The document discusses thermodynamic analysis of biomass gasification. It analyzes the reaction thermoneutral points (R-TNPs) for gasifying rice husk with different gasifying agents and their ratios. Key findings include:
- For CO2 alone, R-TNPs decreased with higher CO2:carbon ratios, with syngas output and CO2 conversion also decreasing. Heat requirements initially rose then fell with a heat exchanger.
- R-TNPs were not found for H2O alone at any ratio.
- With CO2+H2O, R-TNPs were only obtained at low total gasifier agent:carbon ratios. Higher ratios supported
A short introduction to Gasification process and a brief description on various types of Gasifiers used in industries to obtain fuel and energy through this presentation.
References:-
1. http://www.enggcyclopedia.com/2012/01/types-gasifier/
2. https://en.wikipedia.org/wiki/Gasification
3. https://www.youtube.com/watch?v=GkHKXz3VaFg
4. https://www.google.co.in/
An undergraduate project explaining the working and science of a bio-mass gasifier for production of bio-fuel used for heating, cooking and other purposes. Research on the bio-mass gasifier was done at a manufacturing plant in Savli, Gujarat, India.
BIOMASS GASIFICATION,gasification and gasifier.
A slide about biomass gasification including brief description about thermo-chemical conversion process and applications
A short introduction to Gasification process and a brief description on various types of Gasifiers used in industries to obtain fuel and energy through this presentation.
References:-
1. http://www.enggcyclopedia.com/2012/01/types-gasifier/
2. https://en.wikipedia.org/wiki/Gasification
3. https://www.youtube.com/watch?v=GkHKXz3VaFg
4. https://www.google.co.in/
An undergraduate project explaining the working and science of a bio-mass gasifier for production of bio-fuel used for heating, cooking and other purposes. Research on the bio-mass gasifier was done at a manufacturing plant in Savli, Gujarat, India.
BIOMASS GASIFICATION,gasification and gasifier.
A slide about biomass gasification including brief description about thermo-chemical conversion process and applications
Production of Syngas from biomass and its purificationAwais Chaudhary
This project includes production of syngas from biomass and its purification. Firstly we discuss feasibility and availability of raw material. Then we have literature survey. A lot of techniques are there to produce syngas, we have discuss process selection. Environmental considerations are also have been discussed. Piping and instrumentation (P&ID) diagrams also have been attached. At the end we've our conclusion and our recommendations.
Biomass Energy Resourses; Mechanism of green plant
photosynthesis, effiency of conversion, solar energy plantation,
Biogas- Types of Biogas plants, factors affecting production
rates, Pyrolysis, Gasifess Types & Classification of vegetable
oils a a liquid fuel and their properties, esterification process,
formation of Biodiesel, Biodiesel & its properties, suitable species
for Biodiesel formation and its cultivation, byproduct formation
during esterification, Biodiesel economics.
Hydrogen Production through Steam Reforming process.pptxFAHADMUMTAZ10
The Presentation is about the production of steam reforming process, its purity. Meanwhile, I have also discussed the other processes. I have also discussed the future trends of hydrogen in Germany and its bright future!
Biomass gasification is a mature technology pathway that uses a controlled process involving heat, steam, and oxygen to convert biomass to hydrogen and other products, without combustion.
Production of Syngas from biomass and its purificationAwais Chaudhary
This project includes production of syngas from biomass and its purification. Firstly we discuss feasibility and availability of raw material. Then we have literature survey. A lot of techniques are there to produce syngas, we have discuss process selection. Environmental considerations are also have been discussed. Piping and instrumentation (P&ID) diagrams also have been attached. At the end we've our conclusion and our recommendations.
Biomass Energy Resourses; Mechanism of green plant
photosynthesis, effiency of conversion, solar energy plantation,
Biogas- Types of Biogas plants, factors affecting production
rates, Pyrolysis, Gasifess Types & Classification of vegetable
oils a a liquid fuel and their properties, esterification process,
formation of Biodiesel, Biodiesel & its properties, suitable species
for Biodiesel formation and its cultivation, byproduct formation
during esterification, Biodiesel economics.
