Batch reactor by sanmelody


									Batch reactor

The Batch reactor is the generic term for a type of vessel widely used in the process industries. Its name is something of a misnomer
since vessels of this type are used for a variety of process operations such as solids dissolution, product mixing, chemical reactions, batch
distillation, crystallization, liquid/liquid extraction and polymerization. In some cases, they are not referred to as reactors but have a name
which reflects the role they perform (such as crystallizer, or bio reactor).

A typical batch reactor consists of a tank with an agitator and integral heating/cooling system. These vessels may vary in size from less
than 1 litre to more than 15,000 litres. They are usually fabricated in steel, stainless steel, glass lined steel, glass or exotic alloy. Liquids
and solids are usually charged via connections in the top cover of the reactor. Vapors and gases also discharge through connections in the
top. Liquids are usually discharged out of the bottom.

The advantages of the batch reactor lie with its versatility. A single vessel can carry out a sequence of different operations without the
need to break containment. This is particularly useful when processing, toxic or highly potent compounds.


The usual agitator arrangement is a centrally mounted driveshaft with an overhead drive unit. Impeller blades are mounted on the shaft. A
wide variety of blade designs are used and typically the blades cover about two thirds of the diameter of the reactor. Where viscous
products are handled, anchor shaped paddles are often used which have a close clearance between the blade and the vessel walls.

Most batch reactors also use baffles. These are stationary blades which break up flow caused by the rotating agitator. These may be fixed
to the vessel cover or mounted on the side walls.

Despite significant improvements in agitator blade and baffle design, mixing in large batch reactors is ultimately constrained by the
amount of energy that can be applied. On large vessels, mixing energies of more than 5 Watts per litre can put an unacceptable burden on
the cooling system. High agitator loads can also create shaft stability problems. Where mixing is a critical parameter, the batch reactor is
not the ideal solution. Much higher mixing rates can be achieved by using smaller flowing systems with high speed agitators, ultrasonic
mixing or static mixers.

[edit] Heat cooling systems

Products within batch reactors usually liberate or absorb heat during processing. Even the action of stirring stored liquids generates heat.
In order to hold the reactor contents at the desired temperature, heat has to be added or removed by a cooling jacket or cooling pipe.
Heating/cooling coils or external jackets are used for heating and cooling batch reactors. Heat transfer fluid passes through the jacket or
coils to add or remove heat.

Within the chemical and pharmaceutical industries, external cooling jackets are generally preferred as they make the vessel easier to clean.
The performance of these jackets can be defined by 3 parameters:

        Response time to modify the jacket temperature
        Uniformity of jacket temperature
        Stability of jacket temperature

It can be argued that heat transfer coefficient is also an important parameter. It has to be recognized however that large batch reactors with
external cooling jackets have severe heat transfer constraints by virtue of design. It is difficult to achieve better than 100 Watts/litre even
with ideal heat transfer conditions. By contrast, continuous reactors can deliver cooling capacities in excess of 10,000 W/litre. For
processes with very high heat loads, there are better solutions than batch reactors.

Fast temperature control response and uniform jacket heating and cooling is particularly important for crystallization processes or
operations where the product or process is very temperature sensitive. There are several types of batch reactor cooling jackets:

[edit] Single external jacket

Batch reactor with single external cooling jacket

The single jacket design consists of an outer jacket which surrounds the vessel. Heat transfer fluid flows around the jacket and is injected
at high velocity via nozzles. The temperature in the jacket is regulated to control heating or cooling.

The single jacket is probably the oldest design of external cooling jacket. Despite being a tried and tested solution, it has some limitations.
On large vessels, it can take many minutes to adjust the temperature of the fluid in the cooling jacket. This results in sluggish temperature
[edit] Half coil jacket

Batch reactor with half coil jacket

The half coil jacket is made by welding a half pipe around the outside of the vessel to create a semi circular flow channel. The heat
transfer fluid passes through the channel in a plug flow fashion. A large reactor may use several coils to deliver the heat transfer fluid.
Like the single jacket, the temperature in the jacket is regulated to control heating or cooling

The plug flow characteristics of a half coil jacket permits faster displacement of the heat transfer fluid in the jacket (typically less than 60
seconds). This is desirable for good temperature control. It also has provides good distribution of heat transfer fluid which avoids the
problems of non uniform heating or cooling between the side walls and bottom dish. Like the single jacket design however the inlet heat
transfer fluid is also vulnerable to large oscillations (in response to the temperature control valve) in temperature.

