13. Distribution of Residence Times for Chemical Reactors^*

Topics

1. Residence Time Distribution
2. RTD for Ideal Reactors
3. RTD to Diagnose Faulty Operation
4. Models to Calculate Exit Concentrations and Conversions
   1. Segregation Model
      1. Segregation Model Applied to an Ideal PFR
      2. Segregation Model Applied to an LFR
      3. Segregation Model Applied to a CSTR
      4. Mean Concentration for Multiple Reactions
   2. Maximum Mixedness Model
5. Comparing X_MM and X_seg
6. RTD and Multiple Reactions

We shall use the RTD to characterize existing (i.e. real) reactors and then use it to predict exit conversions and concentrations when reactions occur in these reactors.

Inject a tracer and measure exit concentration, C_T(t). 
 

From the exit tracer concentration we can determine the following information:

A.  RTD (Residence Time Distribution)  Function (E(t)) 

= Fraction of molecules exiting the reactor that have spent a time between (t) and (t + dt) in the reactor.

B.  The Cumulative Distribution Function F(t)

= Fraction of molecules exiting the reactor that have spent a time t or less in the reactor.

= Fraction of molecules that have spent a time t or greater in the reactor.

C. Definitions

1. Mean Residence Time

Mean Residence Time

Residence Time Distribution Analysis using COMSOL Multiphysics

2. Variance

3. Space Time - For no dispersion/diffusion and v = v₀, the space time equals the mean residence time.

4. Internal Age Distribution, = Fraction of molecules inside the reactor that have been inside the reactor between a timeand.

5. Life Expectancy = Fraction of molecules inside the reactor with agethat are expected to leave the reactor in a timeto.

From our experimental data of the exit tracer concentration from pulse trace test

We can obtain                                                                           

-> ->  -> ->

Calculate E(t), t and s²

Using the E(t) curves

for Ideal Reactors
PFR- Inject a pulse at t=0
	Dirac Delta Function

CSTR
Laminar (LFR)

Drawing the F(theta) curves for the above ideal reactors

Matching Reactors with Tracer Step Inputs

Matching Reactor Models with E(t)

Experimentally injecting and measureing the tracer in a laminar flow reactor can be a difficult task, if not a nightmare. For example, if one uses tracer chemicals that are photo-activated as they enter the reactor, the analysis and interpretation of E(t) from the data becomes much more involved.

Diagnostics and Troubleshooting

The CSTR

	Concentration
	RTD Function
	Cumulative Function
	Space Time

a. Perfect Operation

b. Passing (BP)

c. Dead Volume

A summary for ideal CSTR mixing volume is shown in Figure 13-14

Tubular Reactor

A similar analysis to that for a CSTR can be carried out on a tubular reactor.

a. Perfect Operation of PFR (P)

b. PFR with Channeling (Bypassing, BP)

c. PFR with Dead Volume (DV)

A summary for PRF is shown in Figure 13-18

In addition to its use in diagnosis, the RTD can be used to predict conversion in existing reactors when a new reaction is tried in an old reactor. However, the RTD is not unique for a given system, and we need to develop models for the RTD to predict conversion.

Medicinal Uses of RTD

If using mathematical software to apply the models described below, you may need to fit C(t) and E(t) to a polynomial. The procedure for fitting C(t) and E(t) to a polynomial is identical to the techniques use to fitting concentration as a function of time described in Chapter 5.

 Polymath regression analysis tutorial

Use combinations of ideal reactors to model real reactors that could also include: Zero parameter models

Models the real reactor as a number of small batch reactors, each spending a different time in the reactor.  All molecules that spend the same length of time in the reactor (i.e., that are of the same age) remain together in the same globule (i.e., batch reactor). Mixing of the different age groups occurs at the last possible moment at the reactor exit.

Mixing of the globules of different ages occurs here.

Little batch reactors (globules) inside a CSTR.

X₃>X₂>X₁

Mixing occurs at the latest possible moment.Each little batch reactor (globule) exiting the real reactor at different times will have a different conversion. (X₁,X₂,X₃...)
 
 

        But, the mean conversion for the segregation model is

Lets apply the segregation model to an ideal PFR and see if we get the same result for conversion as we did in Chapter 4.

Solve for X(t) for a first order reaction in a batch reactor.

For the batch reactor the conversion-time relationship is

Calculate the mean conversion

which is the same conversion one finds from a mole balance (Chapter 4)

Further Explanation of Mean Conversion in Segregation Model

4A.2 Segregation Model Applied to an LFR

For a Laminar flow reactor the RTD function is

The mean conversion is

The last integral is the exponential integral and can be evaluated from tabulated values. Fortunately, Hilder developed an approximate formula (=Da).

Hilder, M.H. Trans. IchemE 59 p143(1979)

For large values of the Damkohler number then there is complete conversion along the streamlines off the center streamline so that the conversion is determined along the pipe axis.

4A.3 Segregation Model Applied to a CSTR

4A.4 Mean Concentration for Multiple Reactions

Solutions Using Software Packages

For multiple reactions use an ODE solver to couple the mole balance equations, dC_i/dt=r_i, with the segregation model equations: d/dt=C_i(t)*E(t), where C _i is the concentration of i in the batch reactor at time t andis the concentration of i after mixing the batch reactors at the exit.

Batch, PFR, CSTR, Segregation

4B Maximum Mixedness Model

Mixing occurs at the earliest possible moment.

Note E(l)=E(t)                 

E(l)dl =Fraction of molecules that have a life expectancy between l+dl and  l.

Modeling maximum mixedness as a plug flow reactor with side entrances.

Dividing byDland taking the limit asDlgoes to zero. Substitute,

                                          Differentiating the first term and recalling we obtain.

We need to integrate backwards from(the entrance) to= 0 (the exit). In real systems we have some maximum value of(say= 200 minutes) rather thanminutes. Consequently we integrate backward from= 200. However, because most ODE packages will not integrate backwards, we have to use the transfer

z = T -to integrate forward

Thus 

In terms of conversion,

Maximum Mixedness Model

Calculate X_mm and X_seg

For example, if the rate law is a power law model

From the product [(n)(n-1)], we see

For multiple reactions use an ODE solver to couple the mole balance equations, dC_i/dt=r_i (where r_i is the net rate of reaction), with the segregation model equations: dC_i/dt=C_i(t)*E(t) as previously shown.  For maximum mixedness:

To obtain solutions with an ODE solver, first fit E(t) to a polynomial or several polynomials. Then let z = T -where T is the largest time in which E(t) is recorded. Proceed to solve the resulting equations.

Object Assessment of Chapter 13

  ^* All chapter references are for the 4th Edition of the text Elements of Chemical Reaction Engineering .

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