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Analysis of hydrogen generation through thermochemical gasification of coconut shell using thermodynamic equilibrium model considering char and tar.

1. Introduction

Gasification is a thermochemical process by which low energy density fuels like biomass can be converted into gaseous fuels with the aid of a series of chemical reactions. One of the main components of gaseous fuel obtained from gasification is hydrogen, which can be used in internal combustion engines and fuel cells. Hydrogen is a clean fuel and energy released by it on combustion is higher than any other fuel on mass basis [1]. Thus it can be considered as a suitable solution for problems associated with fossil fuel depletion and global warming, if its availability is ensured from a sustainable source. Being a renewable energy source, biomass can be considered as a potential candidate for hydrogen production by gasification. Hydrogen yield from biomass gasification depends on several factors like moisture content, feed stock composition, type of gasifier, amount of gasifying agent, and so forth. Influence of different gasifying agents on product gas distribution was studied by Gil et al. [2]. From the study it was found that, compared to air, lower heating value and tar yield are high when steam was used as gasifying agent. Critical component of anygasification system is the gasifier where the homogeneous and heterogeneous reactions take place. A comparison between fixed bed and fluidised bed gasifiers was made by Warnecke [3]. It was concluded that in spite of low ash melting point and high dust content in the product gas, fluidised bed gasifiers have higher heat and mass transfer compared to fixed bed, which result in better temperature distribution.

Mathematical models can be used to investigate biomass gasification especially when large scale experimental study seems to be difficult and uneconomical. A detailed review on different gasification models was presented by Puig-Arnavat et al. [4] and D. Baruah and D. C. Baruah [5]. The comparison of different models showed that thermodynamic equilibrium model (TEM) is the simplest and can be used as an effective preliminary tool to study the effect of process parameters and fuels on gasification. Thermodynamic equilibrium model can be implemented through two approaches, namely, stoichiometric and nonstoichiometric [6]. Compared to the former approach the latter one is complex, even though the basic principle of both is one and the same. Thus many researchers formulated stiochiometric equilibrium models for simulating biomass gasification [7-13]. Application of stoichiometric models for air gasification was successfully demonstrated by Zainal et al. [14], and the modification method used to augment the prediction accuracy of similar models was given by Jarungthammachote and Dutta [15]. Modification of thermodynamic equilibrium model, to reduce its deviation from experimental data, is done mainly by considering char conversion, tar formation, and introducing suitable correction factors to equilibrium constants. A Gibb's free energy minimisation model for air gasification was developed by Ghassemi and Shahsavan-Markadeh [16] and the prediction accuracy of the model was improved by incorporating carbon conversion and tar formation from Azzone et al. [17] and Barman et al. [18], respectively. Azzone et al. [17] considered char conversion as a function of equivalence ratio (ER) in air-steam gasification whereas tar was incorporated by Barman et al. [18] in air gasification, as a compound containing carbon, hydrogen, and oxygen. The deviation of stoichiometric model developed by Huang and Ramaswamy [19], from thermodynamic equilibrium, was reduced by multiplying suitable coefficient with equilibrium constants as done by Jarungammachote and Dutta [15] and Loha et al. [11] for air and steam gasifications, respectively. Similar modification was applied by Lim and Lee [20] to air-steam gasification model in which char conversion was expressed as a function of equivalence ratio and temperature. Abuadala et al. [13] included unreacted char as 5% of biomass carbon content and tar as benzene in steam gasification model. A pseudoequilibrium air-steam gasification model with correction factors for equilibrium constants in terms of reactor temperature was developed by Ng et al. [10]. This model considered tar as a compound containing carbon, hydrogen, and oxygen, and char as solid carbon. A three stage quasi-equilibrium model (considering pyrolysis, chargas reactions and gas phase reactions in each stage) for steam gasification of biomass was developed by Nguyen et al. [21] where empirical relations were used to reduce the deviation from thermodynamic equilibrium. Puig-Arnavat et al. [22] developed a modified equilibrium model for air steam gasification of biomass using Engineering Equation Solver (EES). Deviation of this model from pure equilibrium is minimised by considering pyrolysis, heat loss in pyrolysis, char and tar, and particles leaving the gasifier and setting the amount of C[H.sub.4] produced. Review of the literatures reveals that stoichiometric models formulated for biomass air-steam gasification considering both char and tar are limited. Present work deals with the stoichiometric modeling of air-steam gasification considering tar and char. Coconut shell, a locally available nonedible biomass waste, is the feedstock selected for the study.

