Recent advances in the performance of Co-Current gasification technology: A review

Recent advances in the performance of Co-Current gasification technology: A review

international journal of hydrogen energy xxx (xxxx) xxx Available online at www.sciencedirect.com ScienceDirect journal homepage: www.elsevier.com/l...

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international journal of hydrogen energy xxx (xxxx) xxx

Available online at www.sciencedirect.com

ScienceDirect journal homepage: www.elsevier.com/locate/he

Review Article

Recent advances in the performance of Co-Current gasification technology: A review Senthil Ramalingam, Balamurugan Rajendiran*, Sudagar Subramiyan Department of Mechanical Engineering, University College of Engineering Villupuram, Anna University, Chennai, India

highlights  Improved gasifier efficiency of the co current gasifier process has been examined.  Optimized reactor design of the co current gasifier reactor is identified.  Different briquettes feedstock can be used in a single automated cocurrent gasifier.  Feeding, preheated air and discharge system is modified by recent method in the cocurrent gasifier.  Gasification efficiency affected parameters are presented.

article info

abstract

Article history:

The Co-Current reactor gasifier is a promising technique, owing to its good performance

Received 6 August 2019

and less residue content. Even though it can be used only for low moisture feedstock, it is

Received in revised form

needed improvement by incorporating modifications in the design of reactor, feeding

18 October 2019

system, air supply system, preheating air or feedstock, discharge system, recirculation

Accepted 24 October 2019

technique, and co-gasification. Many of the researchers found that various improvement

Available online xxx

methods have been done to improve the performance of the gasifier at different operating condition. Therefore, in this paper a detailed review has been made to study about that

Keywords:

developments of Co-Current gasifier and their effects on the performance of the gasifier.

Co-current gasifier

Further to improve the performance a suitable method for the gasifier is identified. A

Improvement

comparision with various methods reveals that design modification showed better per-

Process parameter

formance, higher producer gas yield and less pollution.

Thermo chemical

© 2019 Hydrogen Energy Publications LLC. Published by Elsevier Ltd. All rights reserved.

Biomass gasification

* Corresponding author. E-mail addresses: [email protected] (S. Ramalingam), [email protected] (B. Rajendiran), [email protected] (S. Subramiyan). https://doi.org/10.1016/j.ijhydene.2019.10.185 0360-3199/© 2019 Hydrogen Energy Publications LLC. Published by Elsevier Ltd. All rights reserved. Please cite this article as: Ramalingam S et al., Recent advances in the performance of Co-Current gasification technology: A review, International Journal of Hydrogen Energy, https://doi.org/10.1016/j.ijhydene.2019.10.185

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international journal of hydrogen energy xxx (xxxx) xxx

Contents Introduction . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Gasification process . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Drying zone . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Pyrolysis zone . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Oxidation zone . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Reduction . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Development of gasifier . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Design improvements . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Feeding system . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Air supply system . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Re-circulating system . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Discharge system . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Process parameter . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Gasification agent . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Equivalence ratio . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Feeding rate . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Gasification temperature . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Feed stock characteristics . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Feedstock size . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Feedstock moisture content . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Feedstock in briquette method . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Co-gasification . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Preheated biomass . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Comparison of various types of modified co-current gasifier with traditional type reactor . . . . . . . . . . . . . . . . . . . . . . . Design improvement . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Process parameter . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Feedstock characteristics . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Gasifier efficiency . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Barriers in gasification . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Applications in IC engine . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Conclusions . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . Future developments . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . References . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .

Introduction Nowadays the world facing major problems such as global warming, acid rain, ozone depletion etc, from energy sector on the environment due to the rapid growth of automobiles. In order to minimize the energy demand and issues related to environment, can be used instead of fossil fuels. The production of re-generable source of energy from biomass through biochemical and thermochemical processes. Thermo chemical conversion techniques can be categorized into three different types such as combustion, gasification and pyrolysis (Excess air used for conversion of biomass into bio-energy. Controlled air for conversion of biomass into bioenergy is gasification. Absence of air for conversion of biomass into bioenergy is called pyrolysis process). During the combustion process biomass burned in open place, the outcome of the process is heat energy, which can convert into electrical energy by means of operating the turbine. In the controlled air

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operation techniques (gasification) the biomass is subjected to the combustion process in which the producer gas is generated and it can be utilized in CI engine and turbine as an alternate fuel. The absence of air operation process (pyrolysis) the bio-oil is obtained and it can be also used as alternate fuel for CI engine and SI engine. Comparing these processes, gasification is having higher efficiency and lower emissions. Therefore using this alternate source of energy will reduce global warming considerably. Another major global problem is energy demand, while increasing the petroleum product price, will give a great impact on domestic energy. According to that, situation needs to develop the clean re-generate energy. Gasification is a process that can convert biomass into a combustible and non-combustible gas (producer gas). The solid feedstock is converted into thermal and chemical energy of the (producer gas) gas. Thus the chemical compositions (carbonaceous material) of the feedstock determine fuel quality. High concentration of combustible gases such as H2, CO and CH4 increases the calorific value of the producer gas.

Please cite this article as: Ramalingam S et al., Recent advances in the performance of Co-Current gasification technology: A review, International Journal of Hydrogen Energy, https://doi.org/10.1016/j.ijhydene.2019.10.185

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Based on the Feedstock, feed direction, air supply direction and gas output flow direction in the gasifier it can be categorized into downdraft (Co-Current), updraft (current) and cross draft [1]. Gasifier Co-current gasifier is most suitable to generate clean producer gas with a low content of tar and particulate, because of the tar is combusted in the oxidation zone. The construction and development of the co-current gasifier is very simple operation and also need a less maintenance, semiskilled operator for co-current gasifier when

Fig. 1 e Layout of Co-Current (Down Draft)Gasifier Reactor [2].

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compared to other gasifiers. Among the various types of gasifier reactor, Co-current reactor type gasifier is highly efficient method because of low residue and required semi skilled operator [2e4]. In Co-Current reactor gasifier, biomass is fed at the top of the gasifier and sent to drying, pyrolysis, oxidation, and reduction zones as shown in Fig. 1. Syn gas or Producer gas, is a product outcome of gasification process, it leaves gasifier from the gas outlet at the lower part of the gasifier reactor. Producer gas consists of combustible gases like CO, H2, and CH4 and non-combustible gases such as CO2 and N2. Producer gas quality is depends upon the heating value, and no of carbon atom present in the feedstock material. High heating value feed stock gives good quality of producer gas and low residue content. The gas quality can improve by the process parameter, operating parameter, and core design of the gasifier reactor. The process parameters include the size of the feedstock, chemical composition (C,H,O,N), density of feed stock, no. Of fixed carbon, volatile matter, ash and moisture. Operating parameters includes temperature of the reactor, equivalence ratio of air with feed stock and feeding rate. Design improvement methods are feeding system, air supply system, recirculation system and discharge system. It has been reported that clean and high heating value gas can be used as fuel for Internal Combustion (IC) or engine gas burner.

Fig. 2 e Various stages in thermo chemical conversion (gasification) process [5].

Fig. 3 e Shows biomass pyrolysis stage of conversion process [5]. Please cite this article as: Ramalingam S et al., Recent advances in the performance of Co-Current gasification technology: A review, International Journal of Hydrogen Energy, https://doi.org/10.1016/j.ijhydene.2019.10.185

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Recent Developments in Co-Current

Process Parameters

Design Improvements

Air

Belt Conveyor Screw Conveyor

Feeding System

Gasification Agent Multi Stage

Air

Feed stock Characteristic

Oxyge

Biomass Size

Steam

Biomass Moisture

Pre- Heating Stage

Equivalence Ratio

Recirculation System Discharge System

Grate

Biomass Briquettes

Feeding Rate

Ash Removal

Vibrating

Screw

Rotating

Pneumatic

Reciprocating

Reciprocating

Gasification Temp. Co-Gasification

Pre-Heating Biomass

Fig. 4 e Recent Developments in Co-Current Gasifier process.

Co-Current type gasifier reactor is highly recommended for small scale function. Generally, gasifier capacity of 10e50 kW for small scale purpose are used [5]. A Few cases power generation for commercial application from small to medium scale, woodchips are used as feedstock [6]. Cocurrent gasifier operator facing difficulties while handling the biomass with both higher amount of moisture and ash content, due to having more than 20% moisture content and this leads to grate block, bridging, scaling and finally affect quality of producer gas and reduce the gasifier efficiency. High amount of energy need in drying process, for high moisture content when compare to that of low moisture content feedstock, and also the excess energy is used from the oxidation process. Feedstock having lower bulk density and moisture content more than 20% are leads to grate blocking, channeling, bridging, and finally affecting quality of producer gas and gasification efficiency. In order to avoid those problems, modification needed in the co-current gasifier reactor. Development in the reactor design can be listed, such as development in feeding system, modification in air supply system, added a recirculation of producer gas and residue handling system. In case of continuous loading to the gasifier, various type of conveyors, grate should be used for feeding as well as residue handling. Modification in air supply system is implementation of multi-stage and pre-heating air unit. Particularly in the multi-stage air supply system, air is supplied into the reactor with two or more stage. Recirculation of gas unit is adopted for adopting the heat generated from the gas and also used for drying the feedstock, preheating the air. Numerous papers have been studied in the performance of the gasifier only, some of researchers were discussed the

operating parameter and their modification in the performance of the gasifier. The intention of this paper is to conduct detailed review on the various improvement of Co-current gasifier available and finding out the optimum method.

