Selection and Design of Condensers
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 CHOICE OF COOLANT
5 LAYOUT CONSIDERATIONS
5.1 Distillation Column Condensers
5.2 Other Process Condensers
6 CONTROL
6.1 Distillation Columns
6.2 Water Cooled Condensers
6.3 Refrigerant Condensers
7 GENERAL DESIGN CONSIDERATIONS
7.1 Heat Transfer Resistances
7.2 Pressure Drop
7.3 Handling of Inerts
7.4 Vapor Inlet Design
7.5 Drainage of Condensate
8 SUMMARY OF TYPES AVAILABLE
8.1 Direct Contact Condensers
8.2 Shell and Tube Exchangers
8.3 Air Cooled Heat Exchangers
8.4 Spiral Plate Heat Exchangers
8.5 Internal Condensers
8.6 Plate Heat Exchangers
8.7 Plate-Fin Heat Exchangers
8.8 Other Compact Designs
9 BIBLIOGRAPHY
FIGURES
1 DIRECT CONTACT CONDENSER WITH INDIRECT COOLER FOR RECYCLED CONDENSATE
2 SPRAY CONDENSER
3 TRAY TYPE CONDENSER
4 THREE PASS TUBE SIDE CONDENSER WITH INTERPASS LUTING FOR CONDENSATE DRAINAGE
5 CROSS FLOW CONDENSER WITH SINGLE PASS COOLANT
An overview of distillation column design concepts and major design considerations. Explains distillation column design concepts, what you would provide to a professional distillation column designer, and what you can expect back from a distillation system design firm. To speak with an engineer about your distillation column project, call EPIC at 314-207-4250.
Selection and Design of Condensers
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 CHOICE OF COOLANT
5 LAYOUT CONSIDERATIONS
5.1 Distillation Column Condensers
5.2 Other Process Condensers
6 CONTROL
6.1 Distillation Columns
6.2 Water Cooled Condensers
6.3 Refrigerant Condensers
7 GENERAL DESIGN CONSIDERATIONS
7.1 Heat Transfer Resistances
7.2 Pressure Drop
7.3 Handling of Inerts
7.4 Vapor Inlet Design
7.5 Drainage of Condensate
8 SUMMARY OF TYPES AVAILABLE
8.1 Direct Contact Condensers
8.2 Shell and Tube Exchangers
8.3 Air Cooled Heat Exchangers
8.4 Spiral Plate Heat Exchangers
8.5 Internal Condensers
8.6 Plate Heat Exchangers
8.7 Plate-Fin Heat Exchangers
8.8 Other Compact Designs
9 BIBLIOGRAPHY
FIGURES
1 DIRECT CONTACT CONDENSER WITH INDIRECT COOLER FOR RECYCLED CONDENSATE
2 SPRAY CONDENSER
3 TRAY TYPE CONDENSER
4 THREE PASS TUBE SIDE CONDENSER WITH INTERPASS LUTING FOR CONDENSATE DRAINAGE
5 CROSS FLOW CONDENSER WITH SINGLE PASS COOLANT
An overview of distillation column design concepts and major design considerations. Explains distillation column design concepts, what you would provide to a professional distillation column designer, and what you can expect back from a distillation system design firm. To speak with an engineer about your distillation column project, call EPIC at 314-207-4250.
Heat/light/electrical energy is out today’s necessity and has scarcity also. Energy conservation is key requirement of any industry at all times.
In general, industries use heat energy for conservation of raw material to finished product. The source of heat energy is generally saturated or super heated steam. The steam generation is common use one boiler with carity of fuels. Whatever may be the fuel the generation should be as economy as possible which adds to the product cost. Further the usage of steam and recycling steam condensate back to boiler is an art depending on plant layouts.
In this project the steam generator is water tube boiler fired with rice husk. The steam is transferred to the tyre/tube moulds where tyres/tubes are cured while the heat is rejected to the tyres the condensate forms and this condensate is put back to the boiler. While doing so the steam is also stopped back to boiler without rejecting complete heat to the product. This gets flashed into atmosphere at feed water tank. The science of separation of condensate from steam saves energy. Better the separation more the fuel conservation.
In the steam generator the fuel is burnt to heat the water and form steam. This fuel burnt flue gas carries lot of energy, out through chimney. Prior to exhausting through the heat left in flue need to be recovered, through heat recovery mechanisms’. In this project an air-preheater condensate heat recovery unit is the major energy consuming station.
