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International Journal of Civil Engineering and Technology (IJCIET) Volume 8, Issue 6, June 2017, pp. 109–124, Article ID: IJCIET_08_06_013 Available online at http://www.iaeme.com/IJCIET/issues.asp?JType=IJCIET&VType=8&IType=6 ISSN Print: 0976-6308 and ISSN Online: 0976-6316 © IAEME Publication Scopus Indexed

DEVELOPMENT OF BIO MASS GASIFICATION FOR THERMAL APPLICATIONS

G. Ananda Rao MLR Institute of Technology, Hyderabad, Telangana, India

M. Vidhisha Adam's Engineering College, Paloncha, Telangana, India.

M. Sudhakar Chowdary

Navabharath Ferro Alloys Ltd, Paloncha, Telangana, India

ABSTRACT Biomass is a major potential source for energy production and also other

industrial heating applications. Sugar cane and bagasse is one of the biomass largely available from agricultural waste and tapped from the sugar factories. In this present work the proximate analysis is carried out to estimate the carbon percentage in sugarcane and bagasse and development of producer gas using up draught gasifier is employed. From the results, it is demonstrated that low density biomass gasifier on sugarcane leaves or bagasse has developed successfully for existing oil fired furnaces or boilers in metallurgical and other industries. The producer gar is utilized in thermal industries applications like preheating of foundry ladle to minimize the solidification of molten metal especially in ferro alloy production. Key words: Biomass, Sugarcane, Bagasse, Up draught gasifier and Producer gas

Cite this Article: G. Ananda Rao, M. Vidhisha and M. Sudhakar Chowdary. Development of Bio Mass Gasification for Thermal Applications. International Journal of Civil Engineering and Technology, 8(6), 2017, pp. 109–124. http://www.iaeme.com/IJCIET/issues.asp?JType=IJCIET&VType=8&IType=6

1. INTRODUCTION Gasification is of course old technology used even before the Second World War and later there is no significant development because of the liquid fuel (petroleum based) which is easily available. During the 20th century, the gasification technologies rouse intermittent and fluctuating interest among the researchers. However, with rising prices of fossil fuel this technology has regained interest and has been developed with modern and sophisticated technology. Gasification is a process of thermo-chemical conversion of organic materials at elevated temperature with partial oxidation. India produces approximately 320 million tons of agricultural residues comprising of mainly rice husks, paddy straw, wheat residues and sugarcane leaves [1]. It is estimated that about one third of this or 100 million tons of residues

G. Ananda Rao, M. Vidhisha and M. Sudhakar Chowdary


are not being utilized and are disposed and simply burning them in the open fields. These solid fuels can be converted into a gaseous combustible fuel known as ‘Producer gas’ in properly designed reactors. This producer gas has a gross calorific value of 3.5-5 MJ Nm-

3consists of carbon monoxide (25% v/v) and hydrogen (15- 20% v/v). It can be combusted in suitable burners with flame temperatures exceeding 10000C and can be used for industrial thermal applications. There are reports of gasifiers being used for thermal applications both in India [2]. Certain engineering design of the gasification system was developed on a laboratory model and then validated on a bench-scale model [3]. The availability of oil and natural gas is declining day by day. It is not going to last for longer period becomes heavy burden on the economy [4]. The large amount of sugarcane is produced all over the world and in India. It generates huge amount of biomass residues such as dry leaves and bagasses [5].

The gasification is a process in which any other organic matter or biomass is converted to combustible gases (mixture of CO, CH4 and H2), with char, water, and condensable as minor products. In the first step called pyrolysis, the organic matter is decomposed by heat into gaseous and liquid volatile materials and char (which is mainly a nonvolatile material, containing high carbon content). In the second step, the hot char reacts with the gases (mainly CO2 and H2O), leading to product gases namely, CO, H2 and CH4. Producer gas is a mixture of carbon monoxide, hydrogen and methane, together with carbon dioxide, nitrogen and other incombustible gases. Foused on an updraft gasifier is construct and is used to carry out the experiment. updraft gasifier is one of the boiler. The waste material like coconut shells, sugarcane waste, and wood particles are used for the generation of producer gas. And study the effect of waste products (coconut shells, sugarcane waste, and wood particles) in form of biomass [6]. This paper reports the development of a laboratory-scale updraft biomass gasifier was designed, built, and instrumented for stable gasification using low-bulk density biomass. Related accessories, such as biomass feeder, inlet air temperature controller, air injection nozzle, were also developed to enhance gasifier performance. The effect of operation parameters on gasifier performance was studied. Two operational parameters, including air flow rate and feed-air temperature, were studied on two sources of biomass such as sugar cane leaves, and bagasse. Results showed that higher air flow rate increased tar contents in syngas for all two types. It was also found that different biomasses gave significantly different tar contents, in the order of bagasse and sugar cane leaves where higher feed air temperature reduced tar. A statistical model was implemented to study differences on syngas composition.

