Adsorption_ VIVEK_NEERI

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ADSORPTION/ HEAT OF ADSORPTION/ REGENERATION METHODS/ PORE SIZE DISTRIBUTION ETC

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ADSORPTION EQUILIBRIA AND REGENERATION VIVEK KUMAR

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A d sorption is the process in which matter is extracted from one phase and concentrated at the surface of a second phase. (Interface accumulation). This is a surface phenomenon as opposed to absorption where matter changes solution phase, e.g. gas transfer. This is demonstrated in the following schematic. ADSORPTION d

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Adsorption Mechanism ADSORPTION MECHANISM

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Exchange adsorption (ion exchange)– electrostatic due to charged sites on the surface. Adsorption goes up as ionic charge goes up and as hydrated radius goes down. Physical adsorption : Van der Waals attraction between adsorbate and adsorbent. The attraction is not fixed to a specific site and the adsorbate is relatively free to move on the surface. This is relatively weak, reversible, adsorption capable of multilayer adsorption. C hemical adsorption: Some degree of chemical bonding between adsorbate and adsorbent characterized by strong attractiveness. Adsorbed molecules are not free to move on the surface. There is a high degree of specificity and typically a monolayer is formed. The process is seldom reversible. TYPES OF ADSORPTION

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SOME GENERAL ISOTHERMS

ADSORPTION ON SOLID SURFACES:

Adsorption process Adsorbent and adsorbate Adsorbent (also called substrate ) - The solid that provides surface for adsorption high surface area with proper pore structure and size distribution is essential good mechanical strength and thermal stability are necessary Adsorbate - The gas or liquid substances which are to be adsorbed on solid Surface coverage,  The solid surface may be completely or partially covered by adsorbed molecules ADSORPTION ON SOLID SURFACES define  =  = 0~1 number of adsorption sites occupied number of adsorption sites available

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Rate of adsorption Rate of desorption At equilibrium Mono-layer coverage ( m : mass of adsorbate adsorbed per unit mass of adsorbent) Adsorption Isotherm : the mass of adsorbate per unit mass of adsorbent at equilibrium & at a given temperature ( f : fraction of surface area covered) f 1- f LANGMUIR ISOTHERM

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For the Langmuir model linearization gives: A plot of C e /q e versus C e should give a straight line with intercept : and slope: Or:

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For the special case of heterogeneous surface energies (particularly good for mixed wastes) in which the energy term, “K F ”, varies as a function of surface coverage we use the Freundlich model. n and K F are system specific constants. FREUNDLICH ISOTHERM Here a plot of 1/q e versus 1/C e should give a straight line with intercept 1/Q a o and slope For the Freundlich isotherm use the log-log version : A log-log plot should yield an intercept of log K F and a slope of 1/n.

The BET isotherm:

The BET isotherm Theoretical development based on several assumptions: multimolecular adsorption 1st layer with fixed heat of adsorption H 1 following layers with heat of adsorption constant (= latent heat of condensation) constant surface (i.e. no capillary condensation) gives OT fig1.3 BET method useful, but has limitations microporous materials: mono - multilayer adsorption cannot occur, (although BET surface areas are reported routinely) assumption about constant packing of N 2 molecules not always correct? theoretical development dubious (recent molecular simulation studies, statistical mechanics) - value of C is indication o f the shape of the isotherm, but not necessarily related to heat of adsorption

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For the BET isotherm we can arrange the isotherm equation to get: Intercept = Slope =

Simplified method:

Simplified method 1-point method simplefied BET assuming value of C  100 (usually the case), gives usually choose p/p 0  0,15 method underestimates the surface area by approx. 5%.

ADSORPTION ON SOLID SURFACE:

Summary of adsorption isotherms Name Isotherm equation Application Langmuir Temkin   = c 1 ln( c 2 P ) Freundlich BET ADSORPTION ON SOLID SURFACE Chemisorption and physisorption Chemisorption Chemisorption and physisorption Multilayer physisorption Useful in analysis of reaction mechanism Chemisorption Easy to fit adsorption data Useful in surface area determination

ADSORPTION ON SOLID SURFACE:

