DEVELOPMENT OF SHIP SYSTEMS FOR AIR PURIFICATION FROM DROPLET MOISTURE

2 (8) 2017 sm.nuos.edu.ua sm@nuos.edu.ua УДК 629.12.03 Р93 DEVELOPMENT OF SHIP SYSTEMS FOR AIR PURIFICATION FROM DROPLET MOISTURE РАЗРАБОТКА СУДОВЫХ СИСТЕМ ОЧИСТКИ ВОЗДУХА ОТ КАПЕЛЬНОЙ ВЛАГИ DOI 10.15589/SMI20170220 Serhy S. Ryzhkov Рыжков Сергей Сергеевич Serhy S. Ryzhkov C. С. Рижков, канд. техн. наук, доц. sergy.ryzhkov@nuos.edu.ua ORC ID: 0000-0002-2201-6172 Admral Makarov Natonal Unversty of Shpbuldng, Nkolaev Национальный университет кораблестроения имени адмирала Макарова, г. Николаев Abstract. The study of gas dynamcs and deposton coeffcents of the separatng profle has been performed. The three-dmensonal model of workng channels of the shp systems for ar purfcaton from droplet mosture s developed. The dstrbuton of velocty, statc pressure, dynamc pressure, knetc energy of turbulence, and deposton coeffcents for the flow rates of 5, 10, 15, 20 m/s n separatng profles wth the rad of 5, 10, 15, 20, 25 mm. The droplet mosture deposton coeffcent s 99.9 %. Desgns of the shp systems for ar purfcaton from droplet mosture are developed for the ar flow rangng from 20 to 2000 m 3 /hour. Keywords: separator; ar purfcaton system; mosture separator; 3D modelng. Аннотация. Выполнены исследования газодинамики и коэффициентов осаждения сепарационного профиля. Разработаны трехмерные модели рабочих каналов судновых систем очистки воздуха от капельной влаги. Получено распределение скорости, статического давления, динамического давления, кинетической энергии турбулентности и коэффициентов осаждения для скоростей потока 5, 10, 15, 20 м/с в сепарирующих профилях с радиусами 5, 10, 15, 20, 25 мм. Разработаны конструктивные решения судовых систем очистки воздуха от капельной влаги для расхода воздуха от 20 до 2000 м 3 /ч. Ключевые слова: сепаратор; системы очистки воздуха; влагоотделитель; 3D-моделирование. Анотація. Виконано дослідження газодинаміки та коефіцієнтів осадження сепараційного профілю. Розроблено тривимірні моделі робочих каналів судових систем очищення повітря від краплинної вологи. Отримано розподіл швидкості, статичного тиску, динамічного тиску, кінетичної енергії турбулентності та коефіцієнтів осадження для швидкостей потоку 5, 10, 15, 20 м/с у сепаруючих профілях з радіусами 5, 10, 15, 20, 25 мм. Розроблено конструктивні рішення суднових систем очищення повітря від краплинної вологи для витрат повітря від 20 до 2000 м 3 /год. Ключові слова: сепаратор; системи очищення повітря; вологовіддільник; 3D -моделювання. References [1] Belousov V. V. Teoretcheskye osnovy protsessov gazoochstk [Theoretcal foundatons of gas purfcaton processes]. Moscow, Metallurgya Publ., 1988. 256 p. [2] Ryzhkov S. S., Basok B. I. Ekologcheskye resursosberegayushchye tekhnolog dlya promyshlennoy teplotekhnk na osnove dspersnykh dvukhfaznykh sred [Ecologcal resourcesavng technologes for ndustral heat engneerng based on dspersed two-phase meda]. Promyshlennaya teplotekhnka Industral heat engneerng, 2001, no. 4 5, pp. 141 145. [3] Van-Dayka M. Techenye zhdkost gaza [Lqud and gas flow]. Moscow, Mr Publ., 1986. 114 p. [4] Rayst P. Aerozol. Vvedenye v teoryu [Aerosols. Introducton to the theory]. Moscow, Mr Publ., 1987, pp. 34-40. [5] Mednkov Ye. P. Turbulentnyy perenos osazhdenye aerozoley [Turbulent transfer and deposton of aerosols]. Moscow, Nauka Publ., 1981. 176 p. [6] Kalvert S., Inglund G. M. Zashchta atmosfery ot promyshlennykh zagryazneny: Spravochnk Ch. 1 [Protecton of the atmosphere from ndustral polluton: Handbook. Part 1]. Moscow, Metallurgya Publ., 1988. 760 p. 115

