INIS-mf—1 5509
University of Jordan J09600040 Faculty of Graduate Studies f’'r*dit.i(c Department of Engineering
Mnthrm.'Ucs nncl Physical Science: SHALE OIL COMBUSTION
13 Y MOHAMMED AW WAD ALI AL-DABJJAS
SUPERVISOR Dr. MOHAMMED II AMD AN AND
Dr. V. II. KHRA1SIIA
Submitted in partial fulfillment of Hie requirements for the degree
of master of science in mechanical engineering.
Faculty of Graduate Studies,
University of Jordan.
Amman , Jordan
May , 1002 tr** POUR QUALITY I ORIGINAL 8 Ns OS u We regret that some of the pages in this report may not be up to the proper legibility standards, even though the best possible copy was used for scanning The Examining CommiU.ee considers this thesis satisfactory and acceptable for Ui award of the Degree of Master of Science in Mechanical Engineering in MAY, 1992.
Dr. Mohammed Hamdan Chairman of Conrfhittee
Mechanical Engineering Department
University of Jordan
Dr. Y. II. Khraisha
Chemical Engineering Department
University of Jordan
Dr. S. A. Saved Member of Committee
Chemical Engineering Department
University of Jordan
Dr. M. Ham mad Member of Committee
Mechanical Engineering Department
University of Jordan
Dr. Ali Badran Member of Committee
Mechanical Engineering Department
University of Jordan To my mother and father I
Acknowledgements
H. is of my pleasure to express my gratitude to all people who helped me in completing the present work. Special thanks are indebted to my supervisors Dr. M. Hamdan and
Dr. Y. Khraisha, whom without their support, encouragement and advice, my work could have been infinitely more difficult . Also special thanks are indebted to my family, especially my father and my mother for their advice and encouragement . Also I highly appreciate the great assistance conducted through the mechanical engineering lab staff, computer center staff, industrial engineering department workship staff at the faculty of engineering and Technology.
Also I highly appreciate the support ami great help given to me by Dr. M. Ilammad and AL-ICayyali Company for their help in providing live burner. The. Royal Scientific
Society, especially Dr. Najclv Akeel for their help in carrying out the volumetric prod uct concentration analysis, and Jordan Electricity Authority for their help in providing information about oil shale.
Finally, not to forget, the support and great help to me by ell my friends throughout my research. JLJL
Abstract
A ’coutant ’ carbon steel combustion chamber cooled by water jacket was constructed to burn tliescl fuel and mixture of shale oil & diesel fuels. During experimental work air fuel ratio was determined , temperatures were measured using Chrornel/ Alumel thermocouple, finally the gasous combustion product analysis was carried out using gas chromatograph technique. The constructed combustion chamber was operating satisfac tory for several hours of conliuous work. According to the measurements it was found that: the flame temperature of a mixture of diesel imd shale oil fuels was greater Ilian the flame temperature of diesel fuel, and the suiter emissions of a mixture of tliescl and shale oil fuels was liighcr than that of diesel fuel.
Calculation indicated that the dry gas energy loss was very high and the incomplete combustion energy loss was very small. Ill
Contents Acknowledgements...... i
Abstract ...... ii
List vf Figures viii
1 INTRODUCTION 1
1.1 The Objectives of the Present Work ...... 2
1.2 layout of the thesis...... 3
2 LITERATURE REVIEW 5
2.1 Introduction
2.2 Review of Efforts in Exploitation and Development of Oil Shale in Jordan 10
2.3 PRINCIPLE OIL SIIALE DEPOSITS ...... 13
2.3.1 EL LAJJUN...... J4
2.3.2 SULTANI...... 15
2.3.3 Jurf ed Darawish...... 16
2.3.4 Altarat bin Ghudrnn ...... 17
2.3.5 Wadi Maghar...... 18
2.3.6 Nabi Musa...... 19
3 THEORY OF COMBUSTION 21
2.1. Intoduclion ...... 21
3.2 Combustion of liquid fuels 22 3.3 Combustion of solid fuels 23
3.4 Combustion of gas fuels ...... 24
3.5 Type of flames ...... 24
4 EXPERIMENTAL APPARATUS, CONDITIONS AND TECHNIQUES 27
4.1 Introduction ...... 27
4.2 Combustor component ...... 28
4.2.1 Combustor wall...... 28
4.2.2 Combustor Flame Tube ...... 29
4.2.3 Exhaust pipe...... "...... 29
4.3 Existing facilities...... 30
4.3.1 Oil burner nozzles ...... 30
4.3.2 Inlet nozzle ...... 31
4.3.3 Temperature measurement ...... 31
4.3.4 Air supply system...... 32
4.3.5 Riel supply systems...... 33
4.4 Instrument measurement ...... 33
4.4.1 Velocity measurement ...... 33
4.4.2 Fuel consumption . '...... 34
4.4.3 Gas analysis ...... 34
4.4.4 Heating value and energy losses ...... 35
4.5 Type of liquid fuel used in experiment ...... 36
4.0 Experimental observation ...... 38
4.7 Experimental procedure ...... 39 V
5 RESULTS 41
5.1 Introduction ...... 41
5.2 Flame Temperature Measurement ...... 41
5.2.1 Temperature of diesel & mixture of shale oil and diesel ...... 41
5.2.2 Effect of air consumption on flame temperature...... 41
5.2.3 Effect of fuel consumption on the flame temperature ...... 41
5.2.4 Effect of air fuel ratio on the flame temperature...... 42
5.3 Stack temperature ...... 42
5.3.1 Effect of air consumption on stack temperature ...... 42
5.3.2 Effect of fuel consumption on stack temperature...... 42
5.3.3 Effect of air fuel ratio on stack temperature ...... 42
5.3.4 Effect of shale oil percentage on stack temperature ...... 42
5.4 Volumetric concentration of the mean gaseous product ...... 43
5.4.1 Effect of air consumption on volumetric concentration of the mean
gaseous product ...... 43
5.4.2 Effect of fuel consumption on volumetric concentration of the mean
gaseous product ...... 43
5.4.3 Effect of air fuel on volumetric concentration of the mean gaseous
product ...... 43
5.4.4 Effect of shale oil percentage on volumetric concentration of the
mean gaseous product ...... 43
5.5 Dry gas combustion loss...... 44
5.5.1 Effect of air consumption on dry gas combustion loss ...... 44 \
5.5.2 Effect of fuel consumption on dry gas combustion loss ...... 44
5.5.3 Effect of air fuel ratio on dry gas combustion loss ...... 44
5.5.4 Effect of shale oil percentage in the mixture on dry gas combustion
loss ...... 44
5.5.5 Effect of stack stack temperature on dry gas combustion loss ... 44
5.6 Incomplete combustion loss ...... 45
5.6.1 Effect of air consumption on incomplete combustion loss ...... 45
5.6.2 Effect of fuel consumption on incomplete combustion loss ...... 45
5.6.3 Effect of air fuel ratio on incomplete combustion loss ...... 45
5.6.4 Effect of carbon monoxide and carbon dioxide on incomplete com
bustion loss ...... 45
0 DISCUSSION 47
6.1 Flame Temperature...... 47
6.1.1 Flame temperature within diesel flame & mixture of shale oil and
diesel flames...... 47
6.1.2 Effect of air consumption on the flame temperature...... 48
6.1.3 Effect of fuel consumption on the flame temperature ...... 48
6.1.4 Effect of air fuel ratio on the flame temperature...... 48
6.2 Stack temperature ...... 49
6.2.1 Effect of air consumption on stack temperature ...... 49
6.2.2 Effect of fuel consumption on stack temperature...... 49
6.2.3 Effect of air fuel ratio on stack temperature ...... 49
6.2.4 Effect of shale oil percent in the mixture on stack temperature . . 50 VfT
C.3 volumetric product concentration of the main gaseous product ...... 50
0.3.1 Effect of air consumption on volumetric concentration of the main
gaseous product at constant diesel fuel consumption ...... 50
0.3.2 Effect of fuel consumption on volumetric product concentration at
constant mass of air consumption ...... 51
0.3.3 Effect of air fuel ratio on volumetric concentration of the mean
product ...... 51
0.3.4 Effect of shale oil percentage on volumetric product concentration 51
0.4 Dry gas combustion loss ...... 52
0.4.1 Effect of air consumption on dry gas combustion loss ...... 52
0.4.2 Effect of fuel consumption on dry gas combustion loss ...... 52
0.4.3 Effect of air fuel ratio on dry gas combustion loss ...... 52
0.4.4 Effect of shale oil percentage in the mixture on dry gas combustion
loss ...... 53
0.4.5 Effect of slack slack temperature on dry gas combustion loss ... 53
0.5 Incomplete combustion loss ...... 54
0.5.1 Effect of air consumption on incomplete combustion loss ...... 54
0.5.2 Effect of fuel consumption on incomplete combustion loss ...... 54
0.5.3 Effect of air fuel ratio on incomplete combustion loss ...... 54
7 Conclusion and Recommendation 55
7.1 Conclusions ...... 55
7.2 Recommendation ...... 55
Appendix ...... 02 - VIII List of Figures
Figure 3.1 Bunsen burner with premixed imd diffusion flames [211...... 63
Figure 3.2 Comparison between laminar and turbulent fronts for premised com
bustion [21] 64
Figure 3.3 Comparison between laminar flame front in stagnant air wil.li turbu
lent flame front and ordered air motion for diffusion controlled combustion
[21]...... or.