2. BIOMASS FUEL ANALYSIS Two types of analysis proximate and ultimate are useful for defining the physical, chemical and fuel properties of a particular biomass feed stock. Analysis done on wet basis.

2.1. Proximate Analysis This analysis records moisture, volatile matter, ash and fixed carbon as percentages of the original weight of the sample.

It is a quantitative analysis of the following parameters. Moisture content,

Volatile matter

Ash content and

Fixed carbon

Development of Bio Mass Gasification for Thermal Applications


2.1.1. Moisture Content Moisture is generally determined by heating a known quantity (1g) of air -dried sample in a silica crucible to 105 to 110 0 C for 1 hour in an muffle furnace or electric hot air oven. After heating, the silica crucible is taken out with the help of tongs, cooled in a dissector and weighed. The loss in weight is reported as the moisture content on percentage basis. More the moisture contents will leads to decrease the thermal efficiency since heat is used may absorbed by water content and consequently this energy is not available for the reduction reactions. Hence high moisture content will result in low gas heating values. When the gas is used for direct combustion purposes, low heating values can be tolerated and the use of feedstocks with moisture contents (dry basis) of up to 40-50% is feasible, especially when using updraft gasifier. Sugar cane leaves are heated to 1500 c and then go for further analysis

% =loss in weight x 100

weight of coal smple taken

Figure 1 sugar cane leaves Figure 2 Dry sugar cane leaves and bagasse

2.1.2. Determination of the Volatile Matter Content of the Fuels The fuel samples were crushed into powdered form, 1 g of each of the crushed samples was placed in different porcelain crucibles. They were each covered with a lid with little opening left and placed on hot plates at a temperature of 925 0C ± 200c to drive off the volatiles. The heating is continued until the flame coming out through the holes have ceased. This shows that the volatile matter was driven off. After this, the weight of each of the heated samples was taken. For bagasse powder: Volatile matter + H2O:

W1 = CRUCIBLE WEIGHT= 11.8421 W2 = SAMPLE WEIGHT = 0.43221 W3 = after heating to 9200C = 12.0330

Formula for VMS = ( ) ×100

=( . . ) ..

×100 =55.83%

For sugarcane leaves: Volatile matter + H2O:

W1 = CRUCIBLE WEIGHT = 12.9122 W2= SAMPLE WEIGHT = 0.3004 W3= after heating to 9200C= 13.1072



Formula for VMS = ( ) ×100

=( . . ) ..

×100= 35.08%

Figure 3 Sample is kept in crucible to expel volatile matter at 8940c

Figure 4 Volatile matter substance

2.1.3. Determination of the Ash Content The ash content test of the fuel samples was carried out by crushing the samples and accurately weighed 1 g in a open crucible at 700-750 0 c for 45minutes in a muffle furnace. The weight of the samples was taken and given as follows: For sugar cane leaves

Ash content: W1 =CRUCIBLE WEIGHT= 42.7248 W2=SAMPLE WEIGHT = 0.3557 W3= after heating to 7500 C =42.8565

Formula for ash = ×100

= . ..

×100 =37.02

For bagasse Ash content: W1 =CRUCIBLE WEIGHT= 29.1657 W2=SAMPLE WEIGHT = 0.2336



W3=after heating to 7500C =29.1792

Formula for ash = ×100

= . ..

×100=5.77%

Figure 5 Sample ashes weighing in silica crucible Figure 6 Sample ash

2.1.4. Determination of the Fixed Carbon Fixed carbon represents the quantity of carbon in coal that can be burnt by a primary current of air drawn through the hot bed of fuel. The total sum of the percentages of moisture, volatile matter and ash subtracted from 100 gives the percentages of fixed carbon. For bagasse:

C(%)= 100-(% (volatility+ H2O) + %(ash) C(%)=100- (55.83%+5.77%)=38.4%

For sugar cane leaves: C(%) = 100-(% (volatility+ H2O) + %(ash) C(%) =100- (35.08%+37.02%) = 27.8%

2.1.5. Discussionon Proximate Analysis of the Feedstock The results of the proximate analysis carried out on the properties of the feedstock (sugar cane leaves and bagasse). This analysis gives the suitability of the feedstock, this includes moisture content, the fixed carbon, volatile content, and ash content in the both the sugar cane leaves and bagasse. The two feedstocks considered have very low moisture content and ash content. The moisture content of the feedstock has dried in outdoor solar radiation to obtain a high gasification temperature which results in the high energy values obtained. This results gives the abundant biomass energy potentials are available in the feedstock.