2. Model Development

In general thermodynamic equilibrium calculations are independent of gasifier design and are suitable for analysing the effect of fuel and process parameters [6]. These models are more appropriate for simulating entrained flow gasifiers in chemical process simulators or for downdraft fixed-bed gasifiers, as long as high temperature and gas residence time are achieved. The objective of present work is to develop a thermodynamic equilibrium model to simulate fluidised bed biomass gasifier.

Biomass gasification being a complex process, its theoretical modeling

requires certain assumptions. The assumptions used to formulate the biomass gasification process are as follows.

(i) Gasifier is considered as a steady state system with uniform temperature and pressure throughout.

(ii) The residence time of the gases in the gasifier is high enough to establish thermodynamic and chemical equilibria.

(iii) All the gases behave ideally.

(iv) Gases except [H.sub.2], CO, C[O.sub.2], C[H.sub.4], and [N.sub.2] are considered dilute.

(v) [N.sub.2] is considered as inert in the entire process.

(vi) Biomass is considered to be made up of carbon, hydrogen and oxygen.

(vii) Steam is supplied under superheated condition of 1 bar and 300[degrees]C.

By considering chemical formula of feedstock as C[H.sub.x][O.sub.z], global gasification reaction can be written as

[MATHEMATICAL EXPRESSION NOT REPRODUCIBLE IN ASCII] (1)

where X and Z are the number of atoms of hydrogen and oxygen for each atom of carbon per mole of biomass; [omega] is the amount of moisture present in dry ash free biomass; s and m are the amount of steam and oxygen supplied, respectively. On the right hand side, [MATHEMATICAL EXPRESSION NOT REPRODUCIBLE IN ASCII], and [n.sub.tar] are the numbers of moles of [H.sub.2], CO, C[O.sub.2], C[H.sub.4], and tar, and a is the char conversion factor which can be expressed as a function of equivalence ratio [23], given by

[alpha] = 0.32 + 0.82 (1 - [e.sup.-ER/0.229]). (2)

Tar is incorporated in the model as a mixture of benzene, toluene, and naphthalene in 1: 2.5: 6.5 proportions by weight [24, 25] and its yield can be obtained as a weight percentage of the total gasification products using the following [20]:

[Tar.sub.wt.%] = 35.98 exp (-0.0029T), (3)

where T is the temperature.

Total weight of the gasification product is obtained by applying mass balance to the global reaction between the reactants and the products. So mass of tar yield ([m.sub.tar]) is given by [m.sub.tar] = [Tar.sub.wt.%]/100 (biomass feed + SBR * biomass feed

+ moisture in biomass + air supplied). (4)

To determine five unknown constituents of the producer gas, five separate equations are required. These equations are developed from mass balance of C, H, and O from (1) and equilibrium constant relations for water gas shift reaction (see (9)) and methane reaction (see (11)): carbon balance:

[MATHEMATICAL EXPRESSION NOT REPRODUCIBLE IN ASCII] (5)

hydrogen balance:

[MATHEMATICAL EXPRESSION NOT REPRODUCIBLE IN ASCII] (6)

oxygen balance:

[MATHEMATICAL EXPRESSION NOT REPRODUCIBLE IN ASCII] (7)

water gas shift reaction:

CO + [H.sub.2]O [right arrow] C[O.sub.2] + [H.sub.2]. (8)

Considering equilibrium constant [K.sub.1] for water gas shift reaction,

[MATHEMATICAL EXPRESSION NOT REPRODUCIBLE IN ASCII] (9)

