Lecture 14-15_gas-liquid Equipment 474j7

Mass Transfer Operations I Equipment for Gas-Liquid Operations

Lecture 14 The major gas-liquid operations include absorption and stripping, distillation, humidification and dehumidification etc. The operations involve interphase mass transfer and require intimate among the phases. The main purpose of the equipment for interphase mass transfer is to provide intimate of the immiscible phases. In many applications, the mass transfer equipment operates in the continuous mode. Batch ing is sometimes used, particularly for low processing capacities or in small production units. A high degree of turbulent mixing is created properly disperse one phase into the other. This helps in generating a large interfacial area of as well as in increasing the mass transfer coefficient. Mass transfer equipment is mostly custom built (i.e., designed and fabricated according to the requirements of the client; these types of equipment cannot be readily purchased from the market as on-the-self items like pumps, valves, blowers, air conditioners etc.). A variety of gas-liquid ing equipment is in use. These can be classified as follows: (1)

Gas Dispersed: In some equipment, the gas is dispersed in the liquid in the form of bubbles. For example: bubble columns, agitated vessels, tray towers, etc

(2)

Liquid Dispersed: In some equipment, the liquid is dispersed in the form of droplets or discontinuous films in a continuous gas phase. For example: venturi scrubbers, wetted wall column, spray towers, packed towers, etc.

Tray and packed columns are most widely used for gas-liquid ing - namely for gas absorption, stripping, distillation. 1. Gas-Liquid Operations: Gas Dispersed Main objectives are the following: (a) Design bubble columns

(b) Design tray or plate columns (c) Estimate the stage efficiencies for tray columns

1.1 Sparged Vessels

A sparger is a device by which a stream of gas can be introduced in the form of bubbles into the liquid.

For small vessel diameter, a single open tube located at the bottom of the vessel may be used as sparger. For larger diameter vessels (dia>0.3 m) several orifices are generally used for better distribution of gas into the liquid. In this case: Sparger dia: varies from 1.5 mm to 3 mm. Sparger materials: ceramics, plastics or sintered metals

Purpose of sparger: (i) ing sparged gas with the liquid or (ii) simply may be a device for agitation

TRAY OR PLATE COLUMN A tray tower primarily consists of a vertical cylindrical shell and a set of 'tower internals' that include (i) trays or plates on which the gas-liquid occurs, (ii) arrangements for flow of the liquid from one tray to the lower one through the down comer, and (iii) inlet and outlet nozzles for the two phases. Figure 5.1 schematically shows a few essential parts of a 'sieve tray' column. In a gas absorption application, the liquid enters the top tray through a nozzle. It flows across each tray and flows into the lower tray through a 'downcomer'. The gas flows upwards and vigorously bubbles through the liquid on a tray, forming a turbulent 'gas-liquid dispersion' in which bubble breakage and coalescence occur continuously. An average depth of the dispersion is maintained on a tray. Mass transfer from the gas to the liquid (or from the liquid to the gas) phase occurs depending on the direction of the driving force. For example, in 'gas absorption', the solute gets transported from the gas to the liquid phase; the reverse occurs in stripping.