Hydrogen Production through Steam Reforming process.pptxFAHADMUMTAZ10
The Presentation is about the production of steam reforming process, its purity. Meanwhile, I have also discussed the other processes. I have also discussed the future trends of hydrogen in Germany and its bright future!
Biomass gasification is a mature technology pathway that uses a controlled process involving heat, steam, and oxygen to convert biomass to hydrogen and other products, without combustion.
Microbial catalysis of syngas fermentation into biofuels precursors - An expe...Pratap Jung Rai
Search for environment-friendly sustainable energy sources is of global interest due to continuous depletion of fossil fuels resources and excessive carbon dioxide emissions. Syngas fermentation is one of the promising sustainable alternative for liquid biofuel and chemical production from energy content wastes/byproducts. This study mainly focuses on acetic acid and ethanol production via fermentation, using hydrogen and carbon dioxide as substrates to mimic syngas. A laboratory scale, batch fermentation was performed at different headspace pressure ranged from 0.29 to 1.51 bar, 1200 rpm stirrer speed, and 22±1.4ºC.
Formation of acetic acid and ethanol were found significant. The maximum acetic acid concentration 68 mmol/L was obtained at 1176 hours and 1.12 bar headspace pressure. However, maximum ethanol concentration of 15 pA*s was found at 1297 hours and 1.51 bar headspace pressure. Ethanol consumption was observed during first 553 hours. Maximum H2 consumption rate was 0.153 mmol/h•gVS during 478-527 hours at 1.12 bar headspace pressure, which was 51 times higher than that obtained during first 71 hours at 0.29 bar headspace pressure (0.003 mmol/h• gVS). The total consumed hydrogen gas measure as COD (CODHydrogen) was equivalent to the increase in bulk liquid COD, 11.02 gCOD and 11.44 gCOD; in which 68% of CODHydrogen was converted to acetic acid (7.44 gCOD). A significant influence of headspace pressure and dissolved hydrogen concentration were observed on the volumetric mass (H2) transfer coefficient (kLa) and the solubility of hydrogen in the inoculum (CH). The maximum kLa and CH of 0.082 h-1 (R2 = 0.995) and 1.2 10-3 mol/L were found at 1.12 bar headspace pressure and 89 mmol/L dissolved hydrogen concentration, respectively. The calculated biomass yields ranged from 0.001-0.066 and 0.001-0.059 gVSS/gCOD, for acetic acid and ethanol formation, respectively, when the assumption of free energy efficiency use in growth was changed from 0.1 to 1.
Acetic acid and ethanol were dominant final product whereas other organic acids were almost constant and insignificant throughout the experiment. This implies that the microbial fermentation of hydrogen and carbon dioxide at headspace pressure ranged from 0.29-1.51 bar, 1200 rpm stirrer speed, and 22±1.4ºC, can be performed with digested food waste sludge for efficient acetic acid and ethanol production.
Modification & Application of Borate Zirconia CatalystRanjeet Kumar
Solid catalysts are of great advantages in alkylation reaction due to heterogenous reaction which makes separation of catalysts very easy and environment friendly. Here, sulfated and borate zirconia catalysts are used to search for ortho-xylene with Toluene & methanol. To find a new path to get o-xylene, catalysts surface was studied and a new mesoporous borate zirconia catalyst was prepared. Mesoporous Borate Zirconia had showed a very efficient path to manufature o-xylene.
