There are many advantages to using eductors for heating liquids in open vessels. These give the vessel heating eductor a place as a viable option for heating in many types of vessels.
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The tank eductor heater provides direct contact of the steam into the liquid. This assures complete transfer of the energy in the steam into the liquid being heated. Other types of heating lose efficiency as the interior of the heat exchanger builds up a scale. With eductors, the velocity of the steam being injected into the vessel also causes the liquid contents of the vessel to be agitated while heating occurs, without the need for other types of mixers in the vessel. This provides for more even heating of the vessel contents. They also permit the steam to be dispersed over more of the liquid volume, resulting in a more homogenous heating than with other methods of injecting steam.
These designs of eductors allow steam to be used from 10 to 140 PSIG for heating. Because of the nature of direct steam injection, heating vessels at atmospheric pressure beyond 140° F should not be attempted. Exceeding this temperature could result in uncondensed steam evolving from the liquid.
Computer optimized flow paths enable the tank eductor to maintain a high "pick-up ratio" (the ratio of fluid entrained to the motive fluid) while maximizing the hydraulic efficiency (the ratio of hydraulic power at the outlet of the tank eductor to the hydraulic power at the inlet) to generate an optimum flow field from the greatest flow amplification.
No moving parts in the sparger nozzle, minimizing maintenance expenses.
Optimum flow field enables more activity within the tank than competitive units without changing pumps.
Compact design and ease of mounting keeps the tank eductor from interfering with other tank equipment.
"In-tank" mounting eliminates need for costly, complex mounting structures above tanks.
The TLA & TLM can be used in a wide variety of open vessels or closed tanks.
Eliminates stratification and promotes a homogenous tank with relation to pH, temperature, solids or gas dispersion, and distribution of chemicals.
Produces a unique agitation not available with other types of mixers, as the eductor can generate a directed flow field within the fluid being mixed including viscous fluids, slurries, and suspensions.
Easily mixes liquids of differing specific gravities and is excellent for scrubbing applications where a lower specific gravity fluid is driven into the higher one.
Flow amplification due to high "pick-up ratio" and hydraulic efficiency permits the use of smaller pumps, which translates to reduced costs of mixing or agitation.
Reduces investment cost because existing transfer pumps can be utilized for more than one purpose.
This coating is applied via electrostatic powder spray or fluidized powder bed. In addition to possessing the high chemical and temperature resistance which all fluoropolymers are noted for, Edathon's strengths, radiation resistance, wear resistance, and creep resistance are significantly greater than those of other fluoropolymers such as PTFE, FEP, or PFA.
The standard tank eductor models for heating in vessels are the TLA, TLM and ULJ. The model TLA and TLM are well suited to providing strong tank agitation while heating. Compared with other heaters, the cost per application is small. The model ULJ is designed to provide vigorous circulation of the liquid with low pressure steam inputs.
Sparger Nozzles should be located with the outlet pointed toward the most remote portion of the tank to provide the best agitation possible.
Tank eductor offers an inexpensive, yet highly effective way to improve circulation, agitation and heating of liquids in tanks.
The TLA & TLM are a ejector-type jet, requiring no nipple, recommended for tanks in a multiple of installations.
What is the tank liquid? (If it is not water (Sg =1.0, Sh =1.0), contact us.)
What temperature rise (AT) is needed?
What is the final tank temperature?
What is the vessel capacity?
Time available to heat the vessel (t)?
Steam pressure available?
Step 1 To determine the amount of steam required to heat the liquid in the vessel, multiply the gallons in the vessel to be heated x 8.33 x Sg x Sh x temperature rise delta T desired, divided by (BTUs per Lb steam). Lb steam required (Wm) = Gal x 8.33 x Sg x Sh x delta T/
Step 2 To calculate the flow of steam required per minute, divide the steam flow from Step 1 by the time you need to complete the heating process. Lb steam per minute (Qm)= Wm/minutes (t)
Step 3 If multiple units are going to be used, divide the number from Step 2 by the number of units to be used.
