Gasification Reaction Characteristics between Biochar and C[O.sub.2] as well as the Influence on Sintering Process.
The energy consumption of the iron ore sintering process generally accounts for about 10% of iron and steel enterprises, 75%~80% of which are consumed in the form of solid fossil fuels like coke breeze or anthracite [1, 2]. Fuel cost accounts for 40% or more of the sinter processing costs . Also, previous research found that the combustion of solid fossil fuels served as the main source of C[O.sub.2], SOx, NOx, and so on in this process [4, 5]. To address these problems, substituting extensively distributed, renewable, and clean biochar for fossil fuels in sintering process was believed to be a promising strategy to reduce the emissions of C[O.sub.2], SOx, NOx, and so on [6-10].
CSIRO in Australia conducted a study on the application of charcoal in iron ore sintering process. The results showed that the ash content of charcoal produced by red eucalyptus was low and the residual impurities were few after burning. When applied to sintering process, the biochar could replace part of the coke breeze but reduced the strength of the sinter product. In particular, the tumble strength was reduced significantly when biochar dosage was high [11, 12]. The British and Dutch scholars of the Corus Technology and Development Research Center jointly conducted a series of sintering tests which used the sunflower seed shells to replace part of the coke breeze. The results showed that it was feasible to use sunflower seed shell to replace 10% coke breeze in iron ore sintering. The sintering characteristics were similar to the ones when using coke breeze only, while the sintering time shortened and the productivity was improved by 6.4%. However, when the substitution ratio was 20% or higher, the sintering production and quality indicators deteriorated seriously [13, 14]. Brazil research institutions used biochar powder with grain size of 5-10 mm to replace 6% and 12% coke breeze for sintering production, finding that sinter products with the large specific surface area and good metallurgical performance were obtained, and the products could meet the requirements of blast furnace although the tumble strength reduced . Liming LU from CSIRO found that, compared with the sinter fired with coke breeze, the sinter from the mixtures with <50% coke powder replaced by charcoal was marginally weaker in terms of sinter yield, tumble strength, and reduction disintegration [16, 17]. Our group also did a lot of work on the influences of biochar replacing coke breeze on sintering process. The research showed that it could reduce emissions of NOx, SOx, and so on when applying the carbonized products of straw, trees, and molded-sawdust [18-21].
There were lots of differences between biochar and conventional fuels in terms of chemical composition, physical properties, proximate analysis, and so on. Biochar replacing coke breeze would bring a series of changes to the behavior of the fuel in sintering process. Therefore, in this paper the differences between biochar and coke breeze in reactivity were studied, as well as the kinetic characteristics of biochar reacting with C[O.sub.2]. In addition, the mechanism how biochar replacing coke breeze affected the yield and quality of sinter was revealed by researching the influences of biochar on combustion efficiency.
2. Materials and Methods
2.1. Raw Materials. Iron ore blend, solid fuels, fluxes (dolomite, limestone, and quicklime), and return fines were utilized to produce sinter. The chemical compositions of raw materials are shown in Table 1. Several kinds of iron ores were blended to satisfy the requirement of sinter compositions, with TFe (total iron content) of 57.5%, Si[O.sub.2] of 4.8% in sinter. Fluxes had the conventional compositions, and their percentages in mixture were calculated to meet basicity (CaO/Si[O.sub.2]) of 2.0 and MgO of 2.0%.
Two types of solid fuels were applied in the experiments. Onewascokebreeze, whichcamefromanindustrialsintering plant, and the other was biochar carbonized from acutissima at 700[degrees]C for 30 min in nitrogen gas. Ultimate and proximate analyses of fuels are illustrated in Table 2. The chemical compositions of ash in fuels are shown in Figure 1. It can be seen that biochar had lower N and S contents, which was advantageous to reduce the generation of SOx and NOx. Compared with coke breeze, biochar was lower in ash content, but higher in fixed carbon, volatile, and calorific value.