3. PHYSICAL TEST

3.1. Bulk Density The most important biomass fuel physical characteristics are the bulk density. The bulk density is the ratio of weight of biomass packed loosely to the volume occupied in the container. It is depends on the exact packing of the particles. The fuel shape and feeding characteristics can be evaluated either it will be feasible to simply use gravity feeding techniques or assistance by stirring and shaking which will be required. The angle of repose for a particular fuel type is generally measured by filling a large tube with the fuel, and then lifting the tube and allowing the fuel to form a pile. The angle of repose is inclination with



horizontal to the sides of the pile. The basic feed characteristic is more easily find by the dugout angle of repose.

3.1.1. Bulk density of sugar cane leaves Height of container =36.5 cm Diameter = 28 cm Sugar cane leaves chopped to =50mm Weight of empty container = 1.700 kg Weighted with sugar cane leaves = 2.150 kg Weight = 2.150 – 1.700 kg = 450 grams

Area= ^ = ( )^ = 616 cm2

Volume = Area × Height= 616 × 36.5 =22484 cm3

Bulk density = = gm/cm3 = 0.0200 gm/cm3 = 20 kg/m3

3.1.2. Similarly for bagasse Bulk density = 30 kg/m3

Figure 7 Measuring weight of container with chopped leaves

3.2. Physical properties of sugar cane leaves (chopped) and bagasse

Table 1

S. No Sugar cane leaves bagasse

1.Partical size in cm 1 - 10 < 5

2.bulk density, kg/m3 20- 40 50-75

3.3. Other Fuel Parameters The tests and analyses just mentioned are in widespread use because they were developed for use in other industries. However, many more tests need to be developed specifically for gasification processes. The effects of other fuel parameters on biomass gasification, illustrating the need for more specific testing procedures. The basic fuel parameters important in gasifier design are



Particle size and shape

Particle size distribution

3.3.1. Particle Size and Shape The size and shape of the fuel particles are important for moving and delivering the fuel and also the behavior of the fuel in the gasifier. A good fuel hopper design has a cone angle that is double the dugout angle of repose. With an angle of repose over 450, the fuel may not flow even in a straight cylinder and will require either an inverted cone or some agitation. Smooth hopper walls are always desirable .Gasifiers frequently suffer from ridging and channeling of the fuel. The size and shape of the fuel decide the thickness of the gasification zone, the pressure drop through the bed, and the minimum and maximum hearth load for satisfactory operation. A uniform particle size helps to overcome some problems. Improving the grate design, as well as added agitation or stirring, can give a long run trouble-free gasifier operation.

Figure 8 Chopped to 50mm

4. BIOMASS THERMAL CONVERSION PROCESSES Thermal conversion processes for biomass involve some or all of the following processes:

Pyrolysis: Biomass + Heat -> Charcoal, oil, gas Gasification: Biomass + Limited oxygen ->Fuel gas Combustion: Biomass + Stoichiometric' oxygen-> Hot combustion products

4.1. Biomass Pyrolysis Pyrolysis is the breaking down (lysis) of a material by heat (pyro). It is the first step in the combustion or gasification of biomass. When biomass is heated in the absence of air to about 350'C (pyrolysis), it forms charcoal (chemical symbol: C), gases (CO, CO2, H2, H20, CH4), and tar vapors (with an approximate atomic makeup of (C 1.2O 1.5)' The tar vapors are gases at the temperature of pyrolysis but condense to form a smoke composed of fine tar droplets as they cool.



