DEVELOPMENT OF COMBUSTION MODEL IN THE INDUSTRIAL CYCLONE-CALCINER FURNACE USING CFD-MODELING

Transcription

1 CHEMISTRY & CHEMICAL TECHNOLOGY Chem. Chem. Technol., 2017, Vol. 11, No. 1, pp Chemcal Technology DEVELOPMENT OF COMBUSTION MODEL IN THE INDUSTRIAL CYCLONE-CALCINER FURNACE USING CFD-MODELING DOI: dx.do.org/ /chcht Roman Havrylv 1,*, Vоlоdymyr Maystru 1 Abstract. 1 A three-dmensonal computer model has been developed for the smulaton of combuston process, temperature felds and concentraton speces n the wor secton of ndustral cyclone-calcner furnace. The RANSapproach wth dfferent turbulence models for modelng was used. Smulaton results obtaned wth the model are compared wth ndustral furnace data. The results obtaned wth the computer model have mportant effects on the predcted temperature dstrbuton n the furnace as well as on other sgnfcant desgn parameters for future theoretcal and ndustral research. Keywords: CFD-modelng, combuston model, turbulence models, cyclone-calcner furnace. 1. Introducton Turbulent combuston s the bass of many dfferent ndustral processes. These processes are used n a wde range of materal processng ndustres, of whch lme producton s the most mportant. Currently, lme s produced by lmestone calcnng n furnaces of varous desgns: shaft furnaces, rotary lns, fludzed bed furnaces, and cyclone furnaces. Temperature s a crucal mode for operaton of these furnaces and all the techncal and economc performance of ther wor. The performance of the furnace systems deployed for fuel combuston s strongly dependent on the appled set-up, such as: furnace geometry, confguraton of burner, composton of fuel and gas-ar flows too. For a long tme, the ndustral furnaces desgn was performed on the bass of emprcal equatons and physcal experments. Ths approach s very expensve and naccurate, needed a lot of tme for expermental studes. In addton, technologcal calcnng process s a complcated dynamc object characterzed by a large number of functonally related varables. 1 Lvv Polytechnc Natonal Unversty 12, S. Bandera St., Lvv, Urane * havrlvroman@gmal.com Havrylv R., Maystru V., 2017 Under such crcumstances, the analyss of ts dynamc propertes often becomes possble only by usng numercal modelng methods. Among the modern methods of numercal modelng, the CFD-methods are prevalent. Computatonal flud dynamcs (CFD) smulatons provde a much better nsght nto ndustral combuston systems than any other technologes of modelng or measurements. It s possble to get nformaton on temperature dstrbuton, speces concentratons, velocty dstrbuton, heat transfer and the mxture of fuel and oxdzng flud. Thus t s possble to see and solve potental problems even before combuston systems are constructed or n operaton. However, t s necessary that the proposed model adequately descrbes the combuston process n the furnace. In ths artcle the nvestgaton results of cyclone furnace calcner are presented. The present wor s a step towards modelng the cyclone furnace used by "Pustomyty lme plant" (Pustomyty, Urane). The man focus s on the development of combuston model whch adequately descrbes the temperature feld n the worng area of the apparatus and can be used n future studes to optmze the exstng nstallaton and analyss. 2. Expermental 2.1. Materals and Methods of CFD-Modelng The gas-sold flow n cyclone furnace used by "Pustomyty lme plant" n Urane has been analyzed n a prevous wor [1]. The results obtaned from CFD smulatons were used to optmze furnace wor. Expermental valdatons at the plant later confrmed that the results from smulatons were ndeed very effectve and helped to mprove the aerodynamcs of the apparatus. However, there are many mportant questons whch reman to be answered.

