Devolatilization of Residual Biomasses for Chemical Looping Gasification in Fluidized Beds Made Up of Oxygen-Carriers

The chemical looping gasification of residual biomasses—operated in fluidized beds composed of oxygen-carriers—may allow the production of biofuels from syngas. This biomassto-fuel chain can contribute to mitigate climate change, avoiding the accumulation of greenhouse gases in our atmosphere. The ongoing European research project Horizon2020 CLARA (G.A. 817841) investigates wheat-straw-pellets (WSP) and raw-pine-forest-residue (RPR) pellets as feedstocks for chemical looping gasification. This work presents experimental results from devolatilizations of WSP and RPR, in bubbling beds made of three different oxygen-carriers or sand (inert reference), at 700, 800, 900 ◦C. Devolatilization is a key step of gasification, influencing syngas quality and quantity. Tests were performed at laboratory-scale, by a quartz reactor (fluidizing agent: N2). For each pellet, collected data allowed the quantification of released gases (H2, CO, CO2, CH4, hydrocarbons) and mass balances, to obtain gas yield (ηav), carbon conversion (χC), H2/CO ratio (λav) and syngas composition. A simplified single-first order-reaction model was adopted to kinetically analyze experimental data. WSP performed as RPR; this is a good indication, considering that RPR is similar to commercial pellets. Temperature is the dominating parameter: at 900 ◦C, the highest quality and quantity of syngas was obtained (WSP: ηav = 0.035–0.042 molgas gbiomass, χC = 73–83%, λav = 0.8–1.0); RPR: ηav = 0.036–0.041 molgas gbiomass, χC = 67–71%, λav = 0.9–1.0), and oxygencarries generally performed better than sand. The kinetic analysis suggested that the oxygen-carrier ilmenite ensured the fastest conversion of C and H atoms into gases, at tested conditions.


Introduction
The use of biomasses as a renewable feedstock has been investigated with great interest for producing energy and biofuels [1][2][3][4]. Several governmental programs have sustained this interest [1]: the European Union (EU) imposed to reach a 10% share of biofuels in the transport sector by 2020 [5]; in the USA, biofuels are expected to reach a production of 36 billion gallons by 2022 [6]. In the near future, so-oriented policies may represent a viable way to combine economic growth with the urgent need to oppose climate change, which was recently highlighted by the Paris agreement and the subsequent Conferences of the Parties to the United Nations Framework Conventions on Climate Change [1,[7][8][9][10].
The chemical looping gasification for sustainable production of biofuels (CLARA) research project, funded by the EU Horizon 2020 framework program, G.A. 817841 [11] aims to contribute in this sense. This project deals with chemical looping gasification (CLG) of biogenic residues, with the obtained syngas used in the Fischer-Tropsch synthesis to produce liquid fuels, as also obtained by the hydrocracking of waxes resulting from Fischer-Tropsch. The main goal of CLARA is the realization of a full biomass-to-fuel chain up to 1 MWth scale, in an industrially relevant environment (targets: cold gas efficiency of 82%, carbon conversion of 98%, tar in outlet syngas lower than 1 mg Sm −3 ) [11,12]. Table 1. Properties of fluid-dynamic interest and related minimum fluidization velocities of all bed materials, as functions of temperature (adapted from [12] for the OCs).  [3,2] determined by Malvern Mastersizer 2000. 2 Determined by comparison with known granular material. 3 Calculated by the semiempirical correlation presented in [12], with correlation constants C1 = 27.2 and C2 = 0.0408 [42,43].

Devolatilization Experiments
Devolatilization tests were performed at 700 • C, 800 • C and 900 • C, to observe the instantaneous pyrolysis behavior of WSP and RPR in bubbling fluidized beds made up of one OC or sand. The laboratory-scale experimental apparatus ( Figure 1) included one reactor made of quartz (5 cm internal diameter), placed in a cylindrical electric furnace, and fed upward by N 2 (carrier gas and fluidizing agent at 1.5 u mf ).