The gas then leaves the froth or dispersion and enters the next upper tray. The liquid flows across a tray and then over a 'weir' to enter into the downcomer. The downcomer is a region near the wall, separated by a 'downcomer plate', in which the bubbles get disengaged from the liquid. In this way, countercurrent and stage-wise gas liquid takes place in the tower. Each tray acts as a stage in which the liquid flowing down from the upper tray and the gas flowing up from the lower tray come into ; the tower acts as a cascade. The number of equilibrium stages (ideal trays) required for a given separation is determined solely from material balances and equilibrium considerations. The stage efficiency and therefore the number of real trays is determined by mechanical design and the conditions of operation. The constructional and operational features of a tray tower and tower internals are briefly discussed below. The Shell The shell is usually made of a metal or an alloy. Plastic shells are also used sometimes. The material is selected on the basis of corrosiveness of the fluids, temperature and pressure conditions, and cost. If the shell diameter is small, it may be made of several flanged sections in order that the trays may be fitted into it and maintained, when necessary, by opening it. Tray towers of diameter less than 1 metre are rarely used. On the other extreme, towers as big as 10 metre in diameter are known to be in use. Shell thickness is calculated by using a standard vessel design code (for example, ASME Section VllI; IS 2825). A tower is generally 'skirt-ed' on concrete foundations. The should be strong enough to take the column weight, the liquid load and the wind stress. The seismic factor at the particular location is also needed to be considered during column and design. Since the bending moment due to wind load is maximum at the tower bottom, it is a common practice to use different wall thicknesses for different sections of the shell. The bottom section has the maximum thickness and the upper sections have gradually smaller thicknesses. This strategy substantially reduces the weight, and hence the cost, of the shell. The Tray A 'tray' has two major functions: I. It allows the gas to flow through the holes or ages; the gas vigorously bubbles through the liquid to form a 'gas-liquid dispersion'. The tray holds the dispersion on it. 2. The trays separate the column into a number of compartments each of which constitutes a stage. Mass transfer between the phases occurs on a tray. Therefore, the trays as a whole

constitute the heart of a column. The performance of a column depends upon the performance of the trays. Trays are also called 'plates'. There are quite a few types of trays in use. The bubble-cap tray A bubble cap consists of two major components-a bell-shaped 'cap' and a 'riser' (also called a 'chimney'). The riser is inserted through a hole on the tray floor and the bell-shaped cap is bolted to it. A ring gasket is used below the nut. The riser is a piece of tube with a flared or expanded bottom end. In fact, the riser acts as the vapour age and also holds the cap. The caps and the risers are made of low carbon steel, stainless steel or any other suitable material that can withstand the environment within the tower. Caps are arranged on a tray on equilateral triangular pitch with rows normal to the direction of liquid flow. Bubble caps generally range from 1 inch to 6 inches in diameter. The sieve tray This is the simplest type of tray in which the bubble caps are replaced by holes or perforations for entrance of the gas into the liquid. The holes are of relatively small diameter - usually ranging 1

1

from 8 to 2 inch. This is why the name 'sieve tray' (also called 'perforated tray'). For clean services, 3

use of a hole diameter of 16 inch is common. However, for liquids that foul or cause deposition, a 1

1

hole diameter of 2 inch may have to be used. In vacuum services, 8 inch hole diameter is preferred. Small holes enhance tray capacity, reduce entrainment, reduce weeping, promote froth regime operation and exhibit better mass transfer characteristics. The valve tray The valve tray is a relatively new class of tray that provides variable area for the gas or vapour flow depending upon the flow rate or 'throughput'. This is why it is called 'valve tray'. A valve tray is a proprietary tray. Different types of valve trays are made by different companies. A common valve tray has sufficiently large punched holes on the tray floor, each fitted with a movable disk, generally circular. A disk has guides that can slide vertically up or down along the thickness of the tray floor. The opening for the gas flow changes in this way, but the disk is always held in the same vertical line. As the gas flow increases, the disk is automatically raised. It settles down at a low vapour rate to prevent 'weeping'. The guides or retaining legs are bent at the end so that the disk does not pop up or gets detached even at a large vapour rate. The trays do not easily acquire deposits from dirty liquids, polymers or other solids because of the up and down motion of the disk and the guides. Valve units are, therefore, self-cleaning. The valve

