SciELO - Scientific Electronic Library Online

 
vol.35 issue2HYDROTALCITE-IMPREGNATED COPPER AND CHROMIUM-DOPED COPPER AS NOVEL AND EFFICIENT CATALYSTS FOR VAPOR-PHASE HYDROGENATION OF FURFURAL: EFFECT OF CLAY PRETREATMENTDEVELOPMENT OF ANTIOXIDANT POLY(THIOETHER-ESTER) NANOPARTICLES author indexsubject indexarticles search
Home Pagealphabetic serial listing  

Services on Demand

Journal

Article

Indicators

Related links

Share


Brazilian Journal of Chemical Engineering

Print version ISSN 0104-6632On-line version ISSN 1678-4383

Braz. J. Chem. Eng. vol.35 no.2 São Paulo Apr./June 2018

http://dx.doi.org/10.1590/0104-6632.20180352s20160495 

Kinetics and Catalysis, Reaction Engineering, and Materials Science

THEORETICAL MODELS FOR RATES OF HETEROGENEOUS REACTIONS DURING COMBUSTION AND GASIFICATION OF LIQUID FUELS IN FLUIDIZED BEDS

Marcio L. de Souza-Santos1  * 

1University of Campinas (UNICAMP), Faculty of Mechanical Engineering, Department of Energy, Cidade Universitária, C. Postal 6122, Campinas, São Paulo 13083-970, Brazil. Email: dss@csfmb.com


Abstract

Two mathematical models to allow computations of chemical species production or consumption rates by heterogeneous reactions taking place during combustion and gasification of liquid fuels sprayed on or injected into fluidized beds of solid particles are proposed. The possibilities envisaged here are called: the CIP (Coated Inert Particles) and the CSP (Coke Shell Particle) models. The former assumes that the injected liquid fuel immediately coats the fluidized inert particles in the bed and then goes through pyrolysis, combustion and gasification reactions. The latter presumes that the liquid fuel drops go through fast pyrolysis before meeting any inert particles and the remaining coke hollow particles react with gases in the bed. Analytical solutions for various geometries of the inert particles in the bed are presented. The work does not include the governing equations which constitute the whole mathematical model of fluidized-bed reactors. Such can be found elsewhere. The present work concentrates only on the theoretical aspects. Experimental tests would allow verification if they properly represent the processes of liquid consumption during combustion and gasification processes consuming liquid fuels in fluidized beds and which model would better fit each individual situation.

Key words: Liquid Fuels; Combustion; Gasification; Mathematical Models; Fluidized-Bed

INTRODUCTION

Fluidized-Bed technology has been successfully applied for cases of solid fuels as energy sources. The various advantages of fluidized beds, either bubbling, circulating, or entrained over more conventional combustion and gasification techniques are listed elsewhere (Basu, 2016; Kunii and Levenspiel, 1991; Kunii and Levenspiel, 1997; Geldart, 1986; de Souza-Santos, 1987; de Souza-Santos, 2010). Fluidized beds have been particularly useful when dealing with high-moisture biomasses, municipal solid residues, high-ash coals and other low heating-value fuels (de Souza-Santos, 2010;, Muskala et al., 2011).

During the years, many models have been developed to allow predictions of the behavior of existing units as well and optimizations of future ones. The list of those is too extensive, but many are described or listed in reviews (Gomez-Barea and Leckner, 2010; Philippsen et al., 2015; Alagoz, 2006; Saraiva et al., 1993). Nonetheless, no model has been found in the literature including the alternative of liquid fuel feeding into fluidized beds.

The present development

An existing simulation program (www.csfmb.com) has been validated (de Souza-Santos, 1987, 1989, 1994a, 1994b, 2007, 2008, 2009, 2010; Rabi and de Souza-Santos, 2003, 2004, 2008; Krzywanski et al., 2016; Englebrecht et al., 2011) and used in studies involving various possibilities and consuming many fuels, including low-quality ones (Muskala et al., 2011; de Souza-Santos, 1989, 1994a, 1994b, 2007, 2008, 2009, 2010, 2015; Rabi and de Souza-Santos, 2003, 2004, 2008; Krzywanski et al., 2016; Englebrecht et al., 2011; de Souza-Santos and Chaves, 2012a, 2012b, 2012c; de Souza-Santos and Ceribeli, 2012, 2013; de Souza-Santos and Beninca, 2014; de Souza-Santos and Lima, 2015; de Souza-Santos et al., 2015).