Gasification process The gasification process is consists of four discrete thermal processes which includes drying, pyrolysis, oxidation and reduction as shown in Fig. 2.    

Drying process - Removal of Moisture Pyrolysis process -Release of Volatile Matter Oxidation process -Partial Combustion Reduction process eDecomposition of Char

During drying process moisture present in the feedstock is removed by heat supplied. The heat is supplied from the oxidation zone of the gasification process and it is used for pyrolysis process as well as reduction process. The volatile gas is obtained at the end of pyrolysis process. Then partial combustion and decomposition char is produced, finally producer gas is obtained.

Drying zone Generally, feedstock is having 30e60% of moisture content and it has to be removed to improve the performance of gasifier. The moisture removal is done by means of applying heat into the feedstock. The high quality of producer gas and yield depends on the moisture percentage content in the biomass [8]. The feed stock will release the moisture when it is

Please cite this article as: Ramalingam S et al., Recent advances in the performance of Co-Current gasification technology: A review, International Journal of Hydrogen Energy, https://doi.org/10.1016/j.ijhydene.2019.10.185

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Table 1 e Shows the previous development in gasification process by improve the Rector Design System. Development in Rector Design [[15e17]] Layout

Description

Feed Material

Result

Reactor: down draft gasifier. Oxidation and reduction zones size through top to bottom height of the bed ¼ 810 mm, diameter of the oxidation zone ¼ 450 mm, diameter of the drying hopper zone ¼ 305 mm, Diameter of the throat ¼ 135 mm. In terms of the construction, the gasifier system is consisting of four parts. The gasifier experimental system having packed-bed scrubber, filter box, circulating fan and a pilot burner.

Hazelnut shells 17.9  16.5  8.5 mm3

Reactor: fluidized bed type is used. The gasifier is designed to get the continuous flow of syn gas. To achieve continues syn gas flow solar or auto thermal reactor is used. The steam is used as gasification agent. The gasification reactor contains SiC absorbing tube with a Al2O3 eSiC cavity in a fluidized bed.

Wood chips

The gasifier operates between in 1.44 and 1.47 N m3/kg of air fuel ratio. The producer gas has a GCV 5 MJ/ m3 at a volumetric flow of 8 e9 N m3/h product gas. At this optimum, low tar and char were produced at a ratio of 0.005 and 0.051 of the feed. Optimum output were listed below.  Char rate is determined as 0.201 kg/h.  Tar output rate is found as 0.023 kg/h.  combustible gas flow is obtained as 10.96 N m3/h. The gasifier results were analyzed The effect of H2C:C, O2:C with two method of variance. The maximum Carbon conversion is reached 0.79 and the cold gas ratio is 1.16. The maximum solar with fuel efficiency is 22%.

The main objective of the study is to evaluate the effect of design and operating parameters, particularly reactor design, air velocity, moisture content, particle size and biomass (pine bark and sewage sludge), on the performance of the gasification process using fixed bed downdraft reactor. The experiment is to identify and optimize the behavior of the conversion process. The study will also enhance the effect of operating and design parameter by means of multi factorial design experiment.

Pine bark sewage sludge

heated above 100  C, and further increasing to 200  C, lowering molecular weight and volatilized [7,9]. The rate of drying depends on the surface area of the feedstock [10] used in the gasification process.

Pyrolysis zone Pyrolysis is a complicated process, which involves decomposition of biomass. During pyrolysis the feed stock

Results obtained from the study, while the reactor diameter increased, the flame velocity, biomass consumption and the fuel/ air equivalence ratio will slightly increase. Gasification of high moisture content biomass it leads to reduce the gasification temperature, high consumption biomass. If using the higher particle size biomass led to lower consumption biomass, maximum gasification temperatures, and reduction of flame velocities. While increase the air flow rate, it will shift over from gasification to combustion. The gasification process will transfer when the flame velocity reaches maximum.

molecules are decomposed into gases, tar, and char, at the temperature range of 200e700  C as shown in Fig. 3. Depending upon the biomass feedstock, the decomposition process releases solid charcoal, liquid tar and some inert gases. In the wood feed stock large size biopolymer like cellulose, hemi-cellulose, and lignin are converted into carbon or medium size volatile matter. Normally pyrolysis process takes between temperature of 150e500  C.

Please cite this article as: Ramalingam S et al., Recent advances in the performance of Co-Current gasification technology: A review, International Journal of Hydrogen Energy, https://doi.org/10.1016/j.ijhydene.2019.10.185

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Layout

Description

Feed Material

Result

Compare the fixed bed and fluidized bed reactor. Properties preparation of biomass feedstock plays a major role of selecting the gasifier system. Development of gasification system is to reducing the green house gas by altering the fissile fuel.

Wood

The basic design parameters for complete gasification system are feed stock properties and feed stock pre-treatment. The down draft gasifier produces the lower amount of tar content than the up draft gasifier. The gasifier has a filtering effect which leads to produce lower particulate content of gas.

Reactor: Co gasification system Down draft gasifier, pilot scale operated capacity 200 kW. Biomass: wood sawdust, sunflower seed combined with pellets. The biomass is fed at the top of the gasifier by using a screw conveyor Gasification agent; air. Wet ash removing system

wood sawdust pellet and sunflower seeds pressing.

Co-gasifier achieved best syngas compositions like H2 17.2%, N2 46.0%, CH4 2.5%, CO 21.2%, CO2 12.6%, and C2H4 0.4%, specific gas production (2.2e2.4 N m3 kg1) and cold gas efficiency in the range of 67.7 e70.0%

Down draft fixed bed type reactor is used for gasification process. The 20 wt% dried sewage sludge is an effective feedstock for energy conversion process. The sewage sludge is collected from water treatment plant. Biomass is blended with different ratio to feed into gasifier

wood chips dried sewage sludge. Wood chips dimension is 35 mm length, 10 mm width, 2.5 mm thickness.

The results obtained from the gasifier is maximum sewage feedstock is 30% in the ratio. If more than 30% sewage is leads to blockage of gasifier. The equivalence ratio factor is highly influence to produce the cold gas efficiency. If feedstock is high moisture content the cold gas efficiency is lower. The maximum cold gas efficiency is reached at the optimum equivalence ratio of 0.386.

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Please cite this article as: Ramalingam S et al., Recent advances in the performance of Co-Current gasification technology: A review, International Journal of Hydrogen Energy, https://doi.org/10.1016/j.ijhydene.2019.10.185

Table 2 e shows the previous development of gasification process in the Feeding System. Development Gasification Feeding System [22,24,28]

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Table 3 e Shows the recent developments of gasification process using Multi-stage air supply system. Development in Multi stage Air Supply [32,34] Layout

Description

Feed Material

Result

Reactor: experimental investigated biomass gasification using down draft gasifier with different operating condition. Air is supplied in two different conditions like primary and secondary conditions to get higher syn gas calorific value. To reduce the Syn gas temperature by using two separate heat exchanger. Biomass is preheated using the gasifier surface heat to dry the wood chips. Cyclone separator is used to clean the syn gas.

Wood chips

The constant equivalence ratio 0.25 is while operating the gasifier and the air is used as gasification agent. Calorific value of syn gas is obtained in the range from 4.3 MJ/ m3 to 5.5 MJ/m3. The biomass which has lower moisture content having higher calorific value. Gasification has cold gas efficiency varied in range from 45.6% to 61.9%, but hot gas efficiency from 51.9% to 69.3%.

 Reactor: down draft gasifier, operates air to biomass ratio, variable operating parameters like pressure, gas velocity, temperature and gas composition.

Different kind of wood chips

The thermal equilibrium model is developed to analyze the effect of air to feedstock ratio during the gasification process. The equilibrium and simulation models can be used as tool to achieve suitable design of gasifier to get clean gas. Analysis of temperature parameters and effect of heat energy loss by wall can be reduced with appropriate material for heat resistant to create gasifiers.

Biomass is preheated, different kind of woodchips to produce the syn gas. Air is supplied with 5 different nozzles. Cyclone separator is used to eliminate the large particles in the syngas. Based on the temperature variations the gasifier zones were differentiated. CFD model is developed to improve the gasifier performance.

Oxidation zone In the oxidation zone the volatile matter present in the biomass is oxidized under exothermic chemical reaction. It generates high heat at a temperature of 1100e1500  C with some residues. Oxidation zone is very important of the gasification process because the quality and efficiency of the process will decide at this stage. The heat generated from the combustion stage is used for pyrolysis and drying zone in the gasification process.

Reduction The partial combustion products CO2 and H2O obtained from oxidation zone are now passed through reduction zone. CO2 and H2O are reduced to form carbon monoxide (CO) and hydrogen (H2) by absorbing heat from the oxidation zone [5]. Oxidation zone raises the temperature of reduction zone to promote the gasification process which has higher activation energy. Over 85% of CO2 is

reduced to CO at temperature above 1000  C. The other reaction with carbon/steam gasification occurs at lower temperature between 500 and 600  C. The principal reaction in the reduction zone is that of carbon dioxide with hot carbon to produce carbon monoxide and this is reaction is called an endothermic reaction.