Packed Bed Reactor for Catalytic Cracking of Plasma Pyrolyzed Gasijsrd.com
Packed bed reactors play vital role in chemical industries for obtaining valuable product, like steam reforming of natural gas, ammonia synthesis, sulphuric acid production, methanol synthesis, methanol oxidation, butadiene production, styrene production. It is not only used for production but also used in separation process like adsorption, distillation and stripping section. Packed bed reactors are work horse of the chemical and petroleum industries. Its low cost, and simplicity makes it first choice to any chemical processes. In our experimental work vacuum residue is used as a feed which is pyrolyzed in the primary chamber with the help of plasma into hydrogen and hydrocarbon gases which is feed stream to the Ni catalyst containing packed bed reactor called catalytic cracker. Ni loading in the catalyst about 70 % is used to crack or decompose lower molecular hydrocarbon in to hydrogen to maximize the energy content per mass flow of gas steam and also to minimize the carbon dioxide equivalent gases at outlet of the reactor. Since cracking is surface phenomena so the catalyst play important role in designing of reactor shape. Parallel Catalytic packed bed with regeneration and deactivation can be used for commercial production of clean fuel.
Study of the Influence of Nickel Content and Reaction Temperature on Glycerol...IJRESJOURNAL
ABSTRACT: La2O3-SiO2-supported nickel catalysts were evaluated in glycerol steam reforming. The samples (30wt% La and 5, 10 and 15wt% of Ni on 70wt% commercial SiO2), prepared by the simultaneous impregnation method, were characterized by EDX, nitrogen physisorption, XRD, in-situ XRD, XANES and TPR. The analyses revealed NiO species weakly interact with the support and the different metallic surface areas of the catalysts. Catalytic tests were performed in a fixed bed reactor at 600oC and 15Ni catalyst, which showed the best performance, was also evaluated at 500oC and 700oC. According to the results, the Ni content on the catalyst surface interferes in the distribution of gaseous products H2, CO, CO2 and CH4. The increase in the Ni content increases the carbon formation during reaction. The reaction temperature affected the catalytic performance and the best results were obtained with the 15Ni catalyst at 600oC, which was also tested for 20 hours for the analysis of its stability.
2. Introduction
Gasification is a process that converts organic or fossil based
carbonaceous materials mainly into carbon monoxide,
hydrogen and carbon dioxide
Today there is a huge demand for fuel because of the
increasing population. Biomass is renewable resource and is
available very easily. It is the third among the primary energy
sources after coal and oil
The gasification of biomass allows the production of a
synthesis gas or “syngas”, consisting primarily of H2, CO, CH4,
CO2 and N2, which further has a variety of uses
3. Introduction
A thermodynamic analysis of the process of biomass
gasification was conducted to find the Thermoneutral Points
(TNP’s) for different gasifying agents for different compositions
of the input streams to the gasifier
Reaction TNP’s (R-TNP’s), Process TNP’s (P-TNP’s) with and
without Heat Exchanger were calculated and product gas
compositions at TNP’s were analysed for syngas production,
syngas ratio, %CO2 conversion and heat utilities during the
course of this study
4. Introduction
It is assumed that the exit products of the coal gasifier are in
thermodynamic equilibrium.
HSC Chemistry software is well known software that uses
the Gibbs free energy minimization algorithm to find the
equilibrium product composition from a feed mixture and
has been used in gasification studies earlier
[Kumabe K, Hanaoka T, Fujimoto S, Minowa T, Sakanishi K.
Co-gasification of woody biomass and coal with air and
steam. Fuel 2007;86:684–9.]
We have also used HSC Chemistry 5.11 for our calculations
5. Literature Survey
We downloaded many abstracts and shortlisted around 80
relevant abstracts
We sorted out the shortlisted abstracts in the following
divisions
- Thermodynamic Analysis
- Experimental
- Modelling
- Reviews
- Theoretical
6. Biomass Selection
We chose Rice husk as the biomass to be gasified.
