Ultimate analysis and several characteristics of bio-oil derived from hardwood fast pyrolysis
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Tiefenbacher",publishedDate:null,coverURL:"https://cdn.intechopen.com/books/images_new/10765.jpg",keywords:"Managing Urbanization, Managing Development, Managing Resource Use, Drought Management, Flood Management, Water Quality Monitoring, Air Quality Monitoring, Ecological Monitoring, Modeling Extreme Natural Events, Ecological Restoration, Restoring Environmental Flows, Environmental Management Perspectives",numberOfDownloads:null,numberOfWosCitations:0,numberOfCrossrefCitations:null,numberOfDimensionsCitations:null,numberOfTotalCitations:null,isAvailableForWebshopOrdering:!0,dateEndFirstStepPublish:"January 12th 2021",dateEndSecondStepPublish:"February 9th 2021",dateEndThirdStepPublish:"April 10th 2021",dateEndFourthStepPublish:"June 29th 2021",dateEndFifthStepPublish:"August 28th 2021",remainingDaysToSecondStep:"23 days",secondStepPassed:!1,currentStepOfPublishingProcess:2,editedByType:null,kuFlag:!1,biosketch:"A geospatial scholar working at the interface of natural and human systems, collaborating internationally on innovative studies about hazards and environmental challenges. Dr. Tiefenbacher has published more than 200 papers on a diverse array of topics that examine perception and behaviors with regards to the application of pesticides, releases of toxic chemicals, environments of the U.S.-Mexico borderlands, wildlife hazards, and the geography of wine.",coeditorOneBiosketch:null,coeditorTwoBiosketch:null,coeditorThreeBiosketch:null,coeditorFourBiosketch:null,coeditorFiveBiosketch:null,editors:[{id:"73876",title:"Dr.",name:"John P.",middleName:null,surname:"Tiefenbacher",slug:"john-p.-tiefenbacher",fullName:"John P. Tiefenbacher",profilePictureURL:"https://mts.intechopen.com/storage/users/73876/images/system/73876.jfif",biography:"Dr. John P. Tiefenbacher (Ph.D., Rutgers, 1992) is a professor of Geography at Texas State University. His research has focused on various aspects of hazards and environmental management. Dr. Tiefenbacher has published on a diverse array of topics that examine perception and behaviors with regards to the application of pesticides, releases of toxic chemicals, environments of the U.S.-Mexico borderlands, wildlife hazards, and the geography of wine. More recently his work pertains to spatial adaptation to climate change, spatial responses in wine growing regions to climate change, the geographies of viticulture and wine, artificial intelligence and machine learning to predict patterns of natural processes and hazards, historical ethnic enclaves in American cities and regions, and environmental adaptations of 19th century European immigrants to North America's landscapes.",institutionString:"Texas State University",position:null,outsideEditionCount:0,totalCites:0,totalAuthoredChapters:"1",totalChapterViews:"0",totalEditedBooks:"6",institution:{name:"Texas State University",institutionURL:null,country:{name:"United States of America"}}}],coeditorOne:null,coeditorTwo:null,coeditorThree:null,coeditorFour:null,coeditorFive:null,topics:[{id:"12",title:"Environmental Sciences",slug:"environmental-sciences"}],chapters:null,productType:{id:"1",title:"Edited Volume",chapterContentType:"chapter",authoredCaption:"Edited by"},personalPublishingAssistant:{id:"194667",firstName:"Marijana",lastName:"Francetic",middleName:null,title:"Ms.",imageUrl:"https://mts.intechopen.com/storage/users/194667/images/4752_n.jpg",email:"marijana@intechopen.com",biography:"As an Author Service Manager my responsibilities include monitoring and facilitating all publishing activities for authors and editors. 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Energy is a central part of every human being’s daily life. In all its forms, such as chemical energy (food), thermal energy (heat), or electricity, energy has the ability to transform the daily lives of humans across the world by easing workloads, boosting economies and generally increasing the comfort of our lives. Worldwide energy consumption has been increasing rapidly. This has been accelerated by the improvement of the quality of life that almost directly relates to the amount of energy consumed. At present, fossil fuels based energy resources, such as coal, gas, and oil supply the majority of the total world energy requirement.
The global warming owing to the emissions of greenhouse gas is the most drastic consequence of the use of fossil fuels. According to experts in the field, global warming can disturb the natural equilibrium of the Earth’s ecosystem. If CO2 emissions are not regulated, global warming can have severe consequences for environment. These consequences, although some of them are not fully corroborated, are increasing sea and ocean levels, ocean acidification, change in rainfall patterns, hurricanes, volcanic eruptions, earthquakes and plant or animal extinctions, among others.
The development of non-conventional sources like wind, sunlight, water, biomass, etc., is inevitable. Among the renewable sources of energy, substantial focus of research is currently on the use of biomass. Besides being a renewable source of energy, there are many other advantages associated to the use of biomass. It is available abundantly in the world. Its use does not increase the net amount of CO2in the atmosphere and can reduce the emissions of SO2 and NOx remarkably.
Biomass gasification is a promising technology, which can contribute to develop future energy systems which are efficient and environmentally friendly in order to increase the share of renewable energy for heating, electricity, transport fuels and higher applications.
The gasification of carbon-containing materials to produce combustible gas is an established technology. Biomass gasification is a thermochemical process that produces relatively clean and combustible gas through pyrolytic and reforming reactions. The syngas generated can be an important resource suitable for direct combustion, application in prime movers such as engines and turbines, or for the production of synthetic natural gas (SNG) and transportation fuels e.g. Fischer-Tropsch diesel.
For energy production, the major concerns about syngas are its heating value, composition, and possible contamination. The proportion of the combustible gas hydrogen (H2), methane (CH4), carbon monoxide (CO), and moisture determines the heating value of the gas. The composition of syngas depends on the biomass properties and gasifier operating conditions. For a specific gasification system, operating conditions play a vital role in all aspects of biomass gasification. These include carbon conversion, syngas composition, tars and soot formation and oxidation (Devi et al., 2003).
The main hurdles for large-scale implementation of energy production from solid biomass are the nature of biomass - non uniform, low-energy density, sometimes large ash content - together with the usual inconsistency between the local availability of biomass and the demand for biomass related products: heat, electricity, fuels and chemicals. Usually, import/transport of fossil fuels is cheaper. Pyrolysis may be a process to overcome these hurdles: biomass is transformed into a versatile liquid called bio-oil, easy to handle and to transport. This bio-oil would then be transported to centralized air/steam gasification units. Bio-oil is an intermediate product which is produced from relatively dry biomass via fast pyrolysis process. It is a liquid with similar elemental composition to its original feedstock and with high bulk and energy density.The high bulk and energy density of bio-oil can reduce transportation costs to large scale centralized gasification plants; these costs have been a detrimental factor in large scale use of solid biomass resource. Bio-oil can be produced where the biomass is available and then be transported over long distances to central processing units of similar scales as the current petrochemical industry. Besides technical and logistic advantages, this conversion chain may also give incentives for economic development and job creation especially in rural areas.