Development of gasifier Development of Co-Current Gasifier involved in modification of design, process parameters and feedstock characteristics [11]. The recent developments in the gasifier is as shown in Fig. 4. These methods are playing a major role in generating quality of producer gas and efficiency of the gasifier [12]. Number of researchers across in the world put their effort to improve the Co-Current gasifier and a prominent advancement has been reached as yet. Repeated the experimental process have been conducted to optimize the quality of producer gas and efficiency [13].

Please cite this article as: Ramalingam S et al., Recent advances in the performance of Co-Current gasification technology: A review, International Journal of Hydrogen Energy, https://doi.org/10.1016/j.ijhydene.2019.10.185

8

Development Gasification Preheated [32,35,37] Layout

Description

Feed Material

Result

Reactor: down draft gasifier, dual fire gasification to produce clean and pure producer gas. Recycling the waste heat from the gas, hot air injection to improve the gasification performance and reduce the impurities. Double wall insulator layer to reduce the heat loss. Three reactors are used to reduce the tar content to produce clean gas.

Wood

The two-stage gasifier generates the gas with a tar content of less than 25 mgNm3. The gas production rate is 2.78 Nm3 kg-1 The improved dual fired downdraft system produced high calorific gas is 5.3 MJNm3. The specific fuel consumption is 1.1 kg of fuel wood per kWh with the normal value of 1.5e1.6 kg kWh1.

Co- gasification fixed bed reactor is used. Biomasses for gasification are wood pellets and chicken manure. The test carried out two phase, first phase wood pellets and raw pre-treated chicken manure is used, during second phase both biomass are pellet form. The gasifier having the feed stock of 5 kg/h capacity.

Wood pellets chicken manure

The syn gas has been precipitate by using co gasification methods. Among the two phases the second method of gasification produce better quality syn gas compare to the first method. The chicken manure can replace the wood pellet consumption, and hence the co gasification method is key for syn gas production from the chicken manure.

Raw and torrefied biomasses are used as a biomass feed stock in fluidized bed gasifier. The important operating parameters that are affecting the heat transfer inside the gasifier such as gasification temperature, excess air ratio, biomass feeding point and steam applied the relative outcomes of bed pressure throughout the gasifier. Improve the gasifier design to get better efficiency.

Wood chips

The raw biomass and torrefied grassy biomass are tested in the gasifier. The results are concluded such as gasification temperature is raised in both biomasses. Due to to-refication the physical and chemical properties of biomass were changed, and torrefied biomass have low yield and carbon conversion.

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Table 4 e Shows developments of gasification process using Pre-heaters.

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Design improvements To enhance the efficiency of the gasifier, the reactor design of the gasifier has been improved. Several modifications in the reactor design have been discussed by many of the researchers and it is listed in Table 1. The modification in the reactor design were done on the feeding system, air supply system, gas recirculation system and discharge system. The biomass feeding system is done by automated screw or belt conveyor system [14,15]. Multi stage air supply system is used instead of single air supply system. Utilize the producer gas in the recirculation system, therefore drying zone does not required additional heat from oxidation zone [15]. Discharge system can be automated by using grate system and ash handling system. Table 1. Shows the developments in gasification the rector design system and its influence on the performance [17].

Feeding system In order to get continues gas flow in the outlet of the gasifier, feed stock hopper is attached at the top of the gasifier [18]. The feedstock loaded in the hopper can also automated by using conveyors. This helps to get a continuous feeding of feedstock from the hopper to gasifier reactor [27], so that manual loading time can be reduced [19,20]. A pneumatic type feeding conveyor system [21,22] and belt conveyor [23,24] can be used for above purpose. Table 2 shows the previous development of gasification process in the Feeding System. Depending upon the size of the feed stock the feeds system is selected [25,26] for the gasifier. The automated feeding can reduce the feedstock loading time and also provide continuous gas output.

Air supply system Air is a one of the gasification agent used in the gasification process. Ratio air fuel mixture is the important key factor in the thermo chemical process of the gasifier. The way of supplying of air can also improve the performance of the gasifier, further modification. The various methods for supplying of air to gasification are discussed below.

Multi-stage system. Lalta Prasad et al. [26] discussed the results of Co-Current reactor gasifier with sir supply modification of two stage air supply unit such as primary and secondary. The primary air unit is located at 300 mm from the top of the grate and the secondary unit is supplied air at 400 mm above the primary air unit. Table 3 shows the recent developments of gasification process using Multi-stage air supply system. The similar modification work is used with eucalyptus wood as a feedstock [27,28]. The two stage air unit increases the oxidation process [29], so that tar content is reduced in the producer gas [30]. Increase in the pyrolysis zone temperature, will help to convert the high density feed material into low density feed material. It has been reported [31,32] are indicated that reactor with two and more than two stage air supply unit improves the reactor performance with four stage air unit, primary stage air supply feeding system with a tail pipe along with vertical direction of the reactor and the secondary air unit supply the agent in five nozzles an around the reactor circumference

9

[33] also improved the performance. The multistage stage air unit can maintain the uniform temperature in the oxidation zone and reduction zone to enhance the chemical rector [34,35].

Preheating system. Heating the air will improve the performance of the gasifier. The air agent is heated before entering to the reactor by using electric heater or heat of producer gas can be used any modification [36]. Electric heater is installed in air supply line and it does not repair the reactor [38]. Table 4 shows developments of gasification process using Preheaters. Heating of air will raise the temperature in drying zone, pyrolysis zone and the oxidation zone which in turn reduce in the grate section [39]. Re-circulating system Recalculating the producer gas is the promising method [40] for improving the gasifier. The main objective of the installation of recirculation system is to utilize the heat from the producer gas to remove in moisture content of feedstock [41] this can be achieved by providing separate feeding system hopper. Table 5 shows that various in recirculation gas system in the gasifier. Utilizing the producer gas heat also additional benefit in reducing the temperature of the producer gas [42].

Discharge system Discharge system can be divided into two categories such as grate system and ash handling system [43]. The purpose of grate system is to hold the feed stock material during the chemical conversion process and guide the ash to flow down to the pit. After that removing the ash and char from the pit by the ash handling system [44]. Table 6 shows various methods used in discharge System. It has been reported that in the grate system can be done by shaking [45,46] vibrating, rotating [47], and reciprocating the grate. This will prevent bridging and channeling in particularly using [48] of low density biomass material in the gasifier. The grate unit is operated manually for shaking the grade and electrical motors can be used for vibrating and reciprocating the grade [49,50]. Screw or belt and pneumatic conveyor can be utilized in the ash handling system to improve the gasification.

Process parameter The gasifier performance can be improved by various operating parameters. The parameters are gasification agent, equivalence ratio, feeding rate and gasification temperature. Operating the gasifier system is an important parameter, Table 7 Shows recent modifications of the process parameter in the gasifier.

Gasification agent The quality and the quantity of the producer gas not only depend on the feed stock characteristics, it depends upon the reactor type the gasification agents. Generally air, steam, oxygen are used as a gasification agents [53]. Table 8 shows the improvements of gasification process using different gasification agents. The main objective of gasification agent is to

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10

Development Gasification Recirculation System [40,42] Layout

Description

Feed Material

Result

Reactor: down draft gasifier, dual fire gasification to produce clean and pure producer gas. Recycling the waste heat from the gas, hot air injection to improve the gasification performance and reduce the impurities. Double wall insulator layer to reduce the heat loss. Three reactors are used to reduce the tar content to produce clean gas.

Wood

The two-stage gasifier generates the gas with a tar content of less than 25 mgNm3 The gas production rate is 2.78 Nm3 kg-1 The improved dual fired downdraft system produced high calorific gas is 5.3 MJNm3. The specific fuel consumption is 1.1 kg of fuel wood per kWh with the normal value of 1.5e1.6 kg kWh1.

Biomass gasification with different operating conditions is carried out in fixed bed updraft reactor type gasifier. The effect of gasification temperature, equivalence ratio, and addition of catalyst in the gas efficiency and tar yield were investigated. The gasifier consist of refractory steel tube having diameter of 81 mm and height of 1000 mm the reformer is made up of quartz material. The dimensions of reformer are 31 mm diameter and height 500 mm. The gasifier having two electrical furnaces to provide heating and reforming reactions. Air is used as gasification agent.

Pine sawdust

The results from the tests are the H2 and CO, gas yield and LHV is increased, and also tar yield and CH4, CO2, C2H2 are decreased. After using the catalyst the gasification efficiency is increase by 17%e54% at the temperature of 750  Ce950  C. The catalyst is influence the hydrogen yield and also decreases the formation of CH4, CO2, C2H2. Copper slag catalyst will diminish the tar yield to increase the gas quality. The Copper slag catalyst is a good catalyst to increase the performance of gasification.

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Please cite this article as: Ramalingam S et al., Recent advances in the performance of Co-Current gasification technology: A review, International Journal of Hydrogen Energy, https://doi.org/10.1016/j.ijhydene.2019.10.185

Table 5 e Shows that various in recirculation gas system in the gasifier.

