Historical overview of using fluidized-bed technology for oil shale combustion in Estonia.
The first fluidized-bed combustor with heat output of 0.15 [MW.sub.th] was completed in the Department of Furnaces of IIR in 1949-1950 under the guidance of Hans Truu, and the first oil shale combustion tests were carried out in 1951 . The first results of oil shale combustion tests in this fluidized-bed combustor were successful and formed the main part of his doctoral thesis. To curry out industrial tests of this technology the reconstruction project of a 10-[MW.sub.th] boiler with mechanical grate in the Pussi Power Plant was worked out. In 1957, the year H. Truu died, the reconstruction of the boiler was completed. In 1959 the boiler was fired up, and the oil shale combustion tests lasted up until 1962 [2, 3]. After industrial combustion tests the laboratory tests of Estonian oil shale and other fuels in fluidized bed continued in TEFI [4, 5]. A new laboratory oil shale fluidized bed gasifier with heat output of 0.2 [MW.sub.th] was constructed, basing on the experience of the industrial and laboratory experiments .The construction of the new oil shale gasifier was protected by the Author's Certificate USSR 709938 .
For industrial tests for oil shale combustion with gasification in fluidized bed a new fluidized bed gasifier with heat output of 35 [MW.sub.th] was worked out . For unknown reasons the implementation of the project in the Kohtla-Jarve Power Plant was not completed.
The first laboratory fluidized bed combustor
The layout of the first experimental fluidized-bed furnace for burning oil shale fines successfully tested in 1951 is presented in Fig. 1.
The main dimensions of the experimental fluidized bed furnace were: diameter of the gasification chamber 205 mm and height--980 mm, grate area--0.0288 [m.sup.2] and the part of free flow of the grate area--1.3%; diameter of the burning chamber of gasification products--340 mm and height 1000--mm.
The process parameters of the experiments of the first laboratory fluidized bed furnace are given in Table 1.
The process parameters of the experimental fluidized-bed furnace (fuel load, primary and secondary air amount) were varied on a large scale. It enabled to determine temperature limits (margins) of oil shale bubbling bed. The lowest bed temperature was higher than the oil shale inflammation temperature, and the highest temperature was lower than the fuel ash sintering temperature. In the fluidized bed coarse coke and a small amount of gas were burned to get heat for oil shale gasification. In the temperature range of bubbling bed 568-1035 [degrees]C the apparent heat load of the grate was 2.28-4.61 MW/[m.sup.2]. The gasification products and fine coke particles were burned in the burning chamber with secondary air.
[FIGURE 1 OMITTED]
The main results of the first experiments of oil shale combustion in the laboratory fluidized bed furnace were as follows:
* The usability of the fluidized-bed technology for oil shale combustion was successfully proved.
* High content of the volatile matter of oil shale (average content in used oil shale was 82.5%) enabled to use the gasification process of oil shale in fluidized bed. It allowed significantly to decrease the grate area.
* For oil shale a new combustion technology was proposed. Oil shale is gasified in the fluidized bed, and the gasification products and fine coke particles are burned in a separate furnace.
The first industrial fluidized-bed combustor
Good results of laboratory tests encouraged to carry out industrial tests of oil shale combustion with gasification in fluidized bed. Under the guidance of Dr. Sc. H. Truu a project for reconstruction of a 10-[MW.sub.th] boiler with mechanical grate in the Pussi Power Plant was worked out. In the process of reconstruction the mechanical grate of the boiler was removed, and the fluidized bed gasifier and the burning chamber of gasification products and fine fly coke were inserted in front of the boiler. In 1957 the reconstruction of the boiler was completed.
The cross-section of the fluidized bed gasifier and the combustion chamber of gasification products and fine fly coke of the reconstructed boiler in the Pussi Power Plant is presented in Fig. 2.
