Novel Application of Pretreatment and Diagnostic Method Using Dynamic Pressure Fluctuations to Resolve and Detect Issues Related to Biogenic Residue Ash in Chemical Looping Gasification

Biogenic residues are a promising feedstock to produce liquid biofuels via chemical looping gasification (CLG), but they form ashes with a high inorganic matter content, thus causing agglomeration and deposition in CLG-fluidized beds made of oxygen carriers (OC). The aim of this work is to develop pretreatments for residual biomasses to prevent this issue. Raw forest pine (as a reference material) and wheat straw residues were considered. The latter were pretreated by torrefaction at 250, 260, or 270 °C and through the washing of torrefied biomasses. Torrefaction encouraged a de-chlorinating effect, while washing allowed the removal of 30–40% of S, 60–70% of K, and 40–50% of P. The analysis of pressure fluctuation signals (standard deviations and dominant frequencies) was utilized to verify the improvement of the performance of treated biomass in fluidized beds: three OCs were, respectively, coupled with ashes from all biomasses, then fluidized from 700 to 1000 °C at two and three times the minimum fluidization velocity. The diagnostic method used to analyze pressure fluctuations was shown to be effective for detecting the incipient fading of bubbling fluidization. This phenomenon was related to the agglomeration or the severe fragmentation of OC particles mixed with ashes, thanks to scanning electron microscopy and particle-size measurements. These characterizations and pressure fluctuations analyses confirmed the general improvement of wheat straw performances after pretreatments.


Introduction
The maximum target of a temperature increase of 2 • C above preindustrial levels, proposed by the Paris Agreement [1], is becoming an increasingly urgent issue in the current global scenario [2], requiring the reduction to zero of greenhouse gas (GHG) emissions by the end of this century [1,3]. Five key mitigation options have been proposed in order to achieve this goal, and the use of renewable sources and non-CO 2 emissions have the highest shares of these proposals, at 27% and 20%, respectively [4]. The use of biomass brings together these two options, since it is a renewable fuel (i.e., biofuel) and its CO 2 emissions can be potentially considered as neutral, owing to the fact that the produced CO 2 has previously been removed from the atmosphere in the process of biomass growth. Furthermore, the use of CO 2 -capture systems coupled with biomass combustion power plants would imply that the generated CO 2 would not be emitted. The approach using biomass and carbon-capture systems has pine or pine residues-favoring agglomeration phenomena. CLG may be suited for managing fuels with a high content of impurities, such as wheat straw. However, the reducing conditions of the fuel reactor can contribute to interactions between wheat straw and OC particles, by affecting the chemistry of impurities and even driving to issues due to trace elements. Finally, despite CLG flexibility in processing biogenic residues, the low energy density of wheat straw leads to the increase of costs for transport and problems with feeding systems.
For all these reasons, proper pretreatments of biogenic residual feedstock may be needed, in order to limit harmful agglomerative interactions with OCs in fluidized beds and negative effects from trace elements, as well as to increase the energy density of biomass. The aim of the CLARA project is to propose specific pretreatments to improve these qualities in wheat straw residues. Those pretreatments were developed by the National Renewable Energy Centre of Spain (CENER) and are described in this work.
The measurement of pressure in fluidized beds generally allows the evaluation of their fluidization quality [34]. The static pressure measurements are a usual method to monitor operating conditions in industrial fluidized-bed reactors, e.g., the determination of overall bed expansion or the control of elutriated fine particles which return to the bed through the cyclone dip-leg circuit [37]. In addition, the instantaneous pressure fluctuations are strongly related to the intrinsically heterogeneous bubbling state of fluidized beds [34]. For this reason, the detection and analysis of pressure fluctuations is a powerful diagnostic tool in cold-model studies [38][39][40][41], and bench- [42,43] and pilot-scale reactors [44]. It is also scalable up to direct applications in industrial reactors [35,45,46].
Several techniques have been developed so far to analyze signals of dynamic pressure fluctuations, usually classified into three groups: statistical study of pressure time-series (standard deviation) [47], study of dominant frequencies in power spectral density functions (PSDF) [38,39], and attractors comparison (state space analysis applied to the bed chaotic behavior) [40].
The research group of University of L'Aquila (UNIVAQ) has focused for more than twenty-five years on the analysis of dominant frequencies and standard deviations [38,39]; according to their approach, in most cases, the fluidized suspension may be regarded as being in a quasi-stationary state, with the mean values of its physical properties being time-independent over a finite period of time (ergodic signal) [48], so pressure fluctuation signals of finite duration can be studied. For a pressure fluctuation signal from a bubbling fluidized bed: • The amplitude of pressure fluctuations (i.e., standard deviation of their signal) mainly depends on bed oscillations, which are in turn caused by the eruption of bubbles at the bed upper surface [49] (the larger the bubbles, the higher the standard deviations, with all other properties of the system being equal).

•
The dominant frequency of the PSDF, representative of bubbling, is proportional to the number of erupting bubbles [50,51].
These properties of pressure fluctuation signals allow the investigation of the fluctuation quality in bubbling fluidized beds, also in the case of particles agglomeration. Schouten and van den Bleek [45] suggested a method which uses the short-term predictability of local pressure fluctuations to provide a warning signal of incipient agglomeration of the particles, and possible de-fluidization, in high-temperature fluidized bed reactors. Scala [35] reviewed the issue of agglomeration in fluidized beds during the combustion of biomass, due to low melting compounds (typically alkali metals) in this feedstock: at the industrial scale, the "on-line" early detection of particles agglomeration is needed to avoid unscheduled shutdowns. This excludes all methods based on the characterization of biomass ashes, as well as the usual simple monitoring of temperature and pressure at different bed locations, as they both detect significant changes only when de-fluidization has already occurred. In the same review, Scala [35] reports successful applications of agglomeration early detection at the industrial scale, based on the statistical analysis of non-linear time-series of pressure fluctuations (attractor comparison), named early agglomeration recognition system (EARS).
The aim of this study is to apply the analysis of instantaneous pressure fluctuations, both in the frequency and time domains, as a tool to detect de-fluidization phenomena in bubbling fluidized beds made of materials to be used in the CLG of biogenic residues. Pressure fluctuations from these fluidized beds, made of OCs and ashes from biogenic residual biomasses-pretreated or not-were investigated at the lab-scale, as functions of gas flux, temperature, kind of ash, and kind of OC. This work also describes and validates the pretreatments of wheat straw, developed by experimental tests which combined thermal treatment (torrefaction) and washing, to prevent operational issues due to ashes and improve biomass performances in CLG.