With the help of optical microscope, microstructures of coke breeze and biochar were obtained, as shown in Figure 2. Apparently, more microspores were distributed uniformly inside biochar and the majority of which were microscope. Porosity of biochar and coke breeze was measured by optical microscope, while specific surface areas were tested by Quantachrome Quadra Win. The biochar used in this paper was without activation, so nitrogen was used as adsorbate and BET method was used to calculate specific surface area. The porosity of biochar was 58.22%, which was higher than that of the coke breeze by 12.47%. The specific surface area of biochar was 54.76 [m.sup.2]/g, which was 9.13 times bigger than that of coke breeze.
2.2.1. Methods to Research Gasification Reaction Behavior. The reactivity of biochar under the nonisothermal condition was studied using the synchronous heat analyzer (NETZSCH STA 449C, German). 5.0 mg sample was put in the [Al.sub.2][O.sub.3] crucible of the thermobalance stent and heated by controlled computer process. The gas flow velocity was controlled, 0.5 m/s, and the speed of temperature increasing was 15[degrees]C/min. The TG-DTG curve and DSC curve of gasification reaction between the biochar and C[O.sub.2] were analyzed to obtain the characteristic parameters of gasification reaction, including reactions starting temperature (Ts), the end temperature (Te), the maximum weight loss rate (Vmax), and the maximum heat release (Qmax).
The reactivity of the biochar under isothermal conditions was studied in a vertical furnace. Using a fused silica tube with 038 x 550 mm as reaction tank, there was a cup for placing sample, which charged by 25 g dried fuel with a size fraction of 3 mm. The weight was measured and recorded by electronic balance and computer, respectively, and the system read the data every 20 s. Before starting the test, nitrogen as protective gas with flow rate of 5 L/min was passed into the tube until the temperature reached the preset temperature again. Then, the reaction tank was weighed and the nitrogen gas was cut off. Then inlet C[O.sub.2] with the flow rate of 10 L/min until the weight loss reached a constant value. Thus the gasification reaction conversion rate ([x.sub.c]) and the instantaneous rate R at a certain time were calculated according to the weight loss value of each time. The formulas are as follows:
[x.sub.c] = (1 - m/[m.sub.0]) x 100%
R = 1 -/[m.sub.0] dm/dt, (1)
where [x.sub.c] is conversion rate, %; R is reaction rate, %/min; [m.sub.0] is initial mass, g; m is the mass of reaction of the time t, g; dm/dt is weight loss rate at reaction of the time t, g/min.
The rate of gasification reaction was evaluated using the instantaneous rate [R.sub.1/2] at a fuel conversion of 50%.
2.2.2. Sintering Trials. Sintering process was simulated in a sinter pot of 180 mm diameter x 700 mm deep. The procedure involved ore proportioning, blending, granulation, ignition, sintering, and cooling. Raw materials were granulated in a drum of 600 mm diameter x 1400 mm deep for 4 min and then charged into the sinter pot. A hearth layer approximately 20 mm thick was used to protect the grate from thermal erosion. After charging, the fuel in the surface layer was ignited at 1150 [+ or -] 50[degrees]C for 1 min by an ignition hood. The combustion front moved downwards with the support of a downdraught system with a negative pressure of 10 kpa. In the sintering process, a infrared analyzer was used to detect the CO and C[O.sub.2] contents in exhaust gas, and combustion efficiency of C[O.sub.2]/(CO + C[O.sub.2]) was calculated to assess the burning degree of fuels. After sinter cake discharging, dropping test (2 m x3 times), screening, and tumble strength were carried out to evaluate the physical strength of sinter. Yield was the proportion of product sinter which deducted the hearth layer material and the fines -5 mm. Productivity was defined as the weight of product sinter produced per area per time. The test of tumble strength was conducted in a drum of 01000 x 500 mm where 7.5 kg product sinter was tumbled for 200r, then tumbled sinter was screened at 6.3 mm, and the proportion of +6.3 mm was treated as tumble strength. Sintering speed was the ratio between the height of sintering bed and the total sintering time.