[edit] Constant flux cooling jacket

Batch reactor with constant flux (Coflux) jacket

The constant flux cooling jacket is a relatively recent development. It is not a single jacket but has a series of 20 or more small jacket
elements. The temperature control valve operates by opening and closing these channels as required. By varying the heat transfer area in
this way, the process temperature can be regulated without altering the jacket temperature.

The constant flux jacket has very fast temperature control response (typically less than 5 seconds) due to the short length of the flow
channels and high velocity of the heat transfer fluid. Like the half coil jacket the heating/cooling flux is uniform. Because the jacket
operates at substantially constant temperature however the inlet temperature oscillations seen in other jackets are absent. An unusual
feature of this type jacket is that process heat can be measured very sensitively. This allows the user to monitor the rate of reaction for
detecting end points, controlling addition rates, controlling crystallization etc.

Chemical reactor

In chemical engineering, chemical reactors are vessels designed to contain chemical reactions. The design of a chemical reactor deals
with multiple aspects of chemical engineering. Chemical engineers design reactors to maximize net present value for the given reaction.
Designers ensure that the reaction proceeds with the highest efficiency towards the desired output product, producing the highest yield of
product while requiring the least amount of money to purchase and operate. Normal operating expenses include energy input, energy
removal, raw material costs, labor, etc. Energy changes can come in the form of heating or cooling, pumping to increase pressure,
frictional pressure loss (such as pressure drop across a 90 o elbow or an orifice plate), agitation, etc.


There are two main basic vessel types:

        a tank
        a pipe

Both types can be used as continuous reactors or batch reactors. Most commonly, reactors are run at steady-state, but can also be operated
in a transient state. When a reactor is first brought back into operation (after maintenance or inoperation) it would be considered to be in a
transient state, where key process variables change with time. Both types of reactors may also accommodate one or more solids (reagents,
catalyst, or inert materials), but the reagents and products are typically liquids and gases.

There are three main basic models used to estimate the most important process variables of different chemical reactors:

        batch reactor model (batch),
        continuous stirred-tank reactor model (CSTR), and
        plug flow reactor model (PFR).

Furthermore, catalytic reactors require separate treatment, whether they are batch, CST, or PF reactors, as the many assumptions of the
simpler models are not valid.

Key process variables include

        residence time (τ, lower case Greek tau)
        volume (V)
        temperature (T)
        pressure (P)
        concentrations of chemical species (C1, C2, C3, ... Cn)
        heat transfer coefficients (h, U)

[edit] Types

[edit] CSTR (Continuous Stirred-Tank Reactor)

In a CSTR, one or more fluid reagents are introduced into a tank reactor equipped with an impeller while the reactor effluent is removed.
The impeller stirs the reagents to ensure proper mixing. Simply dividing the volume of the tank by the average volumetric flow rate
through the tank gives the residence time, or the average amount of time a discrete quantity of reagent spends inside the tank. Using
chemical kinetics, the reaction's expected percent completion can be calculated. Some important aspects of the CSTR:

        At steady-state, the flow rate in must equal the mass flow rate out, otherwise the tank will overflow or go empty (transient state).
         While the reactor is in a transient state the model equation must be derived from the differential mass and energy balances.
        The reaction proceeds at the reaction rate associated with the final (output) concentration.
        Often, it is economically beneficial to operate several CSTRs in series. This allows, for example, the first CSTR to operate at a
         higher reagent concentration and therefore a higher reaction rate. In these cases, the sizes of the reactors may be varied in order to
         minimize the total capital investment required to implement the process.
        It can be seen that an infinite number of infinitely small CSTRs operating in series would be equivalent to a PFR.

The behavior of a CSTR is often approximated or modeled by that of a Continuous Ideally Stirred-Tank Reactor (CISTR). All calculations
performed with CISTRs assume perfect mixing. If the residence time is 5-10 times the mixing time, this approximation is valid for
engineering purposes. The CISTR model is often used to simplify engineering calculations and can be used to describe research reactors.
In practice it can only be approached, in particular in industrial size reactors.