Figure 9 Pyrolysis

All the processes involved in pyrolysis, gasification and combustion can be seen in the flaming match. The flame provides heat for pyrolysis, and the resulting gases and vapors burn in the luminous flame in a process called flaming combustion. After the flame passes a given point, the char may or may not continue to burn (some matches are chemically treated to prevent the charcoal from smoldering). When the match is extinguished, the remaining wood continues to undergo residual pyrolys is, generating a visible smoke composed of the condensed tar droplets. A more quantitative picture of pyrolysis obtained through thermo gravimetric analysis (TGA). In this technique, a small piece of biomass is suspended on a balance pan in a furnace, and the temperature is increased with time at a known rate. One sees that moisture is released first, at1000 C, followed by the volatile materials at 2500 -4500 C these temperatures are important in understanding pyrolysis, gasification, and combustion. a fraction of char and ash remains in the end .If air is allowed to enter the system after pyrolysis, the carbon (char) will bum, leaving the ash as the final product. Each form of biomass produces slightly different quantities of char, volatile material, and ash. Knowledge of these quantities, as well as the temperature dependencies of the reaction and associated weight losses, are useful in understanding gasifier operation and design

4.2. Gasification

4.2.1. Principles of Gasification A process that converts carbon-based materials (e.g., wood/biomass) into combustible gases (principally CO + H2) by reacting the solid fuel at high temperatures with a controlled (limited) amount of oxygen Gasification is a thermo-chemical process, where heat converts solid biomass into flammable gases 1. Updraft gasifiers 2. Downdraft gasifiers and 3. Cross draft gasifier

The terms "updraft gasifier" and "downdraft gasifier” may seem like trivial mechanical descriptions of gas flow patterns. In practice, however updraft biomass gasifiers can tolerate high moisture feeds and thus have some advantages for producing gas for combustion in a burner However updraft gasifiers produce 5 % to 20% volatile tar-oils and so are unsuitable for operation of engines. Downdraft gasifiers produce typically less than 1 % tar-oils and so are used widely for engine operation.



4.2.2. Operation of the Updraft Gasifier In updraft gasifier Biomass enters through an air seal (lock hopper) at the top and travels downward into a rising stream of hot gas. In the pyrolysis section the hot gas pyrolysis the biomass to tar-oil, charcoal and some gases. In the reduction zone the charcoal thus formed reacts with rising CO 2 and H2O to make CO and H2.Finally below the reduction zone incoming air burns the charcoal to produce CO 2 and heat. Note that the combustion to CO 2 is Exothermic and the heat produced in the gas here is an absorbed in the endothermic reduction and pyrolysis reactions.

The product gas from this process contains 10-20% tar; this side effect is due to the fact that syngas emanating from the combustion zone carries aromatic vapors from the biomass, produced in the pyrolysis zone. These gases exit the gasifier without being decomposed Tar removal methods are required in order to use syngas from updraft gasification for industrial and power generation applications such as internal combustion engines, turbines, and fuel synthesis.

4.3.1. Reaction Chemistry The following major reactions take place in combustion and reduction zone

4.3.2. Combustion Zone The combustible substance of a solid fuel is usually composed of elements carbon, hydrogen and oxygen. In complete combustion carbon dioxide is obtained from carbon in fuel and water is obtained from the hydrogen, usually as steam. The combustion reaction is exothermic and yields a theoretical oxidation temperature of 14500 C

The main reactions, therefore, are: C + O2 = CO2 (+ 393 MJ/kg mole) (1) 2H2 + O2 = 2H2 O (- 242 MJ/kg mole) (2)

4.3.3. Reaction Zone The products of partial combustion (water, carbon dioxide and uncombusted partially cracked Pyrolysis products) now pass through a red-hot charcoal bed where the following reduction reactions take place.

C + CO2 = 2CO (- 164.9 MJ/kg mole) (3) C + H2O = CO + H2 (- 122.6 MJ/kg mole) (4) CO + H2O = CO + H2 (+ 42 MJ/kg mole) (5) C + 2H2 = CH4 (+ 75 MJ/kg mole) (6) CO2 + H2 = CO + H2O (- 42.3 MJ/kg mole) (7) Reactions (3) and (4) are main reduction reactions and being endothermic have the

capability of reducing gas temperature. Consequently the temperatures in the reduction zone are normally 800-10000 C Lower the reduction zone temperature (~ 700-8000 C), lower is the calorific value of gas.

4.3.4. Pyrolysis Zone Pyrolysis is an intricate process that is still not completely understood. The products depend upon temperature, pressure, residence time and heat losses. However following general remarks can be made about them. Upto the temperature of 2000 C only water is driven off. Between 2000C to 280 C carbon dioxide, acetic acid and water are given off. The real pyrolysis, which takes place between2800 C to 5000 C, produces large quantities of tar and



gases containing carbon dioxide. Besides light tars, some methyl alcohol is also formed. Between 500 to 7000C the gas production is small and contains hydrogen. Thus it is easy to see that updraft gasifier will produce much more tar than downdraft one.