Figure 4.1 The combustor rig component ...... GO
Figure 4.2 Combustor section showing coutant bottom [22] ...... 07
Figure 4.3 Sectional view of burner wall showing combustor shape [22| .... 08
Figure 4.4 Sectional view of the vertical tube convection section [22]...... 69
Figure 4.5 Sectional plan showing fire box and convection section [22]...... 70
Figure 4.6 The photograph of the combustor rig ...... 71
Figure 4.7 The component of the nozzle [23]...... 72
Figure 4.8 Hollow spray cone pattern [23]...... 73
Figure 4.9 Solid spray cone pattern [23] ...... 74
Figure 4.10 Variation of spray angle [23] ...... 75
Figure 4.11 Gas sampling arrangement ...... 76 L<
Figure 5.1 Isothermal contours temperature lines inside the combustion chamber
for diesel fuel at air fuel ratio equal 56.40 ...... 77
Figure 5.2 Isothermal contours temperature lines inside the combustion chamber
for a mixture of 10 % slmlc oil and 90 % diesel at air fuel ratio equal 57.43 78
Figure 5.3 Horizontal axes temperature distribution for two different quantity
of air flow for diesel fuel ...... 79
Figure 5.4 Vertical axes temperature distribution for two different quantity of
air flow for diesel fuel...... 80
Figure 5.5 Horizontal axes temperature distribution for two different quantity
of fuel for diesel fuel ...... 81
Figure 5.6 Vertical axes temperature distribution for two different quantity of
fuel for diesel fuel...... '. 82
Figure 5.7 Effect of air fuel ratio on the variation of the flame temperature along
the horizontal axes for diesel fuel at two different x positions ...... 83
Figure 5.8 Effect of air fuel ratio on the variation of flame temperature along
the vertical axes for diesel fuel at two different y positions ...... 84
Figure 5.9 Effect of air fuel ratio on the variation of the flame temperature along
the horizontal axes for a mixture of shale oil & diesel at two different x
positions ...... 85
Figure 5.10 Effect of air fuel ratio on the variation of the flame temperature along
the vertical axes f--r mixture <-f shale oil & diesel fuels at two different y
positions ...... 86 Figure 5.11 Effect of air consumption on stack temperature at constant fuel
consumption for diesel fuel...... 87
Figure 5.12 Effect of fuel consumption on stack temperature under constant air
consumption for diesel fuel...... 88
Figure 5.13 variation of air fuel ratio with stack temperature for diesel fuel . . 89
Figure 5.14 variation of air fuel ratio with stack temperature for mixture of
shale oil & diesel fuels ...... 90
Figure 5.15 Effect of shale oil percent in the mixture on the stack temperature 91
Figure 5.16 Effect of air consumption on volumetric concentration of carbon
monoxide and carbon dioxide at constant fuel consumption for diesel fuel 92
Figure 5.17 Effect of air consumption on volumetric concentration of oxygen
and nitrogen at constant fuel consumption for diesel fuel...... 93
Figure 5.18 Effect of fuel consumption on volumetric concentration of carbon
monoxide and carbon dioxide at constant air consumption for diesel fuel 94
Figure 5.19 Effect of fuel consumption on volumetric concentration of oxygen
and nitrogen at constant air consumption for diesel fuel...... 95
Figure 5.20 Variation of volumetric concentration of carbon monoxide and car
bon dioxide with air fuel ratio for diesel fuel...... 96
Figure 5.21 Variation of volumetric concentration of oxygen and nitrogen with
air fuel ratio for diesel fuel...... 97
I'igure 5.22 Variation «if volumetric concentration of carbon monoxide and car
bon dioxide with percent of shale oil ...... 98 Figure 5.23 Variation of volumetric concentration of nitrogen ami oxygen willi
percent of shale oil ...... f)fl
Figure 5.24 Effect of nit consumption on dry gas Ions percentage at mnntrml
fuel consumption for diesel fuel ...... Figure 5.25 Effect of fuel consumption on dry gas loss percentage n.l constant air consumption for diesel fuel...... |(J0 Figure 5.20 Variation of dry gas Ions percentage null, nir fuel ratio for diesel fuel 101 Figure 5.27 Variation of dry gas loss percentage wil.li nir fuel ratio for shale oil 11)2 Figure 5.28 Variation of dry gas loss percentage will, percentage of shale oil for diesel fuel...... 103 Figure 5.2!) Variation of dry combustion loss percentage will, slack tempera lure nl constant air consumption for diesel fuel...... 1(1-1 Figure 5.30 Variation of dry combustion loss percentage with stack temperature at constant fuel consumption for diesel fuel...... 105 Figure 5.31 Variation of dry combustion loss percentage with stack temperature for diesel fuel...... JOG Figure 5.32 Variation of dry combustion loss percentage with slack temperature for mixture of shale oil & diesel fuels...... 107 Figure 5.33 Effect of nir consumption on incomplete loss for diesel fuel .... JOB Figure 5.34 Effect of fuel consumption on incomplete loss at constant fuel con sumption for diesel fuel...... 109 Figure 5.35 Variation of incomplete combustion loss with air fuel ratio f»»r diesel fuel...... HO 1 Chapter 1 INTRODUCTION The energy utilization in the world is increasing at a high rate. Considering the present rale of energy consumption and the steady increase in population, very large demand for energy will undoubtedly occur by the turn of this century. This calls for technical innovations to reduce energy use or more effective use of energy. This is accomplished through further development and widespread use of renewable energy sonrces(solar, wind, geothermal, nuclear etc.), and development of energy conservation and management tech nology. The accelerated research and development for alternative energy resources to augment the dwindling supply of petroleum and natural gas is currently under way throughout the world. ^ Solid fuels have, in past, been the most common energy sources for large central generating station. These solid fuel have recently shared the market with gas and oil as / the supplies of these alternative fuels decrease. It is likely that coal will return to a more dominant role in the combustion of solid fuels. ^.Jordan is a non-producing nil country with a limited source of energy. As a result the country has to allocate a significant portion of the national income to cover the 2 cost of the imported oil.However the country has substantial reserves of oil shale which represent an untapped source of indigenous fossil fuel for the country. The Kingdom has been investigating methods of economically utilizing this fuel resource for over n decn.dc. Lhrftt~rcGOTTtffc. rrtost of this effort has been directed towards retorting processes to extract oil from the oil shale, and direct combustion of oil shale to generate electric power. The Jordanian oil shale is considered to have too low a fuel quality to be effec tively used in conventional combustion process. However, in recent years, the circulating fluidized bed combustion process lias demonstrated at commercial scale the ability to effectively utilize low grade fuels [!.]. It is well known that the large quantities of oil shale exist in Jordan which are not widely used due to the following problems: • The high cost of the distillation oil shale compared with the world cost of the crude oil. • The technology that facilitates the conversion of existing power plants from con ventional fuel to oil shale is not yet available. Most accelerated research on oil shale in the world is in two directions • Retorting process at which oil is extracted from oil shale. • Direct combustion in circulating fluidized bed for electric power generation. 1.1 The Objectives of the Present Work The objectives of this work me:- 1. The development of a furnace that can burn liquid fuel, especially shale oil, and diesel. 2. The development of an experimental set up for testing two types of fuel (diesel, mixture of shale oil and diesel) to analyse relevant data such as : • Fuel consumption • energy losses from the stack • air fuel ratio • Volumetric product concentration Exhaust gas analysis will be carried out to investigate the concentration of the main pollutants emitted during combustion. 3. Data collection on the temperature distribution throughout the combustion cham ber. This data may provide useful information in future analysis of combustion chamber design. 1.2 layout of the thesis The thesis is divided into six chapters, of which this introduction is the first. Chapter 2 is a literature review of the previous related literature to help in under standing the problem. Theory of combustion is discussed in chapter 3. Chapter 4 is a full description of the experimental combustor rig and measuring tech niques, as well as, the experiment procedure and observation. The result of measurements are presented graphically in chapter 5 and discussed in chapter 6. The concluding remarks axe discussed in chapter 7 which also include the recommen dation for future work. Figures that describe the experimental work and figures that describe the result obtained in the present work are shown in the appendix. Chapter 2 LITERATURE REVIEW 2.1 Introduction The word ’’oil shale” is not the scientific equivalent of kcrogen-rich limestone and marls, such os the residual hydrocarbon bearing deposits that ore found in Jordan and a few other countries. The term oil shale is used worldwide as indicative of sedimentary rocks that contain organic matter, mainly kerogen when healed to about 500nC this rock yields oil, gas, and carbon residues [2], Jordanian oil shales ore kerogen rich bituminous limestones that were deposited in a shallow marine cuxinic environment, mostly during the macslriclilian and paleoccnc stages of geologic lime. The origin of kerogen ill these limestones is the fossil remain of plants and animals that accumulated in prehistoric seas and lakes that covered most of Jordan some 80 million years ago during the upper cretaceous period [2], Oil shales are abundant and wide spread in Jordan. Major deposits are divided into two groups according to depth of burial: 1. Near-surface deposits (about 30m below the surface) that are exploitable by open pit mining. 2. Deep subsurface deposits (present a maximum depth of 78-lm)Uiat arc exploitable 6' by under ground mining or in-situ retorting techniques. Both [2] near surface and deep subsurface deposits are characterized by the following properties: 1. High carbonate content of bituminous limestones and marls, generally greater than 25%by weight. 2. High sulfur content of the shale which, when retorted, yields about 10% sulfur. 