Step 4 Go to the Steam Flow table. Find the amount of steam flow Qm (Lb/Min) at the steam pressure available. This is the steam flow for a 1-1/2" unit. Take the steam flow obtained in Step 3 divided by the steam flow from the Steam Flow table. This will give the Sizing Factor (S.F.) needed to heat the vessel in the time required.
S.F. = Desired Steam Flowrate/ Saturated Steam Flowrate
Step 5 Choose the eductor size that has at meets or exceeds the number determined in Step 4
The temperature rise desired is ?T = 50°F
The final tank temperature is 120°F
The vessel holds 550 gallons
The time to heat it is 20 minutes
Steam is available at 40 psig
Use two model TLAs
Step 1 Wm = 550 x 8.33 x 1.0 x 50/ = 208 Lb of steam required
Step 2 Qm = Lb steam per minute = 208/20 = 10.4 Lb steam per minute
Step 3 Are multiple units going to be used? If so how many? In this case, we will use two eductors. 10.4 Lb steam per minute/2 = 5.2 Lb/min per eductor
Step 4 S.F. = 5.2/13.4 = .39 desired S.F.
Step 5 Choose the model TLA 3/4" with a S.F. of .50 as this is the smallest unit that meets or exceeds the desired S.F.
Qm per unit = 13.4 x.50 = 6.7 Lb/Min
Qm for installation = 6.7 x 2 =13.4 Lb/Min
Time to heat tank = 208 Lb (Step 1)/13.4 = 15.5 minutes
If two TLAs (3/4" size) are installed and operated at 40 psig of steam pressure, they will heat the liquid in 15.5 minutes.
10
20
40
There are many advantages to using eductors for heating liquids in open vessels. These give the vessel heating eductor a place as a viable option for heating in many types of vessels.
The tank eductor heater provides direct contact of the steam into the liquid. This assures complete transfer of the energy in the steam into the liquid being heated. Other types of heating lose efficiency as the interior of the heat exchanger builds up a scale. With eductors, the velocity of the steam being injected into the vessel also causes the liquid contents of the vessel to be agitated while heating occurs, without the need for other types of mixers in the vessel. This provides for more even heating of the vessel contents. They also permit the steam to be dispersed over more of the liquid volume, resulting in a more homogenous heating than with other methods of injecting steam.
These designs of eductors allow steam to be used from 10 to 140 PSIG for heating. Because of the nature of direct steam injection, heating vessels at atmospheric pressure beyond 140° F should not be attempted. Exceeding this temperature could result in uncondensed steam evolving from the liquid.
Computer optimized flow paths enable the tank eductor to maintain a high "pick-up ratio" (the ratio of fluid entrained to the motive fluid) while maximizing the hydraulic efficiency (the ratio of hydraulic power at the outlet of the tank eductor to the hydraulic power at the inlet) to generate an optimum flow field from the greatest flow amplification.
No moving parts in the sparger nozzle, minimizing maintenance expenses.
Optimum flow field enables more activity within the tank than competitive units without changing pumps.
Compact design and ease of mounting keeps the tank eductor from interfering with other tank equipment.
"In-tank" mounting eliminates need for costly, complex mounting structures above tanks.
The TLA & TLM can be used in a wide variety of open vessels or closed tanks.
Eliminates stratification and promotes a homogenous tank with relation to pH, temperature, solids or gas dispersion, and distribution of chemicals.
Produces a unique agitation not available with other types of mixers, as the eductor can generate a directed flow field within the fluid being mixed including viscous fluids, slurries, and suspensions.
Easily mixes liquids of differing specific gravities and is excellent for scrubbing applications where a lower specific gravity fluid is driven into the higher one.
Flow amplification due to high "pick-up ratio" and hydraulic efficiency permits the use of smaller pumps, which translates to reduced costs of mixing or agitation.
Reduces investment cost because existing transfer pumps can be utilized for more than one purpose.
This coating is applied via electrostatic powder spray or fluidized powder bed. In addition to possessing the high chemical and temperature resistance which all fluoropolymers are noted for, Edathon's strengths, radiation resistance, wear resistance, and creep resistance are significantly greater than those of other fluoropolymers such as PTFE, FEP, or PFA.
