- Stationary Head-Channel
- Stationary Head-Bonnet
- Stationary Head Flange
Channel or Bonnet
- Channel Cover
- Stationary Head Nozzle
- Stationary Tubesheet
- Shell Flange
Stationary Head End
- Shell Flange
Rear Head End
- Shell Nozzle
- Shell Cover Flange
- Floating Tubesheet
- Floating Head Cover
- Floating Head Cover Flange
- Floating Head Backing Device
- Tierods and Spacers
- Transverse Baffles
or Support Plates
- Impingement Plate
- Vent Connection
- Drain Connection
- Instrument Connection
- Support Saddle
- Lifting Lug
- Pass Partition
Non removable bundle exchangers
These types of units are often used in high pressure services and services where you wish to avoid leakage problems at gasketed joints. Another advantage is that they are generally more cost effective than removable bundle designs.
NEU- The most cost effective design available. The tubesheet is welded to both the shell and Bonnet. There is no access to the shell. Tubes may be chemically cleaned, water blasted or steam cleaned from inside only. These units are commonly used in high pressure services (such as feedwater heaters), where process conditions allow for even pass exchangers.
NEN- Tubesheets are welded to both the Shell & Bonnets. Access to the tubes is through covers on the channels. These units are favored in very high pressure designs as their construction minimizes the tubesheet thickness and number of high pressure retaining flanges.
AEM/BEM/AEL-Shell side is completely welded up, however, the Bonnets are removable. Chemical, mechanical, and water blast cleaning of the tubes is possible, however you do not have access to the shell.
You should avoid using Steam cleaning on a fixed tube sheet unit unless the unit has a shell side expansion joint. The steam will cause the tubes to expand and pull out of the Tube Sheet causing failure at startup.
Differential thermal expansion
Since the duty of Heat Exchangers includes the handling of fluids of differing temperature, flow rate and thermal properties, differential expansion of the metals will take place.
When the terminal temperature difference between the fluids is substantial, over 50-60 degrees, these stresses can become severe, causing shells to become deformed and damage mounting supports, tubes to deform the tube sheet or tubes to become broken or dislodged from the tube sheet.
Fixed tube sheet designs are most vulnerable to differential thermal expansion, because there is no inherent provision to absorb the stresses. One approach in common use is installing an expansion joint in the shell pipe of such designs. This is a cost effective approach for pipe-size shells. An expansion joint can also be installed in the tube side of floating head designs, but manufacturing costs are much higher.
Diagram of U-Tube Heat Exchanger
Alternative approaches involve the design of a U-tube bundle so that each tube can inpendently expand and contract as needed or by using a rear floating internal tube sheet design which allows the entire bundle as a unit to expand and contract. The floating head is typically sealed against the interior of the shell by means of packing or O-ring designs.
U-tube designs while offering the best answer for differential thermal expansion, have some drawbacks. Individual tubes can be difficult of expensive to replace, especially for interior tubes. Also, the tube interior cannot be effectively cleaned in the u-bends. Erosion damage is also frequently seen in the u-bends in high tube side velocity applications. In large diameter shells, the long length of unsupported tube in the u-bends of outer tubes can lead to vibration induced damage.
Floating head designs of head exchangers
In an effort to reduce thermal stresses and provide a means to remove the tube bundle for cleaning, several floating rear head designs have been established.
The simplest is a "pull-through" design which allows the tube bundle to be pulled entirely through the shell for service or replacement. In order to accomodate the rear head bolt circle, tubes must be removed resulting in a less efficient use of shell size. In addition, the missing tubes result in larger annular spaces and can contribute to reduced flow across the effective tube surface, resulting in reduced thermal performance. Some designs include sealing strips installed in the shell to help block the bypass steam.
Another floating head design that partially addresses the above disadvantages is a "split-ring floating head". Here the floating head Bonnet is bolted to a split backing ring instead of the tube sheet.
This eliminates the bolt circle diameter and allows a full complement of tubes to fill the shell. This construction is more expensive than a common pull through design, but is in wide use in petrochemical applications. For applications with high pressures or temperatures, or where more positive sealing between the fluids is desired, the pull-through design should be specified.
Two other types, the "outside packed lantern ring" and the "outside packed stuffing box" designs offer less positive sealing against leakage to the atmosphere than the pull though or split ring designs, but can be configured for single tube pass duty.
The most common TEMA shell type is the "E" shell as it is most suitable for most industrial process cooling applications. However, for certain applications, other shells offer distinct advantages.
For example, the TEMA-F shell design provides for a longitudinal flow plate to be installed inside the tube bundle assembly. This plate causes the shell fluid to travel down one half of the tube bundle, then down the other half, in effect producing a counter-current flow pattern which is best for Heat Transfer.
This type of construction can be specified where a close approach temperature is required and when the flow rate permits the use of one half of the shell at a time. In heat recovery applications, or where the application calls for increased thermal length to acheive effective overall Heat Transfer, shells can be installed with the flows in series.
Up to six shorter shells in series is common and results in counter-current flow close to performance as if one long shell in a single pass design were used.
TEMA G and H shell designs are most suitable for phase change applications where the bypass around the longitudinal plate and counter-current flow is less important than even flow distribution. In this type of shell, the longitufinal plate offers better flow distribution in vapor streams and helps to flush out non-condensables. They are frequently specified for use in horizontal thermosiphon reboilers and total condensers.
TEMA J Shells are typically specified for phase change duties where significantly reduced shell side pressure drops are required. They are commonly used in stacked sets with the single nozzles used as the inlet and outlet.
A special type of J-shell is used for flooded evaporation of shell side fluids. A separate vapor disengagement vessel without tubes is installed above the main J shell with the vapor outlet at the top of this vessel. The TEMA K shell, also termed a "Kettle Reboiler" is specified when the shell side stream will undergo vaporization.
The liquid level of a K shell design should just cover the tube bundle, which fills the smaller diameter end of the shell.
This liquid level is controlled by the liquid flowing over a wier at the far end of the entrance nozzle. The expanded shell area serves to facilitate vapor disengagement for boiling liquid in the bottom of the shell. To insure against excessive liquid carry-though with the vapor stream, a separate vessel as described above is specified.
Liquid carry-through can also be minimized by installing a mesh demister at the vapor exit nozzle. U-bundles are typically used with K shell designs. K shells are expensive for high pressure vaporization due to shell diameter and the required wall thickness.
The TEMA X shell, or crossflow shell is most commonly used in vapor condensing applications, though it can also be used effectively in low pressure gas cooling or heating.
It produces a very low shell side pressure drop, and is therefore most suitable for vacuum service condensing. In order to assure adequate distribution of vapors, X-shell designs typically feature an area free of tubes along the top of the exchanger. It is also typical to design X shell condensers with a flow area at the bottom of the tube bundle to allow free condensate flow to the exit nozzle. Careful attention to the effective removal of non-condensables is vital to X-shell constructions.
Part 1: Heat Transfer and types of Heat Exchangers.
Part 2: Shell and Tube Heat Exchangers.
Part 3: Tubes and Tube Sheets of Heat Exchangers.
Part 4: Shell Assembly of Heat Exchangers.
Part 5: TEMA Designations of Heat Exchangers.