Devolatilization Experiments
Devolatilization tests were performed at 700 °C, 800 °C and 900 °C, to observe the instantaneous pyrolysis behavior of WSP and RPR in bubbling fluidized beds made up of one OC or sand. The laboratory-scale experimental apparatus ( Figure 1) included one reactor made of quartz (5 cm internal diameter), placed in a cylindrical electric furnace, and fed upward by N2 (carrier gas and fluidizing agent at 1.5umf). A sintered porous quartz plate sustained the fluidized bed and served as a gas distributor. The bottom part of the reactor, underneath this quartz plate, was filled by a packed bed made of SiC particles; this bulk of SiC was placed inside the furnace, so to work as a preheater for the fluidizing N2 flow. The masses of loaded OCs or sand were selected in order to obtain 7.5 cm high beds (1.5 times the bed diameter).
The temperature of the bed was controlled by a K-type thermocouple, protected by a quartz socket and submerged in the bed. Devolatilization products and N2 left the reactor from its top, passed through an ice trap and a double-pipe glass condenser (cooled by diethylene glycol at about 0 °C), to be then analyzed by an ABB online system (ABB S.p.A., Sesto San Giovanni (MI), Italy) and by a micro-gas chromatograph (μGC) (Agilent 490, Agilent Technologies Italia S.p.A., Cernusco sul Naviglio (MI), Italy).
The ABB system included an ADVANCE OPTIMA URAS 14 module for CO, CO2, CH4 (non-dispersive infrared detector, NDIR), an ADVANCE OPTIMA CALDOS 17 module for H2 (thermal conductibility detector, TCD), and an ADVANCE OPTIMA MULTI-FID14 (flame ionization detector, FID) for hydrocarbons. Concentrations of CO, CO2, CH4 and H2 were measured as vol%, while the overall hydrocarbons content was expressed as ppmv of equivalent C3H8. The Agilent 490 μGC system was equipped in order to identify: ethane, ethylene/acetylene, propane, propene, propadiene, propyne, n-butane, isobutane, n-pentane, isopentane, neopentane, n-hexane, benzene and toluene. These species could contribute to the total hydrocarbons quantified by the FID. For each tested pellet, one μGC analysis was performed on the stream of dry product gases thanks to a single sampling injection per test.
Biomass pellets were fed individually by hand, thanks to a vertical double-valve system over the reactor top (Figure 1), at room temperature: (i) the upper valve was opened to load the pellet, while the lower one remained closed to isolate the reaction environment; (ii) the upper valve was closed to isolate the reaction environment, then the lower one was opened to make the pellet fall into the bed. This manual system allowed to make the pellet experience a temperature transition similar to that of industrial feeding, i.e., an abrupt A sintered porous quartz plate sustained the fluidized bed and served as a gas distributor. The bottom part of the reactor, underneath this quartz plate, was filled by a packed bed made of SiC particles; this bulk of SiC was placed inside the furnace, so to work as a preheater for the fluidizing N 2 flow. The masses of loaded OCs or sand were selected in order to obtain 7.5 cm high beds (1.5 times the bed diameter).
The temperature of the bed was controlled by a K-type thermocouple, protected by a quartz socket and submerged in the bed. Devolatilization products and N 2 left the reactor from its top, passed through an ice trap and a double-pipe glass condenser (cooled by diethylene glycol at about 0 • C), to be then analyzed by an ABB online system (ABB S.p.A., Sesto San Giovanni (MI), Italy) and by a micro-gas chromatograph (µGC) (Agilent 490, Agilent Technologies Italia S.p.A., Cernusco sul Naviglio (MI), Italy).
The ABB system included an ADVANCE OPTIMA URAS 14 module for CO, CO 2 , CH 4 (non-dispersive infrared detector, NDIR), an ADVANCE OPTIMA CALDOS 17 module for H 2 (thermal conductibility detector, TCD), and an ADVANCE OPTIMA MULTI-FID14 (flame ionization detector, FID) for hydrocarbons. Concentrations of CO, CO 2 , CH 4 and H 2 were measured as vol%, while the overall hydrocarbons content was expressed as ppm v of equivalent C 3 H 8 . The Agilent 490 µGC system was equipped in order to identify: ethane, ethylene/acetylene, propane, propene, propadiene, propyne, n-butane, isobutane, n-pentane, isopentane, neopentane, n-hexane, benzene and toluene. These species could contribute to the total hydrocarbons quantified by the FID. For each tested pellet, one µGC analysis was performed on the stream of dry product gases thanks to a single sampling injection per test.