Production, Pretreatments, and Characterizations of Biomasses
Two biogenic residues were selected for this work, because of their availability and potential for use in Europe and worldwide: wheat straw and raw pine forest residues, both coming from Navarra in the North of Spain. In addition, several batches of wheat straw pellets were pretreated.
Raw and pretreated biomass samples were characterized according to the European reference standards' specifics for solids biofuels (Table 1). Microwave acid digestion was applied instead of ashing at 550 • C for major elements, prior to the determination by optical emission spectroscopy combined with inductively coupled plasma source (ICP/OES). This option was preferred in order to avoid the volatilization of substances caused by a pretreatment with a muffle furnace. With regard to the study of ash melting behavior, ash samples were produced at 550 • C with a muffle furnace. The same temperature was set to determine ash content, instead of 880 • C. Several experimental campaigns on raw biomasses were carried out by the pretreatment unit in the biorefinery and bioenergy center (BIO2C) of CENER ( Figure 1). The pretreatment unit gathers several pilot plants, including chipping, chopping, drying, milling, and pelleting, with a productive capacity between 150 and 500 kg h −1 . The chopping and chipping units allow decreasing and homogenizing the biomass particles' size, for either wood-based or fiber-based materials. The drying unit consists of a trommel-type rotary dryer, which decreases the moisture content of biomass. A hammer miller serves as the milling unit: it produces a biomass meal which is suitable as a feedstock in pelleting operation. Finally, the pelleting unit is a 30 kW pellet press, using ring die and rollers. Further information on these pilot plants is given elsewhere [52].
Thermal treatments were applied only to wheat straw, and the related procedures were developed through one experimental campaign, by a lab-scale rotating batch reactor for torrefaction ( Figure 2). This reactor was designed and constructed by CENER, under the framework of the CLARA project. It can process up to 10 L of many different materials. It is electrically heated by an independent furnace, which reaches temperatures up to 300 • C. The temperature is measured by three thermocouples located along the reactor. Thermal treatments were applied only to wheat straw, and the related procedures were developed through one experimental campaign, by a lab-scale rotating batch reactor for torrefaction ( Figure 2). This reactor was designed and constructed by CENER, under the framework of the CLARA project. It can process up to 10 L of many different materials. It is electrically heated by an independent furnace, which reaches temperatures up to 300 °C. The temperature is measured by three thermocouples located along the reactor. The raw pine forest residues underwent chipping, drying to obtain humidity of ~9.0%, milling, and eventually pelleting.
The raw wheat straw was only chopped before milling and pelleting. Afterwards, different pretreatments were carried out on batches of wheat straw pellets, which consisted of torrefaction or torrefaction followed by washing. Each torrefaction step lasted for 30-40 min while 360 NL h −1 of N2 were continuously fed to avoid the presence of oxygen in the reactor. In order to increase the torrefaction degree, three temperatures were chosen: 250 °C (T1), 260 °C (T2), or 270 °C (T3).
Afterward, the obtained pellets were subjected to the first step of the chemical fractionation procedure [53][54][55][56] and then analyzed to verify the effect of torrefaction degree on the leachability of sulfur, chlorine, and potassium. The potential leachability of inorganic matter is well known for different straws and many other biomasses [57] by the chemical fractionation procedure, but no bibliographic data have been identified yet for torrefied biomasses.
The washing of torrefied samples, about 100 g, consisted of a treatment with de-ionized Milli-Q water for 24 h at room temperature (20 °C), with a solid to liquid ratio of 1:10. The final solid was recovered by filtration and rinsed three times with 100 mL of de-ionized Milli-Q water. Finally, the wet samples were dried overnight at 45 °C, until the moisture became stable.
The obtained samples were named as follows: • Wheat straw pellets (WSP, i.e., pellets of raw wheat straw)  Thermal treatments were applied only to wheat straw, and the related procedures were developed through one experimental campaign, by a lab-scale rotating batch reactor for torrefaction ( Figure 2). This reactor was designed and constructed by CENER, under the framework of the CLARA project. It can process up to 10 L of many different materials. It is electrically heated by an independent furnace, which reaches temperatures up to 300 °C. The temperature is measured by three thermocouples located along the reactor. The raw pine forest residues underwent chipping, drying to obtain humidity of ~9.0%, milling, and eventually pelleting.
The raw wheat straw was only chopped before milling and pelleting. Afterwards, different pretreatments were carried out on batches of wheat straw pellets, which consisted of torrefaction or torrefaction followed by washing. Each torrefaction step lasted for 30-40 min while 360 NL h −1 of N2 were continuously fed to avoid the presence of oxygen in the reactor. In order to increase the torrefaction degree, three temperatures were chosen: 250 °C (T1), 260 °C (T2), or 270 °C (T3).
Afterward, the obtained pellets were subjected to the first step of the chemical fractionation procedure [53][54][55][56] and then analyzed to verify the effect of torrefaction degree on the leachability of sulfur, chlorine, and potassium. The potential leachability of inorganic matter is well known for different straws and many other biomasses [57] by the chemical fractionation procedure, but no bibliographic data have been identified yet for torrefied biomasses.
The washing of torrefied samples, about 100 g, consisted of a treatment with de-ionized Milli-Q water for 24 h at room temperature (20 °C), with a solid to liquid ratio of 1:10. The final solid was recovered by filtration and rinsed three times with 100 mL of de-ionized Milli-Q water. Finally, the wet samples were dried overnight at 45 °C, until the moisture became stable.
The obtained samples were named as follows: • Wheat straw pellets (WSP, i.e., pellets of raw wheat straw) The raw pine forest residues underwent chipping, drying to obtain humidity of~9.0%, milling, and eventually pelleting.
The raw wheat straw was only chopped before milling and pelleting. Afterwards, different pretreatments were carried out on batches of wheat straw pellets, which consisted of torrefaction or torrefaction followed by washing. Each torrefaction step lasted for 30-40 min while 360 NL h −1 of N 2 were continuously fed to avoid the presence of oxygen in the reactor. In order to increase the torrefaction degree, three temperatures were chosen: 250 • C (T1), 260 • C (T2), or 270 • C (T3).
Afterward, the obtained pellets were subjected to the first step of the chemical fractionation procedure [53][54][55][56] and then analyzed to verify the effect of torrefaction degree on the leachability of sulfur, chlorine, and potassium. The potential leachability of inorganic matter is well known for different straws and many other biomasses [57] by the chemical fractionation procedure, but no bibliographic data have been identified yet for torrefied biomasses.
The washing of torrefied samples, about 100 g, consisted of a treatment with de-ionized Milli-Q water for 24 h at room temperature (20 • C), with a solid to liquid ratio of 1:10. The final solid was recovered by filtration and rinsed three times with 100 mL of de-ionized Milli-Q water. Finally, the wet samples were dried overnight at 45 • C, until the moisture became stable.
The obtained samples were named as follows: • Raw pine forest residue pellets (RPR), as a reference material for the comparative study.