The grate of the fluidized-bed gasifier was made from cast iron plate. The grate area was 2.8 [m.sup.2] (width 1 m, length 2.8 m) and the open-grate area made 2.3% of it. The air box under the grate was divided into three parts along the grate length; it enabled to regulate the primary air input into different parts of the fluidized bed. The inclination angle of the grate was 5[degrees] in the direction of the end. Gasification products and fine coke particles were burned in the combustion chamber with secondary air. For better separation of ash from gases the combustion chamber was designed in the form of horizontal (semi)cyclone. The combustion products were cooled in the furnace and in the convection pass of the boiler, purified from fly ash in the cyclone and directed into the atmosphere with the help of the flue-gas exhauster.
[FIGURE 2 OMITTED]
In 1958 the first team from the Department of Furnaces Endel Jurismaa (head), Ants Martins and Roland Karjus started the fieldwork in the Pussi Power Plant to fire up the reconstructed boiler. It took about one and a half year to amend and improve some components of the reconstructed boiler. In 1959 the boiler was fired up and oil shale combustion tests lasted up until 1962 .
Oil shale used for experiments (max particle size 3-5 mm) was screened out from oil shale used in the Pussi Power Plant furnaces. It took about a week to fulfil the hopper of the reconstructed boiler with screened oil shale (about 90 t) sufficient for one experiment with duration maximally 30 hours. If there had been a stationary oil shale preparation system, the reconstructed boiler would have worked continuously.
For preheating of the fluidized-bed gasifier wood (about 30-40 kg) was burned on the grate, which was covered with oil shale ash. After burning of wood oil shale was led into the gasifier. The general start-up time of the boiler lasted 1.5-2.5 hours, after that the steam from the boiler was directed into the steam turbine.
The oil shale was led into the gasifier by screw conveyor at the input to the grate. By the general idea of that time the fuel, canalised into fluidized bed, had to mix very quickly with whole bed material. Actually the mixing of fresh oil shale particles with bed material was of local character at the input to the grate. The bed material (fuel, coke and ash particles) moved on along the grate like a fluid, with speed determined by fuel load. Due to the horizontal movement of the bed material, oil shale gasification took place in the first zone of the bed, burning of coarse coke particles occurred in the second zone, and the third zone worked as the hot ash cooler (or air heater). The medium thickness of the fluidized bed was regulated by the height of the grate barrier.
The preliminary tests showed that the area 2.8 [m.sup.2] of the fluidized-bed grate was designed too large for the boiler in operation, as coke was completely burned out in the second zone at the full load of the boiler. Therefore the last part of the air box was closed and the grate area decreased to 1.8 [m.sup.2]. The process parameters of the experiments of the industrial fluidized-bed furnace are given in Table 2.
There was no need to use heat exchange surfaces in the bed. In the gasification zone temperature level of the bed was very easy to regulate with the amount of primary air ([[alpha].sub.1] = 0.35-0.45). In the coke combustion zone the temperature was higher (895-958 [degrees]C) than that in the gasification zone, but much lower than the sintering temperature of the bed ash (about 1050 [degrees]C).
The combustion process of gases and fine fly coke was very intensive in the burning chamber due to high temperature of gases and very good mixing of gases and secondary air. Therefore sometimes the temperatures in burning chamber exceeded the temperatures of ash sintering and melting. To prevent this process the amount of cold secondary air was increased ([[alpha].sub.2] = 1.4-1.7) and frequent ash separation from the burning chamber was provided.
Aerodynamic separation of coke and ashes particles took place in the fluidized bed gasifier. The content of CaO + MgO in the bottom ash from the gasifier was 45-50% and that in the bottom ash from the combustion chamber 36-39%. The decomposition rate of carbonate compounds of the oil shale mineral part in ashes from the fluidized bed was 82-97% and in bottom ashes from the burning chamber 85-98%.