tray is a good choice for highly fouling services. In addition, they offer lower pressure drop than the bubble-cap type and generally they are cheaper than the latter type. A few problems common to all kinds of valve trays are (i) mechanical wear and corrosion because of continuous movement of the valve legs, and (ii) sticking of the disk on the tray if there is sticky deposition on the tray. In a common valve tray layout, 12 to 16 valves per ft2 of tray area are accommodated. Because of high flexibility, high turndown ratio and relatively low cost, valve trays are now widely used for gas absorption and distillation. Downcomers and weirs The 'downcomer' is a age through which the liquid flows down from one tray to the next below. The desired depth of the gas-liquid dispersion is maintained on a tray by using a 'weir' in the form of a vertical plate. The liquid, along with some dispersed gas or vapour bubbles, overflows the weir and enters the 'downcomer' or the 'downspout'. Disengagement of the gas as bubbles occurs in the upper region of a downcomer. The lower region contains clear liquid that enters the lower tray. The downcomer must provide sufficient residence time for gas-liquid disengagement. The residence time is usually 3 to 5 seconds. However for a foaming liquid, considerably higher residence time and therefore a larger downcomer volume has to be provided. The 'clear liquid' velocity in the downcomer normally ranges between 0.3 and 0.5 ft/s. This value may vary depending upon the liquid properties. The weir length may vary from 60 to 80% of the tower diameter; the downcomer area correspondingly varies from 5 to 15% of the tray area. A weir height of 1 to 2 inches is generally maintained. Nozzles A tower for ing a liquid and a vapour (or a gas) should be provided with a few nozzles for feed entry (both gas and liquid), entry of reflux at the top and of the reboiler vapour return at the bottom (in a distillation column), and for product withdrawal from the tower. The primary criterion of a feed nozzle design is to ensure that the feed is introduced with minimum splashing or jetting (the velocity of liquid feed in the nozzle should not exceed 1 m/s). The feed should be evenly distributed and mixed with internal liquid or vapour. Mist Eliminator Even under normal operating conditions, a little entrainment of liquid in the upflowing vapour may occur. In order to prevent entrainment in the vapour leaving the top tray, a pad made of wire mesh or a pack of suitably bent and spaced thin sheets is fitted above it. The droplets are retained after they strike the surface of the pad. Such a device is called 'mist eliminator' or a 'demister'

Lecture 15 OPERATIONAL FEATURES OF A TRAY COLUMN The flow phenomena on a tray with the gas bubbling vigorously through the flowing liquid are pretty complex. The tray internals are selected and designed, keeping in view the complexity of the flow and the problems that may arise out of it.

Hydraulic Gradient and Multi Trays The difference between the 'clear liquid heights' at the points of inlet and outlet on a tray is called the 'hydraulic gradient' or 'liquid gradient’. It is the liquid head required for overcoming the resistance to liquid flow on a tray. The hydraulic gradient on a tray should not exceed a fraction of 1

an inch. It should preferably be kept within 2 inch. An excessive liquid gradient causes severe malfunctioning of the tray; most of the gas flows through the holes near the middle of the tray and at the outlet weir and only a small part flows through the holes at the liquid inlet side of the tray. Such maldistribution of the gas or the vapour severely reduces the 'tray efficiency'. In extreme cases, liquid 'dumping' or 'back-trapping' may occur through the end where the liquid enters the tray. Hydraulic gradient is a very important quantity to be checked during tray design. It remains pretty small for a sieve tray. But for a bubble-cap tray it may be significant because the bubble caps offer a larger resistance to liquid flow.

Weeping and Dumping If a very small fraction of the liquid flows from a tray to the lower one through perforations or openings of the tray deck, the phenomenon is called 'weeping'. Weeping causes some reduction of the 'tray efficiency' because the liquid dripping down to the tray below through the perforations has not been in full with the gas or vapour. On the other hand, 'dumping' is an extreme case of leakage through the tray deck if the vapour velocity is low and the vapour pressure drop across the tray is not sufficient to hold the liquid. In practice, a little bit of weeping may occur intermittently through sieve trays because of the instantaneous pressure imbalance. Entrainment When a gas bubbles through the liquid pool vigorously, droplets of liquid are formed in the vapour space by quite a few mechanisms including shearing action of the gas jet or rupture of the liquid film as a gas bubble bursts. Depending upon the size of a droplet, its velocity of projection and the drag force acting on it due to the gas velocity, the droplet may descend back into the liquid on the tray or may be carried into the tray above. The phenomenon of carry over of the suspended droplets