Development Gasification in Discharge system [43,45,47,49,50] Layout

Description

Feed Material

Result

Reactor: down draft gasifier Additional design parameters are listed Ash handling system, cyclone separator, rotary stirrer, ash scrapper, And electric air heater is used. Pyrolysis Tar Cracking zone consists two cylinder unit, extended to downward from the top of the gasification. The specific air input rate of 542 kg of air/ h-m2.

Wood

Maximum tar cracking temperatures is around 1100  C. Average volumetric levels of major combustible product gases are 22% CO and 11% H2. Hot and cold gas efficiencies are 72% and 66%, respectively.

Analysis the gasification process effect of design and operating parameter, particularly reactor design, equivalence ratio and biomass feed rate, on the performance of the gasification process with three stage air supply in fixed bed reactor. The gasification of corn straw was carried out in the gasifier pressure, gasifying agent. Using air supply system and rotating grate can avoid bridging and channeling. The gas composition and tar yield are affected by the parameters including equivalence ratio (ER) and biomass feed rate.

Corn starw

The test results shows that three stage of air supply can yield a high and uniform temperature in the oxidation and reduction zones for best tar cracking. While Increase feed rate it will increase the biomass consumption which resulting in increase the temperatures. So that, particularly high feed rate is no use for biomass gasification cracking and reforming reactions, which will give reduction of H2 and CO content in gases and an increase in tar yield.

(continued on next page)

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Table 6 e Shows various methods used in discharge System.

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Development Gasification in Discharge system [43,45,47,49,50] Layout

Description

Feed Material

Result

Using different refractory materials evaluate the slagging gasification conditions. Refractory probes were exposing through up to 27 h in atmosphere. Slag infiltration depth and microstructure is tested using SEM EDS. The fused cast materials are least affected, if it is dissolution and slag penetration could still be observed the heat.

Bark and peat powder

The zircon brick shows that failure by dissolution of the binding multiple phase which led to removal of zircon grains from the material. If the ash slags come to contact with material probes, refractory components dissolve and change the composition slag. The slag composition from the graphite probe was assumed to be the true composition of the ash slag, due to the lack of components probe that could be dissolved slag.

Down draft fixed bed type reactor is used for gasification process. The 20 wt% dried sewage sludge is an effective feedstock for energy conversion process. The sewage sludge is collected from water treatment plant. Biomass is blended with different ratio to feed into gasifier

wood chips dried sewage sludge. Wood chips dimension is 35 mm length, 10 mm width, 2.5 mm thickness.

The results obtained from the gasifier is maximum sewage feedstock is 30% in the ratio. If more than 30% sewage is leads to blockage of gasifier. The equivalence ratio factor is highly influence to produce the cold gas efficiency. If feedstock is high moisture content the cold gas efficiency is lower. The maximum cold gas efficiency is reached at the optimum equivalence ratio of 0.386.

Fixed bed down draft gasifier is used to generate the producer gas by using a 100 kg/h downdraft gasifier system. Biomass for gasifier is olive pits for clean synthesis gas production. Biomass gasification system is a suitable process for the production of clean energy generation in the form of electricity or heat; process can reduce greenhouse gas and facilitate to complete of the carbon cycle.

Wood

Test results shows that briquetted olive pits could be converted by downdraft gasifier to produce clean syngas with a calorific value of around 5 MJ/Nm3. Hot gas efficiency of the gasifier was calculated. Results identified that gasification of dry and oil free olive waste pits for energy generation is suitable by small scale downdraft gasifiers with addition of good designed grate mechanism and air distribution in the reaction bed.

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Table 6 e (continued )

Development in process parameters [49,51,52] Layout

Description

Feed Material

Result

Reactor: down draft gasifier, steady state and transient state gasification mathematical model has been developed, and simulate the model. With different influencing variable operating parameters. The model will identify the best gas composition The steady state analysis is deals with higher equivalence ratio and lower steam biomass ratio which will produce higher reaction temperature and finally produce high yield of char conversion.

Wood

The results were get form the gasification model is if steam and biomass ratio is 0 and mass flow rate of biomass is 20.9 kg/ h, then the char conversion rate increased 76%e100% because of equivalence ratio is increased around 0.39 to 0.43. If steam and biomass ratio is increased in the range of 1e4. And other factors are same as like ER ¼ 0.43 and mass flow rate of biomass equal to 20.9 kg h1, char conversion rate is decreased because of steam and biomass ratio.

Gasification process was analyzed thermodynamically. The system is coupled with chemical loop combustion. In this experiment steam and CO2 are used as a gasification agent. Gas composition and energy requirement were identified with different region reactor.

Wood chips

The maximum energy is delivered at 650  C and 1 bar pressure in coal gasification process. Balancing of mass can be done by using air reactor. The net energy is obtained by individual energies of process components. The maximum exothermic energy of whole process is 390.157 kJ the total gasification energy is calculated by sum of gasification enthalpy and preheating energy.

Biomass from the palm oil mills used for gasification system, gasification system has ca capacity of 50 kW. Experiments were carried out and compared with equilibrium model to identify the optimum operating parameter. Batch type reactor is used to feed the biomass into the gasifier. Experiments were carried out under atmospheric condition. Gasifier reactor size is 1000 mm height and 400 mm diameter and the reactor throat angle is 70 .

Palm fronds

Testing of gasifier is carried out with refractory cement coating in the thickness of 25 mm due to avoid the gasifier energy losses. The OPT feedstock has a 29% of moisture content, so that the hydrogen yield, cold gas efficiency. From the test results, shows that high moisture content produce less calorific value producer gas. When oxidation zone temperature is increase the gasification efficiency will also increase.

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Table 7 e Shows recent modifications of the process parameter in the gasifier.

14

Development Gasification Agent [53e55] Layout

Description

Feed Material

Result

Reactor: Co gasification system Down draft gasifier, pilot scale operated capacity 200 kW. Biomass: wood sawdust, sunflower seed combined with pellets. The biomass is fed at the top of the gasifier by using a screw conveyor Gasification agent; air. Wet ash removing system

wood sawdust pellet and sunflower seeds pressing.

Co-gasifier achieved best syngas compositions like H2 17.2%, N2 46.0%, CH4 2.5%, CO 21.2%, CO2 12.6%, and C2H4 0.4%, specific gas production (2.2e2.4 N m3 kg1) and cold gas efficiency in the range of 67.7 e70.0%

Compare the fixed bed and fluidized bed reactor. Properties preparation of biomass feedstock plays a major role of selecting the gasifier system. Development of gasification system is to reducing the green house gas by altering the fissile fuel.

Wood

The basic design parameters for complete gasification system are feed stock properties and feed stock pre-treatment. The down draft gasifier produces the lower amount of tar content than the up draft gasifier. The gasifier has a filtering effect which leads to produce lower particulate content of gas.

Down draft fixed bed type reactor is used for gasification process. The 20 wt% dried sewage sludge is an effective feedstock for energy conversion process. The sewage sludge is collected from water treatment plant. Biomass is blended with different ratio to feed into gasifier

wood chips dried sewage sludge. Wood chips dimension is 35 mm length, 10 mm width, 2.5 mm thickness.

The results obtained from the gasifier is maximum sewage feedstock is 30% in the ratio. If more than 30% sewage is leads to blockage of gasifier. The equivalence ratio factor is highly influence to produce the cold gas efficiency. If feedstock is high moisture content the cold gas efficiency is lower. The maximum cold gas efficiency is reached at the optimum equivalence ratio of 0.386.

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Please cite this article as: Ramalingam S et al., Recent advances in the performance of Co-Current gasification technology: A review, International Journal of Hydrogen Energy, https://doi.org/10.1016/j.ijhydene.2019.10.185

Table 8 e Shows the improvements of gasification process using different gasification agents.

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Table 9 e Shows the advantages of different agents [56e58]. Agent Air

Oxygen

Steam

Benefits Medium range of Residue and Char content. Enhance the partial combustion in gasification Minimize the residue and enhance the H2, CO and CH4 in gas. Improve the chemical conversion efficiency. To increase the Heating value of producer gas, H2 rich in producer gas. Reduce the tar content.

15

Feedstock size The properties of producer gas are influenced by the size of the feedstock. Usually fixed bed reactor feedstock size is 2 cm [67]. It is reported that the smaller size feedstock producing higher energy compared to large size feedstock. Since smaller size feedstock heat transfer rate is high [68,69]. Table 12 shows the different feedstock used in the gasification process. Using of larger size feedstock in the reactor, induces bridging and starting problem, and thereby reduces the efficiency of the gasifier. Further it also produces high residue, resulting which consumption rate of feedstock will increase.

Feedstock moisture content convert the feed stock into bio gas. In case of rich mixture fuel is accumulated in the oxidation zone, excess of oxygen needed and it will provided gasification agent. Advantages of different gasification agents are shown in Table 9.