3. Organic matter containing 8.95% hydrogen and 0.73% nitrogen by weight 4. Raw shale contains phosphorous, vanadium, and variable amount of valuable trace metals and rare earth elements. However, by international standards, Jordanian oil shales are of high grade and are capable of yielding as much as 10% oil. The world reserves of oil shale are different from source to another, until this time, the reserves of all countries in world are not known, on the other hand, the U.N reported that the assurance reserves of oil shale in the world equal 69 billion ton, and the large amount of these reserves are found in USA , USSR, China, Morocco, and Jordan [3] In this chapter, some of the investigation that have been reported were summarized to show comprehensive account of recent contribution to the literature and oil shale on oil shale combustion. Fox et al. [4] described the collection, preparation, stabilization, and chemical analysis - high or very low levels of many constituents. The sample was taken from the Laramie Energy Technology Center in 1976 . The sample was analyzed by 13 separate laboratories using six instrumental techniques and a wide range of wet chemical methods. The results of this survey were presented and discussed, including the analytical problem of specific process waters. Hepler et al. [5] presented the result of exposure, acutetoxicity, and reproduction- developmental studies undertaken to define health risks sample which produced in the Laramie Energy Technology Center ’s in 1976. This investigation represents the first animal toxicity evaluation of a retort oil shale water and therefore incorporated a broad base of various tests selected to determine toxicity as a function of exposure route and species exposed. Sterka et al. [6] reported the experiment which was conducted at the Laramie Energy Technology, in this experiment the "Omega 9" process water was produced in an in situ oil shale combustion. They reported the characterization of the retort water from the process. They evaluated the effectiveness of air ambient temperature and elevated dissolved organic. Chen et al. [7] presented the result of study of fluidized bed oil shale combustion, particularly from an environmental standpoint, they reported oil shale classification and characterization. Also, they focussed on mineralogical composition, porosity, specific gravity ,...... , etc. They discussed the mechanisms and kinetics of oil shale retorting and combustion, they examined the cleaning of CO and they explored fluidized bed oil shale combustion. Also they described the simulation of oil shale combustion in a fluidized bed, 6 inch in diameter and they presented the advantages and disadvantages of combustion in a fluidized bed Kuehl and Steller [8] studied the possibibties of the use of oil shale combustion in a fluidized bed furnace and estimated the cost of power plant. They drafted an overall concept of oil shale combustion in a fluidized bed furnace, and established pilot plant of 200 ton/hour steam scale. The concept was technically revised, resulting in a cost estimate of about 15% accuracy. Macauley et al. [9] presented the geological investigation in various of completion for five Canadian deposits of which Mississippian Albert Formation oil shale in New Brunswick is the most significant. Organic geochemistry concerned with both quantity and type of kerogen present as well as with bitumen content to define oil yields. They studied the mineralogy to determine the possibility of using it in related secondary in dustries ( fertilizer, cement, wallboard, brick etc.). At the New Brunswick Research and productivity Council, combined retorting and fluidized coal-oil shale combustion research is attempting of oil and electrical power generation and controlling emissions from high sulfur coal. The Research was conducted in the Morgantown Energy Technology Center (METC)[10] on the feasibility studies of combustion and retorting of five types of oil shales: These studies generated technical data about • the effect of retorting conditions ** the combustion characteristics applicable to developing an optimum process design technology * establishing a data base application to oil shales worldwide The METC research program showed that shale-oil yields were a fleeted by the process parameters of retorting temperature, residence time, shale particle size, fluidization gas velocity, and gas composition. Inguva R [11] presented a model (mathematical modeling of modified in-situ and aboveground oil shale retorting), This model is valid for electro magnatic beating process, in which some of oil evolved during pyrolysis of ICerogen is lost to coking, cracking and combustion , and this model is used in numerical calculation of heating value. Levy, Y. [12] studied oil shale combustion in pressurized fluidized beds (PFBCs) for use in Brayton or in combined thermodynamic cycles, power plant incorporating coal- fired PFBCs, which are developed mainly in the USA, UK, West Germany and Sweden, have estimated thermal efficiencies higher than existing power plants. Such plants are usually designed to include a combined cycle of steam and gas turbines which are coupled to the air compressor and electric generator. Several fluidized bed combustion operate successfully on low grade fuels including oil shale but none of them operates yet at high pressure with oil shale at elevated pressure should not present additional significant difficulties and technology similar to the coal-fired PFBC could be used. Vassal os et al. [13] studied the use of a fluidized bed combustor to burn the coke residue (the coke residue is part of the organic material remain in the inorganic matrix during the pyrolysis process). They used the basis of the two-phase theory of fluidization for predicting the performance of the fluidized bed combustor. They calculated the carbon burning efficiency as function of temperature, pressure, and bubble size for the same conditions. They established the carbonate decomposition and the associated energy loss, and they found the conditions which make feasible complete carbon combustion .10 with minimum carbon decomposition. Shirav et al. [14] suggested a model for the pathway of some trace element during fluidized bed combustion of Israeli oil shale based on pilot plant mid laboratory tests. Tliis model demonstrate the role of carbonate matrix in suppressing the volatilization of trace element due to fixation of most elements in new-formed silicates. They predicted the quality of leachates derived from oil shale combustion wastes on the basis of the proposed model. Krypina et al. [15] considered the transformation of structure of the organic matter of the combustion shales on their heating in the air and in an inert atmosphere. It was shown that the thermal decomposition of the organic matter of combustible shale depends substantially on the type of its structure. Dung et al.[16j presented an integrated process model for the retorting block of an oil shale conversion process. The model integrated only the key process operations such as drying/preheating, combustion of spent of shale and pyrolysis of raw oil shale and sensible heal, recovery from combusted shale. The flowsheeting package ASPEN has been used to achieve mass and energy balance around the process, performance data for individual process units were generated using detailed reactor models developed previously. 2.2 Review of Efforts in Exploitation and Develop ment of Oil Shale in Jordan So far, only the deposit of El Lajjun and Sultani have been geologically investigated in detail at the Jordanian Natural Resources. During the last decade, geological technoe- ouiuinic and prefeasibility studies for the exploitation of El Lajjun deposits for oil shale retorting and power generation, and for Sultani deposits for direct combustion in Circu 11 lating Fluidized Bed (CFB) thermal power plant have been undertaken by Ministry of Energy and Mineral Resources (MEMR) in collaboration with American, Canadian, and German consultants. In 1979, NR A [17] commissioned a study by BGR(German) for the evaluation of El ba jjun deposit and the technoeconomic prefeasibility of an oil shale retorting complex using Lurgi-Ruhrgas process. The results of this study indicated that El-Lajjun oil shale deposit shows continuous hydrocarbon impregnation over an area of 18. Ami2,with about 1 billion tons of oil shale reserves containing some 100 million tons of shale oil. It [17] is suitable for open cast mining, and could support a 50,000 barrels/day shale oil retorting complex for 30 years NRA [17] commissioned phase I of the two, prefeasibility studies for: • Installing an oil shale retorting complex using Lurgi Ruhrgas(LR) process for ex tracting 50,000 barrels/day shale oil. • Installing a power plant of a 300 MW capacity utilizing El Lajjun oil shale but using Lurgi circulation fluidized bed combusting process. This study was completed in 1982, and concluded that both options were technically viable. In March 1986, NRA contacted with the west Germany Consortium klockner -Lurgi for updating the previous feasibility with a view of assessing technical and economic feasibility of a large scale oil retorting complex. This study consisted of revised, geo logical study updated prefeasibility study performance of retorting pilot test and CFB o'ltibuslion test on 201) Ions of El Lajjun oil shale sample in Germany and hydrogeo logical studies for water resources, hi 1980 NRA commissioned a prefeasibility study by Technopromexport to asses the potential for directly burning oil shale in a 300 MW power plnnt( conventional combustion). In 1981 the study was completed which concluded that .Jordanian oil shale is suitable as a fuel for direct burning combustion and recommended the construction of experiment demonstration plant of 200 MW which is similar to a plant in the USSR using Estonian shales as fuel. The study was terminated at this point because the Soviet disagreed with the Jordanian proposal of providing the technology in a 20/30A/W pilot plant. In December 1985, NRA [17] contracted China petrochemical International Company( SINOPEC INTL) to perform tests on El Lajjun oil shale using the existing Chinese pro cess. Initially the company completed the chemical analysis and the evaluation of about half ton of oil shale sample provided by NRA, later, NRA supplied about 1,200 tons oil shale sample to China in order to determine whether Fushun- type retorting is technically suitable to process El-Lajjun shale. These test proves the technical viability of extraction shale oil from El-Lajjun oil shales. The Chinese submitted the technical and financial out lines on the fushun retort with a capacity of 100 tons/day oil shale. The cooperation between NRA and Sinopec stopped at this point due to high investment and the technical uncertainties of the Chinese process. In 1986, Jordan Electricity Authority (JEA) asked Brown, Bovary Company (BBC) for building small station for generating electricity based on CFB. On this basis the company should build the station and operate it, and, at the same time, JEA should buy the electric energy produced in a price that both parties agree on. Further, after ten years of operation, the company should give the station to JEA, However, and due to the high cost , the project was terminated. I During November 1987 and July 1989, the JEA asked Lummus Canada. Combustion Engineering to build commercial energy station of capacity 100MW , and experiment energy station of capacity 25 , 50 Mw, for direct burning combustion of oil shale and recommended to construct a power station similar to Chattham power station which operate on the basis of CFB technology. In December 1985, [18] the Pyropower company(USA) with cooperation of Bechtel company carried out some experiment on oil shale by direct combustion in CFB. The result of the study showed that Jordanian oil shale can be burnt in CFB very efficiently and with high stability. In 1989, some feasibility studies related to the oil shale utilization for electricity production have been completed, and pilot plant test burns have been conducted on Jordan oil shale to determine its suitability as fuel for direct burning, The test results have shown that Jordanain oil shale can be burnt in a very stable manner to generate steam for power production, however, its commercial utilization will not be considered economical unless the price of oil increase significantly. The studies showed that the oil shale can be burnt in CFB with continuous combustion without any help of secondary fuel. Also the results showed that the gaseous product resulting from burning oil shale does not have a negative effect on environment within the international standards). 