Five types of physisorption isotherms are found over all solids Type I is found for porous materials with small pores e.g. charcoal. It is clearly Langmuir monolayer type, but the other 4 are not Type II for non-porous materials Type III porous materials with cohesive force between adsorbate molecules greater than the adhesive force between adsorbate molecules and adsorbent Type IV staged adsorption (first monolayer then build up of additional layers) Type V porous materials with cohesive force between adsorbate molecules and adsorbent being greater than that between adsorbate molecules ADSORPTION ON SOLID SURFACE I II III IV V relative pres. P/P 0 1.0 amount adsorbed

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To determine which model to use to describe the adsorption for a particular adsorbent/adsorbate isotherms experiments are usually run. Data from these isotherm experiments are then analyzed using the following methods that are based on linearization of the models. DETERMINATION OF APPROPRIATE MODEL

ADSORPTION-DESORPTION HYSTERESIS:

ADSORPTION-DESORPTION HYSTERESIS Hysteresis is classified by IUPAC (see fig.) Traditionally desorption branch used for calculation H1: narrow distribution of mesopores H2: complex pore structure, network effects, analysis of desorption loop misleading H2: typical for activated carbons H3 & 4: no plateau, hence no well-defined mesopore structure, analysis difficult H3: typical for clays Handbook fig 2 s 431

PORES AND POROUS SOLIDS:

Pore sizes micro pores d p <20-50 nm meso-pores 20nm < d p <200nm macro pores d p >200 nm Pores can be uniform (e.g. polymers) or non-uniform (most metal oxides) Pore size distribution Typical curves to characterise pore size: Cumulative curve Frequency curve Uniform size distribution (a) & non-uniform size distribution (b) PORES AND POROUS SOLIDS b d a d w d d  d w t b a  wt d Cumulative curve Frequency curve

POROSITY AND PORE SIZE:

POROSITY AND PORE SIZE The pore structure (porosity, pore diameter, pore shape) is important for the catalytic properties pore diffusion may influence rates pores may be too small for large molecules to diffuse into Measurement techniques: Hg penetration interpretation of the adsorption - desorption isotherms electron microscopy techniques

Hg PENETRATION:

Hg PENETRATION Based on measuring the volume of a non-wetting liquid forced into the pores by pressure (typically mercury) Surface tension will hinder the filling of the pores, at a given pressure an equilibrium between the force due to pressure and the surface tension is established: where P = pressure of Hg,  is surface tension and  is the angle of wetting Common values used:  = 480 dyn/cm and  = 140° give average pore radius valid in the range 50 - 50000Å

PORE SIZE DISTRIBUTION:

PORE SIZE DISTRIBUTION If the Hg-volume is recorded as a function of pressure and this curve is differentiated we can find the pore size distribution function V(r)=dV/dr OT fig 2.3.

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FACTORS WHICH AFFECT ADSORPTION EXTENT (AND THEREFORE AFFECT ISOTHERM) ARE: Adsorbate : Solubility In general, as solubility of solute increases the extent of adsorption decreases. This is known as the “Lundelius’ Rule”. Solute-solid surface binding competes with solute-solvent attraction as discussed earlier. Factors which affect solubility include molecular size (high MW- low solubility), ionization (solubility is minimum when compounds are uncharged), polarity (as polarity increases get higher solubility because water is a polar solvent). pH pH often affects the surface charge on the adsorbent as well as the charge on the solute. Generally, for organic material as pH goes down adsorption goes up. Temperature Adsorption reactions are typically exothermic i.e.,  H rxn is generally negative. Here heat is given off by the reaction therefore as T increases extent of adsorption decreases. Presence of other solutes In general, get competition for a limited number of sites therefore get reduced extent of adsorption or a specific material.

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If the a d sorbent and adsorbate are contacted long enough an equilibrium will be established between the amount of adsorbate adsorbed and the amount of adsorbate in solution. The equilibrium relationship is described by isotherms . Define the following: q e = mass of material adsorbed (at equilibrium) per mass of adsorbent C e = equilibrium concentration in solution when amount adsorbed equals q e. q e /C e relationships depend on the type of adsorption that occurs, multi-layer, chemical, physical adsorption, etc. Adsorption heat: The increase in enthalpy when 1 mole of a substance is adsorbed upon another at constant pressure. Adsorption is usually exothermic (in special cases dissociated adsorption can be endothermic) The heat of chemisorption is in the same order of magnitude of reaction heat; the heat of physisorption is in the same order of magnitude of condensation heat. DEFINITION