Biomass pellets were fed individually by hand, thanks to a vertical double-valve system over the reactor top (Figure 1), at room temperature: (i) the upper valve was opened to load the pellet, while the lower one remained closed to isolate the reaction environment; (ii) the upper valve was closed to isolate the reaction environment, then the lower one was opened to make the pellet fall into the bed. This manual system allowed to make the pellet experience a temperature transition similar to that of industrial feeding, i.e., an abrupt switch from room temperature up to that of the bed. This was not possible by more usual equipment, such as thermogravimetric analyzers. For each set "biomass kind/bed material/bed temperature", three repetitions of individual pellet devolatilization were performed. The devolatilization of one pellet was carried out until completion, before feeding the following; as a consequence, the process was in unsteady-state.
Outlet molar flow rates (F i,out ) were determined as functions of time (t) for produced H 2 , CO, CO 2 , CH 4 and equivalent C 3 H 8 , thanks to ABB measurements and assuming the N 2 inlet flow rate as the internal standard. Values of F i,out , individual pellet masses (m p ) and biomass composition [38] allowed the calculation of integral-average values of: gas yield (η av , Equation (1)), percentage composition on dry and dilution-free basis (Y av i , Equation (2)), carbon conversion (χ av C , Equation (3), with n j as the number of C atoms in j), outlet H 2 /CO molar ratio (λ av , Equation (4)). For each set "biomass kind/bed material/bed temperature", average values of the three repetition were calculated for η av , Y av i , χ av C , and λ av , provided with related standard deviations:

Kinetic Parameters for Devolatilization in Fluidized Beds
The proposed modelling approach (see Appendix A) was based on some simplifying hypotheses, so to provide a simple tool for evaluations in the context of this work, tailored to the kind of data obtained by the experimental procedure described in Section 2.3.
In general, the different reaction zones of biomass devolatilization-which correspond to the decomposition of biomass components-tend to merge with more severe heating conditions [44]; therefore, when fast heating rate or high temperature conditions occur (like in this work), the devolatilization mechanism consists of a one-stage decomposition, made up of three parallel reactions: three lumped products are involved (char, liquid and tars, gases) [44], according to the scheme proposed by Shafizadeh and Chin [45] for wood ( Figure 2). yield (η av , Equation (1)), percentage composition on dry and dilution-free basis (Y av i, Equation (2)), carbon conversion (χ av C, Equation (3), with nj as the number of C atoms in j), outlet H2/CO molar ratio (λ av , Equation (4)). For each set "biomass kind/bed material/bed temperature", average values of the three repetition were calculated for η av , Y av i, χ av C, and λ av , provided with related standard deviations:

Kinetic Parameters for Devolatilization in Fluidized Beds
The proposed modelling approach (see Appendix A) was based on some simplifying hypotheses, so to provide a simple tool for evaluations in the context of this work, tailored to the kind of data obtained by the experimental procedure described in Section 2.3.
In general, the different reaction zones of biomass devolatilization-which correspond to the decomposition of biomass components-tend to merge with more severe heating conditions [44]; therefore, when fast heating rate or high temperature conditions occur (like in this work), the devolatilization mechanism consists of a one-stage decomposition, made up of three parallel reactions: three lumped products are involved (char, liquid and tars, gases) [44], according to the scheme proposed by Shafizadeh and Chin [45] for wood ( Figure 2).  For this mechanism, the single first order reaction (SFOR) model is usually adopted [44,46,47] as generalized in Equation (5), where w(t) is the mass fraction of biomass (i.e., all the biomass not transformed in char, liquid-tars, gases) as a function of time (t), and k is the specific reaction rate expressed by an Arrhenius-type function: In this work, the SFOR model was adapted to the nature of available experimental devolatilization data. The adapted model (see Appendix A) allowed the determinationfor each bed material-of specific reaction rates for the conversion of C and H atoms from biomass into gas products H 2 , CO, CO 2 , CH 4 . These specific reaction rates were named k C and k H , respectively.
Thanks to experiments at three temperature levels (T), pre-exponential factors (A C and A H ) and activation energies (E a,C and E a,H ) were calculated from values of k C and k H , for each couple "biomass kind/bed material". Readers should refer to Appendix A for further details. Figure 3 shows examples of gas produced by devolatilizations of individual pellets, evidencing the intrinsic unsteady-state of the monitored process: devolatilization products were released in the carrier gas and transported to the analyzers, determining the characteristic peak form of the calculated outlet molar flowrates (F i,out ). As previously verified in the same laboratory of this work [30], an experimental system as the one described in Section 2.3 generates a flow-mixing which is reasonably well modeled as a perfect mixer (reactor) together with plug flow (transport lines to the analyzers). As to F i,out curves of H 2 , CO, CO 2 , CH 4 , the lag time related to transmission lines was eliminated by the data treating process; on the other hand, the peak of F C3H8,out presented a systematic delay in comparison to others. This depends on the position of the sampling point of MULTI-FID 14: it was placed at the very end of the experimental apparatus, just before the vent of the product gases, therefore after these gases had already passed through all other analyzers.