sm.nuos.edu.ua sm@nuos.edu.ua 2 (8) 2017 [7] Ryzhkov S. S., Kharytonov Yu. M., Blahodatny V. V. Metody ochyshchenna povtranoho seredovyshcha vd zabrudnen [Methods for the ar medum purfcaton from contamnants]. Mykolav, UDMTU Publ., 2002. 56 p. Problem statement. Provdng comfort n shp accommodatons and servce premses, as well as mantanng necessary technologcal condtons n producton premses, requres ar purfcaton from droplet mosture. Mosture ngress nto the ar duct leads to the dampness of ar-condtoned rooms, ntense corroson of equpment, whch can lead to accumulaton of mosture n certan areas, etc. It s reasonable to ncrease the effcency and reduce the dmensons of shp systems ntended for ar purfcaton from droplet mosture through desgnng devces wth the most effectve deposton surfaces wth the help of separaton gradent aerosol technologes. The development of models and research methods that allow for the calculaton of gas dynamcs n the workng channels of the purfcaton systems and deposton coeffcents for the equpment s entre operatng range wll provde the bass for the development of shp systems for ar purfcaton from droplet mosture. Latest research and publcaton analyss. At present, vast use s made of nertal separators, the separatng elements of whch ether have demster pads or are empty and provde nternal dranage of droplet mosture [1]. Tests of the mst elmnators descrbed n [2] have showed ther nsuffcent separaton ablty and ncreased aerodynamc drag. In addton, the manufacture of such separatng elements requres a large amount of work that can not be mechanzed. A possble soluton s the development of hgh-effcency gradent separators of aerosol meda for shp power plants. Creaton of the technologes for separaton of aerosol meda wth the use of new phase capture technques offers a sgnfcant reserve for energy savng. It s promsng to develop nnovatve methods mplementng gradent ntensfcaton of the transfer processes n the boundary layers of multfunctonal surfaces of power plants. The multfunctonal surfaces nclude those characterzed wth a compactness coeffcent exceedng 2000 m 2 /m 3, enhanced heat exchange, and separatng propertes. The use of methods and technques for desgnng and mplementng flters based on gradent technologes wll ncrease the relablty and servce lfe of the shp s power equpment and ts elements. In turn, ths wll promote the creaton of hgh-effcency energy-savng technologes and effcent desgn solutons for a wde range of gradent separators of shp power plants [5]. THE ARTICLE AIM s to present the development of shp systems for ar purfcaton from droplet mosture. The am can be acheved by tacklng the followng obectves: to perform mathematcal modelng of the processes at the ntal veloctes of 5, 10, 15, 20 m/s on the bass of separaton gradent aerosol technologes at dfferent flow rates n the separatng profles wth the rad of 5, 10, 15, 20, 25 mm; to calculate the dstrbuton of velocty, statc pressure, dynamc pressure, knetc energy of turbulence, and deposton coeffcents on the bass of separaton gradent aerosol technologes for the flow rates of 5, 10, 15, 20 m/s n separatng profles wth the rad of 5, 10, 15, 20, 25 mm; to calculate the coeffcent of deposton of droplet mosture for the flow rates of 5, 10, 15, 20 m/s n separatng profles wth the rad of 5, 10, 15, 20, 25 mm; to develop desgn solutons of shp systems for ar purfcaton from droplet mosture for ar consumpton rangng from 20 to 2000 m3/h; to develop and approve drawngs for a lneup of shp systems for ar purfcaton from droplet mosture; to develop and approve the enterprse standard for the lneup of shp systems for ar purfcaton from droplet mosture. Basc materal. Mathematcal modelng. The Reynolds stress transport equatons ρ u u can be wrtten n the followng form: ( u u ) + C = DT, + DL + P + G ρ + t, + φ ε + F + S, (1) user ρ s the partal dervatve of tme; where ( u u ) + t Ñ ( u k u u ) k D [ ρu u u + p( δ u + δ u )] T, ρ s the convectve component; k k k k represents the turbulent dffuson; D µ ( u u ) L, s k k u u the lamnar dffuson; P ρ uuk + u uk k k stands for the formaton of tenson; ( g u θ + g u θ ) G ρβ s the formaton of buoyancy force; u u φ + p ndcates the stress exerted u u by pressure; ε 2 µ stands for dsspaton; ( u u ε + u u ε ) k F 2 ρ Ω k m km m km represents the formaton of the rotatonal system; S user s the element set by the user. The energy equaton obtaned on the bass of ths theory has the followng form: k 116