[edit] PFR (Plug Flow Reactor)

In a PFR, one or more fluid reagents are pumped through a pipe or tube. The chemical reaction proceeds as the reagents travel through the
PFR. In this type of reactor, the changing reaction rate creates a gradient with respect to distance traversed; at the inlet to the PFR the rate
is very high, but as the concentrations of the reagents decrease and the concentration of the product(s) increases the reaction rate slows.
Some important aspects of the PFR:

        All calculations performed with PFRs assume no upstream or downstream mixing, as implied by the term "plug flow".
        Reagents may be introduced into the PFR at locations in the reactor other than the inlet. In this way, a higher efficiency may be
         obtained, or the size and cost of the PFR may be reduced.
        A PFR typically has a higher efficiency than a CSTR of the same volume. That is, given the same space-time, a reaction will
         proceed to a higher percentage completion in a PFR than in a CSTR.

For most chemical reactions, it is impossible for the reaction to proceed to 100% completion. The rate of reaction decreases as the percent
completion increases until the point where the system reaches dynamic equilibrium (no net reaction, or change in chemical species
occurs). The equilibrium point for most systems is less than 100% complete. For this reason a separation process, such as distillation,
often follows a chemical reactor in order to separate any remaining reagents or byproducts from the desired product. These reagents may
sometimes be reused at the beginning of the process, such as in the Haber process.

Continuous oscillatory baffled reactor (COBR) is a tubular plug flow reactor. The mixing in COBR is achieved by the combination of
fluid oscillation and orifice baffles, allowing plug flow to be achieved under laminar flow conditions with the net flow Reynolds number
just about 100.

[edit] Semi-batch reactor

A semi-batch reactor is operated with both continuous and batch inputs and outputs. A fermenter, for example, is loaded with a batch,
which constantly produces carbon dioxide, which has to be removed continuously. Analogously, driving a reaction of gas with a liquid is
usually difficult, since the gas bubbles off. Therefore, a continuous feed of gas is injected into the batch of a liquid. An example of such a
reaction is chlorination.

[edit] Catalytic reactor
Although catalytic reactors are often implemented as plug flow reactors, their analysis requires more complicated treatment. The rate of a
catalytic reaction is proportional to the amount of catalyst the reagents contact. With a solid phase catalyst and fluid phase reagents, this is
proportional to the exposed area, efficiency of diffusion of reagents in and products out, and turbulent mixing or lack thereof. Perfect
mixing cannot be assumed. Furthermore, a catalytic reaction pathway is often multi-step with intermediates that are chemically bound to
the catalyst; and as the chemical binding to the catalyst is also a chemical reaction, it may affect the kinetics.

The behavior of the catalyst is also a consideration. Particularly in high-temperature petrochemical processes, catalysts are deactivated by
sintering, coking, and similar processes.

A common example of a catalytic reactor is the catalytic converter following a motor.

Continuous stirred-tank reactor

The continuous stirred-tank reactor (CSTR), also known as vat- or backmix reactor, is a common ideal reactor type in chemical
engineering. A CSTR often refers to a model is used to estimate the key unit operation variables when using a continuous [†] agitated-tank
reactor to reach a specified output. (See Chemical reactors.) The mathematical model works for all fluids: liquids, gases, and slurries.

The behavior of a CSTR is often approximated or modeled by that of a Continuous Ideally Stirred-Tank Reactor (CISTR). All calculations
performed with CISTRs assume perfect mixing. If the residence time is 5-10 times the mixing time, this approximation is valid for
engineering purposes. The CISTR model is often used to simplify engineering calculations and can be used to describe research reactors.
In practice it can only be approached, in particular in industrial size reactors.

Integral mass balance on number of moles Ni of species i in a reactor of volume V.