Basing on the first industrial tests of oil shale combustion with gasification in the fluidized bed the following observations attracted attention:
* The lengthwise motion of the bubbling fluidized bed along the grate demonstrated the obvious formation of the gasification zone of oil shale and the combustion zone of coarse coke particles.
* The rate of ash separation from the fluidized-bed gasifier together with the ash from the burning chamber formed 85-88% of fuel ash.
* The combustion process of the gases and fine fly coke in the burning chamber was very intensive due to high temperature of gases and very good mixing of gases with secondary air, and therefore sometimes the temperatures in the burning chamber exceeded the temperatures of ash sintering and melting.
* Depending on aerodynamic separation, the chemical content of the mineral part of ashes from the gasifier and from the combustion chamber differed substantially. It brought about the fact that the melting temperature of the bottom ash from the burning chamber was lower than that of the ash from the fluidized bed.
The new bench-scale oil shale fluidized-bed gasifier
After completing oil shale industrial combustion tests in the Pussi Power Plant, the laboratory combustion tests of Estonian oil shale and other fuels continued in EEI.
A new laboratory oil shale fluidized bed gasifier with heat output of 0.2 [MW.sub.th] was constructed, basing on the experience of industrial and laboratory experiments [4-6]. The diagram of the new gasifier is given in Fig. 3.
[FIGURE 3 OMITTED]
The main modernizations of the new test bench were:
* dividing wall 5 between the gasification zone 2 and coke combustion zones 3 and 4;
* transfer of coarse coke into the combustion zone through the hole 7 in the dividing wall 5;
* cleaning of hot gases in the fly coke separator 8;
* canalisation of separated fly coke back into the fluidized bed in the coke combustion zone;
* combustion of coarse and fly coke in different combustion zones in 3 and 4, separated by the barrier 6.
The air for combustion of coarse and fine coke was introduced into fluidized beds from different air boxes. It enabled to regulate the appropriate air speed for fluidization of coarse and fine coke and to prevent the secondary elutriation of fly coke and fly coke ash from the fluidized bed.
The construction of the new oil shale gasifier was protected by the Author's Certificate USSR 709938 .
The principle objectives of the tests were:
* to assess suitable temperature level for oil shale gasification in the fluidized bed and sulphur capture in the fluidized bed and in the freeboard on the one hand;
* to guarantee complete combustion of coke residue in the fluidized bed and to avoid the ash sintering process in the gasifier on the other hand [9, 10].
The chemical analysis of the used oil shale was the following: [Q.sup.d.sub.i] = 11.75 MJ/kg, [(C[O.sub.2]).sup.d.sub.k] = 18.93%; [S.sup.d] = 1.7%; [A.sup.d] = 48.40 %; particle size--0-3 mm.
In the oil shale gasification zone the fluidized bed temperature was regulated only by the amount of primary air. In the range of the excess air rate from 0.28 to 0.53 the temperature in the fluidized bed rose from 800 to 950 [degrees]C. At the same time the calorific value of hot gases decreased from 7000 to 4000 kJ/[m.sup.3]. The temperature in the gasification zone was regulated only by the amount of primary air. The dependence of calorific value and temperature of hot gases on the excess air rate is presented in Fig. 4.
[FIGURE 4 OMITTED]
The apparent heat load of the grate in the gasification zone was 3.9-5.9 MW/[m.sup.2]. The apparent heat load of the fluidized bed gasifier grate was controlled by Formula 1 :
Q/F = [q.sub.a] x [w.sub.0]/[alpha], MW/[m.sup.2], (1)
Q--heat supplied into the fluidized bed with fuel, MW;
F--fluidized bed grate area, [m.sup.2];
[q.sub.a] = [Q.sup.r.sub.i]/[W.sub.0], MJ/[m.sup.3] ([Q.sup.r.sub.i],--calorific value of oil shale as received, MJ/kg,
[W.sub.0]--theoretical amount of dry air for complete combustion of oil shale, [m.sup.3]/kg);
[w.sub.0]--air speed, m/s;
[alpha]--excess air rate.
