О влиянии распределения удельной скорости диссипации на эффективность массопереноса в аппаратах с жидкофазными средами

Мұқаба

Дәйексөз келтіру

Толық мәтін

Ашық рұқсат Ашық рұқсат
Рұқсат жабық Рұқсат берілді
Рұқсат жабық Тек жазылушылар үшін

Аннотация

Выполнен теоретический анализ влияния распределения локальной удельной скорости диссипации энергии на удельную поверхность контакта фаз, поверхностный и объемный коэффициенты массоотдачи в аппаратах с гетерофазными процессами и жидкой сплошной фазой, а также на качество смешения в аппаратах с гомофазными реакциями в жидкой фазе. Показано, что среднее по объему аппарата значение удельной скорости диссипации энергии не является полноценным критерием для оценки полезного эффекта, поскольку не учитывает, с одной стороны, локальный уровень диссипации энергии в активных зонах, с другой стороны, особенности структуры потоков и локальное время пребывания в активных зонах, в зависимости от геометрии аппарата и способа ввода в него энергии. Обсуждаются предельные случаи: неравномерное распределение энергии при наличии небольшой зоны объема с высокой скоростью диссипации; идеально равномерное распределение энергии по всему объему аппарата. В первом случае существенная часть объема используется неэффективно, во втором случае затрачивается чрезмерное количество энергии. В связи с этим рассматриваются концепции дозированного распределенного ввода энергии для длительных процессов и максимальной концентрации энергии в микрообъеме для быстропротекающих процессов.

Толық мәтін

Рұқсат жабық

Авторлар туралы

Р. Абиев

Санкт-Петербургский государственный технологический институт (технический университет)

Хат алмасуға жауапты Автор.
Email: abiev.rufat@gmail.com
Ресей, Санкт-Петербург

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1. JATS XML
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2. Fig. 1. Dependence of the ratio of the micromixing time to the square of the characteristic size (tm/d2) on the Reynolds number for eight types of micromixers [18]. The dashed line corresponds to formula (7).

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3. Fig. 2. Relationship between the segregation index Xs and mixing time tm in microreactors using the iodide-iodate method [18].

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4. Fig. 3. Distribution of the relative energy dissipation rate (φi = εi/εave) and the relative volume of zones Vrel.i by zones of a reactor with a turbine stirrer (data from [28] were used).

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5. Fig. 4. Diagram of the transformation of energy introduced into systems with a continuous liquid phase (liquid-liquid, liquid-gas, liquid-solid) taking into account the need to form an interphase surface.

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6. Fig. 5. Bubble column fermenter (BCF) 2

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7. Fig. 6. Tray column fermenter (TCF): 1 – body, 2 – plate, 3 – overflow pipe, 4, 5 – liquid inlet and outlet, 6, 7 – air inlet and outlet. The red dashed-dotted line outlines the zone of maximum shear stresses occurring near the holes in the plate. Above this zone – energy dissipation due to the work of the buoyant force during the movement of bubbles.

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8. Fig. 7. Gas-lift loop column fermenter (GLCF): 1 – body, 2 – air ejection unit, 3 – zones of intensive gas dispersion, 4 – zones with free movement of gas-liquid flow.

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9. Fig. 8. Typical character of the dependence of the specific rate of energy dissipation ε on the residence time in the apparatus τ in real apparatuses (a) and in an apparatus with a uniformly high specific rate of energy dissipation ε (b). The zone τact corresponds to the most intense local energy dissipation εloc.max.

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10. Fig. 9. The nature of the dependence of the specific rate of energy dissipation ε on the residence time in the apparatus τ in the apparatus with repeated (pulse) effects on the processed medium. The zones τact correspond to the most intensive local energy dissipation εloc.max.

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11. Fig. 10. Diagram of a flow-type pulsating apparatus [34, 35].

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12. Fig. 11. Dependences of the Sauter bubble diameter (d32, m) on the specific energy dissipation rate (ε, W/kg) for a flow-through pulsating apparatus (1 – 8th section, 2 – average for PAPT) [35], an apparatus with a turbine mixer (3–6), Lightnin static mixers (7–9) [33], 3 – data from Laakkonen et al. [37], 4 – data from Calderbank [32], 5 – Heyouni correlation at φ = 6% [33]; 6 – data from Alves et al. [38] for coalescing systems; 7–9 – Lightnin structures 1–3, respectively [33].

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13. Fig. 12. Dependence of the volumetric mass transfer coefficient on the specific energy dissipation rate (ε, W/kg): lines 1–3 – in the apparatus with Lightnin static mixers (structures 1–3, respectively) and in the flow-type pulsating apparatus (line 4) at φ = 6%.

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14. Fig. 13. Dependence of the volumetric mass transfer coefficient kLa (1/s) on the average specific energy dissipation rate ε (W/kg) for gas-liquid reactors: bubble columns (1), apparatus with stirrers (2), static mixers (3) and PAPT (4) (regions 1–3 are constructed according to data from [33], region 4 – according to data from [35]).

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