Composition by weight: 47.8% C, 5.1% H, 38.9% O, 0.1% N
(Ref : Jenkins, B.M. & Ebeling, J.M, Correlation of physical &
chemical properties of terrestrial biomass with conversion,
symposium, Energy from biomass & waste, Pg no-371)
Weight for 1 mole of rice husk is calculated to be 25.105 grams
We calculated the compositions in moles for one mole of
carbon in biomass as follows,
For 1 mole carbon, 0.6402 moles of H2, 0.3052 moles O2,
0.0008 moles N2
Temperature range considered in this study is 500-1000 °C
7. Methodology
PART A : R-TNP Analysis
For a particular feed condition, we calculated the output
composition of the reactor using 'Equilibrium Compositions'
module of HSC Chemistry 5.11 at temperatures ranging from
500 to 1000 °C, with intervals of 50 °C and constant pressure
of 1 bar
Using those compositions and 'Reaction Equations' module of
HSC Chemistry 5.11, we calculated the reaction enthalpy at
respective temperatures
8. Methodology (cont.)
PART A : R-TNP Analysis
By plotting the graph of Enthalpy vs. Temperature we
calculated the R-TNP's of the reaction
We calculated the product gas compositions at the R-TNP's
and analysed the parameters: Syngas, Syngas Ratio, %CO2
Conversion, Heat utility (without HE), Reduced Heat Utility
(with HE)
9. 1. Gasifying Agent: CO2
We defined the parameter CCBR (CO2 to Carbon in biomass
molar ratio)
We varied CCBR in the input of the gasifier. Values of CCBR
are: 0, 0.5, 1, 1.5, 2, 2.5, 3, 4, 5
From the graphs of enthalpy change vs. temperature for all
the CCBR, we found that thermoneutral points (TNP’s) can
be obtained for all the CCBR considered except 0 and 0.5
Thermoneutral temperature decreased with increase of
CCBR
14. Gasifying Agent: CO2 - Trends
Syngas, Syngas Ratio and % CO2 conversion decreased with
increase in CCBR
Heat utility (without HE) increased linearly with increase in
CCBR
However, Heat utility (with HE) decreased then remained
constant with the increase of CCBR
22. 2. Gasifying Agent: H2O
We defined the parameter HCBR (H2O to Carbon in biomass
molar ratio)
We varied HCBR in the in the input of the gasifier. Values of
HCBR are: 0, 1, 2, 3, 4
From the graphs of enthalpy change vs. temperature for all
the HCBR, we found that no thermoneutral points can be
obtained for any of the HCBR considered
24. 3. Gasifying Agent: CO2 & H2O
We defined the parameter GaCR (Gasifying Agents to
Carbon in Biomass molar ratio)
We varied GaCR from 1 to 4 in the input of gasifier and
considered different combinations of CCBR and HCBR for
each GaCR
For GaCR = 1, R-TNP’s were obtained only for 1/0
For GaCR = 2, P-TNP’s were obtained only for 2/0
For GaCR = 3, P-TNP’s were obtained for 3/0, 2.5/0.5
For GaCR = 4, P-TNP’s were obtained for all combinations
which had CCBR greater than or equal to 3
31. GaCR = 4 - Trends
R-TNP first slightly decreased with HCBR then increased
Syngas increased (from 1.9124 to 2.0298 moles per moles of
Biomass) with increase in HCBR
Syngas ratio showed a maxima (of 0.403) at HCBR = 0.714
% CO2 conversion first decreased then increased with increase
in HCBR
Heat utility (with HE) increased with increase in HCBR
However, Heat utility (without HE) first decreased slightly and
the increased with increase in HCBR
38. Methodology
PART B: Process TNP Analysis (without HE)
We calculated the Biomass preheating value for temperatures
between 500 to 1000 °C, with intervals of 50 °C.