Types of Distillation & column internalsBharat Kumar
More:- https://chemicalengineeringworld.com
Distillation is a method of separating the components of a solution which depends upon distribution of the substances between a gas and liquid phase, applied to cases where all components are present in both phases.
* What is distillation ?
* Types of Distillation
* Batch Distillation
* Azeotropic Distillation
* Flooding
* Priming
* Coning
* Weeping
* Dumping
* Packed Column
* Tray column
* Reflux Ratio
* Relative volatility
* Distillation column
Distillation is a method of separating mixtures based on differences in volatility (volatility is the tendency of a substance to vaporize. Volatility is directly related to a substance's vapor pressure.) of components in a boiling liquid mixture. Distillation is a unit operation, or a physical separation process, and not a chemical reaction
Equilibrium Effects
- Methane Steam
- Water Gas Shift
Relationship of Kp to Temperature
Relationship of WGS Kp to Temperature
Effect of Temperature on Methane Slip
Approach to Equilibrium
Reaction Path and Equilibrium
Effect of Pressure Increase
Operating Parameters
- Pressure
- Temperature
- Feed Rate
- Steam to Carbon
Effect of Exit Temperature Spread
Useful Tools
Calculating ATM
Armfield Gas Absorption Column ExperimentHadeer Khalid
The absorption of CO2 from air to water was studied in Gas absorption column built by Armfield company. Lab report and experiment was part of Separation Lab.
Purpose
Key to good performance
Problem Areas
Catalysts, heat shields and plant up-rates
Burner Guns
Development of High Intensity Ring Burner
Case Studies
Conclusions
Why have a Secondary Reformer ?
Need nitrogen to make ammonia
Wish to make primary as small as possible
Wish to minimise methane slip since methane is an inert in the ammonia synthesis loop
Other methods of achieving this
Braun Purifier process
Can address all these with an air blown secondary
Slides for the eLearning course Separation and purification processes in biorefineries (https://open-learn.xamk.fi) in IMPRESS project (https://www.spire2030.eu/impress).
Subject: 2.4 Plate efficiencies.
HOT TOPIC
TON OF REFRIGERATION,
WORK, U FACTOR, LRA (Locked rotor amps)
RPM of motor, HEAT FORMULA, GAS PIPING (Sizing – CF/hr.), CALCULATING OIL NOZZLE SIZE (GPH):
PYTHAGOREAN THEOREM, Linear Measurement Equivalents (U.S. Conventional - SI Metric)
Heat/light/electrical energy is out today’s necessity and has scarcity also. Energy conservation is key requirement of any industry at all times.
In general, industries use heat energy for conservation of raw material to finished product. The source of heat energy is generally saturated or super heated steam. The steam generation is common use one boiler with carity of fuels. Whatever may be the fuel the generation should be as economy as possible which adds to the product cost. Further the usage of steam and recycling steam condensate back to boiler is an art depending on plant layouts.
In this project the steam generator is water tube boiler fired with rice husk. The steam is transferred to the tyre/tube moulds where tyres/tubes are cured while the heat is rejected to the tyres the condensate forms and this condensate is put back to the boiler. While doing so the steam is also stopped back to boiler without rejecting complete heat to the product. This gets flashed into atmosphere at feed water tank. The science of separation of condensate from steam saves energy. Better the separation more the fuel conservation.
In the steam generator the fuel is burnt to heat the water and form steam. This fuel burnt flue gas carries lot of energy, out through chimney. Prior to exhausting through the heat left in flue need to be recovered, through heat recovery mechanisms’. In this project an air-preheater condensate heat recovery unit is the major energy consuming station.
Types of Distillation & column internalsBharat Kumar
More:- https://chemicalengineeringworld.com
Distillation is a method of separating the components of a solution which depends upon distribution of the substances between a gas and liquid phase, applied to cases where all components are present in both phases.
* What is distillation ?
