Hydrodynamic modeling of downward gas-solids flow. Part I: Counter-current flow
Samo za registrovane korisnike
2014
Autori
Garić-Grulović, RadmilaKaluđerović-Radoičić, Tatjana
Arsenijević, Zorana
Đuriš, Mihal
Grbavčić, Željko
Članak u časopisu (Objavljena verzija)
Metapodaci
Prikaz svih podataka o dokumentuApstrakt
The one-dimensional model of accelerating turbulent downward counter-current gas-solids flow of coarse particles was formulated and experimentally verified by measuring the pressure distribution along the transport tube. The continuity and momentum equations were used in the model formulation and variational model was used for the prediction of the fluid-particle interphase drag coefficient. Experiments were performed by transporting spherical glass particles 1.94 mm in diameter in a 16 mm i.d. acrylic tube at constant solids mass flux of 392.8 kg/m(2)s. Tube Reynolds number ranged from 170 to 5300 and the slip Reynolds number from 650 to 1060. Under these conditions loading ratio (G(p)/G(f)) varied between 66 and 2089. Visual observations show that particles flow downward in apparently homogenous dispersion. Experimental data for the static fluid pressure distribution along the transport tube agree quite well with the model predictions. The mean voidage and the particle velocity decre...ase, while the slip velocity increases with the increase in gas superficial velocity. The values of the pressure gradient, porosity, particle velocity and slip velocity along the tube were calculated according to the formulated model. In these calculations, particle-wall friction coefficient was determined indirectly by adjusting the f(p) value to agree with the experimental data. The effect of the value of fp on the model calculations was significant. Calculations show that the acceleration length for the same particles (1.94 mm) in downward counter-current gas-solids flow is about two times higher than the acceleration length in upward co-current gas-solids flow. In the system investigated, "choking" occurs at slip velocity which is about 73% of the single particle terminal velocity.
Ključne reči:
Counter-current gas-solids flow / Solids downward / Gas upward / Hydrodynamic modelingIzvor:
Powder Technology, 2014, 256, 404-415Izdavač:
- Elsevier, Amsterdam
Finansiranje / projekti:
- Razvoj efikasnijih hemijsko-inženjerskih procesa zasnovan na istraživanjima fenomena prenosa i principima intenzifikacije procesa (RS-MESTD-Basic Research (BR or ON)-172022)
DOI: 10.1016/j.powtec.2014.01.090
ISSN: 0032-5910
WoS: 000335097600049
Scopus: 2-s2.0-84896398979
Institucija/grupa
Tehnološko-metalurški fakultetTY - JOUR AU - Garić-Grulović, Radmila AU - Kaluđerović-Radoičić, Tatjana AU - Arsenijević, Zorana AU - Đuriš, Mihal AU - Grbavčić, Željko PY - 2014 UR - http://TechnoRep.tmf.bg.ac.rs/handle/123456789/2860 AB - The one-dimensional model of accelerating turbulent downward counter-current gas-solids flow of coarse particles was formulated and experimentally verified by measuring the pressure distribution along the transport tube. The continuity and momentum equations were used in the model formulation and variational model was used for the prediction of the fluid-particle interphase drag coefficient. Experiments were performed by transporting spherical glass particles 1.94 mm in diameter in a 16 mm i.d. acrylic tube at constant solids mass flux of 392.8 kg/m(2)s. Tube Reynolds number ranged from 170 to 5300 and the slip Reynolds number from 650 to 1060. Under these conditions loading ratio (G(p)/G(f)) varied between 66 and 2089. Visual observations show that particles flow downward in apparently homogenous dispersion. Experimental data for the static fluid pressure distribution along the transport tube agree quite well with the model predictions. The mean voidage and the particle velocity decrease, while the slip velocity increases with the increase in gas superficial velocity. The values of the pressure gradient, porosity, particle velocity and slip velocity along the tube were calculated according to the formulated model. In these calculations, particle-wall friction coefficient was determined indirectly by adjusting the f(p) value to agree with the experimental data. The effect of the value of fp on the model calculations was significant. Calculations show that the acceleration length for the same particles (1.94 mm) in downward counter-current gas-solids flow is about two times higher than the acceleration length in upward co-current gas-solids flow. In the system investigated, "choking" occurs at slip velocity which is about 73% of the single particle terminal velocity. PB - Elsevier, Amsterdam T2 - Powder Technology T1 - Hydrodynamic modeling of downward gas-solids flow. Part I: Counter-current flow EP - 415 SP - 404 VL - 256 DO - 10.1016/j.powtec.2014.01.090 ER -
@article{ author = "Garić-Grulović, Radmila and Kaluđerović-Radoičić, Tatjana and Arsenijević, Zorana and Đuriš, Mihal and Grbavčić, Željko", year = "2014", abstract = "The one-dimensional model of accelerating turbulent downward counter-current gas-solids flow of coarse particles was formulated and experimentally verified by measuring the pressure distribution along the transport tube. The continuity and momentum equations were used in the model formulation and variational model was used for the prediction of the fluid-particle interphase drag coefficient. Experiments were performed by transporting spherical glass particles 1.94 mm in diameter in a 16 mm i.d. acrylic tube at constant solids mass flux of 392.8 kg/m(2)s. Tube Reynolds number ranged from 170 to 5300 and the slip Reynolds number from 650 to 1060. Under these conditions loading ratio (G(p)/G(f)) varied between 66 and 2089. Visual observations show that particles flow downward in apparently homogenous dispersion. Experimental data for the static fluid pressure distribution along the transport tube agree quite well with the model predictions. The mean voidage and the particle velocity decrease, while the slip velocity increases with the increase in gas superficial velocity. The values of the pressure gradient, porosity, particle velocity and slip velocity along the tube were calculated according to the formulated model. In these calculations, particle-wall friction coefficient was determined indirectly by adjusting the f(p) value to agree with the experimental data. The effect of the value of fp on the model calculations was significant. Calculations show that the acceleration length for the same particles (1.94 mm) in downward counter-current gas-solids flow is about two times higher than the acceleration length in upward co-current gas-solids flow. In the system investigated, "choking" occurs at slip velocity which is about 73% of the single particle terminal velocity.", publisher = "Elsevier, Amsterdam", journal = "Powder Technology", title = "Hydrodynamic modeling of downward gas-solids flow. Part I: Counter-current flow", pages = "415-404", volume = "256", doi = "10.1016/j.powtec.2014.01.090" }
Garić-Grulović, R., Kaluđerović-Radoičić, T., Arsenijević, Z., Đuriš, M.,& Grbavčić, Ž.. (2014). Hydrodynamic modeling of downward gas-solids flow. Part I: Counter-current flow. in Powder Technology Elsevier, Amsterdam., 256, 404-415. https://doi.org/10.1016/j.powtec.2014.01.090
Garić-Grulović R, Kaluđerović-Radoičić T, Arsenijević Z, Đuriš M, Grbavčić Ž. Hydrodynamic modeling of downward gas-solids flow. Part I: Counter-current flow. in Powder Technology. 2014;256:404-415. doi:10.1016/j.powtec.2014.01.090 .
Garić-Grulović, Radmila, Kaluđerović-Radoičić, Tatjana, Arsenijević, Zorana, Đuriš, Mihal, Grbavčić, Željko, "Hydrodynamic modeling of downward gas-solids flow. Part I: Counter-current flow" in Powder Technology, 256 (2014):404-415, https://doi.org/10.1016/j.powtec.2014.01.090 . .