In many situations, fluidized beds require inert solids, such as sand or alumina, as temperature regulator and to allow more stable fluidization (Basu, 2016; Kunii and Levenspiel, 1991; Kunii and Levenspiel, 1997; Geldart, 1986; de Souza-Santos, 1987; de Souza-Santos, 2010). Ash particles, detached from the feeding solid fuel, can replace part or even the total amount of that inert material.

In addition to solid fuels, liquids or slurries are also an important segment of the spectrum found in industry. Among them there are heavy or viscous oils, whose combustion in pulverized form is cumbersome. Furthermore, several works have explored the application of residual hydrocarbon to enrich low heating value solid fuels to allow their ignition, as well as improve the combustion or gasification processes (Breault, 2010). Amid those, glycerol has shown particular interest since it is a byproduct of biodiesel production, which has increased substantially in many countries (Leonetia et al., 2012; Wei et al., 2011; Sricharoewnchaikul and Atong, 2012; Manara and Zabanioutou, 2016; Czernichowski, 2009; Fosso-Kankeu et al., 2015; Maintinguer et al., 2015; Pagliaro and Rossi, 2010). For instance, just the Brazilian output should reach 4.1 million m3 in 2016 (Barros, 2015). Since glycerol represents around 11% of biodiesel production, its rate of generation would also increase fast in the coming years (Dasari et al., 2005; Schultz et al., 2014).

An alternative for the utilization of those liquid fuels is their injection into fluidized bed boilers or gasifiers.

BASIC MODELS

The following possibilities can be visualized:

  1. As the liquid fuel enters the fluidized bed, it immediately coats the inert solid particles. Then, the fuel goes through pyrolysis or devolatilization and the resulting coke layers remain on the inert particles. Then, those layers are attacked by gases. This model is called here CIP (Coated Inert Particle) and the situation is illustrated by Figure 1. The Appendix describes how it can be applied for each situation where the supporting solid has a particular basic shape, i.e., planar or flat, cylindrical, or spherical.

    Figure 1 Scheme for the CIP model 

  2. As the liquid fuel is sprayed into the bed, the drops go through pyrolysis before having the opportunity of meeting any inert particle. A hollow coke shell forms from each fuel drop after the volatiles escape from its interior through small holes in the respective shell. Then, the remaining shell of that hollow sphere of coke reacts with the gases. The average size among the spheres is assumed to be the same as the average drop size in the original sprayed fuel. This model is called here CSP (Coke Shell Particle) and the situation is illustrated by Figure 2.

    Figure 2 Scheme for the CSP model. 

Before describing the mathematical models, it is important to stress that the present work assumes isothermal conditions in the layer of fuel and inert particles. The local temperature of particles, as well as temperature, pressure, and composition of the surrounding gas, should be given by a comprehensive model for fluidized-bed equipment. The governing equations that constitute the mathematical model of fluidized-bed reactors can be found elsewhere (de Souza-Santos, 2010). The only objective here is to present the equations proposed for the reaction rates between gases and the liquid fuel injected into the reactor with fluidized inert solid particles.

The treatment for a single heterogeneous reaction i, in which a chemical component j of the surrounding gas is consumed or produced, has been presented by de Souza-Santos (2010). In any case, the fundamental equation for conservation of species leads to

2y=Φ2yn (1)

The Laplacian operator is generalized as:

2=xpddxxpddx (2)

the coefficient p takes the following possible values: 0 for plane geometry, 1 for cylindrical, and 2 for spherical. Here:

x=rrA (3)

y=ρ˜jρ˜j,eqρ˜j,ρ˜j,eq (4)

The Thiele coefficient is given by:

Φ=rAkiρ˜j,ρ˜j,eqn1Dj,N1/2 (5)

On the above, it has been assumed that all reaction rates could be written as:

r˜i=kiρ˜jρ˜j,eqn (6)

which is valid for most of the combustion and gasification reactions. For those, the reaction order n varies between 0 and 2. However, the main cases of carbon-oxygen and carbon-water reactions-which control most of the combustion and gasification processes-follow a first order behavior. A list of several reactions found in those processes as well their kinetic coefficients are presented elsewhere (de Souza-Santos, 2010).