During the sinter pot tests, the mass of biochar was calculated on the basis of replacement percentage biochar replacing coke and the heat replacement ratio by
[m.sub.b] x [h.sub.b] x a = [m.sub.c] x [h.sub.c] x r, (2)
where [m.sub.b] is the mass of biochar, kg; [m.sub.c] is the mass of coke for the base case, kg; r is the percentage of biochar replacing coke, which means the reduction percentage of coke compared to the base case as biochar replacing coke; [h.sub.c] is the calorific value of coke, MJ x [kg.sup.-1]; [h.sub.b] is the calorific value of biochar, MJ * [kg.sup.-1]; a is the heat replacement ratio, which means that 1 kj heat released by biochar can replace the amount of heat released by coke; as a = 1, it means that the heat ofbiochar combustion was equivalent to that for the coke breeze substituted.
3. Results and Discussion
3.1. Thermochemical Behavior of Biochar
3.1.1. Gasification Characteristic Parameters. The TG-DSC curves of nonisothermal gasification of fuels are shown in Figure 3. Biochar heated in C[O.sub.2] atmosphere went through four stages, which were drying, warming up, volatiles desorption, and gasification reaction of carbon, respectively. Volatile began to separate out when the temperature reached a certain value, compared with coke breeze, the weight loss of biochar during which process was more obvious and the volatile weight loss ratio could normally reach more than 8%. After the desorption of volatile, it came to the gasification of fixed carbon, and the weight loss ratio of fuel sped up significantly. The DTG and DSC curves of biochar showed sharp peaks, indicating that the reaction was more intense compared with coke breeze.
The TG-DTG and DSC curves of fuels' gasification were analyzed to obtain the characteristic parameters. It showed that biochar started to gasify at low temperature, and the reaction starting temperature (Ts) and the end temperature (Te) were both lower than those of the coke breeze, while the maximum weight loss rate (Vmax) and maximum heat absorption value (Qmax) were both higher than those of the coke breeze. It manifested that biochar had a higher reactivity than coke breeze and easily reacted with C[O.sub.2] to generate CO.
3.1.2. Gasification Dynamics. The reaction rates of biochar and coke breeze with C[O.sub.2] were studied by isothermal thermogravimetric analysis and the conversion rates are shown in Figure 4. For comparing the gasification process between fuel and C[O.sub.2], the rate of gasification reaction was evaluated by the instantaneous speed ([R.sub.1/2]) when the conversion rate was 50%. It was known from Figure 3 that, at the same temperature, the gasification reaction rate of the biochar was 3.85%/min, which was faster than that of the coke breeze (0.57%/min) at 1050[degrees]C. With temperatures rising, gasification reaction speed of fuel got faster, which shortened the time during which fuel conversion rate reached 50%. When the temperature ranged from 950[degrees]C to 1100[degrees]C, the gasification reaction rate ([R.sub.1/2]) of biochar increased from 1.50%/min to 4.35%/min, and [t.sub.1/2] decreased from 34.33 min to 11.52 min.
In this paper, a typical shrinking core reaction model was used to study the gasification reaction kinetics of solid fuels. The reaction can be divided into three zones: chemical reaction kinetics zone, inner diffusion zone, and outer diffusion zone. In the chemical reaction kinetics zone, the controlling factor of the reaction rate is the chemical reaction of coke and C[O.sub.2]. In the outer diffusion zone, the controlling factor is the effect of C[O.sub.2] diffusing to coke surface, while the internal diffusion zone is affected by both chemical reaction and diffusion. Tseng and Edgar  analyzed the different reaction zones of coke. In the chemical reaction kinetics zone, the kinetic constant of coke gasification reaction is expressed by the following formula:
[mathematical expression not reproducible] (3)
The internal diffusion rate constant of coke gasification in the internal diffusion zone is described in the following formula:
[mathematical expression not reproducible] (4)
In the outer diffusion zone, the external diffusion rate constant of coke gasification is represented by the following formula:
[mathematical expression not reproducible] (5)
In the formula, [k.sub.v] is gasification rate constant; [k.sub.s] is the internal diffusion rate constant; [S.sub.h] is the outer diffusion rate constant; [x.sub.c] is coke conversion rate; [t.sub.1/2] is the reaction time when the conversion rate reached 50%; S is specific surface area at any time during gasification process; is the oxygen partial pressure; n is intrinsic reaction order; [mathematical expression not reproducible] is apparent reaction order; [r.sub.0] is initial particle radius of coke; [D.sub.b] is diffusion coefficient of C[O.sub.2]; [x.sub.a] is ash ratio; [omega] is the amount of carbon consumed per mole of C[O.sub.2]; R is gas constant.
