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Andrea Heins , Ramón Veiga , Carlos Ruiz , Andrés Riera
Fouling in preheat networks of crude distillation units (CDU) plays an important role in energy consumption. In this work a procedure to monitor the performance of the heat exchanger network (HEN) and to optimize the cleaning is presented.
The procedure is based on a rigorous simulation of the HEN using Hysys (from Aspen Technology). The simulation is used to estimate the service overall heat transfer coefficient with real operational data acquired from the unit's Plant Information System (PI). The clean overall heat transfer coefficient is calculated for each one of the individual heat exchangers with a rigorous simulation using TASC (rigorous heat exchanger simulator also from Aspen Technology), embedded into Hysys. A comparison between the service and clean overall heat transfer coefficients provides the actual performance for each individual heat exchanger and for the complete HEN.
The first step is to collect the HEN operative data from the Plant Information System and to perform an ad-hoc pre- processing of each individual exchanger data (i.e., feed and product inlet and outlet temperatures and flow rates) in order to identify stable periods from which the mentioned calculations will be performed. As the feed/products flow rates and unit operating conditions are constantly changing, the steady intervals detection is a very important task because calculations performed with data of unstable operation time intervals could be erroneous and produce non-sense results.
The overall procedure is managed from an Excel environment, which performs the needed calls to PI and Hysys/TASC simulators in order to calculate each exchanger fouling and HEN overall performance under the actual fouling situation. Excel also commands the evaluation of the cleaning policies economics, searching between several pre- defined cleaning alternatives.
Results of the above mentioned methodology applied to a complex feed preheat HEN of the Topping IV CDU of REPSOL YPF Luján de Cuyo Refinery, Argentina, are presented.
In the refining industry, the heat exchangers used for energy recovery suffer a progressive heat transfer efficiency loss due to fouling. The immediate consequences of this loss are a major consumption of energy in the furnaces and, in certain cases, the need to reduce throughput to compensate the low efficiency of the preheat train. In addition, Atmospheric and Vacuum units represent between 35% and 40% of the total process energy consumption in a refinery. Due to this, any saving that could be achieved in these units will have a great impact in reducing operating costs and greenhouse effect related gaseous emission.
The main objective of this work is to develop and implement a methodology to perform the heat exchangers network monitoring and cleaning optimisation, as well as the evaluation of the economic impact due to cleaning strategies. Also, to implement the software and information architecture needed to carry on those tasks in a periodic, routine and non-attended way.
The methodology was developed based on a particular case study for Topping IV Unit, at REPSOL YPF Luján de Cuyo Refinery, located in Mendoza Province, Argentina.
The first stage of the study consisted of a pre-processing of the historical data available to assure that the information to be used in the calculations belonged to a "stable" operating period of the Unit and that they did not contain gross measurements errors.
Initially it was considered the possibility of classify the quality of the information and stability of the process using statistical criteria (standard deviation) or the range calculated from maximum and minimum during a given period. They were collected from the historical information average on a daily basis, but after reviewing them, poor results were observed, possibly due to the accumulative effect of the disturbances suffered by the Plant along the day. As a consequence, it was decided to collect data on a shorter basis (every 1 minute) to detect process steady periods to perform the calculations. Also, the usage of standard deviation as a possible index of steadiness detection was discarded, because it turned out to be a poor tool for detecting signal stability (as steady state refers). Standard deviation was more related to the signal noise than to its steadiness.
The steadiness of each time interval is defined using the range (maximum - minimum) during the period of study and a criterion of stability defined for every particular variable. The average values of all the variables, during the stable periods, are calculated in a space corresponding to a certain fraction of the given interval. For example, if the stability period lookup was for 2 hours, the average values were calculated for the last 30 minutes of this period.
As a second stage of data checking, once steadiness was detected, heat balances are calculated for both sides of every heat exchanger. The goal is to check if the heat exchanged on each side match. As a reference, it was pointed out that a type J thermocouple has a range from 0 to 750 oC, with an uncertainty of 2.25 oC and that the rates measured by plate orifice have an uncertainty of 5 % (Tonin et al.). Therefore, the major total uncertainty in the heat duty calculation of each side is 7.5 %. Considering this previous value, the maximum technically expected error would be 15 %. Heat differences between both sides of the exchanger bigger than this percentage can indicate that the measurements would not be acceptable for calculations. This acceptance percentage was considered in our methodology as a starting value, but other percentages can be used for gross errors detection. In fact, for some particular equipment, the heat calculation errors can be significantly bigger than the mentioned 15 % due to diverse factors (for example, errors in both flow and temperature measurements bigger than the technically expected maximum percentage).
