Oct 16, 2013 Selection and Design of Condensers 1. GBH Enterprises, Ltd. Process Engineering Guide: GBHE-PEG-HEA-508 Selection and Design of Condensers Information contained in this publication or as otherwise supplied to Users is believed to be accurate and correct at time of going to press, and is given in good faith, but it is for the User to satisfy itself of the suitability of the information for its. PROCESS DESIGN OF SHELL AND TUBE HEAT EXCHANGER, CONDENSER AND REBOILERS. Calculation of heat transfer co-efficient. Type of heat exchanger and design pressure. Downloads lagu opick taubat. The optimum thermal design of a shell and tube heat exchanger involves the. Tube heat exchangers calculations it is very important to remember some.
Condenser Heat Exchanger is very common in process industry, condensers may be classified in two main types; Condensers which have a coolant and a condensing vapor brought into direct contact and other types which have the coolant and a condensate stream separated by a tube wall or a solid surface.
This Software deals with the type where the streams are separated when condensation occurs inside or outside the tubes.
Condenser Heat Exchanger Software Features (CnD)
- Support S.I Units and English (U.S) Units of measurement, Units converter containing 23 measurements and 200 units conversions
- Import physical properties data to hot side and cold side from Microsoft Excel & from WeBBusterZ Physical properties database included.
- Estimate the Physical properties of pure components for more than 1450 components; the database has the ability to estimate Thermal Conductivity, Density, Heat Capacity and Viscosity. The database also included critical properties, boiling and melting points and come as separate software but easily integrated with the software.
- Ability to add your own properties in the additional user databases.
- Tube counts and standard tube sizes tables
- Fouling factors
- Overall heat transfer coefficients
- Materials Thermal Conductivity.
- Maximum Allowable design velocities inside tubes for liquids
- Ability to add your own components to use for simulations.
- Save/Load results
- Generate an engineering datasheet (can be exported to .pdf file format), Export Results to Engineering Data sheet in Microsoft Excel for editing
- Export Results summary to Microsoft Word or Print Results summary.
- Supports Horizontal shell side/Horizontal tube side/Vertical shell side/Vertical tube side and Reflux condensers design.
14. Supports Full condensation and Partial condensation (Subject to condensation model selection please see the table provided below for full information). FEATURE Horizontal Shell Side Condenser Horizontal Tube Side Condenser Vertical Shell Side Condenser Vertical Tube Side Condenser Reflux Condenser Orientation Horizontal Horizontal Vertical Vertical Vertical Condensation in Shell Tube Shell Tube Tube Full Condensation Yes Yes Yes Yes Yes Partial Condensation Yes Yes No Yes No Sub cooling Yes, with Full condensation only No YES Yes YES Super heated vapor Yes, with Full condensation only No YES Yes YES Shear Controlled Condensation Yes No No Yes No Gravity Controlled Condensation Yes Yes Yes Yes Yes Zone Analysis Yes, with Partial condensation only No No Yes, with Partial condensation only No TEMA Shell Supported E,J,X E E E E TEMA Front Head Supported A,B,C,D,N A,B,C,D,N A,B,C,D,N A,B,C,D,N A,B,C,D,N TEMA Rear Head Supported S,U,L,M,N,P,T,W S,U,L,M,N,P,T,W S,L,M,N,P,T,W S,L,M,N,P,T,W S,L,M,N,P,T,W - Support Sub cooling, super heated vapor, Zone analysis, Shear Controlled and Gravity Controlled condensation
- Basis and assumptions that the software makes during the calculations are stated on a visible panel.
- Support single phase vapour condensation on hot side and liquid coolant on cold side, bare tubes only
- TEMA designations.
- Unknown Cold side temperature, Unknown Hot or cold side flow rate can also be calculated.
- Triangular and square pitch tube orientation
- Detailed calculation than displays many calculated variables such as: Duty, Area, Number of tubes, Shell/Tube velocities, flooding velocity and operating velocity for reflux condenser, Reynolds numbers, Condensation heat transfer coefficient, Condensation flow regime, Number of Baffles and Baffle spacing, Scale resistance (dirt factor), Overall heat transfer coefficient for both Clean and Fouled conditions, Pressure drops…etc. and many more
- Ability to track calculation changes from trial to another.