2 (8) 2017 sm.nuos.edu.ua sm@nuos.edu.ua t = [ ]= ( ρe) + u ( ρe + p) c pµ t T k + + u Prt ( τ ) eff, (2) where Е s the total energy; u u uk ( τ ) µ 2 = eff eff + µ eff δ s the devator x x 3 k stress tensor. The turbulent mass transfer equaton s modeled by substtutng the enthalpy of equaton (2) wth the concentraton of partcles of a dspersed multphase flow: = t [ ]= ( ρc) + u ( ρc) µ t D + ρ Prt D C + u ( τ ) eff. (3) The contnuty equaton for the flow wthout the partcle source at a constant densty of the lqud s as follows: u = 0. (4) The equaton of the dynamcs of the partcles movement n the gas flow s wrtten as follows: u p t = F + F + F + F + F 1 2 3 4 D, (5) where x t s the tme, force per unt mass of the partcle; '2 1 ρ uk F1 = ( u uk ) s the force of nerta, F2 = 0, 5mk 2 ρk t y P u s the force of turbophoress, F uk P 3 = s the dffusophoretc force, F w 1/ 2 2Kυ ρd ( ) ( υ υ ) 4 = P s the Saffman ρ d d d p p 18µ CD lft force, and FD = Re s the force of resstance. 2 ρpd P 24 In these expressons, P w s the value of pressure of the wall, p s the flow pressure, d P s the partcle dameter, ρ P s the partcle densty, υ P s the partcle velocty, ρ s the densty of multphase hgh-pressure fuel mxtures, υ s the gas velocty, d s the deformaton tensor, K s equal up u to 2.594, Re = ρdp s the Reynolds number, u s µ the ntal flow rate; u P s the partcle velocty; μ s the molecular vscosty of the flow; ρ s the flow densty; ρ P s the partcle densty; d P s the partcle dameter. The coeffcent of resstance s calculated as follows: lk kl b2 ( 1+ b Re ) 24 b3 Re CD = 1 +, (6) Re b + Re where b s the polynomal coeffcent to be set. The quanttes C, D L,, P and F are calculated drectly from the above expressons, whle D T,, G, φ, ε are modeled n the form that allows closng the system 4 of equatons. The methods used n ther modelng have been detaled n prevous publcatons. Upon the soluton of the equatons, the purfcaton ntensty s determned by the mass, hydrodynamc, and energy coeffcents for ntensfcaton of deposton (labeled as Km, Kh, and Ke, respectvely). The prncples of calculaton of these coeffcents suggest maxmzng the mass of deposted partcles whle mnmzng the geometrc volume of the processes and the mechancal work of the partcles transfer relatve to the nternal and external energy expendture. Based on these prncples, the ntegrated ndcator of the purfcaton ntensty IPI s calculated wth the use of the followng formula: where IPI = 1 (1 Km)(1 Kh)(1 Ke), (7) Km = (ΣMn ΣΜout)/ΣMn, (8) Kh = (ΣV ΣVu)/ΣV, (9) Ke = 1 (A + L)/(E nt + E ex ), (10) In these formulas, ΣMn and ΣΜout are the total mass of the partcles wth the sze of at the nlet and outlet of the zone, respectvely; ΣV and ΣVu s the total volume undergong purfcaton or left unprocessed, respectvely; A = ΣlF s the total work on the partcles transfer over the dstance l under the mpact of the forces F; L = G[Δ(pv) + Δ(w 2 /2) + gδh] + L t + L f s the work performed by the flow of the G consumpton; E nt = Δ(c v tgτ) s the nternal energy expendture of the flow, whle E ex s the external energy expendture. Research results. Development of shp systems ntended for ar purfcaton from droplet mosture nvolved a study of the separatng profle (Fg. 1) wth the followng parameters: R1 = (0.05 0.5)L; h = (0.5 5.0)R1; R2 = (0.01 1.0)L. The profle under study s 80 mm long, wth 2 dran grooves on the top and 2 dran grooves on the bottom; the grooves are 3 mm long and 2 mm deep. The curvature rad of the profle selected for analyss are 5, 10, 15, 20, and 25. The study of the separatng profles has been performed wth the help of three-dmensonal desgn grds (Fg. 2). On the bass of the mathematcal model of the processes, the ntal and boundary condtons were set for substtuton to the system of equatons. It allowed calculatng the basc parameters of the separatng profle. For the calculaton accuracy, the crteron of concdence 10 4 was appled to the varables of velocty, flow contnuty, knetc energy of turbulence, and Reynolds stresses. In the process of calculaton, the followng parameters were set: three-dmensonal real-sze geometry (length of 80 mm and heght of 5...25 mm); 117