The bed temperature is one of the most sensitive parameters for sulphur capture in the fluidized-bed combustor. The other parameters are the presence of sorbent (Ca, Mg) and time for chemical reaction. The mineral part of oil shale contains a sufficient amount of carbonate compounds to bind the sulphur in it, in oil shale the molar ratio Ca/S = 7-8. The ratio Ca/S = 2.5-3 is sufficient for the total capture of sulphur .
During oil shale gasification the sulphur in gases was mainly in the form of [H.sub.2]S. The sulphur capture process in the fluidized-bed gasifier occurred according to the following reactions [13, 14]: calcination of carbonate compounds of oil shale mineral part in the gasification zone
CaC[O.sub.3] [right arrow] CaO + C[O.sub.2]; (2)
capture reactions in the gasification zone
CaO + [H.sub.2]S - CaS + [H.sub.2]O (3)
CaC[O.sub.3] + [H.sub.2]S - CaS + [H.sub.2]O + C[O.sub.2]; (4)
oxidation reaction in the zones of coarse and fine coke combustion
CaS + 2[O.sub.2] [right arrow] CaS[O.sub.4]. (5)
Maximum sulphur capture rate 0.9 was measured at temperatures from 828 to 850 [degrees]C in the fluidized bed and in the freeboard of the gasifier (Fig. 5). During performed tests two main sulphur capture requirements were guaranteed: suitable temperature interval and needed calcium to sulphur molar ratio (Ca/S). However, the time for capture reactions was too short (about 2 s) because of small dimensions of the gasification chamber to achieve the maximum feasible sulphur capture rate. Theoretically it was approved that sulphur capture rate 0.99 could be achieved in case the retention time is 4-5 s .
[FIGURE 5 OMITTED]
The complete combustion of coke and oxidation of sulphides were guaranteed at medium temperature of the fluidized bed 895 [degrees]C and excess air rate 1.15-1.25 in the coke combustion zone (Fig. 3-4, 5). 85-89% of oil shale ash was discharged from the gasifier.
Temperature rise in the fluidized bed, especially in the gasification zone in the deoxidation medium, caused ash sintering and collapse of fluidization. Temperatures of ash sintering and softening depend on its chemical composition [15,16]. Chemical composition of ash fractions is heterogeneous, most changeable is the content of Si[O.sub.2] and CaO. Due to aerodynamic separation in fly ash the content of Si[O.sub.2] is increased and CaO content is decreased. CaO content of the coarse bottom ash was 41-45% and of the fine bottom ash 33-36%.
A special method was elaborated for determination of the sintering temperature of oil shale ash . This method enabled to determine experimentally the dependence of oil shale ash sintering temperature [T.sub.s] on the ratio Si[O.sub.2]/CaO = [m.sub.0]. The increase in CaO content of oil shale ash increases the sintering temperature of ash.
The sintering temperature of oil shale ash is described by empirical Formula:
[T.sub.s] = 1530 - 366 x [m.sub.0], K. (6)
Member of Estonian Academy of Sciences I. Opik defined the deformation temperature of oil shale ashes by Formula :
[T.sub.1] = 1730 - 233 x [m.sub.0], K. (7)
From Formulas (6) and (7) it follows:
[T.sub.s] = 1.57 x [T.sub.1] - 1188, K. (8)
Formula (8) could be used for evaluation of sintering temperatures [T.sub.s] of oil shale ash in the case the deformation temperatures [T.sub.1] of these ash samples are measured by the standard method.
The main results of testing the improved model of the oil shale fluidized-bed gasifier:
* Oil shale gasification tests in the fluidized bed enabled to determine the influence of the excess air rate on the temperature in the fluidized bed and on calorific value of hot gases.
* The combustion of coarse and fine coke in separate zones of the gasifier enabled to discharge 85-89% of oil shale ash from the gasifier.