The essential features to obtain high yields of bio-oil (up to 75 wt% on dry basis) are a moderate pyrolysis temperature (500°C), high heating rates (103-105°C/s), short vapour residence times (<2 s) and rapid quenching of the pyrolysis vapours.
The combination of fast pyrolysis of biomass followed by transportation in large units for steam reforming has attracted considerable attention of the research community, as one of the most promising viable methods for hydrogen production.For the high temperature applications such as gasification, steam reforming or even combustion, it is of particular interest to understand the behavior of bio-oils during the very first step of its decomposition under pyrolysis conditions. However, only few works can be found on the understanding of processes occurring during thermal conversion of bio-oils.
The earliest combustion tests of bio-oil droplets were conducted in Sandia National Laboratory (Wornat et al., 1994).Streams of monodispersed droplets were injected into a laminar flow reactor. The experimental conditions were as follows: droplet diameter of about 300 m, reactor temperature of 1600 K and O2 concentrations of 14–33%. In-situ video imaging of burning droplets reveals that biomass oil droplets undergo several distinct stages of combustion. Initially biomass oil droplets burn quiescently in a blue flame. The broad range of component volatilities and inefficient mass transfer within the viscous biomass oils bring about an abrupt termination of the quiescent stage, however, causing rapid droplet swelling and distortion, followed by a microexplosion.
Thermogravimetric analysis (TGA) is widely used to characterize the evaporation, thermal decomposition and combustion properties of bio-oils. The weight loss process of bio-oils in inert atmospheres can be divided into two stages: the evaporation of light volatiles (<150-200°C) and the subsequent thermal decomposition of unstable heavier components (<350-400°C). In the case of TGA tests performed in the presence of air, the weight loss of bio-oils can be divided into three stages. The first two stages are similar to those in inert atmospheres and the third stage is the combustion of chars formed in the first two stages (>400°C)(Ba et al., 2004a, 2004b).
Branca et al.(Branca, 2005a) studied the devolatilization and heterogeneous combustion of wood fast bio-oil. Weight loss curves of wood fast bio-oil in air have been measured, under controlled thermal conditions, carrying out two separate sets of experiments. The first, which has a final temperature of 600 K, concerns evaporation/cracking of the oil and secondary char formation. A heating rate of 0.08 °C/swas applied. The yield of secondary char varies from about 25% to 39% (on a total oil basis). After collection and milling, in the second set of experiments, heterogeneous combustion of the secondary char is carried out to temperatures of 873 K.In another study, Branca et al. (Branca et al., 2005b) found that thermogravimetric curves of bio-oil in air show two main reaction stages. The first (temperatures ≤ 600 K) concerns evaporation, formation and release of gases and formation of secondary char (coke). Then, at higher temperatures, heterogeneous combustion of secondary char takes place. They found that the pyrolysis temperature does not affect significantly weight loss dynamics and amount of secondary char (approximately equal to 20% of the liquid on a dry basis).
Hallet et al.(Hallett et al., 2006)established a numerical model for the evaporation and pyrolysis of a single droplet of bio-oil derived from biomass. The model is compared with the results of suspended droplet experiments, and is shown to give good predictions of the times of the major events in the lifetime of a droplet: initial heating, evaporation of volatile species, and pyrolysis of pyrolytic lignin to char.
Guus van Rossum et al.(Van Rossum et al., 2010) studied the evaporation of bio-oil and product distribution at varying heating rates (~1.5×10-2–1.5×104°C/s) with surrounding temperatures up to 850°C. A total product distribution (gas, vapor, and char) was measured using two atomizers with different droplet sizes. A big difference is seen in char production between the two atomizers where the ultrasonic atomizer gives much less char compared to the needle atomizer, ~8 and 22% (on carbon basis), respectively. Small droplets (88-117µm generated by ultrasonic atomizer, undergoing high heating rate) are much quicker evaporated than larger droplets (~ 1.9 mm, generated by needle atomizer, undergoing low heating rate).
Calabria et al. carried out lots of studies on the combustion behaviors of fibre-suspended single bio-oil droplets. The droplet size varied between 300 and 1100 m and the furnace temperature changed in the range of 400–1200°C. The droplets were observed to undergo initial heating, swelling and microexplosion before ignition. During this stage, the temperature–time curves showed two zones with constant temperatures (100 and 450°C), which corresponded to the evaporation of light volatiles and the thermal cracking of unstable components, respectively. The droplets were ignited at around 600°C. The combustion of the droplets started with an enveloping blue flame. Then, the flame developed a yellow tail with its size increasing, which indicated the formation of soot. After that, the flame shrank and extinguished, and the remaining solid carbonaceous residues burned leading to the formation of ash (Calabria et al., 2007).
In air/steam gasification process the essential steps are pyrolysis, partial oxidation, cracking of tar, solid carbon residue gasification, reforming (steam and/or dry), and water gas shift to yield syngas, water, carbon dioxide, and unwanted products like tars, methane and carbon (Levenspiel et al., 2005). As a summary, a schematic representation of air/steam gasification of single droplet of bio-oil is proposed in Figure 1.
Schematic representation of air steam gasification of bio-oil droplet
The steam reforming of the bio-oil can be simplified as the steam reforming of an oxygenated organic compound (CnHmOk) following:
During the last decade, catalytic steam reforming of bio-oil components has been widely studied, focusing on acetic acid as one of the most representative compounds.
Production of hydrogen from catalytic steam reforming of bio-oil was extensively investigated by NREL (Wang et al., 1997, 1998). Czernik et al. obtained hydrogen in a fluidized bed reactor from the carbohydrate derived fraction of wood bio-oil with a yield of about 80% of theoretical maximum (Czernik et al., 2002).The catalytic steam reforming of the bio-oil or the model oxygenates (e.g., ethanol, acetic acid) has been widely explored via various catalysts, e.g., Ni-based catalysts (Sakaguchi et al., 2010), Mg-doped catalysts (Garcia et al., 2000)and noble metal-loaded catalysts (Goula et al., 2004; Rioche et al., 2005; Trimm et al., 1997).Noble metals (Pt, Ru, Rh) are more effective than the Ni-based catalysts and less carbon depositing. Such catalysts are not common in real applications because of their high cost. Catalytic steam reforming of bio-oil is a costly process and presents several disadvantages such as carbon deposit and the deactivation of catalysts due to coke or oligomer deposition even in the presence of an excess of steam (S/C > 5)(Trimm et al., 1997; Rostrup-Nielsen et al., 1997). For these reasons, there is an interest in developing non catalytic gasification of bio-oil.