[accumulation] = [in] - [out] + [generation]


where Fio is the molar flow rate inlet of species i, Fi the molar flow rate outlet, and νi stoichiometric coefficient. The reaction rate, r, is
generally dependent on the reactant concentation and the rate constant (k). The rate constant can be figured by using the Arrhenius
temperature dependence. Generally, as the temperature increases so does the rate at which the reaction occurs. Residence time, τ, is the
average amount of time a discrete quantity of reagent spends inside the tank.


         constant density (valid for most liquids; valid for gases only if there is no net change in the number of moles or drastic
          temperature change)
         isothermal conditions, or constant temperature (k is constant)
         steady state
         single, irreversible reaction (νA = -1)
         first-order reaction (r = kCA)

A → products

NA = CA V (where CA is the concentration of species A, V is the volume of the reactor, N A is the number of moles of species A)


The values of the variables, outlet concentration and residence time, in Equation 2 are major design criteria.

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

CSTR's are known to be one of the systems which exhibit complex behavior such as steady-state multiplicity, limit cycles and chaos.


  Occasionally the term "continuous" is misinterpreted as a modifier for "stirred", as in 'continuously stirred'. This misinterpretation is
especially prevalent in the civil engineering literature. As explained in the article, "continuous" means 'continuous-flow' — and hence
these devices are sometimes called, in full, continuous-flow stirred-tank reactors (CFSTR's).

Fixed Bed Reactor (small)

Heat treatment of samples in a controlled atmosphere

Key Specifications

Reactor (outer tube): Ø60 x 1400mm

Max t = 1200°C

Max sample size = 45 g


The setup includes the following components:

         a gas mixing system
         a reactor
         a gas conditioning system
         gas analyzers
         a thermocouple
         a data acquisition system.

The reactor consists of a two-zone electrically heated oven, in which a cylindrical alumina tube is mounted horizontally, having water-
cooled flanges at both ends. The configuration and dimensions of the reactor tubes are shown in Figure 1.

 A sample (e.g., biomass, waste, coal, salt, etc.) can be inserted in the middle of the (pre-heated) reactor. The reactor can then be sealed
and a gas (mixture) can be introduced into the reactor, for example to pyrolyze or combust the sample. The sample temperature and the
exit gas composition (e.g., O2, CO, and CO2) can be monitored online, so that the conversion process can be followed during an
experiment. After the desired residence time, the sample boat can be withdrawn from the reactor (see Figure 2), weighed, and the residue
can be collected for chemical analysis.

 The setup allows for conversion (pyrolysis and combustion) of solid fuel samples under well-controlled conditions (temperature, gas flow
rate and composition, and residence time), simulating the conditions on the grate of a utility boiler. By performing accurate weight
measurements and chemical analysis of the sample before and after the treatment in the reactor, quantitative data can be obtained on the
release to the gas phase of inorganic elements from relatively small samples. Such data are important for the understanding and modeling
of ash and aerosol formation in grate-fired boilers.

Fluidized bed reactor

A fluidized bed reactor (FBR) is a type of reactor device that can be used to carry out a variety of multiphase chemical reactions. In this
type of reactor, a fluid (gas or liquid) is passed through a granular solid material (usually a catalyst possibly shaped as tiny spheres) at
high enough velocities to suspend the solid and cause it to behave as though it were a fluid. This process, known as fluidization, imparts
many important advantages to the FBR. As a result, the fluidized bed reactor is now used in many industrial applications.

[edit] Basic principles

The solid substrate (the catalytic material upon which chemical species react) material in the fluidized bed reactor is typically supported
by a porous plate, known as a distributor.[1] The fluid is then forced through the distributor up through the solid material. At lower fluid
velocities, the solids remain in place as the fluid passes through the voids in the material. This is known as a packed bed reactor. As the
fluid velocity is increased, the reactor will reach a stage where the force of the fluid on the solids is enough to balance the weight of the
solid material. This stage is known as incipient fluidization and occurs at this minimum fluidization velocity. Once this minimum velocity
is surpassed, the contents of the reactor bed begin to expand and swirl around much like an agitated tank or boiling pot of water. The
reactor is now a fluidized bed. Depending on the operating conditions and properties of solid phase various flow regimes can be observed
in this reactor.