Methane Reaction is as follows:

C + 2[H.sub.2] [right arrow] C[H.sub.4]. (10)

Considering equilibrium constant [K.sub.2] for methane reaction,

[MATHEMATICAL EXPRESSION NOT REPRODUCIBLE IN ASCII] (11)

Considering product gas as ideal gas, K1 and K2 can be expressed as a function of temperature [14], given by

[K.sub.1] = exp + 1.86 ln T - 0.27 x [10.sup.-3]T - 58200/[T.sup.2] - 18), (12)

[MATHEMATICAL EXPRESSION NOT REPRODUCIBLE IN ASCII] (13)

Thus equilibrium composition of the product gas is obtained by simultaneously solving three linear equations (see (5)-(7)) and two nonlinear equations (see (9) and see (11)) in MATLAB platform using Newton-Raphson method.

Lower heating value of the dry product gas is estimated from the gas composition and is expressed in volume basis as [26]

[MATHEMATICAL EXPRESSION NOT REPRODUCIBLE IN ASCII] (14)

Gasification efficiency of the process is given by

[[eta].sub.gas]

Energy content in the product gas/Energy content in biomass + Energy content in steam (15)

The results of proximate and ultimate analyses of coconut shell are presented in Table 1.

3. Model Validation

Accuracy of the model is checked by comparing the predicted gas composition from the model with experimental results [27]. The error was estimated by using the statistical parameter of root mean square (RMS) error:

RMS = [square root of ([SIGMA] ([X.sub.e] - [X.sub.p]/N))], (16)

where [X.sub.e], [X.sub.p], and N are experimental data, predicted value, and number of observations, respectively. An average RMS value of 7.93 is obtained when the nine sets of experimental results are compared with their corresponding theoretical predictions, given in Figure 1.

4. Model Modification

It is observed that [H.sub.2] and CO concentrations were over-predicted and C[O.sub.2] and C[H.sub.4] concentrations were under-predicted by the present model from the experimental values. Similar results were observed by Melgar et al. [28] when they compared their model predicted gas composition with the experimental work of Jayah et al. [29]. Same results were obtained when the equilibrium models [30-33] were compared with the experimental results from fluidised bed steam gasification by Hofbauer et al. [34] and Rapagna et al. [35]. The effect was also reported in [4, 22]. This deviation in concentration may be attributed to the existence of nonequilibrium conditions in the gasifier during the experiment. The model is upgraded to match the experimental results by multiplying with suitable coefficients A and B to [K.sub.1] and [K.sub.2], respectively [14]. The variation in RMS error is monitored by changing the values of A and B and the coefficient values corresponding to minimum RMS error are incorporated in the model for better prediction. The variation of RMS error with different values of A and B is shown in Figures 3 and 4, respectively. Incorporating suitable coefficients (A = 0.85 and B = 48), the average initial RMS error is reduced from 7.93 to a minimum of 2.61. A comparison between experimental results and that obtained from modified model is presented in Figure 2.

5. Model Application

The modified quasi-equilibrium model is used to predict the influence of key process parameters like temperature, steam to biomass ratio (SBR), and equivalence ratio (ER) on product gas composition, heating value, and gasification efficiency. Gasification study was conducted by keeping biomass mass flow rate as 1.0 kg/h and varying temperature and SBR and ER in the ranges of 800 to 1800 K, 0 to 2 and 0.15 to 0.4, respectively.