2 72 Roman Havrylv et al. The man queston concerns the mpact of the new regme apparatus whch s proposed n [1] on the temperature feld and partcles calcnatons process. To answer ths queston, the combuston computer model that wll mae t possble to evaluate temperature feld n the apparatus must be developed. Currently hydrodynamcs modelng of the vortex gas flows n the apparatus of dfferent desgns based on CFD-modelng are wdely studed [2, 3]. ANSYS Fluent verson 15 was used n ths study to perform the smulaton of the combuston process n the ndustral cyclone-calcner furnace. Frstly, based on the drawngs of the ndustral furnace, geometrc model of the nternal flows of the apparatus was bult. Then by means of the mesh generator a computatonal mesh was created for ths model. The resultng mesh contans Nodes and Elements. All geometrc transformatons were done n a software module Desgn Modeller, and the mesh was created n ANSYS Meshng. Modelled cyclone-calcner furnace s shown n Fg. 1a, b. The calcnatons processes tae place n the wor zone 1 of the furnace, consstng of a 0.8 m dameter cylnder wth 4.4 m heght and the combuston processes tae place n a concal secton 2. Ar s ntroduced nto the calcner n two places. The prmary ar flow enters the burner 3 through the ppe 4 and addtonal flows enter the concal part of the calcner-furnace va two ppes 5 tangentally. The addtonal flows are nlet n the concal part of the calcner through the blades 9 where ar creates a swrlng of the flow. Ths mode of the furnace was descrbed n [1] and called an addtonal mode of the apparatus. The fuel (methane) enters the burner through the nlet tube 6, whch has a crcular shape. Natural gas and ar run nto a burnng chamber and are mxed up. In the burner, the burnt fuel and gases are derved through a concal secton 2 and cylndrcal secton 1. In ths type of furnace, the GGB-MGP-200 burner s used. The CaCO 3 partcles are ntroduced to the concal secton of the wor zone through the tube 7 n central part of the calcner-furnace. The products such as calcned CaO solds, CO 2, and other gases go out through the outlet tube 8 wth a dameter of m. The total furnace volume s 3.4 m 3. In ths study the mode wthout burnng of lmestone partcles has been tested. Ar enters nto the burner through the ppe 4 only and the fuel (methane) enters nto the burner through the nlet tube 6. Ths mode s used to preheat the furnace. All the geometrc data and the ntal and boundary condtons were suppled by "Pustomyty lme plant" (Urane). a) b) Fg. 1. Cyclone-calcner furnace geometry: general vew of furnace (a) and burner locaton (b)

3 Development of Combuston Model n the Industral Cyclone-Calcner Furnace Usng CFD-Modelng Model Descrpton and Boundary Condtons To smulate the dffuson methane-ar combuston n a turbulent flow, two approaches n Ansys Fluent 15 were used. Frst, the most popular approach s eddydsspaton model based on the wor of Magnussen and Hjertager [4]. It s a turbulent-chemstry reacton model where the reacton rate wll be determned assumng that turbulent mxng s the rate-lmtng process wth the turbulence-chemstry nteracton modelled. The combuston wll be modelled usng a global one-step reacton mechansm assumng complete converson of the fuel (methane) to CO 2 and H 2 O. Ths reacton wll be defned n terms of stochometrc coeffcents, formaton enthalpes, and parameters that control the reacton rate. Ths mechansm gves the average value of enthalpy and s applcable to estmate the dstrbuton of the man products of combuston (CO 2, H 2 O) and temperature felds. Its advantage s smplcty and maxmum smulaton rate. The second approach uses the Non-Premxed combuston model [5]. Ths model was used because the fuel as well as the oxdzer enters the burner of calcner furnace n dfferent dstnct streams. Ths software model smplfes the thermochemstry assocated wth ths type of combuston through the use of the mxture fracton. Ths fracton s the mass fracton of the burnt and unburnt fuel elements n all of the speces present. Ths s an mportant technque because atomc elements are conserved durng the reacton process, and the governng transport equaton does not have a source term. Through the smplfcaton of usng the mxture fracton, closng non-lnear mean reacton rates are no longer necessary snce ths s smply a mxng problem. The chemstry was modelled n the