Characterization of Oxygen-Carriers
Three OCs were studied in this work, kindly provided by University of Chalmers (Sweden), a partner of the CLARA project: ilmenite (iron-titanium-based mineral) [58], Sibelco calcined (manganese-iron-based mineral), and LD-slag (iron-manganese-calcium-based material) [59]. From here on, they are respectively named ILM, SIB, LD.
The following physical-chemical properties of these OCs were determined: • Particle density (ρ p ), by comparison with granular materials with similar granulometries and known densities.

•
Particle size distribution and average particle diameter (d p ), by a Malvern Mastersizer 2000.

•
Semi-quantitative elemental composition, by X-ray fluorescence (XRF) carried out with a Spectro Xepos I.

•
Morphological-topological aspects, observed by scanning electron microscopy (SEM) with a Zeiss GeminiSEM 500 microscope equipped with energy dispersive X-ray spectrometry (EDS) for elemental analyses (EDS equipment: OXFORD Aztec Energy with a detector INCA X-ACT PELTIER COOLED ADD). Results of EDS analyses are mentioned in the next sections, but only the related SEM micrographs are shown.

Acqusition and Data Processing of Pressure Fluctuation Signals
Fluidization tests were carried out at UNIVAQ. The signals of dynamic pressure fluctuation were acquired from fluidized beds made of one OC and ashes from one of the available biomasses, at temperatures of interest for CLG, with N 2 as the fluidizing medium. All possible OC-ashes couples were tested (three OCs and eight kinds of ash).
For each test, 90 mL of OC particles were mixed with 9 mL of ashes (bulk volumes), so as to: (i) avoid influences from the parameter "bed height" on pressure fluctuation signals [51], and (ii) make the results from different tests comparable to each other. Acquisitions were performed during seven temperature dwells (700, 750, 800, 850, 900, 950, and 1000 • C) while N 2 was fluidizing the bed. Two N 2 flow rates were set at each temperature, to develop superficial velocities (u) equal to two and three times the minimum fluidization velocity (u mf ) of the investigated OC, determined as described at the end of this sub-section. Two repeated acquisitions were taken for each u at each temperature, at least. At the end of each temperature dwell, a small sample of the bed was taken for further characterizations.
The test rig ( Figure 3) included one fluidized bed quartz reactor (internal diameter of 4.5 cm), fed upward by N 2 , placed in an electrical furnace, and equipped with a pressure probe submerged in the fluidized bed. That probe was connected to a piezoelectric pressure transducer, which in turn transmitted its signal to an integrated charge-amplifier/digital-converter KISTLER 5165A, interfaced with a PC to store data via the KISTLER Network Setup Wizard. The temperature of the solid inventory was measured independently, by a type-K thermocouple inside the bed, protected by a cylindrical socket made of quartz.
Signals were processed by a purposely developed MATLAB ® R2020a script, which corrects their drift and calculates standard deviations and PSDF by fast Fourier transform (FFT). The standard deviations of pressure signals were divided by the bed weight per unit of reactor circular cross-section, in order to obtain normalized values and compare results from different tests without fail.
Signals of pressure fluctuation must be made of at least 10,000 points [60], in order to be statistically significant. Thus, considering the requirements of FFT, the number of sampled points per acquisition was set as the equal of 16,384 (2 14 , the first power of 2 higher than 10,000). A sampling frequency of 100 Hz was chosen. It is higher than the typical frequencies of bubbling beds by one order of magnitude, so that requirements of the Nyquist theorem are fulfilled. As a consequence, each acquisition lasted 163.84 s. Signals were processed by a purposely developed MATLAB ® R2020a script, which corrects their drift and calculates standard deviations and PSDF by fast Fourier transform (FFT). The standard deviations of pressure signals were divided by the bed weight per unit of reactor circular cross-section, in order to obtain normalized values and compare results from different tests without fail.
Signals of pressure fluctuation must be made of at least 10,000 points [60], in order to be statistically significant. Thus, considering the requirements of FFT, the number of sampled points per acquisition was set as the equal of 16,384 (2 14 , the first power of 2 higher than 10,000). A sampling frequency of 100 Hz was chosen. It is higher than the typical frequencies of bubbling beds by one order of magnitude, so that requirements of the Nyquist theorem are fulfilled. As a consequence, each acquisition lasted 163.84 s.
Prior to tests: • Ashes were produced in a muffle furnace: pellets of all biomasses were burnt at 700 °C for 3 h, in such a way that ashes could experience temperatures from 700 to 1000 °C in the presence of OCs for the very first time during fluidization.
• umf of OCs were experimentally determined at the temperatures of pressure fluctuation acquisitions, by fluid-dynamic curves of bed pressure drops vs. superficial velocity [61].