sm.nuos.edu.ua sm@nuos.edu.ua 2 (8) 2017 Fg. 1. Structure dagram of the separatng profle wth varyng curvature rad and dmensons: R1 = (0.05 0.5)L; h = (0.5 5.0)R1; R2 = (0.01 1.0)L: 1 profle nlet; 2 R1 zone; 3 R2 zone; 4 R1 zone; 5 droplet capture (demstng) zone calculaton grd bult of trangular segments wth the area of S = 30 10 8 m 2 ; envronment parameters normal condtons; gas densty of ρ g = 1.225 kg/m 3 ; gas vscosty of µ g = 1.79 10 5 kg/(m s); the channel wall materal s alumnum wth the roughness of 0.1 mm and densty of ρ al = 2690 kg/m 3 ; mnmal partcle dameter of 3 μm; average partcle dameter of 100 μm; maxmum partcle dameter of 150 μm; concentraton of the lqud phase (H 2 O) 5, 10, 15, 20 %; velocty range 5, 10, 15, 20 m/s. Fg. 3 10 present the dstrbuton of velocty (flow rate), knetc energy of turbulence, statc and dynamc pressure for the channel wth the rad of 5, 10, 15, 20, 25 mm at U = 5 20 m/s. The calculaton results ndcate that the channel wth the length of 80 mm and radus of 15 mm has the most effcent hydrodynamc characterstcs. Aerosol deposton n the separatng profle has been calculated for the partcle dameter of 1...3 μm, lqud phase concentraton (H 2 O) of 5, 10, 15, 20 % and the velocty range of 5, 10, 15, 20 m/s. At that, the problems of non-statonary condtons wth the fnal step n tme were solved wth the Rasng Rambler method for the partcle traectory to reach the deposton surface (the pro- fle walls or the outlet cross secton) n the calculaton grd. The calculaton assumed that the concdence of the partcle traectores mpled ther combnaton (Table 1). The partcle was consdered to be captured f ts traectory concded wth the wall of the channel. At the rate of 5...10 m/s, the deposton coeffcent of the profle wth the radus of 5 mm makes up 36.1...30.2 %. When the flow rate s ncreased up to 20 m/s, the lqud phase breaks away and the deposton coeffcent decreases to 20.8 %. At the rates up to 5...10 m/s, the deposton coeffcent of the profle wth the radus of 10 mm makes up 91.9...90.4 %. When the flow rate s ncreased up to 20 m/s, the lqud phase breaks away and the deposton coeffcent decreases to 51.9 %. At the rates up to 5...10 m/s, the deposton coeffcent of the profle wth the radus of 15 mm makes up 99.9...99.1 %. When the flow rate s ncreased up to 20 m/s, the lqud phase breaks away and the deposton coeffcent decreases to 74.9%. At the rates up to 5...10 m/s, the deposton coeffcent of the profle wth the radus of 20 mm makes up 85.6...72.9 %. When the flow rate s ncreased up to 20 m/s, the lqud phase breaks away and the deposton coeffcent decreases to 50.5%. At the rates up to 5...10 m/s, the deposton coeffcent of the profle wth the radus of 25 mm makes up 42.5...31.3 %. When the flow rate s ncreased up to 20 m/s, the lqud phase breaks away and the deposton coeffcent decreases to 15.9 %. Table 1. Calculaton of the coeffcent of deposton n the separatng profle R (mm) 5 % 10 % 15 % 20 % 5 % 10 % 15 % 20 % 5 % 10 % 15 % 20 % 5 % 10 % 15 % 20 % 5 35.7 34.7 35.8 36.1 31.3 31.2 31.4 30.2 25.9 24.8 25.7 26.4 20.8 20.6 20.4 20.2 10 91.6 91.4 91.3 91.9 94.8 92.8 91.3 90.4 70.9 69.4 68.2 68.3 51.9 50.3 50.5 49.4 15 99.9 99.9 99.9 99.9 99.6 99.3 99.4 99.1 82.3 82.4 83.5 84.9 74.9 73.5 74.1 73.8 20 84.3 85.1 85.6 85.5 82.0 78.9 74.4 72.9 61.3 61.6 60.8 60.3 50.5 50.4 49.7 48.4 25 42.5 42.1 41.9 41.2 32.0 32.5 31.3 31.4 22.7 22.4 21.8 21.4 15.4 15.1 15.9 14.6 118

