The continuous stirred-tank reactor (CSTR), also known as vat- or backmix reactor, mixed flow reactor (MFR), or a continuous-flow stirred-tank reactor (CFSTR), is a common model for a chemical reactor in chemical engineering and environmental engineering. A CSTR often refers to a model used to estimate the key unit operation variables when using a continuous agitated-tank reactor to reach a specified output. The mathematical model works for all fluids: liquids, gases, and slurries.

The behavior of a CSTR is often approximated or modeled by that of an ideal CSTR, which assumes perfect mixing. In a perfectly mixed reactor, reagent is instantaneously and uniformly mixed throughout the reactor upon entry. Consequently, the output composition is identical to composition of the material inside the reactor, which is a function of residence time and reaction rate. The CSTR is the ideal limit of complete mixing in reactor design, which is the complete opposite of a plug flow reactor (PFR). In practice, no reactors behave ideally but instead fall somewhere in between the mixing limits of an ideal CSTR and PFR.

Ideal CSTR

Modeling

A continuous fluid flow containing non-conservative chemical reactant A enters an ideal CSTR of volume V.

Assumptions:

• perfect or ideal mixing
• steady state ${\displaystyle {\Bigl (}{\frac {dN_{A}}{dt}}=0{\Bigr )}}$, where N_A is the number of moles of species A
• closed boundaries
• constant fluid density (valid for most liquids; valid for gases only if there is no net change in the number of moles or drastic temperature change)
• n^th-order reaction (r = kC_Aⁿ), where k is the reaction rate constant, C_A is the concentration of species A, and n is the order of the reaction
• isothermal conditions, or constant temperature (k is constant)
• single, irreversible reaction (ν_A = −1)
• All reactant A is converted to products via chemical reaction
• N_A = C_A V

Integral mass balance on number of moles N_A of species A in a reactor of volume V:${\displaystyle 1.=-+}$

${\displaystyle 2.{\frac {dN_{A}}{dt}}=F_{Ao}-F_{A}+V\nu _{A}r_{A}}$^[1]

where,

• F_Ao is the molar flow rate inlet of species A
• F_A is the molar flow rate outlet of species A
• v_A is the stoichiometric coefficient
• r_A is the reaction rate

Applying the assumptions of steady state and ν_A = −1, Equation 2 simplifies to:

${\displaystyle 3.\ 0=F_{Ao}-F_{A}-Vr_{A}}$

The molar flow rates of species A can then be rewritten in terms of the concentration of A and the fluid flow rate (Q):

${\displaystyle 4.\ 0=QC_{Ao}-QC_{A}-Vr_{A}}$^[2]

Equation 4 can then be rearranged to isolate r_A and simplified:

${\displaystyle 5.\ r_{A}={\frac {Q}{V}}(C_{Ao}-C_{A})}$^[2]

${\displaystyle 6.\ r_{A}={\frac {1}{\tau }}(C_{Ao}-C_{A})}$

where,

• ${\displaystyle \tau }$ is the theoretical residence time (${\displaystyle \tau ={\tfrac {V}{Q}}}$)
• C_Ao is the inlet concentration of species A
• C_A is the reactor/outlet concentration of species A

Residence time is the total amount of time a discrete quantity of reagent spends inside the reactor. For an ideal reactor, the theoretical residence time, ${\displaystyle \tau }$, is always equal to the reactor volume divided by the fluid flow rate.^[2] See the next section for a more in-depth discussion on the residence time distribution of a CSTR.

Depending on the order of the reaction, the reaction rate, r_A, is generally dependent on the concentration of species A in the reactor and the rate constant. A key assumption when modeling a CSTR is that any reactant in the fluid is perfectly (i.e. uniformly) mixed in the reactor, implying that the concentration within the reactor is the same in the outlet stream.^[3] The rate constant can be determined using a known empirical reaction rate that is adjusted for temperature using the Arrhenius temperature dependence.^[2] Generally, as the temperature increases so does the rate at which the reaction occurs.

Equation 6 can be solved by integration after substituting the proper rate expression. The table below summarizes the outlet concentration of species A for an ideal CSTR. The values of the outlet concentration and residence time are major design criteria in the design of CSTRs for industrial applications.