6. Results and Discussion

6.1. Effect of ER, SBR, and Temperature on Gas Composition. The influence of ER and temperature on product gas composition is depicted through Figures 5-8. It is observed that all the gas species except C[O.sub.2] are decreasing with ER. This is due to shifting of the process more towards combustion by the addition of more and more air. Similar effect of ER on product gas composition was observed by Lim and Lee [20] and Puig-Arnavat et al. [22]. H2 mole fraction increases with temperature to a maximum value and then shows a slow and gradual decrease. The increase is more predominant at lower temperatures ranging from 800 to 1300 K, as shown in Figure 5. This is similar to the variation observed for [H.sub.2] concentration by Lv et al. [36]

This trend of [H.sub.2] is mainly due to the effect of exothermic water gas shift reaction. At higher temperature ranges reversal of the reaction, as per Le-Chatelier's principle, is responsible for the decrease in [H.sub.2] mole fraction. The effect of shifting of endothermic reactions like methane reformation and water gas towards the product side is less pronounced to the reversal of water gas shift reaction. This may be the reason for the slight decrease of [H.sub.2] concentration at higher temperature ranges. For SBR = 1, a maximum [H.sub.2] mole fraction of 36.14% is obtained at a gasification temperature of 1500 K and ER of 0.15.

From Figure 6, it is clear that CO concentration increases with temperature and the rate of increase is more at lower temperature ranges. This is due to the combined effect of endothermic char gasification, water gas and methane reformation, and reversal of water gas shift reaction.

Effect of temperature on C[O.sub.2] and C[H.sub.4] concentrations is shown in Figures 7 and 8, respectively. Throughout, decrease of C[O.sub.2] with temperature shows the dominance of endothermic Boudouard reaction on the process.

The decrease in C[H.sub.4] with temperature is due to the combined effect of the shifting of endothermic steam methane reformation reaction and exothermic methanation reaction towards the product side and reactant side, respectively.

Figures 9-12 show the influence of SBR and temperature on product gas composition. [H.sub.2] concentration seemed to increase throughout with SBR, but the rate of increase decreases gradually. This increase in [H.sub.2] is due to the combined-effect of watergas, steam methane reforming, and water gas shift reaction. When the SBR is increased from 0.8 to 1.2 the corresponding increase in [H.sub.2] mole fraction is only 4%. Thus increasing SBR beyond a value of unity will not contribute much to hydrogen production compared to the energy spent for steam generation.

The adverse and favorable effect of steam addition on CO and C[O.sub.2] mole fractions are depicted through Figures 10 and 11, respectively. The higher rate of C[O.sub.2] increase at low temperature ranges is attributed to the effect of exothermic water gas shift reaction. Similar effect of increase in [H.sub.2] and C[O.sub.2] and decrease in CO molar concentrations with SBR at a temperature of 988 K and ER of 0.12 was observed in [37].

6.2. Effect of ER, SBR, and Temperature on Efficiency. Influence of process parameters on gasification efficiency is shown through Figures 13,14, and 15. For any fixed values of ER and temperature, efficiency is observed to decrease with SBR.

The decrease in efficiency with increase in SBR is due to the increased energy input in the form of steam, whereas the reason for efficiency degradation with ER is the reduced LHV of the product gas. Product gas composition, LHV, and gas yield predicted using the modified model at different operating conditions are given in Table 2. It is observed that irrespective of ER and SBR values, [H.sub.2] concentration is more for 1500 K.

7. Conclusion

A thermodynamic equilibrium model was developed to analyse air steam gasification of biomass. The developed model was compared with experimental results for product gas composition and its prediction accuracy is improved by multiplying equilibrium constants with suitable coefficients. The modified quasi-equilibrium model is used to conduct parametric study and first law analysis on air steam gasification of coconut shell. For an SBR of unity, the maximum mole fraction of hydrogen in the product gas was found to be 36.14% with a lower heating value of 7.49 MJ/[Nm.sup.3] at a gasification temperature of 1500 K and ER of 0.15.

Conflict of Interests

The authors declare that there is no conflict of interests regarding the publication of this paper.

http://dx.doi.org/10.1155/2014/654946

Acknowledgment

Authors gratefully acknowledge the financial support provided by MNRE through R&D project on "Investigation on biohydrogen production by thermochemical method in fluidised bed gasifier under catalytic support and its utilization" (no. 103/181/2010-NT).

