Meta Data

Проект документа:

Пересмотр более раннего документа?:

Год вступления в силу:

2001

Виды актов по количеству участников:

National

Тип документа:

Guideline

Экономический сектор:

Energy

Виды энергоресурсов:

All, Other

Подготовлен:

Bureau of Energy Efficiency

Источник:

Bureau of Energy Efficiency

Ссылка на документ:

Energy Performance Assessment of Heat Exchangers Guidebook

Сводный обзор:

The Energy Performance Assessment of Heat Exchangers Guidebook is a guidebook for the energy performance assessment of heat exchangers.

Full Document Text

NOTE: Some content may not display correctly, including tables and figures. See PDF for full details.

4. ENERGY PERFORMANCE ASSESSMENT OF HEAT EXCHANGERS

4.1 Introduction

Heat exchangers are equipment that transfer heat from one medium to another. The proper design, operation and maintenance of heat exchangers will make the process energy efficient and minimize energy losses. Heat exchanger performance can deteriorate with time, off design operations and other interferences such as fouling, scaling etc. It is necessary to assess periodically the heat exchanger performance in order to maintain them at a high effi- ciency level. This section comprises certain proven techniques of monitoring the perfor- mance of heat exchangers, coolers and condensers from observed operating data of the equipment.

4.2 Purpose of the Performance Test

To determine the overall heat transfer coefficient for assessing the performance of the heat exchanger. Any deviation from the design heat transfer coefficient will indicate occurrence of fouling.

4.3 Performance Terms and Definitions

Overall heat transfer coefficient, U

Heat exchanger performance is normally evaluated by the overall heat transfer coefficient U that is defined by the equation.

When the hot and cold stream flows and inlet temperatures are constant, the heat transfer coefficient may be evaluated using the above formula. It may be observed that the heat pick up by the cold fluid starts reducing with time.

Nomenclature

A typical heat exchanger is shown in figure 4.1 with nomenclature.

Heat duty of the exchanger can be calculated either on the hot side fluid or cold side fluid as given below.

Heat Duty for Hot fluid, Q_h = W_x C_ph x (T_i–T_o)......................... Eqn–1,

Heat Duty for Cold fluid, Q_c = wx C_pc x ( t_o–t_i)........................... Eqn–2

If the operating heat duty is less than design heat duty, it may be due to heat losses, fouling in tubes, reduced flow rate (hot or cold) etc. Hence, for simple performance monitoring of exchanger, efficiency may be considered as factor of performance irrespective of other para- meter. However, in industrial practice, fouling factor method is more predominantly used.

4.4 Methodology of Heat Exchanger Performance Assessment

4.4.1 Procedure for determination of Overall heat transfer Coefficient, U at field

This is a fairly rigorous method of monitoring the heat exchanger performance by calculating the overall heat transfer coefficient periodically. Technical records are to be maintained for all the exchangers, so that problems associated with reduced efficiency and heat transfer can be identified easily. The record should basically contain historical heat transfer coefficient data versus time / date of observation. A plot of heat transfer coefficient versus time permits ratio- nal planning of an exchanger-cleaning program.

The heat transfer coefficient is calculated by the equation U = Q / (A x LMTD)

Where Q is the heat duty, A is the heat transfer area of the exchanger and LMTD is tem-

perature driving force.

The step by step procedure for determination of Overall heat transfer Coefficient are described below

Density and viscosity can be determined by analysis of the samples taken from the flow stream at the recorded temperature in the plant laboratory. Thermal conductivity and specific heat capacity if not determined from the samples can be collected from handbooks.

4.4.2 Examples

Liquid - Liquid Exchanger

A shell and tube exchanger of following configuration is considered being used for oil cool- er with oil at the shell side and cooling water at the tube side.

Tube Side

460 Nos x 25.4mmOD x 2.11mm thick x 7211mm long
Pitch - 31.75mm 30° triangular
2 Pass
787 mm ID
Baffle space - 787 mm
1 Pass

Shell Side

Heat Duty: Actual duty differences will be practically negligible as these duty differences could be because of thespecific heat capacity deviation with the temperature. Also, there could be some heat loss due to radiation from the hot shell side.