Outlet Concentration for an Ideal CSTR

Reaction Order	CA
n=0	${\displaystyle C_{A}={C_{Ao}}-{k\tau }}$
n=1	${\displaystyle C_{A}={\frac {C_{Ao}}{1+k\tau }}}$[1]
n=2	${\displaystyle C_{A}={\frac {-1+{\sqrt {1+4k\tau C_{Ao}}}}{2k\tau }}}$
Other n	Numerical solution required

Residence time distribution

An ideal CSTR will exhibit well-defined flow behavior that can be characterized by the reactor's residence time distribution, or exit age distribution.^[4] Not all fluid particles will spend the same amount of time within the reactor. The exit age distribution (E(t)) defines the probability that a given fluid particle will spend time t in the reactor. Similarly, the cumulative age distribution (F(t)) gives the probability that a given fluid particle has an exit age less than time t.^[3] One of the key takeaways from the exit age distribution is that a very small number of fluid particles will never exit the CSTR.^[5] Depending on the application of the reactor, this may either be an asset or a drawback.

Non-ideal CSTR

While the ideal CSTR model is useful for predicting the fate of constituents during a chemical or biological process, CSTRs rarely exhibit ideal behavior in reality.^[2] More commonly, the reactor hydraulics do not behave ideally or the system conditions do not obey the initial assumptions. Perfect mixing is a theoretical concept that is not achievable in practice.^[6] For engineering purposes, however, if the residence time is 5–10 times the mixing time, the perfect mixing assumption generally holds true.

Non-ideal hydraulic behavior is commonly classified by either dead space or short-circuiting. These phenomena occur when some fluid spends less time in the reactor than the theoretical residence time, ${\displaystyle \tau }$. The presence of corners or baffles in a reactor often results in some dead space where the fluid is poorly mixed.^[6] Similarly, a jet of fluid in the reactor can cause short-circuiting, in which a portion of the flow exits the reactor much quicker than the bulk fluid. If dead space or short-circuiting occur in a CSTR, the relevant chemical or biological reactions may not finish before the fluid exits the reactor.^[2] Any deviation from ideal flow will result in a residence time distribution different from the ideal distribution, as seen at right.

Modeling non-ideal flow

Although ideal flow reactors are seldom found in practice, they are useful tools for modeling non-ideal flow reactors. Any flow regime can be achieved by modeling a reactor as a combination of ideal CSTRs and plug flow reactors (PFRs) either in series or in parallel.^[6] For examples, an infinite series of ideal CSTRs is hydraulically equivalent to an ideal PFR.^[2] Reactor models combining a number of CSTRs in series are often termed tanks-in-series (TIS) models.^[7]

To model systems that do not obey the assumptions of constant temperature and a single reaction, additional dependent variables must be considered. If the system is considered to be in unsteady-state, a differential equation or a system of coupled differential equations must be solved. Deviations of the CSTR behavior can be considered by the dispersion model. CSTRs are known to be one of the systems which exhibit complex behavior such as steady-state multiplicity, limit cycles, and chaos.

Cascades of CSTRs

Cascades of CSTRs, also known as a series of CSTRs, are used to decrease the volume of a system.^[8]

Minimizing Volume

As seen in the graph with one CSTR, where the inverse rate is plotted as a function of fractional conversion, the area in the box is equal to ${\displaystyle {\frac {V}{F_{Ao}}}}$ where V is the total reactor volume and ${\displaystyle F_{Ao}}$ is the molar flow rate of the feed. When the same process is applied to a cascade of CSTRs as seen in the graph with three CSTRs, the volume of each reactor is calculated from each inlet and outlet fractional conversion, therefore resulting in a decrease in total reactor volume. Optimum size is achieved when the area above the rectangles from the CSTRs in series that was previously covered by a single CSTR is maximized. For a first order reaction with two CSTRs, equal volumes should be used. As the number of ideal CSTRs (n) approaches infinity, the total reactor volume approaches that of an ideal PFR for the same reaction and fractional conversion.

Ideal Cascade of CSTRs

From the design equation of a single CSTR where ${\displaystyle \tau ={\frac {C_{Ao}-C_{A}}{-r_{A}}}}$, we can determine that for a single CSTR in series that ${\displaystyle {\mathrm{\tau <!--\; \tau \; -->}}_i=\frac{{}_{}}{}}$Zdroj:https://en.wikipedia.org?pojem=Continuous_stirred-tank_reactor
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