The basic equations to allow computation of the CIP and CSP models are present below.

Coated Inert Particle (CIP) Model

Figure 1 illustrates the CIP model. The inert particle, coated by a coke layer, may present three basic shapes: plane (in the case of chips), cylindrical (in the case of pellets or fibers), and spherical or almost spherical. As detailed in the Appendix, the solutions can be condensed into a single formula for the rate of consumption or production of component j by reaction i as

rj=1rAρ˜j,ρ˜j,eqk=13Uk (7)

The sum that appears in the denominator represents the three resistances in series for mass transfers of chemical species j that depend on the inert particle original shape. Table 1 summarizes the various possibilities. The first parameter U1 represents the resistance to the mass transfer at the gas boundary layer, U2 the resistance at the ash layer, and the U3 the combined resistances of reacting gas mass transfer trough the reactive coke layer and its respective chemical reaction with the coke material. The various resistances for the basic geometries are summarized at Table 1. An example of deduction is shown in the Appendix.

Table 1 Formulas to compute the mass transfer resistances in the case of CIP model. 

Shape Resistance
U1 U2 U3 (*)
Plate 1NShDj,G 1aDj,A 1ΦDj,NCaCbSaSbSaCbCaSb
Cylinder 1NShDj,G lnaDj,A 1aΦDj,NI0aΦK1bΦ+I1bΦK0aΦI1aΦK1bΦIbΦK1aΦ
Sphere 1NShDj,G 1aaDj,A 1aDj,NSbbΦCbCaCbbΦSbSaCbbΦSbSaaΦCaSbbΦCbCaaΦSa

*Here: Sa=sinhaΦ,Sb=sinhbΦ,Ca=coshaΦ,Cb=coshbΦ

Coke Shell Particle (CSP) Model

Figure 2 illustrates the situation for the CSP model. Here just the spherical shape is possible.

The first aspect to face is to estimate the radius of the internal space filled with gases.

The original mass of the droplet is given by

mι=4π3rA3ρι (8)

On the other hand, the mass of the coke before the formation of ash over it, is provided by

mc=4π3rA3r03ρc (9)

However,

mc=mι1fVfM=mιf (10)

Therefore,

r0=rA1ριfρc1/3 (11)

The deduction for the resistances are presented in the Appendix. These resistances can be employed in Eq. (7) to compute the rate of consumption or production of gas component j by reaction i.

DISCUSSION

According to Equation 58 of the Appendix, in the case of CSP model, if no mass transfer at the internal cavity surface takes place (i.e., N2 = 0), the parameter w equals the variable a and the resistance forms reproduce the CIP case for spherical geometry.

Another interesting aspect of that case can be appreciated by noticing that the parameter gj (Eq. 45 in the Appendix) is a function of the average concentration inside the cavity. At the beginning of cavity formation, the concentration would be equal to those obtained from the pyrolysis. After a while, the composition tends to equalize the concentration of the equilibrium atmosphere in which the particle is immersed. Therefore, for long exposure times, gj would tend to zero. This situation reproduces the case where N2 = 0.

CONCLUSIONS

The possibility of using the fluidized-bed technique for combustion and gasification of liquid fuels is known. In those cases, the liquid is sprayed over or injected into the bed where inert solid is fluidized.

The adaptation of existing simulation models to such situations required methods to compute the kinetics for heterogeneous reactions. To allow that, two possible approaches are proposed here: the CIP (Coated inert Particle) Model and the CSP (Coke-Shell Particle) Model. The work introduces the analytical solutions for those models, as well as for cases of different basic shapes of inert particles present in the bed.

The present proposals are theoretical. Future publications might confirm the deductions made here and which model would better represent the process in each situation.

APPENDIX

CIP Model for Plane Geometry

Figure 3 illustrates the situation where the slab or chip is assumed to have a thickness much smaller than any other dimension. Therefore, all variations occur in the r direction, which is normal to the surface with largest area.

Figure 3 CIP model for planar geometry. 