2 (8) 2017 sm.nuos.edu.ua sm@nuos.edu.ua 1) 2) 3) 4) 5) 6) Fg. 2. Calculaton grd of the three-dmensonal operatonal geometry of the separatng profle: 1) R1 = 60 mm, R2 = 5 mm, h = 15 mm, L = 80 mm; 2) R1 = 25 mm, R2 = 10 mm, h = 15 mm, L = 80 mm; 3) R1 = 12 mm, R2 = 15 mm, h = 15 mm, L = 80 mm; 4) R1 = 4 mm, R2 = 20 mm, h = 15 mm, L = 80 mm; 5) R1 = 1 mm, R2 = 25 mm, h = 15 mm, L = 80 mm; 6) a = 2 mm, b = 3 mm, c = 5 mm, d = 14 mm 119

sm.nuos.edu.ua sm@nuos.edu.ua 2 (8) 2017 Dstrbuton of velocty (m/s) Statc pressure (Pa) R = 25 mm R = 20 mm R = 15 mm R = 10 mm R = 5 mm Fg. 3. Calculaton of the dstrbuton of velocty and statc pressure for the channel rad of 5, 10, 15, 20, 25 mm at 120

2 (8) 2017 sm.nuos.edu.ua sm@nuos.edu.ua Knetc energy of turbulence (m 2 /s) Dynamc pressure R = 25 mm R = 20 mm R = 15 mm R = 10 mm R = 5 mm Fg. 4. Calculaton of the dstrbuton of knetc energy of turbulence and dynamc pressure for the channel rad of 5, 10, 15, 20, 25 mm at 121

sm.nuos.edu.ua sm@nuos.edu.ua 2 (8) 2017 Dstrbuton of velocty (m/s) Statc pressure (Pa) R = 25 mm R = 20 mm R = 15 mm R = 10 mm R = 5 mm Fg. 5. Calculaton of the dstrbuton of velocty and statc pressure for the channel rad of 5, 10, 15, 20, 25 mm at 122

2 (8) 2017 sm.nuos.edu.ua sm@nuos.edu.ua Knetc energy of turbulence (m 2 /s) Dynamc pressure R = 25 mm R = 20 mm R = 15 mm R = 10 mm R = 5 mm Fg. 6. Calculaton of the dstrbuton of knetc energy of turbulence and dynamc pressure for the channel rad of 5, 10, 15, 20, 25 mm at 123

sm.nuos.edu.ua sm@nuos.edu.ua 2 (8) 2017 Dstrbuton of velocty (m/s) Statc pressure (Pa) R = 25 mm R = 20 mm R = 15 mm R = 10 mm R = 5 mm Fg. 7. Calculaton of the dstrbuton of velocty and statc pressure for the channel rad of 5, 10, 15, 20, 25 mm at 124