Results
For this mechanism, the single first order reaction (SFOR) model is usually adopted [44,46,47] as generalized in Equation (5), where w(t) is the mass fraction of biomass (i.e., all the biomass not transformed in char, liquid-tars, gases) as a function of time (t), and k is the specific reaction rate expressed by an Arrhenius-type function: In this work, the SFOR model was adapted to the nature of available experimental devolatilization data. The adapted model (see Appendix A) allowed the determinationfor each bed material-of specific reaction rates for the conversion of C and H atoms from biomass into gas products H2, CO, CO2, CH4. These specific reaction rates were named kC and kH, respectively.
Thanks to experiments at three temperature levels (T), pre-exponential factors (AC and AH) and activation energies (Ea,C and Ea,H) were calculated from values of kC and kH, for each couple "biomass kind/bed material". Readers should refer to Appendix A for further details. Figure 3 shows examples of gas produced by devolatilizations of individual pellets, evidencing the intrinsic unsteady-state of the monitored process: devolatilization products were released in the carrier gas and transported to the analyzers, determining the characteristic peak form of the calculated outlet molar flowrates (Fi,out). As previously verified in the same laboratory of this work [30], an experimental system as the one described in Section 2.3 generates a flow-mixing which is reasonably well modeled as a perfect mixer (reactor) together with plug flow (transport lines to the analyzers). As to Fi,out curves of H2, CO, CO2, CH4, the lag time related to transmission lines was eliminated by the data treating process; on the other hand, the peak of FC3H8,out presented a systematic delay in comparison to others. This depends on the position of the sampling point of MULTI-FID 14: it was placed at the very end of the experimental apparatus, just before the vent of the product gases, therefore after these gases had already passed through all other analyzers.    Figure 4 compares all integral-average gas yields (η av , Equation (1)), carbon conversions (χ av C, Equation (3)) and outlet H2/CO molar ratios (λ av , Equation (4)). Figure 5 does the same for integral-average compositions (Y av i, Equation (2)) of produced H2, CO, CO2, CH4 and equivalent C3H8. Numerical data represented in Figures 4 and 5 were reported in the Appendix B of this work. For each individual devolatilization, one online sampling of produced gas was carried out by the μGC AGILENT 490; for the sake of brevity, results are not detailed in this work, but just discussed in Section 4. The integration of those peaks with respect to time allowed the calculation of mass balances for each tested pellet, and then the quantification of results summarized in Figures 4 and 5, according to the procedure described in Section 2.3. Figure 4 compares all integral-average gas yields (η av , Equation (1)), carbon conversions (χ av C , Equation (3)) and outlet H 2 /CO molar ratios (λ av , Equation (4)). Figure 5 does the same for integral-average compositions (Y av i , Equation (2)) of produced H 2 , CO, CO 2 , CH 4 and equivalent C 3 H 8 . Numerical data represented in Figures 4 and 5 were reported in the Appendix ?? of this work. For each individual devolatilization, one online sampling of produced gas was carried out by the µGC AGILENT 490; for the sake of brevity, results are not detailed in this work, but just discussed in Section 4.  The integration of those peaks with respect to time allowed the calculation of mass balances for each tested pellet, and then the quantification of results summarized in Figures 4 and 5, according to the procedure described in Section 2.3. Figure 4 compares all integral-average gas yields (η av , Equation (1)), carbon conversions (χ av C, Equation (3)) and outlet H2/CO molar ratios (λ av , Equation (4)). Figure 5 does the same for integral-average compositions (Y av i, Equation (2)) of produced H2, CO, CO2, CH4 and equivalent C3H8. Numerical data represented in Figures 4 and 5 were reported in the Appendix B of this work. For each individual devolatilization, one online sampling of produced gas was carried out by the μGC AGILENT 490; for the sake of brevity, results are not detailed in this work, but just discussed in Section 4.     According to the procedure described in Appendix A, the values of H2, CO, CO2, CH4 outlet molar flowrates (Fi,out) were also used to determine the specific reaction rates kC and kH, representative of the overall conversion of C and H atoms from biomass into gas products; kinetic constants related to the different temperature levels allowed the calculation of pre-exponential factors (AC and AH) and activation energies (Ea,C and Ea,H). Values of kC and kH are in Appendix B of this work, while Table 2 summarizes the obtained values of AC, AH, Ea,C and Ea,H. Table 2. Pre-exponential factors and activation energies calculated from devolatilization data according to the procedure described in Appendix A.