Equivalence ratio Equivalence ratio is one of the most important process parameter in the gasification process since it will directly influence efficiency. Fig. 5 shows the effect of equivalence ratio on mole fraction of the producer gas. Proper air and fuel ratio has required maintaining the stoichiometric combustion process. Table 10 Shows the recent developments of gasification process with Equivalence ratio. If air fuel ratio, increases, then it increases the reaction temperature and decrease the efficiency of the process when the ratio reduced and it will produce the more carbon dioxide [59]. In order to get a good efficiency of gasification process the equivalence ratio must be maintained in the range of 0.2e0.4.

Moisture content of the feedstock is the important factor, which can affect the efficiency directly in the gasification process and quality of the gas. It also reduces the calorific value of the producer gas. Moisture content range of 20% is suitable for gasification process. Feedstock contains more than 20% moisture content having higher H2 and CO in the producer gas [72].

Feedstock in briquette method A compressed piece of combustible feedstock consists of waste products from agriculture or combined with coal. Utilization of briquette feedstock can reduce emission and quantity of fossil fuel [73]. In developed countries briquette feedstock made from waste wood dust, which can replace the firewood. The briquette feedstock gasifier produces constant flow of gas and good quality of producer gas. Table 13 shows the recent methods of briquette feedstock used for gasification process. The efficiency of briquette type feedstock is high for 5% moisture content. But the fire wood feedstock having more than 20% moisture has low efficiency.

Feeding rate

Co-gasification

Biomass feed rate is directly proportional to the gasification agent and inversely proportional to the biomass size [64]. The gasification agent flow rate increases with the oxidation reaction. The feed rate can be controlled using the automated feeding system. In case of manual feeding, the briquette type feedstock can be used or use similar weight feedstock to control the feed rate in the gasification process.

Two or more than two feedstocks are combined together and producing gas is called co-gasification method. Feedstock can also made through briquette method with binding agent for

Gasification temperature Temperature of the gasification process is depending upon the equivalence ratio. The equivalence ratio, increases with [65] temperature of the gasification process. Increasing the gasification temperature will increase the yield of producer gas efficiency [66]. Gasification temperature is always in varying nature, because of nature of bed, heat obtained oxidation process and supply of air in the gasification chamber.

Feed stock characteristics The feedstock is influenced by its characteristics such as char composition, feedstock density, and moisture content [68]. Table 11 shows the study in the feedstock characteristics. The feed stock characteristics which are mainly involved in the performance of gasifier are discussed below.

Fig. 5 e Effect of equivalence ratio gasification process [7].

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16

Development Gasification in Equivalence Ratio [60e63] Layout

Description

Feed Material

Result

The gasification reactor is down draft fixed bed type, operating with atmospheric pressure with air as agent. The corn straw is used as biomass for gasification process so that it is called as non woody biomass. The performance effecting parameters are temperature, producer gas composition with respect the heating value and tar concentration of producer gas and rate of gasification efficiency.

Corn straw

The equivalence ratio (ER) is the important operating parameter of gasification process, if ER increase or decrease they affect quality of producer gas and gasification efficiency. The perfect value of ER in the rage of 0.28 e0.32, the low heating value of producer gas is 5.39 MJ/Nm3, gasification yield around 2.86 Nm3/kg, efficiency is 73.61% and tar concentration of 4617 mg/Nm3 the above values are grab from ER.

Down draft gasifier is used as a reactor. The anaerobic digestion by products is digestate. The digestate consider as a used as a biomass for gasification to produce a syngas. The gasifier perform in the temperature range of 600  Ce800  C.with the maximum air and biomass ratio 0.25 to 0.30

Wood

The good quality of producer gas was achieved at the temperature of reached at 800  C. The gold gas efficiency and the quality of producer Gas increased with an average ER of 0.28.but the tar content is reduced to 1.61 g/N m3 with ER of 0.30.

Gasifier use down draft type reactor, with double stage variable of air supply. The supplying the air is controlled and measured. The double stage air supply system is to improve the quality of gas and reduce the tar content presented in the gasifier. The gas flow variation between the primary and secondary stage air flow will give the proper air distribution in the gasifier.

Eucalyptus wood. Cylindrical shape 6 cm.

The double stage air supply is increase the tar conversion rate. The flow air is the essential parameter to operate the gasifier and it will control the biomass consumption, gasification rate and equivalence ratio. The double stage gasification system reach the producer gas range of CO-19.04, CH4-0.89 and H2 e 16.78% when the air flow of 20 Nm3 h1 and an AR ratio is around 80%. The above condition producer gas had calorific value of 4539 kJ Nm3

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Table 10 e Shows the recent developments of gasification process with Equivalence ratio.

Wood

The equivalence ratio will affect the producer gas calorific value. If equivalence ratio is increase it will reach a peak in initially and then reduced with further increasing of equivalence ratio. The cost of gas per unit weight of fuel directly proportional to the equivalence ratio. The conversion is fully recorded that the complete carbon conversion to the gaseous fuel is not happen further increase of above the optimum equivalence ratio.

Gasification process can convert the any type of biomass in to useful energy, but the oil palm fronds are very changeling one to convert the useful energy. In the present study down draft fixed bed gasifier is used. The amount of gas yield, ash, and char contest were measured. Cleaning of gas unit also is analyzed.

Palm fronds

The experiment is carried out 12 kg of fuel, airflow rate is 200 lpm. Experiment is carried out 110 min. The fuel feed rate is 6.5 kg/h. Temperature of oxidation zone is in the range of 800◦C-1200  C. after cleaned tar value is 1.92 g/Nm3. Oil palm fronds also having the capable, as same the biomass like wood, hazelnut shell.

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Down draft gasifier operated with furniture wood and wood chips. The effects of operating parameter were investigated in this paper. The main effective operating parameter is equivalence ratio, what will happen it will increase and decrease. Identify the best performance of operating variable.

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Development in Feedstock Characteristics [69e71] Layout

Description

Feed Material

Result

Fixed bed reactor is used, with different air velocities, and the different composition of biomass mixture. The biomass mixture consists of woodchips and sawdust. The biomass mixture is prepared by the following ratios (0, 30, 70, and 100% of sawdust, wt%). The gasification experiments were carried out small scale bed reactor.

Woodchips and sawdust

During the performance test in the biomass mixture. Test identified that more amount of saw dust were went out and escaped from the chamber due to the light weight. The energy loss in the biomass because of the weight reduction when the drying process.

Fixe bed down draft, throat type gasifier is used to generate the combustible gas. The gasification system is combined with diesel engine to analyze the producer gas performance and emission characteristics by dual fuel mode. The orifice meter is use to measure the gas flow rate. The engine test is carried out various load condition in single cylinder water cooled direct injection four stroke diesel engine.

Cotton stalks Bagasse Rice husk Rice straw Wood chips

The diesel engine can able run efficiently in dual fuel mode operation. By using the producer gas and diesel fuel in the engine, the break thermal efficiency is increase by 40% than the diesel, due to methane presents in the producer gas. Fuel consumption of the engine is reducing by 50%, while operating in dual fuel mode. In dual fuel mode operation the carbon monoxide emission is increase than the diesel fuel in all type of conditions, however the nitrous oxide emission is low when compare to the diesel fuel, without any engine modification.

Biomass gasification process is to generate power. Different type of biomass feedstock is used. Down draft fixed type reactor is used. The experiments carried performance of gasifier with different feedstock and feedstock loading to identify the optimum equivalence ratio with gasification temperature and calculate the electrical output

babul wood, neem wood and mango wood.

The temperature of the producer gas is 220  Ce240  C. The power output is 23.4, 22.17, 20.4 kVA for babul, neem, mango wood. Test identified the optimum operated equivalence ratio is 0.3134. Compare to other wood, the babul wood having better conversion efficiency and output power, because of heating value.

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Table 11 e Shows the study in the feedstock characteristics.

Development Gasification in Biomass Size [67e71] Layout

Description

Feed Material

Result

Reactor: downdraft gasifier, wood as feed stock. Air supply: manual air supply in single system. Control: air ratio 0.3 to 035 for gasification Syn gas temperature is 700e1000  C is obtained. Cold gas efficiency 69e72%

wood chip sizes ranging from 3 to 5 cm

The CO2 emission as reduced. Tar content is reduced about 3.9e4.4 gNm3 compared to other gasifier. The HC emission form the gasifier is below 200 PPM. Another emission is NOx in the range of 40 PPM.

Gasifier use down draft type reactor, with double stage variable of air supply. The supplying the air is controlled and measured. The double stage air supply system is to improve the quality of gas and reduce the tar content presented in the gasifier. The gas flow variation between the primary and secondary stage air flow will give the proper air distribution in the gasifier.

Eucalyptus wood. Cylindrical shape 6 cm.

The double stage air supply is increase the tar conversion rate. The flow air is the essential parameter to operate the gasifier and it will control the biomass consumption, gasification rate and equivalence ratio. The double stage gasification system reach the producer gas range of CO-19.04, CH4-0.89 and H2 e 16.78% when the air flow of 20 Nm3 h1 and an AR ratio is around 80%. The above condition producer gas had calorific value of 4539 kJ Nm3.

Down draft reactor is used to gasification process. Sectional heating technique is used with different equivalent ratio of biomass. The main parameters that affecting the gasification process are gasification temperature, gasify agent, depend upon biomass. Sectional heating gasifier consists of four section chains.

Wood chips, Briquette type biomass is used size of Ø 5  20 mm.