The reaction rate constant k(T) can be represented by the Arrhenius formula
k(T) = [k.sub.0] exp (-E/RT). (6)
Combining the above equations, the following formula (7) can be obtained:
ln = 1/[t.sub.1/2] = ln [k.sub.0]/C - E/RT. (7)
The activation energy E of gasification can be obtained by the slope of ln [1/t.sub.1/2] and 1/T. The change curve of ln [1/t.sub.1/2] of biochar and coke breeze with the change of 1/T was shown in Figure 5, and the activation energy and transition temperature were shown in Table 3.
It was shown in Table 3 that when the gasification reaction was in the external diffusion and internal diffusion control zone, the activation energy of biochar's gasification was slightly smaller than that of coke breeze, while, in the control of the chemical reaction zone, the activation energy of biochar's gasification was significantly lower than that of coke breeze. The activation energy of biochar's gasification was 131.10 kJ/mol, which was lower than that of coke breeze by 56.26 kJ/mol. Biochar's gasification transferred from chemical reaction control to internal diffusion control at 900[degrees]C, while transferring from internal diffusion control to external diffusion at 1000[degrees]C. Obviously, the transition temperature was lower than that of the coke breeze.
3.2. The Effect of Biochar on Sintering. The effect of proportion of biochar replacing coke at equal heat substitution on sintering process was studied. The effect of biochar replacing coke breeze on the emission of C[O.sub.2] and CO during sintering was shown in Figure 6. With the increase of substitute proportion, the content of C[O.sub.2] and CO in flue gas increased. More fuel was burned per unit time due to the increasing of burning speed when using biochar in sintering. When the substitute proportion increased from 0% to 100%, the average concentration of C[O.sub.2] and CO in flue gas increased from 10.32% and 1.43% to 12.27% and 2.14%, respectively.
Combustion efficiency refers to the ratio of complete combustion to the whole combustion. The ratio of C[O.sub.2]/(CO + C[O.sub.2]) can reflect the combustion efficiency. When C is combust at high temperature, the reaction on the surface of C is the gasification reaction between C and C[O.sub.2], and the produced CO diffuses outward and reacts with [O.sub.2] diffusing inward to generate C[O.sub.2]. Therefore, combustion efficiency was affected by the rate of C[O.sub.2] + C = 2CO reaction on the surface of carbon particle. The influences of biochar replacing coke breeze on combustion efficiency were illustrated in Figure 7. Evidently, combustion efficiency was decreased with the increase of biochar ratios, and when they were 20%, 40%, 60%, and 100%, the average combustion efficiency was decreased from 87.83% to 87.82%, 86.92%, 86.04%, and 85.15%, respectively, which indicated that incomplete combustion developed with the increase of biochar ratios in sintering process. The heat released by the combustion of carbon was just 29.25% of its total calorific value when it combusted incompletely, which meant a high heat loss portion of 70.75%. Therefore, biochar replacing coke breeze would lower the efficiency of heat utilization.
From the above, it is known that biochar was characterized by higher reactivity than coke breeze and could react with C[O.sub.2] rapidly. Therefore, more CO was generated on the surface of biochar. Furthermore, as biochar burned quickly, more [O.sub.2] was consumed per unit time and the concentration of [O.sub.2] in flue gas was relatively low, which limited the secondary combustion reaction of CO and finally made combustion efficiency drop, which finally decreased the production and quality index of sintering.