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ADSORPTION EQUILIBRIA If the a d sorbent and adsorbate are contacted long enough an equilibrium will be established between the amount of adsorbate adsorbed and the amount of adsorbate in solution. The equilibrium relationship is described by isotherms . Heats of Adsorption Gas adsorption to a solid is exothermic. The magnitude and variation as a function of coverage may reveal information concerning the bonding to the surface. Calorimetric methods determine heat, Q evolved. q i = integral heat of adsorption q D = differential heat of adsorption

HEAT OF ADSORPTION .. CONTINUED:

3/22/2012 HEAT OF ADSORPTION .. CONTINUED Since  G =  H - T  S , it is clear that for  G to be negative,  H of adsorption process must be negative. That is, the adsorption is an exothermic process . the amount of gas adsorbed will decrease as the temperature is increased. The molar enthalpy,  ads H m , of adsorption in reversible system will adhere to the Clausius-Clapeyron equation The subscript n represents an isosteric adsorption.  ads H m is called the molar isosteric enthalpy of adsorption .

ENTHALPY OF ADSORPTION:

ENTHALPY OF ADSORPTION Heats of adsorption change as a function of surface coverage differentiate Van’t Hoff equation

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DESORPTION AND REGENERATION OF ADSORBENTS Adsorbent particles have finite capacity for fluid phase molecules. An extended contact with the feed fluid will ultimately lead to the creation of a thermodynamic equilibrium between the solid adsorbent and the fluid phases. At this equilibrium condition the rates of adsorption and desorption are equal and the net loading on the solid cannot increase further, It is now becomes necessary either to regenerate the adsorbent or to dispose of it. In certain applications it may be more economical to discard the adsorbent after use. Disposal would be favoured when the adsorbent is of low cost, is very difficult to regenerate, and the non-adsorbed component is the desired product of very high value. In the majority of applications, the disposal of adsorbents as waste is not an economic option and therefore regeneration is carried out either in situ or external to the adsorption vessel to an extent that the adsorbents can be reused.

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Practical methods of desorption and regeneration include one, or more usually a combination, of the following: Increase in temperature Reduction in partial pressure Reduction in concentration Purging with an inert fluid Displacement with a more strongly adsorbing species Change of chemical conditions, e.g. pH The final choice of regeneration method(s) depends on technical and economic considerations. PRACTICAL REGENERATION METHODS

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FIXED-BED ADSORPTION PROCESS AND THEIR REGENERATION METHODS A. Pressure Swing Adsorption (PSA) Regeneration in a PSA process is achieved by reducing the partial pressure of the adsorbate. There are 2 ways in which this can be achieved: (1) a reduction in the system total pressure, and (2) introduction of an inert gas while maintaining the total system pressure. In the majority of pressure swing separations a combination of the 2 methods is employed. Use of a purge fluid alone is unusual.

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The Figure below shows the effect of partial pressure on equilibrium loading for a Type I isotherm at a temperature of T1. Reducing the partial pressure from p1 to p2 causes the equilibrium loading to be reduced from q1 to q2. PICTORIAL EXPLAINATION Changes in pressure can be effected very much more quickly than changes in temperature, thus cycle time of pressure swing adsorption (PSA) processes are typically in the order of minutes or even seconds. PSA processes are often operated at low adsorbent loadings because selectivity between gaseous components is often greatest in the Henry's Law region. It is desirable to operate PSA processes close to ambient temperature to take advantage of the fact that for a given partial pressure the loading is increased as the temperature is decreased. Typical PSA processes consist of 2-Bed system, although other systems (e.g. 1-Bed system or complex, multiple-beds system) had also been developed.

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PSA processes is a popular process for performing bulk separations of gases. Separations by PSA and VSA are controlled by adsorption equilibrium or adsorption kinetics. Both types of control are important commercially. For the separation of air with zeolites, adsorption equilibrium is the controlling factor. Nitrogen is more strongly adsorbed than oxygen. For air with about 21% oxygen and 79% nitrogen, a product of nearly 96% oxygen purity can be obtained. When carbon molecular sieves are used, oxygen and nitrogen have almost the same adsorption isotherms, but the effective diffusivity of oxygen is much larger than nitrogen. Hence more oxygen is adsorbed than nitrogen, and a product of very high purity nitrogen ( 99%) can be obtained. USES OF PSA PROCESSES