Only very few works can be found on the non catalytic reforming of whole bio-oil. Bimbela et al. studied catalytic and non catalytic steam reforming of acetol (bio-oil model compound) in fixed bed at low temperature (550-750°C) in order to highlight the specific role of the catalyst in this process (Bimbela et al., 2009). The same study is carried out by Guus van Rossum et al. concerning catalytic and non catalytic gasification of bio-oil in a fluidized bed over a wide temperature range (523-914°C)(van Rossum et al., 2007). Marda et al. has developed a system for the volatilization and conversion of a bio-oil mixed with methanol to syngas via non-catalytic partial oxidation (NPOX) using an ultrasonic nozzle to feed the mixture. The effects of both temperature (from 625 to 850°C) and added oxygen (effective O/C ratio from 0.7 to 1.6) on the yields of CO and H2 have been explored. They obtained hydrogen yield of about 75% of theoretical maximum (Marda et al., 2009). Panigrahi et al.gasified biomass-derived oil (BDO) to syngas and gaseous fuels at 800°C.They obtained syngas (H2 + CO) yield ranging from 75 to 80 mol % (Panigrahi et al., 2003).Henrich et al. gasified lignocellulosic biomass.The first process step is a fast pyrolysis at atmospheric pressure, which produces large condensate that was mixed to slurries. The slurries are pumped into a slagging entrained flow gasifier and are atomized and converted to syngas at high operating temperatures and pressures (Henrich et al., 2004).
The objective of this work is to bridge the lack of knowledge concerning the physicochemical transformation of bio-oil into syngas using non catalytic steam gasification in entrained flow reactors. This complex process involves vaporization, thermal cracking reactions with formation of gas, tars and char that considered as undesirable product. This is followed by steam reforming of gas and tars, together with char conversion. To better understand the process, the first step of gasification (pyrolysis) and thereafter the whole process (pyrolysis + gasification) were studied. The pyrolysis study focused on the influence of the heating rate and the final pyrolysis temperature, for this aim, two complementary devices namely: a Horizontal Tubular Reactor (HTR) and a High Temperature - Entrained Flow Reactor (HT-EFR) were used to study on the one hand a wide range of heating rates, in the range from 2 to 2000°C/s and on the other hand final temperature ranging from 550 to 1000°C. Concerning gasification, the effect of temperature on syngas yield and composition wasstudiedover a wide range from 1000°C to 1400°C, for this aim HT-EFR was used.
Two complementary devices, namely: a Horizontal Tubular Reactor (HTR) and a High Temperature - Entrained Flow Reactor (HT-EFR), were used to study a wide range of heating rates, in the range from 2 to 2000°C/s and final temperature from 550 to 1000°C.
The experiments of fast pyrolysis were carried out in a HTR (Fig. 2). This device allowed carrying out experiments in conditions of fast pyrolysis which is not possible in a thermobalance. The reactor consisted of a double-walled quartz pipe. The length and inside diameters were 850 mm and 55 mm respectively for the inner tube, and 1290 mm and 70 mm respectively for the outer tube. The reactor temperature can reach 1100°C.
Horizontal Tubular Reactor (HTR) ready for sample introduction
The procedure carried out for an experiment was the following. First, the furnace was heated and the gas flowrate (nitrogen) was adjusted using a mass flow meter controller. When the temperature was stabilized, the sample was placed on the metal grid at the unheated section of the reactor. This section was swept by half of the total cold nitrogen flow injected, in order to maintain it cold and under inert atmosphere, and therefore avoid its degradation. Meanwhile the second half of the nitrogen flow was preheated through the double-walled annular section of the reactor as shown in Fig. 1. The sample consisted in 1g of bio-oil was placed inside a crucible of 25 mm diameter and 40 mm height for studying the effect of temperature and of ash content. In order to achieve higher heating rates, some runs were performed with 1g of bio-oil previously soaked in a refractory ceramic wool sample of 100x20 mm length and width and 3 mm thickness. The choice of this sample holder allowed increasing the exchange surface and subsequently obtaining larger heating rates. We proved that this wool has no catalytic effect on bio-oil pyrolysis. Indeed, previous bio-oil pyrolysis experiments were carried out first with a single crucible, and secondly in the refractory ceramic wool deposited in the crucible. The wool didn’t induce any change on the products yield.
The reactor outlet was first connected to an O2 gas analyser to ensure that there is no oxygen in the reactor. Afterwards, a manual insertion enabled to move the sample in the furnace at different velocities, ranging between 0.06 and 30 cm/s. The sample temperature evolution was measured using a thermocouple placed in the middle of the sample in order to determine a heating rate for each experiment. Variation of the heating rate was obtained by varying the sample introduction through the tubular reactor. Four different durations have been used: 16, 8, 4 and finally 0.03 min resulting in four different heating rates. The sample then remained in the middle of the reactor for a definite time and is brought back out of the furnace; the solid residue was weighed after cooling. Even after several experiments, no char deposit was observed inside the reactor. Only tar deposits were observed in the cold outlet of the reactor. The reactor outlet was connected to a sampling bag at t = 0 just before sample introduction. The gases formed by pyrolysis were collected in the bag. The duration of all experiments was 10 min with a 2 NL/min N2 flowrate which enabled to know accurately the volume of N2 sampled in the bag. In HTR reactor, the volume of formed gas never exceeded 1% of the volume of N2 sampled in the bag. After the experiment the bag was disconnected from HTR, and connected to the micro-chromatograph analyser (µGC). From the total volume of gas in the bag and measure of the gas concentration, the quantity of each gas formed by 1g of bio-oil can be precisely calculated.
A laboratory scale high temperature entrained flow reactor HT-EFR was used in this work. It consisted in a vertical tubular reactor electrically heated by a total of 18 kW three-zones electrical furnace, and was able to reach 1600°C in a 1m long isothermal reaction zone, as illustrated in Fig. 3.
Entrained flow reactor
The atmosphere gas is generated by feeding the controlled flow of nitrogen in a 2 kW electrical steam generator. This atmosphere gas is then preheated to 900°C using a 2.5 kW electrical battery of heating elements before reaching the isothermal reaction zone. The HT-EFR was initially set up to achieve high heating-rate gasification of solid biomass, and was equipped for the present work with a specially designed bio-oil pulverization feeder, in order to obtain a very constant mass flowrate spray.
The feeder consists of a 1 m long and 14 mm o.d. probe cooled with water at 30°C. At its end a commercial stainless steel nozzle is integrated. This allows uniform distribution with fine atomization. Nozzle type (DELAVAN WDB) is a solid cone, with orifice diameter of 0.46mm and a spray angle of 60°.
The oil is fed with a syringe which is automatically pushed. The expected mass flowrate of 0.3 g/min was too low for direct pulverization. Therefore, a 3.5 NL/min N2 flowrate was used to entrain oil in the feeding probe and to ensure a thin spray of the oil. The spray of droplets is dispersed on the section of a 75 mm i.d. alumina reactor swept by 15 NL.min-1 of atmosphere gas. The steam gasification experiments were carried out in HT-EFR with steam to fuel mass ratio (fuel includes inherent water in bio-oil) of S/F=4.5.