Chemcal Equlbrum Model. Ths model allows ncludng the effects of ntermedate speces as well as dssocaton reactons, whch creates a realstc approxmaton of the flame temperature. Flud flow wll be modelled usng the contnuty (1), Naver-Stoes (2) and (3) energy equatons shown below [6, 7]: ρ r + dv( ρu) = 0 (1) t r du r T ρ = ρf + dvτ (2) dt dt r ρ cp = E dvq+ q (3) T dt For an ncompressble flud flow ρ = 0 and tang nto account the nternal frcton Newton s law (1) and (2) equatons are: r dv( u ) = 0 (4) r du r 1 2r ρ = F gradp+ ν u (5) dt ρ where ρ densty; u velocty; τ stress tensor; p statc pressure; F external body force; c P heat capacty at constant pressure; T local temperature of flow; E energy dsspaton; q specfc local heat flux; q T an addtonal source of heat (for example by chemcal reacton); ν nematc vscosty of fluds. There are the basc equatons of hydrodynamcs whch represent the basc model of the medum flow [8]. Eq. (5) s the Naver-Stoes equaton and for the Newtonan flud n Cartesan coordnate system t can be wrtten as: dux 1 p ux ux ux = Fx + ν ( + + ) dt ρ x x y z duy 1 p uy uy uy = Fy + ν ( + + ) dt ρ y x y z duz 1 p uz uz uz = Fz + ν ( + + ) dt ρ z x y z (6) where ν nematc vscosty. To approxmate the contnuty and Naver-Stoes equatons for turbulent flow, the most popular method Reynolds-Averaged approach was used (RANS) [8-11]: ρ + ( ρu) = 0 (7) t x p ( ρu) + ( ρuu j) = + t x x j u u j 2 u l + µ ( + δj ) + ( ρuu j) xj xj x 3 xl xj (8) where μ dynamc vscosty; u and u are the mean and fluctuatng velocty components and δ j -delta functon or the Kronecer delta. Eqs. (7) and (8) are called Reynolds-averaged Naver-Stoes (RANS) equatons. Addtonal terms ρ uu j represent the effects of turbulence and are called the Reynolds stresses (also called turbulent stresses) and requre addtonal modelng. There are several approaches avalable n lterature [12] for soluton of the Reynolds stresses. Commonly used Boussnesq hypothess [13] to relate the Reynolds stresses n whch the Reynolds stress term s replaced by the product of the turbulent vscosty (whch s a property of the flud flow) and the mean velocty gradents: u u j 2 u ρ uu j = µ t( + ) ( ρ + µ t ) δj x x 3 x (9) j

4 74 Roman Havrylv et al. Ths approach s assocated wth the computaton of the turbulent vscosty μ t and the turbulence netc energy. Turbulence modelng s probably the most unresolved problem n classcal physcs. It s an unfortunate fact that no sngle turbulence model s unversally accepted for all classes of problems. The choce of turbulence model wll depend on consderatons such as the physcs of the flow, the establshed practce for a specfc class of problem, the level of accuracy requred, the avalable computatonal resources, and the amount of tme avalable for the smulaton. The Boussnes hypothess s used n the Spalart- Allmaras model, the - models, and the -ω models. These models of turbulence are mplemented n the Ansys Fluent 15. Dfferences between these models are the method of determnng μ t [14]. Analyss of furnace desgn, 3-D model, mesh qualty, flud flows and operatng modes show that the - turbulence models group can be used n ths study. Ths type of model s used to solve many engneerng problems n CFD-modelng. Ansys Fluent 15 provdes three types of - models: Standard, RNG, and Realzable - models [15]. The standard - model presented n ANSYS Fluent was proposed by Launder and Spaldng [16]. The - model s based on the eddy-vscosty (turbulent vscosty) concept and defnes μ t as: 2 ut = C µ ρ (10) The turbulence netc energy and ts rate of dsspaton are obtaned from the followng transport equatons: ( ρ) + ( ρu ) = t x µ t = ( µ + ) + G + Gb ρ YM + S xj σ xj (11) µ t ( ρ) + ( ρ u) = ( µ + ) + t x xj σ xj 2 + G + ( G + C G ) C ρ + S 1 3 b 2 (12) where G the generaton of turbulence netc energy due to the mean velocty gradents; G b the generaton of turbulence netc energy due to buoyancy; Y M the contrbuton of the fluctuatng dlataton n compressble turbulence to the overall dsspaton rate; C 1, C 2, C 3 constants; σ and σ the turbulent Prandtl numbers for and, respectvely; S, S user-defned source terms. The model constants are: C 1 = 1.44; C 2 = 1.92; C µ = 0.09; σ = 1.0; σ = 1.3 The standard - model s one of the most wdely used turbulence models due to ts smplcty and applcablty n a modelng range of turbulent flows. A