International Journal of Chemical Engineering

International Journal of Chemical Engineering / 2010 / Article
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Quality and Pollution Control Technologies for Water, Air, and Soil

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Research Article | Open Access

Volume 2010 |Article ID 967853 | https://doi.org/10.1155/2010/967853

Ala'a Abdulrazaq Jassim, "Assessment of the Performance of Membranes Type Koch in Hartha Power Plant", International Journal of Chemical Engineering, vol. 2010, Article ID 967853, 5 pages, 2010. https://doi.org/10.1155/2010/967853

Assessment of the Performance of Membranes Type Koch in Hartha Power Plant

Academic Editor: Evans Chirwa
Received14 Jul 2009
Accepted28 Jan 2010
Published01 Apr 2010

Abstract

This paper deals with the assessment of the performance of reverse osmosis membranes type (TFC-Koch) model (8822XR-365) which are used in water desalination unit in Hartha power plant, one of the electrical power plant in the south Iraq. This unit has a capacity of 100  withdraws water from Shat Al-Arab River as a raw water having total dissolved solid (TDS)  ppm, and consists of two stages with total recovery and salt rejection of about 60% and 95%, respectively. The first array contains twelve vessels and the second six vessels. Each vessel contains six elements, 8 inches in diameter and 40 inches in length. The performance of the reverse osmosis (RO) membranes is based on surveying the chemical analysis of different ions present in water for both permeate and rejected streams from the unit log book, and only those readings where the overall recovery was 60% were selected. The results depicted that the reduction of membrane efficiency is attributed to the membrane blockage due to scaling and fouling. Under high fouling conditions the permeate flow rate is reduced and accordingly a high feed pressure is required to produce the design flow rate of permeate or percent recovery. A simulation of the behavior of RO membranes was conducted using standard Saehane software and compared with predicted model that was developed by the same authors. The results revealed that the reduction in water flow in both elements one and two in each vessel in the first array is attributed to the high permeate water flux through these two elements beyond the operation limits. Accordingly it is necessary to replace these two elements or change their position relative to other elements periodically.

1. Introduction

Membrane technology has become of great interest for treatment of different feeds. Depending on the membrane types, materials in the feed and process conditions, the membrane loses its performance with time. A reverse osmosis (RO) desalination system has many advantages in point of saving energy and less installation spaces and has become a favored technology for the production of fresh water.

In Basrah, one of the major industrial cites in the southern Iraq, RO is predominately utilized for the production of desalted water both for drinking and industry including Hartha power plant. This plant has RO unit of capacity 100 m3/h and withdraws water from Shat AL-Arab River with TDS3000 ppm.

It is well known that RO system of recoveries higher than 50% requires more than one stage in order not to exceed the single element recovery limit. Usually two arrays will suffice for recoveries up to 75% [1], however, three arrays must be used for higher recoveries up to 87.5%. The rejected water from the first stage is fed to the second stage, while the permeates from all vessels are combined to form the product. Recently, most of RO units use double-pass systems rather than single pass, the advantage of this arrangement is as follows[2].

(1)Production cost for fresh water is reduced by around 15%.(2)Unit installation space is reduced.(3)Unit capacity can be easily expanded up to around 15% by only adding a second stage array.(4)Disposal of brine water is reduced to about two thirds.

The performance of RO system is influenced by feed pressure, feed water composition, temperature, and percent recovery. For example, a feed temperature drop of C will cause a decrease of permeates flow of about 10% [2].

AbdulSattar et al. [3] studied the effect of applied pressure on the performance of two types of membranes; Koch type (8822-XR) and Saehane type (RE8040BE). They showed that the amount of permeate for Saehane membranes is larger than that for Koch membranes by about 26%. Abdul Sattar et al. [4] developed a mathematical model for evaluating the performance of RO unit using various types of membranes. El-Manharawy and Hafez [5] studied the effect of percent recovery and feed concentration on the design of RO units.

In this work the effect of operation time on the performance of Koch membranes type (8822-XR) was studied. The assessments of membranes performance based on water analysis of different ions concentration in both permeate and rejected water with 60% recovery were considered. The study covered two years of plant operation. A complete set of operating data including permeate flow rates for each array, permeate flux, permeate TDS, and feed pressure for each element were made available from the unit log books.

2. Plant Process Description

Feed water is pumped from Shat Al-Arab River to the sedimentation tank to precipitate the large suspended particles by the addition of ferric chloride FeCl3 and polyelectrolyte as a coagulant. The water is then pumped to the precipitator of the lime-soda ash process to remove carbonate hardness as shown by the following equations [6].