Reactions take place along the reactor during a controlled gas residence time, which was of about 3-4s. The residence time of droplets or solid residue after reaction is assumed to be similar to that of the gas because of the very small particle size. The gas residence time was calculated as the ratio of the reaction zone length to the average gas velocity in the reactor. At 1650 mm downstream of the injection point, gases and solid residue were sampled by a hot-oil cooled probe at 150°C. Gas and solid residue were separated using a settling box and a filter, both heated to avoid water condensation. The water and potential remaining tars were first condensed in a heat exchanger, and non-condensable gases were forwarded to a micro-chromatograph analyser (µGC) to quantify H2, CO, CO2, CH4, C2H2, C2H4, C2H6, C3H8 and C6H6. The µGC offers excellent resolutions of all analyze species at higher concentrations with repeatability of ± 2 percent relative standard deviation, the system offers also a minimum detectable quantity of about 10 ppm for most gases species.
Gases were also analyzed by other analyzers that allowed checking the absence of O2, to confirm the analysis and to control continuously gas production: a Fourier Transform InfraRed (FTIR) analyser, a Non-Dispersive InfraRed (NDIR) analyser coupled with a paramagnetic analyser for O2 and a Thermal Conductivity Detector (TCD) to quantify H2.
The feedstock used for all experiments was a bio-oil produced by fast pyrolysis of softwood on an industrial-scale fluidized bed unit (Dynamotive, West Lorne, Ontario) and provided by CIRAD, France. Its physico-chemical properties have been measured (see Table 1). The water content of the bio-oil measured by Karl Fischer method (ASTM E203) is around 26 wt % which is in agreement with the average values reported in the literature. It can be noticed that the solid particles content is rather high (2.3 wt.%) while the ash content remains low (around 0.06 wt.%). This confirms that the solid particles mainly consist of high-carbon content char particles. These particles were entrained during bio-oil production by the gas stream to the bio-oils condensers. Ultimate analysis and LHV of the bio-oil are very similar to those of wood. From the ultimate analysis, the chemical formula of the bio-oil can be established as CH1.18O0.48.0.4H2O.
Ultimate analysis (wt.%) | H2O | Ash | Solids | LHV | Kinematic viscosity | |||||
C | H | O | S | N | (wt.%) | (wt.%) | (wt.%) | (MJ.kg-1) | at 20 °C (mm2.s-1) | |
42.9 | 7.1 | 50.58 | < 0.10 | < 0.10 | 26.0 | 0.057 | 2.34 | 14.5 | 103 |
Ultimate analysis and several characteristics of bio-oil derived from hardwood fast pyrolysis
Two reactor temperatures were tested in order to evaluate the effect of the final pyrolysis temperature on devolatilization process affecting the yield of gas, condensate and residual solid:
Moderate temperatures at 550°C;
High temperature 1000°C to approach the severe conditions of gasification.
The yields of final products are listed in Figure 4. With temperature increasing from 550 to 1000°C, the total gas yield sharply increases from 12.2 to 43.0 wt.%, while condensate (tar + water) decreases from 73.2 to 47.5 wt.%. Varying temperature shows a great influence on the gas composition as well.
Figure 5 shows that the main gas products are H2, CO, CO2, CH4 and some C2 hydrocarbons (C2H2, C2H4 and C2H6). Among them, the H2 and CO content increased significantly from 0.056 wt.% to 1.65 wt.% and from 5.9 to 23.9 wt.% respectively as temperature increased from 550 to 1000°C. Yields of CH4 also increased from 1.2 to 5.0 wt.% whilst that of CO2 increased from 4.2 to 10.8 wt.%. The yields of C2H2, C2H4 and C2H6 are relatively small. The specie C2H6 only appears at 550°C while C2H2 only appears at 1000°C. The thermal cracking of gas-phase hydrocarbons at high temperature might explain the variation of gas product composition observed.
Finally, with increasing temperature from 550°C to 1000°C, the char yield decreased significantly from 14.5 to 9.4 wt.%. However changing the reactor temperature implies a change of both the heat flux density imposed to bio-oil (and hence its heating rate) but also the final temperature reached by the char produced. Therefore the later trend observed might be due to two reasons:
The char formed at 550°C contains residual volatile matters which are released when theemperature increases to 1000°C;
Increasing the heating rate results in the decrease of the char yield. This is actually in good agreement with what is usually observed in the literature from pyrolysis of biomass (Ayllόn et al., 2006; Haykiri-Acma et al., 2006; Mani et al.,2010).
To check the first assumption, a char first prepared at 550°C was submitted to a second heating step at 1000°C. During this second step, the mass of char did not change, which excluded the first assumption, and highlighted actually the effect of heating rate. In order to confirm this trend, additional experiments were carried out to separate the effect of these two parameters. This is studied in details in the following section.
The temperature profiles obtained in the HTR are illustrated in Figure 6. A calculation of the highest heating rate is then made taking into account only the linear part of curves. Details of the calculated heating rates and products yields obtained from experiments are given in Table 2.
The temperature profiles curves show that the heating rate ranges from 2 to 14°C/s at the final pyrolysis temperature of 550°C, and from 2 to 100°C/s at the final pyrolysis temperature of 1000°C. The response time of temperature measurement system was characterized by placing the thermocouple alone and the thermocouple placed in the refractory ceramic wool without bio-oil sample together inside the reactor in 0.03 min. The results are also plotted in Figure 6. At 1000°C we can notice that the response of the thermocouple and refractory ceramic wool does not exceed 100°C/s. But, it appears that the actual heating rate for the sample introduced in 0.03min may be still higher than 100°C/s. This is further illustrated on Figure 6.
t (min)a | Heating rate °C/s | Solid %wt | Total gas %wt | condensate %wt | |
Pyrolysis at 550 °C | 16 | 2 | 14.4 | 14.1 | 71.4 |
8 | 5 | 12.4 | 13.7 | 73.8 | |
4 | 10 | 11.4 | 13.3 | 75.2 | |
0.03 | 14 | 10.5 | 13.3 | 76.0 | |
flash | "/>2000 | 1.2 | 13.6 | 85.1 | |
Pyrolysis at 1000 °C | 16 | 2 | 11.5 | 41.6 | 46.8 |
8 | 5 | 10.4 | 41.7 | 47.8 | |
4 | 14 | 8.6 | 40.9 | 52.2 | |
0.03 | 100 | 3.8 | 43.8 | 53.4 | |
flash | "/>2000 | 0.9 | 40.3 | 58.7 |
Product yield of bio-oil pyrolysis at different temperatures and heating rates
In order to highlight the effect of heating rate and final temperature on the yields of char, they were plotted in figure 7, with the heating rate as the x scale, using a log scale. The low heating rate experiments gave higher yields of char. Char yield then decreased significantly: from 14.4 wt.% down to 10.5 wt.% when heating rate increased from 2 to 14°C/s at the final temperature of 550°C, and from 11.5 to 3.8 wt.% when heating rate was increased from 2 to 100°C/s at the final temperature of 1000°C.