The system had 8 thermocouple are used. The equivalence ratio of biomass is 0.28 in the oxidizing stage, the LHV producer gas is 4200e4600 kJ/m3. The gas volume fraction are O2-4.5%, CO210.2%,H2-14.5%,CO-23.5%,NO0.024%,NOx-0.025% and SO2- 0.032%. The sectional heating of gasifier has increase the gasification efficiency.

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(continued on next page)

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Table 12 e Shows the different feedstock used in the gasification process.

20

Development Gasification in Biomass Size [67e71] Layout

Description

Feed Material

Result

Experimental investigation is carried out laboratory scale batch type fixed bed gasification. Analyses were carried out by repeat the experiment, and maintain the input parameter constantly like air flow, moisture, size, shape of biomass. The gasification system is compared with different feed stock under transient condition. B

Jacaranda Copaia Biomass dimension is 10 mm  10 mm x 15 mm

Analysis the effect of different gasification agent by through cold gas efficiency, lower heating value, gas composition. Experiments were carried out in down draft gasifier with two stage reactor. The analysis of gasification system is extending to calculate mass balance and equivalence ratio of biomass like gasification agent.

Eucalyptus spp biomass size of 5 cm  5 cm X 5 cm

The test results show that gasifier performance is affected by the following factors gasifying agent, temperature, flame front velocity, biomass consumption rate, air/fuel equivalence ratio. While repeating the test the results were very by 18.75% because of biomass packing in the rector bed. The performance variable in thermo chemical process is flame front velocity, biomass consumption rate, fuel/air ratio, and gasification temperature. Test results were repeatable rage of 95%. The results obtained from gasification system, the cold gas efficiency is 70e75% which produce the optimum equivalence ratio 0.412 and if it is steam agent the optimum value is 0.495. Using the O2 as an oxidizing agent the tar content is reduced marginally. Compare to all gasification agent the steam can blend with O2 can produce the better gasification for two stage reactor.

international journal of hydrogen energy xxx (xxxx) xxx

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Table 12 e (continued )

Development of Briquette Gasification [72,73,75,76] Layout

Description

Feed Material

Result

Reactor: open top reactor, different feedstock Reactor working range 1.53e1.7 kW. Air supply: simple stage air supply. Feeding system: manual feeding system. Discharge system: manual discharge system.

(wood, groundnut shell briquettes), dia. 16 cm, and high 47 cm.

The reactor having 35% thermal efficiency. The max. flame temperature is reached 763  C by through cashew nut as feedstock The emission in the rage of 3e6 PPM of CO. 17e25 PPM of CO2.

Reactor: down draft gasifier Gasification agent: air, oxygen/steam. The biomass gasification is compared with air and oxygen/steam. Self heating reactor is used to reduce the fuel consumption and use the char as catalyst. The gas cleaning attachment having three stage spray shower.

Pin wood block as a feed stock and the Size 3 cm  3 cm X 3 cm

Hydrogen yield is improved while using oxygen/steam as gasification agent. Maximum hydrogen gas yield is achieved 45.16 g H2/kg biomass. There is no affecting the hydrogen flow rate, while increasing the feed rate.

Reactor: down draft gasifier capacity of 10 kW. The height of the gasifier 55 cm and consists of twin cylinder Stainless steel sheet. In drying zone diameter is 28 cm at height of 20 cm. The internal diameter of gasifier is 20 cm and gradually reduced end at 7 cm. In reduction zone diameter 19 cm than 23 cm secondary air passage in 5 different lines. Experiments were carried out 3e4 h. Temperature is measured in 6 different heights. Wood pellets are used as a Biomass feedstock

Wood pellet

Gasification influencing operating parameters is such as equivalence ratio, gasification temperature, and biomass moisture content. Thermodynamically equilibrium model, hydrogen rich gas output get from the wood biomass. Different oxidizing agent and different biomass with variable ratio produces hydrogen concentration. The maximum hydrogen production for air is 30.09%, oxygen 43.05% and 42.59% air-steam gasifying agent.

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Table 13 e Shows the recent methods of briquette feedstock used for gasification process.

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Test results were shows that wood block of size less than 50 mm has higher calorific value of 3.978 MJ/Nm3 and when coconut shells are mixed with wood, the calorific value obtained is highest i.e. 4.865 MJ/ Nm3. Calorific value of gas from wood blocks of <50 mm size is 3.978 MJ/Nm3. Gasification Air velocity is 2.9 m/s is optimum for wood and air velocity of 3.88 m/s is optimum for biomass briquettes

Result

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further improving efficiency of the gasifier [74]. The main advantage of co-gasification is degradable and nondegradable products can be combined together and efficiently burned to produce the gas. The best combination of feedstock is municipal waste with degradable product. Cogasification method is utilizes number of none gradable products such as waste plastic, thermo cool, waste tyre etc, with degradable products and this will reduce the environmental pollution [78]. Table 14 shows the recent methods of Co-gasification of the gasifier.

Preheated biomass Preheated the feedstock is done to increase the efficiency of the gasifier. Feedstock having more moisture content must be preheated using the heat energy from the producer gas or external source for producing the gas [75]. It is reported that without preheated high moisture feedstock reduces the gasifier efficiency and quality of the producer gas [79].

Feed Material

Comparison of various types of modified co-current gasifier with traditional type reactor

Evaluation of prototype downdraft gasifier. Gasifier is designed 20 KW capacity for generating producer gas. Feed stock for gasification is wood blocks it various sizes. The performance characteristics of the gasifier are study at different air flow rates. Performances of gasifier with other feed stocks such as agricultural waste briquettes are evaluated and their results were compared.

Development of Briquette Gasification [72,73,75,76]

Modification in the gasification reactor design is done in the feeding system, air supply system, recirculation system and discharge system. Among these methods, air supply system is the highly efficient method. It is very simple design and increases the conversion rate, there by enhances the oxidation process. Specific modification in the gasifier reactor design is shown in Table 15. The air supply system can be done into primary and secondary air supply or multi stage air supply to the gasifier. This reduces the tar content in the producer gas when supplying of more air during the oxidation zone and reduces the residue.

Process parameter The various process parameters in the gasification are gasification agent, equivalence ratio, feeding rate and gasification temperature. Among these parameters equivalence ratio and gasification agent have shown better performance when compared to other parameters. The various process parameter used in the gasification process is shown in Table 15. Depending upon the feedstock characteristics use of particular gasification agent will enhance gasification efficiency. When using different feedstock size, the correct equivalence ratio has to be chosen to improve combustion and increase the gasification process.

Feedstock characteristics

Layout

Table 13 e (continued )

Description

Wood blocks

Design improvement

Feedstock characteristics play vital role in the combustion and its characteristics are biomass size, biomass moisture, briquette biomass, co-gasification and preheating biomass. Among these moisture and briquette feedstock are giving high efficiency and better performance compared to other characteristics. The recent studies on Feedstock characteristics modification in the gasification process is shown in Table 15. It is reported that, when the feedstock is having below 20% moisture content will be giving better conversion efficiency. Further if briquette feedstock is used, it will

Please cite this article as: Ramalingam S et al., Recent advances in the performance of Co-Current gasification technology: A review, International Journal of Hydrogen Energy, https://doi.org/10.1016/j.ijhydene.2019.10.185

Development Gasification Co-Gasification [72e74] Layout

Description

Feed Material

Result

Down draft gasifier with fixed bed type reactor, and used co gasification technique. The co gasification of blended biomass with variable loading

Wood chips crude glycerol

The gasification results shows, if the crude glycerol content is increased the following output takes place CO,CH4 and tar concentration of gas is increased. In different ratio blending with crude glycerol limited to 20 (wt%)Co-gasification technique is an appropriate to handle excess glycerol produced from transesterification process.

Reactor: fixed bed down draft gasifier. Coal as feed stock, with different temperature under atmospheric pressure. Catalyst: waste egg shell is used as catalyst to improve the gasification. The performance of gasifier is analyst with addition of catalyst or without addition of catalyst. Rational kinetics parameters are fin out to achieve good conversion rate, syn gas yield.

Indonesian sub-bituminous Komisi Pemilihan Umum (KPU) coal. Egg shell

The results collate to raw coal gasification and with catalyst. The purpose of using the ES as catalyst will improve the syngas carbon conversion, conversion rate and hydrogen yield. The calcium catalytic will increase the coal gasification because of there are more than reactive chain process. The catalyst added gasification is 31% higher than the normal gasification. With the use of calcium catalyst hydrogen yield is increased about 80%.

(continued on next page)

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Please cite this article as: Ramalingam S et al., Recent advances in the performance of Co-Current gasification technology: A review, International Journal of Hydrogen Energy, https://doi.org/10.1016/j.ijhydene.2019.10.185

Table 14 e Shows the recent methods of Co-gasification of the gasifier.

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Development Gasification Co-Gasification [72e74] Layout

Description

Feed Material

Result

Gasification process is one of the process to convert the energy from the biomass. It can produce the clean fuel. Novelty of the gasification process is preheating the agriculture residue to give better efficiency. In this present study investigate gasification temperature in the range of 800Ke1200K and the equivalence ratio is 0.3 and 0.4 were used. Thermodynamic model is developed to minimize the energy loss in the conversion. Experiment is carried out using three different biomasses. Different biomass with variable equivalence ratio is used to thermodynamically analyze the process.