Experimental Data
As a first point for this discussion, it is worth to stress that the reactor feed was anoxic and dry (pure N2), so the main sources of oxygen are the bed, when OCs are used, and the biomass. As a consequence, the presence of oxidized carbon in gases (CO and CO2, see Figure 5) is due to the solids involved in the process. Some general effects due to temperature emerged from the results presented in Section 3. As can be seen in Figure 4, for all bed materials (sand, ILM, SIB, LD) and both biomasses (WSP and RPR) integral-average gas yields (η av , Equation (1), Figure 4a-c), carbon conversions (χ av C, Equation (3), Figure 4d-f) and H2/CO ratios (λ av , Equation (4), Figure 4g-i) increased as the temperature was increased from 700 °C to 900 °C. As to integral-average gas composition (Y av i, Equation (2), Figure 5), whatever the bed material or the converted biomass, concentrations of CO2, CH4 and equivalent C3H8 decreased as the temperature was increased, while that of H2 concomitantly became higher; this could be ascribed to the enhancement of hydrocarbons decomposition (thermal cracking or reforming reactions), while the decrease of CO2 could be ascribed to a the lower extent of exothermic reactions (combustion and water gas shift). CO did not show relevant trends of variation with tem- According to the procedure described in Appendix A, the values of H 2 , CO, CO 2 , CH 4 outlet molar flowrates (F i,out ) were also used to determine the specific reaction rates k C and k H , representative of the overall conversion of C and H atoms from biomass into gas products; kinetic constants related to the different temperature levels allowed the calculation of pre-exponential factors (A C and A H ) and activation energies (E a,C and E a,H ). Values of k C and k H are in Appendix ?? of this work, while Table 2 summarizes the obtained values of A C , A H , E a,C and E a,H . Table 2. Pre-exponential factors and activation energies calculated from devolatilization data according to the procedure described in Appendix A.

Experimental Data
As a first point for this discussion, it is worth to stress that the reactor feed was anoxic and dry (pure N 2 ), so the main sources of oxygen are the bed, when OCs are used, and the biomass. As a consequence, the presence of oxidized carbon in gases (CO and CO 2 , see Figure 5) is due to the solids involved in the process. Some general effects due to temperature emerged from the results presented in Section 3. As can be seen in Figure 4, for all bed materials (sand, ILM, SIB, LD) and both biomasses (WSP and RPR) integral-average gas yields (η av , Equation (1), Figure 4a-c), carbon conversions (χ av C , Equation (3), Figure 4d-f) and H 2 /CO ratios (λ av , Equation (4), Figure 4g-i) increased as the temperature was increased from 700 • C to 900 • C. As to integral-average gas composition (Y av i , Equation (2), Figure 5), whatever the bed material or the converted biomass, concentrations of CO 2 , CH 4 and equivalent C 3 H 8 decreased as the temperature was increased, while that of H 2 concomitantly became higher; this could be ascribed to the enhancement of hydrocarbons decomposition (thermal cracking or reforming reactions), while the decrease of CO 2 could be ascribed to a the lower extent of exothermic reactions (combustion and water gas shift). CO did not show relevant trends of variation with temperature. The measurements of µGC generally agreed with trends of equivalent C 3 H 8 (especially data related to sand). In addition, they suggested that the equivalent C 3 H 8 contained hydrocarbons among those detectable by the µGC (see Section 2.3); for instance, at 700 • C with sand, peaks with retention times compatible to all detectable hydrocarbons appeared at least once, except for n-hexane, toluene, propadiene and propene; at 800 • C with sand, only peaks compatible with ethylene/acetylene, ethane, n-butane and benzene were found, while at 900 • C no hydrocarbons were identified. With OCs, only benzene and C 4 hydrocarbons were occasionally identified. In any case, the µGC analyses must be considered only as an optional support to the identification of hydrocarbons quantified by the FID detector; the fact that the sampling was started manually, during an intrinsically unsteady process, imposes to use caution in the interpretation of µGC results.
