Chemical looping combustion

Chemical looping combustion (CLC) typically employs a dual fluidized bed system (circulating fluidized bed process) where a metal oxide is employed as a bed material providing the oxygen for combustion in the fuel reactor. The reduced metal is then transferred to the second bed (air reactor) and re-oxidized before being reintroduced back to the fuel reactor completing the loop.

Isolation of the fuel from air simplifies the number of chemical reactions in combustion. Employing oxygen without nitrogen and the trace gases found in air eliminates the primary source for the formation of nitrogen oxide (NO
x), producing a flue gas composed primarily of carbon dioxide and water vapor; other trace pollutants depend on the fuel selected.

Description

Chemical looping combustion (CLC) uses two or more reactions to perform the oxidation of hydrocarbon based fuels. In its simplest form, an oxygen carrying species (normally a metal) is first oxidised in air forming an oxide. This oxide is then reduced using a hydrocarbon as reducer in a second reaction. As an example, a nickel based system burning pure carbon would involve the two redox reactions:

2Ni(s) + O(g)
2 → 2NiO(s)

 

 

 

 

(1)

C(s) + 2NiO(s) → CO(g)
2 + 2Ni(s)

 

 

 

 

(2)

If (1) and (2) are added together, the reaction set reduces to straight carbon oxidation – the nickel acting as a catalyst only i.e.:

C(s) + O(g)
2 → CO(g)
2

 

 

 

 

(3)

Fig 1: Sankey diagram of energy fluxes in a reversible CLC system.

CLC was first studied as way to produce CO
2 from fossil fuels, using two interconnected fluidized beds.[1] Later it was proposed as a system for increasing power station efficiency.[2] The gain in efficiency is possible due to the enhanced reversibility of the two redox reactions; in traditional single stage combustion, the release of a fuel’s energy occurs in a highly irreversible manner - departing considerably from equilibrium. In CLC, if an appropriate oxygen carrier is chosen, both redox reactions can be made to occur almost reversibly and at relatively low temperatures. Theoretically, this allows a power station using CLC to approach the ideal work output for an internal combustion engine without exposing components to excessive working temperatures.

Fig 1 illustrates the energy exchanges in a CLC system graphically, and shows a Sankey diagram of the energy fluxes occurring in a reversible CLC based engine. Studying Fig 1, a heat engine is arranged to receive heat at high temperature from the exothermic oxidation reaction. After converting part of this energy to work, the heat engine rejects the remaining energy as heat. Almost all of this heat rejection can be absorbed by the endothermic reduction reaction occurring in the reducer. This arrangement requires the redox reactions to be exothermic and endothermic respectively, but this is normally the case for most metals.[3] Some additional heat exchange with the environment is required to satisfy the second law; theoretically, for a reversible process, the heat exchange is related to the standard state entropy change, ΔSo, of the primary hydrocarbon oxidation reaction as follows:

Qo = ToΔSo

However, for most hydrocarbons ΔSo, is a small value and, as a result, an engine of high overall efficiency is theoretically possible.[4]

Although proposed as a means of increasing efficiency, in recent years, interest has been shown in CLC as a carbon capture technique. Carbon capture is facilitated by CLC because the two redox reactions generate two intrinsically separated flue gas streams: a stream from the oxidiser, consisting of atmospheric N
2 and residual O
2, but sensibly free of CO
2; and a stream from the reducer containing CO
2 and H
2O with very little diluent nitrogen. The oxidiser exit gas can be discharged to the atmosphere causing minimal CO
2 pollution. The reducer exit gas contains almost all of the CO
2 generated by the system and CLC therefore can be said to exhibit 'inherent carbon capture', as water vapour can easily be removed from the second flue gas via condensation, leading to a stream of almost pure CO
2. This gives CLC clear benefits when compared with competing carbon capture technologies, as the latter generally involve a significant energy penalty associated with either post combustion scrubbing systems or the work input required for air separation plants. This has led to CLC being proposed as an energy efficient carbon capture technology.[5][6]

Actual operation of chemical-looping combustion with gaseous fuels was demonstrated in 2003,[7] and later with solid fuels in 2006.[8] Total operational experience in pilots of 0.3 to 120 kW is more than 4000 h.[9] Oxygen carrier materials used in operation include oxides of nickel, copper, manganese and iron.