2 (8) 2017 sm.nuos.edu.ua sm@nuos.edu.ua Knetc energy of turbulence (m 2 /s) Dynamc pressure R = 25 mm R = 20 mm R = 15 mm R = 10 mm R = 5 mm Fg. 8. Calculaton of the dstrbuton of knetc energy of turbulence and dynamc pressure for the channel rad of 5, 10, 15, 20, 25 mm at 125

sm.nuos.edu.ua sm@nuos.edu.ua 2 (8) 2017 Dstrbuton of velocty (m/s) Statc pressure (Pa) R = 25 mm R = 20 mm R = 15 mm R = 10 mm R = 5 mm Fg. 9. Calculaton of the dstrbuton of velocty and statc pressure for the channel rad of 5, 10, 15, 20, 25 mm at 126

2 (8) 2017 sm.nuos.edu.ua sm@nuos.edu.ua Knetc energy of turbulence (m 2 /s) Dynamc pressure R = 25 mm R = 20 mm R = 15 mm R = 10 mm R = 5 mm Fg. 10. Calculaton of the dstrbuton of knetc energy of turbulence and dynamc pressure for the channel rad of 5, 10, 15, 20, 25 mm at 127

sm.nuos.edu.ua sm@nuos.edu.ua 2 (8) 2017 As a result, t has been establshed that the deposton channel wth the radus of 15 mm and the velocty range of 1...10 m/s are the most effcent separaton optons. Upon studyng the most effcent radus of the separatng profle and determnng the workng veloctes n the channel, there has been developed a general scheme of shp ar purfcaton systems amed at elmnaton of droplet mosture and created a three-dmensonal model of the 1000 500 116 mm separator (Fg. 11). The model was taken as a bass for buldng a calculaton grd (see Table 2 and Fg. 12) wth the followng parameters: hree-dmensonal real-sze geometry of 1000 500 116 mm; calculaton grd bult of trangular segments wth the area of S = 30 10 8 m 2 ; envronment parameters normal condtons; gas densty of ρ g = 1.225 kg/m 3 ; gas vscosty of µ g = 1.79 10 5 kg/(m s); the channel wall materal s alumnum wth the roughness of 0.1 mm and densty of ρ al = 2690 kg/m 3 ; mnmal partcle dameter d mn of 3 μm; average partcle dameter d md of 100 μm; maxmum partcle dameter d max of 150 μm; concentraton of the lqud phase (H 2 O) 5, 10, 15, 20 %; velocty range 1, 2, 3, 4, 5, 6, 7, 8, 9, 10 m/s. Ar purfcaton from droplet mosture that take place n shp systems nvolves mosture deposton on the surface of separatng profles and water dranage nto a tray, wthout damage to the formed water flm (secondary floodng of the flow). In the curved channel, droplets of water transported by the ar flow are deposted under the acton of nertal forces both on the convex (frontal) and concave part of the channel. In shp ar condtoners, the ntake ar velocty s wthn the range of 2...10 m/s, the concentraton of droplet mosture reaches 30 g/kg, and the average weght dameter of droplets reaches 100 150 μm when water s beng dspersed wth mechancal nozzles and 200 μm when the flm breaks away from the edges. The droplet mosture deposton has been studed expermentally on a test stand n the form of an open-type aerodynamc tube. As a result, the maxmum concentraton of the lqud phase for ths separatng profle was establshed at the ntal ar velocty of U = 1...10 m/s. The dsperse ar-water mxture was prepared n the mxng chamber wth the help of mechancal and pneumatc nozzles. The dspersty was determned by means of the contact method,.e. by applyng droplets onto mrror plates wth subsequent photographng. The separa- a) b) Fg. 11. General scheme of shp systems for ar purfcaton from droplet mosture (a), three-dmensonal model of the separator of 1000 500 116 mm (b): 1 separatng profle; 2 fastenng flange; 3 dran tray; 4 dran ppe; 5 separatng profle fastenng; (for А А: 1 separatng profle; 2 separatng profle fastenng); А, В А1, H, b, h equpment dmensons 128