Cp value of Rice husk was taken as 2.094 J/gK [Kaupp (1984)]
We then calculated the preheating value of gasifying agents
(CO2 and H2O) for respective temperatures. Cp value of CO2
and H2O was taken from Perry's Chemical Engineers'
Handbook 7e
We then calculated the Process enthalpy (without Heat
Exchanger) as the sum of Reaction enthalpy, Biomass
preheating and Gasifying Agents preheating
(Figure 1)
40. Methodology (cont.)
PART B: Process TNP Analysis (without HE)
We plotted the graph of Process enthalpy without heat
exchanger vs. Temperature and calculated the P-TNP's without
HE
We calculated the product gas compositions at the P-TNP's
and analysed the parameters: Syngas, Syngas Ratio, %CO2
Conversion, Reaction Enthalpy at P-TNP's
41. 1. Gasifying Agent: CO2
We varied CCBR in the input of gasifier from 0 to 5
From the graphs of enthalpy change vs. temperature for all
the CCBR, we found that TNP’s can be obtained for all the
CCBR except 0 and 5
45. Gasifying Agent: CO2 - Trends
P-TNP’s, Syngas and %CO2 conversion decreased with
increase in CCBR
Syngas Ratio showed a minima (of 0.469) at CCBR =2.056
Reaction Enthalpy at P-TNP’s was calculated and it showed a
decrease with increase in CCBR
50. Process TNP’s without Heat Exchanger
-120
-110
-100
-90
-80
-70
-60
-50
0.5 1 1.5 2 2.5 3 3.5 4
Enthalpy(KJ)
CCBR
Reaction Enthalpy at P-TNP's
51. 2. Gasifying Agent: H2O
We varied HCBR from 0 to 4 in the input of gasifier
From the graphs of enthalpy change vs. temperature for all
the HCBR, we found that TNP can be obtained only for HCBR
= 1, in the range of 500-1000 °C
HCBR
TNP
oC
CO2(g)
moles
CO(g)
moles
H2O(g)
moles
H2(g)
moles
CH4(g)
moles
N2(g)
moles
C
moles
Syngas
moles
Syngas
Ratio
% CO2
Conv.
1 580.012 0.4341 0.2164 0.5254 0.7704 0.1721 0.001 0.1775 0.9868 3.56 47.46
53. 3. Gasifying Agent: CO2 & H2O
We varied GaCR from 1 to 4 in the input of gasifier
For GaCR = 1, P-TNP’s were obtained for all the
combinations of CCBR and HCBR considered
For GaCR = 2, P-TNP’s were obtained for three combinations
2/0, 1.5/0.5, 1/1
For GaCR = 3, P-TNP’s were obtained for two combinations
3/0, 2.5/0.5
For GaCR =4, only 1 P-TNP was obtained for 4/0
60. Gasifying Agent: Both -Trends
P-TNP’s and Syngas production decreased with increase in
HCBR for both GaCR 1 and 2
Syngas ratio showed an increase with increase in HCBR for
both the GaCR
Reaction enthalpy at P-TNP’s decreased with increase in
HCBR
61. Process TNP’s without HE at GaCR = 1 & 2
500
520
540
560
580
600
620
640
660
680
0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1
TNP(oC)
HCBR
P- TNP's
GaCR 1
GaCR 2
62. Process TNP’s without HE at GaCR = 1 & 2
0.6
0.7
0.8
0.9
1
1.1
1.2
1.3
0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1
syngas(moles)
HCBR
Syngas
GaCR 1
GaCR 2
63. Process TNP’s without HE at GaCR = 1 & 2
0
0.5
1
1.5
2
2.5
3
3.5
4
0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1
SyngasRatio
HCBR
Syngas ratio
GaCR 1
GaCR 2
64. Process TNP’s without HE at GaCR = 1 & 2
-120
-100
-80
-60
-40
-20
0
0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1
Enthalpy(KJ)
HCBR
Reaction Enthalpy at P-TNP's
GaCR 1
GaCR 2
65. Methodology
PART C: Process TNP Analysis (with HE)
We calculated the Product Gas Cooling Energy released at
respective temperature. Product gas consisted of CO2(g),
CO(g), C, H2O(g), H2(g), CH4(g) and N2(g). Cp values of all the
components were taken from Perry's Chemical Engineers'
Handbook 7e
We then calculated the Process enthalpy (with Heat
Exchanger) as the sum of Reaction enthalpy, Biomass
preheating, Gasifying Agents preheating + Product Gas
Cooling (Figure 2)