* For the first time it was experimentally proved that the use of the fluidized-bed technology enables to bind oil shale sulphur with carbonate compounds of oil shale ash. The optimum sulphur capture process took place within the temperature range 800-850 [degrees]C in the fluidized bed and in the freeboard. The moderate sulphur capture rate 0.9 was achieved because dimensions of the gasification chamber of laboratory test bench were small. Theoretically it was approved that sulphur capture rate 0.99 could be achieved in case the retention time is 4-5 s .
* The sintering temperatures of oil shale ash are substantially lower than their deformation temperatures (Formula 7). The temperature rise over [T.sub.s] in the bubbling fluidized bed caused the collapse of fluidization especially during the fire-up time, when the temperature regime of the bed was not stable.
Combustion of cleaned gases
Hot gases from the gasifier were burned in the compact vertical cyclone furnace . The temperature of gases was 740-870 [degrees]C and ash content 43-58 g/[nm.sup.3]. The walls of the cyclone furnace were cooled by secondary air to get hot air for combustion of gases. The air tubes were covered with refractory bricks. The temperature of secondary air was in the range 555-640 [degrees]C. The combustion process of hot gases with hot secondary air was very intensive and the temperature achieved the level of 1420-1640 [degrees]C in the furnace. The melted fly ash (low fusion-temperature, [m.sub.0] ~ 1.2) separated from gases onto the walls of the furnace formed a liquid slag layer and left the furnace in the liquid form.
The main results of the tests obtained from cleaned gases combustion:
* Combustion of cleaned gases in the wet-bottom vertical cyclone furnace guaranteed complete combustion of gases and high separation of ash from combustion products--95-98%.
* High flame temperature in the furnace caused dissociation of sulphur-ash compounds and along with this the increase in sulphur emission.
* Combustion tests of oil shale gases from the fluidized-bed gasifier confirmed the requirement to burn these gases at lower temperatures. In order to reduce combustion intensity of the hot gas it is necessary to feed secondary air into the furnace in parts and from different heights of the furnace or to use the diffusion-flame gas burners.
Project of 35 [MW.sub.th] oil shale fluidized-bed gasifier
In the Institute of Termophysics and Elektrophysics the fluidized-bed gasifier with heat capacity of 35 [MW.sub.th] for industrial tests of two-stage oil shale combustion method was worked out in 1981 . The technical solution of the gasifier project was based on the ideas presented in the Author's Certificate USSR 709938 . The fluidized-bed gasifier was designed to be used for reconstruction of the boiler No. 3 at the Kohtla-Jarve Power Plant.
The oil shale handling system was developed by the researchers of the Chair of Thermal Technology of the Tallinn Polytechnical Institute (now the Institute of Thermal Technology of Tallinn University of Technology) .
The technical project of the fluidized-bed gasifier and the reconstruction of the boiler No. 3 were done in the Leningrad Department of Orgenergostroi . Eesti Energia (Estonian Energy) financed the project. The fluidized-bed gasifier was planned to be installed ahead of the boiler No. 3 instead of the one-hammer mill in the ash basement. Cleaned gases were planned to be burned in the furnace of the boiler No. 3. For gas combustion the ENIN-type diffusion-flame burners of gas were adjusted to guarantee low flame temperature in the furnace. For unknown reasons the implementation of the project was not completed.
Presented by A. Siirde
Received May 5, 2011
[1.] Truu, H. K. Theory and Praxis of Oil Shale Combustion. Doctoral thesis of technical sciences.--Academy of Sciences of the USSR, G. M. Krzhizhanovsky Institute of Energy, Moscow, 1951. P. 187 [in Russian].
[2.] The Combustion of Fine Oil Shale in Industrial Fluidized Bed Boiler at Pussi Power Plant.--Scientific Technical Report of the Energy Research Institute of the Estonian Academy of Sciences (compilers Jurismaa, E. and Kartau, T.), Tallinn, 1962. P. 64 [in Estonian].