•
Experimental values of umf (umf,exp) were compared with: (i) theoretical previsions of umf obtained by Equation (1) (umf,Ergun), which represents the balance of weight, buoyance, and drag forces, with the latter calculated by the Ergun equation (assuming φ = 1 and εmf = 0.4) [34,62], semiempirical previsions of umf obtained by the simplified Ergun equation (Equation (2)) (umf,Grace) [62], assuming the correlation constants C1 = 27.2 and C2 = 0.0408, as suggested by Grace [62,63]. Equations (3) and (4) define the Reynolds number at minimum fluidization conditions (Re ) and the Archimedes number (Ar), both dimensionless: N2 density ( ) and dynamic viscosity ( ) were properly evaluated as functions of temperature, and are the OC properties determined experimentally, as described in Section 2.3, and is the gravity acceleration. Prior to tests: • Ashes were produced in a muffle furnace: pellets of all biomasses were burnt at 700 • C for 3 h, in such a way that ashes could experience temperatures from 700 to 1000 • C in the presence of OCs for the very first time during fluidization. • u mf of OCs were experimentally determined at the temperatures of pressure fluctuation acquisitions, by fluid-dynamic curves of bed pressure drops vs. superficial velocity [61].

•
Experimental values of u mf (u mf,exp ) were compared with: (i) theoretical previsions of u mf obtained by Equation (1) (u mf,Ergun ), which represents the balance of weight, buoyance, and drag forces, with the latter calculated by the Ergun equation (assuming ϕ = 1 and ε mf = 0.4) [34,62], semiempirical previsions of u mf obtained by the simplified Ergun equation (Equation (2)) (u mf,Grace ) [62], assuming the correlation constants C1 = 27.2 and C2 = 0.0408, as suggested by Grace [62,63]. Equations (3) and (4) define the Reynolds number at minimum fluidization conditions (Re mf ) and the Archimedes number (Ar), both dimensionless: N 2 density (ρ N 2 ) and dynamic viscosity (µ N 2 ) were properly evaluated as functions of temperature, ρ p and d p are the OC properties determined experimentally, as described in Section 2.3, and g is the gravity acceleration. with:

Pretreatments of Biomasses
The main effects of the torrefaction temperature are summarized in Table 2, which shows the elemental weight percentage of nitrogen, sulfur, and chlorine in torrefied samples WSP-T1, WSP-T2, and WSP-T3. Table 2 highlights that the higher the torrefaction temperature, the lower the chlorine content. The opposite happened to nitrogen and sulfur, albeit to a lesser extent. This is in agreement with the literature [64], driving to consider the torrefaction as a de-chlorinating unit operation. Table 2. Effect of torrefaction temperature on the elemental composition of nitrogen, sulfur, and chlorine, expressed in weight percentage on a dry and ash-free basis, for pellets of raw wheat straw (WSP) and torrefied ones at T1, T2, T3. Chemical fractionation was operated on the torrefied pellets to determine the content of the most problematic inorganic elements (i.e., sulfur, potassium, and phosphorous). Figure 4 shows the effects of the washing treatment, in terms of leached percentage for these inorganic elements, as a function of the torrefaction temperature. It should be noted that chlorine was not represented, since it was below the detection limit (<0.005 wt% dry and ash-free basis (d.a.f.)). The potassium content was slightly decreased when the torrefaction temperature was increased, and the washing treatment removed 65-70% of potassium from torrefied wheat straw pellets. This range is in agreement with the bibliographic data concerning chemical fractionation [57], since about 40-70% of the potassium in straws is leached with a 24 h treatment in water, at room temperature. A similar behavior was observed for the phosphorous content as a function of the torrefaction temperature, achieving the removal of 45-50% from torrefied wheat straw. These figures do not fully agree with the literature; on the other hand, it should be stressed here that results of phosphorus removal by washing greatly depend on the type of biomass, changing in the literature from 60-70% [57] to 0-4% [56,65]. The values of sulfur removal were in the range 30-40%, but they did not lead to a pattern with the torrefaction temperature. These figures were far from the literature data (about 60-85% reported in References [56,57,65]).  Ash melting tests (Standard CEN/TS 15370-1) were carried out on all samples deriving from wheat straw. Figure 5 shows values of both initial deformation temperature (IDT) and hemisphere or softening temperature (SOT). IDT is the temperature at which the first signs of fusion occur, and SOT is the temperature at which the sample takes the form of a hemisphere. Notwithstanding the removal of potassium and chlorine by washing, no significant differences were observed between torrefied-washed samples and only torrefied ones. In addition, the wheat straw sample also had similar values to those of torrefied and torrefied-washed series. This means that a clear connection cannot be established between the investigated pretreatments and the ash melting behavior of wheat-based samples.  Ash melting tests (Standard CEN/TS 15370-1) were carried out on all samples deriving from wheat straw. Figure 5 shows values of both initial deformation temperature (IDT) and hemisphere or softening temperature (SOT). IDT is the temperature at which the first signs of fusion occur, and SOT is the temperature at which the sample takes the form of a hemisphere. Notwithstanding the removal of potassium and chlorine by washing, no significant differences were observed between torrefied-washed samples and only torrefied ones. In addition, the wheat straw sample also had similar values to those of torrefied and torrefied-washed series. This means that a clear connection cannot be established between the investigated pretreatments and the ash melting behavior of wheat-based samples.

WSP
or softening temperature (SOT). IDT is the temperature at which the first signs of fusion occur, and SOT is the temperature at which the sample takes the form of a hemisphere. Notwithstanding the removal of potassium and chlorine by washing, no significant differences were observed between torrefied-washed samples and only torrefied ones. In addition, the wheat straw sample also had similar values to those of torrefied and torrefied-washed series. This means that a clear connection cannot be established between the investigated pretreatments and the ash melting behavior of wheat-based samples.