[edit] History and current uses

Fluidized bed reactors are a relatively new tool in the chemical engineering field. The first fluidized bed gas generator was developed by
Fritz Winkler in Germany in the 1920s.[2] One of the first United States fluidized bed reactors used in the petroleum industry was the
Catalytic Cracking Unit, created in Baton Rouge, LA in 1942 by the Standard Oil Company of New Jersey (now ExxonMobil).[3] This
FBR and the many to follow were developed for the oil and petrochemical industries. Here catalysts were used to reduce petroleum to
simpler compounds through a process known as cracking. The invention of this technology made it possible to significantly increase the
production of various fuels in the United States. [4]

Today fluidized bed reactors are still used to produce gasoline and other fuels, along with many other chemicals. Many industrially
produced polymers are made using FBR technology, such as rubber, vinyl chloride, polyethylene, and styrenes. Various utilities also use
FBR’s for coal gasification, nuclear power plants, and water and waste treatment settings. Used in these applications, fluidized bed
reactors allow for a cleaner, more efficient process than previous standard reactor technologies.[4]
[edit] Advantages

The increase in fluidized bed reactor use in today’s industrial world is largely due to the inherent advantages of the technology.[5]

        Uniform Particle Mixing: Due to the intrinsic fluid-like behavior of the solid material, fluidized beds do not experience poor
         mixing as in packed beds. This complete mixing allows for a uniform product that can often be hard to achieve in other reactor
         designs. The elimination of radial and axial concentration gradients also allows for better fluid-solid contact, which is essential
         for reaction efficiency and quality.

        Uniform Temperature Gradients: Many chemical reactions require the addition or removal of heat. Local hot or cold spots
         within the reaction bed, often a problem in packed beds, are avoided in a fluidized situation such as an FBR. In other reactor
         types, these local temperature differences, especially hotspots, can result in product degradation. Thus FBRs are well suited to
         exothermic reactions. Researchers have also learned that the bed-to-surface heat transfer coefficients for FBRs are high.

        Ability to Operate Reactor in Continuous State: The fluidized bed nature of these reactors allows for the ability to
         continuously withdraw product and introduce new reactants into the reaction vessel. Operating at a continuous process state
         allows manufacturers to produce their various products more efficiently due to the removal of startup conditions in batch

[edit] Disadvantages

As in any design, the fluidized bed reactor does have it draw-backs, which any reactor designer must take into consideration. [5]

        Increased Reactor Vessel Size: Because of the expansion of the bed materials in the reactor, a larger vessel is often required
         than that for a packed bed reactor. This larger vessel means that more must be spent on initial capital costs.

        Pumping Requirements and Pressure Drop: The requirement for the fluid to suspend the solid material necessitates that a
         higher fluid velocity is attained in the reactor. In order to achieve this, more pumping power and thus higher energy costs are
         needed. In addition, the pressure drop associated with deep beds also requires additional pumping power.

        Particle Entrainment: The high gas velocities present in this style of reactor often result in fine particles becoming entrained in
         the fluid. These captured particles are then carried out of the reactor with the fluid, where they must be separated. This can be a
         very difficult and expensive problem to address depending on the design and function of the reactor. This may often continue to
         be a problem even with other entrainment reducing technologies.

        Lack of Current Understanding: Current understanding of the actual behavior of the materials in a fluidized bed is rather
         limited. It is very difficult to predict and calculate the complex mass and heat flows within the bed. Due to this lack of
         understanding, a pilot plant for new processes is required. Even with pilot plants, the scale-up can be very difficult and may not
         reflect what was experienced in the pilot trial.

        Erosion of Internal Components: The fluid-like behavior of the fine solid particles within the bed eventually results in the wear
         of the reactor vessel. This can require expensive maintenance and upkeep for the reaction vessel and pipes.

[edit] Current research and trends

Due to the advantages of fluidized bed reactors, a large amount of research is devoted to this technology. Most current research aims to
quantify and explain the behavior of the phase interactions in the bed. Specific research topics include particle size distributions, various
transfer coefficients, phase interactions, velocity and pressure effects, and computer modeling.[6] The aim of this research is to produce
more accurate models of the inner movements and phenomena of the bed. This will enable scientists and engineers to design better, more
efficient reactors that may effectively deal with the current disadvantages of the technology and expand the range of FBR use.