In order to increase still the heating rate and reach the flash pyrolysis conditions, we have performed additional experiments in the HT-EFR. This process allows achieving very high heating rate.
Temperature evolution of the sample during bio-oil pyrolysis in HTR at different heating rates and two final temperatures. a: 550°C, b: 1000°C
Indeed it is shown that when a particle or droplet is transported by a cold spraying gas, its heating rate is controlled by mixing of the cold gas with the hot gas in the reactor. CFD modeling was used and derived this order of magnitude. Heating rate was estimated at 2000°C/s(Van de Steene et al., 2000). Under these conditions, the char yield measured is very low: < 1 wt.%. As can be seen in Figure 7, the char yield obtained with HT-EFR is in rather good agreement with the values obtained in HTR and extrapolated to high heating rates. This result is in agreement with the work carried out by Guus van Rossum et al.(Van Rossum et al., 2010). They found that small droplets (undergoing high heating rate) are much quicker evaporated and give fewer char compared to larger droplets (undergoing low heating rate pyrolysis).
Char yield obtained from pyrolysis of bio-oil at two final temperatures: 550°C and 1000°C - effect of heating rate
Globally from all the data collected, the char yield depends very much on the heating rate, and less on the final temperature, confirming the observation from section 3-1. These results give important information for understanding the pathways occurring during gasification of bio-oil in reactors such as EFR: the amount of char formed by pyrolysis and submitted to subsequent steam-gasification reactions will be very low whereas the main reactions will occur in the gas phase (reforming, partial oxidation…). Considering that solid gasification is rate-limiting, this might be an advantage of using bio-oil instead of biomass as feedstock for EFR gasification.
Figure 8 shows the effect of heating rate on the product yields at two final pyrolysis temperatures. There is no apparent impact of the heating rate but a drastic influence of the temperature on the total gas yield which remains of about 13–14 wt.% and 40–43 wt.% at 550°C and 1000°C, respectively.
On the other hand, we can notice that the total condensate yield increased when the heating rate increased and when the final temperature decreased. A value of 76 wt.% is obtained at 14°C/s and a final temperature of 550°C, which is about 5 wt.% higher than that obtained at 2°C/s. In the same manner, at 1000°C the total condensate yield increased with the heating rate, up to 53.4 wt.% at 100°C/s. This value was about 6 wt.% higher than that of 2°C/s.
All these trends can be summarized and explained as follows.
Pyrolysis inside the sample
The volatile matters yield increases with the heating rate of bio-oil, to the detriment of the char yield as reported earlier. The primary volatiles may undergo secondary reactions through two competitive pathways (Zaror et al., 1985; Seebauer et al., 1997):
re-polymerizing to form char;
cracking to form lighter volatiles which implies less tar repolymerisation.
The re-polymerization pathway is probably favored by lower heating rates. Indeed, low heating rates lead to longer volatiles residence times inside the sample, and favor secondary reactions of re-polymerization to form solid residue. These conditions are known to favor the formation of secondary char from biomass pyrolysis experiments (Zaror et al., 1985)and apparently, this could be extended to the case of bio-oil pyrolysis.
Gas phase reactions outside the sample
Once the volatiles have escaped from the sample, they can undergo additional secondary gas-phase cracking reactions as previously presented. The conversion rate of this reaction highly increases with the gas temperature, leading to higher gas yields to the detriment of condensates. This result is in agreement with number of pyrolysis works carried out on biomass (Seebauer et al., 1997).
Let’s notice that due to the procedure described, higher heating rate leads to lower residence time of tars in the hot zone because the bio-oil sample is introduced more rapidly to the centre of the heated zone. The estimate of the gas residence time in the HTR was calculated, from their release at the sample position (which varies with time according to the duration of sample introduction) to the exit of the reactor. It varies from 8 to 16s at 550°C and from 5 to 10s at 1000°C.
The first objective was to study the influence of temperature - over a wide range - on the syngas yield and composition.
Generally the gas mixture formed from catalytic reforming of bio-oil is composed of hydrogen, carbon monoxide and dioxide, methane, acetylene, unconverted steam, coke (carbon) and soot. Figure 9, presents the mole fraction of the gaseous products from this work (in dry basis and without N2) as a function of temperature in the range 1000 to 1400°C. Error bars were established by repeating each test 2 or 3 times. The species C2H4, C2H6, C3H8 and C6H6 are not detected by chromatography. Whatever the operating temperature between 1000°C and 1300°C, bio-oil is mainly decomposed to H2, CO, CO2, CH4 and C2H2. Above 1300°C C2H2 disappears, while CH4 disappears above 1400°C. As the temperature rises, the fraction of H2 increases monotonically at the expense of carbon monoxide, methane and acetylene. Above 1300°C the hydrogen content remains almost stable. At 1400°C hydrogen mole fraction reaches the maximum value of 64 mol% of the syngas.
The reactions that may explain the increase of hydrogen with temperature are:
Product yield obtained from bio-oil pyrolysis at two final temperatures. a: 550°C, b: 1000°C- effect of heating rate
Composition of the produced syngas (dry basis and without N2) - effect of temperature, at S/F=4.5
The water gas shift reaction can also explain the increase of carbon dioxide and the decrease of carbon monoxide between 1000 and 1200°C. Above 1200°C, carbon monoxide slightly increases. This may be explained by steam gasification of the solid carbon residue (char and soot) resulting from the pyrolysis of oil dropletsto yield carbon monoxide and hydrogen following the reaction:
and potentially following the Boudouard reaction which would explain the slight decrease of CO2:
It was observed that as the temperature increases the amount of collected solid decreases significantly above 1000°C. The process allows achieving very high heating rate estimated at 2000°C/s(Van de Steene et al., 2000). Under these conditions, the char yield measured is very low: < 1 wt.%. At 1400°C more than the 99.9% the bio-oil is converted to gas.
The thermodynamic equilibrium calculation is independent of reactor and predicts the yield of final products, based on the minimization of the Gibbs free energy of the system. It was conducted here using FactSage software 5.4 to establish whether the syngas was close or not to equilibrium at the different temperatures. Operating temperature varied from 1000°C to 1400°C; pressure was fixed at 1 atm. The software is not presented in detail in this paper; details of the thermodynamic calculation could be found on FactSage web site.
The results of prediction are presented in Figure 10, expressed in g of gas produced per g of crude bio-oil injected. As the temperature increases from 1000 to 1400°C the calculated equilibrium yield of H2 remains approximately constant at 0,11g/g, while the yield of CO increases from 0.3 at 1000°C to 0.45g/g at 1400°C. The CO2 yield decrease from 1.1 g/g at 1000°C down to 0.9 at 1400°C.
