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| [[Image:pipe-PFR.svg|thumb|Schematic diagram of a plug flow reactor]]
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| The '''plug flow reactor model''' ('''PFR''', sometimes called '''continuous tubular reactor''', '''CTR''', or '''piston flow reactors''') is a model used to describe [[chemical reaction]]s in continuous, flowing systems of cylindrical geometry. The PFR model is used to predict the behavior of [[chemical reactor]]s of such design, so that key reactor variables, such as the dimensions of the reactor, can be estimated.
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| Fluid going through a PFR may be modeled as flowing through the reactor as a series of infinitely thin coherent "plugs", each with a uniform composition, traveling in the axial direction of the reactor, with each plug having a different composition from the ones before and after it. The key assumption is that as a plug flows through a PFR, the fluid is [[perfect mixing|perfectly mixed]] in the radial direction but not in the axial direction (forwards or backwards). Each plug of differential volume is considered as a separate entity, effectively an infinitesimally small [[continuous stirred tank reactor]], [[Limit (mathematics)|limiting]] to zero volume. As it flows down the tubular PFR, the [[residence time]] (<math>\tau</math>) of the plug is a function of its position in the reactor. In the ideal PFR, the residence time distribution is therefore a [[Dirac delta function]] with a value equal to <math>\tau</math>.
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| ==PFR modeling==
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| The PFR is governed by ordinary [[differential equation]]s, the solution for which can be calculated providing that appropriate [[Boundary value problem|boundary conditions]] are known........
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| The PFR model works well for many fluids: liquids, gases, and slurries. Although turbulent flow and axial diffusion cause a degree of mixing in the axial direction in real reactors, the PFR model is appropriate when these effects are sufficiently small that they can be ignored......
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| In the simplest case of a PFR model, several key assumptions must be made in order to simplify the problem, some of which are outlined below. Note that not all of these assumptions are necessary, however the removal of these assumptions does increase the complexity of the problem. The PFR model can be used to model multiple reactions as well as reactions involving changing temperatures, pressures and densities of the flow. Although these complications are ignored in what follows, they are often relevant to industrial processes.
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| Assumptions:
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| * [[plug flow]]
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| * [[steady-state (chemical engineering)|steady state]]
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| * constant [[density]] (reasonable for some liquids but a 20% error for polymerizations; valid for gases only if there is no pressure drop, no net change in the number of moles, nor any large temperature change)
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| * single [[chemical reaction|reaction]] occurring in the bulk of the fluid (homogeneously).
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| A material balance on the differential volume of a fluid element, or plug, on species ''i'' of axial length ''dx'' between ''x'' and ''x + dx'' gives:
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| :[accumulation] = [in] - [out] + [generation] - [consumption]
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| Accumulation is 0 under steady state; therefore, the above mass balance can be re-written as follows:
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| 1. <math> F_{i}(x) - F_{i}(x+dx) + A_t dx \nu_i r = 0 </math> .<ref name=Schmidt>{{cite book | last = Schmidt | first = Lanny D. | title = The Engineering of Chemical Reactions | publisher = Oxford University Press | year = 1998 | location = New York | isbn = 0-19-510588-5 }}</ref>
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| where:
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| * ''x'' is the reactor tube axial position, m
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| * ''dx'' the differential thickness of fluid plug
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| * the index ''i'' refers to the species ''i''
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| * ''F<sub>i</sub>(x)'' is the molar flow rate of species ''i'' at the position ''x'', mol/s
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| * ''D'' is the tube diameter, m
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| * ''A<sub>t</sub>'' is the tube transverse cross sectional area, m<sup>2</sup>
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| * ''ν'' is the [[Stoichiometry|stoichiometric coefficient]], dimensionless
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| * ''r'' is the volumetric source/sink term (the reaction rate), mol/m<sup>3</sup>s.
