR. For solid feedstocks, devolatilization and pyrolysis of the solid fuel occur when the solid fuels are introduced into the reducer and mixed with the oxygen carrier particles. With the fluidized bed reducer, the released volatiles, including light organic compounds and tars, may channel through the reducer and exit with the syngas. The light organic compounds may reduce the purity of the syngas, while the tars may accumulate in downstream pipelines and instruments. For example, the carbon efficiency using the coal CLG fluidized bed reducer may vary from 55% to 81%, whereas the carbon efficiency using the coal moving bed reducer can reach 85% to 98%. The syngas derived from the biomass CLG fluidized bed reducer may consist of up to 15% methane, while the syngas derived from the biomass CLG moving bed reducer can reach a methane concentration of less than 5%. In general, increasing the temperature of the CLG system can promote volatile and char conversion. This may also promote the full oxidation side reaction resulting in an increased CO2 concentration in the syngas. Additional equipment for gas