At 1000°C the calculation yields are far away from the experimental results. The deviation from equilibrium at lower temperatures is also reported by Sakaguchi et al (Sakaguchi et al., 2010). At 1200°C the thermodynamic equilibrium begins to establish. The calculation nevertheless does not retrieve the presence of CH4 and C2H2. At 1400°C the experimental yields are very close to the equilibrium calculation yields: 0.11 and 0.12 respectively for H2, 0.45 and 0.45 respectively for CO, and 0.86 and 0.88 respectively for CO2. It can be concluded that at this temperature the equilibrium is reached.
It is also interesting to compare the obtained experimental yields at 1400°C to the theoretical yields corresponding with complete gasification of oil that would follow:
The maximum stoichiometric H2 yield for this oil would be 0.150g per 1g crude bio-oil while a value of 0.126 g was obtained experimentally. This shows that under our experimental conditions and at 1400°C steam reforming of bio-oil lead to a production of H2 with a yield of about 84% of theoretical yields corresponding with complete gasification of oil (reaction 6).
Gas yield from bio-oil reforming at 1000, 1200 and 1400°C, S/F=4.5. □ Experiments; ■ Equilibrium calculation
Gasification of biomass is one of the leading near-term options for renewable energy production. When large scale units are considered, bio-oil shows lots of advantages compared to solid biomass. The combination of decentralized fast pyrolysis of biomass followed by transportation and gasification of bio-oil in bio-refinery has attracted great attention.
The overall purpose of this research was to investigate the feasibility of a whole bio-oil non catalytic steam gasification process for the production of high quality syngas in entrained flow reactor.
From a chemical point of view, bio-oil gasification process is quite complex and consists of the following main stages: vaporization, thermal cracking reactions with formation of gas, tars and char that considered as undesirable products. This is followed by steam reforming of gas and tars, together with char oxidation. To better understand the process, the first step of gasification (pyrolysis) and thereafter, the whole process (pyrolysis+gasification) were separately studied.
In the pyrolysis step, a temperature increase from 550°C to 1000°C greatly enhanced the gas yield, whilst solid and liquid yields decreased significantly in agreement with the literature. The heating rate of bio-oil has little impact on the gas yield, but plays a major role on the char yield. Hence the char yield decreases from 11 wt.% with a heating rate of 2°C/s down to 1 wt.% for flash heating rate of 2000°C/s at a final temperature of 1000°C. At very high heating rate, the final temperature has little influence on the char yield. These results show that for gasification under industrial EFR conditions, the quantity of char is very small. Thus the gasification process mainly consists in gas/tar reforming. Nevertheless, the production of clean syngas will require either complete gasification of char or its removal from the gas produced by the gasifier.
In steam gasification process, whole bio-oil was successfully steam gasified in HT-EFR. An increase in the reaction temperature over a wide range from 1000°C to 1400°C implies higher hydrogen yield and higher solid carbon conversion. A thermodynamic equilibrium calculation showed that equilibrium was reached at 1400°C. At this temperature steam reforming of bio-oil leads to yield of equal 84% of theoretical yields corresponding with complete gasification of oil.
The authors gratefully acknowledge the financial support from EnerBio Program of Fondation Tuck France, and express their gratitude to Mr. Bernard AUDUC technician in Ecole des Mines d\'Albi-Carmaux for his assistance and contribution to experimental device design and operation.
Imagine that you are a manager in a large organization. You ask your subordinate employee for her help with a new project, but she refuses to help out because she has been working on a tight deadline and currently, she does not have any time for extra tasks. You are annoyed by the employee’s reaction and there has been tension between you two ever since. You ask her to meet up and discuss… How do you think the meeting will go? How will you react to the employee and how do you think that the employee will respond?
A key element to take into account before trying to think of possible answers to these questions is that between the two persons, you and the subordinate employee, there is one big difference: power asymmetry. You, manager, have power over the employee, which enables you to punish, reward, or enforce your will to her, whereas the employee does not have power over you. Power asymmetry is a decisive factor in how all kinds of relationships develop and how conflicts are handled and resolved.
Power makes the world go round. Power enables people to enforce their will over others and as such, it determines people’s attitude towards a conflict and the way they choose to resolve it. In this chapter, I will delineate the role of power in conflict management focusing on conflicts in organizations in particular. First, I will explain how power is defined and which are the main sources of power. Consequently, I will present research-based evidence on the role of power in conflict management. Finally, I will touch on the importance of distinguishing power that is construed by the power-holder as opportunity from power that is construed as responsibility.
Power is pervasive and as such, it is difficult to give it an accurate and clear-cut definition. For instance, power can be seen as the access to valuable material (food, money) or social (knowledge, information, decision-making opportunities) resources [1, 2], as the capability to achieve personal goals and influence other people’s outcomes, as the capability to administer punishments and rewards, or as the potential to influence others and modify their attitude and behavior [3].
Power may stem from various sources. For example, a senior manager may rely on their ability to punish or reward others to get things done. A renowned expert in a field may rely on their knowledge and expertise, and a person who is admired by others for their skills or achievements may rely on personal qualities to influence others.
Social psychologists John French and Bertram Raven [4] studied power more than half a century ago and suggested that power can arise from various sources. French and Raven have grouped the forms of power into two broad categories, namely positional (or structural) and personal power. Positional power refers to the type of power that people have because of their status or position in an organization or society. This type of power aims to ensure that individuals and teams conform and work together towards predetermined outcomes and common goals set out for the group. Positional power includes the following three sub-types:
Legitimate power is derived from holding a formal title in some organization or in society and using the power that comes with that title. A country president, a senior manager, a CEO, or a prime minister have legitimate power. However, this type of power is unstable because when the title or position is lost, power instantly evaporates.
Coercive power is derived from one’s ability to punish others for not complying with the rules and regulations or for not doing what needs to be done. Threats and punishment are standard coercive tools. For instance, when people imply that someone will be denied privileges or will get demoted or fired, they use coercive power.
Finally, reward power is derived from one’s ability to reward others for doing positive things or for doing what needs to be done. Some examples of reward power include salary raises, promotions, compliments, and desirable assignments.
Although positional power enables power-holders to get things done and ensure that everyone works towards the same goal, it is not the type of power that inspires people. It is personal power that wins the hearts and minds of people, inspires them, and prompts them to commit to tasks. In other words, personal power inspires people to rise to greater heights, set the bars high, and perform as well as possible. Personal power includes the following two types:
Expert power is derived from having unique, in-depth information, expertise, or knowledge about a subject or a topic. When one has knowledge and skills that enable them to understand a situation, use solid judgment, and suggest useful or practical solutions, people trust them and eventually do what they say or want.
Finally, referent power is derived from the respect or admiration a person commands because of their personality traits and personal qualities. For instance, celebrities have referent power, which is why they exert such an influence on how laypeople think, feel, or behave. Actors, singers, and famous artists can influence everything from what people like or buy to which politician they vote. In the workplace, a person with referent power is a person who often makes everyone feel good and inspired, so that person has a lot of influence on their colleagues.