Pressure drop: Also, the pressure drop in the shell side of the hot fluid is reported normal (only slightly less than the design figure). This is attributed with the increased average bulk temperature of the hot side due to decreased performance of the exchanger.

Temperature range: As seen from the data the deviation in the temperature ranges could be due to the increased fouling in the tubes (cold stream), since a higher pressure drop is noticed.

Heat Transfer coefficient: The estimated value has decreased due to increased fouling that has resulted in minimized active area of heat transfer.

Physical properties: If available from the data or Lab analysis can be used for verification with the design data sheet as a cross check towards design considerations.

Troubleshooting: Fouled exchanger needs cleaning.

b. Surface Condenser

A shell and tube exchanger of following configuration is considered being used for Condensing turbine exhaust steam with cooling water at the tube side.

Tube Side

20648 Nos x 25.4mmOD x 1.22mm thk x 18300mm long Pitch - 31.75mm 60° triangular

1 Pass

The monitored parameters are as below:

Parameters	Units	Inlet	Outlet
Hot fluid flow, W	kg/h	939888	939888
Cold fluid flow, w	kg/h	55584000	55584000
Hot fluid Temp, T	°C	No data	34.9
Cold fluid Temp, t	°C	18	27
Hot fluid Pressure, P	m Bar g	52.3 mbar	48.3
Cold fluid Pressure, p	Bar g	4	3.6

Calculation of Thermal data:

Area = 27871 m²

Duty:

Q = q_S + q_L

Hot fluid, Q = 576990 kW Cold Fluid, Q = 581825.5 kW

Hot Fluid Pressure Drop

Pressure Drop = P_i – P_o = 52.3 – 48.3 = 4.0 mbar.

Cold Fluid Pressure Drop

Pressure Drop = p_i – p_o = 4 – 3.6 = 0.4 bar.

Temperature range hot fluid

Temperature Range DT = T_i– T_o = No data

Temperature Range Cold Fluid

Temperature Range Dt = t_i – t_o = 27 – 18 = 9 °C.

Capacity Ratio

Capacity ratio, R = Not significant in evaluation here.

Effectiveness

Effectiveness, S = (t_o – t_i) / (T_i – t_i) = Not significant in evaluation here.

LMTD

Calculated considering condensing part only

a). LMTD, Counter Flow = ((34.9 – 18)–(34.9–27))/ ln ((34.9–18)/(34.9–27))

= 11.8 deg C.

b). Correction Factor to account for Cross flow F = 1.0.

Corrected LMTD

MTD = F x LMTD = 1.0 x 11.8 = 11.8 deg C.

Heat Transfer Co-efficient

Overall HTC, U = Q/ A DT = 576990/ (27871 x 11.8) = 1.75 kW/m². K

Comparison of Calculated data with Design Data

Parameters	Units	Test Data	Design Data
Duty, Q	kW	576990	588430
Hot fluid side pressure drop, DP_h	mBar	4 mbar	3.7 mbar
Cold fluid side pressure drop, DPc	Bar	0.4
Temperature Range hot fluid, DT	°C
Temperature Range cold fluid, Dt	°C	(27–18) = 9	(28–19) = 9
Capacity ratio, R	-----
Effectiveness, S	-----
Corrected LMTD, MTD	°C	11.8	8.9
Heat Transfer Coefficient, U	kW/(m². K)	1.75	2.37

Pressure drop: The condensing side operating pressure raised due to the backpressure caused by the non-condensable. This has resulted in increased pressure drop across the steam side

Temperature range: With reference to cooling waterside there is no difference in the range however, the terminal temperature differences has increased indicating lack of proper heat transfer.

Heat Transfer coefficient: Heat transfer coefficient has decreased due to increased amount of non-condensable with the steam.

Trouble shooting: Operations may be checked for tightness of the circuit and ensure proper venting of the system. The vacuum source might be verified for proper functioning.

C. Vaporizer

A shell and tube exchanger of following configuration is considered being used for vaporizing chlorine with steam at the shell side.