* Types of Distillation
* Batch Distillation
* Azeotropic Distillation
* Flooding
* Priming
* Coning
* Weeping
* Dumping
* Packed Column
* Tray column
* Reflux Ratio
* Relative volatility
* Distillation column
Distillation is a method of separating mixtures based on differences in volatility (volatility is the tendency of a substance to vaporize. Volatility is directly related to a substance's vapor pressure.) of components in a boiling liquid mixture. Distillation is a unit operation, or a physical separation process, and not a chemical reaction
Equilibrium Effects
- Methane Steam
- Water Gas Shift
Relationship of Kp to Temperature
Relationship of WGS Kp to Temperature
Effect of Temperature on Methane Slip
Approach to Equilibrium
Reaction Path and Equilibrium
Effect of Pressure Increase
Operating Parameters
- Pressure
- Temperature
- Feed Rate
- Steam to Carbon
Effect of Exit Temperature Spread
Useful Tools
Calculating ATM
Armfield Gas Absorption Column ExperimentHadeer Khalid
The absorption of CO2 from air to water was studied in Gas absorption column built by Armfield company. Lab report and experiment was part of Separation Lab.
Purpose
Key to good performance
Problem Areas
Catalysts, heat shields and plant up-rates
Burner Guns
Development of High Intensity Ring Burner
Case Studies
Conclusions
Why have a Secondary Reformer ?
Need nitrogen to make ammonia
Wish to make primary as small as possible
Wish to minimise methane slip since methane is an inert in the ammonia synthesis loop
Other methods of achieving this
Braun Purifier process
Can address all these with an air blown secondary
Slides for the eLearning course Separation and purification processes in biorefineries (https://open-learn.xamk.fi) in IMPRESS project (https://www.spire2030.eu/impress).
Subject: 2.4 Plate efficiencies.
HOT TOPIC
TON OF REFRIGERATION,
WORK, U FACTOR, LRA (Locked rotor amps)
RPM of motor, HEAT FORMULA, GAS PIPING (Sizing – CF/hr.), CALCULATING OIL NOZZLE SIZE (GPH):
PYTHAGOREAN THEOREM, Linear Measurement Equivalents (U.S. Conventional - SI Metric)
The presentation was on final year design project, "Production of LPG from NGLs and condensate". It includes process selection, establishing a flow diagram for the selected process, the sizing of main equipments, detailed design of four Major equipments along with P & ID control for the systems and finally the economic evaluation was conducted to check the feasibility of the process. The final product composition of LPG was simulated using Aspen HYSYS and found to be 49% Propane and 21% butane.
Enhanced Oil Recovery is a great of interest by researchers which divided to thermal and non-thermal methods. Thermal methods indicate the heat transfer to reservoir in order to decrease the viscosity of fluid reservoir and make it mobile.
This document explains on emulsion and emulsifiers ad their application in industry. Emulsifiers are used in cosmetic, personal care, pharma preparations, food applications, paints, oilfiled applications, defoamers, agricultural applications and cleaning compositions
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Sectoral targets and attacks as well as the cost of ransom
Global APT activity, AI usage, actor and tactic profiles, and implications
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In-depth analysis of the cyber threat landscape across North America, South America, Europe, APAC, and the Middle East
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Cyber risk predictions
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Systemic attacks in the Middle East
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https://sectrio.com/resources/ot-threat-landscape-reports/sectrio-releases-ot-ics-and-iot-security-threat-landscape-report-2024/
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Neuro-symbolic (NeSy) AI is on the rise. However, simply machine learning on just any symbolic structure is not sufficient to really harvest the gains of NeSy. These will only be gained when the symbolic structures have an actual semantics. I give an operational definition of semantics as “predictable inference”.
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Orchestrator execution result
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Leading Change strategies and insights for effective change management pdf 1.pdf
Process calculation condensation
1. Process Calculation: Condensation
Chandran Udumbasseri
Technical Consultant
chandran.udumbasseri@gmail.com.
Part II: Condensor / Shell & Tube Heat Exchanger
The vapours coming from the vapour column is condensed in
the Shell and Tube heat exchanger. Cooling water is used to
cool and condense the vapours. As water has fouling and
depositing character cooling water is passed through the tube.
Organic Vapour is allowed to enter from shell side of the
exchanger.