Several software tools were developed to execute all the steps and necessary calculations for the project implementation. The objective was that the whole sequence, from data collection and validation, up to the heat exchangers train simulations and fouling factors calculation, as well as the results write back again in the PI system, could be performed automatically. The tasks sequence is controlled from a main application developed in Visual Basic and embedded in Excel. The calculation sequence is initiated from the VB application every time the procedure is executed (daily or weekly) according to a user defined frequency.
The presented methodology involves the building of a single Hysys simulation file containing the model needed to perform the required calculations. Hysys model includes the necessary information to carry on all the calculations, from the heat exchangers mechanical design and crude oil and products characterization up to the pre-flash column simulation that removes light compounds from crude, located before the last section of HEN, prior to the feed furnace.
In the calculation steps where a more rigorous simulation of the heat exchangers is necessary, TASC is invoked from the Hysys model.
The application manager performs, as first task, the data collection from PI, the detection of the steady periods and calculation of the average values to be used into the calculations.
The stability information is stored in files that were created by the automated data process applications. These files look like the one shown in Fig. 1.
The required information to execute the model runs is provided in another Excel spreadsheet where this information will be loaded to allow the interaction between the application and the simulator (Fig. 2).
Also, an output information template is filled up with the results of the execution to be retrieved. Fig. 3 exemplifies the columns results.
As a first step for heat exchanger fouling monitoring the actual global heat transfer coefficients (Ua) are usually calculated over time. Then, calculation of the fouling factor Rf is carried out, comparing the former with the value of U corresponding to the clean equipment (Uc).
In our methodology, a time varying Uc will be estimated for each exchanger from the inlet conditions of shell and tubes sides (rates and inlet temperatures of both fluids). Therefore, Uc will not remain constant in time, because process conditions are constantly changing or modified (different rates and inlet temperatures as consequence of changes in the unit operation).
The data processing sequence and calculations carried out by the application are as follows:
Evaluation of cleaning alternatives. Impact evaluation for a given set of a-priori defined cleaning alternatives in terms of energy consumption in the furnace. This is done activating and deactivating Hysys model lines from the main Excel application where calculation for the equipments involved in each case study are defined. Files containing the different cleaning alternatives economical impact are generated.
The methodology mentioned in step 4. above includes the following steps:
a. Average heat duty calculation for each heat exchanger
Simple heaters / coolers in the Hysys model are used to calculate the heat exchanged through each side of all the equipments. The comparison between the heats of hot and cold sides is externally done, from the Excel embedded application manager.
The overall exchanged heat should be calculated by the average of both sides but, as mentioned before, errors above the technically expected 15% maximum could appear. Therefore, a confidence factor (Cf) is used in the calculation. If Cf=1, the heat duty calculated for the crude side is more reliable. If Cf =0 the confidence is 100% on the product side heat duty calculation. If Cf is near 1 the temperatures calculated during the overall heat exchanger train simulation for the crude side will be more similar to the measured ones, but the fouling factor calculation will be more disperse (see Fig. 16 on Results section). The confidence factor is a user defined parameter that must be configured for each one of the heat exchangers.
b. Clean global heat transfer coefficient calculation using rigorous simulation
To calculate the clean global heat transfer coefficient, a rigorous simulation is employed. TASC rigorous simulator is used for this step, with actual rates and inlet temperatures given as input for each heat exchanger, defining a fouling factor equal to 0.0. The "clean" outlet temperatures are calculated and the Uc is reported. It is equivalent to calculate the individual film heat transfer coefficients for each side of the heat exchanger.
c. Actual global heat transfer coefficient
The actual global heat transfer coefficient (Ua) needed to exchange the average heat duty estimated in a) is calculated using the Adjust operation in Hysys and a simple model for heat exchangers.
d. Fouling factor calculation
The fouling factors for each piece of equipment are calculated with the actual and clean global heat transfer coefficients determined in b) and c), respectively.
The cleaning cases have been pre-programmed in advance supposing the heat exchangers can be one by one individually cleaned, cleaned by pairs or groups or all the train simultaneously. The objective is to determine the impact of cleaning on the inlet temperature of the furnace and so, on the energy consumption of the unit.
The simulation case is the one that includes the complete HEN with the values of Ua calculated in step c), except for those heat exchangers that are being cleaned. In this cases Uc are used, but this value is not necessarily the U corresponding to deep clean condition (Rf=0.0), because the fouling factor after cleaning depends on the cleaning method. Even the Uc or Rf values after cleaning can be fixed by the user, and a good reference could be the Ua value obtained for each equipment after a given cleaning procedure, calculated from historical data.