5. DESIGN OF UP DRAFT GASIFICATION SYSTEM

5.1. Determination of biomass reactor dimensions from bulk density Sample made for 100 grams fuel:

Bulk density 20 kg/m3

20 kg =1 m3 For 1 kg 1/20×1 = 0.05 m3

100 grams =0.0005(100)3 = 5 ×102 cm3

Volume =500 cm3 1. Let’s take diameter =14cm Area = = = π (7)2 = 153.86 cm2

Height = volume/ area =3.249 cm 2. Let’s take another diameter =10cm Area = = = π (5)2 = 78.571 cm2

Height = volume/ area = 6.36 cm Length = 2πr = 2 (5) = 31.42 cm.

Figure 10 For 100 grams of fuel from derived length and height butt welded to 10 cm diameter

Reactor dimensions for 1kg fuel: Bulk density 20 kg/m3

20 kg =1 m3 For 1 kg 1/20×1 = 0.05 m3 =0.05× (100)3 = 5 ×104cm3

Volume =50000cm3 1. Let’s take diameter = 30cm Volume = = h = π (15)2 h 50000 = π×(15)2×h Height = volume/ area = 70.735 cm For D =30 cm Length = L = π × 30=94.247 cm.



5.2. Determination of Burner Efficiency with Diesel Oil A close coupled gasifier burners has high efficiency burning of solid fuels compared with conventional solid burners. Gas-air mixture and mixing are more easily controlled than are conventional solid fuel burners, resulting in more complete combustion 1. Two Trays (30*30) inches 2. Plate thickness = 4mm 3. 32 liters of water in each tray 4. Water depth= 5cm

By taking 7 liters of diesel, and air pressure 5.5 to 6kg/m2

Table 2

TIME Temp in tray 1 Temp in tray 2 5:15 pm 29.40c 29.60c 5:20 pm 45.50c 840c 5:22 pm 580c 890c 5:24pm 650c 1000c 5:25 pm 78oc 1090c

Time taken 10 minutes =600seconds

Table 3

Tray 1 Tray 2 29.40c 29.60c 780c 1090c

∆ = 48.60C ∆ = 79.40C 1000 kg/cm3 *32 liters/1000 (lit/m3) =32kgs Tray 1= 32000gms* 1 Cal/gm0c*48.6oc =1555200Cal Tray 2=32000gms* 1 Cal/gm0c*79.40c= 2540800Cal Tray1 +Tray2= total energy= 4096000 Cal 10500 Kcal/1 liter of diesel = 10500000 Cal/1 liter Burner Efficiency=(4096000/10500000)*100 =39%

Figure 11 a) Ladle getting preheated with diesel burner, b) carbon lining and c) carbon paste



6. DEVELOPMENT OF LABORATORY SCALE UPDRAFT GASIFICATION SYSTEM

Figure 12 Schematic diagram of gasification system

6.1. Air Supply System Primary air in the oxidation zone was supplied by placed it in the middle of the reaction chamber. These nozzles were connected to the square shape primary air inlet manifold placed around the middle cylinder. The manifold was constructed from 50x50x4 mm square mild steel pipes. Air was supplied to the manifold from a variable speed with blower of air pressure of 4 to 5 kgf maximum air volume 0.065 m3/s at 40 0 C

6.2. Gasifier Operating Procedure The gasifier was operated and tested in the following steps:

A thin layer of charcoal was placed near the throat (pocket area) of the oxidation zone and some of them were wetted with fire lighter (liquid).

The bed was ignited with a torch and fan was switched on to supply sufficient air/oxygen to initiate the combustion.

The top cover plate was closed and tightened.

Then the gasifier was loaded with biomass through fuel feeding hole.

During the second run, gasifier was loaded first and ignition was initiated through the ash hole.

The primary air supply was full at the starting of gasifier and then maintained around 35% of the stoichiometric condition to ensure the partial combustion of the biomass with the help of a fan-controller, gate valve and air flow meter.

After 5 minutes, the producer gas in the form of thick white smoke and tar came out through the burner.

The producer gas was ignited with a firing-torch at the burner.

A yellowish-red flame was observed and continued to ignite for 15 minutes.