Preliminary Characterization of OCs
The semi-quantitative elemental composition of the three OCs was measured by XRF (Table 3): the presence of many more elements than the main constituents was attributed to the production of OCs at the industrial scale, and the low content of nickel suggests that these OCs should not promote reforming reactions catalyzed by this element [66,67].  Table 4 summarizes the results from measurements of d p and ρ p of the fresh OCs. These values allowed the determination of generalized Geldart groups [34] to which the three OCs belong at the experimental conditions of pressure fluctuation acquisitions; with N 2 , at temperatures from 700 to 1000 • C, all fresh OCs belong to Group B (bubbling). Particles which belong to this Group cannot provide homogeneous fluidization, i.e., the minimum fluidization velocity coincides with the bubbling fluidization velocity. From here on, the term "minimum fluidization velocity (u mf )" is chosen to define the reference value at which bubbling fluidization begins for the three OCs.
The study of u mf provided the values in Table 4: a general good agreement between measured and calculated values occurred, and this confirmed the overall reliability of experimental u mf values. Those of SIB were systematically higher than their theoretical or semiempirical counterparts. This was attributed to the experimental transition from the fixed bed state to the full bubbling regime: compared to those of ILM and LD, the transition of SIB was found to be much broader. The experimental u mf values in Table 4 (u mf,exp ) were used as a reference to calculate the N 2 flow rates to be used in pressure fluctuation acquisitions for the three OCs.   (Figure 7a). In addition, the surface of LD particles appeared dusty in pictures with higher magnifications (Figure 8b-d).   (Table 4). SEM-EDS of fresh ILM found particles made of Fe and Ti, the main constituents of this OC, accompanied by other particles mainly made up of Si, Mg, and Al, also with Ca, Al, Mg, and Na (the analyzed particles are in Figure  6a). SEM-EDS of fresh SIB (Figure 7c Figure 9 shows the effects of temperature increase on the quality of bubbling fluidization, in the bed made of ILM and ash from WSP at u = 2u mf . This picture serves as an example of the different kinds of pressure fluctuation signals, and related PSDFs, found in this experimental campaign; moreover, it evidences the target phenomenon which the experimental method proposed in this work aims to observe, i.e., changes in fluidization quality.

Results of Pressure Fluctuations Acquisitions
A signal like the one in Figure 9a (T = 750 • C) corresponds to a fully bubbling bed and the related PSDF in Figure 9b shows a range of dominant frequencies typical of bubbling fluidization (order of magnitude 10 0 -10 1 Hz [68,69]).   Figure 9 shows the effects of temperature increase on the quality of bubbling fluidization, in the bed made of ILM and ash from WSP at u = 2umf. This picture serves as an example of the different kinds of pressure fluctuation signals, and related PSDFs, found in this experimental campaign; moreover, it evidences the target phenomenon which the experimental method proposed in this work aims to observe, i.e., changes in fluidization quality.