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Demo version
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Video Contents
00:00:00 Main screen menus and buttons
00:01:01 Units converter
00:01:32 Tube Counts
00:02:08 Fouling Factors
00:02:29 User Data input screens
00:04:02 Overall heat transfer coefficients & BWG
00:06:03 Example 1 – SI Units
00:12:11 Example 2 – US Units
00:17:31 Importing physical properties
00:00:00 Main screen menus and buttons
00:01:01 Units converter
00:01:32 Tube Counts
00:02:08 Fouling Factors
00:02:29 User Data input screens
00:04:02 Overall heat transfer coefficients & BWG
00:06:03 Example 1 – SI Units
00:12:11 Example 2 – US Units
00:17:31 Importing physical properties
Tubular condensers used in power plant to condense exhaust steam are known as Surface Condensers. However, there are many other applications in which condensers are used, and a wide variety of condenser types has been developed.
The direct-contact condenser is one in which the coolant is brought into contact with the vapor. It has the advantage of low cost and simplicity of mechanical design, but its use is restricted to those applications in which mixing of the vapor and coolant is permissible.
The various types of direct contact condensers are:
Condenser Design Calculation Pdf Reader Pdf
- The Spray Condenser. The coolant is sprayed, using nozzles, into a vessel to which the vapor is supplied. This is shown schematically in Figure 1. It is important that the spray nozzles and vessel are designed to produce a fine spray of liquid (to give a large interfacial area for heat transfer), and a long enough residence time of liquid droplets in the vessel.
- The Baffled Column. This is similar to the spray condenser, except that the coolant is directed to flow over a series of trays in a column (see Figure 2). The vapor is supplied to the bottom of the column. It has the advantage of countercurrent flow of vapor and coolant, though care must be taken to avoid flooding. (Flooding is an unstable condition when the vapor flow is such that the downward flow of condensate is interrupted and held up.)
- The Packed Column. A packed column may consist of tightly-packed metal rings to increase the interfacial area for heat transfer. Liquid is supplied to the top of the column and vapor is supplied to the bottom. The disadvantage of this type of condenser is that the pressure drop is higher than in other types of direct-contact condenser.
- The Jet Condenser. This is a device in which a jet of liquid is directed into a vapor stream, usually with the objective of desuperheating the vapor. A jet of liquid is injected into a pipeline carrying vapor via a small bore pipe and a nozzle located at the center line. The liquid is usually injected in counterflow to the vapor.
- The Sparge Pipe. The sparge pipe consists of a pipe with holes for injecting bubbles of vapor into a pool of liquid. This is a simple method of condensing a vapor, but there are practical problems associated with generating a good distribution of bubbles of small size, which are required for efficient heat transfer.
Figure 1. Spray condense.
Figure 2. Tray type condenser. Source: G. P. Hewitt, G. L. Shires, and T. Bott Process Heat Transfer (1994).
The design of direct-contact condensers is well described by Pair (1972). Most equipment of this type is designed on the basis of empirical information from experimental and operating data.
Shell-and-tube condensers are used extensively in the process industries, typically to condense the overhead vapor from a distillation column. There are three main types.
Condenser Design Calculation Pdf Reader Tool
The crossflow condenser is similar to the surface condenser. It consists of a shell containing tubes through which the coolant flows. The shell-side flow path is designed such that the vapor flows mainly in crossflow direction to the tubes. The crossflow condenser is typically used for low-pressure applications, in which there is a large volume flow of vapor and a low-pressure drop is required.The tubes are supported at intervals by plates to prevent sagging of the tubes and to avoid vibration.The vapor enters at the top of the shell. Often, more than one nozzle is used to minimise pressure loss and promote good distribution.It is particularly important to ensure that the crossflow condenser is properly vented.
The baffled shell-and-tube heat exchanger, with shell-side condensation, is the most common type of condenser used in the process industries. It is most often mounted horizontally. A typical shell-side condenser is shown in Figure 3. This is a shell of the TEMA E-type in which the vapor enters at one end of the shell and flows to the outlet end, where the condensate and any uncondensed vapor and non-condensing gases are removed.
Figure 3. Horizontal shell-side condenser. Source: G. F. Hewitt, G. L. Shires, and T. Bott Process Heat Transfer (1994).
The baffles are normally plates with a single segmental cut. The cut is usually vertical to allow the condensate to flow along the bottom of the shell to the outlet. Double segmental baffles may be specified to achieve reduced pressure drop. The space between the baffles is determined by considerations such as:
- Loopback free for mac free. The tubes must be supported to avoid tube vibration;
- Pressure drop depends on vapor velocity, and hence on baffle spacing;
- The resistance to heat transfer due to the presence of noncondensing gases is inversely proportional to the vapor velocity.
- High vapor velocities can reduce resistance to heat transfer through the shear effect on the condensate film.
