- 1.1 The Rate of Reaction, -rA
- 1.2 The General Mole Balance Equation
- 1.3 Batch Reactors (BRs)
- 1.4 Continuous-Flow Reactors
- 1.5 Industrial Reactors
- Summary
- CRE Web Site Materials
- Questions and Problems

**1.2 The General Mole Balance Equation**

To perform a mole balance on any system, the system boundaries must first be specified. The volume enclosed by these boundaries is referred to as the *system volume.* We shall perform a mole balance on species *j* in a system volume, where species *j* represents the particular chemical species of interest, such as water or NaOH (Figure 1-3).

**Figure 1-3** Mole balance on species *j* in a system volume, *V*.

A mole balance on species *j* at any instant in time, *t*, yields the following equation:

In this equation, *N _{j}* represents the number of moles of species

*j*in the system at time

*t*. If all the system variables (e.g., temperature, catalytic activity, and concentration of the chemical species) are spatially uniform throughout the system volume, the rate of generation of species

*j, G*is just the product of the reaction volume,

_{j},*V*, and the rate of formation of species

*j, r*

_{j}.Now suppose that the rate of formation of species *j* for the reaction varies with position in the system volume. That is, it has a value *r*_{j1} at location 1, which is surrounded by a small volume, Δ*V*_{1}, within which the rate is uniform; similarly, the reaction rate has a value *r*_{j2} at location 2 and an associated volume, Δ*V*_{2}, and so on (Figure 1-4).

**Figure 1-4** Dividing up the system volume, V.

The rate of generation, Δ*G*_{j1}, in terms of *r*_{j1} and subvolume Δ*V*_{1}, is

Δ*G*_{j1} = *r*_{j1} Δ*V*_{1}

Similar expressions can be written for Δ*G*_{j2} and the other system subvolumes, Δ*V _{i}*. The total rate of generation within the system volume is the sum of all the rates of generation in each of the subvolumes. If the total system volume is divided into M subvolumes, the total rate of generation is

By taking the appropriate limits (i.e., let M → ∞ and Δ*V* → 0 ) and making use of the definition of an integral, we can rewrite the foregoing equation in the form

From this equation, we see that *r _{j}* will be an indirect function of position, since the properties of the reacting materials and reaction conditions (e.g., concentration, temperature) can have different values at different locations in the reactor volume.

We now replace *G _{j}* in Equation (1-3), i.e.,

by its integral form to yield a form of the general mole balance equation for any chemical species *j* that is entering, leaving, reacting, and/or accumulating within any system volume V.

From this general mole balance equation, we can develop the design equations for the various types of industrial reactors: batch, semibatch, and continuous-flow Upon evaluation of these equations, we can determine the time (batch) or reactor volume (continuous-flow) necessary to convert a specified amount of the reac-tants into products.