Tube Side

200 Nos x 25.4mmOD x 1.22mm thick x 6000mm long Pitch - 31.75mm 30° triangular

2 Pass

Area = 95.7.m²

The monitored parameters are as below:

Parameters	Units	Inlet	Outlet
Hot fluid flow, W	kg/h	5015	5015
Cold fluid flow, w	kg/h	43500	43500
Hot fluid Temp, T	°C	108	108
Cold fluid Temp, t	°C	30	34
Hot fluid Pressure, P	Bar g	0.4	0.3
Cold fluid Pressure, p	Bar g	9	8.8

Calculation of Thermal data:

Duty:

Q = q_S + q_L

Hot fluid, Q = 3130 kW

Cold Fluid, Q = q_S + q_L = 180.3 kW + 2948 kW = 3128.3 kW

Hot Fluid Pressure Drop

Pressure Drop = P_i – P_o = 0.4 – 0.3 = 0.1 bar

Cold Fluid Pressure Drop

Pressure Drop = p_i – p_o = 9 – 8.8 = 0.2 bar.

Temperature range hot fluid

Temperature Range DT = T_i – T_o = 0 °C

Temperature Range Cold Fluid

Temperature Range Dt = t_i – t_o = 34 – 30 = 4 °C.

Capacity Ratio

Capacity ratio, R = Not significant in evaluation here.

Effectiveness

Effectiveness, S = (t_o – t_i) / (T_i – t_i) = Not significant in evaluation here.

LMTD

Calculated considering condensing part only

a). LMTD, Counter Flow =((108 – 30)–(108–34))/ ln ((108–30)/(108–34)) = 76 °C.

b). Correction Factor to account for Cross flow F = 1.0.

Corrected LMTD

MTD = F x LMTD = 1.0 x 76 = 76 °C.

Heat Transfer Co-efficient

Overall HTC, U = Q/ A DT = 3130/ (95.7 x 76) = 0.43 kW/m². K

Comparison of Calculated data with Design Data

Parameters	Units	Test Data	Design Data
Duty, Q	kW	3130	3130
Hot fluid side pressure drop, DP_h	Bar	0.1	Neg
Cold fluid side pressure drop, DP_c	Bar	0.2
Temperature Range hot fluid, DT	°C
Temperature Range cold fluid, Dt	°C	4	4
Capacity ratio, R	-----
Effectiveness, S	-----
Corrected LMTD, MTD	°C	76
Heat Transfer Coefficient, U	kW/(m². K)	0.42	0.44

Heat Duty: There is no difference inferred from the duty as the exchanger is performing as per the requirement

Pressure drop: The steam side pressure drop has increased in spite of condensation at the steam side. Indication of non-condensable presence in steam side

Temperature range: No deviations

Heat Transfer coefficient: Even at no deviation in the temperature profile at the chlorine side, heat transfer coefficient has decreased with an indication of overpressure at the shell side. This indicates disturbances to the condensation of steam at the shell side. Non-condensable suspect- ed at steam side.

Trouble shooting: Operations may be checked for presence of chlorine at the shell side through tube leakages. Observing the steam side vent could do this. Alternately condensate pH could be tested for presence of acidity.

d. Air heater

A finned tube exchanger of following configuration is considered being used for heating air with steam in the tube side.

The monitored parameters are as below:

Parameters	Units	Inlet	Outlet
Hot fluid flow, W	kg/h	3000	3000
Cold fluid flow, w	kg/h	92300	92300
Hot fluid Temp, T	°C	150	150
Cold fluid Temp, t	°C	30	95
Hot fluid Pressure, P	Bar g
Cold fluid Pressure, p	mBar g	200 mbar	180 mbar

Calculation of Thermal data:

Bare tube Area = 42.8 m²; Fined tube area = 856 m² 1.Duty:

Hot fluid, Q = 1748 kW

Cold Fluid, Q = 1726 kW

Hot Fluid Pressure Drop Pressure Drop = P_i – P_o =Neg
Cold Fluid Pressure Drop

Pressure Drop = p_i – p_o = 200–180 = 20 mbar.

Temperature range hot fluid

Temperature Range DT = T_i – T_o = Not required.

Temperature Range Cold Fluid

Temperature Range Dt = t_i – t_o = 95 – 30 = 65 °C.

Capacity Ratio

Capacity ratio, R = Not significant in evaluation here.

Effectiveness

Effectiveness, S = (t_o – t_i) / (T_i – t_i) = Not significant in evaluation here.