Using p = 0 in Equation (1), it is possible to write

d2ydx2=Φ2y (12)

For the ash layer where no reaction takes place, it leads to

dydx=A1,aX1 (13)

and

y=A1x+B1,aX1 (14)

where the parameter a is given by:

a=rNrA (15)

One boundary condition can be set for the external surface, or at x=1, where continuity imposes that the mass transfer by diffusion of the reacting gas j equals the mass transfer by convection, or:

Dj,Gdρ˜jdr=Dj,Adρ˜jdr=βGρ˜j,ρ˜j,surf (16)

or

y1=NSh1y1Dj,GDj,A=N11y1 (17)

where the Sherwood number is:

NSh=βGrADj,G (18)

and:

N1=NShDj,GDj,A (19)

It should be noticed that the coefficient Dj is the diffusivity of component j into the phase in which the process takes place. If that phase is the particle core, or nucleus, the parameter is called the "effective" diffusivity of j in that porous structure, which is represented by Dj,N. A similar notation will be used for the diffusivity of j through the shell of inert porous solid that coats the core, or Dj,A. For the boundary layer of gas, which surrounds the particle, the value is the average diffusivity of j through the gas mixture that constitutes the layer, or Dj,G. As it was shown long ago by Walker et al. (1959), the values for effective diffusivity can be correlated to the gas-gas diffusivity Dj,G.

From (12) and (13) in (17) it is possible to write

B1=11+N1N1A1 (20)

Therefore,

y=A1x1+N1N1+1,aX1 (21)

In the reacting coke layer, Eq. (12) becomes a Bessel equation and its solution can be written as:

y=A2sinhxΦ+B2coshxΦ,bXa (22)

Where:

b=r0rA (23)

A boundary condition can be found at x = b. As the inert material is impermeable to the reacting gas, the mass transfer is zero at that interface, or

dydxx=b=0 (24)

Therefore, Eq. (22) becomes:

y=B2coshxΦtghbΦsinhxΦ,bXa (25)

The other condition comes from continuity of the mass transfer at the coke-ash interface, or:

Dj,Ndydxx=a=Dj,Adydxx=a+ (26)

Equations (13) and (25) lead to:

B2=A1Dj,ADj,NΦsinhaΦtghbΦcoshaΦ1 (27)

Therefore,

y=A1Dj,AΦDj,NcoshxΦtghbΦsinhxΦsinhaΦtghbΦcoshaΦ,bXa (28)

In addition, the concentrations match at that interface or y(a-)=y(a+). Thus, the above equation can be combined with Eq. (21) to give:

A1=1Dj,ADj,Nξ+1+N1N1a (29)

where:

ξ=1ΦcoshaΦtghbΦsinhaΦsinhaΦtghbΦcoshaΦ (30)

The rate of consumption or production of component j is given by the mass transfer of that component at the external layer, or:

rj=Dj,Adρ˜jdrr=rA=Dj,Aρ˜j,ρ˜j,eqrAdydxx=1 (31)

Finally, using Eq. (13), it is possible to obtain the resistances listed for the plane geometry as shown in Table 1.

The deductions for other geometry (p = 1 and p = 2) follow the same path.

The values of the parameters a (Eq. 15) and b (Eq. 23), or dimensionless variables, need to be addressed. It is easy to show that they can be computed by:

a=dP,inert+2fδdP,inert+2δ (32)

and

b=dP,inertdP,inert+2δ (33)

where f represents the fraction of the fixed-carbon, originally in the feeding fuel, which is converted into gases, and d is the film thickness. This thickness can be easily computed by assuming that all particles present in the bed are equally and uniformly coated by the feeding liquid. Given the very high circulation rates of particles in a bubbling or circulating fluidized bed, this should not be very far from reality.

CSP Model

From Equations (1) and (2)

dydx=A1x2 (34)

y=A1x1+B1,aX1 (35)

The boundary condition (17) leads to

B1=11N1N1A1 (36)

where N1 is given by Eq. (19).