A closely related process is Chemical-Looping Combustion with Oxygen Uncoupling (CLOU) where an oxygen carrier is used that releases gas-phase oxygen in the fuel reactor, e.g. CuO/Cu
2O.[10] This is helpful for achieving high gas conversion, and especially when using solid fuels, where slow steam gasification of char can be avoided. CLOU operation with solid fuels shows high performance[11][12]

Chemical Looping can also be used to produce hydrogen in Chemical-Looping Reforming (CLR) processes.[13][14]

Comprehensive overviews of the field are given in recent reviews on chemical looping technologies[15][16][17]

In summary CLC can achieve both an increase in power station efficiency simultaneously with low energy penalty carbon capture. Challenges with CLC include operation of dual fluidized bed (maintaining carrier fluidization while avoiding crushing and attrition), and maintaining carrier stability over many cycles.

See also

References

  1. ↑ Lewis, W., Gilliland, E. and Sweeney, M. (1951). "Gasification of carbon". Chemical Engineering Progress 47: 251–256.
  2. ↑ Richter, H.J. and Knoche, K.F. (1983). "Reversibility of combustion processes, in Efficiency and Costing – Second law analysis of processes.". ACS symposium series (235): 71–85.
  3. ↑ Jerndal, E., Mattisson, T. and Lyngfelt, A. (2006). "Thermal analysis of chemical-looping combustion". Trans IChemE, Part a Chem. Eng. Res. And Des. 84: 795–806. doi:10.1205/cherd05020.
  4. ↑ McGlashan, N.R. (2008). "Chemical looping combustion – a thermodynamic study". Proc. IMechE, Part C: J. Mech. Eng. Sci. 222: 1005–1019. doi:10.1243/09544062JMES790.
  5. ↑ Ishida, M., and Jin, N. (1997). "CO
    2     Recovery in a power plant with chemical looping combustion". Energy Conv. Mgmt. 38: S187–S192. doi:10.1016/S0196-8904(96)00267-1.
  6. ↑ Brandvoll, Ø. and Bolland, O. (2004). "Inherent CO
    2     capture using chemical looping combustion in a natural gas fired cycle". Trans. ASME 126: 316–321. doi:10.1115/1.1615251.
  7. ↑ Lyngfelt, A. (2004). "A New Combustion Technology". Greenhouse Gas Issues. No.73: 2–3.
  8. ↑ Lyngfelt, A. (2007). "Chemical-looping combustion of solid fuels". Greenhouse Gas Issues. No. 85: 9–10.
  9. ↑ Lyngfelt, A. (2011). "Oxygen carriers for chemical-looping combustion - 4000 h of operational experience". Oil & Gas Science and Technology 66:2: 161–172.
  10. ↑ Mattisson, T., Lyngfelt, A. and Leion, H. (2009). "Chemical-Looping with Oxygen Uncoupling for Combustion of Solid Fuels". International Journal of Greenhouse Gas Control 3: 11–19. doi:10.1016/j.ijggc.2008.06.002.
  11. ↑ Abad, A., Adánez-Rubio, I. Gayán, P. García-Labiano, F. de Diego L. F. and Adánez, J. (2012). "Demonstration of chemical-looping with oxygen uncoupling (CLOU) process in a 1.5kW th continuously operating unit using a Cu-based oxygen-carrier". International Journal of Greenhouse Gas Control 6: 189–200. doi:10.1016/j.ijggc.2011.10.016.
  12. ↑ Zhou, Zhiquan; Han, Lu; Nordness, Oscar; Bollas, George M. (2015-05-01). "Continuous regime of chemical-looping combustion (CLC) and chemical-looping with oxygen uncoupling (CLOU) reactivity of CuO oxygen carriers". Applied Catalysis B: Environmental. 166–167: 132–144. doi:10.1016/j.apcatb.2014.10.067.
  13. ↑ Rydén, M. and Lyngfelt, A., (2006). "Using steam reforming to produce hydrogen with carbon dioxide capture by chemical-looping combustion". Journal of Hydrogen Energy 31: 1631–1641.
  14. ↑ Rydén, M., Lyngfelt, A., and Mattisson, T. (2006). "Synthesis gas generation by chemical-looping reforming in a continuously operating laboratory reactor". Fuel 85: 1631–1641. doi:10.1016/j.fuel.2006.02.004.
  15. ↑ Fan, L.-S. (2010) Chemical Looping Systems for Fossil Energy Conversions, John Wiley & Sons
  16. ↑ Lyngfelt, A. and Mattisson, T. (2011) ”Materials for chemical-looping combustion”, in D. Stolten and V. Scherer, Efficient Carbon Capture for Coal Power Plants, Weinheim, WILEY-VCH Verlag GmbH & Co.. KGaA, 475-504.
  17. ↑ Adánez, J., Abad, A. Garcia-Labiano, F. Gayan P. and de Diego, L. (2012). "Progress in Chemical-Looping Combustion and Reforming technologies'". Progress in Energy and Combustion Science 38: 215–282. doi:10.1016/j.pecs.2011.09.001.

External links

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