Less clear-cut trends could be ascribed to the different kinds of biomass or OCs; still, some evidences could be commented.
WSP and RPR did not show performances of devolatilization with dramatic differences, as far as gas quantity (η av , Figure 4a-c) and quality (λ av , Figure 4g-i and Y av i , Figure 5) are concerned. More in detail, slightly higher carbon conversion (χ av C , Figure 4d-f) generally occurred for WSP. These were good process indications for the CLG of residual biomasses, since RPR could be considered as close to the current commercial reference of wood pellets; the fact that WSP had devolatilization performances similar to RPR corroborated WSP eligibility for the CLG, even though other factors should be taken into account (e.g., agglomeration tendencies of ashes in fluidized beds [12,48]).
With regard to WSP, when comparing the performance of OCs to that of sand, the action of OCs was exalted by the increase of temperature in terms of integral-average gas yield (η av , Figure 4a-c and Table A1) and carbon conversion (χ av C , Figure 4d-f and Table A1): these quantities for sand and OCs were comparable at 700 • C (Figure 4a,d and Table A1) and 800 • C (Figure 4b,e and Table A1), while the OCs generally ensured higher values at 900 • C (Figure 4c,f and Table A1). With regard to RPR, once standard deviation were taken into account for gas yields (Figure 4a-c and Table A2) and carbon conversions (Figure 4d-f and Table A2), less important effects due to the bed material emerged. For both biomasses, Figure 4g,i suggest that LD slightly improved the H 2 /CO ratio when compared to sand; this could be explained by the fact that LD can be involved in water-splitting reactions, thanks to wüstite-structures [49].
As far as integral-average gas compositions are concerned (Y av i , Equation (2)), some differences due to the OCs could be enucleated only at 700 • C (Figure 5a,d,g,j, Tables A1 and A2): SIB and LD increased the fraction of CO 2 in comparison to sand and ILM. Nevertheless, at 900 • C the distribution of gas components became very similar for all bed materials and biomasses (Figure 5c,f,i,l).
After this overall evaluation of the experimental data, 900 • C appeared as the most recommendable temperature to operate the thermal decomposition of both WSP and RPR, as it maximized gas yield (η av , Equation (1)), carbon conversion (χ av C , Equation (3)) and the H 2 /CO molar ratio (λ av , Equation (4)), whatever the used bed material (WSP: η av = 0.035-0.042 mol gas g biomass −1 , χ av C = 73-83%, λ av = 0.8-1.0); RPR: η av = 0.036-0.041 mol gas g biomass −1 , χ av C = 67-71%, λ av = 0.9-1.0). At 900 • C: • C of WSP resulted as slightly more converted into gases than C of RPR, while all other performance parameters could be considered very close; • in general, OCs incremented gas yield and carbon conversion in comparison to sand (the average values of the LD/RPR couple were lower than those of sand, but affected by a significative standard deviation); • the values of the molar H 2 /CO ratio (close to or equaling 1) were promising, since this work dealt with devolatilizations: with steam as a gasifying agent in a CLG process, one would expect to get higher H 2 /CO ratios, closer to the target of 2, which is ideal for the Fischer-Tropsch synthesis hypothesized in the biomass-to-fuel chain of the CLARA project. In this specific regard, LD appeared as the most interesting OC, as it was the only one ensuring a molar H 2 /CO ratio higher than that of sand, with both WSP and RPR.

Kinetic Analysis
As stated by Kersten et al. [50] in their Part I of a review about biomass devolatilization in a fluidized bed reactor, "there is wide variation in data published for combined values of the preexponential factor and activation energy. Published rate and selectivity expressions may be valuable in describing trends, but they can hardly ever be used for reliable quantitative prediction of anything else than the corresponding original data". In the light of this statement, only trends due to the kinetic parameters in Table 2 were analyzed, only for comparisons among the materials studied in this work.
Kinetic parameters in Table 2 must be intended as apparent, i.e., they lumped external heat transfer from bed to pellet, internal heat transfer inside the pellet, intrinsic devolatilization kinetics (in turn according to the one-component reaction scheme in Figure 2). As a matter of facts, in their Part II of the abovementioned review, Wand et al. [51] noted that "for the biomass particle sizes applied in practical reactors, from 1 to 5 mm, the pyrolysis time is influenced by all three mechanisms: the pyrolysis kinetics, the heat transfer from the bulk of the reactor to the particle, and the intraparticle heat conduction". Pellets of this work could be reasonably included in this case.