2. The design is for 1 shell pass Multi tube pass Heat
exchanger
Tube length 6ft
Tube OD ¾”
Pitch square
Tube pitch 1” - (3/4” + ¼”)
Baffle segmental
Tube side cooling water
Fouling factor 0.0002
Shell side organic vapour
Fouling factor 0.0002
Fouling factor coefficients
Medium Fauling factor
Coefficient Resistance
W/m2/C m2.C/W
Cooling water 4000-6000 0.0002-0.0003
Organic
vapour/liquid
5000 0.0002
Light hydrocarbon 5000 0.0002
Heavy hydrocarbon 2000 0.0005
Condensing
organics
5000 0.0002
Heating fluids 5000 0.0002
Steam 4000-10000 0.0001-0.0025
Refrigerating brine 3000-5000 0.0002-0.0003
3. Tube side fluids Shell side fluids
Corrosive fluids
Coolin water
Fouling fluids
Less viscous liquids
High pressure steam
Hotter fluids
Condensing vapour
Fluids with large temperature
difference
Hot fluid (TEA vapour condensation)
Inlet temperature (T1) 192.2o
F (89o
C)
Outlet temperature (T2) 113o
F (45o
C)
Cold fluid (Chilled water)
Initial temperature, t1 50o
F (10o
C)
Outlet temperature t2 104o
F (40o
C)
Pressure of hot vapours 15psi
Pressure of cold fluid 50psi
Fluid (TEA) properties
Viscosity, ft/lb/hr (cP) 0.24395
Density, lb/cu ft 45.2915
Specific heat capacity Btu/lb/ft 0.4551
Specific gravity 0.7255
Thermal conductivity of TEA 1.003 Btu/sq ft.hr/F
Cooling water
Sp gravity 62.43 lb/cu ft
4. Viscosity 2.42lb/ft/hr (1cP)
Specific heat, 1.001 Btu/lb/ft
Thermal conductivity, 0.3455 Btu/sq ft/F
Calculation
Energy balance – No heat loss
Qcw= Qtea = mcw x Cpcw x (t2-t1) = mtea x Cptea x (T1-T2)
Boil up (mtea)= 1410.218Kg/hr= 3108.12 lbs/hr
Cptea = 0.4551Btu/lb/ft
T2 = 113o
F
T1 = 192.2o
F
CW requirement = ?
Cpcw = 1.001 Btu/lb/ft
t1 = 50o
F
t2 = 104o
F
Qtea = 3108.12 x 0.4551 x (192.2-113)
Qcw =? x 1.001x (104 – 50)
5. Flow rate of Cooling water =2072.53lbs/hr
Heat transfer area
Assumption
1.Fixed tubes
2. Outer diameter of tube = ¾”
3.Length of tube = 6ft
4.Tube ID = 0.584”
5.Cooling water is in the tube side
Log mean temperature correction factor
=1.467
= 0.38
FT =
6. Log mean temperature correction factor FT,
FT =0.857
LMTD
=65.8o
F
Heat Transfer Area
It is necessary to assume a value for overall heat
transfer coefficient. For industrial condensers for
organic solvent cooling, using cooling water the overall
heat transfer coefficient, the given range of value in
the below table is 100 to 200 BTU/hr-sq ft.F
7. Overall Heat Transfer Coefficient Table-Condenser
(Engineering Edge website)
Cold fluid Hot fluid Overall U
BTU/hr-sq ft/o
F
Water Steam (pressure) 350-750
Water Steam (vacuum) 100-600
Water/brine Organic solvent(saturated,
atmospheric)
100-200
Water/brine Organic
solvent(atmospheric, high
non condensation)
20-80
Water/brine Organic solvent (saturated,
vacuum)
50-120
Water/brine Organic solvent (Vacuum,
high non condensation)
10-50
Water/brine Aromatic
vapour(atmospheric non
condensation)
5-30
Water Low boiling hydrocarbon
(atm)
80-200
Water High boiling hydrocarbon
(vacuum)
10-30
Assume the OHTC (Ua) as 100 Btu/hr.sq ft.o
F
8. =19.86 sq ft
No of tubes required
Tube length 12’
Tube OD ¾’ (0.75”)
=8.43 =~ 8 tubes
Renaults No, Re
CW mass = 2072.53lbs/hr
No of pass (np)= 4
No of tubes (nt)= 8
ID (di) = 0.584”
Viscosity of cooling water,µ = 2.42 lb/ft/hr
9. Renaults No, Re
Re =11208.67 > 104
Fluid velocity (<1m)
=8927.80ft/hr =2.48ft/sec =0.78m/sec
u = 0.78m/sec,<1m/sec (result acceptable)
Tube side Heat transfer Coefficient
From graph JH Tube-side 44 at Re 11000
Tube side Heat Transfer Curve (D.Q.KERN)
JH= 44 (from graph)