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Shanmughom Rupesh, Chandrasekharan Muraleedharan, and Palatel Arun

Department of Mechanical Engineering, National Institute of Technology Calicut, Calicut, Kerala 673601, India

Correspondence should be addressed to Shanmughom Rupesh; mailtorupeshs@gmail.com

Received 24 May 2014; Revised 7 September 2014; Accepted 8 September 2014; Published 4 November 2014

Academic Editor: J. Alfredo Hernandez

Table 1: Proximate and ultimate analyses of
coconut shell.

Proximate         (wt.%)   Ultimate   analysis
analysis                               (wt.%)

Moisture            8         C        45.61
Volatile matter     71        H         5.61
Ash                 4         O        48.16
Fixed carbon        17        N         0.26
                              S         0.34

Table 2: Product gas composition, LHV, and gas yield
at different operating conditions.

T      ER    SBR   Product gas composition (% dry basis)
(K)
                   [H.     CO      C[O.    C[H.    [N.
                   sub             sub.    sub     sub
                   .2]             2]      .4]     .2]

       0.2   0.4   5.93    1.15    33.25   14.8    44.47
             1.6   7.16    0.41    33.48   12.09   45.26
800    0.3   0.4   4.58    0.82    29.59   8.92    55.69
             1.6   5.08    0.29    29.58   6.59    56.86
       0.4   0.4   3.35    0.55    26.98   4.78    63.94
             1.6   3.2     0.18    26.83   2.77    65.42
       0.2   0.4   27.44   25.32   13.28   2.18    31.38
             1.6   32.54   15.00   20.48   2.08    28.3
1300   0.3   0.4   21.22   20.44   14.48   1.29    42.17
             1.6   25.52   12.17   20.37   1.30    39.04
       0.4   0.4   15.97   16.13   15.74   0.72    51.04
             1.6   19.48   9.61    20.44   0.77    48.1
       0.2   0.4   28.87   29.53   10.00   0.78    30.82
             1.6   33.91   19.57   16.95   0.746   28.82
1500   0.3   0.4   21.86   24.36   11.57   0.44    41.77
             1.6   26.45   16.16   17.41   0.46    39.52
       0.4   0.4   16.15   19.67   13.18   0.24    50.76
             1.6   20.15   13.04   17.96   0.27    30.82
       0.2   0.4   28.85   32.62   7.70    0.23    30.18
             1.6   33.61   23.51   14.05   0.21    27.02
1800   0.3   0.4   21.46   27.44   9.34    0.12    41.24
             1.6   25.99   19.73   14.82   0.13    37.73
       0.4   0.4   15.53   22.59   11.07   0.06    50.35
             1.6   19.66   16.23   15.68   0.07    46.76

T                     LHV    GAS
(K)                          YIELD
       ER     SBR     (MJ/   (N[m.
                      N[m.   sup.
                      sup.   3]
                      3)]    /h)

       0.2    0.4     6.08   1.47
              1.6     5.15   1.41
800    0.3    0.4     3.79   1.76
              1.6     2.94   1.69
       0.4    0.4     2.14   2.05
              1.6     1.35   1.96
       0.2    0.4     6.93   2.07
              1.6     6.14   2.21
1300   0.3    0.4     5.33   2.32
              1.6     4.75   2.43
       0.4    0.4     4.01   2.56
              1.6     3.59   2.65
       0.2    0.4     7.12   2.14
              1.6     7.15   2.28
1500   0.3    0.4     5.59   2.36
              1.6     5.70   2.50
       0.4    0.4     4.31   2.59
              1.6     3.91   2.71
       0.2    0.4     7.31   2.15
              1.6     6.66   2.30
1800   0.3    0.4     5.82   2.37
              1.6     5.34   2.51
       0.4    0.4     4.55   2.60
              1.6     4.19   2.72
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Title Annotation:Research Article
Author:Rupesh, Shanmughom; Muraleedharan, Chandrasekharan; Arun, Palatel
Publication:International Scholarly Research Notices
Article Type:Report
Geographic Code:9INDI
Date:Jan 1, 2014
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