LMTD

Calculated considering condensing part only

a). LMTD, Counter Flow =((150 – 30)–(150–95)/ ln ((150–30)/(150–95)) = 83.3 °C.

b). Correction Factor to account for cross flow F = 0.95

Corrected LMTD

MTD = F x LMTD = 0.95 x 83.3 = 79 °C.

Overall Heat Transfer Co-efficient (HTC)

U = Q/ A DT = 1748/ (856 x 79) = 0.026 kW/m². K

Comparison of Calculated data with Design Data

Parameters	Units	Test Data	Design Data
Duty, Q	kW	1748	1800
Hot fluid side pressure drop, DP_h	Bar	Neg	Neg
Cold fluid side pressure drop, DP_c	Bar	20	15
Temperature Range hot fluid, DT	°C
Temperature Range cold fluid, Dt	°C	65	65
Capacity ratio, R	-----
Effectiveness, S	-----
Corrected LMTD, MTD	°C	79	79
Heat Transfer Coefficient, U	kW/(m². K)	0.026	0.03

Heat Duty: The difference inferred from the duty as the exchanger is under performing than required

Pressure drop: The airside pressure drop has increased in spite of condensation at the steam side. Indication of choking and dirt blocking at the airside.

Temperature range: No deviations

Heat Transfer coefficient: Decreased because of decreased fin efficiency due to choking on air side.

Trouble shooting: Operations may be checked to perform pulsejet cleaning with steam / blow air jet on air side if the facility is available. Mechanical cleaning may have to be planned dur- ing any down time in the immediate future.

4.4.3 Instruments for monitoring:

The test and evaluation of the performance of the heat exchanger equipment is carried out by measurement of operating parameters upstream and downstream of the exchanger. Due care needs to be taken to ensure the accuracyand correctness of the measured parameter. The instru- ments used for measurements require calibration and verification prior to measurement.

Parameters	Units	Instruments used
Fluid flow	kg/h	Flow can be measured with instruments like Orifice flow meter, Vortex flow meter, Venturi meters, Coriollis flow meters, Magnetic flow meter as applicable to the fluid service and flow ranges
Temperature	°C	Thermo gauge for low ranges, RTD, etc.
Pressure	Bar g	Liquid manometers, Draft gauge, Pressure gauges Bourdon and diaphragm type, Absolute pressure transmitters, etc.
Density	kg/m³	Measured in the Laboratory as per ASTM standards, hydrometer, etc
Viscosity	MpaS	Measured in the Laboratory as per ASTM standards, viscometer, etc.
Specific heat capacity	J/(kg.K)	Measured in the Laboratory as per ASTM standards
Thermal conductivity	W/(m.K)	Measured in the Laboratory as per ASTM standards
Composition+	%wt (or) % Vol	Measured in the Laboratory as per ASTM standards using Chemical analysis, HPLC, GC, Spectrophotometer, etc.

4.4.4 Terminology used in Heat Exchangers

Terminology	Definition	Unit
Capacity ratio	Ratio of the products of mass flow rate and specific heat capacity of the cold fluid to that of the hot fluid. Also computed by the ratio of temperature range of the hot fluid to that of the cold fluid. Higher the ratio greater will be size of the exchanger
Co current flow exchanger	An exchanger wherein the fluid flow direction of the cold and hot fluids are same
Counter flow exchanger	Exchangers wherein the fluid flow direction of the cold and hot fluids are opposite. Normally preferred
Cross flow	An exchanger wherein the fluid flow direction of the cold and hot fluids are in cross