10. Tube side heat transfer coefficient, ht = ?
Internal diameter of tube, di = 0.584”
Heat capacity of water, Cp = 1.001Btu/lb/ft
Viscosity of water, µcw = 2.42 lb-sec/sq ft
Thermal conductivity of water,
k = 0.3455 BTU/hr/sq ft/o
F
ht = 598.40 BTU/ft/hr/F
Shell side Heat transfer coefficient
Baffle 25% cut
11. Baffle spacing B = 0.5D = 4”
Equivalent diameter=
Pt = 1”
do = ¾”
De = 0.0795ft
C -= Pt-do = 1-3/4 = ¼ = 0.25”
Shell ID, Ds = 8”
Baffle spacing, B = 0.5 Ds = 0.5x 8 = 4”
Shell side cross flow area = ar =
0.056ft
Renaults No, Re – calculation
Mass velocity, G
12. =3108/0.056 = 55500 lb/sq ft/hr
Renailts No, Re =
=18086.7
Shell Side heat transfer curve (D.Q.KERN)
The last term in the equation is equated =1
13. Equivalent diameter of shell, De = 0.0795ft
Thermal conductivity of organic vapour, K = 1.003
BTU/hr/sq ft/F
Viscosity of organic vapour, µ = 0.24345 lb-sec/sq ft
Heat capacity of organic vapour, Cp = 0.4551 Btu/lb/ft
Organic vapour = triethyl amine
=587.19 Btu/sq ft/hr/F
Overall heat transfer coefficient, U
Stainless steel is used as tube material (MOC) with
thermal conductivity, 25Btu/sq ft/hr/F.
AO/AI= (0.75/0.584)2
= 1.649
(do-di)/2x25 = (0.75-0.584)/50 = 0.00332
1.649xx0.00332 = 0.00547
1/ht = 1/598 = 0.00167
1.649/587.19 = 0.0026
14. AO/AI x0.001 = 1.649x0.001 = 0.001649
= 0.00167 + 0.0005 + 0.00547 + 0.0026 + 0.001649 = 0.011889
(0.011889)-1
= 84 Btu/sq ft/hr/o
F
(100 – 84.8)x100/84.8 = 17.92%
Tube side pressure drop
Tube clearance = 0.25”
Baffle spacing = 4”
Cross area = (0.267x8)/(4x144) = 0.0037sq ft
Mass velocity =2072/0.0037 = 560000 lb/sq f/hr
Tube side frictional factor curve (D.Q.KERN)
15. Frictional factor at Re 11208
=0.00026sq ft/sq in
=0.00026 x 144 sq ft/sq ft
Frictional pressure drop Tube side
Ø is equated to =1
=1.56psi
Return loss
np = 6
Mass velocity = G = 560000lb/ sq ft/hr
S = 0.988
Δp = 0.44psi
P + Δp = 1.56 +0.44 = 2 psi < 10psi
16. Frictional pressure drop - Shell side
Clearance = 0.25”; Baffle spacing = 4”
Mass velocity = G = 55500 lb/sq ft/hr
Re = 18086.7
Shell side frictional factor curve (D.Q.KERN)
Friction factor = 0.0018x144 = 0.2592 sq ft/sq ft
No of baffles, nb,= 12/(4/12)=36
P = 0.46psi
17. Shell side pressure drop = 0.46psi <7psi
Overdesign:
The required total surface area of all tubes
= 3.14 x (3/4) x (1/12) x 12 x 8.43 = 19.85 sq ft
Design surface area
== 3.14 x (3/4) x (1/12) x12 x 8 = 18.85 sq ft
Difference % on required = 5.08% <10%
So the design is within requirement
Condenser Specification
Tube: = fixed
Tube size
OD = 3/4”
ID = 0.584”
Tube length = 12ft
MOC = SS316
No of tubes = 8
No of tube passes = 6
Tube pitch = square
18. Pitch length = 1”
Shell size
ID = 8”
MOC = ss
Shell length = 12ft
Baffles = 25% cut segments
Spacing = 4”
No of baffles = 36
Reference
1.PROCESS HEAT TRANSFER: D.Q.KERN: (Graphs,
curves, table information, equations and
formulas)
2.Engineering Edge site: for data tables