Palm stem Rice husks Sugarcane bagasse

The test out of rice husks sugar, sugarcane bagasse, and palm stem shows that the concentration of H2 has high values of about 21.3%e23.8% with a temperature of 1400K with equivalence ratio of 0.3. The CO formation is maximum at the temperature of 800K with the same equivalence ratio. While this is the case for H2 and CO, high CO2 concentration is reached when 12.1%e28.4% at a temperature of 400Kwith an equivalence ratio of 0.4. The thermodynamic model is conducted shows the result that indicate, the process of preheated air have an effect to increase the chemical energy efficiency of product gas.

The main objective of the study is to evaluate the effect of design and operating parameters, particularly reactor design, air velocity, moisture content, particle size and biomass (pine bark and sewage sludge), on the performance of the gasification process using fixed bed downdraft reactor. The experiment is to identify and optimize the behavior of the conversion process. The study will also enhance the effect of operating and design parameter by means of multi factorial design experiment.

Pine bark sewage sludge

Results obtained from the study, while the reactor diameter increased, the flame velocity, biomass consumption and the fuel/air equivalence ratio will slightly increase. Gasification of high moisture content biomass it leads to reduce the gasification temperature, high consumption biomass. If using the higher particle size biomass led to lower consumption biomass, maximum gasification temperatures, and reduction of flame velocities. While increase the air flow rate, it will shift over from gasification to combustion. The gasification process will transfer when the flame velocity reaches maximum.

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Table 14 e (continued )

Design Modification Modification Part Basic Design of Co-current Gasifier reactor

Air Supply System

Reactor Design

Process parameter modification Basic Process parameter used in Co-current Gasifier reactor

Modification Part Gasification Agent

Equivalence Ratio

Modified design of Co-current Gasifier rector

Description The downdraft gasifier with double stage of air supply was designed and built by the company has an internal diameter of 0.3 m and a height (from the reactor top to the grate) of 1.06 m. The equipment is aimed to produce fuel gas from wood and other carbonaceous materials, with low tar (<35 mg Nm3 in the reactor output) and particulate matter (<10 mgNm3 in the bag house filter output), compatible with RICE. The gasifier is built of carbon steel with an internal coating of refractory material.Improve the quality of the producer gas in a downdraft gasifier [96]. When the equivalence ratio (ER) and the air flow ratio between the stages are carefully selected, a slight increase in the gasifier efficiency can be observed. The two stage air supply effect on the tar and particles content in the producer gas is a consequence of the temperature increase in the pyrolysis and combustion zones [98]. The temperature increase in the pyrolysis zone is much greater and finally leads to the observed increase in the temperature in the combustion zone. Reactors were constructed using refractory cement surrounded by a stainless steel tube. Air supply was controlled and measured by a flow meter, As the reactor diameter increased (more adiabatic reactor), the flame front velocity, the biomass consumption rate and the fuel/air equivalence ratio slightly increased, while the producer gas quality became better (higher heating value).

Modified Process parameter used in Co-current Gasifier reactor

Description The use of a gasification agent is another factor that strongly influences gasification. The gasification agent reacts with biomass and breaks it down into gas molecules (notably, the biomass also breaks down under high temperatures through, for example, pyrolysis). Of the many gasification agents, air is the most common; although its oxygen content is only 21%, air is abundant and requires no storage equipment [97]. Pure oxygen can also be used as a gasification agent to increase the heating values of syngas. Once the reaction is initiated, these two gasification agents achieve self- sufficiency, meaning that no external energy is needed. Steam is another agent used for its ability to extract the most amount of hydrogen from biomass; however, it requires additional power input. Occasionally, CO2 is used as the gasification agent to enhance CO2 recycling and to reduce CO2 concentration in the atmosphere The results show that for gasification process, the product composition strongly depends on the amount of oxidizer or referred here as equivalence ratio.

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Table 15 e Comparison of various type of modified co-current gasifier with traditional type reactor.

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Modification Part Biomass moisture content is restricted to 20%.

Biomass Size

Briquette Biomass

Modified Biomass Characteristics used in Co-current Gasifier reactor Biomass size is changed into 60 cm height and 0.06 m diameter.

Modification of feedstock by the help of briquetting machine to produce 35 mm diameter briquettes for gasification.

Description An experimental study on an updraft gasifier (60 kWth), using large size biomass as fuel, has been carried out to obtain the temperature profile, equivalence ratio, gas composition and its heating value. The feedstock wood size was 1 m in length and 0.06 m in diameter and it was stacked 60 cm high, with a moisture content of 20%. Results for the temperature at the height of oxidation, reduction, pyrolysis and drying zones (23, 66, 78 and 92 cm, respectively) have been provided. The optimum gasifier behavior was reached with an airflow rate of 20.66m3/h (or air inlet velocity of 1 m/s) [94], leading to a producer gas heat- ing value of 4500 kJ/Nm3 and a temperature of 955 ?C at the oxidation stage. Comparison between the theoretical energy balance and thus derived from the tests have allowed for a better identification of the phenomena taking place during the particles conversion. R.N. Singh, P.R. Bhoi, S.R. Patel conduct experiment in gasification process using biomass briquettes, by using commercial briquetting machine. Using the briquette biomass for conversion process. Combustion study of 35 mm diameter briquettes made from groundnut shell was carried out in the improved metal Chula having thermal efficiency of 24%. Firstly a single layer (35 mm diameter and 12 e18 mm length) was maintained in the Chula. A small amount of diesel was spread over it for easy firing. It took 10 min for initial combustion. It was found that 1.04 kg briquettes took around 30 min for complete combustion.

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Biomass characteristics modification

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Table 16 e Heating value of CO, H2, CH4 [23]. Biomass sample Broad Bean Husk Sunflower Shell French Bean Stalk Sunflower Stalk and Stover Sourcheery Stalk Walnut Shell Almond Shell Peanut Shell Cornelian Cheery Stone Apricot Stone Peach Stone Apricot Bagasse Peach Bagasse Hybrid Poplar Ash Tree Pine Cone Soybean Cake Cotton Cake Rapeseed Potato Peel

Moisture (%)

Fixed carbon % (db)

Ash % (db)

Volatile matter % (db)

Organic matter % (db)

Heating value MJ/kg (db)

10.75 10.25 9 8.12 6 10 1.25 8.12 5.5 4 5 3.5 6.5 9 8.75 9.25 12.5 8.25 10.75 8.5

8.68 11.7 4.67 5.17 14.1 16.94 18.93 13.6 23.8 17.83 20.79 15.8 6.15 6.87 14.12 15.15 16 11.58 5.6 9.56

5.88 3.62 6.32 8.98 5.05 3.89 4.05 5.99 2.96 1.04 1.05 3.89 1.87 3.44 5.75 6.89 7.14 4.77 8.13 6.29

85.44 84.68 89.01 85.85 80.85 79.71 77.22 80.41 73.54 81.13 78.16 80.31 91.98 89.69 80.13 77.96 76.89 83.65 86.27 84.15

94.12 96.38 93.38 91.02 94.95 96.11 95.95 94.01 97.04 98.96 98.96 96.11 98.13 96.56 94.25 93.11 92.86 95.23 91.87 93.71

16.07 17.86 15.41 15.87 17.59 18.91 17.96 18.46 19.02 18.8 19.52 18.56 16.24 17.14 18.06 18.55 18.3 17.5 16.61 17.18

Table 17 e Economic stages in gasification. Author Wei ChengNg et al. [81]

 bio CodignoleLuz et al. [82] Fa

Sie Ting Tan et al. [83]

Marcio Montagnan et al. [84]

Description A downdraft gasifier is developed in a capacity of 10 kW. Co-gasification livestock 30% chicken manure and wood feedstock 70% is used as feedstock, successfully converted clean gas. Quality gas with a lower heating value (LHV) of 5.23 MJ/Nm3 is produced. Cost-benefit analysis for the system using a Monte Carlo simulation model. Solid waste from municipality is used to generate the electricity; economical analysis of municipal solid waste gasification is performed. The gasification system is consisting of primary separation, mechanical treatment, gasification, syngas cleaning and power generation. Evaluation includes present value of electricity and internal rate of return with economic of possible increase of system. The study presented the Waste To Energy from Municipal Solid Waste is calculated. Energy economic with respect to environment is a main aim of the paper. Different methods were conducted based on the waste generation and production of energy is discussed on the trade-off of both incineration and anaerobic digestion for MSWM Energy recovery from the Municipal Solid Waste management is by two methods such as landfill biogas and Waste-to-Energy plant. This study is based on urban centre using the MSW characteristics. This study also includes the evaluation of environmental impacts in energy recovery derived from MSW. Landfill as the worst MSW management option and the most promising option is the combustion of MSW for energy generation.

provide complete combustion, low residue and continuous flow of output from the gasifier.