The specific reaction rates k C and k H , recalculated by Equation (6) and parameters in Table 2, helped to reabsorb part of the experimental variabilities obtained pellet by pellet (see Tables A3 and A4). Calculated k C and k H were interpreted as characteristic conversion frequencies of C and H, at a given temperature and at 1.5 u mf . For both WSP and RPR, k C and k H of OCs were higher than those of sand, suggesting a general benefic effect of OCs towards the conversion of biomass pellets into gases, inside a bubbling bed. With regard to C, both WSP and RPR had the highest specific reaction rates with ILM, at 700, 800 and 900 • C (e.g., at 900 • C, WSP: k C = 0.88 min −1 with ILM vs. k C = 0.58 min −1 with sand; RPR: k C = 0.72 min −1 with ILM vs. k C = 0.52 min −1 with sand). The same occurred with H, except for the SIB/WSP couple at 900 • C, even though greater than that of ILM/WSP by only 0.05 min −1 .
For each couple "biomass/bed material", H activation energy (E a,H , Table 2) was higher than C one (E a,C , Table 2): this matched well with the fact that integral-average H 2 fraction in the product gas was always the most affected by temperature increase (Y av H2 , Figure 5).

Conclusions
Once considered that RPR is close to current commercial biomass pellets, WSP resulted as a convincing alternative for thermochemical conversions, since the two biomasses always showed very similar devolatilization performances at the investigated conditions, in terms of gas yield, carbon conversion and H 2 /CO ratio.
Gas yields and carbon conversions from devolatilization tests with ILM, SIB and LD, compared to that of sand, suggested that OCs made a difference in devolatilization only at the highest tested temperature, i.e., 900 • C. This temperature appeared as the most interesting in the range 700-900 • C, from the point of view of CLG and subsequent Fischer-Tropsch reaction (hypothesized in the CLARA project): it maximized the content of H 2 and CO, as well as their ratio (close or equal to 1), at the expense of gaseous hydrocarbons.
A simplified kinetic modelling approach was proposed, which purposely investigated the overall conversion phenomenon of devolatilization in a bubbling bed, lumping external heat transfer, intra-particle heat transfer and intrinsic devolatilization kinetics. The data obtained by this kinetic analysis reabsorbed part of the experimental uncertainty (highlighted by related standard deviations), so helped to evidence some trends: OCs had a positive contribution in the conversion of both WSP and RPR, as they involved higher specific reaction rates in comparison to the inert bubbling bed of sand. Kinetic data suggested that ILM ensured the fastest conversion, all other condition being equal.
This work might do the underground for future developments. Collected data could be used in mathematical models which describe CLG. In addition, the straightforward laboratory-scale experiments of this work may serve as a screening to choose promising combinations of OCs and residual biomasses for more complex CLG tests, at higher scales and relevant industrial conditions; this would allow focusing the necessary characterization efforts (e.g., textural properties of fresh and spent solids) only on the most interesting cases. In conclusion, the methods used in this work are fully general and can be applied to study new kinds of biomass and OCs. χ C (t) = 12 g mol −1 × n C,g (t) These balances, integrated by separation of variables, allowed the calculation of specific reaction rates k C and k H for each devolatilization experiment, by the linear regression in the plots ln(1 − χ C (t)) vs. t and ln(1 − χ H (t)) vs. t, considering a 10-or 8-points neighborhood centered on the maximum of F H2,out (t). This choice ensured the internal coherence when comparing kinetic data from different tests, as all cases were considered at the maximum of their gas release rate; in addition, data at this maximum descended from the most quantitatively substantial measurements in the first part of each devolatilization.
In turn, thanks to experiments at different temperatures (T), pre-exponential factors (A C and A H ) and activation energies (E a,C and E a,H ) were calculated by linear regression in the plots lnk C (T) vs. 1/RT and lnk H (T) vs. 1/RT, with T in Kelvin.

Appendix B
This appendix summarizes, in the form of tables, the numerical results discussed in this manuscript: Tables A1 and A2 show the experimental data of devolatilization tests, discussed in the main text and reported as histograms in Figures 4 and 5; Tables A3 and A4 show the experimental kinetic constants k C and k H obtained according to Section 2.4 and Appendix A.