Apart from the above sources of power, which stem from either one’s position or one’s personal qualities, people may possess a different type of power, the so-called Best Alternative To a Negotiated Agreement (BATNA). The term BATNA was originally used by Roger Fisher and William Ury in 1981 in their book “Getting to Yes: Negotiating Without Giving In” and it involves a type of power that is inherent in conflict management and negotiation situations in particular. BATNA is defined as the most attractive alternative that a person can take if conflict management (i.e., negotiation) with a partner fails and an agreement cannot be made. In other words, one’s BATNA is what one’s best alternative is if negotiations do not succeed. In fact, having an attractive alternative enables people to be less dependent on others, which is translated into increased (sense of) power [5, 6]. For example, “think for a moment about how you would feel walking into a job interview with no other job offers — only some uncertain leads. Think about how the talk about salary would go. Now contrast that with how you would feel walking in with two other job offers. How would that salary negotiation proceed?” ([7], p. 52) In the first situation, your BATNA is unattractive (you have no other job offers and thus no other good alternatives), which increases the likelihood that you accept a low salary in case you are offered the job. In the second situation, however, you have a strong BATNA (you have two other job offers), making you less dependent on your prospective employer and enabling you to negotiate a higher salary. The difference between the two examples is “power” (see Table 1 for a brief description of all sources of power) (for a review of types of power, see also [8]).
Source of power | Description and examples |
---|---|
Positional power | |
Legitimate power | Description: Holding a formal title in some organization or in society and using the power that comes with that title. People are influenced by the power-holder’s position rather than by the power-holder as a person. Example: A president, a CEO, a prime minister, a king. |
Coercive power | Description: Ability to punish others for not doing what needs to be done. People comply out of fear. Example: Use of threats and punishments. |
Reward power | Description: Ability to reward others for doing what needs to be done. People comply in order to get rewarded. Example: Raises, promotions, desirable assignments, training opportunities, compliments. |
Personal power | |
Expert power | Description: Possession of in-depth information or knowledge about a subject. People are actually influenced by the power-holder’s claims and change their attitude and behavior based on the power-holder’s attitude and behavior. Example: Suggestion of effective solutions, use of solid judgment, outperforming others. |
Referent power | Description: Respect or admiration of a person based on his/her personality traits and personal qualities. People “follow” (oftentimes uncritically) the power-holder no matter whether they agree with him/her or not. Example: Celebrities and people with a “charismatic” and inspiring personality and attitude. |
Contextual power | |
Best Alternative To a Negotiated Agreement | Description: The most attractive alternative that a person can take if negotiation or conflict management with a partner fails and an agreement cannot be made. People comply with the will of others more if they have no other attractive alternatives. Example: Going to a job interview while having already another attractive job offer. |
Major sources of power.
Research suggests that besides their content-based differences, all kinds of power have a main characteristic in common: “dependence”. Regardless of the specific sources of power that are involved, it is the level of dependence between individuals that allows power to occur [9]. Accordingly, the less one is dependent on the other, the more powerful one is, and the more one is dependent, the more powerless one is. As such, whether it is positional, personal, or contextual (e.g., BATNA), power should influence the direction of a conflict and conflict management process in the same way.
To test this hypothesis, Van Kleef, De Dreu, Pietroni, and Manstead [10] conducted five studies. In Study 1, power was operationalized as one’s possession of an attractive alternative (BATNA). Participants were recruited in the lab and were assigned into one of the two experimental groups: high or low-power groups. All participants were assigned to the role of a phone seller and were told that two buyers were interested in the phones they were selling. The first buyer had already made an offer and participants had to negotiate the price with the second buyer. Participants in the high-power group were given an attractive offer (alternative) by the first buyer (the first buyer’s offer would give them 570 points, while the maximum points they could reach were 760 points). However, participants in the low-power group were given an unattractive offer (alternative) (the first buyer’s offer would only yield 190 points). Subsequently, participants had to negotiate the phone price with the second buyer and make a counteroffer. Importantly, participants got informed about the buyer’s (opponent) emotional reaction to their counteroffer. More specifically, buyers were presented as having reacted happily or angrily to the participants’ counteroffer. Results showed that low-power participants made more concessions than high-power participants, and also, the buyer’s emotions (angry or happy) influenced them to a greater extent. Specifically, low-power negotiators conceded more to an angry buyer than to a happy one, whereas high-power negotiators were immune to the buyer’s emotional state.
Van Kleef et al. [10] replicated these findings in four additional studies, where power was operationalized differently. For instance, in one study, high-power participants had a managerial position in an organization (legitimate power). In contrast, low-power participants had a junior-trainee position. In another study, high-power participants had the full support of the top management for the negotiation to come. In contrast, low-power participants did not (i.e., note that in conflicts in organizations), the availability of support increases individuals’ sense of power because it enables them to form coalitions with others in order to get their way and assures them that they do not stand alone in the conflict [11]. These findings suggest that regardless of the power source, the mere existence of power asymmetry between negotiators determines the negotiation outcome: The low-power negotiators are more likely to concede to their powerful opponent than the other way around. It is noteworthy, however, that in none of these studies did the researchers operationalize personal power. All five studies used positional power or BATNA to operationalize power and therefore, there is no evidence about how referent or expert power of power-holders influences an opponent’s reaction in the conflict.
An important reason for which power is such a determinant factor of conflict management is that power directs people’s willingness to search for information about their partner [12, 13]. Information gathering involves questioning one’s partner and “asking for information” to test one’s beliefs and assumptions [14, 15] and as such, it is central to conflict management. Importantly, questions can be diagnostic or leading. Diagnostic questions aim at providing evidence for or against one’s beliefs or assumptions, whereas leading questions have the purpose to yield answers that confirm one’s beliefs or assumptions, regardless of whether those beliefs and assumptions are valid or not [16]. Subsequently, diagnostic questions allow negotiators to better understand their partners and their wishes than leading questions [17, 18, 19]. In three experiments, De Dreu and Van Kleef [20] investigated the effects of power on people’s willingness to search for information about their negotiation partner. Participants were placed in a high or low-power position (relatively to their partners) and were also told that their partners had competitive or cooperative personalities. Just before negotiations began, participants were given the opportunity to write down questions they would like to ask their partners. Participants’ questions were then content-coded as diagnostic or leading.
In line with their predictions, De Dreu and Van Kleef [20] found that low-power participants indicated a stronger drive to understand their partner, which prompted them to ask more diagnostic than leading questions, especially when their partner was described as competitive. These findings provide evidence that low-power individuals, especially when faced with a competitive partner, feel less comfortable and are more likely to develop an accurate impression and opinion about their partner. However, high-power participants did not indicate such motivation regardless of their partner’s (competitive or cooperative) personality. These results might also shed light on why low-power negotiators are more influenced by powerful people’s emotions and why they concede more (as was shown by [10]).