Fluidized-Bed Reactor

     A fluidized-bed reactor is a combination of the two most common, packed-bed and stirred tank, continuous flow reactors. It is very
important to chemical engineering because of its excellent heat and mass transfer characteristics. The fluidized-bed reactor can be seen
     In a fluidized-bed reactor, the substrate is passed upward through the immobilized enzyme bed at a high enough velocity to lift the
particles. However, the velocity must not be so high that the enzymes are swept away from the reactor entirely. This causes some mixing,
more than the piston-flow model in the packed-bed reactor, but complete mixing as in the CSTR model. This type of reactor is ideal for
highly exothermic reactions because it eliminates local hot-spots, due to its mass and heat transfer characteristics mentioned before. It is
most often applied in immobilized-enzyme catalysis where viscous, particulate substrates are to be handled.

Plug flow reactor model

The plug flow reactor (PFR) model is used to describe chemical reactions in continuous, flowing systems. The PFR model is used to
predict the behaviour of chemical reactors, so that key reactor variables, such as the dimensions of the reactor, can be estimated. PFRs are
also sometimes called as Continuous Tubular Reactors (CTRs).
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 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 batch reactor, limiting to zero volume. As it flows down the tubular PFR, the residence time (τ) 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 τ.

[edit] PFR modelling

PFRs are frequently referred to as piston flow reactors, or sometimes as continuous tubular reactors. They are governed by ordinary
differential equations, the solution for which can be calculated providing that appropriate boundary conditions are known.

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

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.


         plug flow
         steady state
         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)
         constant tube diameter
         single reaction

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

[accumulation] = [in] - [out] + [generation] - [consumption]

1. Fi(x) − Fi(x + dx) + Atdxνir = 0 . [1]

When linear velocity, u, and molar flow rate relationships, Fi,                      and Failed to parse (Cannot write to or create
math output directory): F_i = A_t u C_i \, , are applied to Equation 1 the mass balance on i becomes

2.                                                                 . [1]

When like terms are canceled and the limit dx → 0 is applied to Equation 2 the mass balance on species i becomes

3.                    , [1]

where Ci(x) is the molar concentration of species i at position x, At the cross-sectional area of the tubular reactor, dx the differential
thickness of fluid plug, and νi stoichiometric coefficient. The reaction rate, r, can be figured by using the Arrhenius temperature
dependence. Generally, as the temperature increases so does the rate at which the reaction occurs. Residence time, τ, is the average
amount of time a discrete quantity of reagent spends inside the tank.


         isothermal conditions, or constant temperature (k is constant)
         single, irreversible reaction (νA = -1)
         first-order reaction (r = kCA)

After integration of Equation 3 using the above assumptions, solving for CA(L) we get an explicit equation for the output concentration of
species A,

4.                               ,
where CAo is the inlet concentration of species A.

[edit] Operation and uses

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.)

An ideal plug flow reactor has a fixed residence time: Any fluid (plug) that enters the reactor at time t will exit the reactor at time t + τ,
where τ is the residence time of the reactor. The residence time distribution function is therefore a dirac delta function at τ. A real plug
flow reactor has a residence time distribution that is a narrow pulse around the mean residence time distribution.

A typical plug flow reactor could be a tube 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.

[edit] Advantages and disadvantages

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.

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. [2]

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.

Plug flow reactor
• Reactor ini biasanya berupa tube (tabung)
yang bereaksi dengan aliran fluida
• Asumsi; tidak ada mixing
• Perfect mixing dan plug flow reactor
merupakan jenis mixingyang terjadi pada
flow reactor (reactor alir)
• Sebagian besar mixing dari jenis reactor
ini beroperasi pada level intermediate

Reactor katalitik
• Katalis merupakan suatu substance yang
bisa mempercepat reaksi
• Sebagian besar, reaktor katalitik
menggunakan katalis solid
Reactor katalitik

Fixed bed reactor
• Biasanya terdiri dari katalis partikel padat
(stationary solid catalyst particle) yang
bereaksi dengan aliran fluida
• Aliran fluida bisa berupa gas atau liquid
(atau campuran keduanya)

Fluidized bed reactor
• Velicity gas yang besar dalam bed
menyebabkan « fluidize » dalam keadaan
hifgh mixing dan heat transfer

Untuk jenis reaktor fixed bed dan fluidized
bed, biasanya beroperasi dalam phase
gas pada reaktan dan phase solid pada

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