dsadvantage of ths model s that t does not gve satsfactory results for flows nvolvng swrl, rotaton, streamlne curvature, and splttng of the streamlnes. It s manly due to the eddy vscosty concept used by ths model, whch assumes the Reynolds stresses to be sotropc. Nevertheless, for CFD modelng ths - model has been selected. Ths approach has an advantage t s less computatonally expensve compared to other - turbulent models and for comparng, the smulaton results wll be used. The RNG model has a smlar form to the standard model [14]. The use of addtonal restrctons and condtons suggests swrl and low-flow, sutable for complex flows wth a transverse velocty gradent, ncludng rapd deformaton, reasonable and nonstatonary flow vortces. These features mae the RNG model more accurate and relable for a wder class of flows than the standard model. ( ρ) + ( ρu ) = αµ eff + t x xj xj + G + Gb ρ YM + S (13) ( ρ) + ( ρu ) = αµ eff + t x xj xj 2 + G1 ( G + C3 Gb) C2 ρ + S (14) The new components compared to Eqs. (13) and (14) are: μ eff effectve vscosty, a, a the nverse effectve Prandtl numbers for and, respectvely. The model constants are: C 1 = 1.42 and C 2 = The RNG - model wors well for hgh Reynolds number flows as well as flows n the transton regon and gves mproved predcton for flows nvolvng swrl n comparson to the standard - model. The "Realzable" - model contans a new formulaton for the turbulent vscosty and a new transport equaton for the dsspaton rate, that s derved from an exact equaton for the transport of the mean-square vortcty fluctuaton [14]. It elmnates the possblty of unrealstc values of normal stresses from occurrng n hghly straned flows. For the estmaton of turbulent vscosty C μ t s treated as varable. The varable form of C μ s a functon of the local stran rate and rotaton of the

5 Development of Combuston Model n the Industral Cyclone-Calcner Furnace Usng CFD-Modelng 75 flud. An mmedate beneft of the "Realzable" - model s that t provdes mproved predctons for flows nvolvng rotaton, separaton, and recrculaton. µ t ( ρ) + ( ρ u) = ( µ + ) + t x xj σ xj + G + G ρ Y + S (15) b M µ t ( ρ) + ( ρ uj) = ( µ + ) + t xj xj σ xj 2 + ρcs ρc + C C G + S + ν b (16) In these equatons, C 2 and C 1 are constants (C 2 = 1.9; C 1 = 1.44); σ and σ the turbulent Prandtl numbers for and, respectvely (σ = 1; σ = 1.2). S and S are user-defned source terms the same as n prevous models. But C µ s not constant and s a functon of the mean stran and rotaton rates, the angular velocty of the system rotaton, and the turbulence felds ( and ). For CFD-modelng gas flows and combuston processes n the cyclone furnace, three types of turbulence models were used wth combuston models. Soluton of the dfferental equatons by fnte volumes method was performed. The system of dfferental equatons was supplemented by relevant boundary condtons. The boundary condton s the settng for the nlet, wall and outlet. Operaton modes of the furnace are: nlet ar 20 m/s; nlet gas 7 m/s. To set up the calculaton module, the followng assumptons were used: 1. The worng volume of the furnace s a mxture of gases (oxygen, ntrogen, fuel, waste products). 2. The heat exchange between the envronment and the wall s mssng (the walls are adabatc ). 3. The thermal radaton from the wall n the volume of gas s smulated by the model of dscrete ordnate at a constant temperature of 1000 K. For the Non-Premxed combuston model sngle mxture fracton probablty functon (PDF) was used (Fg. 2). The fuel composton n mole fractons of the speces CH 4, C 2 H 6, C 3 H 8, C 4 H 10, and CO 2 s presented n Table 1. For all nlet flows temperature was set as 300 K. The oxdzer (ar) conssts of (vol %): O 2 21 and N SIMPLE-based approach was used for pressurevelocty couplng scheme. The soluton was smulated untl convergence was acheved. Approxmately 1500 teratons were performed for the case based on the Eddy- Dsspaton combuston model and 4500 teratons for the case based on the Non-Premxed combuston model. The fuel composton Speces Mole fracton CH C 2 H C 3 H C 4 H CO N Fg. 2. PDF table for mean temperature, mean mxture fracton and scaled varance 3. Results and Dscusson Table 1 The smulaton results from the applcaton of the mathematcal models descrbed n the secton 2.2 are presented n ths secton. The results are manly gven n terms of trajectory