The effect of biochar replacing coke breeze at equal heat substitution on the yield and quality of sinter was shown in Table 4. With the increase of substitute proportion, the sintering speed accelerated, while the sinter yield, tumble strength, and productivity decreased. When the substitute proportion of biochar was relatively low, the decreasing extent was not significant. However, when the substitute proportion exceeded a certain value, the sinter yield and quality index deteriorated greatly. Therefore, the proportion of biochar replacing coke breeze had an appropriate value. When the substitute proportion was more than 40%, the sinter yield and quality index dropped rapidly, indicating that the appropriate substitute proportion was 40%.
The main reason why sinter yield and tumble strength decreased was that the biochar burnt too fast, causing the deterioration of combustion efficiency and the drop of bed layer temperature. Consequently, reducing the heat replacement ratio of biochar for raising the temperature of bed layer could improve the yield and tumble strength of sinter. The effect of heat replacement ratio on sintering indexes was shown in Table 5. When the ratio of the heat released by biochar replacing that for the coke reduced from 1.00 to 0.75, the yield of sinter increased from 65.30% to 69.63%, and the tumble strength increased from 63.27% to 64.18%. Therefore, reducing the heat replacement ratio of biochar could improve the yield and quality of sinter.
(1) The initial temperature and the final temperature of the gasification reaction between biochar and C[O.sub.2] were low, the speed was fast, and the maximum weight loss rate and heat absorption were both higher than those of the coke breeze. Dynamic parameters showed that the gasification activation energy of biochar was 56.26 kJ/mol, lower than coke breeze, which indicated that the biochar had better reactive activity.
(2) Due to biochar's high reactivity, the degree of incomplete combustion in the sintering process increased and the thermal efficiency reduced, which was not conducive to the high-temperature mineralization process. As a result, the sinter yield, tumble strength, and productivity decreased with the increase of biochar's substitute proportion. Therefore, the proportion of biochar replacement of coke breeze at equal heat substitution should be controlled no more than 40%. Reducing the heat replacement ratio of biochar could improve the temperature of sinter bed, improving the yield and tumble strength of sinter.
Conflicts of Interest
The authors declare that they have no conflicts of interest.
The research was financially supported by the State Key Program of National Natural Science Foundation of China (no. U1660206), Natural Science Foundation of Hunan Province in China (no. 2015JJ3164), Hunan Provincial Co-Innovation Center for Clean and Efficient Utilization of Strategic Metal Mineral Resources and Innovation Driven Plan of Central South University (no. 2015CX005), Hunan Provincial Innovation Foundation for Postgraduate (CX2016B054), and Open-End Fund for the Valuable and Precision Instruments of Central South University (CSUZC201703).
 Z. Z. Hao, S. L. Wu, and X. G. Duan, "Practice of reducing sintering process energy consumption in Baosteel," Sintering Pelletizing, vol. 35, article 46, 2010.
 S. Q. Li, Z. J. Ji, L. Wu et al., "An analysis on the energy consumption of steel plants and energy-saving measures," Industrial Heating, vol. 39, no. 5, pp. 1-3, 2010.
 X. M. Liang, D. Q. Zhu, T. Jiang et al., "Present State of Sintering Energy Saving Techniques and Prospect," Sintering and Pelleting, vol. 25, no. 4, pp. 1-4, 2000.
 Y. G. Chen, Z. C. Guo, Z. Wang, and G. S. Feng, "NOx reduction in the sintering process," International Journal of Minerals, Metallurgy and Materials, vol. 16, no. 2, pp. 143-148, 2009.
 Y. Chen, Z. Guo, and Z. Wang, "Influence of CeO2 on NOx emission during iron ore sintering," Fuel Processing Technology, vol. 90, no. 7-8, pp. 933-938, 2009.
 P.-A. Glaude, R. Fournet, R. Bounaceur, and M. Moliere, "Adiabatic flame temperature from biofuels and fossil fuels and derived effect on NOx emissions," Fuel Processing Technology, vol. 91, no. 2, pp. 229-235, 2010.
 J. Liu, G. Zhai, and R. Chen, "Analysis on the characteristics of biomass fuel direct combustion process," Journal of Northeast Agricultural University, vol. 3, pp. 290-294, 2001.