Density	It is the mass per unit volume of a material	kg/m³
Effectiveness	Ratio of the cold fluid temperature range to that of the inlet temperature difference of the hot and cold fluid. Higher the ratio lesser will be requirement of heat transfer surface
Fouling	The phenomenon of formation and development of scales and deposits over the heat transfer surface diminishing the heat flux. The process of fouling will get indicated by the increase in pressure drop
Fouling Factor	The reciprocal of heat transfer coefficient of the dirt formed in the heat exchange process. Higher the factor lesser will be the overall heat transfer coefficient.	(m².K)/W
Heat Duty	The capacity of the heat exchanger equipment expressed in terms of heat transfer rate, viz. magnitude of energy or heat transferred per time. It means the exchanger is capable of performing at this capacity in the given system	W
Heat exchanger	Refers to the nomenclature of equipment designed and constructed to transmit heat content (enthalpy or energy) of a comparatively high temperature hot fluid to a lower temperature cold fluid wherein the temperature of the hot fluid decreases (or remain constant in case of losing latent heat of condensation) and the temperature of the cold fluid increases (or remain constant in case of gaining latent heat of vaporisation). A heat exchanger will normally provide indirect contact heating. E.g. A cooling tower cannot be called a heat exchanger where water is cooled by direct contact with air
Heat Flux	The rate of heat transfer per unit surface of a heat exchanger	W/ m²
Heat transfer	The process of transport of heat energy from a hot source to the comparatively cold surrounding
Heat transfer surface or heat Transfer area	Refers to the surface area of the heat exchanger that provides the indirect contact between the hot and cold fluid in effecting the heat transfer. Thus the heat transfer area is defined as the surface having both sides wetted with one side by the hot fluid and the other side by the cold fluid providing indirect contact for heat transfer	m2
Individual Heat transfer Coefficient	The heat flux per unit temperature difference across boundary layer of the hot / cold fluid film formed at the heat transfer surface. The magnitude of heat transfer coefficient indicates the ability of heat conductivity of the given fluid. It increases with increase in density, velocity, specific heat, geometry of the film forming surface	W/( m².K)

LMTD Correction factor	Calculated considering the Capacity and effectiveness of a heat exchanging process. When multiplied with LMTD gives the corrected LMTD thus accounting for the temperature driving force for the cross flow pattern as applicable inside the exchanger
Logarithmic Mean Temperature difference, LMTD	The logarithmic average of the terminal temperature approaches across a heat exchanger	°C
Overall Heat transfer Coefficient	The ratio of heat flux per unit difference in approach across a heat exchange equipment considering the individual coefficient and heat exchanger metal surface conductivity. The magnitude indicates the ability of heat transfer for a given surface. Higher the coefficient lesser will be the heat transfer surface requirement	W/(m².K)
Pressure drop	The difference in pressure between the inlet and outlet of a heat exchanger	Bar
Specific heat capacity	The heat content per unit weight of any material per degree raise/fall in temperature	J/(kg.K)
Temperature Approach	The difference in the temperature between the hot and cold fluids at the inlet / outlet of the heat exchanger. The greater the difference greater will be heat transfer flux	°C
Temperature Range	The difference in the temperature between the inlet and outlet of a hot/cold fluid in a heat exchanger	°C
Terminal temperature	The temperatures at the inlet / outlet of the hot / cold fluid steams across a heat exchanger	°C
Thermal Conductivity	The rate of heat transfer by conduction though any substance across a distance per unit temperature difference	W/(m².K)
Viscosity	The force on unit volume of any material that will cause per velocity	Pa

QUESTIONS
1.	What is meant by LMTD ?
2.	Distinguish between heat exchanger efficiency and effectiveness.
3.	Explain the terms heat duty and capacity ratio.
4.	What is meant by fouling?
5.	List five heat exchangers used in industrial practice.
6.	What are the parameters, which are to be monitored for the performance assessment of heat exchangers?
7.	In a heat exchanger the hot stream enters at 70°C and leaves at 55°C. On the other side the cold stream enters at 30°C and leaves at 55°C. Find out the LMTD of the heat exchanger.
8.	In a condenser what type of heats are considered in estimating the heat duty? a) Latent Heat b) Sensible heat c) Specific heat d) Latent heat and sensible heat
9.	What is the need for performance assessment of a heat exchanger?
10.	The unit of overall coefficient of heat transfer is a) kCal/hr/m² °C b) kCal/kg °C c) kCal/m² hr d) kCal/hg m²

REFERENCES

"Process Heat Transfer" by D.Q.Kern, Edn. 1965.
"Modern Power Station Practice" - British Electricity International- Volume - G; Chapter - 7 - " Plant performance and performance monitoring.
Coulsons & Richardson's CHEMICAL ENGINEERING Volume 3 third edition
Scimod " Scientific Modeling Software", techno software International, India
Ganapathy. V, "Fouling factor estimated quickly", O&G Journal, Aug 1992.
Liberman, Norman P, Trouble shooting Process Operations, Penwell Books, Tulsa, Oklahoma