To stop the gasifier, first the fan was switched-off then the gate valve in the air supply channel was closed to completely stop the primary air supply.

The gasifier was ultimately stopped after closing the air supply and left in an open space until it cooled down and all gases came out (more than 6 hours).



Figure 13 Experimental set up of gasification system

6.3. Results of the performance test carried out on the updraft gasifier The quantities of both sugar cane leaves and bagasse fed into the gasifier during the performance testing .At the beginning of the test after fire has been introduced into the reactor, white smoke was observed to be emitted, the gasifier started to produce a white smoke which in the indication of the combustible gases been formed. During this time, the white smoke was ignited, gradually; the production of the combustible gases began to be noticed through the production of blue flame at the outlet of the gasifier at about 19 and 15 min for the bagasse and sugar cane leaves respectively and continued until the experiment lasted.

Results of the test parameters for bagasse: Start-up Time = TS = 11 min

Operating time = T0 = 19 min

Total operating time = Tto = TS+T0 = 11+ 19 min = 30 min

Results of the test parameters for sugar cane leaves:

Start-up Time = TS = 12 min

Operating time = T0 = 15 min

Total operating time = Tto = TS+T0 = 12+ 14min = 26 min

6.4. Determination of volume for 1 liter of fuel As sugar cane leaves has low fixed carbon total energy obtained will be low so estimating for bagasse.

For 1 liter of fuel volume determined 1 m3 =1000 liters\ 1 liter = 1× 103 cm3 = 10 cm × 10 cm× 10 cm volume needed

1kg volume of gas =1 m3 Density of diesel = 850 kg/m3 Density of gas = 1 kg/m3 Approximately 1 lit diesel = (850 ×103) cm3 = 850000 CC of volume needed for gas.



7. DETERMINATION OF TOTAL ENERGY WITH BAGASSE FUEL PRODUCER GAS 1. Two Trays (30*30) inches 2. Plate thickness = 4mm 3. 32 liters of water in each tray 4. Water depth= 5cm

By taking 7 liters of diesel, and air pressure 5.5 to 6kg/m2

Table 4

S. No. TIME Temp in tray 1 Temp in tray 2 1 5:15 pm 29.40c 29.60c 2 5:20 pm 45.50c 840c 3 5:22 pm 64 0c 890c 4 5:24pm 76 0c 1000c 5 5:25 pm 87oc 1200c

Time taken 10 minutes

Table 5

S. No. Tray 1 Tray 2 1 29.40c 29.60c 2 870c 1200c 3 ∆ = 57.60C ∆ = 90.40C

1000 kg/cm3 *32 liters/1000 (lit/m3) =32kgs Tray 1= 32000gms* 1 Cal/gm0c*48.6oc = 1843200Cal Tray 2=32000gms* 1 Cal/gm0c*0c= 2892800Cal Tray1 +Tray2= total energy= 4736000Cal As total energy is greater than diesel energy can conclude that burner efficiency will be

more for producer gas

8. CONCLUSIONS Experimental investigations showed that bagasse has more carbon percentage than sugar cane leaves. Biomass gasifier developed from snatch of bagasse showed good results. A yellow flame was observed indicate the production of these combustible gases. Also ash was developed during the gasification process. Oil produced from these can be used as fuel. The present study clearly demonstrated that low-density biomass gasifiers running on sugarcane leaves or bagasse can be successfully retrofitted to existing oil-fired furnace/boilers in metallurgical and other industries. The sulfur content of biomass fuels is usually very low compared with fissile fuels. The absence of sulfur in biomass fuels and free from contaminate producer gas could allow a longer life for an engine rather than petroleum fuels. When the gasifier was run on bagasse it consumed around 1.8 kg of fuel to give a stable flame for 15 minutes. On the other hand, when it was loaded with cane leaves sugar, fuel consumption was 3.1 kg/hr. Updraft producer gas is an excellent fuel for high quality heat applications. The high tar content does not need to be removed, and adds to the heating value. Furthermore, the sensible heat of the gas adds to the flame temperature and overall heat output. Burners are used to pre heat ladle to 500 0 C before pouring molten metal in to ladle in industrial applications.



9. SCOPE FOR FUTURE WORK Gas burner specially designed for biomass mass gasifier which needs to be utilized to check the efficiency of burner. The oil obtained while operating gasifier need to be utilized for thermal application. Producer gas obtained can compress in I. C engine and generate electricity. This technology should be further supported and encouraged to be used in the domestic and industrial operations where combustion is needed.

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