2.3 PRINCIPLE OIL SHALE DEPOSITS There are seventeen [2] location of oil shale deposits in Jordan namely:- 14 2.3.1 EL LAJJUN Tills deposits is situated in a north south trending graben located approximately mid way along the highway between Kerak and Qatrana, south of Amman has the following information: • surface area=20.4A:m2 • oil content=5 to 18%by weight. The average is 10.4% • reserves: 1.1968 billion metric tons • oil held in place(O.H.I.P): 115.5 million metric tons • exploitable reserves(oil shale): 960 million tons » recoverable resetves(oil): 100 million tons • mean calorific value(shale): 1,310 kcal/kg • mean SO 3 content(shale): 4.83% by weight Results of an updated feasibility study by the Consortium of Lurgi and Kiockner in 1986 on a 50,000 barel/day(66f/d) retorting complex including a circular fluidized bed combustion (CFB) and upgrading plant yield the following data: Rate of oil shale feed stock =74,500 metric tons per day. Derived products in metric tons per day(mt/d)are:- • 5070 mt/d syucrudc(38 API,0.5%S) .1512 mt/d naptha(65 API,0.12%S) • 5,350 mt/d refinery gas • 1,416 mt/d pure element sulfur • 350 MW electrical power of which 135 MW would be required by the retorting complex and 215A/1V would be available for distribution to the grid According to the results of a study for a mini-retorting plant (Lurgi and Klockner, 1988), the products per year of the upgrading plant are • 656,000 m3 naptha • 612,000 tu3 kerosene • 490,000 m3 diesel oil which 32000 m3 is needed for internal combustion • 482,000 m3 fuel oil • 442,000 m3 pure element sulfur The total water consumption required to operate the retorting complex is estimated to be 5 million m3 per year if air cooled, and 20 million m3 per year if water cooled. 2.3.2 SULTANI The Sultani deposit is located about 100km south of Amman adjacent to the Desert Highway south of Qatrana. A summary of information from studies on this deposit is listed below. • geological reserves (shale):989,205,000 metric tons •» oil held in place0.1I.I.P:95,952,785 metric tons exploitable reserves (shale)=942,100,000 metric tons • recoverable reserves(oil)=91,383,000 metric tons • mean S03content= 4.38% by weight • mean P2O3 content=3.48% by weight • mean calorific value(shale)=5,689Kcal/kg • elemental composition of organic matter in percent is: — organic carbon 78.6% — hydrogen 8.95% — nitrogen 0.73% — oxegen 1.94% — sulfur 9.78% • trace element identified in the shale are Mo,Cr,W,Zn,V,Ni,Cu,La,aud Co. Phos phorous is found in variable quantities. 2.3.3 Jurf ed Darawish This oil shale deposit is located approximately 115km south of Amman near the Desert Highway and the town of Jurf ed Darawish. The deposit covers an area of approximately .200 km2 and the characteristic of the Jurf ed Darawish deposits: - oil shale thickness: 19 to 128m(mean, 68.3m) • thickness of overburden: 29 to 62m (mean,47.3m) oil content: 1 to 14.9%(mean, both members, 5.7%) 17 • specific gravity of oil: 0.778 at 15°C, 13 API(American Petroulum Institute) • Geological reserves: 8.0563 billion metric tons. • oil held in place (O.H.I.P) million metric tons. • exploitable reserves, lower member: 2.495 billion metric tons « Oil content, exploitable reserves: 195.66 million metric tons(1.27 billion barrels) • SO3 content(oiI shale): 4.37% by weight • P203 content (oil shale): 1.53% by weight • calorific value, total shale:864kcal/kg • calorific value, lower member:l, 300kcal/kg • elemental composition of organic matter, lower shale member (%) C- 79.01; H 8.70; N-0.87; 0-1.61; S-8.65; As-0.10. 2.3.4 Attar at Um Ghudran This oil shale deposit is located approximately 34km east of Qatrana, the area of the deposit has the following properties: • Thickness: 10 to 60m(mean, 45m) ■* Thickness of overburden: 45 to 62m (mean, 53.2m) • Oil shale: 9 to 13% by weight(mean, 11%) • Specific gravity (oil shale): 0.904 at 15 C; 15 API 18 • Geological reserves(shale): 11.3 billion metric tons • Oil content, geological reserves: 1.177 billion metric tons • Exploitable reserves(oil shale): 10.7billion metric tons • oil shale, exploitable reserves: 1.027 billion metric tons • Sulfur contents(shale): 1.093 to 5.31% by weight • Mean P203 content (shale): 4.0% by weight • Mean calorific value(shale): l,050kcal/kg 2.3.5 Wadi Maghar This deposit is approximately 40km southeast of Qatrana. It is the southern extension of the Attarat Um Ghudran deposit, The characteristics of this deposit are:- 1. Thickness: 10 to 61m(mean, 49m) 2. Thickness of overburden: 32.5 to 50m (mean,40.5m) 3. Oil content: 5.8 to 9% by weight (mean, 6.84) 4. Specific gravity (shale oil): 0.98 at 15°C, 12.98° API 5. Geological reserves (shale): 31.6 billion metric tons (i. Oil content, geological reserves: 2 billion metric tons 7. Exploitable reserves (shale): 21.5billion metric tons 8. Oil content, exploitable reserves: 1.5 billion metric tons 9. Sulfur content (shale): 0 9 to 3.5% by weight 10. Mean P203 content (shale): 4.0% by weight .11. Mean calorific value (shale):l,050kcal/kg 2.3.6 Nabi Musa It is located approximately 25km east of Jerusalem along the dead sea- Jericho highway, from the measured section; the characteristics of this deposit are: • Thickness of oil shale: 25 to 40m (mean, 32.5m) • Thickness of overburden: 0 to 30m (mean, 15m) • Oil content: 7.5 to 11.8% (mean, 9.6%) • Specific gravity of oil: 0.969 at 15°C; 15° API • Geological reserves(shale): lOOmillion metric tons • Oil content of geological reserves: 9.6million metric tons • Exploitable reserves(shale): 95 million metric tons • Oil content, exploitable reserves: 9.12million metric tons • Mean SO3 content(shale):4.04% by weight • Mean P2O3 content(shale): 2.89% by weight Mean calorific value(shale): 1,212 Kcal/kg Chapter 3 THEORY OF COMBUSTION 3.1 Intoduction All conventional fossil fuels, whether solid, liquid, or gas, contain basically carbon and/ or hydrogen which in variably react with oxygen in the air, forming carbon monoxide, carbon dioxide or water vapor. The heat energy released els a result of combustion can bn utilized for heating purposes[19]. The liquid fuels are burned either by vaporizing and mixing with the air before the ignition when they behave like gaseous fuels, or in the form of fine droplets which get evaporated while mixing with the air steam and during burning. The gaseous fuels are either burned in burner where the fuel and air are premixed or the fuel and air flow separately into a burner or furnace and simultaneously mix together as combustion proceeds. The first type of burning gives a premixed flame where as the second type is called burning with a diffusion flame. Gaseous fuels have a number of advantages over a solid or liquid fuels . They burn without any smoke and ash, their combustion is complete with a small percentage of excess air, and the control of gas flames is relatively easy. The disadvantage is the difficulty in storing large quantities of gaseous fuels as compared to liquid and solid fuels. All solid fuels contain basic elements such as carbon hydrogen, and sulfur or its compounds. The combustion reactions can, therefore, be dealt with the help of a few simple reaction equation which cover the combustion of other types of fuel as well. The surface area of the liquid and solid fuels exposed to the air or oxygen is usually very small. The surface area of the liquid exposed to the air can be increased by reducing the size of liquid droplets or size of particle of a solid. The liquid fuel can be evaporated and mixed with air before combustion by breaking the liquid into small particles and providing sufficient space for these processes to take place The combustion of liquid fuel consists of the following processes: the mixing of spray with air, its evaporation, and the combustion of the mixture in case of a solid fuel, the atomization step can be eliminated if it is injected inside the combustion chamber as a dust e g coal. Also , the process of atomization and mixing are eliminated if a solid fuel bed is used. The combustion of a solid fuel also includes the evaporation process, which is negligible in most case. The major difference between the solid and liquid fuels: the combustion of all hydrocarbon fuels occur in the vapor phase. But solids may be considered to evaporate according to the equation established for liquid fuels. 3.2 Combustion of liquid fuels A liquid fuel can burned in the form of vapor, small drops, or in a pool depending on the size of liquid droplet. The mode of combustion of fuel droplets in spray can be considered as: * If the drops are extremely small and their concentration is large, they may evaporate 23 and mix by duffusion with the air in the preheat zone of an established flame front. • If the drops and distance between the individual spheres are large, they may burn as diffusion flame in the local atmosphere surrounding them. Droplet- combustion can be divided into two type: • bipropellant combustion • monopropellant combustion fix bipropellant combustion fuel vapor and oxidant diffuse from opposite direction and a flame is formed at the contact surface at some distance from the drop monopropcllant droplets evaporate and decompose exothermaly. 3.3 Combustion of solid fuels The solid fuels are burned in beds in cliunck or pellet form or in pulverized form suspended in the air stream. When piece of coal is gradually heated in a furnace in presence of air , the following happen: • the water vapor from coal is released as the temperature is raised. This process gets over at about 100°C • The decomposition of its unstable compounds starts. This coal now start emitting volatile gaseous, if the furnace temperature is sufficient to ignite the volatile gases, they will burn like the liquid fuel droplets which continuously supply the vapors as the drops are consumed. The coal piece remains dark during these processes because of the burning of the volatile matter around the coal piece, its temperature is raised but normally does not exceed 600°C to 700°C. The flame gradually shortens and is extinguished when all gases get consumed. The piece which now remain is coke. If the rate of heating is very fast and the size of coal is very small, the coal particles may be ignited before the volatile matter is completely burned. 3.4 Combustion of gas fuels Gaseous fuels, including natural gas, are the easiest fuels to burn. The gas needs little or no preparation before combustion. It may be simply proportioned, mixed with air, and ignited. This can be accomplished in several ways[20]. The atmospheric gas burner is one of the more common gas burners. In these systems, the momentum of the incoming gas is used to draw the primary air into the burner. The operation of these systems is normally satisfactory with primary air gas premix from 30 to 70 percent. Secondary air is drawn in around the burner to complete the combustion process. 