flows, velocty contours, temperature, and speces concentraton profles. The gas flow dstrbuton and velocty wthn the cyclone furnace are shown n Fgs. 3 and 4 for the both cases based on the "Realzable" - turbulence models. Case (a) s for Eddy-Dsspaton combuston model and case (b) s for the Non-Premxed combuston model. For other types of turbulence models, character of change trajectory flows and velocty dstrbuton are smlar. A large recrculaton zone s predcted by all the turbulence models n the concal part of the furnace. The recrculaton zone starts from the burner zone and expands to concal secton 2 of the furnace and to the central tube. Ths recrculaton zone s formed due to the nlet fuel gas n the furnace through the burner blades where ar creates a swrlng of the flow. In cylndrcal worng zone recrculaton s low and gases flow to the ext around the central ppe.

6 76 Roman Havrylv et al. a) b) a) b) Fg. 3. The trajectory flow dstrbuton n the furnace: Eddy- Dsspaton combuston model (a) and Non-Premxed combuston model (b) Fg. 4. The velocty contours n a vertcal cross secton of the furnace: Eddy-Dsspaton combuston model (a) and Non- Premxed combuston model (b) As t can be seen n Fg. 4, the velocty contours are dssmlar. Near the walls there are areas of hgh velocty. Calculated maxmum flow velocty near the walls n some areas of the furnace s about m/s. At the ext of the furnace as averagng the square of the velocty s of about 37 m/s for case (a) and of about 19 m/s for case (b). Ths s because the gas flow moves sprally. Ths fact needs attenton and s assocated wth the burner geometry. Probably the burner desgn must be optmzed. The gas temperature dstrbuton n a vertcal cross secton through the furnace s shown n Fgs. 5 and 6 for the both combuston models, respectvely. The hgh-speed hot combuston gases from the burner zone n concal furnace secton flow up to the cylndrcal worng zone. Ths causes hgher temperatures n the upper part of concal furnace secton that are greater than those predcted for the proposed confguraton and operaton mode. The uneven mxng also leads to a hghertemperature bas towards the rght sde as the gas leaves the concal secton. A more extended hgher-temperature zone s predcted wth the Eddy-Dsspaton combuston model. For all the cases of turbulent models wth the Eddy- Dsspaton combuston model the lower temperatures n a small regon close to the burners and hgher temperatures further away from the burner are observed. In order to quantfy those dfferences, vertcal temperature profles n the same vertcal cross secton are shown n Fg. 6 for the Non-Premxed combuston model. evoluton wth the Eddy-Dsspaton combuston model and the temperature dfference between the two models s decreased wth heght. The maxmum temperature predcted wth the Eddy-Dsspaton combuston model s about 2400 K whereas the maxmum temperature predcted wth the Non-Premxed combuston model s about 2100 K. The temperature dfferences of up to 900 K are predcted n the regon between the concal and cylndrcal furnace sectons. In the center of the furnace, where the outlet partcles of the central tube are located, a clear local mnmum n the flue gas temperature s observed. It s good for the lme calcnatons process when partcles fall nto the low temperature zone and are heated. It s very mportant to notce the temperature profle n worng zone wth the furnace heght. The flue gas temperature dstrbuton n the wor zone s very mportant because t s an mportant factor determnng the lme calcnatons processes. Due to the hgh resdence tme of the flue gas n the worng zone and the flow pattern n the furnace shown n Fgs. 3 and 4, the temperature contour n a vertcal cross secton through the cylndrcal furnace secton predcted wth the two combuston models remans approxmately constant for each model, respectvely (see Fgs. 5 and 6). On the contrary, the temperature contour n the concal furnace secton outsde of the worng zone predcted wth the two combuston models s very dfferent. Ths s because the effect of the recrculaton has a strong nfluence on the temperature values n the concal furnace secton, where the burner outlet s located. From Fgs. 5 and 6 t can be observed that the temperatures n the concal secton are very hgh, snce turbulent combuston s domnated at ths regon and the reactons occur where mxng s hgh.