Besides the differential outcomes that powerful and powerless individuals can achieve in conflicts and negotiations (e.g., more or less concessions of the opponent), power can also shape people’s emotional expression during a conflict. For instance, Petkanopoulou, Rodríguez-Bailón, Willis, & Van Kleef [21] carried out three studies to investigate how power shapes anger expression and what are the motives of high- versus low-power individuals to express anger at others. In line with their predictions, researchers found that high-power individuals are more prone to express their anger directly at their target as compared to low-power individuals, who are more likely to express their anger indirectly (e.g., by sharing it with other people rather than with the target of the anger). Moreover, low-power individuals expected that expressing their anger directly would elicit reciprocal anger in the powerful and would cause negative consequences to them. In contrast, high-power participants expected that both direct and indirect anger expressions would elicit fear rather than reciprocal anger in the powerless.
Based on the above, one would conclude that holding power, no matter what the source of power is, makes people appear tougher in conflict management processes, more immune to the others’ emotions, and more focused on self-interested goals. A fundamental question that arises here is: “Is power inherently “selfish”, and what is its functionality in organizations?” This is a very interesting question as power is inherent in organizations, in human interactions and relationships, and of course, in all kinds of conflict.
In real-life, we see that the effects of power on people’s behavior are not uniform. For instance, laypeople frequently rely on powerful others, seek advice, or count on their help whenever they need it. In the following, I present two contradictory functions of power in order to illuminate this issue: power as opportunity versus power as responsibility.
In the above, we defined and examined power as one’s capability to influence one’s outcomes, as one’s access to valuable material and social resources, as one’s capability to administer rewards or punishments to others, and as one’s potential to influence others. As such, power prompts power-holders to view their advantage over the powerless as an opportunity to achieve personal goals instead of taking care of the powerless. Indeed, power-holders frequently show less caring and affection towards the powerless and treat them as a means for goal attainment [22, 23]. The opportunistic propensity of power-holders is nicely depicted in the activation/inhibition system theory [2]. which suggests that possessing power frees people up from external constraints as power makes them feel that their resources approach or even exceed the demands of a situation. Therefore, power-holders have the luxury to experience situations predominantly as opportunities to achieve their own goals and therefore, construe others through a lens of self-interest [2]. In contrast, low power activates an “alarm system” that makes people experience situations and social interactions as a threat. Accordingly, low-power people are more sensitive to powerful others’ potential constraints and become more attentive to the interests, desires, and goals of the powerful. Subsequently, powerless people often become easier targets of power-holders’ aggression, dominance, and self-interested behavior [24, 25].
Based on the above, one would conclude that some paranoia about the powerful seems to be reasonable. There is evidence, however, that the effects of power are not uniform. In fact, we often observe that in real-life (e.g., within an organization) powerful people are more benevolent than they are thought to be, attentive to the others’ needs, and show concern about other people’s goals and interests [26, 27]. Indeed, rather than being careless or selfish, power-holders often see their power as responsibility towards others and as an inner obligation to take care of things that need to happen (e.g., ensuring that important goals are met [28]). For instance, we frequently see in organizations that leaders do show concern for their followers’ outcomes and use their power not only to serve their own goals but also the needs and desires of their followers [29, 30]. All in all, power, apart from giving power-holders the opportunity to act upon will and behave self-servingly, it also entails responsibility towards the powerless [29, 31].
A fundamental and interesting question is “when do power-holders see their power as responsibility or opportunity and how does the differential perception of power influence conflict management”? To the best of my knowledge, there is no empirical evidence to test this hypothesis directly. However, recent research shows that power-holders do not behave opportunistically when their power is stable and safe, that is when they do not fear that they might lose it. In contrast, when their power is unstable, power-holders are more susceptible to act self-servingly [32]. Indeed, prior research in the field of leadership suggests that when leaders are threatened by the prospect of losing power, which goes together with losing access to valuable resources, they react negatively to the prospective loss (see [33]). In a similar vein, research in the field of conflict management revealed that power-holders show more concern for their low-power partners’ needs when their power is not in jeopardy.
Fousiani et al. [34] conducted two studies to come to this conclusion. In the first study, participants were put in dyads and were told that they would negotiate some issues/disagreements with their partner. Participants were split into two groups: high and low-power groups. Participants in the high power group were assigned to the role of a powerful manager who had the ability to make decisions that affect employees. Participants in the low power group were assigned to the role of a powerless employee who had to follow the managers’ decisions. Most importantly, the issues or disagreements that participants were invited to negotiate with each other were not always the same. Dyads were invited to negotiate (in random order) power-related disagreements, that is disagreements about power possession in the decision-making processes, and task-related disagreements, that is disagreements regarding the coordination of work activities. Researchers found that high-power negotiators accommodated (gave in) their low power negotiating partner especially when the disagreements at hand touched on task-related but not power-related disagreements. According to the researchers’ interpretation, these findings point out power-holders’ motivation to accommodate the powerless when their powerful position was safe, and theis inclination to maintain the status quo and keep their power position intact [35, 36, 37]. In other words, high-power negotiators do not mind using their power in favor of the powerless and accommodating them as long as their power position is safe, but they do mind if their power position is in jeopardy.
Overall, these findings reveal that power-holders are not as opportunistic or competitive as they are believed to be. In fact, whether power-holders collaborate, accommodate or compete with the powerless in conflict situations seems to depend on how stable and safe their power is perceived to be. Based on the above, one would expect that power not only is it not inherently “selfish” but it is used responsibly and benevolently, especially when power-holders perceive their position as safe.
This chapter presented the impact of power on organizational conflict and conflict management in organizations based on the negotiation literature. Power is pervasive and as such, it has a great impact on conflicts in organizations. People usually associate power with unethicality and immorality, self-interested attitude and behavior, and win-lose outcomes [34, 38]. Indeed, empirical evidence supports this postulation and shows that power-holders are less empathic to the powerless and unaffected by their low-power partners’ emotions, less willing to search for the beliefs, needs, and desires of the powerless, and they always demand the larger piece of a pie.
However, we should be careful with overgeneralizing these findings as power is also associated with providing help and support to the powerless, taking care of things that others cannot take care of, and treating those in need with responsibility and benevolence. As such, power asymmetry in organizations is desirable and functional and may promote win-win outcomes for the involved members, especially when power-holders feel that their powerful position is safe and not subject to changes. This suggests that organizations should encourage interventions geared at fostering power-holders’ (e.g., leaders) sense of safety regarding their positions (see also, [39, 40]) in order to enable them to see their power as responsibility towards others rather than as opportunity and pay more attention to the needs and goals of the powerless (e.g., subordinate employees). Although power as responsibility is less attractive to power-holders and power as opportunity is particularly alluring [31], organizations might consider fostering the positive sides of being responsible for the outcomes and achievements of the powerless. This is the best way to ensure fairer outcomes and effective conflict management between those involved in asymmetric power relationships.
“The author declares no conflict of interest.”
IntechOpen's Authorship Policy is based on ICMJE criteria for authorship. An Author, one must:
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