For the coke reacting layer, the following can be written

x2y+2xyx2Φ2y=0 (37)

and the solution of that Bessel equation is

y=A2sinhxΦx+B2coshxΦx,bXa (38)

From the continuity for the mass transfer at the coke-ash interface (Eq. 26), it is possible to write:

Dj,NDj,AA1+A2sinhaΦaΦcoshaΦ+B2coshaΦaΦsinhaΦ=0 (39)

The following comes from the continuity or equality of concentration at the two sides of the interface:

A11a+1N1N1+A2sinhaΦa+B2coshaΦa=1 (40)

At the internal surface of the shell (coke-cavity-gas), the following is required:

Dj,Ndρ˜jdrr=r0+=Dj,Gdρ˜jdrr=r0=βcaνρ˜j,r=r0ρ˜j,caν (41)

or:

yb=NSh,caνyb+γDj,GDj,N=N2yb+γ (42)

where:

NSh,caν=βcaνr0Dj,G (43)

and

N2=NSh,caνDj,GDj,N (44)

γj=ρ˜j,caνρ˜j,eqρ˜j,ρ˜j,eq (45)

The combination of above equations leads to:

A2N2b+1b2sinhbΦΑΦcoshbΦb+B2N2b+1b2coshbΦΦsinhbΦb=N2γj (46)

or

A21+N2bSbΦbCb+B21+N2bCbΦbSb=N2γjb2 (47)

The continuity of mass transfer rate at the coke-ash interface leads to:

A2Sa+ΦaCa+B2Ca+ΦaSa=Dj,ADj,NA1 (48)

Equality of concentration at the coke-ash interface, to:

A2Sa+B2Ca=A11+a1N1N1+a (49)

A2, and B2 can be eliminated from the three above equations in order to obtain A1 as:

A1=aC1SaN2γjb2C1C4C2C3+N2γjb2C3C1CaC2Sa/1+a1N1N1C1C1C4C2C3+Dj,ADj,NC1C1CaC2Sa (50)

where:

C1=Sb+N2bSbΦbCb (51)

C2=Cb+N2bCbΦbSb (52)

C3=ΦaCaSa (53)

C4=ΦaSaCa (54)

Finally,

U1=aNShDj,G1ω (55)

U2=1aDj,A1ω (56)

U3=ΞDj,N1ω (57)

Here

ω=aN2b2γjC1SaC3Ξ (58)

with

Ξ=C1CaC2SaC1C4C2C3 (59)

NOMENCLATURE

a, A, b, B, C

parameters (dimensionless)

Ca, Cb

see observation under Table 1 (dimensionless)

dP

particle diameter or thickness in the cases of slabs

Dj

average equivalent or effective diffusivity of chemical species j (the second subscript indicates the medium) (m2 s-1)

f

fractional conversion of fixed-carbon originally in the fuel (dimensionless)

I

Modified Bessel function of the first kind (subscript indicates order)

ki

rate coefficient of reaction i [s-1 (kmol-1 m3)n-1]

K

Modified Bessel function of the second kind (subscript indicates order)

m

mass (kg)

n

reaction order

N

parameter (dimensionless)

NSh

Sherwood number

p

parameter to indicate the geometrical form

r

radial co-ordinate (m). In cases of slabs or chips, it is the distance between the centerline of the slab and the outer surface (with the largest area) of the ash layer (m).

i'''

reaction rate (kmol m-3 s-1)

i''

reaction rate based on the external area of the particle (kmol m-2 s-1)

Sa, Sb

see observation under Table 1 (dimensionless)

U

resistance to mass transfer (s m-2)

x

dimensionless co-ordinate

y

dimensionless concentration of reacting gas

Greek Letters

β

mass transfer coefficient (m s-1)

γ

dimensionless concentration

δ

film thickness (m)

Φ

Thiele modulus or coefficient (dimensionless)

ρ

density (kg m-3)

ρ̃j

molar concentration of the reacting chemical species j (kmol m-3)

ξ

parameter (dimensionless)

ω

parameter (dimensionless)

Ξ

parameter (dimensionless)

Subscripts

A

ash

c

coke

Eq

at equilibrium condition

G

gas phase

i

chemical reaction number

j

chemical component

l

liquid

M

moisture in the original fuel

N

active or reacting coke layer

O

original or internal

V

volatile in the original fuel

at conditions in the surrounding gas and far from the reacting particle

REFERENCES

Alagoz, D. E., Mathematical Modeling of Fluidized Bed Combustors with Radiation Model, M.Sc. Thesis presented to The Graduate School of Natural and Applied Sciences of Middle East Technical University, 2006. [ Links ]

