3.1. Rheological Behaviors
Pumping and transporting are crucial processes prior to gasification or combustion. The rheological behaviors of slurry fuels with different coal concentrations were measured. Due to the very high apparent viscosity of coal BFT slurry that cannot be measured at room temperature,
Figure 3 only presents the evolution of rheological characteristics of the other bioslurries with different concentrations, and
Figure 4a presents the rheological behavior of coal BFT slurry at an elevated temperature of 70 °C. All of the slurry fuels exhibit apparent shear-thinning characteristics below 50 s
−1, which is consistent with other slurries. This is attributed to the breakdown of the gel structure of the mixture [
6]. The apparent viscosity tends to be stable as the shear rate reaches 100 s
−1. It is also remarkable that the increase in solid concentration of slurry contributes to the increase of apparent viscosity. With similar viscosity (around 850 mPa·s) and at a shear rate of 100 s
−1, the coal loading of coal BSR slurry is 34%, while it is 48% for coal BPA slurry. This indicates that in industrial applications, coal BPA may carry more coal to form slurry fuels and the heating values are more likely to be higher.
Figure 4a shows the rheological behavior of coal BFT slurry with 10% coal concentration. Although the concentration of coal BFT slurry is significantly lower than the other two slurries, its apparent viscosity reaches 2589 mPa·s, far exceeding the viscosity of the other two slurries with 36% coal concentration at room temperature. This shows that during BFT slurry preparation, the amount of coal added is extremely limited, and the viscosity is high even at 70 °C, which is not suitable for preparing slurry fuels.
The Herschel–Bulkley model was used to fit the rheological model of coal bio-oil slurry shown in
Figure 4b, and the fitting parameters are shown in
Table 2.
where
τ is shear stress,
τ0 is yield stress,
k is consistency factor,
γ is shear rate, and
n is flow index.
The rheological curve fitting coefficient R2 of slurries is close to 1, which confirms that the Herschel-Bulkley model may describe the coal bio-oil slurries. The flow characteristic index n is less than 1, which implies that the slurry fuels exhibit a yield of pseudoplastic fluid. The K value of coal BPA slurry is larger than that of coal BSR slurry and coal BFT slurry, and the n value is smaller than that of other slurries, indicating that coal BPA slurry is the most pseudoplastic. In industrial applications, slurry fuels are expected to have a higher solid content and heating value, but at the same time, this also brings about an increase in viscosity. Therefore, efforts were then taken to carry out further work for reduction in viscosity.
Coal bio-oil slurries are thermodynamically unstable systems, which are significantly affected by temperature. The aforementioned coal BFT slurry with an excessively high viscosity that could not be measured at room temperature decreased to 2589 mPa·s when the temperature was increased to 70 °C. The temperature–viscosity relation was shown in
Figure 5a. The apparent viscosity of all slurries decreases as the temperature increases. Coal BPA slurry is more sensitive to temperature, and its apparent viscosity decreased from 725 mPa·s at 25 °C to 249 mPa·s at 60 °C. It has been reported that the increase in temperature will cause the viscosity of the liquid phase bio-oil to decrease significantly. The viscosity change of the coal bio-oil slurry has a good correlation with the change of the viscosity of bio-oil, which is the main factor that causes the reduction in viscosity [
4]. Furthermore, the difference in the thermal expansion characteristics of the liquid and solid phases leads to an increase in the volume share of free water; that is, the expansion rate of the liquid phase is higher than that of the solid phase under the heating state, resulting in a decrease in the viscosity of coal slurry. Scholars [
19,
20,
21] found that the influence of temperature on the apparent viscosity of coal-water slurries can be fitted with the Arrhenius equation as shown in Equation (2). The equation was also applied for coal bio-oil slurries, and the results were shown in
Figure 5b. It can be seen that the Arrhenius equation fits well with all slurries, which indicates that the influence of temperature on the apparent viscosity of the coal bio-oil slurries could also be described by the Arrhenius equation.
where
µ represents apparent viscosity,
C1 and
C2 are constant, and
T represents temperature, K.
3.2. Gasification of Slurry Fuels
The process of gasification in a thermobalance is widely used in gasification and reaction kinetics studies [
22,
23,
24]. The TG and DTG (Derivative Thermogravimetric) curves of CO
2 gasification of bio-oils a presented in
Figure 6. After gasification, residual char was also seen in
Figure 6a, which shows higher yield for BFT and lower yields for BSR and BPA as observed. This is related to the ash content of the bio-oils. BFT is the most viscous and has more ash and heavy organic matters than the others; thus its residual char yield is higher. The weight loss process of individual bio-oil took place in three stages, namely the volatile removing stage, CO
2-pyrolysis, and gasification stages. The temperature range and weight loss of these three stages may vary for the compositions of fuels. Moreover, the reactions that occurred in each stage may cross each other, which blurs the boundaries of stages. For BSR and BPA, the light volatile removing stage (referred to as stage 1) occurred at a temperature around 100 °C, which is mainly devolatilization (evaporation of H
2O and small organic matter), decomposition, and char formation gradually at the end of this stage. It was then followed by the pyrolysis stage (referred to as stage 2) which occurs below 600 °C [
2,
25,
26,
27]. For BFT, as seen in
Figure 6b, the first two stages were joined as it shows three continuous weight losses between 100 °C to 600 °C. The pyrolysis of heaver components in BFT is likely to occur in this range. The last stage (referred to as stage 3) took place above 600 °C, and the carbon in bio-oils and newly formed char reacted with CO
2 introduced in the furnace. The TG curves of individual bio-oils indicate that BFT had higher mass loss compared to the other bio-oils owing to its higher carbon content and higher content of heavy organic matter. Since the carbon content of BPA is relatively low, the carbon gasification in the third stage was neglectable.