 C. Bartolome and A. Gil, "Emissions during co-firing of two energy crops in a PF pilot plant: Cynara and poplar," Fuel Processing Technology, vol. 113, pp. 75-83, 2013.
 H. Spliethoff and K. R. G. Hein, "Effect of co-combustion of biomass on emissions in pulverized fuel furnaces," Fuel Processing Technology, vol. 54, no. 1-3, pp. 189-205, 1998.
 R. C. Guo, J. R. Tang, H. Xu, and H. C. Ma, "The status and vision for utilization of lignified biomass energy," Forest Inventory & Planning, vol. 32, no. 1, pp. 90-94, 2007.
 R. Lovel, K. Vining, and M. Dell'Amico, "Iron ore sintering with charcoal," Transactions of the Institutions of Mining and Metallurgy, Section C: Mineral Processing and Extractive Metallurgy, vol. 116, no. 2, pp. 85-92, 2007.
 M. Zandi, M. Martinez-Pacheco, and T. A. T. Fray, "Biomass for iron ore sintering," Minerals Engineering, vol. 23, no. 14, pp. 1139-1145, 2010.
 T. C. Ooi, E. Aries, B. C. R. Ewan et al., "The study of sunflower seed husks as a fuel in the iron ore sintering process," Minerals Engineering, vol. 21, no. 2, pp. 167-177, 2008.
 S. N. Silva, F. Vernilli, D. G. Pinatti et al., "Behaviour of biofuel addition on metallurgical properties of sinter," Ironmaking and Steelmaking, vol. 36, no. 5, pp. 333-340, 2009.
 H. Helle, M. Helle, H. Saxen, and P. Frank, "Mathematical optimization of ironmaking with biomass as auxiliary reductant in the blast furnace," ISIJ International, vol. 49, no. 9, pp. 1316-1324, 2009.
 L. Lu, M. Adam, M. Kilburn et al., "Substitution of charcoal for coke breeze in iron ore sintering," ISIJ International, vol. 53, no. 9, pp. 1607-1616, 2013.
 L. Lu, M. Adam, M. Somerville, S. Hapugoda, S. Jahanshahi, and J. G. Mathieson, "Iron ore sintering with charcoal," in Proceedings of the 6th Int. Cong. of the Science and Technology of Ironmaking--ICSTI2012, Brazilian Association for Metallurgy, Materials and Mining, Rio de Janeiro, Brazil, 2012.
 M. Gan, X. Fan, X. Chen et al., "Reduction of pollutant emission in iron ore sintering process by applying biomass fuels," ISIJ International, vol. 52, no. 9, pp. 1574-1578, 2012.
 X. Fan, Z. Ji, M. Gan, X. Chen, Q. Li, and T. Jiang, "Influence of charcoal replacing coke on microstructure and reduction properties of iron ore sinter," Ironmaking and Steelmaking, vol. 43, no. 1, pp. 5-10, 2016.
 X. Fan, Z. Ji, M. Gan, X. Chen, L. Yin, and T. Jiang, "Preparation technologies of straw char and its effect on pollutants emission reduction in iron ore sintering," ISIJ International, vol. 54, no. 12, pp. 2697-2703, 2014.
 M. Gan, X. Fan, Z. Ji, X. Chen, T. Jiang, and Z. Yu, "Effect of distribution of biomass fuel in granules on iron ore sintering and NOx emission," Ironmaking and Steelmaking, vol. 41, no. 6, pp. 430-434, 2014.
 H. P. Tseng and T. F. Edgar, "Identification of the combustion behaviour of lignite char between 350 and 900 [degrees]C," Fuel, vol. 63, no. 3, pp. 385-393, 1984.
Min Gan, Wei Lv, Xiaohui Fan, Xuling Chen, Zhiyun Ji, and Tao Jiang
School of Minerals Processing & Bioengineering, Central South University, Changsha, Hunan 410083, China
Correspondence should be addressed to Xiaohui Fan; email@example.com
Received 4 June 2017; Accepted 17 September 2017; Published 23 October 2017
Academic Editor: Merrick Mahoney
Caption: Figure 1: Chemical compositions of ash in fuels.