[3.] Martins, A. First industrial combustion of oil shale with gasification in fluidized bed // Gazette of Estonian Energy. 1997. Vol. 16, No. 1/2. P. 14-17 [in Estonian].
[4.] Uuesoo, R., Martins, A., Loone, R., Saar, J. The use of fluidized bed technology for oil shale combustion.--Proceedings of the 3rd All-Union Symposium of Solid Fuels Combustion. Novosibirsk: "Nauka", 1969. P. 204-207 [in Russian].
[5.] Martins, A., Uuesoo, R. The fusible characteristics of oil shale fly ash from fluidized bed gasifier.--Proceedings of the 1st All-Union Scientific-Technical Conference about Influence of Fuels Mineral Part on the Operation of Power Plant Boilers.--Alma-Ata, 1971. P. 150-157 [in Russian].
[6.] Martins, A., Kartau, J., Mere, H. The gasification of oil shale in fluidized bed to get gas for the energetic boilers.--Proceedings of the 4th All-Union Symposium of the Academy of Sciences of the USSR "The Combustion of Gases and Natural Fuels". Alma-Ata, Chernogolovka, 1980. P. 70-73 [in Russian].
[7.] Martins, A., Kartau, J., Nurk, A., Uuesoo, R. Gasificator for oil shale in fluidized bed. The Author's Certificate USSR 709938. 21.08.1978 [in Russian].
[8.] Martins, A., Kallaste, E., Nurk, A., Mere, H. Elaboration of the Industrial Fluidized Bed Gasifier (Project Task).--The Report of Contract No. 2-81. The Institute of Termophysics and Elektrophysics of the Academy of Sciences of the ESSR. Tallinn, 1981. P. 94 [in Russian].
[9.] Martins, A., Nurk, A., Kallaste, E., Mere, H. Verbrennung von festen Brennstoffen in der zweistufigen Wirbelschicht // Energietechnik. 1983. No. 7. S. 247-249.
[10.] Martins, A. Potentials for the fluidized bed technology by burning local fuels--Proceedings of Estonian-Finnish Energy Seminar. Hakapaino OY, Helsinki, 1994. P. 33-41.
[11.] Syromjatnikov, N. The rational combustion of small-sized fuels.--Proceedings of the Conference of the Universities. Sverdlovsk: Publishing House of the Ural Polytechnic Institute, 1959. P. 62-65 [in Russian].
[12.] Valk, M.(Ed.). Atmospheric Fluidized Bed Coal Combustion. Research, Development and Application.--ELSEVIR, Amsterdam-Lausanne-New York-Oxford-Shannon-Tokyo, 1995. P. 462.
[13.] Kallaste, E., Uuesoo, R. The retention of sulphur compounds by calcium oxide in the fluidized bed.--Proceedings of All-Union Scientific-Technical Seminar of Fuels Combustion with Minimal Amount of Harmful Emissions. The Institute of Termophysics and Elektrophysics of Academy of Sciences of ESSR, Tallinn, 1974. P. 19-22 [in Russian].
[14.] Kallaste, E. The Sulphur Distribution during Oil Shale Gasification in Fluidized Bed. The Thesis of Candidate Technical Sciences (Ph.D).--Tallinn Polytechnic Institute, Tallinn, 1978. P. 157 [in Russian].
[15.] Opik, I. Ots, A. The Use of Oil Shale for Energy Production I.--Tallinn: Publishing House "Valgus", 1967. P. 99 [in Russian].
[16.] Opik, I. The Impact of Oil Shale Mineral Part on the Operational Conditions of the Boiler Unit.--Tallinn: Estonian National Publishing House, 1961. P. 249 [in Russian].
[17.] Nurk, A. The Physical-Chemical Properties of Ash Samples from Fluidized Bed. Abstract of Thesis of Candidate Technical Sciences (Ph.D.).--Tallinn: Tallinn Polytechnical Institute, 1980. P. 19 [in Russian].