7 Development of Combuston Model n the Industral Cyclone-Calcner Furnace Usng CFD-Modelng 77 a) b) c) Fg. 5. Temperature profle n a vertcal cross secton through the furnace based on Eddy-Dsspaton combuston model: for - turbulence model (a); for - RNG turbulence model (b) and for "Realzable" - turbulence model (c) a) b) c) Fg. 6. Temperature profle n a vertcal cross secton through the furnace based on Non-Premxed combuston model: for - turbulence model (a); for - RNG turbulence model (b) and for "Realzable" - turbulence model (c) It s shown that the temperature evoluton wth the Non-Premxed combuston model lags the temperature Theoretcal excess rato by volume accordng to a mathematcal model s 1:11.5. Based on the actual data for ths type of burner ar excess rato by volume s n the range of 1:11.5 to 1:12.6. Under worng condtons, the flame length and unformty of heatng are regulated by changng the excess rato. The temperature dfferences predcted wth the two combuston models suggest dfferent fuel combuston rates. The concentraton profles of the fuel component (СН 4 ) n the same cross secton where the temperature profles have been presented are shown n Fgs. 7 and 8. The results are presented n the same manner as prevous results: Fg. 7 s for Eddy-Dsspaton combuston model and Fg. 8 s for the Non-Premxed combuston model.

8 78 Roman Havrylv et al. It s readly notced that combuston progress for methane s slower n the case of the Eddy-Dsspaton combuston model, leadng to larger flames when ths model s used. Smlar results are obtaned for the concentraton profles of the major combuston products, namely CO 2 and H 2 O. The concentraton of CO 2 and ts dstrbuton n the furnace wll be consdered durng the calcnaton reacton smulaton n the future study. The dstrbutons of CO concentratons deserve specal attenton. They are calculated based on Non- Premxed combuston model and are shown n Fg. 9. The process of carbon monoxde combuston s almost complete at the end of concal furnace secton ndcatng that the correct ar excess rato and the correct heght of ths secton were desgned. The expermental measurement of temperature n the furnace was carred out by fve sensors located at the apparatus shown n Fg. 10a. The temperature measurement at the furnace concal secton above the burner was not possble and therefore the comparson of the temperature dstrbuton n the furnace wth the practcal data receved on the bass of these 5 measurement ponts are shown n Fg. 10b. The dstrbuton of temperatures averaged over the cross secton shown n Fg. 10b and calculated on a model Non-Premxed (case 2), showed satsfactory agreement wth the practcal data that confrms the fundamental pcture of the temperature dstrbuton n heght, depth and wdth of the furnace. These graphs show that the calculaton results based on the Non-Premxed combuston model are the closest to the expermental data wth "Realzable" - turbulence model. The maxmum relatve error s about 14 % for pont 1. For other ponts, the maxmum relatve error vares n the range from 6 to10 %. a) b) c) Fg.7. Contours of СН 4 mass fractons n a vertcal cross secton through the furnace based on Eddy-Dsspaton combuston model: for - turbulence model (a); for - RNG turbulence model (b)and for "Realzable" - turbulence model (c) a) b) c) Fg. 8. Contours of СН 4 mass fractons n a vertcal cross secton through the furnace based on Non-Premxed combuston model: for - turbulence model (a); for - RNG turbulence model (b) and for "Realzable" - turbulence model (c)