Thus, if adequate pressure drop is available, it may be possible to reduce baffle spacing to obtain increased heat transfer rates.
The size of the baffle cut is generally chosen such that the vapor velocity in the baffle window is roughly equal to that in the overlap zone between the baffle plates.
The number of tube passes is determined by the required coolant velocity. Plain tubes are generally used, though low-finned tubes can be used to obtain increased heat transfer rates when the condensate resistance to heat transfer with plain tubes is significantly greater than that of the coolant.
The vapor vent should be situated at the end of the vapor flow path. A typical vent location is shown in Figure 3.
It is possible to use other TEMA shell types, such as the J-type, to minimize pressure drop. A possible configuration for low pressure drop is the J-shell with double segmental baffles.
Condensation on the tube-side is preferred when the coolant is a gas, such as air. It may also be preferred if the condensing fluid is at a higher pressure than the coolant, since it is usually less expensive to contain a higher pressure inside tubes than inside a shell. An air-cooled condenser is typical of a tube-side condenser. It consists of a tube bundle, normally with finned tubes, over which air flows in crossflow. The air flow is driven by fans, either in forced- or induced-draft mode. A typical forced-draft, air-cooled condenser is depicted in Figure 4.
Figure 4. Schematic of air-cooled condenser operating in forced-draft mode. Source: G. F. Hewitt, G. L. Shires, and T. Bott Process Heat Transfer (1994).
Condenser Design Calculation Pdf Reader 1
If the tubes are vertical, the two configurations in common use are:
- Cocurrent downward vapor and liquid flow;
- Countercurrent flow with the vapor flowing upward and the liquid flowing downward. This is commonly known as the reflux condenser.
It is not advisable to attempt cocurrent upward vapor and liquid flow unless there is a high vapor velocity at the outlet of the tubes.
The reflux condenser must be designed such that vapor velocity is less than the flooding velocity. This is a limiting velocity above which drainage of condensate is irregular. (See Flooding and Flow Reversal.)
Area calculation.
In condensation of a single pure vapor, provided that the pressure drop is small compared to the absolute pressure, the temperature of the condensing stream is a constant value determined by the saturation pressure.
If the coolant is single-phase, and if the overall heat transfer coefficient is reasonably constant, then the assumptions underlying the “logarithmic mean temperature difference (LMTD)” are valid. (See Mean Temperature Difference.) This means that the surface area requirement, A, of the condenser can be determined from:
(1)
where QT is the total heat load and U is the mean overall heat transfer coefficient.
In condensation from mixtures, with or without a noncondensing gas, the variation of the equilibrium temperature with enthalpy can be highly nonlinear. Also, the heat transfer coefficient of the condensing stream can vary by an order of magnitude over the condensing path. This means that it is not possible to assign a single representative temperature difference and overall heat transfer coefficient to the exchanger, and that a zonal or stepwise calculation of the surface area is required.
The thermal design of condenser is therefore considerably more complicated than that of a single-phase heat exchanger.
Figure 5 shows a typical temperature/enthalpy relationship for a mixture which is superheated at entry. This relationship, and the corresponding physical properties, are normally obtained from specialist computer programs which perform vapor-liquid equilibrium calculations and determine the compositions of the vapor and liquid phases along the condensing path. The corresponding relationship for a single-phase coolant flowing in a single pass in counterflow to the condensing stream is also shown.
Figure 5. Example of temperature/enthalpy curves for a condensing stream and coolant, showing subdivision into zones.
An outline of the procedure to determine the surface area requirement for such a condensing duty is as follows:
- Divide the temperature/enthalpy diagram into a number of zones such that the curves of both the condensing stream and the coolant can be regarded as being reasonably linear. An example of how this is done is shown in Figure 5.
- Specify the principal geometric parameters of the design, such as the number of tubes, tube outside diameter and wall thickness, tube pitch, baffle cut, baffle pitch and shell diameter.
- Calculate the local overall heat transfer coefficients at the zone boundaries.
- For each zone, calculate the zonal overall heat transfer coefficient, Uz, from the arithmetic average of the local overall coefficients at the zone boundaries.
- Calculate the LMTD for each zone from the temperatures at the zone boundaries.
- Calculate the surface area requirement for each zone by applying Eq. (1) above.
- Calculate the total surface requirement by summing the zonal surface areas.
The design process consists of repeating the above process, varying the main geometrical parameters to both meet the pressure drop constraints and minimize either area or cost. The procedure is generally carried out using a computer program.