3.5 Type of flames A flame is a thermal wave in which rapid exothermic chemical reactions occur and travel with subsonic velocities. The shape of a flame is mainly governed by two factors: the flame pattern of the mixture or products and the quenching effect of solid surface. I.. Pre mixed flame In premixed flames, the fuel/ air mixture must always be close In stoichiomet- ric(chemically correct) for reliable ignition and combustion, with premixed reac- zb tants the flame moves relative to the reactants, so separating the reactants and products. An example of premixed combustion is with oxy acetylene equipment, for welding, the flame is fuel rich to prevent oxidation of the metal, while, for metal cutting, the flame is oxygen rich in order to burn as well as to melt the metal[21]. 2. Diffusion flames The diffusion flame arc formed when the combustible and oxidizer arc not premixed before entering the reaction zone. The burning of fuel droplets is diffusion flame. In the diffusion flames, the flame occurs at interface between fuel and oxidant. The products of combustion diffuse into the oxidant, and the oxidant diffuses through the products. Similar processes occur on the fuel side of the flame, and the burning rate is controlled by diffusion. A common example of a diffusion flame is the candle. The fuel is melted and evaporated by radiation from the flame, and then oxidized by air, the process is evidently one governed by diffusion as the reactants are not premixed. The Bunsen burner, shown in figure 2.1, has both a premixed flame and a diffusion flame. The air entrained at the burner is not sufficient for complete combustion with a single premixed flame, a second flame front is established at the interface where the air is diffusing into the unburnt fuel. For premixed combustion the effect of turbulence is to break up the flame front. There can be pockets of burnt gas in the unburnt gas and vice versa. This increase the flame front area and speeds up combustion. Figure 3.2 shows a comparison of laminar and turbulent flame fronts. For diffusion controlled combustion the turbulence again enhances the burning ve locity. Fuel is injected as a fine spray into air which is hot enough to vaporise and ignite the fuel. Chapter 4 EXPERIMENTAL APPARATUS, CONDITIONS AND TECHNIQUES 4.1 Introduction The experiments were conducted in a combustion chamber, Several instruments were used to measure the mass of air consumption, temperature of the flame inside the combustor along the axes of the nozzle tip, and along the vertical axes from the nozzle tip, mass of fuel consumption, stack temperature, and volumetric product concentration. A general view of the combustor rig and instruments are shown in figure 4.1. In this chapter a full description of combustor rig and measuring techniques used in the present work will be presented. The second section of this chapter (4.3) is devoted to represent the component of the experimental rig that was designed by the researcher and manufacted locally and installed by the researcher the in lab, while the third section of this chapter (4.3) is devoted to represent the existing faclalies that was used in the experiment 4.2 Combustor component The combustor is of a coutant shape which horizontally oriented and it is cooled by means of a water jacket. An air blower is used to supply the combustor with the necessary combustion air. Figure 4.1.shows the combustor and tube centerline dimensions. 4.2.1 Combustor wall lnl.ially, an attempt was carried out to construct the combustor rig by welding two halves of casted metal, unfortunatly and during the welding it was realized that some welded joint broken due to high thermal stress. Then it was decided to use carbon steel sheet to build the rig instead of cast iron since it is much easier to weld this type of material. The combustor wall [22] construction must be one that will resist ash build up and tolerate the erosive action of wall blowers to remove any accumulated ash. To ensure continuity in operating conditions the combustor bottom must be designed ' . for continuous ash removal. This suggests the use of a ('coutant/ type bottom where wall tube are bent to form the hopper shaped bottom as shown in figure 4.2, with ash being discharged to a hopper through the narrow opening. The opening must be kept small to prevent slagging in the ash hopper by excessive leakage radiation. A conceptual furnace design employing these specific design feature is presented in figure 4.3 through 4.5. Figure 4.3 shows the cross sectional shape of furnace with its coutant bottom and Inral.ivn of Die oil shale burners. Itetails of the longitudinal convection section are given in figure 4.4, which shows the vertical U-tube and ash hopper which extends over the entire length of the furnace. Simple baffles in the ash hopper can be used to prevent bypassing of hot flue gas, figure 4.5 is a plan view showing the over arrangement of the radiant and convective section. Figure 4.6 shows photograph of the experimental combustor with the associated sup ply system and auxiliary equipment. 4-2.2 Combustor Flame Tube The combustor flame tube is made from carbon steel sheets to withstand liigh tempera ture. The dimension of the combustor wall tube are shown in figure 4.1, it is cooled by a water jacket.The following holes are drilled in the wall: 1. A 0.10 X 0.20m2 rectangular hole on the top of the combustor was covered with 0.15 x 0.27.m 2 rectangular glass of thickness 0.013 m, it was used to observe the flame temperature, shape, length and colour. 2. Two circular pipe hole of 0.070. m length on the side view of combustor are welded to the wall tube in which thermocouple are inserted inside these circular pipe. 3. A 0.07m circular pipe hole on the side of the combustor was connected to a vacuum pump and a trap and it was used to collect the exhaust gas for samples. 4.2.3 Exhaust pipe The exhaust pipe is made from sheet metal with 0.10 m in diamcter(stack diameter) and 10 m in the length to convey the gaseous product of the combustion above the building. The exhaust pipe is fixed with the combustor tube by means of flanges and bolts. The f’xhansl pipe has a hole drilled into it. In withdraw sample of exhaust product and to measure the stack temperature. 30 4.3 Existing facilities 4.3.1 Oil burner nozzles An oil burner nozzle [23] is a device designed to deliver a fixed amount of fuel to the combustion chamber in a uniform spray pattern and spray angle best suitable to the requirement of a specific burner. The oil burner nozzle atomizes fuel oil (i,e breaks it down into extremely small droplets) so that the vaporization necessary for combustion can be accomplished more quickly. Fuel oil supplied under pressure to the nozzle where it is converted to velocity energy in the swirl chamber by directing it through a set of tangential slots. The centrifugal force caused within the swirl chamber drives the fuel oil against the chamber walls producing a core of air in the center. The latter effect moves the oil out through the orifice of the tip of the nozzle in a core shaped pattern. The component of an oil burner nozzle is shown in figure 4.7 The two basic types of spray cone pattern are: • the hollow cone • the solid cone Each has certain advantages depending upon its use, The hollow cone pattern is shown in figure 4.8 is recommoned for use in smaller burner (those firing 1.00 GP.ll and under)as shown in figure 4.10. there is little or no distribution of droplets in the center of cone. The principal advantage of the hollow pattern and angle under adverse conditions than solid rone patterns operating under the same conditions and at the same Mow rale. The solid cone pattern illustrated in figure 4.9 is characterized by a uniform dis tribution of fuel droplets throughout the cone pattern, nozzles producing this type are particularly recommended for smoother ignition in oil burner firing above 2.00 or 3.00 GPU .Also recommended where long fires are required or where the air pattern or the oil burner is heavy in the center. Oil burner nozzles are also selected on the basis of the spray angle that produce was shown figure 4.10. The spray angle refers to the angle of the spray cone and this angle will generally from 30 to 90, (the nozzle size of my work was 0.50 GPII and the spray angle is 80(23]. V 4.3.2 Inlet nozzle / The inlet nozzle [23] is made from sheet metal with 0.16 m in diameter and 0.175 in in length. The nozzle is fixed with the combustor tube by means of flanges and bolts. 4.3.3 Temperature measurement Tubes are mounted on the flame combustor tube through the water jacket in three differ ent location of the combustor rig, the first lubes are located at 12.5 cm from the nozzle tip, it was used to measure the temperature distribution along the vertical axes of the flame, the second tube located at 37.5 cm from the nozzle tip, it was used to measure the temperature along the axes of the flame, and the third tube located at 37.5 cm from the nozzle tip in a vertical U-tube, for gas sampling. A five Chromel-Alumel thermocouple were used to measure the temperature of the flame along the axes of the nozzle tip, while the number of thermocouples used to mea sure the temperature of the flame along the vertical of the nozzle tip were four. These thermocouple are distributed uniforinally at equal spaces. 5% The thermocouples are externally connected to digital microprocessor to read the flame temperature directly. 4.3.4 Air supply system The air system used consists of the following: • Air blower The necessary combustion air was supplied by means of centrifugal blower driven by electric motor of constant speed, the air mass flow rate was controlled by two means of movable gate mounted at the blower suction, the first gate was used to control the primary air neccarrey for combustion,while the second gate (secondary air) was used for flame length controlling and turbulent air mixing, in other word, the mean function of the secondary air to enhance the combustion elfccieucy in the lean region( rich oxygen). • Air intake nozzle and pitot tube: The air intake nozzle was 76 mm in diameter and made from sheet metal. The nozzle is connected to square box which is fitted on the suction line of the centrifugal fan. A pitot tube is attached to the nozzle tapping to measure the dynamic head and hence the velocity of air is calculated, thus the mass flow of air is calculated using: rna = A * U * p * Co (4.1) where A is the nozzle area U is the stream velocity p is the stream density and Cp is the coefiicent of discharge which was taken equal (.625) 4.3.5 Fuel supply systems The fuel supply system consist of the following: • Fuel pump used to supply the burner with necessary fuel. • fuel tank used to store the liquid fuel, and it was placed at 2 m above the burner. • control valve placed on the main line. • electric motor used to drive the fuel pump. • separated funnel used to measure the amount of fuel consumed. • delivery pipe used to return the unburned fuel to the main tank. 4.4 Instrument measurement In this section a full description of the measuring techniques used in presented work. 4.4.1 Velocity measurement A pitot tube was used to measure pressure difference in order to measure the velocity of the stream . Applying Bernouli equation ,the velocity of the stream is : u = y]2g{hx - h2)/n (4.2) wlu’m (/;t —h2) is the deflection of the. manometer in {iumH20), p is the. stream density {kg jin U is the velocity of the stream. 