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| The flow linear velocity, ''u'' (m/s) and the concentration of species ''i'', C<sub>i</sub> (mol/m<sup>3</sup>) can be introduced as:
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| :<math> u = \frac{\dot{v}}{A_t} = \frac{4 \dot{v}}{\pi D^2} </math> and <math> F_i = A_t u C_i \, </math>
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| On application of the above to Equation 1, the mass balance on ''i'' becomes:
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| 2. <math> A_t u [C_i(x) - C_i(x + dx)] + A_t dx \nu_i r = 0 \, </math>.<ref name=Schmidt/>
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| When like terms are cancelled and the limit ''dx'' → 0 is applied to Equation 2 the mass balance on species ''i'' becomes
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| 3. <math> u \frac{dC_i}{dx} = \nu_i r </math>,<ref name=Schmidt/>
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| The temperature dependence of the reaction rate, ''r'', can be estimated using the [[Arrhenius equation]]. Generally, as the temperature increases so does the rate at which the reaction occurs. Residence time, <math>\tau</math>, is the average amount of time a discrete quantity of reagent spends inside the tank.
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| Assume:
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| * [[isothermal]] conditions, or constant temperature (k is constant)
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| * single, irreversible [[chemical reaction|reaction]] (ν<sub>A</sub> = -1)
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| * [[rate law|first-order reaction]] (r = k C<sub>A</sub>)
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| After integration of Equation 3 using the above assumptions, solving for ''C<sub>A</sub>(x)'' we get an explicit equation for the concentration of species ''A'' as a function of position:
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| 4. <math> C_A(x) = C_{A0} e^{-k \tau} \, </math>,
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| where ''C<sub>A0</sub>'' is the concentration of species ''A'' at the inlet to the reactor, appearing from the integration boundary condition.
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| ==Operation and uses==
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| PFRs are used to model the chemical transformation of compounds as they are transported in systems resembling "pipes". The "pipe" can represent a variety of engineered or natural conduits through which liquids or gases flow. (e.g. rivers, pipelines, regions between two mountains, etc.)
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| An ideal plug flow reactor has a fixed residence time: Any fluid (plug) that enters the reactor at time <math>t</math> will exit the reactor at time <math>t+\tau</math>, where <math>\tau</math> is the residence time of the reactor. The residence time distribution function is therefore a [[dirac delta function]] at <math>\tau</math>. A real plug flow reactor has a residence time distribution that is a narrow pulse around the [[arithmetic mean|mean]] residence time distribution.
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| A typical plug flow reactor could be a tube [[packed bed|packed]] with some solid material (frequently a [[catalyst]]). Typically these types of reactors are called packed bed reactors or PBR's. Sometimes the tube will be a tube in a shell and tube [[heat exchanger]].
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| == Advantages and disadvantages ==
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| {{procon|date=November 2012}}
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| CSTRs (Continuous Stirred Tank Reactor) and PFRs have fundamentally different equations, so the kinetics of the reaction being undertaken will to some extent determine which system should be used. However there are a few general comments that can be made with regards to PFRs compared to other reactor types.
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| Plug flow reactors have a high volumetric unit conversion, run for long periods of time without maintenance, and the heat transfer rate can be optimized by using more, thinner tubes or fewer, thicker tubes in parallel. Disadvantages of plug flow reactors are that temperatures are hard to control and can result in undesirable temperature gradients. PFR maintenance is also more expensive than CSTR maintenance.<ref>[http://www.engin.umich.edu/~cre/asyLearn/bits/pfrfinal/index.htm University of Michigan website: Plug Flow Reactors]</ref>
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| Through a recycle loop a PFR is able to approximate a CSTR in operation. This occurs due to a decrease in the concentration change due to the smaller fraction of the flow determined by the feed; in the limiting case of total recycling, infinite recycle ratio, the PFR perfectly mimics a CSTR.
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| ==Applications==
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| Plug flow reactors are used for some of the following applications:
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| *Large-scale reactions
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| *Fast reactions
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| *Homogeneous or heterogeneous reactions
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| *Continuous production
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| *High-temperature reactions
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| ==See also==
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| *[[chemical reactors]]
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| *[[chemical reactions]]
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| *[[microreactor]]
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| *[[oscillatory baffled reactor]]
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| *[[laminar flow reactor]]
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| ==Reference and sources==
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| <references/>
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| [[Category:Chemical reactors]]
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Andrew Simcox is the name his mothers and fathers gave him and he totally enjoys this title. For a while I've been in Alaska but I will have to move in a year or two. Invoicing is my occupation. To play lacross is the thing I love most of all.
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