Barros, S., Brazil’s Biofuels Annual Report, Gain Report Number: BR15006, USDA Foreign Agricultural Service, 2015 (on line: http://gain.fas.usda.gov/Recent%20GAIN%20Publications/Biofuels%20Annual_Sao%20Paulo%20ATO_Brazil_8-4-2015.pdf, accessed on September 2016) [ Links ]

Basu, P., Combustion and Gasification in Fluidized Beds. Miami, FL: CRC Press, 2006. ISBN 9780849333965 [ Links ]

Breaut, R. W., Gasification Processes Old and New: A Basic Review of the Major Technologies. Energies, 3(2) 216-240 (2010). DOI: 10.3390/en3020216 [ Links ]

Czernichowski, A., Conversion of waste glycerol into synthesis gas, In 19th Int. Symp. on Plasma Chem.(ISPC-19), Bochum, Germany, July 26 (Vol. 31, p. 4) (2009) ECP - GlidArc Technologies, La Ferté St. Aubin, France, http://www.ispc-conference.org/ispcproc/ispc19/697.pdfLinks ]

Dasari, M. A., Kiatsimkul, P. P., Sutterlin, W. R., and Suppes, G. J., Low-pressure hydrogenolysis of glycerol to propylene glycol, Appl. Catal. A Gen., 281(1-2), 225-231 (2005). [ Links ]

de Souza-Santos, M. L., Modelling and Simulation of Fluidized-Bed Boilers and Gasifiers for Carbonaceous Solids. Ph.D. Dissertation, University of Sheffield, United Kingdom, 1987. etheses.whiterose.ac.uk/1857/1/DX196027.pdf (accessed on 03/03/2014) [ Links ]

de Souza-Santos, M. L., Solid Fuels Combustion and Gasification: Modeling, Simulation, and Equipment Operation. 2nd ed. New York: CRC Press; 2010. (ISBN 9781420047493) [ Links ]

de Souza-Santos, M. L., Comprehensive Modelling and Simulation of Fluidized-Bed Boilers and Gasifiers, Fuel, 68 1507-1521 (1989). [ Links ]

de Souza-Santos, M. L., Application of Comprehensive Simulation of Fluidized-Bed Reactors to the Pressurized Gasification of Biomass. Journal of the Brazilian Society of Mechanical Sciences, 16, 376-383 (1994a). [ Links ]

de Souza-Santos, M. L., Application of Comprehensive Simulation to Pressurized Fluidized Bed Hydroretorting of Shale. Fuel, 73, 1459-1465 (1994b). DOI: 10.1016/0016-2361(94)90063-9 [ Links ]

de Souza-Santos, M. L., A New Version of CSFB, Comprehensive Simulator for Fluidized Bed Equipment. Fuel, 86 1684-1709 (2007). DOI: 10.1016/j.fuel.2006.12.001 [ Links ]

de Souza-Santos, M. L., and Chavez, J. V., Preliminary studies on advanced power generation based on combined cycle using a single high-pressure fluidized bed boiler and consuming sugar-cane bagasse. Fuel, 95, 221-225 (2012a). DOI: 10.1016/j.fuel.2011.12.008 [ Links ]

de Souza-Santos, M. L., and Chavez, J. V., Development of Studies on Advanced Power Generation Based on Combined Cycle Using a Single High-Pressure Fluidized Bed Boiler and Consuming Sugar Cane Bagasse. Energy and Fuels, 26, 1952-1963 (2012b). DOI: 10.1021/ef2019935 [ Links ]

de Souza-Santos, M. L., and Chavez, J. V., Second round on advanced power generation based on combined cycle using a single high-pressure fluidized bed boiler and consuming biomass. The Open Chemical Engineering Journal, 6, 41-44 (2012c). DOI 10.2174/1874123101206010041 [ Links ]

de Souza-Santos, M. L, and Ceribeli, K., Technical Evaluation of a Power Generation Process Consuming Municipal Solid Waste. Fuel, 108 578-585 (2012). DOI: 10.1016/j.fuel.2012.12.037 [ Links ]