Results of Pressure Fluctuations Acquisitions
A signal like the one in Figure 9a (T = 750 °C) corresponds to a fully bubbling bed and the related PSDF in Figure 9b shows a range of dominant frequencies typical of bubbling fluidization (order of magnitude 10 0 -10 1 Hz [68,69]). Figure 9c,d (T = 850 °C) have the same features of Figure 9a, b respectively, but they have lower standard deviation and PSDF values at around 10 Hz: this reveals a decrease in the bubbles size.  Figures 10-12 graphically summarize these kind of evaluations, performed for the three OCs coupled with all ashes from studied biomasses, at 2umf and 3umf. Figure 10 reports evaluations based on PSDF shape and dominant frequency, in agreement with the just discussed exemplification in Figure 9. Figures 11 and 12 show the experimental values of normalized standard deviations, as functions of temperature. The combined observation of acquired signals and related analyses (standard deviations and PSDF) allowed the determination of a threshold value of the normalized standard deviation, which equals 2.2 × 10 −3 : signals with normalized standard deviations higher than this threshold generally correspond to bubbling fluidized beds (Figure 9a-d). Noticeably, the same normalized value was found for all the OC-ashes combinations. Figures 11 and 12 compare the experimental normalized standard deviations with this threshold.
As regards ILM at u = 2umf, WSP-T1, WSP-T2, and WSP-T3 performed better than RPR: their PSDFs showed the features of bubbling beds until 950 °C, while RPR resisted until 900 °C ( Figure  10a). The corresponding normalized standard deviations were similar to or higher than those of RPR, in the whole explored temperature range (Figure 11a, b). At u = 2umf with ILM, WSP behaved worse than RPR for temperatures above 750 °C (Figure 11a,b). At nominal u = 3umf, only data of washed biomass samples were available on the whole temperature range (Figure 10b and Figure  12a). They generally resulted in trends of acceptable bubbling fluidization quality (Figure 12a,b, normalized standard deviation > 2.2 × 10 −3 ), with dominant frequencies in the range 5-10 Hz. This is a good process indication, since it suggests that an increase in superficial velocity can re-fluidize a bed with poorer fluidization quality at lower flow rates (compare Figure 11a,b with Figure 12a,b). With regard to torrefied samples, at u = 3umf, only WSP-T1 did not allow a bubbling fluidization at 1000 °C (Figure 12a,b), as well as WSP. Figures 10-12 graphically summarize these kind of evaluations, performed for the three OCs coupled with all ashes from studied biomasses, at 2u mf and 3u mf . Figure 10 reports evaluations based on PSDF shape and dominant frequency, in agreement with the just discussed exemplification in Figure 9. Figures 11 and 12 show the experimental values of normalized standard deviations, as functions of temperature. The combined observation of acquired signals and related analyses (standard deviations and PSDF) allowed the determination of a threshold value of the normalized standard deviation, which equals 2.2 × 10 −3 : signals with normalized standard deviations higher than this threshold generally correspond to bubbling fluidized beds (Figure 9a-d). Noticeably, the same normalized value was found for all the OC-ashes combinations. Figures 11 and 12 compare the experimental normalized standard deviations with this threshold.
As regards ILM at u = 2u mf , WSP-T1, WSP-T2, and WSP-T3 performed better than RPR: their PSDFs showed the features of bubbling beds until 950 • C, while RPR resisted until 900 • C (Figure 10a). The corresponding normalized standard deviations were similar to or higher than those of RPR, in the whole explored temperature range (Figure 11a, b). At u = 2u mf with ILM, WSP behaved worse than RPR for temperatures above 750 • C (Figure 11a,b). At nominal u = 3u mf , only data of washed biomass samples were available on the whole temperature range (Figures 10b and 12a). They generally resulted in trends of acceptable bubbling fluidization quality (Figure 12a,b, normalized standard deviation > 2.2 × 10 −3 ), with dominant frequencies in the range 5-10 Hz. This is a good process indication, since it suggests that an increase in superficial velocity can re-fluidize a bed with poorer fluidization quality at lower flow rates (compare Figure 11a,b with Figure 12a,b). With regard to torrefied samples, at u = 3u mf , only WSP-T1 did not allow a bubbling fluidization at 1000 • C (Figure 12a,b), as well as WSP.  Figure 10. Evaluation of fluidization quality based on the experimental PSDFs. Legend: green square = bubbling bed (corresponding to the situation described by Figure 9a-d), yellow square = bubbling fluidization fading out (corresponding to the situation described by Figure 9e,f), red square = no bubbling (corresponding to the situation described by Figure 9g,h), and white = not acquired.    As for SIB at u = 2u mf , all SIB-ash couples had a good fluidization quality until 850 • C, except WSP-T2W (Figures 10c and 11c,d). Most of the SIB-ash couples underwent a worsening of bubbling fluidization quality in the range 850-950 • C (Figures 10c and 11d): this behavior is more likely ascribable to intrinsic properties of this OC, seeing that it occurred with many different ashes. WSP-T3W and RPR ashes, on the contrary, ensured an acceptable quality of bubbling fluidization with SIB up to 950 • C (Figure 10c), respectively equal to and higher than the temperature limits reached with ILM. The differences due to ashes disappeared at u = 3u mf , since all SIB-ash couples performed with a good fluidization quality (Figure 10d), with normalized standard deviations sufficiently higher than the 2.2 × 10 −3 threshold (Figure 12c,d); at this condition, the best performance belonged to SIB with WSP-T3.
Regarding LD at u = 2u mf , a general difficulty in obtaining full bubbling fluidization emerged from experiments with all ashes (Figures 10e and 11e,f). At u = 3u mf , an overall improvement occurred (Figure 10f), even though the intensities of bubbling fluidization were significantly lower than those of other OCs (Figure 12e,f); in other words, LD developed smaller bubbles than other OCs, all other conditions being equal. With WSP-T1W and WSP-T2W, LD kept dominant frequencies in the representative range of bubbling fluidization from 700 to 1000 • C (Figure 10f), but the associated normalized standard deviations of WSP-T2W became very close to 2.2 × 10 −3 at 950 and 1000 • C (Figure 12f). LD behaved quite differently from the other OCs, hindering a clear classification, under the normalized standard deviation, of bubbling or non-bubbling beds. The correct diagnosis had to be obtained from a combined observation of normalized standard deviation and PSDF dominant frequency.    Figure 14. SEM micrographs of SIB after fluidization steps: with WSP ash after the step at 700 °C at 80× (a) and 1000× (b), with WSP ash after the step at 1000 °C at 80× (c) and 350× (d), with WSP-T3 ash after the step at 700 °C at 80× (e) and 350× (f), and with WSP-T3 ash after the step at 1000 °C at 80× (g) and 1000× (h). Figure 14. SEM micrographs of SIB after fluidization steps: with WSP ash after the step at 700 • C at 80× (a) and 1000× (b), with WSP ash after the step at 1000 • C at 80× (c) and 350× (d), with WSP-T3 ash after the step at 700 • C at 80× (e) and 350× (f), and with WSP-T3 ash after the step at 1000 • C at 80× (g) and 1000× (h).  Figure 15. SEM micrographs of LD after fluidization steps: with WSP ash after the step at 700 °C at 80× (a) and 3000× (b), with WSP ash after the step at 1000 °C at 80× (c) and 1000× (d), with WSP-T3 ash after the step at 700 °C at 80× (e) and 3000× (f), and with WSP-T3 ash after the step at 1000 °C at 80× (g) and 350× (h). Figure 15. SEM micrographs of LD after fluidization steps: with WSP ash after the step at 700 • C at 80× (a) and 3000× (b), with WSP ash after the step at 1000 • C at 80× (c) and 1000× (d), with WSP-T3 ash after the step at 700 • C at 80× (e) and 3000× (f), and with WSP-T3 ash after the step at 1000 • C at 80× (g) and 350× (h).