into the upper tray is called 'entrainment'. The chances of entrainment are more if a droplet is small, if the gas velocity is large, or if the tray spacing is small. Flooding Under normal operating conditions, an average liquid depth is maintained on a tray. 'Flooding' is an abnormal condition of excessive accumulation of liquid and simultaneous excessive pressure drop across the flooded tray. If accumulation of liquid on a tray continues, a part or eventually the entire column may be filled with the liquid. Flooding of a tray or a column may occur because of one or more of the following reasons: Spray entrainment flooding At a low liquid rate, the spray height increases as the vapour velocity is increased. The spray may eventually reach the downside of the tray above, causing a substantial carry over of the liquid droplets and leading to flooding of the tray and the column. Froth entrainment flooding Froth appears on a tray over a range of gas and liquid flow rates. Depending upon the flow rates of the phases and the tray spacing, the froth may almost fill the entire space between two successive trays. Most of the liquid droplets suspended in the gas are then carried into the upper tray causing liquid accumulation thereon and eventual flooding of the tray. If the liquid is prone to foaming on aeration, flooding may occur even at lower gas velocities. Downcomer flooding When the liquid flow rate is high, the rate of flow of the gas-liquid dispersion into the downcomer also becomes high. If the downcomer cannot accommodate the dispersion load and the gas-liquid disengagement does not occur properly, the aerated frothy liquid fills the downcomer and finally backs up onto the tray above leading to 'downcomer flooding'. One strategy of overcoming the problem of downcomer flooding is to provide a larger tray spacing. The Performance Diagram The performance of a particular type of tray depends upon the relative liquid and vapour throughputs. The effects of the phase flow rates on the performance of a sieve tray are qualitatively shown in Figure 5.10. This is also called the tray stability diagram. Let us assume that the tray operates at gas and liquid rates corresponding to point N located in the 'region of normal operation' in Figure 5.10. If we keep on increasing the gas throughput at a constant liquid rate, more liquid is entrained in the gas. At point E, the gas rate is high enough to

cause excessive entrainment. The tray efficiency falls to an unacceptable level. At point F, the tray gets flooded and is inoperable. Also, the tray does not operate satisfactorily if the gas rate is kept on decreasing. At a gas rate corresponding to point W, the gas pressure drop across the tray decreases to the extent that some liquid starts leaking through the tray holes. This is weeping of the tray as discussed before. As the gas rate is further reduced to point L, the weeping rate increases significantly causing deterioration of performance of the tray. The tray should be operated above this point. If the gas throughput is yet reduced to the point D, dumping of liquid starts. Under such a condition, most of the liquid es through the tray holes and little, if any, flows into the downcomer. The operable limits of a tray in respect of gas and liquid flow rates depend on the tray design, temperature and pressure conditions as well as the properties of the liquid and vapour phases. Turndown Ratio A column designed for a particular capacity may have to be operated at an enhanced or reduced capacity depending upon changes in the production rate in the plant due to various factors. It is, therefore, desirable that the trays have some degree of flexibility to operate over a range of throughput around the design capacity. Such flexibility is expressed in of the 'turndown ratio', which is defined as the ratio of the 'design vapour throughput' to the 'minimum operable throughput'. Sieve trays have a low turndown ratio of about 2. Valve trays normally have a turndown ratio of 4; bubble-cap trays have a still larger turndown ratio. Tray Spacing Tray spacing is the distance or gap between two consecutive trays in a column. An adequate tray spacing is important for quite a few reasons. The rate of entrainment strongly depends upon the tray spacing. If a larger spacing is provided, most of the liquid droplets descend back to the tray reducing the entrainment. The column can operate at a greater superficial gas velocity and a smaller column diameter can be used for a given throughput. But the column height increases if the same number of trays have to be accommodated. Hence, a trade-off between a smaller column diameter and a larger height has to be struck. Tray spacing varies over a pretty wide range of 8 to 36 inches. For a column 4ft or larger in diameter, a tray spacing of 18 to 24 inches is adequate.