The standard tank eductor models for heating in vessels are the TLA, TLM and ULJ. The model TLA and TLM are well suited to providing strong tank agitation while heating. Compared with other heaters, the cost per application is small. The model ULJ is designed to provide vigorous circulation of the liquid with low pressure steam inputs.
Sparger Nozzles should be located with the outlet pointed toward the most remote portion of the tank to provide the best agitation possible.
Tank eductor offers an inexpensive, yet highly effective way to improve circulation, agitation and heating of liquids in tanks.
The TLA & TLM are a ejector-type jet, requiring no nipple, recommended for tanks in a multiple of installations.
What is the tank liquid? (If it is not water (Sg =1.0, Sh =1.0), contact us.)
What temperature rise (AT) is needed?
What is the final tank temperature?
What is the vessel capacity?
Time available to heat the vessel (t)?
Steam pressure available?
Step 1 To determine the amount of steam required to heat the liquid in the vessel, multiply the gallons in the vessel to be heated x 8.33 x Sg x Sh x temperature rise delta T desired, divided by (BTUs per Lb steam). Lb steam required (Wm) = Gal x 8.33 x Sg x Sh x delta T/
Step 2 To calculate the flow of steam required per minute, divide the steam flow from Step 1 by the time you need to complete the heating process. Lb steam per minute (Qm)= Wm/minutes (t)
Step 3 If multiple units are going to be used, divide the number from Step 2 by the number of units to be used.
Step 4 Go to the Steam Flow table. Find the amount of steam flow Qm (Lb/Min) at the steam pressure available. This is the steam flow for a 1-1/2" unit. Take the steam flow obtained in Step 3 divided by the steam flow from the Steam Flow table. This will give the Sizing Factor (S.F.) needed to heat the vessel in the time required.
S.F. = Desired Steam Flowrate/ Saturated Steam Flowrate
Step 5 Choose the eductor size that has at meets or exceeds the number determined in Step 4
The temperature rise desired is ?T = 50°F
The final tank temperature is 120°F
The vessel holds 550 gallons
The time to heat it is 20 minutes
Steam is available at 40 psig
Use two model TLAs
Step 1 Wm = 550 x 8.33 x 1.0 x 50/ = 208 Lb of steam required
Step 2 Qm = Lb steam per minute = 208/20 = 10.4 Lb steam per minute
Step 3 Are multiple units going to be used? If so how many? In this case, we will use two eductors. 10.4 Lb steam per minute/2 = 5.2 Lb/min per eductor
Step 4 S.F. = 5.2/13.4 = .39 desired S.F.
Step 5 Choose the model TLA 3/4" with a S.F. of .50 as this is the smallest unit that meets or exceeds the desired S.F.
Qm per unit = 13.4 x.50 = 6.7 Lb/Min
Qm for installation = 6.7 x 2 =13.4 Lb/Min
Time to heat tank = 208 Lb (Step 1)/13.4 = 15.5 minutes
If two TLAs (3/4" size) are installed and operated at 40 psig of steam pressure, they will heat the liquid in 15.5 minutes.
10
20
40
60
80
100
120
140
Steam Flow, Qm (lb/Min)
6.4
8.8
13.4
18.3
22.8
27.4
31.9
36.5
Size Dimension A Dimension B Dimension C Dimension D IN (mm) IN (mm) IPS (mm) IN (mm) 3/8" 5.00 (127) 2.50 (64) 3/8 MNPT (10) .50 (12) 3/4" 7.25 (184) 3.69 (94) 3/4 MNPT (20) .81 (20) 1-1/2" 10.88 (276) 5.50 (140) 1-1/2 FNPT (40) 1.12 (28) 2" 14.50 (368) 7.69 (195) 2 FNPT (50) 1.62 (41) 3" 22.00 (559) 11.75 (298) 3 FNPT (80) 2.50 (63) 4" 25.00 (635) 12.00 (305) 4 FLGD (100) 3.00 (76) 6" 35.00 (889) 25.00 (635) 6 FLGD (150) 4.50 (114) 8" Contact Us for Data On Units Over 8 "
Since the flotation process is interaction between particles and air bubbles, the greater the concentration of hydrophobic particles and available air bubble surface, the more effective the process. In practical terms, the concentration of particles is limited to the maximum viscosity that allows a homogeneous distribution of ascending bubbles at a uniform rate and to the maximum acceptable hydrophilic entrainment in the froth. In turn, the amount of air is limited to the maximum flow rate that still provides a homogeneous distribution of rising bubbles without excessive turbulence and bubble collapse.