2 (8) 2017 sm.nuos.edu.ua sm@nuos.edu.ua Table 2. Calculaton results for the deposton coeffcent of the 1000 500 116 mm separator U, m/s Lqud phase concentraton n the flow 5 % 10 % 1 5% 20 % d mn d md d max d mn d md d max d mn d md d max d mn d md d max 1 90.1 99.9 100 85.9 99.9 100 83.9 99.9 100 82.8 99.9 100 2 90.3 99.9 100 85.6 99.9 100 83.6 99.9 100 82.2 99.9 100 3 90.6 99.9 100 85.2 99.9 100 83.3 99.9 100 81.9 99.9 100 4 90.0 99.9 100 85.4 99.9 100 83.2 99.9 100 81.6 99.9 100 5 90.4 99.9 100 85.1 99.9 100 83.1 99.9 100 81.2 99.9 100 6 90.1 99.9 100 84.5 99.9 100 82.7 99.9 100 80.8 99.9 100 7 90.2 99.9 100 84.1 99.9 100 82.3 99.9 100 80.4 99.9 100 8 89.9 99.9 100 83.9 99.9 100 81.9 99.9 100 80.2 99.9 100 9 89.4 99.9 100 83.6 99.9 100 81.5 99.9 100 79.8 99.9 100 10 89.1 99.9 100 83.1 99.9 100 81.1 99.9 100 79.1 99.9 100 GENERAL THREE-DIMENSIONAL MODEL 1000 500 116 MM sosymmetry sde vew top vew Velocty dstrbuton n the channel (m/s) Fg. 12. Calculaton grd and velocty calculaton for the separator model of 1000 500 116 mm 129

sm.nuos.edu.ua sm@nuos.edu.ua 2 (8) 2017 ton ablty was determned va three methods: materal balance, contact method, and fltraton wth the help of analytcal Petryanov flters. The analyss has showed that droplets are deposted on the convex and concave parts of the profle n comparable amounts. As a result, two-sde dran elements should be ftted nto the separatng profles to prevent secondary floodng. A specal feature of the profles under development s a combnaton of a wave-shaped mddle part wth flat nlet and outlet parts. The profles are assembled nto curved channels wth a number of successve convergng and dffusng sectons. The latter have breakaway zones wth the reverse gas flow. There, the lqud flm resultng from the deposton of droplets s subect to the mpact of vortces whch prevent the flm movement wth the man flow, contrbutng to ts dranage under the acton of gravty. The vortex zones provde complete removal of the captured mosture from the smooth profle surface up to the velocty of 5 m/s. Above ths velocty, some part of the mosture s removed from the vortex zones. That s why, specal dran elements are provded to prevent secondary floodng of the flow n the flat secton of the separatng profle. In ar condtonng systems wth surface heat exchangers, the man source of droplet mosture s the ar cooler. The ar flow breaks the condensate flm away from the edges of the heat exchange surface, thus formng droplets. In the systems wth contact devces, the processed ar s saturated wth mosture droplets n nozzle chambers, flm machnes, etc. The droplet sze depends on the mode of spatterng, the condtons of the water partcles breakaway from the surface, and the essence of nteracton of the partcles wth the ar flow. Large droplets may be crushed under the mpact of aerodynamc forces. Theoretcal and expermental studes ndcate that the dsntegraton of droplets s determned by the Weber number. When t exceeds 14, all the drops are dsntegrated; the larger the Weber number s, the smaller the newly formed droplets are. The conducted theoretcal and expermental studes allowed for the development and approval of drawngs for a lneup of shp systems for ar purfcaton from droplet mosture, as well as an enterprse standard for ths lneup (Table 3 5). Table 3. Expermental data for the deposton coeffcent of the 1000 500 116 mm separator U, Lqud phase concentraton n the flow m/s 5 % 10 % 15 % 20 % 25 % 30 % 35 % 40 % 45 % 50 % 55 % 60 % 65 % 70 % 75 % 80 % 1 99.9 99.9 99.9 99.9 99.9 94.9 91.4 90.6 81.1 79.2 75.0 71.9 67.8 61.7 55.4 53.1 2 99.9 99.9 99.9 99.9 99.9 94.1 91.9 91.3 81.8 78.4 75.1 71.2 66.4 62.9 55.4 51.9 3 99.9 99.9 99.9 99.9 99.9 95.9 91.0 91.6 81.9 79.3 74.8 70.9 67.7 63.8 54.2 50.4 4 99.9 99.9 99.9 99.9 99.9 95.4 91.1 91.2 81.3 78.9 74.1 69.0 68.5 62.3 55.2 51.1 5 99.9 99.9 99.9 99.9 99.9 95.1 91.9 90.2 80.3 79.6 73.0 68.8 69.4 61.3 54.2 51.9 6 99.9 99.9 99.9 99.9 99.9 90.1 84.8 89.9 78.9 71.9 68.9 61.9 63.2 54.1 49.9 45.9 7 99.9 99.9 99.9 99.9 99.9 82.9 82.5 82.2 74.1 69.2 62.1 57.1 53.9 49.4 44.1 39.9 8 99.9 99.9 99.9 99.9 99.9 80.3 79.3 74.9 70.7 64.3 57.8 52.0 47.3 41.6 37.8 32.9 9 99.9 99.9 99.9 99.9 99.9 78.2 77.1 71.2 66.4 59.9 51.2 45.7 41.2 36.7 32.5 26.9 10 99.9 99.9 99.9 99.9 99.9 83.9 75.9 69.9 61.9 54.9 46.9 41.8 35.9 31.9 28.2 24.9 Table 4. Classfcaton of water separators Types of water separators VVM VVM1 VVK General purpose Man ar/water separators for ar condtonng and ventlaton systems Man ar/water separators for machne ventlaton systems Ar/water separators of central ar condtoners n ar condtonng systems Table 5. Lst of water separators by volumetrc consumpton Desgnaton Volumetrc ar consumpton, m3/h (mm of water column) Aerodynamc drag, Pa VVM 6.3 630 1600 40 250 VVM 10.0 1000 2500 55 315 VVM 16.0 1600 4000 40 250 VVM 25.0 2500 6300 40 250 VVM 40.0 4000 10000 45 315 VVM 63.0 6300 16000 40 250 VVM1 100.0 10000 16000 60 155 VVM1 160 16000 25000 65 150 VVM1 250.0 25000 40000 92 235 VVM1 400.0 30000 40000 100 160 VVK 16.0 1600 4000 20 100 VVK 25.0 2500 6300 25 125 VVK 40.0 4000 10000 20 100 VVK 63.0 6300 16000 20 155 Workng mosture saturaton, g/kg of dry ar Separatng property, % (margnal devaton 1.0) 20 100 130