TRAY DESIGN While deg a process plant or a part of it, complete material and energy balance calculations for every piece of equipment or device are done in order to establish the design basis in of the flow rate, the composition, the temperature 'and pressure of each stream as well as the amount of heat input, output and generation, if any. For example, before we proceed to design a tray or a packed tower, we need to know the flow rates, the compositions, and the temperatures of all the liquid and the gas (or vapour) streams entering and leaving the tower as well as the operating pressure. In addition, the physical properties of the streams such as density, viscosity, diffusivity, surface tension, etc. are required to be known or estimated for use in design calculations. Of the three most common types of trays-namely, bubble-cap, sieve and valve trays-the design methods of the former two are pretty well-established. Here we give a brief outline of the procedure of design of a sieve tray (also called 'perforated tray'). Valve trays are 'proprietary' trays and only limited information on their design is available in the open literature. Design of a sieve tray for gas (or vapour)-Liquid Once the design basis (the flow rates, the compositions, the temperatures, the pressures, etc.) of the streams is established, the number of trays required for the specified degree of separation of a feed mixture is determined following the procedures described in other Chapters. The next step is the selection and design of the tray. So far as the design of a sieve tray is concerned, the major items to be determined are the tray diameter (i.e. the column diameter), Tray gas-pressure drop, the size and layout of the holes, the tray spacing and tower internals such as downcomers and weir, and Tray efficiency. Tray (or Column) Diameter The required diameter of a tray or the column for the given flow rates of the gas and the liquid phase is determined from flooding considerations. It has been stated before that as the gas velocity in a column is gradually increased, a limiting velocity is attained above which entrainment is high enough to cause accumulation of liquid on the trays leading to flooding. This velocity corresponds to the theoretical maximum capacity of the column. There are a few methods of calculation of the flooding velocity. Brown equation that gives the flooding velocity for 'spray entrainment flooding' is as follows:

𝑢𝑠,𝑓𝑙

𝜌𝐿 − 𝜌𝐺 1/2 = 𝐶𝑆𝐵 ( ) 𝜌𝐺

Here 𝑢𝑠,𝑓𝑙 is the 'superficial velocity, at flooding, and CSB is called the 'Souders-Brown flooding constant' (sometimes called 'capacity factor'). In reality the quantity CSB is not a constant; it depends upon tray spacing S, liquid load, fractional hole area on a tray and the hole diameter. The value of the empirical constant C depends on the tray design, tray spacing, flow rates, liquid surface tension and foaming tendency. This can be estimated using the following relationship: 𝐶𝑆𝐵 = 𝐹𝑠𝑡 𝐹𝐹 𝐹𝐻𝐴 𝐶𝐹 where Fst = surface tension factor = (/20)0.2  = surface tension, dyn/cm FF = foaming factor = 1.0 for nonfoaming systems; for many absorber may be 0.75 or even less FHA = 1.0 for (Ah/Aa)0.10, and 5(Ah/Aa)+0.5 for (Ah/Aa) 0.1 (Ah/Aa) = ratio of vapor hole area to tray active area 1

𝐶𝐹 =  log (𝑋) + 𝛽 where  = 0.0744t + 0.01173 β = 0.0304t + 0.015 X = flow parameter = (L/G) (𝜌𝐺 /𝜌𝐿 )0.5 t = tray spacing, m If the value of X is in the range of 0.01 to 0.1, then use X = 0.1 in the above eqn.

Typically, the column diameter is based on a specific fractional approach to flooding f. Then, 1/2

4𝑄𝐺 𝐷=( ) 𝐴𝑑 𝑓 𝑉𝐺𝐹 (1 − ⁄𝐴 )  𝑡 It is suggested that Ad/At must be chosen based on the value of X, as

0.1 𝐴𝑑 𝑋 − 0.1 = {0.1 + 𝐴𝑡 9 0.2

𝑓𝑜𝑟 𝑋0.1 𝑓𝑜𝑟 0.1𝑋 1.0 𝑓𝑜𝑟 𝑋1.0

Problem: Ammonia is absorbed by pure water from air-ammonia mixture using a sieve-tray tower. The mixture contains 10% NH3 and 90% air. It is desired to remove 90% NH3. The gas enters at the bottom of the tower at a flow rate of 150 kmol/h at 298K and 1atm. The water is fed at the top of the tower at flow rate of 150kmol/h. Assume surface tension of liquid is 80 dyn/cm. The diameter of the sieve is 2 mm which is on an equilateral-triangular pitch of 10mm. The density of the liquid is 1000 kg/m3. The recommended foaming factor is 0.75. Design the tower for a 75% approach to the flooding velocity.