de Souza-Santos, M. L., and Ceribeli, K. B., Fuel-Slurry Integrated Gasifier/Gas Turbine (FSIG/GT) Alternative for Power Generation Applied to Municipal Solid Waste (MSW). Energy and Fuels, 27(12) 7696-7713 (2013). DOI: 10.1021/ef401878v. [ Links ]

de Souza-Santos, M.L., and Beninca, W.A., New Strategy of Fuel-Slurry Integrated Gasifier/Gas Turbine (FSIG/GT) Alternative for Power Generation Applied to Biomass. Energy & Fuels, 28 (4): 2697-2707, 2014. DOI: 10.1021/ef500317a, [ Links ]

de Souza-Santos, M. L., and Lima, E. H. S., Introductory Study on Fuel-Slurry Integrated Gasifier/Gas Turbine (FSIG/GT) Alternative for Power Generation Applied to High-Ash or Low-Grade Coal, Fuel, 143 275-284 (2015). doi: 10.1016/j.fuel.2014.11.060 [ Links ]

de Souza-Santos, M. L., Bernal, A. F. B., and Rodriguez-Torres, A. F., New Developments on Fuel-Slurry Integrated Gasifier/Gas Turbine (FSIG/GT) Alternative for Power Generation Applied to Biomass; Configuration Requiring No Steam for Gasification, Energy & Fuels, 29(6) 3879-3889 (2015). DOI: 10.1021/acs.energyfuels.5b00775. [ Links ]

de Souza-Santos, M. L., Very High-Pressure Fuel-Slurry Integrated Gasifier/Gas Turbine (FSIG/GT) Power Generation Applied to Biomass. Energy & Fuels, 29: 8066-8073, 2015. DOI: 10.1021/acs.energyfuels.5b02093. http://pubs.acs.org/doi/ipdf/10.1021/acs.energyfuels.5b02093Links ]

de Souza-Santos, M. L., Comprehensive Simulator (CSFMB) Applied to Circulating Fluidized Bed Boilers and Gasifiers. The Open Chemical Engineering Journal, 2: 106-118 (2008). DOI 10.2174/1874123100802010106 [ Links ]

de Souza-Santos, M. L., CSFB Applied to Fluidized-bed Gasification of Special Fuels. Fuel, 88: 826-833 (2009). doi.org/10.1016/j.fuel.2008.10.035Links ]

Engelbrecht, A. D., North, B. C., Oboirien, B. O., Everson, R. C., and Neomagus, H. W. P. J., Fluidised bed gasification of high-ash South African coals: An experimental and modelling study. IFSA 2011 Conference on Industrial Fluidization, Johannesburg, South Africa, November 16-17, 2011. www.saimm.co.za/Conferences/IFSA2011/145-Engelbrecht.pdf (accessed on 03/03/2014) [ Links ]

Fosso-Kankeu, E., Marx, S., and Globler, C., Simultaneous gas and electricicy production from na MCF stimulated by cruce glycerol, 7th Int. Conference on Latest Trends in Engineering & Technology (ICLTEL’2015), Nov. 26-27, 2015, Irene, Pretoria, South Africa. http://iieng.org/images/proceedings_pdf/5338E1115021.pdfLinks ]

Geldart, D., Gas Fluidization Technology, John Wiley, Chichester, U.K., 1986. [ Links ]

Gomez-Barea, A., and Leckner, B., Modeling of biomass gasification in fluidized bed, Progress in Energy and Combustion Science, 36(4) 444-509 (2010). [ Links ]

Krzywanski, J.; Żyłka, A., Czakiert, T., Kulicki, K., Jankowska, S., and Nowak, W., A 1.5D model of a complex geometry laboratory scale fluidized bed CLC equipment, Powder Technology, 316 592-598 (2017).: (http://dx.doi.org/10.1016/j.powtec.2016.09.041) [ Links ]

Kunii, D., and Levenspiel, O., Fluidization Engineering, 2nd Ed., John Wiley, New York, 1991. [ Links ]

Kunii, D., and Levenspiel, O., Circulating fluidized-bed reactors, Chemical Engineering Science, 52(15) 2471-2482 (1997). [ Links ]