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B. TEMPERATURE SWING ADSORPTION (TSA) Regeneration of adsorbent in a TSA process is ahieved by an increase in temperature. The Figure below showed schematically the effect of temperature on the adsorption equilibrium (Type I isotherm) of a single adsorbate. For any given partial pressure of the adsorbate in the gas phase (or concentration in the liquid phase), an increase in temperature leads to a decrease in the quantity adsorbed. If the partial pressure remains constant at p1, increasing the temperature from T1 to T2 will decrease the equilibrium loading from q1 to q2. A relatively modest increase in temperature can effect a relatively large decrease in loading. It is therefore generally possible to desorb any components provided that the temperature is high enough. However, it is important to ensure that the regeneration temperature does not cause degradation of the adsorbents.

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A change in temperature alone is not used in commercial processes because there is no mechanism for removing the adsorbate from the adsorption unit once desorption from the adsorbents has occurred. Passage of a hot purge gas or steam, through the bed to sweep out the desorbed components is almost always used in conjunction with the increase in temperature. A very important characteristic of TSA processes is that they are used virtually exclusively for treating feeds with low concentrations of adsorbates. TSA.. CONTD........

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C. DISPLACEMENT PURGE ADSORPTION (DPA) Adsorbates can be removed from the adsorbent surface by replacing them with a more preferentially adsorbed species. This displacement fluid, which can be a gas, a vapour or a liquid, should adsorb about as strongly as the components which are to be desorbed. If the displacement fluid is adsorbed too strongly then there may be subsequent difficulties in removing it from the adsorbent. The mechanism for desorption of the original adsorbate involves 2 aspects: (1) partial pressure (or concentration) of original adsorbate in the gas phase surrounding the adsorbent is reduced (2) there is competitive adsorption for the displacement fluid. The displacement fluid is present on the adsorbent and thus will contaminate the product. One advantage of the displacement fluid method of regeneration is that the net heat generated or consumed in the adsorbent will be close to zero because the heat of adsorption of the displacement fluid is likely to be close to that of the original adsorbate. Thus the temperature of the adsorbent should remain more or less constant throughout the cycle.

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With neither pressure nor temperature changes from adsorption to desorption, regeneration by displacement purge depend solely on the ability of the displacement fluid to cleanse the bed in readiness for the next adsorption step. A typical Displacement Purge Adsorption (DPA) process is shown in the Figure below. PICTORIAL EXPLAINATION A is the more strongly adsorbed component in the binary feed mixture of (A and B) while D is the displacement purge gas. The feed mixture of (A and B) is passed through Bed 1 acting as the adsorber, which is preloaded with D from the previous cycle (when Bed 1 was the regenerator). A is adsorbed and the product of a mixture of (B and D) emerges from the top of the column. (B and D) are easily separated by distillation so that B is collected in a relatively pure state. The displacement gas D then enters Bed 2 acting as regenerator and from which emerges a mixture of (A and D). (A and D) can be separated without difficulty in another distillation column.

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In effect the original mixture of (A and B), which would have been difficult to separate by PSA or TSA, is separated by the "intervention" of another strongly adsorbed component D. The ease of separation of A from D, and B from D, in the additional distillation stages, is crucial in determining the economies of displacement purge cycle operation. Examples of commercial processes include the separation of linear paraffins from mixtures containing branched chain and cyclic isomers in the range of C10 - C18 hydrocarbons . DPA.. CONTD........ Other Adsorption Cycles Virtually all adsorption processes use changes in temperature, pressure, concentration of a competitvely adsorbing component to effect adsorption and desorption. But presumably any other variables which could effect changes in the shape of an adsorption isotherm could also be used. One such variable is the pH. The bonding between some adsorbents and adsorbates such as amino acids in water can be changed remarkably as the pH is changed from above the isoelectric point of the amino acid to below its isoelectric point. The isoelectric point is the pH at which the amino acid molecule has zero charge. The economic problem of using pH swing as a means to drive a cyclic process is the cost of the acid and base required to change the pH, as well as the cost of disposal of the salt by-product. Another means for changing the shape of the adsorption isotherm is the use of electric charge. Electrosorption involves adsorption when the adsorbent is subjected to one voltage and the desorption when the voltage is changed. Typically the voltage can be small, such as 1V or less. This process can only be accomplished in cases in which both the adsorbent and the feed stream are highly conductive. An example is EDA (ethylenediamine), which demonstrates different loading at different voltages.

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