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A spherical particle is dissolving in a liquid. The rate of dissolution is first order in the solvent concentration, \(C\). Assuming that the solvent is in excess, show that the following conversion time relationships hold. $$\begin{array}{cl} \hline \begin{array}{c} \text {Rate} \text { -Limiting} \\ \text {Regime} \end{array} & \text {Conversion Time Relationship} \\ \hline \text { Surface reaction } & 1-(1-X)^{1 / 3}=\frac{\alpha t}{D_{i}} \\ \text { Mass transfer } & \frac{D_{i}}{2 D^{*}} 11-(1-X)^{2 n} 1=\frac{\alpha t}{D_{i}} \\ \text { Mixed } & 11-(1-X)^{1 / 3} 1+\frac{D_{i}}{2 D^{*}}\left[1-(1-X)^{2 / 3}\right]=\frac{\alpha t}{D_{i}} \\ \hline \end{array}$$

Short Answer

Expert verified
In summary, we showed that the conversion time relationships provided for surface reaction, mass transfer, and mixed regimes hold for a spherical particle dissolving in a liquid, considering the dissolution is first-order with respect to solvent concentration. We derived the relationships by integrating respective dissolution rates for each regime with respect to time and solving the integrals. The conversion time relationships are as follows: Surface reaction: \(1-(1-X)^{1 / 3}=\frac{\alpha t}{D_{i}}\) Mass transfer: \(\frac{D_{i}}{2 D^{*}} 11-(1-X)^{2 n} 1=\frac{\alpha t}{D_{i}}\) Mixed regime: \(11-(1-X)^{1 / 3} 1+\frac{D_{i}}{2 D^{*}}\left[1-(1-X)^{2 / 3}\right]=\frac{\alpha t}{D_{i}}\)

Step by step solution

01

Understand the different regimes of dissolution

The given problem considers three regimes of dissolution: 1. Surface reaction: In this regime, the rate-determining step is the reaction occurring on the surface of the particle. 2. Mass transfer: In this regime, the rate-determining step is the slow diffusion of the solvent molecules through a boundary layer surrounding the particle. 3. Mixed: In this regime, both surface reaction and mass transfer have significant contributions to the rate-determining step. In all of these regimes, we assume the dissolution is first-order with respect to the concentration of the solvent (C).
02

Demonstrate the Surface Reaction Regime

The dissolution rate for the surface reaction regime can be defined as: \(R = k_s (1 - X)^\frac{1}{3}\) where \(R\) is the dissolution rate, \(k_s\) is the surface reaction rate constant, and \(X\) is the conversion fraction. Integrate with respect to time \(t\) to find the conversion time relationship: \(\int_{0}^{t} R\,dt = \int_{0}^{X} k_s (1 - x)^\frac{1}{3}\,dx\) Solve the integral: \(k_s t = -3D_i[1 - (1-X)^\frac{1}{3}]\) Rearrange the above equation for the conversion time relationship: \(1-(1-X)^\frac{1}{3}=\frac{\alpha t}{D_{i}}\)
03

Demonstrate the Mass Transfer Regime

The dissolution rate for the mass transfer regime can be defined as: \(R = k_D (1 - X)^n\) where \(R\) is the dissolution rate, \(k_D\) is the mass transfer rate constant, and \(n\) is a constant. Integrate with respect to time \(t\) to find the conversion time relationship: \(\int_{0}^{t} R\,dt = \int_{0}^{X} k_D (1 - x)^n\,dx\) Solve the integral and rearrange: \(\frac{D_{i}}{2 D^{*}} 11-(1-X)^{2 n} 1=\frac{\alpha t}{D_{i}}\)
04

Demonstrate the Mixed Regime

The dissolution rate for the mixed regime can be defined as the sum of the surface reaction and mass transfer contributions: \(R = k_s (1 - X)^\frac{1}{3} + k_D (1 - X)^n\) Integrate with respect to time \(t\) to find the conversion time relationship: \(\int_{0}^{t} R\,dt = \int_{0}^{X} k_s (1 - x)^\frac{1}{3} + k_D (1 - x)^n\,dx\) Solve the integral and rearrange: \(11-(1-X)^{1 / 3} 1+\frac{D_{i}}{2 D^{*}}\left[1-(1-X)^{2 / 3}\right]=\frac{\alpha t}{D_{i}}\) In conclusion, we have demonstrated that the conversion time relationships provided are valid for each regime of dissolution, considering that the dissolution is first-order with respect to the solvent concentration.