[18.] Martins, A., Nurk, A. The combustion of oil shale ash-laden gases in the cyclone-type wet-bottom furnace // Thermal Energetics. 1976. No. 8. P. 42-44 [in Russian].
[19.] Rajur, K., Oispuu, L. The Principles of the Fuel Preparation for Combustion in the Fluidized Bed // Abstract of the All-Union Scientific-Technical conference "The Progressive Processes in the Heating Power Engineering." The Ural Polytechnical Institute.--Sverdlovsk, 1984. P. 25-26 [in Russian].
[20.] The Industrial-Scale Testing of Fluidized Bed Gasifier for Boiler No. 3 of the Kohtla-Jarve Power Plant (designer Leningrad Department of Orgenergostroi). The Contract No. 16/13-83, January 17, 1983 [in Russian].
A. MARTINS, Corresponding author : e-mail email@example.com
Department of Faculty of Science, Research Laboratory on Multiphase Media Physics, Tallinn University of Technology
5 Ehitajate Rd, 19086 Tallinn, Estonia
Table 1. The process parameters of laboratory experiments Parameter Unit Result Oil shale calorific value as MJ/kg 8.22-16.6 received, [Q.sup.[gamma].sub.i] Oil shale max particle size, [d.sub.p] mm 3.5 Fuel load, B kg/h 22.5-14.4 Excess-air rate in oil shale - 0.39-1.09 gasification chamber, [[alpha].sub.g] Overall excess air rate, [alpha] - 1.06-1.46 Thickness of fluidized bed, L mm 400-450 Bed temperature, tb [degrees]C 568-1035 Temperature in the burning [degrees]C 872-1166 chamber of gasification products and fine coke particles, [t.sub.f] Apparent heat load of grate, [q.sub.g] MW/[m.sup.2] 2.28-4.61 Calorific value of gasification MJ/[nm.sub.3] 2.8-5.7 products, [Q.sub.g] Medium velocity of gases in oil shale m/s 0.77-2.80 gasification chamber, [w.sub.g] Bottom ash, [A.sub.b] % 28-60 Table 2. The process parameters of the experiments of the industrial fluidized-bed furnace Parameter Unit Result Oil shale - moisture, [W.sup.r] % 12.7-16.7 - ash, [A.sup.d] % 43.8-49.5 - carbonates, % 13.1-15.7 [(C[O.sub.2]).sup.d.sub.M] - calorific value, [Q.sup.r.sub.i] MJ/kg 9.6-10.6 - max particle size, [d.sub.p] mm 5-Mar Fuel load, B t/h 2.75-4.72 Excess-air rate in oil - 0.35-0.45 shale gasification zone, [[alpha].sub.1] (primary air) Excess-air rate in gas and fine - 1.2-1.7 fly coke burning chamber, [[alpha].sub.2] (secondary air) Thickness of fluidized bed, L mm 300-400 Bed temperature, [t.sub.b] [degrees]C 840-875 Temperature in the burning [degrees]C 1350-1050 chamber of gasification products and fly coke, [t.sub.g] Apparent heat load of grate, [q.sub.g] MW/[m.sup.2] 4.7-6.8 Calorific value of gasification MJ/[nm.sup.3] 4.2-6.7 products, [Q.sub.g] Medium velocity of gases in m/s 1.35-1.53 oil shale gasification chamber, [w.sub.g] Actual thermal output of the boiler, D MW 6.0-9.4 Ash balance - ash from fluidized bed gasifier, % 23-25 [A.sub.g] - ash from burning chamber of gas % 62-63 and fine fly coke, [A.sub.bc] - ash from furnace and from % 4.5 convection part, [A.sub.cp] - ash from cyclone, [A.sub.c] % 1.0-.5 - ash loss (into the atmosphere) , % 6.0-9.5 [A.sub.a]
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