The methodology developed in this project was applied to the particular case of Topping IV CDU at REPSOL YPF Luján de Cuyo Refinery. This Unit has an 18 heat exchangers train used to preheat the crude before the feed furnace. The process diagram of the HEN is shown in Fig. 4, 5 and 6.
The white triangles represent existing rate measurements, and the yellow ones are temperature measures.
Heat exchangers previous to desalter:
Between desalter and pre-flash column:
Between preflash column (flashed crude) and furnace:
In all cases there are redundant temperature measurements, the average was assumed.
Several views of the Hysys model developed for this case study are presented:
In the first line simple heaters / coolers are used to calculate the duty exchanged on both sides of each heat exchanger.
In line #2 there is rigorous simulation models calling TASC, to calculate the Uc under actual operation conditions.
In line #3, the Ua needed to exchange the actual duty is calculated using the available Adjust operations in Hysys.
Finally, line #4, where overall HEN is simulated, is used to evaluate the impact of cleaning cases on the inlet furnace temperature.
For a tags collection list (approximately 70 existing tags in PI) chosen from the Topping IV diagram, data was collected once a minute since January 2005 up to January 2007. Raw data was inspected and analyzed in order to determine an appropriate period of time in which maximum, minimum, range, average and stability could be calculated properly (e.g., 120 minutes).
Fig. 7 shows an example corresponding to two days of April, 2005, data collection period for the CE-1 heat exchanger. Red vertical lines show periods of detected steadiness.
Grey bands in Fig. 7 show the 120 minutes intervals where steadiness for a particular heat exchanger was detected. It could be seen that data was stable during those periods (more or less horizontal flat lines) while unstable zones did not fulfilled the detection criteria.
In Fig. 8 two months of data (June / July, 2005) are shown for all of the CE-6E heat exchanger tags. Vertical lines show stable operation periods. As it could be noticed, a big variables values variation is produced during the considered period. There is a region where steady points were not detected, approximately in the first third of the above mentioned period; it could be noted by the vertical lines and grey zones absence.
Fig. 9 shows a detailed portion of Fig. 8, corresponding to the final third of the 2 months period initially presented. Simultaneous steadiness periods of 1 hour have been highlighted. For the overall explored period, all the variables averages to be used in the Rf calculation for this heat exchanger were calculated. It could be noticed that the methodology used, based in the range of each variable, was able to detect periods where the curves are flat (steady) and discard others where the curves have notorious variations.
The results obtained by the methodology application to the Case Study are the following.
An ad-hoc calculation procedure was developed to inspect all the sampled data and find the steady periods. The steadiness for all the variables related to a given heat exchanger was simultaneously searched. The range (i.e., maximum minus minimum value) of a given moving back horizon time period was inspected. A given tolerance was defined for each tag or variable. Once all the variables (typically, 2 flow-rates and 4 temperatures per heat exchanger) were found to be stable, the proper average value is calculated at a fraction of the assumed moving period. For a Crude Unit, 120 minutes period was used because such a period is approximately the time needed to reach steady state after a disturbance.
As an example, in Fig. 10 can be shown the calculated fouling factors for CE-2B heat exchanger during March / August, 2006 period. Black squares correspond to constant, equally spaced data, every 23 hrs, without stability estimation. White squares correspond to calculations performed during steady periods detected with the above described methodology. It can be clearly seen the non-steady samples calculated points (black squares) are much more disperse that the others. Encircled are the calculated points with the higher and notorious differences with respect to the stable (steady) periods. In this particular heat exchanger, the use of stability considerations to search the steady data samples helps to calculate smoother and coherent fouling factors.
Similarly, on a long term plot, as presented in Fig. 11 for the heat exchanger CE-5A, the fouling factors calculated under a period of more than one year using stable samples do not show noise. The calculations using equally spaced samples show noise and a bigger dispersion.
In the next figures, the effect of a chemical cleaning on Heat Exchangers CE-5C and CE-5D is shown. The effect of such a cleaning was clearly captured by our proposed methodology. It is interesting to note how much smoother both plots are after the cleaning, especially for heat exchanger CE-5C, whose plot was noisy in the time period previous to the cleaning.
Also, Fig. 13 shows the effect of cleaning on CE-4AB.
To produce a trend for the heat exchangers fouling factors involves usually the calculation of the actual global heat transfer coefficients (Ua) over time and comparing them with the design clean heat transfer coefficient (Uc). This Uc should only be valid for process conditions similar to those of design, but not for others. Under our methodology, however, Uc is not supposed to remain constant but updated based on the current process conditions (feed rates and inlet temperatures).