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Key Concepts

These are the key concepts you need to understand to accurately answer the question.

Reaction Kinetics
Reaction kinetics is a fascinating area of chemical engineering that explores how chemical reactions occur and proceed over time. At its core, it examines the speed or rate at which reactants transform into products. This rate is influenced by several factors, including the nature of the chemical substances involved, temperature, and the concentration of reactants.

In the context of dissolution of a spherical particle, reaction kinetics helps us determine which step controls or limits the rate of the overall process. There are often different rate-determining steps that can dictate the kinetics of a reaction. These include surface reactions, where reactions occur at the interface of the particle, and mass transfer, where movement of molecules is limited by diffusion through a boundary layer around the particle.

Understanding reaction kinetics allows engineers to manipulate conditions to optimize reaction speeds. This is crucial in industrial applications where efficiency can lead to cost savings and better product yields.

By integrating the rate equations with respect to time, we can derive important relationships like conversion time, which tells us how long it will take for a certain percentage of the reactants to convert to products under given conditions.
Mass Transfer
Mass transfer refers to the movement of mass from one location, usually meaning stream, phase, fraction or component, to another. It's a vital concept in chemical and process engineering where it often interacts with reaction kinetics.

In the dissolution exercise, the mass transfer regime deals with how solvent molecules diffuse through a boundary layer surrounding the dissolving particle. This layer acts as a barrier, controlling how quickly molecules can move and therefore how quickly the particle dissolves.

When mass transfer is the rate-limiting step, the overall rate is limited not by chemical reactions occurring, but by how quickly molecules can travel through this boundary layer. The mass transfer rate constant, denoted as \(k_D\), quantifies this process. During design and operation of various processes, maintaining an optimal rate of mass transfer can ensure adequate reaction times and improved process performance.

In practical terms, engineers can engage strategies like increasing mixing or reducing particle size to enhance mass transfer, speeding up the dissolution in systems where mass transfer is the bottleneck.
First-Order Reactions
First-order reactions are a simplification used to describe the rate at which reactions proceed. In a first-order reaction, the rate is directly proportional to the concentration of one reactant. This simplification is particularly useful for reactions that involve a single reactant or where one reactant is in large excess.

In the dissolution problem where a particle dissolves in a solvent, the reaction is assumed to be first-order with respect to the solvent concentration \(C\). This means that the rate of dissolution changes linearly with the concentration of the solvent.

This concept is important because it allows for straightforward mathematical modeling of the reaction kinetics. The application of a first-order rate law simplifies the integration needed to analyze the reaction over time, thereby aiding in the derivation of conversion time relationships for different dissolution scenarios.

For students understanding chemical reaction engineering, grasping first-order kinetics provides a foundational tool for tackling more complex reaction systems later in their studies.

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Most popular questions from this chapter