67. Methodology (cont.)
PART C: Process TNP Analysis (with HE)
We plotted the graph of Process enthalpy with heat
exchanger vs. Temperature and calculated the P-TNP's with
HE
We calculated the product gas compositions at the P-TNP's
and analysed the parameters: Syngas, Syngas Ratio, %CO2
Conversion, Reaction Enthalpy at P-TNP's
68. 1. Gasifying Agent: CO2
We varied CCBR in the input of gasifier from 0 to 5
From the graphs of enthalpy change vs. temperature for all
the CCBR, we found that TNP’s can be obtained for all the
CCBR except 0
72. Gasifying Agent: CO2 - Trends
P-TNP’s, Syngas production, Syngas ratio and % CO2
conversion decreased with increase in HCBR
Reaction enthalpy at R-TNP’s increased and went from
exothermic region to endothermic region
Reaction enthalpy for CCBR = 2.68 was zero. Thus, R-TNP
and P-TNP is same for CCBR 2.68
78. 2. Gasifying Agent: H2O
We varied HCBR in the input of gasifier from 0 to 4
From the graphs of enthalpy change vs. temperature for all
the HCBR, we found that TNP’s can be obtained for all the
HCBR except 0
81. Gasifying Agent: H2O - Trends
P-TNP’s and Syngas Production decreased with increase in
HCBR
Syngas ratio and % CO2 Conversion increased with increase
in HCBR
Reaction enthalpy at P-TNP’s decreased with increase in
HCBR
86. Process TNP’s with Heat Exchanger
-60
-55
-50
-45
-40
-35
-30
1 1.5 2 2.5 3 3.5 4
Enthalpy(KJ)
CCBR
Reaction Enthalpy at P-TNP's
87. 3. Gasifying Agent: CO2 & H2O
We varied GaCR from 1 to 4 in the input of gasifier
For all the GaCR, P-TNP’s were obtained for all the
combinations of CCBR and HCBR considered
99. 3. Gasifying Agent: Both - Trends
Syngas decreased with increase in HCBR
Syngas ratio increased with increase in HCBR
% CO2 conversion and Reaction enthalpy at P-TNP’s
decreased with increase in HCBR
104. Conclusions
Sandeep et. al. varied SBR (Steam to Biomass Ratio) from
0.75 to 2.7. The hydrogen yield is found to be 104 g/kg of
biomass at SBR of 2.7. Significant enhancement in H2 yield
is observed at higher SBR compared with lower range SBR
REF: Sandeep, K., Dasappa, S., Oxy–steam gasification of
biomass for hydrogen rich syngas production using
downdraft reactor configuration
International Journal of Energy Research – 2013
In our study, for SBR = 3, hydrogen yield is found to be
130.45g/kg of biomass
105. Conclusions
Exothermal regions were obtained in the biomass
gasification with no oxygen in the input stream
Biomass Gasification can be done auto thermally even
without any input of external oxygen or air
Inbuilt oxygen content in biomass is large enough to carry
out the gasification process
The product gas for some of the feed conditions can be
used for Fischer Tropsch process in petroleum industries
106. GaCR
CCBR/
HCBR
Syngas
(moles)
without HE
Syngas
Ratio
without HE
Syngas
(moles)
with HE
Syngas
Ratio
with HE
1 0/1 - - 1.905 1.806423
2 1.5/0.5 0.822 1.216828 - -
2 1/1 0.6785 2.931054 1.9021 1.072682
2 0.5/1.5 - - 1.8972 1.923267
3 2.5/0.5 0.587 1.269037 - -
3 1.5/1.5 - - 1.8895 1.328978
3 1/2 - - 1.8874 2.116064
4 2.5/1.5 - - 1.8804 1.070469
4 2/2 - - 1.8799 1.578031
4 1.5/2.5 - - 1.8786 2.327901
Syngas Ratio between 1 to 3
For Fischer Tropsch