4.4.2 Fuel consumption The mass of fuel consumption was calculated using volume »«/ = ' e * specific.gravityof fuel (4.3) where the specific gravity was found experimentally by dividing the density of the liquid fuel over the density of the water, and the volume of fuel consumption was read directly from separated fanel 4.4.3 Gas analysis The gas sampling arrangement was shown in figure 4.11, which consisted of : 1. vacuum pump 2. trap was used to absorb the moisture of water vapor in the section line and prevent this moisture to enter the vacuum pump, and the component of the trap, which shown in figure 4.11, axe: • glass flask • absorbing material to remove the moisture content A typical gas analyzer was used to determine the volumetric concentration of the exhaust gas. The sample of the flue gas was drawn into the trap to remove all moisture content before it. was introduced into the vacuum pump, finally the drawn sample was collected by ballon for sampling. 35 The analysis of the exhaust gas sample was carried out to investigate the volumetric product concentration of the following product through gas chromatograph: • carbon monoxide • carbon dioxide • oxygen • nitrogen • sulfur 4.4.4 Heating value and energy losses Combustions results in a release of thermal energy or heat. The quantity of heat generated by complete combustion of a unit of sped lie fuel is constant, and is termed the heating value, heat of combustion or calorific value of that fuel. The heating value of a fuel can be determined by measuring the heat evolved during combustion of a known quantity of the fuel in a calorimeter, or it can be estimated from chemical analysis of the fuel and the heating value of several chemical elements in the fuel. Higher healing value is determined when water vapor in fuel combustion products is condensed, and the latent heat of vaporization of water is included in the fuels heating value. Conversely, lower heating value is obtained when latent heat, of vaporization is iv >1, included. When the heating value of a fuel is specified without designating higher or lower value, it generally means the higher heating value. When complete combustion, not all fuel is completely oxidized, and the heat released is less than the heating value of the fuel. Therefore, the quantity of heat produced per unit of fuel consumed decrease, implying lower combustion efficiency. Not all heat released during combustion can be utilized effectively. The largest heat loss in the form of increased temperature(thermal energy) of hot exhaust gases above the temperature of incoming air and fuel called dry gas loss(DGL)[20]. The DGL can be calculated using: DGL = (ra, + my) * CP * [T. - Ta) (4.4) where Cp is the specific heat of flue ga.s(assumed to be the same as that of air), T, is the stack temperature, Ta is the air temperature The incomplete combustion loss (ICL) is the energy lost as a result of the formation of carbon monoxide instead of carbon dioxide in the combustion process. This loss, like the unburned carbon loss, is equal to the mass carbon monoxide produced per unit mass of fuel limes the higher heating value of carbon monoxide. The incomplete combustion loss can be obtained from the CO ICL — 23G30 *Ct* cq~^Tc02 <4 5> where C& is the mass of carbon burned per mass of fuel and CO.%, C02.% are the values of volumetric gaseous analysis 4.5 Type of liquid fuel used in experiment, The following liquid fuels were used in the experiment: 37 1. VDiseal fuel Several experiments were carried out on this type of fuel to investigate the following parameter: • temperature distribution of the flame • stack temperature • volumetric product concentration analysis 2. A mixture of shale oil and diseal fuels The properties of Jordanian shale oil used in the experiment are: • specific gravity = 0 981 • the elementary analysis are: - C% = 78.75 — H% = 9.91 - S% = 8.78 — N% = 0.42 • water content = 1.1 % by weight • calorific value(Kcal/I " viscosity = 8.47 density = 0.8852 Six sets of experiments were carried out on this type of fuel to investigate the following parameter: • temperature distribution of the flame. • stack temperature • volumetric product concentration analysis • combustion efficiency During the experimental work, the shale oil was heated to 23°C to overcome the liigli viscosity of shale oil. The shale oil was mixed with diesel at different percentage namely:5, 10, 15, 20, 25, 30 since the amount of shale oil that was supplied by NRA was terminated. It should be mentioned that the University of Jordan had tried to get 2 liter of shale oil from the NRA through the Dean of faculty of Engineering and Technology to continue my experiment, unfortunatly, the NRA was refused our request. 4.6 Experimental observation Some observation were noted during the experimental work namely : 1. The noise of the combustor was increased as the mass of the fuel was increased . 2. The length of the flame was increased as the mass of the fuel and the mass of air were increased. 3. The length of the flame of a mixture of shale oil and diesel was greater than the length of the flame of diesel liquid fuel as a result of an increase in the flame temperature. 39 4. The color of the flame turned more light orange .as the reaction reached the com pletion stages as a result of more mixing between the reactant and air. 4.7 Experimental procedure The following procedure was followed in each test: • The shale oil was heated to overcome the high viscosity of this liquid, and, at the s&me time, mixed with low fuel viscosity (diesel). » The mixture of shale oil and diesel was clean from durities by passing it through paper filter. • The tank of fuel was full of fuel before the beginning of the experiment. • The water jacket around the combustor chamber was full of water , at the beginning of the test process. • the water supply and the drain of the water was continuously opened to ensure continuous cooling. • The manometer clamps on the side of the pitot tube control panel was adjusted to give zero reading. • The pressure difference in mm H20 and the temperature distribution within the flame was measured every 5 minute. • The flame length and color were observed during the experiment operation. • After one hour of operation, the main electrical supply was switched off and the volume of diesel consumption was read NEXT PAGE(S) I left BLANK § [■■■■■■■■■iiueewMenMnJ Chapter 5 RESULTS 5.1 Introduction The temperature distribution of the flame, stack temperature, combustion efficiency, volumetric concentration of mean gaseous product, combustion process are represented. 5.2 Flame Temperature Measurement 5.2.1 Temperature of diesel Sc mixture of shale oil and diesel Figure 5.1 & 5.2 show the isothermal contours temperature lines inside the combustion chamber for diesel & mixture of shale oil and diesel. 5.2.2 Effect of air consumption on flame temperature Figure 5.3 & 5.4 show the effect of air consumption on the flame temperature inside the combustion chamber along both vertical and horizontal axes of the flame at a constant fuel consumption for diesel liquid fuel. 5.2.3 Effect of fuel consumption on the flame temperature figure 5.5 & 5.6 show the effect of fuel consumption on the flame temperature inside the combustion chamber along both vertical and horizontal axes of the flame at a constant air consumption for diesel liquid fuel. 5.2.4 Effect of air fuel ratio on the flame temperature Figures 5.7 through figure 5.10 show the effect of air fuel ratio on the (lame temperature inside the combustion chamber along both vertical and horizontal axes of the flame 5.3 Stack temperature 5.3.1 Effect of air consumption on stack temperature Figure 5.11 shows the effect of air consumption on the stack temperature at a constant fuel consumption for diesel fuel. 5.3.2 Effect of fuel consumption on stack temperature Figure 5.12 shows the effect of air consumption on the stack temperature at a constant fuel consumption for diesel fuel. 5.3.3 Effect of air fuel ratio on stack temperature Figure 5.13 & figure 5.14 show the effect of air fuel ratio on stack temperature for different types of fuel. 5.3.4 Effect of shale oil percentage on stack temperature Figure 5.15 show the of shale oil percentage on stack temperature 5.4 Volumetric concentration of the mean gaseous product 5.4.1 Effect of air consumption on volumetric concentration of the mean gaseous product As previously discussed, the analysis of the product gas concentration is an essential parameter affecting on the combustion efficiency and environment. Figure 5.16 & figure 5.17 show the effect of air consumption on volumetric concentra tion of the mean gaseous product at a constant fuel consumption for diesel fuel. 5.4.2 Effect of fuel consumption on volumetric concentration of the mean gaseous product Figure 5.18 & figure 5.19 show the effect of fuel consumption on volumetric concentration of the mean gaseous product at a constant of air consumption for diesel fuel. 5.4.3 Effect of air fuel on volumetric concentration of the mean gaseous product Figure 5.20 & figure 5.21 show the effect of air fuel ratio on volumetric concentration of the mean gaseous product for diesel liquid fuel. 5.4.4 Effect of shale oil percentage on volumetric concentra tion of the mean gaseous product Figure 5.22 & figure 5.23 show the effect of percentage of shale oil on volumetric concen tration of the mean gaseous product for shale oil fuel. 5.5 Dry gas combustion loss 5.5.1 Effect of air consumption on dry gas combustion loss Figure 5.24 shows the effect of air consumption on dry gas combustion loss (DGL) at constant fuel consumption for diesel fuel. 5.5.2 Effect of fuel consumption on dry gas combustion loss Figure 5.25 shows the effect of fuel consumption on dry gas combustion loss at constant air consumption for diesel fuel. 5.5.3 Effect of air fuel ratio on dry gas combustion loss Figure 5.26 & 5.27 show the effect of air fuel ratio on dry gas combustion loss for diesel fuel & mixture of of shale oil and diesel fuels. 5.5.4 Effect of shale oil percentage in the mixture on dry gas combustion loss figure 5.28 shows the effect of shale oil percentage in the mixture on dry gas combustion loss . 5.5.5 Effect of stack stack temperature on dry gas combustion loss figure 5.20 through 5.32 inclusive shows the effect of stack stack temperature on dry gas combustion loss for diesel fuel & mixture of shale oil and diesel fuels. 5.6 Incomplete combustion loss 5.G.1 Effect of air consumption on incomplete combustion loss Figure 5.33 shows the effect of air consumption on incomplete combustion loss at constant fuel consumption for diesel fuel. 5.6.2 Effect of fuel consumption on incomplete combustion loss Figure 5.34 shows the effect of fuel consumption on incomplete combustion loss constant air consumption for diesel fuel. 5.6.3 Effect of air fuel ratio on incomplete combustion loss Figure 5.35 & 5.36 show effect of air fuel ratio on incomplete combustion loss for diesel fuel & mixture of shale oil and diesel fuels. 