In order to optimize flotation for a specific aeration rate, the air sparging system must produce small bubbles. The small bubbles provide higher surface area, which is favorable for flotation kinetics. This effect has been shown in several studies. (Finch and Dobby, ; Gorain, ; Zhou, )
In the past few decades, the main evolution of column flotation technology has occurred in the development of new sparger systems. Sparger systems are essential in pneumatic flotation since both aeration and particle suspension depend on them.
The main criteria to be considered when developing or choosing spargers are:
Column spargers can be classified according to either their position in the column or the phenomenon involved in bubble generation. In terms of position, they are classified as internal if they are inserted into the column, or external if they are assembled outside the column tank.
In terms of bubble generation principles, most commercial spargers for columns create bubbles either by cavitation, or by direct injection of air (jetting).
In jetting techniques, air is injected into the column at high velocities and bubbles are formed by the intense shear of the air jet with the pulp (Finch, ). The higher the intensity of the air injection, the higher the number of bubbles and the smaller their size.
60
80
100
120
140
Steam Flow, Qm (lb/Min)
6.4
8.8
13.4
18.3
22.8
27.4
31.9
36.5
Size Dimension A Dimension B Dimension C Dimension D IN (mm) IN (mm) IPS (mm) IN (mm) 3/8" 5.00 (127) 2.50 (64) 3/8 MNPT (10) .50 (12) 3/4" 7.25 (184) 3.69 (94) 3/4 MNPT (20) .81 (20) 1-1/2" 10.88 (276) 5.50 (140) 1-1/2 FNPT (40) 1.12 (28) 2" 14.50 (368) 7.69 (195) 2 FNPT (50) 1.62 (41) 3" 22.00 (559) 11.75 (298) 3 FNPT (80) 2.50 (63) 4" 25.00 (635) 12.00 (305) 4 FLGD (100) 3.00 (76) 6" 35.00 (889) 25.00 (635) 6 FLGD (150) 4.50 (114) 8" Contact Us for Data On Units Over 8 "
Since the flotation process is interaction between particles and air bubbles, the greater the concentration of hydrophobic particles and available air bubble surface, the more effective the process. In practical terms, the concentration of particles is limited to the maximum viscosity that allows a homogeneous distribution of ascending bubbles at a uniform rate and to the maximum acceptable hydrophilic entrainment in the froth. In turn, the amount of air is limited to the maximum flow rate that still provides a homogeneous distribution of rising bubbles without excessive turbulence and bubble collapse.
In order to optimize flotation for a specific aeration rate, the air sparging system must produce small bubbles. The small bubbles provide higher surface area, which is favorable for flotation kinetics. This effect has been shown in several studies. (Finch and Dobby, ; Gorain, ; Zhou, )
In the past few decades, the main evolution of column flotation technology has occurred in the development of new sparger systems. Sparger systems are essential in pneumatic flotation since both aeration and particle suspension depend on them.
The main criteria to be considered when developing or choosing spargers are:
Column spargers can be classified according to either their position in the column or the phenomenon involved in bubble generation. In terms of position, they are classified as internal if they are inserted into the column, or external if they are assembled outside the column tank.
In terms of bubble generation principles, most commercial spargers for columns create bubbles either by cavitation, or by direct injection of air (jetting).
In jetting techniques, air is injected into the column at high velocities and bubbles are formed by the intense shear of the air jet with the pulp (Finch, ). The higher the intensity of the air injection, the higher the number of bubbles and the smaller their size.
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