Leonetia, A. B., Aragão-Leoneti, V., and Oliveira, S. V. W. B., Glycerol as a by-product of biodiesel production in Brazil: Alternatives of the use of unrefined glycerol, Renewable Energy, 45: 138-145, 2012. DOI: 10.1016/j.renene.2012.02.032, [ Links ]

Maintinguer, S. I., Hatanaka, R. R., and de Oliveira, J. E., Glycerol as raw material for hydrogen production, Biofuels - Status and Perspectives, Ed. Biernat K., INTECH, ISBN 978-953-51-2177-0, 2015. DOI: 10.5772/60013. http://www.intechopen.com/books/biofuels-status-and-perspective/glycerol-as-a-raw-material-for-hydrogen-production. [ Links ]

Manara, P., and Zabanioutou, A., Co-valorization of crude glycerol waste streams with conventional and/or renewable fuels for power generation and industrial symbiosis perspectives, Waste and Biomass Valorization, 7: 135-150, 2016 [ Links ]

Muskala, W., Krywanski, J., Cakiert, T., and Nowak, W., The research of CFB boiler operation for oxygen-enhanced dried lignite combustion, Rynek Energii, 92(1) 172-176 (2011). [ Links ]

Pagliaro, M., and Rossi, M., The Future of Glycerol, Green Chemistry Series, 2nd ed. RSC Publishing, Cambridge, 2010. [ Links ]

Philippsen, C. G., Vilela, A. C. F., and Zen, L. D., Fluidized bed modeling applied to the analysis of processes review and state of the art, Journal of Materials Research and Technology, 4(2) 208-216 (2015). [ Links ]

Rabi, J. A., and de Souza-Santos, M. L., Incorporation of a two-flux model for radiative heat transfer in a comprehensive fluidized bed simulator. Part I: Preliminary theoretical investigations. Thermal Engineering, 3 64-70 (2003). DOI: 10.5380/ret.v2i1.3516 [ Links ]

Rabi, J. A., and de Souza-Santos, M. L., Incorporation of a two-flux model for radiative heat transfer in a comprehensive fluidized bed simulator. Part II: Numerical results and assessment. Thermal Engineering, 4 49-54 (2004). DOI: 10.5380/ret.v2i2.3476 [ Links ]

Rabi, J. A, and de Souza-Santos, M. L., Comparison of Two Model Approaches Implemented in a Comprehensive Fluidized-Bed Simulator to Predict Radiative Heat Transfer: Results for a Coal-Fed Boiler. Computer and Experimental Simulations in Engineering and Science, 3 87-105 (2008). [ Links ]

Saraiva, P. C., Azevedo, J. L. T., and Carvalho, M. G., Mathematical simulation of a circulating fluidized bed combustor, Combustion Science and Technology, 93(1) 223-243 (1993). [ Links ]

Schultz, E. L., de Souza, D. T., and Damaso, M. C. T., The glycerol biorefinery: a purpose for Brazilian biodiesel production, Chemical and Biological Technologies in Agriculture, 1(1), 7 (2014). DOI: 10.1186/s40538-014-0007-z [ Links ]

Sricharoenchaikul, V., and Atong, D., Fuel gas generation from thermochemical conversion of crude glycerol mixed with biomass wastes, Energy Procedia, 14: 1286-1291, 2012. http://dx.doi.org/10.1016/j.egypro.2011.12.1090Links ]

Walker, P. L. Jr., Rusinko, F. Jr., and Austin, L. G., Gas Reactions of Carbon, in Advances in Catalysis, Vol. XI, Academic Press, New York, 1959. [ Links ]

Wei, L., Pordesimo, L. O., Haryanto, A., and Wooten, J., Co-gasification of hardwood chips and crude glycerol in a pilot scale downdraft gasifier. Bioresource Technology, 102(10): 6266-6272, 2011. DOI: 10.1016/j.biortech.2011.02.109, [ Links ]

Received: August 15, 2016; Revised: December 19, 2016; Accepted: March 24, 2017

*Corresponding author: Marcio L. de Souza-Santos. Email: dss@csfmb.com

Creative Commons License This is an Open Access article distributed under the terms of the Creative Commons Attribution License, which permits unrestricted use, distribution, and reproduction in any medium, provided the original work is properly cited.