5.6.4 Effect of carbon monoxide and carbon dioxide on incom plete combustion loss Figure 5.37 shows the effect of carbon monoxide and carbon dioxide on incomplete com bustion loss for diesel fuel & mixture of shale oil and diesel fuels. «tb Chapter 6 DISCUSSION As previously mentioned, the experiments were carried out to investigate the following items: 1. the flame temperature along the vertical and horizontal axes of the flame 2. volumetric concentration of the main gaseous product 3. stack temperature This chapter is devoted to discuss the results obtained during this research. 6.1 Flame Temperature 6.1.1 Flame temperature within diesel flame & mixture of shale oil and diesel flames Figures 5.1 and 5.2 show the isothermal contours temperature lines of diesel fuel, & a mixture of shale oil and diesel fuel flames. As expected ,the flame temperature of the mixture of shale oil & diesel fuels was higher than the flame temperature of diesel fuel , since the calorific value of the mixture of shale oil & diesel fuels was greater than the calorific value of diesel fuel. 47 6.1.2 Effect of air consumption on the flame temperature Figure2 5.3 and 5.4 show the effect of air consumption on flame temperature along the vertical and horizontal axes for diesel fuel.The general trend of these curve indicate con tinuous increase in the flame temperature along the vertical and horizontal axes as the air consumption is increased. This is due to the fact that as more air is supplied the combustion efficiency will increase which leads to an increase of the temperature. 6.1.3 Effect of fuel consumption on the flame temperature All figures that contain only two data points are used to give an indication of the be haviour of the specified parameter since the experimental measurement are only a pre- mi raly ones. Figures 5.5 and 5.6 show the effect of fuel consumption on the flame temperature along both vertical and horizontal axes for diesel fuel. The general trend of these curves indicate continuous increase in the flame temperature ns the fuel consumption is increased. This is due to the fact that the rate at which heat or thermal energy released will be increased ns a result of increase fuel consumption. 6.1.4 Effect of air fuel ratio on the flame temperature Figures 5.7 through figure 5.10 show the effect of air fuel ratio on the flame temperature along vertical and horizontal axes for diesel fuel, and mixture of shale oil & diesel fuels. As expected, the general trend of these curves indicates that the flame temperature will be increased with the air fuel ratio, this is due in the fact that as more air is supplied, the < 'unbustiou efficiency will increase which leads to a raise in the flame temperature. Also when the air fuel ratio reaches its optimum value, the flame temperature will be decreased with air fuel ratio because the combustion effecicncy was decreased. 48 6.2 Stack temperature G.2.1 Effect of air consumption on stack temperature Figure 5.11 shows the effect of air consumption on stack temperature at constant diesel fuel consumption. The general trend of this curve indicates continuous decreasing in stack temperature as the air consumption was increased, as a result of cooling the gaseous product by the excess air in the exhaust. G.2.2 Effect of fuel consumption on stack temperature Figure 5.12 shows the effect of diesel fuel consumption on slack temperature at constant air consumption. The general trend of this curve indicates continuous increase in slack temperature with the diesel fuel consumption, as a result of more release of heat or thermal energy. G.2.3 Effect of air fuel ratio on stack temperature Figures 5.13 and 5.14 show the variation of stack temperature with air fuel ratio. As expected, the general trend of this curve indicate that the stack temperature will be increased with air fuel ratio as a result of increasing in the combustion rlfeciency. when I lie air fuel ratio reaches its optimum value the stack temperature will be decreased with the air fuel ratio as a result of decreasing in the combustion effeciency. 6.2.4 Effect of shale oil percent in the mixture on stack tem perature Figure 5.15 shows the effect of shale oil percentage in the mixture on slack temperature. As previously mentioned, the stack temperature was affected by the heat or thermal en ergy released, which depends on the calorific value of the fuel, so that the energy released will be increased as the percent of shale oil in the mixture is increased. Consequently the stack temperature will be increased with shale oil percent increased. 6.3 volumetric product concentration of the main gaseous product 6.3.1 Effect of air consumption on volumetric concentration of the main gaseous product at constant diesel fuel con sumption Figures 5.16 and 5.17 show the effect of air consumption on the volumetric concentration of the following gaseous product: • oxygen content • nitrogen content • carbon momoxide( CO )content • carbon dioxide( Co2 )content Basically, as the air consumption is increased, the carbon monoxide will react with oxygen to produced carbon dioxide. Consequently, the volumetric concentration of carbon dioxide will be increased & the volumetric concentration of carbon monoxide will be decreased as more air is supplied.ns a result of increasing of combustion elfccicncy The general trend of these curves indicates an increase in the concentration of nitrogen & 50 carbon doixide and a decrease in the concentration of oxygen &: carbon monoxide , as a result of increasing the air consumption. 6.3.2 Effect of fuel consumption on volumetric product con centration at constant mass of air consumption Figures 5.18 and 5.19 show the effect of increase fuel consumption on volumetric product concentration. Basically, as the fuel consumption is increased, the concentration of carbon monoxide will be increased, and the concentration of carbon dioxide will be decreased ms a result of incomplete combustion The general trend of these curve indicate a decrease in concentration of oxygen and carbon dioxide and a relative increase in concentration of oxygen and carbon monoxide . 6.3.3 Effect of air fuel ratio on volumetric concentration of the mean product Figures 5.20 and 5.21 show the effect of air fuel ratio on volumetric concentration. As expected, the general trend of this curve indicate that the volumetric concentration of the of carbon monoxide was increased while that of the carbon dioxide was decreased as the air fuel ratio was increased, as a result of incomplete combustion. When the air fuel ratio reaches its optimum value, the volumetric concentration of nitrogen and carbon monoxide will be decreased while that of oxygen and carbon dioxide will be increased 6.3.4 Effect of shale oil percentage on volumetric product con centration Figures 5.22 and 5.23 show the effect of shale oil percentage with diesel on the volumetric product concentration. The general trend of these curve indicate that this effect is the same as that of diesel fuel. 6.4 Dry gas combustion loss As previously mention in chapter 3, the DGL was function mainly of stack temperature and mass of flue gas. 6.4.1 Effect of air consumption on dry gas combustion loss Tliis section is devoted to reresent the effect of air consumption, fuel consumption, air fuel consumption, and stack temperature on the percent of dry gas loss of higher heating value. Figure 5.24 shows the effect of air consumption on percent of dry gas combustion loss (DGL)at constant fuel consumption for diesel fuel. The general trend of this curve indi cate that the variation of DGL is relatively constant as the air consumption is relatively increased because the stack temperature was relatively decreased. 6.4.2 Effect of fuel consumption on dry gas combustion loss Figure 5.25 shows the effect of fuel consumption on the percent of dry gas combustion loss at constant air consumption for diesel fuel. The general trend of this curve indi cate continuous increase in DGL as the fuel consumption is increased since the stack temperature was increased. 6.4.3 Effect of air fuel ratio on dry gas combustion loss Figures 5.26 and 5.27 show the effect of air fuel ratio on dry gas combustion loss for diesel fuel & mixture of of shale oil and diesel fuels. As expected, the general trend of these curve indicate that the DGL will he increased as the air fuel ratio was increased, until the air fuel ratio reach its optimum value, because the stack temperature was increased, then, the percent of the DGL will be decreased with increase in the air fuel ratio because the stack temperature was decreased. 6.4.4 Effect of shale oil percentage in the mixture on dry gas combustion loss Figure 5.28 shows the effect of shale oil percentage in the mixture on dry gas combustion loss. The general trend of this curve indicate continuous decreasing in DGL ns the percent of shale oil in the mixture is increased because the stack temperature was decreased. 6.4.5 Effect of stack stack temperature on dry gas combustion loss Figure 5.29 through 5.32 inclusive show the effect of stack temperature on dry gas com bustion loss for diesel fuel & mixture of shale oil and diesel fuels. As previously mention in chapter 4, the DGL was mainly function of slack tempera ture, as a result, the general trend of figure 5.29 indicate continuous increase in DGL as the fuel consumption was increased, also, the general trend of figure 5.30 indicated that that the DGL was relatively constant as a relative increase in air consumption. Further more, the general trend of figure 5.31 & 5.32 indicate that the DGL will be increased as the air fuel ratio is increased, until the air fuel ratio reach its optimum value, because • he stack temperature was increased, then, the DGL will be decreased with increase in the air fuel ratio because the stack temperature was decreased. 6.5 Incomplete combustion loss 6.5.1 Effect of air consumption on incomplete combustion loss Figure 5.33 shows the effect of air consumption on incomplete combustion loss at constant fuel consumption for diesel fuel. The general trend of this curve shows continuous decrease of ICL as the air consumption was increased because the carbon monoxide was decreased and the carbon dioxide was increased. 6.5.2 Effect of fuel consumption on incomplete combustion loss Figure 5.34 shows the effect of fuel consumption on incomplete combustion loss constant air consumption for diesel fuel. The trend of this curve indicated continuous increasing of ICL as the fuel consump tion was increased because the carbon monoxide(CO) was increased and the carbon dioxide(C02) was decreased. 6.5.3 Effect of air fuel ratio on incomplete combustion loss Figures 5.35 and 5.36 show effect of air fuel ratio on incomplete combustion loss for diesel fuel & mixture of shale oil and diesel fuels. The general trend of this curve indicate that the ICL will be increased as the air fuel ratio was increased, until the air fuel ratio reach its optimum value, because the carbon monoxide(CO) was increased & the carbon dioxide (C02) was decreased, then, the ICI will be decreased with increase in the air fuel ratio because the carbon monoxide will be decreased and carbon dioxide will be increased I NEXT PAGElS) ! ANK rf-'Y r^Tgarml Chapter 7 Conclusion and Recommendation 7.1 Conclusions This section is devoted to asses the important points which have emerged from the present investigation. These can be summarized as follows: 1. It was found that the temperature of shale oil is greater than temperature of diesel under the same conditions. 