9 Development of Combuston Model n the Industral Cyclone-Calcner Furnace Usng CFD-Modelng 79 a) b) c) Fg. 9. Contours of СO mass fractons n a vertcal cross secton through the furnace based on Non-Premxed combuston model: for - turbulence model (a); for - RNG turbulence model (b) and for "Realzable" - turbulence model (c) Temperature, K Measurement ponts 1) к-е model 1) RNG model 1) Realzable model Expermental data 2) к-е model 2) RNG model 2) Realzable model a) b) Fg. 10. Expermental measurement of temperature: ponts of the temperature measure n the furnace (a) and expermental data of the temperature measurement (b) 4. Conclusons In ths study, a comprehensve comparson of turbulence models and combuston models for cyclonecalcner furnace was conducted. 3-D feld of temperatures n the reacton zone and n the whole system volume, concentraton speces dstrbuton, and the length of the torch were obtaned. The smulaton results were analyzed and valdated wth the expermental data. The expermental data are n good agreement wth the feld tests results of the devce for the Non-Premxed combuston model wth "Real-

10 80 Roman Havrylv et al. zable" - turbulence model. In these ponts, the error n the calculaton of temperature s not more than 10% n all the calculaton optons. The developed computer model provdes very mportant results for better understandng of the complex processes occurrng wthn the furnace and can be a baselne for future modelng of pollutant emssons and lmestone calcnaton processes. The smulaton results of calcnaton reacton based on ths model wll be presented n the followng studes. References [1] Havrylv R., Maystru V. and Bla V.: EEJET, 2015, 75, 14. [2] Artyuhov A. and Slabnsry V.: Chem. Chem. Technol., 2015, 9, 175. [3] Slabnsry V., Laposhcheno O., Logvyn A. and Al-Rammah M.: Chem. Chem. Technol., 2014, 8, 479. [4] Magnussen B. and Hjertager B.: 16 th Symp. on Combuston. The Combuston Insttute, USA, Pttsburgh 1976, 719. [5] Peters N.: Turbulent Combuston. Cambrdge Monographs on Mechancs. Cambrdge Unversty Press, Cambrdge [6] Brhoff G.: Hydrodynamcs: A study n Logc, Fact, and Smltude, 2 nd edn. Prnceton Unversty Press, Prnceton [7] Batchelor G.: An Introducton to Flud Dynamcs. Cambrdge Unversty Press, Cambrdge [8] Salv R. (Ed.): Naver-Stoes Equatons. Theory and Numercal Methods. Marcel Deer, Inc., New Yor [9] Spalart P. and Allmaras S.: Conference Reno, USA, Nevada 1999, 92. [10] Wlcox D.: Turbulence Modelng for CFD, 1 st edn. DCW Industres, Inc., La Canada CA [11] Furbo E.: MA thess. Uppsala Unversty, [12] Pope S.: Turbulent Flows. Cambrdge Unversty Press, Cambrdge [13] Schmtt F.: Comptes Rendus Mecanque, Elsever Masson, 2007, 335, 617. [14] Orszag S., Yahot V., Flannery W. et al.: Int. Conf. on Near- Wall Turbulent Flows, USA, Tempe [15] Menter F.: AIAA J., 1994, 32, [16] Launder B. and Spaldng D.: Lectures n Mathematcal Models of Turbulence. Academc Press, London Receved: Aprl 27, 2016 / Revsed: May 27, 2016 / Accepted: September 12, 2016 РОЗРОБЛЕННЯ МОДЕЛІ ГОРІННЯ В ПРОМИСЛОВІЙ ЦИКЛОННІЙ ПЕЧІ-ДЕКАРБОНІЗАТОРІ МЕТОДАМИ ЧИСЛОВОГО МОДЕЛЮВАННЯ Анотація. Розроблено тривимірну комп ютерну модель для дослідження процесу горіння в промисловій циклонній печі-декарбонізаторі. Моделювання руху потоків виконано на основі RANS-підходу з використанням різних моделей турбулентності. Представлені результати дають можливість спрогнозувати розподіл температури в печі, визначити концентрації компонентів в газовій фазі та добре узгоджуються з експериментальними даними. Дані отримані на основі комп ютерного моделювання будуть використані в наступних теоретичних та експериментальних дослідженнях для оптимізації конструкції апарату. Ключові слова: CFD-моделювання, модель горіння, моделі турбулентності, циклонна піч-декарбонізатор.