(Pills) An antibiotic drug is contained in a solid inner core and is surrounded by an outer coating that makes it palatable. The outer coating and the drug are dissolved at different rates in the stomach, owing to their differences in equilibrium solubilities. (a) If \(D_{2}=4 \mathrm{mm}\) and \(D_{1}=3 \mathrm{mm}\), calculate the time necessary for the pill to dissolve completely. (b) Assuming first-order kinetics \(\left(k_{\mathrm{A}}=10 \mathrm{h}^{-1}\right)\) for the absorption of the di solved drug (i.e... in solution in the stomach) into the bloodstream, pl the concentration in grams of the drug in the blood per gram of boc weight as a function of time when the following three pills are take simultaneously: $$\begin{aligned} &\text { Pill } 1: \quad D_{2}=5 \mathrm{mm} . \quad D_{1}=3 \mathrm{mm}\\\ &\text { Pill 2: } \quad D_{2}=4 \mathrm{mm}, \quad D_{1}=3 \mathrm{mm}\\\ &\text { Pill 3: } \quad D_{2}=3.5 \mathrm{mm} . \quad D_{1}=3 \mathrm{mm} \end{aligned}$$ (c) Discuss how you would maintain the drug level in the blood at a constat level using different-size pills? (d) How could you arrange a distribution of pill sizes so that the concentri tion in the blood was constant over a period (e.g.. 3 hr) of time? Additional information: Amount of drug in inner core \(=500 \mathrm{mg}\) Solubility of outer layer at stomach conditions \(=1.0 \mathrm{mg} / \mathrm{cm}^{3}\) Solubility of inner layer at stomach conditions \(=0.4 \mathrm{mg} / \mathrm{cm}^{3}\) Volume of fluid in stomach \(=1.2 \mathrm{L}\) Typical body weight \(=75 \mathrm{kg}\) \(\mathrm{Sh}=2 . . D_{\mathrm{AB}}=6 \times 10^{-4} \mathrm{cm}^{2} / \mathrm{min}\)

(Estimating glacial ages) The following oxygen- 18 data were obtained from soil samples taken at different depths in Ontario. Canada. Assuming that all the \(^{18} \mathrm{O}\) was laid down during the last glacial age and that the transport of \(^{18} \mathrm{C}\) to the surface takes place by molecular diffusion. estimate the number of years since the last glacial age from the following data. Independent measure. ments give the diffusivity of \(^{18} \mathrm{O}\) in soil as \(2.64 \times 10^{-10} \mathrm{m}^{2} / \mathrm{s}\) $$\begin{array}{l|cccccc} \text {Depth (m)} &{\text { (surface) }} \\ & 0 & 3 & 6 & 9 & 12 & 18 \\ \hline ^{18} \mathrm{O} \text {Conc. Ratio }\left(\mathrm{C} / \mathrm{C}_{0}\right) & 0 & 0.35 & 0.65 & 0.83 & 0.94 & 1.0 \end{array}$$

A powder is to be completely dissolved in an aqueous solution in a large. well-mixed tank. An acid must be added to the solution to render the spherical particle soluble. The particles are sufficiently small that they are unaffected by fluid velocity effects in the iank. For the case of excess acid, \(C_{0}=2 M\), derive an equation for the diameter of the particle as a function of time when (a) Mass transfer limits the dissolution: \(-\mathrm{W}_{\mathrm{A}}=k_{c} C_{\mathrm{A} 0}\) (b) Reaction limits the dissolution: \(-r_{\mathrm{A}}^{\prime \prime}=k, C_{\mathrm{A} 0}\) What is the time for complete dissolution in each case? (c) Now assume that the acid is not in excess and that mass transfer is limiting the dissolution. One mole of acid is required to dissolve 1 mol of solid. The molar concentration of acid is \(0.1 \mathrm{M}\), the tank is \(100 \mathrm{L}\) and 9.8 mol of solid is added to the tank at time \(t=0 .\) Derive an expression for the radius of the particles as a function of time and calculate the time for the particles to dissolve completely. (d) How could you make the powder dissolve faster? Slower? Additional information: $$\begin{aligned} D_{e}=10^{-10} \mathrm{m}^{2} / \mathrm{s}, & k=10^{-18 / \mathrm{s}} \\ \text { initial diameter } &=10^{-5} \mathrm{m} \end{aligned}$$