2. The emissions of sulfur monoxide and dioxide during diesel fuel combustion was lower than that of a mixture of shale oil and diesel fuels. 3. The NOx emissions for diesel was 14 PPM. 4. The percentage of the dry gas energy loss from the higher heating value was very high 5. The incomplete combustion loss was very low. 7.2 Recommendation The literature survey together with the present experimental investigation suggest that there are areas which need further experimental and theoretical investigation. Some of these areas are mentioned in this section as follows: 56 • Studying the effect of oil shale on environment especially the fly ash. • Studying the mode of heat transfer rate along the combustor wall experimentally and theoretically . • Building large retorting unit to extract the shale oil . • Investigation the effect of the location at which the gas sample was withdrawn on the volumetric concentration . • Studying the burning of oil shale directly in CFB NEXT PAGEIS) ieU BLANK tsse&asae arimm references 1. Jordan Electric!ty Authority "The Investment of Oil Shale by Direct Combustion", Report , Amman, Augest 1991. 2. Ministry of Energy and Mineral Resources, NRA, "Mineral Resources of Jordan", Amman, 1989. 3. Natural Resources Authority, Report, Jordan, "Oil Shale”, 1990. 4. Fox et al. "Chemical Characterization and Analytical Consideration for an in Situ Oil Shale Process Water”, Department of Energy, Latame, WY, Energy Technology Center, 49P, November 78. 5. Ilepler et al. "Toxicological Evaluation of an in Situ Oil Shale Process Water”, Oil Shale Symp Process, Golden, Colo., Publ by Colo Sch of Mines Press, Golden, pp.139-148, Aprial 18-20, 1979. G. Sierka et al. "Physical — Chemical Treatment of Oil Shale Retort Water", Process of the Specific Configuration — Water Form ' 81, San Francisco, Califonia, USA, vol. 2, pp.902-909, Augest 10-14 1981. 7. Chen cl id. "Basic. Mechanism to Achieve Clean Combustion of Oil Shale in Flu idized Beds", "National Science Foundnalion, Washington, DC. Div. of INduslrial Science and Technological Innovation", Report no.: N5F/CPE-82(.117 , pp.117, 31 March 82 . 8. Kuchi, M. ; Steller, P., ’’Technical Study on the Possibility of Oil Shale Combustion in a Fluidized Red Furnace Including Cost Estimate for a Plant to He Constructed ”, Report no. : DM FT- TB- T- 82-085 June 82 G3P. 9. Macauley et al. "Some Geological Consideration for the Economic Evaluation of Candian Oil Shale deposits", Oil Shale Symp. Proc., pp.G 1-13, 1983. 10. Department of Energy, Morgantown, Wv. Morgantown Energy Technology Center, "Oil Shale Combustion Retorting", Report no.: DOE/METC/SP-197 pp.49, May 83. 11. Insguva, lb, "Physics of Oil Shale : A Program of Theoretical and Experimen tal Studies", Quarterly Progress Report, , Report no. : DOE/LC/ ID7R3-6, pp.7, January 1- April 1, 1983. 1.2. Levy, Y., "Pressurized Fluidized Bed Combustion Using Oil Shale for Gas Tur bine Operation ”, Journal of the Institute of energy, void, No/1/18, pp.157-16'1, September 1988. 13. Vasatos et al. "Modeling of Oil Shale Fluid Bed Combustor", Industrial & Engi neering Chemistry Research, vol.27, No. 2, , pp 317-321, Febuary 1988. 1-1. Shirav (Schwartz) cl al. "Pathway of Trace Element During Oil Shah: Combustion/-A In Their Availability fur Leaching Process ’’, Envirornctilal Geoh'gy mid Water Sci ence, vol.ll, No.l, Febuary 1988. 60 j5. Krypina et al. "Ail Lnvctigalion of the tlicnnal Decomposition of Combustible Shale", Ilimija tverdogo topliva, 1989(4) 16-21. 1C. Dung et al. "Modeling of Oil Shale Retorting Block Using ASPEN Process", Fuel, vol.69, no. 9, pp.1113-1118, September 1990. 17. Natural Resources Authority, "Oil Shale Resources in Jordan" 18. Betchal National, "Prefcasibilily Study Oil Shale Utilization for Power Production in the Hashemite Kingdom of Jordan ”, vol.VI of VI- Appendices 7 Thru 12, Report no. 89-02, May 1989. 10. SP Slianna, Chander Moliam "Fuels and Combustion", Tala McGraw-Hill Jjic ., 1984. 20. Culp "Principle of Energy Conversion ”, McGraw-Hill, Inc., 1979. 21. Richard Stone "Introuction to Internal Combustion Engines, Macmillan Publishers LTD, 1985. 22. O’Sulivan et al. "Coal-Fired Process Heaters”, Energy Managmenl, pp.87-94. 23. Audi ,IIeat and Ventilation Oil burners. NEXT PAGE(S) left BLANK appendix Diffusion flame Pre mixed flame Air regulator wit.li p remixed and diffusion flames L'a 0 Bunsen burner Riire 1 64- Figure 3.2 Comparison between laminar ancl turbulent, fronts for premixed combustion C 2# J 05 Air Fuel vapour Figure 3.3 Comparison between laminar flame front in stagnant air with turbulent flame front and ordered air motion for diffusion controlled combustion C 5» 3 (if-i 0.0? Figure '1.1 The combustor rig component 67 Figure 4.2 Combustor section showing cout.ant bottom Burner - 4..3 Sectional view oi burner wall showing combustor shape 53 T n[i J-t)>? I •jt-i !!ii|! L. Ash hopper Bottom U-bends —- -A_L/ 0 a I lie Figure 4.4 Sectional view of the vertical tube convection section 70 o oo Flue gas —liCtui. Figure 4.5 Sectional plan showing lire box and sonvection section 71 NEXT FAQE(S) 73 Figure. 4.8 Hollow spray cone pattern 74 Figure 4A) Solid spray cone pattern 7% 76 Figure 4.11 Gas sampling arrangement air vacuum pump glass flask absorbing material ballon 77 r1in1..«nr<; I fmji't.il Iir<* Imri iushI'* < l>r < ..iuli|-:l wix Ji.] Isnl IkTIII.I -li -vi m!.f-.r f <• *-«] f«11 LO CU figure 5.2 hothcrmil cnnlimrs icmp'-r-ihirc lines imM'" the cnmlmslirm rlwml.'rr f<.»r mixlure »»f slirvlr oil fc 'liesrl r 0 mo—20.22 gm#/* ^ma=»24.76 gme/« 1000 r ? 700 l 500 15 , , 20 Axfot dfetoncofrom tho noxzf* Up (cm) Figure 5.3 Horizontal axes temperature distribution for two different quantity of air flow for diesel fuel Flame temperature along the vertical axes (C) 500 400 600 Figure - - - O mo 5.4 i — 24.763 Vertical gmi/i axes temperature Vertical £ of ma»*2Q.21 air flow distance 8 for gme/e distribution from diesel the fuel nozzle for tlp(cm) two different quantity =§ the axes of flame (C) Figure 700 Qmf- 5.5 Horizontal 0.4668 gm«/s quantity axes eml-,6539 temperature Axial of distance fuel for gme from /1 diesel distribution the nozzle fuel tip (cm) for two different d\ 1100 r • mf—.5538 gme/« ^mf«».e651 gme/e 900 - 800 - £ 700 Vertical dletance from the nozzle tip (cm) Figure 5.6 Vertical axes temperature distribution for two different quantity of fuel for diesel fuel qx —5 cm /, x-25 cm O O Air fuel ratio Figure 5.7 Effect of air fuel ratio on the variation of the flame temperature along the horizontal axes for diesel fuel t£4 q. 5 cm —5 cm 540 r f 380 Figure 5.8 EiFect of Air fuel ratio on tLe variation of llame Ifmperature t along the vertical axes for diesel fuel tl x~ 25 000 r 500 l Air fuel ratio Figure 5-ti f.lfect «ir fuel ratio mi the variation of the !Ume tern;:,rnmr: along the horizontal axes for oil shale g>.n j- 0 >,-|i-,| i u 5" aiv o } o; 11 # | r> viivj ii" j>|j jva \ iv uvi jo sip ^tuvrj^ «oC* mf-.4405a 9gm/e Air consumptlon(gm/») Figure 5.11 EIFect of air consumption on stack temperature under constant fuel consumption for diesel fuel 8.300 Fuel consumption (gms/s) Figure 5.12 Effect of fuel consumption on stack temperature under constant air consumption for diesel fuel Air fuel ratio Figure 5.13 variation of air fuel ratio with stack temperature for diesel fuel 600 r Air fuel ratio Figure 5.14 variation of air fuel ratio with stack temperature for mixture of shale oil k. diesel fuel 91 Shale oil percent by volume Figure 5.15 Effect of percentage of shale oil in the mixture on stack temperature Volumetric product concentration carbon Figure monoxide 5.16 Effect and of air carbon Air consumption consumption dioxide diesel fuel (gms/e) at on constant volumetric fuel concentration consumption for of 9& Volumetric product concentration # Figure oxygen N2 5.17 and Effect nitrogen of air A Air at 02 consumption coneumptlon(gme/e) constant fuel on consumption volumetric concentration for diesel fuel of e co A C02 AJr fuel ratio Figure 5.18 EiFect of fuel consumption on volumetric concentration of carbon monoxide and carbon dioxide at constant air consumption for diesel fuel 95 0.56 , Fuel consumption (gms/s) Figure 5..19 Effect of fuel consumption on volumetric concent ration •’! osygen c«u Figure -44 5.20 and Variation carbon 46 dioxide of volumetric 48 with Air fuel air ratio concentration 50 fuel ratio 52 for 54 "Z> of diesel carbon V fuel monoxide 56 X ioo r Air fuel ratio Figure 5.21 Variation of volumetric concentration of oxygen and nitrogen with air fuel ratio for diesel fuel Volumetric product concentration Figure 5.22 and Variation carbon of dioxide volumetric with concentration percentage of of shale carbon oil monoxide / Volumetric goaoua concentration 100 r Figure 5.23 Variation of with Shale volumetric percentage oil percent concentration by volume of shale oil of oxygen and nitrogen Dry gaseous loss percentage Figure 5.24 ElFrct. of air consumption consumption Air consumption for on diesel (gm/s) «.lry fuel gas loss at constant fuel Fuel coneumptlon (gm/e) Figure 5.25 ElFect of fuel consumption on dry gas loss at constant air consumption for diesel fuel Air fuel ratio Figure 5.26 Variation of dry gas loss with air fuel ratio for diesel fuel 11)3 AJr fuel retie f i-.'iifr t Variation «>f .fry 5 as lost will) air fu*l ratio }nr ,,,| 104 Shole oil percentage Figure 5.28 Variation of dry gas loss with percentage of shale oil for diesel fuel 70 60 50 8 O **• 20------'------»— 250 260 270 280 290 300 31 0 St o ck temper olure (C) Figure 5.29 Variation ol dry combustion loss |>cirentage with stark temperature at constant aii consumption for diesel fuel 300 , % Stock temperoturo (C) Figure 5.30 Variation of dry combustion loss percentage with stack temperature at constant furl consumption for diesel fuel 107 420 43( Stack temperature (C) Figure 5.31 Variation of dry combustion loss percenta^r with stack temperature for diesel fuel 110 fe>i 20 * 1 t. . —.i.. . - x------1------1------1——I------1—.—j 375 400 425 450 475 500 Stock temperature (C) Figure E>.-32 Variation of dry combustion loss percentage with stack temperature for mixture of shale oil k. diesel fuels I — Incomplete gaeeoua lose (KJ/Kg) 10.00 Figure r Fi.."V3 Eifect. ol -iir consumi'l-ion Alr consumption on (gm/s) inconjjilclr loss lor -liesrl furl 10^ loss (KJ/Kg) 101 r Figure 5.3*1 EIFert. «>f fuel fuel Fuel consumption consumption consumption (gm/») for on diesel ineonij>lc(-c furl less ol ronst-'viit Incomplete gaseous loss (KJ/Kg) 10' 42 r Figure 5.35 44 V.iri.\lio» 46 of incomplete for 48 Air diesel fuel rmnl.mstiou ratio fuel 50 loss 52 witli ,\ir 54 fuel ratio 56 111 j=lUUi ji^LoJI Oj)JI jl/Lxl Jj_M < Jii-J I—J-*J Juu-“< J-h? *->La L>-* ^>Vva-» j jU. tluuj { \ »..rt'> 4_ILujJI ai» ^3 , JjjjJI 4_l—u-i yj I «lj_fJI 4_U-uu yLo. ^3 oiJ . ■> i/J I J_ju-J! 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