Lignite was added into bio-oils for preparation of bioslurries, and the TG and DTG curves of lignite are shown in
Figure 7. The three stages of CO
2 gasification of lignite are also seen in
Figure 7b. The first stage also concentrates at 100 °C, representing the moisture removal of lignite. The second stage ranges from 200 °C to 700 °C, where the pyrolysis of lignite occurs. The last stage (700–1020 °C) is the CO
2 gasification, where the char was gasified.
The gasification reactivity of fuels was quantitatively evaluated by gasification performance indices, which can be obtained from the TG and DTG curves, such as the final weight loss temperature (T
f) and temperature at which the maximum weight loss rate in each stage (T
m1, T
m2, T
m3 for stages 1 to 3, respectively) [
28]. Among the T
ms, T
m3 represents the peak temperature at the maximum weight loss rate in CO
2 gasification and needs special attention in comparison.
Gasification performance indices of individual fuels were shown in
Table 3. There is no obvious gasification stage for BPA, and its T
m3 and T
f are not listed. T
m1 for the bio-oils is higher than for lignite. In the first stage of gasification, moisture and gases are removed from lignite, while in bio-oils, both water and other organic molecules volatilized and cause a wider and delayed peak temperature in this stage. The advances in gasification of bio-oils over lignite were concentrated in the gasification stage, as they give lower T
m3 and T
f. This indicates that carbon in bio-oil is more reactive than lignite, and by mixing bio-oils and lignite, the gasification may improve, which is investigated in the next section.
The biofuels were prepared by mixing lignite with individual bio-oil, and their TG and DTG curves are shown in
Figure 8. They show comprehensive characteristics with lignite and bio-oils. Similarly, the gasification of biofuels could also be divided into three stages. Compared with BFT, the peak temperatures of lignite BFT slurry in three stages were delayed by 20 °C or even longer. This indicates that the coal particles in BFT to some extent inhibit the gasification of liquids. T
f was also delayed for 20 to 60 °C. This phenomenon could also be proved by comparing the T
m3 of BSR, BPA, and the slurries prepared by them.
The characterization of temperature during gasification of biofuels is shown in
Table 4. The biofuels have T
m3s ranging from 895 °C to 959 °C, which implies that the addition of bio-oil has different effects on lignite gasification. Compared with lignite, T
m3 of lignite BFT slurry was delayed for 60 °C, and T
m3 of lignite BSR slurry and lignite BPA slurry remain almost the same. However, T
fs of all bio slurries move in advance. This implies that the gasification was compressed in a shorter range of temperature and that the gasification does not require temperatures as high as for lignite.
3.3. Thermaodynamic Analysis
The kinetics of gasification is known to be complicated since gasification of coal, bio-oil, and biofuels is a heterogeneous action. In the present research, activation energy (
E) is estimated by a non-isothermal single heating rate method. DTG data under this circumstance could be used to calculate kinetic parameters by the Coats–Redfern method. The kinetics of reaction is described by Equation (3):
in which
T is the sample temperature, K;
α is the extent of conversion, %;
f(
α) is the hypothetical model of the reaction mechanism;
A is the frequency factor;
E is the apparent activation energy, kJ·mol
−1;
R is the gas constant and equals 8.314 J·mol
−1·K
−1; and
t is time, s.
Based on TG curves,
α can be described by Equation (4):
in which
W0 is the initial weight of sample,
W is the weight at time
t, and
Wf is the residual mass after gasification.
As the heating rate
is constant during gasification, Equation (1) can be expressed as Equation (5):
Normally, it is assumed that the main gasification process can be described by first-order kinetics. Thus,
f(
α) is substituted by (1 −
α). The equation derived for calculating activation energy is given as Equation (6):
where
E and
A can be calculated from the slope and intercept of a plot of
against
.
The fitting curves of Arrhenius diagram of fuels for calculating
E and
A were shown in
Figure 9, and the estimated results were shown in
Table 5. The fitting curves of lignite BSR slurry, lignite BFT slurry, and lignite BPA slurry lay on both sides of the lignite gasification curve, which indicates that the three bio-oils have different effects on gasification of biofuels.
A noticeable decrease in
E occurred in lignite BSR slurry and lignite BPA slurry compared to lignite; in particular, for lignite BSR slurry, the activation energy is reduced by 15.98 KJ/mol. This means the co-gasification of lignite and BSR or BPA needs less energy than lignite with lower
E, which is inconsistent with lower T
f of these slurries than lignite showing synergetic effects. During the heating process, due to the addition of liquid, micro-explosions may occur in the slurry fuel droplets, resulting in an increase in the reaction area and reaction rate. There is also literature that shows that alkali metals and alkaline earth metals have a catalytic role in the gasification process, which can increase the reaction rate of carbon.
Lignite BFT slurry lies on the opposite side and has higher E than lignite and other slurries. This is also proven by lignite BFT slurry having delayed Tm3 compared to lignite. This seems to contradict the conclusions of the two previous slurries, because lignite BFT slurry may also contain alkali metals and microburst during high-temperature processes. However, in this case, the differences between the three bio-oils must be considered. Compared with BPA and BSR, BFT has lower water content, higher viscosity, higher density, and more heavy components. During the early heating process, the heavy components are less volatilized and surround the coal particle surface more. The droplets formed are larger and denser, which hinders the heat and mass transfer of coal particles in high-temperature regions, which in turn causes the higher gasification reaction temperature.