Gasifier efficiency Gasifier efficiency can be determined by using Eq. (1) [80]. h¼

HVpgXVpg  100% HVpg

(1)

where HVpg is the heating value of producer gas (kJ/Nm3), Vpg is producer gas yields (Nm3/kg), and HVb is the heating value of feedstock (kJ/kg). The heating value of producer gas can be calculated as follows:

HVp ¼

ðx1: Hv ÞCO þ ðx2 Hv ÞH2 þ ðx3: Hv ÞCH4 100

(2)

where x1, x2, and x3 are the percentage of combustible gases such as CO, H2, and CH4 in producer gas. It can be measured using Gas Chromatograph. The proximate analysis results, total organic matter contents and net heating values of the feedstock and its shown in Table 16.

Barriers in gasification It has been noted from the various research articles that gasification has been identified as promising technology, but it

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Development Gasification coupled with Engine [75,76,79] Layout

Description

Feed Material

Down draft gasifier coupled with diesel engine measuring the performance of diesel engine, operated with dual fuel mode with the effect of bio-ethanol with thermal barrier coating. The HOME (Honge oil methyl ester) biodiesel and producer gas as dual fuel mode with 5% addition of bio ethanol in thermal barrier coating four stroke single cylinder diesel engine. Performance test were carried out at 80% load, during the test break thermal efficiency is improved when dual fuel is applied.

Babul wood

Down draft fixed bed reactor type gasifier is used to generate the producer gas. In twin cylinder diesel engine used to test the blended fuel in single fuel & dual fuel mode. The dual fuels are producer gas and karanja biodiesel with different ratio. The testing of blend fuel with two conditions. First case [K10 þ 90% disel]þ producer gas flow rate of 21.49 kg/h, and [K20 þ 80% diesel]þproducer gas. In second case same as in biodiesel ratio with different gas flow rate in constant load of 10 KW.

Babul wood 25 mm length and 25 mm diameter

Result Test resulted showed that performance is improved and emission is reduced when the engine operated with BE5eProducer gas in coating engine. The other emission and performance parameter are Smoke emission levels were list below 27.1% in HOMEe Producer gas, 12.5% BE5eProducer gas and 8.7% HOMEe Producer gas in coated engine. Test the various blending BE5e producer gas operation with coating blend shows better performance and lower emission smoke, HC and CO emission levels compared to HOMEeproducer gas operation The experimental investigate the two cases, may concluded that in dual fuel mode producer gas can replace the diesel role up to 80% of rated load. In the first case pilot fuel saving of 83% in this is high rate by the high flow rate of producer gas K20% at 8 KW load. While increase the flow rate of producer gas, the following emission parameters change is occur NOx and smoke emissions values are decrease, but the CO, CO2 and HC emission were increase in all kind test fuels. From the experimental investigation test result the blends of Karanja oil K20 and woody biomass producer gas can suitable fuel with less amount of emission in a twin cylinder diesel engine and no need to modify the engine.

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Table 18 e Shows the developments of internal Combustion Engine gasifier system.

Results obtained from the evaluation of the gasifier coupled with engine system are, cold gas efficiency of the gasifier is about 80%, and with calorific value of producer gas is 4.5 MJ/kg. Diesel consumption is reduced by 75% have shown in commercial diesel engine with dual fuel mode. The Specific Fuel Consumption is found to be about 1 kg/ kWh of biomass along with about 55 ml/ kWh of diesel. The specific energy consumption is 17 MJ/kWh in the dual fuel mode.

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has barriers to implement in the high scale in the commercial purpose. The ash generated from the feedstock is the main barrier, which affects the environment and living medium. Bridging and scaling of the residue in the reactor causes decreases the efficiency of the gasifier and damaging the components of reactor. Asadullah et al. indicated that power generation using the gasification technology with catalytic tar reduction method is successful for reducing ash pollution and can be used for commercial purpose. Zhehan., et al. evaluated the powdered crop straw in the reactor, reduces the scale and bridging formation in the reactor [79] significantly. Therefore it is necessary to identify each and every feedstock for the right method of controlling pollution scaling and bridging in the gasifier reactor. Economic aspect of gasification is an important factor and it has to implement depends upon efficiency of gasifier, performance of reactor design, initial investment, operating, labor and maintenance cost, returns of the system. The detailed of economic aspects is given in Table 17.

Performance Evaluation of diesel engine coupled with gasifier. The diesel engine is operated in dual fuel mode. Performance test is carried out both engine and gasification system. Aim of the of dual fuelling an engine is to substitute diesel by an alternate fuel, while using producer gas, it will reduce the fossil fuel consumption. The method adapted allows the mixture of air and gas into the engine cylinder and allows the diesel governor to take control on the speed.

Wood chips

Applications in IC engine The IC engines are playing major role in automobile power generation and industrial sector. Further IC engines are now facing problem of shortage/demand of fuel. Therefore researchers are working with IC engine with gas. The gasifier to be used in IC engine requires additional components, such as cyclone, scrubber, and filter for producer gas cleaning. Many IC engine-gasifier systems have been developed for different biomass feed-stocks. D. K. Das et al., developed a gasifier-IC engine system with biomass feedstock of furniture wastes. Charcoal and coconut shells are used for feedstock in the gasifier [76]. Small-scale gasifier-gas engine systems are using with feedstock of rice husk [28] and feedstock of wood chip [61] have been also reported. Table 18 shows the developments of internal Combustion Engine gasifier system. Small-scale downdraft-generator set with wood as feedstock to generate electricity was reported which low conversion efficiency of 17% due to low generator set efficiency and low calorific value of the producer gas [46,48]. Different feed stocks can be used in the downdraft gasifier-engine system, depending upon the heating value of individual feedstock [52,53,61].

Conclusions Biomass is recognized as a possible source of energy and, it can able to meet the present energy demand and supply to the modern world. Among various biomass energy generation methods, thermo chemical conversion method has very attractive and less expensive. Since it does not require any separate system. The cost involved for maintenance of this method is very minimum when compared with other process. Based on the review, the following conclusions have been arrived with respect to the cocurrent gasifier. 1. Gasifier performance is improved by providing multistage and preheated air supply to the gasifier. In multistage air Please cite this article as: Ramalingam S et al., Recent advances in the performance of Co-Current gasification technology: A review, International Journal of Hydrogen Energy, https://doi.org/10.1016/j.ijhydene.2019.10.185

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supply have two or more than two stages of air is supplied to the reactor, to increase the conversion of mass into energy and this leads to complete combustion process. The multistage air supply unit maintains uniform temperature in the oxidation and reduction zone, during the chemical reaction. 2. Gasifying agents react with solid carbon and heavier hydrocarbons to convert them into low-molecular-weight gases like CO and H2. The main gasification agents are oxygen, steam and air. Oxygen is a popular gasifying agent, though it is primarily used for the combustion step. It may be supplied to a gasifier either in pure form or through air. The heating value and the composition of the gas produced in a gasifier are based on the nature and amount of the gasification agent is used. The equivalence ratio shows two opposing effects on the gasification process such as increasing the amount of air and temperature, but at the same time, produces higher CO2. Feeding rate is directly proportional to the gasification agent, when increase feed rate and increases the oxidation reaction. Increasing gasification temperature will increase the combustion efficiency and depending upon producer gas composition, tar concentration and ash of the feedstock. 3. Improvements depend upon biomass characteristics The biomass size is important parameter during the gasification process, when the biomass size is getting smaller; the area to volume ratio of the particle is increased. The decrease of size will increase the contact with the reactant. Hence, the reaction rate increases with size of feedstock. Moisture presented in the feedstock is another important factor for the gasification performance. The moisture content reduces the Boudouard reaction and also CO content and there by decreases quantity of the producer gas. The moisture content in gasification process is removed by providing supplementary air in the reactor. The calorific value of producer gas is in the range of 2.5e6.0 MJ/Nm3 when biomass moisture content is reduced from 29% to 22% wb. Briquetting is preprocess technology which improves the handling of large quantity lower density and loose pore feedstock and it increases calorific value of feedstock. Briquette has more producer gas conversion efficiency and loose feedstock with the ratio of 8:2 by weight is the best for the gasifier. The preheating of feedstock will enhances the thermal decomposition during combustion. This feedstock allows quick conversion of the feedstock into clean producer gas through different heterogeneous reactions. The energy losses due to internal thermal energy exchange may be reduced by preheating of feedstock an also with preheated air. Based on the above it is conclude that several gasifier feedstock and process parameter have been discussed and any of researchers pointed out the advantages and disadvantages of different methods. ➢ The fixed bed Co-current method can produce clean high quality producer gas and calorific value of 6MJ/Nm3. ➢ The optimum equivalence ratio in the gasification process is in the range of 0.18e0.3.

➢ The down draft fixed bed gasifier is also suitable for both engine and thermal application due to less residue with high efficiency.

Future developments Choosing of appropriate Co-current reactor gasifier plays vital role of gasification process. Usually gasifier reactor is designed for particular feedstock and based on the operating method. Different feedstock can't used in the same gasifier. Briquette form feedstock is only method, for all type of feedstock can use in the single gasifier reactor. In order to reduce the gasifier designing cost and the pelletized feedstock processing, and mathematical modeling can be analyzed before fabrication. Computer simulation software may be used for future improvement in the real time analysis, and design of reactor. In addition to computerized analysis, optimization of data's can maintain the efficiency of the gasifier.

references

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