Comparison between fouling factors calculated with a constant overall heat transfer coefficient (black squares) versus our methodology (white squares) is shown in Fig. 14, where some periods of time with very different noise and variability of both trends can be seen (Periods 1 and 2).
In the next figures, the effect of a chemical cleaning on Heat Exchangers CE-5C and CE-5D is shown. The effect of such a cleaning was clearly captured by our proposed methodology. It is interesting to note how much smoother both plots are after the cleaning, especially for heat exchanger CE-5C, whose plot was noisy in the time period previous to the cleaning. Also, Fig. 13 shows the effect of cleaning on CE-4AB.
Also, moving averages smoothing trends have been plotted (continuous lines). It can be shown how smoother the plot of our proposed calculation methodology is against the one that uses a "fixed nominal" global heat transfer coefficient to compute the fouling factor. During Period 1, the statistical variance of fouling calculated by the traditional method was 10 times higher than the variance of our proposed calculation. During period 2 it was 4 times higher.
Similar smoothness curves can be see for exchanger CE-6BC, as shown in Fig. 15 (note the smoother averaging curves for our proposed calculation methodology).
Every heat exchanger can be provided with a confidence factor as a configuration parameter as part of the proposed calculation methodology. This value is used to evaluate the overall heat duty based on the individually calculated duties for both sides of the equipment (shell and tubes). Several calculations over the analyzed period were made to evaluate the confidence factor influence on the fouling factor (Rf) calculation, concluding that calculation dispersion is lower when confidence factor is nearest to 0.50. Dispersion was evaluated based on the global transfer coefficient standard deviation.
Due to real time data uncertainties, duty calculated differences will result in a mismatch between calculated temperatures and actual process data. The error propagates from one piece of equipment to the other, perhaps giving, at the end of the train, as a result of accumulated effects, a big error on the furnace inlet temperature calculation. As one of the main objectives of this work is to predict heat exchangers cleaning influence on the furnace inlet temperature, seems to be a good practice to use confidence factors between 0.5 and 1.0, preferably close to 1.0 (i.e., more confidence on crude side temperatures). Choosing the confidence factor close to 1.0 will tend to minimize the furnace inlet temperature calculation mismatch.
A methodology within an industrial, practical application framework, as opposite to an academic theoretical treatment, was developed. The calculation methodology and procedures used both already available commercial standard software and several pieces of ad-hoc programmed routines. In particular, REPSOL YPF has corporate network licenses of the commercial software used and no extra cost in licenses was incurred.
Processing a good portion of the historic data already stored in the plant information system provided a good representation of the HEN fouling factors evolution during time and the historical cleaning procedures and effects were very well identified.
Performing the calculations with data from stable, steady periods, generated less disperse and more coherent results, minimizing the impact of process instability on the calculated fouling factors.
The data and results for individual heat exchangers must be analyzed particularly for each case, with engineering criteria, to determine the confidence factor that better fits each exchanger.
The proposed methodology of calculating the Uc from actual process conditions, instead of using an Uc design value, generates fouling factors curves with no variations due to changes in unit operation (rates and temperatures different from design).
To have confidence calculations for fouling factors allows the user to simulate the complete HEN under different cleaning scenarios in order to choose the one with major economic benefit.
Future work will try to find a practical way to predict fouling factors trends over time using the historically calculated data. This prediction would be used to analyze different future cleaning scenarios, anticipate the need of cleanings and evaluate their economic impact.
Heavy Gas Oil
Light Gas Oil
Global heat transfer coefficient
Vacuum Light Gas Oil
F. dos Santos Liporace and S. Gregório de Oliveira, 2005, June 5 – 10, Real time fouling diagnosis and heat exchanger performance, ECI Symposium Series, Volume RP2: Proceedings of 6th International Conference on Heat Exchanger Fouling and Cleaning, Kloster Irsee, Germany.
H. Rodera, D.L. Westphalen, H.K. Shethna, 2003, A methodology for improving heat exchanger network operation, Applied Thermal Engineering 23.
P .C. T onin, C.O. Negrão, L.G. Lima, 2003, An approach for monitoring the thermal performance of heat exchanger network, Proc. 2o Congresso Brasileiro de P&D em Petróleo e Gás, Rio de Janeiro, June 2003.
L.G. Lima, C.O. Negrão, 2003, The effect of Thermophysical Properties of Work Fluids on the Heat Exchanger Effectiveness (in Portuguese), Procedures of the VII Scientific and Technological Initiation Seminar of CEFETPR, pp. 180-183, 13-15/Aug, Curitiba, Brazil
D. Palmerio, 2004, Estudio de Performance de un Tren de Intercambio de Calor, XIX AADECA, Buenos Aires.
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