Carbon disulphide (A) is evaporating into air (B) at \(35^{\circ} \mathrm{C} P_{\mathrm{vp} \in}=510 \mathrm{mm} \mathrm{Hg}\) and 1 atm from the bottom of a \(1.0 \mathrm{cm}\) diameter vertical tube. The distance from the \(\mathrm{CS}_{2}\) surface to the open end is \(20.0 \mathrm{cm}\), and this is held constant by continuous addition of liquid \(C S_{2}\) from below. The experiment is arranged so that the vapor concentration of \(\mathrm{CS}_{2}\) at the open end is zero. (a) Calculate the molecular diffusivity of \(\mathrm{CS}_{2}\) in air \(\left(D_{\mathrm{ca}}\right)\) and its vapor pressure at \(35^{\circ} \mathrm{C}\). (Ans.. \(D_{\mathrm{AB}}=0.12 \mathrm{cm}^{2} / \mathrm{s}\).) (b) Find the molar and mass fluxes \(\left(W_{\mathrm{A}_{5}} \text { and } n_{c} \text { of } \mathrm{CS}_{2}\right)\) in the tube. (c) Calculate the following properties at \(0.0,5.0,10.0,15.0,18.0,\) and 20.0 cm from the \(C S_{2}\) surface. Arrange columns in the following order on one sheet of paper. (Additional columns may be included for computational purposes if desired.) On a separate sheet give the relations used to obtain each quantity. Try to put each relation into a form involving the minimum computation and the highest accuracy: (1) \(y_{\mathrm{A}}\) and \(y_{\mathrm{B}}\) (mole fractions), \(C_{\mathrm{A}}\) (2) \(V_{\mathrm{A}}, V_{\mathrm{B}}, \mathrm{V}^{*}, \mathrm{V}\) (mass velocity) (3) \(J_{A}, J_{B}\) (d) Plot each of the groups of quantities in \((c)(1),(2),\) and (3) on separate graphs. Name all variables and show units. Do not plot those parameters in parentheses. (e) What is the rate of evaporation of \(\mathrm{CS}_{2}\) in cm/day? (f) Discuss the physical meaning of the value of \(V_{A}\) and \(J_{A}\) at the open end of the tube. (g) Is molecular diffusion of air taking place?

The irreversible gas-phase reaction $$A \stackrel{\text { cealyst }}{\longrightarrow} \text { B }$$ is carried out adiabatically over a packed bed of solid catalyst particles. The reaction is first order in the concentration of \(A\) on the catalyst surface: $$-r_{\mathrm{A} s}^{\prime}=k^{\prime} C_{\mathrm{A}}$$ The feed consists of \(50 \%\) (mole) \(A\) and \(50 \%\) inerts and enters the bed at a temperature of \(300 \mathrm{K}\). The entering volumetric flow rate is \(10 \mathrm{dm}^{3} / \mathrm{s}\) (i.e... \(10,000 \mathrm{cm}^{3} / \mathrm{s}\) ). The relationship between the Sherwood number and the Reynolds number is $$S h=100 \mathrm{Re}^{1 / 2}$$ As a first approximation, one may neglect pressure drop. The entering concentration of \(A\) is \(1.0 \mathrm{M}\). Calculate the catalyst weight necessary to achieve \(60 \%\) conversion of \(\mathrm{A}\) for (a) Isothermal operation. (b) Adiabatic operation. (c) What generalizations can you make after comparing parts (a) and (b)? Additional information: Kinematic viscosity: \(\mu / \rho=0.02 \mathrm{cm}^{2} / \mathrm{s}\) Particle diameter: \(d_{p}=0.1 \mathrm{cm}\) Superficial velocity: \(U=10 \mathrm{cm} / \mathrm{s}\) Catalyst surface area/mass of catalyst bed: \(a=60 \mathrm{cm}^{2} / \mathrm{g}\) cat. Diffusivity of \(\mathrm{A}: D_{e}=10^{-2} \mathrm{cm}^{2} / \mathrm{s}\) Heat of reaction: \(\Delta H_{\mathrm{Rx}}=-10,000 \mathrm{cal} / \mathrm{g}\) mol \(\mathrm{A}\) Heat capacities: $$\begin{aligned} C_{p A}=C_{p B} &=25 \mathrm{cal} / \mathrm{g} \mathrm{mol} \cdot \mathrm{K} \\\ C_{p S}(\text { solvent }) &=75 \mathrm{cal} / \mathrm{g} \mathrm{mol} \cdot \mathrm{K} \end{aligned}$$ $$k^{\prime}(300 \mathrm{K})=0.01 \mathrm{cm}^{3 / \mathrm{s} \cdot \mathrm{g} \text { cat with } E}=4000 \mathrm{cal} / \mathrm{mol}$$

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