Characterization of Samples after Tests
After the 1000 • C fluidization step with WSP ash (Figure 13a), ILM underwent agglomeration around its particles made up of Si, Mg, and Al (see Section 3.2), as evidenced in Figure 13b: the EDS of this agglomerate found that the central darker particle is none other than an ILM particle based on Si, sealed with the upper plaquette and the lighter grain on the right side, which both contain Fe, Ti, Si, Mg, Ca, and K. The presence of K suggests that agglomeration might be due to interactions between ILM and the WSP ash. After the 1000 • C fluidization step with WSP-T3 ash, the original ILM seems to have undergone fragmentation, followed by conglomeration of the fines which had just formed (compare Figure 6a with Figure 13c): the EDS of these agglomerates (an example in Figure 13d) revealed that the granular bridges which keep them together mainly contain Ni, S, and Al, but not Ti. In the light of these findings, the formation of these agglomerates was not related to direct interactions between ILM and ash, but rather to the stainless-steel pressure probe in use during the test. Only that probe could have brought an important amount of Ni in the system; actually, after that test, the pressure probe was slightly corroded only in the part submerged in the ILM bed, empirically confirming that it released the Ni of the agglomerates, thus promoting their formation. This is a remarkable piece of information, so as to choose proper materials at the industrial scale, able to prevent harmful chemical interactions with OC beds. Consequently, after these tests (the fourth out of twenty-four), the steel pressure probe was substituted with a quartz one for the rest of the experimental campaign. Figure 14 shows samples of SIB mixed with WSP or WSP-T3 ashes, after fluidization steps at 700 and 1000 • C. With WSP ash at 700 • C, agglomeration did not occur (Figure 14a), but a new layer appeared on the OC particles ( Figure 14b). This layer mainly contains Na and S, with traces of Ca and K, as determined by EDS. It was associated to the presence of WSP ashes, seeing that it is made up of trace elements typical of living matter (e.g., S in Table 2). With WSP ashes at 1000 • C, agglomeration of smaller SIB particles of about 100 µm occurred frequently (Figure 14c), thanks to the formation of smooth bridges (Figure 14d). EDS of those bridges found Si and K, very often accompanied by Pb, Cu, and Na. With WSP-T3 ashes at 700 • C (Figure 14e,f), SIB particles seem quite similar to their fresh version (Figure 7). At 1000 • C (Figure 14g,h), a lower occurrence of agglomeration was noted for WSP-T3, in comparison to the SIB-WSP couple (Figure 14c,d), due to Si-K-Pb-Cu-Na bridges also in this case. Figure 15 shows LD micrographs of samples after fluidization at 700 and 1000 • C with WSP or WSP-T3. In all cases, LD particles did not agglomerate as ILM and SIB did, but other peculiar phenomena emerged: (i) LD particles resulted as more cracked than their fresh counterpart (Figure 8), (ii) fragmentation of LD particles occurred, forming fines with diameters lower than 100 µm, and (iii) on LD particles, a very thin layer (1-2 µm) with a melted aspect formed, made up of Na, P, and S (trace elements ascribable to biogenic substances, as ashes). In this last regard, Figure 15b,f located this layer, while Figure 15h shows a shell of this kind, detached from an LD particle. Figure 16a shows the average diameters of the three fresh OCs, compared with those of some samples after the fluidization tests at 1000 • C. Treatments in bubbling fluidized bed, up to 1000 • C with ashes, engendered different kinds of modifications of the OC bed particles. Ashes from WSP caused the highest variations of OC average diameters (+14% for ILM, +25% for SIB, −42% for LD). All pretreated wheat straw pellets produced smaller variations than WSP (see data in Figure 16a): in the ranges from −3% to +7% for ILM, from +8% to +21% for SIB (always increasing), and from −8% to −34% for LD (always decreasing).
As far as LD is considered, all after-test samples underwent a quantitatively important decrease of particle sizes: the particle size distributions shifted towards smaller values, and a new secondary bell appeared between 10 and 100 µm, absent in the fresh LD.
As far as LD is considered, all after-test samples underwent a quantitatively important decrease of particle sizes: the particle size distributions shifted towards smaller values, and a new secondary bell appeared between 10 and 100 μm, absent in the fresh LD.