2 (8) 2017 sm.nuos.edu.ua sm@nuos.edu.ua a) b) с) Fg. 13. Three-dmensonal exteror desgn of the shp system for ar purfcaton from droplet mosture: а 500 250 116 mm; b 1000 500 116 mm; c 2000 1000 116 mm Fg. 13 demonstrates the typcal desgn of a shp system for ar purfcaton from droplets mosture wth a sngle-row package of separatng profles wth the followng dmensons: 500 250 116 mm, 1000 500 116 mm, 2000 1000 116 mm. They have been suppled wth desgn documentaton and workng prototypes. Tests of these water separators have showed that the capture coeffcent s practcally equal to 100 % at the mosture saturaton up to 50 g/kg and the ntake ar velocty up to 10 m/sec. At the velocty of 5 m/s, the aerodynamc drag makes up 50 N/m 2. CONCLUSIONS. 1. Mathematcal modelng of separaton at the ntal ar velocty of 5, 10, 15, 20 m/s has been performed wth the use of separaton gradent aerosol technologes at dfferent flow rates n separatng profles wth the rad of 5, 10, 15, 20, 25 mm. 2. Dstrbuton of velocty, statc pressure, dynamc pressure, knetc energy of turbulence and deposton coeffcents has been calculated based on separaton gradent aerosol technologes for the flow rates of 5, 10, 15, 20 m/s n separatng profles wth the rad 5, 10, 15, 20, 25 mm. The coeffcent of droplet mosture deposton was calculated for the flow rates of 5, 10, 15, 20 m/s n separatng profles wth the rad 5, 10, 15, 20, 25 mm. 3. There have been developed desgn solutons for shp systems for ar purfcaton from droplet mosture for the ar consumpton rangng from 20 to 2000 m 3 /h. 4. Drawngs for a lneup of the shp ar purfcaton systems have been developed. 5. The enterprse standard for the lneup of the shp ar purfcaton systems has been developed. C. С. Рыжков Статью рекомендует в печать д-р экон. наук, проф. Н. И. Радченко 131