Caption: Figure 2: Microstructure of solid fuels: (a) coke breeze; (b) biochar; C: carbon; P: pore.
Caption: Figure 3: TG-DSC curves of nonisothermal gasification of fuels.
Caption: Figure 4: Effect of temperature on gasification of fuels.
Caption: Figure 5: Relationship between ln [1/t.sub.1/2] and 1/T of fuel gasification.
Caption: Figure 6: Effect of proportion of biochar replacing coke on COx concentrate of flue gas.
Caption: Figure 7: Influence of biochar replacing coke breeze on combustion efficiency.
Table 1: Chemical compositions of raw materials and their proportions in mixture. Chemical composition/wt-% Types of raw materials TFe FeO Si[O.sub.2] CaO MgO Iron ores blend 63.02 6.50 4.58 0.35 0.28 Dolomite 0.21 0.13 0.71 32.64 19.83 Limestone 0.14 0.10 1.49 50.66 2.28 Quicklime 0.4 0.23 2.86 76.69 1.18 Return fines 56.81 6.25 5.11 9.02 1.86 Chemical composition/wt-% Types of [Al.sub.2] * Percent/ raw materials [O.sub.3] LOI wt-% Iron ores blend 1.42 3.10 60.73 Dolomite 0.56 46.47 5.58 Limestone 0.43 40.72 2.16 Quicklime 1.20 12.36 4.62 Return fines 2.00 0.00 23.08 * The ratio was calculated when the proportion of coke was 3.85%. Table 2: Ultimate and proximate analyses of solid fuels. Ultimate analyses/wt-% Proximate analyses (dry base)/wt-% Fixed Fuel types [C.sub.total] S N carbon Ash volatile Coke breeze 78.89 0.500 0.72 74.68 19.54 5.88 Biochar 94.64 0.037 0.19 87.34 5.10 7.55 Calorific value/ Fuel types MJx[kg.sup.-1] Coke breeze 26.84 Biochar 30.77 Table 3: Activation energy of fuel gasification and the transition temperature of every zone. Activation energy/kJx[mol.sup.-1] Chemical Internal External Fuel reaction diffusion diffusion Coke breeze 187.36 77.16 33.51 Biochar 131.10 71.82 31.88 Transition temperature/[degrees]C Chemical reaction Internal diffusion [right arrow] [right arrow] Fuel internal diffusion external diffusion Coke breeze 950 1100 Biochar 900 1000 Table 4: Effect ofbiochar replacing coke breeze on sintering indexes. Biochar Sintering replacing Suitable speed/ coke ratio/% moisture/% mmx[min.sup.-1] Yield/% 0 7.25 21.94 72.66 20 7.25 24.58 68.69 40 7.50 24.73 65.30 60 7.50 27.20 55.35 100 7.75 27.17 41.11 Biochar Productivity/ replacing Tumble tx[m.sup.-2]x coke ratio/% strength/% [h.sup.-1] 0 65.00 1.48 20 64.40 1.52 40 63.27 1.43 60 54.67 1.32 100 23.87 0.93 Table 5: Effect of heat replacement ratio on sintering indexes. Heat Sintering Productivity/ replacement speed/mm Tumble tx[m.sup.-2]x ratio [min.sup.-1] Yield/% strength/% [h.sup.-1] 1.00 24.73 65.30 63.27 1.43 0.85 24.29 67.27 64.47 1.41 0.75 23.88 69.63 64.18 1.46
|Printer friendly Cite/link Email Feedback|
|Title Annotation:||Research Article|
|Author:||Gan, Min; Lv, Wei; Fan, Xiaohui; Chen, Xuling; Ji, Zhiyun; Jiang, Tao|
|Publication:||Advances in Materials Science and Engineering|
|Date:||Jan 1, 2017|
|Previous Article:||Novel Technologies and Applications for Construction Materials 2016.|
|Next Article:||Preparation and Properties of Agricultural Residuals-Iron Concentrate Pellets.|