Discussion
With regard to the chemical consequences of pretreatments on WSP, clear effects were detected as regards N, S, and Cl ( Table 2). The same was observed as for the leachability of K and P, which is slightly decreased as the torrefaction degree is increased (Figure 4). On the other hand, similar values of IDT and SOT were obtained when comparing wheat straw ashes with torrefied and torrefied-washed series ( Figure 5).
Pressure fluctuation tests highlighted some peculiarities as for each OC, independently from the ash with which they were coupled, e.g., the agglomerative effect of trace elements (Pb and Cu) in SIB or the tendency to fragment of LD particles. This feature of LD requires it to be evaluated separately, while SIB and ILM can be more easily compared one to another.
The ratings of pressure fluctuations signals allowed an assessment of influences from ashes on OCs in fluidized beds. WSP behaved worse than RPR at 2u mf (the lowest fluidization velocity) with both ILM and SIB (Figure 10a,c). With regard to ILM (Figure 10a), the pretreatments on WSP improved the bubbling bed performances in comparison with RPR ones. An analogous trend is not so evident for SIB ( Figure 10c); therefore, the alterations in its fluidization quality, as temperature was increased, were correlated with intrinsic features of this OC. On the other hand, at 3u mf , ILM with torrefied and torrefied-washed samples (Figure 10b) ensured a fluidization in the bubbling regime in the whole explored temperature range (700-1000 • C), and SIB did the same with all ashes (Figure 10d). This confirms the usefulness of the wheat straw pretreatments purposely developed in this work. It is worth to stress here that tests on ILM with ashes from WSP, RPR, WSP-T1, and WSP-T3 were affected by the presence of the stainless-steel pressure probe. Nevertheless, the couple ILM/WSP-T3 at 1000 • C and 3u mf was in full bubbling fluidization regime.
The increase of superficial gas velocity from 2u mf to 3u mf (Figure 10a-d) generally improved the bubbling fluidization quality in both ILM and SIB beds. This indicates that ILM and SIB can be employed in CLG with pretreated or untreated biogenic residues, since this process uses gas flow rates so high to cause bed circulation. Nonetheless, it is crucial to avoid severe sintering/agglomeration phenomena, in order to ensure the smooth operation of the whole CLG plant, especially in its parts which work at the highest temperature and the lowest gas velocities. For ILM and SIB, SEM micrographs allowed observing that the agglomeration mainly involved fine particles, which probably formed because of attrition during fluidization tests. The dimensions of produced agglomerates were comparable to those of fresh OCs particles, even in the worst case of untreated WSP. The inferences from pressure fluctuation analyses, summarized just above for ILM and SIB, found confirmation in the characterization of after-test samples: ILM with ashes from pretreated wheat straw had more limited variations of average diameters, when compared to the ILM-WSP couple (Figure 16a). SIB showed an increase of average diameter for all analyzed after-test samples (Figure 16a). SEM-EDS highlighted the significant agglomeration tendency of SIB ( Figure 7) and connected it to the combined presence of Pb and Cu and low-melting elements (Si, K, Ca, Na). Pb and Cu seem to be unexpected originators of agglomeration, as they are neither main components of biogenic residues nor of the investigated OC. However, XRF helped to explain the SEM-EDS results: traces of Pb and Cu in SIB are higher than those in ILM and LD, by two orders of magnitude for Pb, and by at least one order of magnitude for Cu (Table 3). SEM-EDS analyses only found the smooth sealing bridges based on Pb-Cu in those SIB samples which underwent the fluidizations at 1000 • C ( Figure 14). No Pb or Cu were detected by SEM-EDS in SIB samples in fresh state or after fluidizations at 700 • C. This suggests that the traces of Pb and Cu-already present in the fresh SIB solid bulk (see XRF in Table 3)-acquired the sufficient mobility to form the bridges only above a temperature threshold between 700 and 1000 • C. In addition to Pb and Cu, the bridges contain Si, K, Ca, and Na, thus the low melting elements-brought by ashes or already included in SIB (e.g., Si, K, Ca)-are also involved in this process.
A significant formation of fines during the fluidization of LD samples was found by measurements of particle size distributions ( Figure 16b) and SEM-EDS analyses ( Figure 15). It can explain the ambiguous fluid-dynamic behavior of LD (Figure 10e,f, Figure 11e,f, and Figure 12e,f): the decrease of average particle size makes the bed inventory of LD and ashes straddle Groups A (homogeneous fluidization) and B (bubbling) of generalized Geldart map [34].
In most of the OC-ash couples, a non-linear, decreasing trend was observed for standard deviations as the temperature is increased (Figure 11a,c,e and Figure 12a,c,e). According to the "two-phase theory" for bubbling beds, the formation of bubbles is related to the excess surface gas velocity (u -u mf ) [61,70]: this quantity, for our case of study, has quasi-linear decreasing trends as the temperature is increased between 700 and 1000 • C (calculation based on Table 4), thus the influence of experimental temperature on the performances of OC-ash beds cannot be uniquely associated to the lower absolute values of u at higher temperatures. Rapagnà et al. [71] found that the standard deviation of the pressure fluctuations in the bubbling regime is not appreciably affected by temperature in the case of a moderate-size particle system, whereas with small particles (≤100 µm), its value reduces noticeably as the temperature is increased from ambient to 850 • C, over a wide range of gas velocities. This last consideration matches with the observed behavior of LD (Figure 11e,f and Figure 12e,f), and the detection of significant fragmentation by SEM ( Figure 15) and variations of particle size distributions by Malvern Mastersizer 2000 (Figure 16b).
Remarkably, for all the OCs, a unique threshold value of the normalized standard deviation was found (2.2 × 10 −3 ), which discriminates between bubbling and non-bubbling beds. This represents a considerable corroboration of the approach used in this work to analyze data from the fluidization tests, since it was applied without the need of specific adaptations for the investigated bed material.
Overall, none of the ashes showed a definitively better behavior than the others, meaning that the quality of bubbling fluidization greatly depends on the couple OC-biomass (Figures 10-12). Therefore, the choices of solid fuel feedstock and fluidized bed material are mutually influenced and, in turn, are affected by the specific operating conditions of the chemical conversion to be performed. When considering industrial-scale processes, as the CLG hypothesized in the CLARA project, an important operating condition to be carefully evaluated is the accumulation of biomass ashes in the circulating bed, i.e., the ash to OC ratio. This factor could increase the occurrence of agglomeration phenomena, incipiently observed in this work with a constant bulk volume ratio between ash and OCs.
An additional remarkable issue at industrial scale is the choice of equipment and reactor materials, as evidenced by bad interactions intervened between ILM and the stainless-steel pressure probe in the first fluidization experiments.

Conclusions
Pretreatments of wheat straw biomass, based on torrefaction and washing, were developed and validated for CLG applications, in the framework of the European research project CLARA. Torrefaction was effective for removing Cl. This allows torrefaction to be considered as a de-chlorinating process, which prevents the formation of related pollutants and the accelerated corrosion in thermochemical processes. The washing pretreatment, carried out on torrefied wheat straw pellets, removed 30-40% of S, 60-70% of K, and 40-50% of P, with potential beneficial effects in limiting agglomeration phenomena, as far as their use in fluidized bed is concerned. The leachability of K and P is slightly decreased as the torrefaction degree is increased.
The study of standard deviations and dominant frequencies from pressure fluctuation signals turned out to be a suitable tool to detect incipient modifications of the bubbling fluidization regime. The case of study of OCs, mixed with ashes from different biogenic residues for CLG, evidenced that this method can promptly detect the fading of bubbling fluidization, due to particles agglomeration or important particle fragmentation. This was confirmed by cross-checking the evaluations from fluidization tests and the results from the characterization of after-tests samples. Moreover, the evaluations of pressure fluctuation signals were uniquely carried out on the basis of general fluid-dynamic considerations. Therefore, the analysis method proposed in this work, founded on the study of standard deviation and PSDF, is a tool with a good potential for the "online" monitoring of bubbling fluidization quality at the industrial scale. In addition, this method can be used at the laboratory scale to perform the screening of solid feedstock and bed particles, in order to choose in advance those materials which can prevent the scaled-up reactor from de-fluidization.
As far as wheat straw pretreatments are concerned (torrefaction and torrefaction-washing), their effectiveness in preventing agglomeration also depends on the nature of the OC. In several cases, the fluidization quality of a given OC was better with ashes from pretreated wheat straw pellets than with ashes from raw wheat straw and pine forest residues. The most evident improvements, in comparison with raw wheat straw, were generally obtained by torrefaction, while the washing seemed less determinant. As regards the torrefaction degree, no clear dependencies can be inferred. Generally, pretreatments of wheat straw seem desirable to improve the biomass-to-fuel chain by CLG hypothesized in the CLARA research project.
With regard to materials choices for CLG of biomasses, it is worth mentioning that the investigated OCs contain Si, Ca, Al, and K, which can give place to low-melting systems; therefore, they can mitigate