If, as is often the case, condensation occurs on the shell-side with multiple tube-side passes, the calculation of temperature profiles and zonal surface areas is more complicated. A suitable methodology is described by Bell and Ghaly (1972).
The above procedure for calculating surface area requires evaluation of the local heat transfer coefficient at the zone boundaries. This, in turn, requires calculation of:
- The coolant heat transfer coefficient;
- The resistance to heat transfer due to the tube wall;
- The condensate heat transfer coefficient associated with heat transfer through a film of condensate on the tube wall;
- The resistance to heat transfer associated with the presence of non-condensing gases, or with a mixture of more than one vapor.
In addition, it is necessary to estimate the resistance to heat transfer due to fouling on both sides of the tube wall. (See Fouling and Fouling Factors.)
Calculation of the condensate heat transfer coefficient depends strongly on condenser geometry. Appropriate methods are described by Hewitt, Shires and Bott (1994), who also prescribed the calculation of the gas-phase resistance. Use of a computer program is required for all but the simplest calculations.
The pressure gradient in condensers is due to both frictional and accelerational effects. The frictional effect, which gives rise to a pressure loss, can be calculated by applying a two-phase multiplier to the pressure gradient for single-phase flow. The accelerational effect gives rise to a pressure increase due to the deceleration of the flow. It is usually only significant at low pressures, and can be calculated on the basis of the vapor flow rate alone.
Some types of plate heat exchangers, which have been traditionally used in other applications, are increasingly used as condensers. For example, the plate-and-frame and brazed-plate heat exchangers, have advantages of lower cost and lower fluid inventory. The use of plate heat exchangers as condensers is discussed by Kumar (1983). Normally, a special plate passage and inlet port configuration will be required to handle the high-vapor volume flow rate at a condenser inlet.
The plate-fin heat exchanger, traditionally used in cryogenic applications, can also be applied to some general condensing applications in which compactness is required.
Removal of gases
It is important to provide a condenser with a vent for removal of gases, either during start-up and/or for continuous operation. The vent must be located near the end of the vapor flow path. It is particularly important in crossflow shell-and-tube condensers to avoid regions of very low vapor velocity, where stagnant zones of noncondensing gas can form and consequently render some of the heat exchanger surface ineffective.
The condensate drain from a condenser must be carefully designed to ensure that it is adequately-sized for the condensate flow rate, and to avoid entrainment of uncondensed vapor or gas into the condensate pipework.
Fogging in a condenser is due to the formation of tiny droplets of liquid in the vapor. Fog formation can occur when the temperature of the vapor-gas mixture falls significantly below the local saturation temperature during the condensation process. This tends to happen when the transport properties of a vapor-gas mixture and the process conditions are such that more heat than mass is removed from the mixture. Fog formation represents undesirable loss of product and may, in some circumstances, represent a pollution problem. The actual onset of fog formation will depend on the presence or otherwise of nucleation sites. Removal of fog may require special separation methods. Steinmeyer (1972) gives a good practical account of how fog forms and how its effects can be minimized.
REFERENCES
Bell, K. J. and Ghaly, M. A. (1972) An Approximate Generalised Design Method for Multicomponent/Partial Condensers, AIChE Symp. Series, 131 (69), 72.
Fair, J. R. (1972) Designing Direct-Contact Coolers/Condensers, Chem. Engng., 12 June, 91-100.
Hewitt, G. F., Shires, G. L., and Bott, T. R. (1994) Process Heat Transfer, CRC Press, Boca Raton, Florida.
Condenser Design Calculation
Kumar, H. (1983) Condensation Duties in Plate Heal Exchangers, Instn. Chem Engnrs Symposium Series, 75, 2, 1275.
Steinmeyer, D. E. (1972) Fog Formation in Partial Condensers, Chem. Engng Progress, 68, 7, 64-68.
References
Condenser Design Calculation Pdf Reader 2017
- Bell, K. J. and Ghaly, M. A. (1972) An Approximate Generalised Design Method for Multicomponent/Partial Condensers, AIChE Symp. Series, 131 (69), 72.
- Fair, J. R. (1972) Designing Direct-Contact Coolers/Condensers, Chem. Engng., 12 June, 91-100.
- Hewitt, G. F., Shires, G. L., and Bott, T. R. (1994) Process Heat Transfer, CRC Press, Boca Raton, Florida.
- Kumar, H. (1983) Condensation Duties in Plate Heal Exchangers, Instn. Chem Engnrs Symposium Series, 75, 2, 1275.
- Steinmeyer, D. E. (1972) Fog Formation in Partial Condensers, Chem. Engng Progress, 68, 7, 64-68.