The lime-soda ash process can also reduce the silica concentration, due to the formation of aluminum and iron silicate calcium carbonate when ferric chloride is added as a coagulant [1]. Hypochlorite is added to remove the biological matter. The clarified water is collected in a tank having a capacity of about 50 m3. A booster pump (capacity of 180 m3/h and pressure of 5 bars) which draws water from the clarifier tank pumps it through an anthracite filter to remove any dissolved organics and chlorine in water. The output stream from the anthracite filter is collected in a special tank having a capacity of 500 m3. A centrifugal booster pump (capacity 165 m3/h and 5 bar pressure) draws water from the water tank and sends it to the polishing filter vessel (sand filter) to remove turbidity and any other impurities. Hydrochloric acid is added to the clarified water to adjust the pH so as to reduce the risk of precipitating soluble carbonate salts. Sodium hexametaphosphate (SHMP) is also added to the feed water prior to RO system to provide a further safety against scaling of the membrane by gypsum and other soluble salts. The treated water is passed through a microfilter (5 m) to remove small particles prior to pumping. The treated water to the RO membrane vessels utilizes a high pressure pump (capacity 165 m3/h and pressure 35 bars). Desalted water or permeate is collected in a service tank (capacity about 150 m3 ) while the waste or rejected water is treated prior to being discharged to the river. A process flow diagram is shown in Figure 1.

Al-Hartha RO unit consists of two stages, the first stage comprises of 12 vessels and the second 6 vessels where each vessel contains six elements (40 inches in length and 8 inches in diameter). The raw water is divided into 12 branches, one for each vessel. The first array of these vessels has a percent recovery of about 40%. The rejected water of the first array is fed to the second array which contains six vessels in parallel arrangement with a recovery of about 20%, which means that the total recovery of the unit is around 60%.

3. Results and Discussion

The aim of this work is to assess the performance of Koch membranes type (8822XR-365Koch) of USA origin, which is used in the reverse osmosis unit at the Hartha power plant.

The chemical analyses were derived from the log book of the unit, all having recoveries of 60%. Chemical analysis for (14) samples was collected from permeates and rejected streams.

The chemical compositions of the concentrated streams (rejected water) can be estimated from the material balance based on the composition of various ions in the feed water and the percent recovery. The Concentration factors as follows [1]:

where R is the percent recovery.

Table 1 shows the properties of Koch membranes type TFC-8822XR. Membrane efficiency depends on the variation of the ions concentration through the permeate stream which reflects membrane fouling and scaling problems, due to the deposition of such ions on the membrane surface.


Permeate flow rate (m3/d)34.1
Chloride rejection %99.7
Membrane area (m2)33.9
Maximum operation pressure (kpa)4140
Maximum operation temperature ( C)45
Maximum continuous feed chlorine (ppm) 0.1
Maximum differential pressure per element (kpa)69
Maximum differential pressure per vessel (kpa)414
Maximum feed turbidity NTU1
Maximum feed SDI5
Construction Spiral wound with fiberglass outer warp
Application Extra high rejection for brackish water treatment

Figures 2, 3, 4, 5, 6, and 7 show the concentration of profiles Ca+2, Mg+2, , , TH (Total Hardness), and TDS (Total Dissolved Solids) in mg/l for the permeate stream as a function of operation time in months. It can be seen that the concentrations of these various ions increase with time and they decrease and reach zero value after chemical cleaning.

The increase in the ions concentration in the permeate stream with operation time may be attributed to the membrane blocking by both calcium sulphate and organic substances. The effect of concentration polarization could be another reason for increased salinity in the permeate flow rate.

The effect of concentration polarization is specifically felt near the membrane surface and is considered as a major reason for the increased ions concentration in the permeate stream. The effect of concentration polarization increases osmotic pressure, leading to a reduction of net driving pressure differential across the membrane and hence reducing the product flow rate and increasing the scale potential. In order to compensate for such adverse effects, higher pressure should be applied. Table 2 shows the ions concentrations in the rejected stream, both experimentally and theoretically.


Ions concentration ppm
Theoretical valuesExperimental values

Ca+2Mg+2 Cl-1THTDSCa+2Mg+2 Cl-1THTDS

347.4302.6118618766507121444337164921117817418
386.832118132250707686043536199012887967590
405.3342.1181328137238476401333118226817348280
407.9339.5193129397478984401540143630419418316
365.8294.7178622396606966340291131821466316158
326.3255.3143917395815210364211106516715754488
439.5373.7213128348138631359309141820796636679
489.5426.3201831059169186582302115630179028659
610.5434.21713315810211053148936187212638506389
531.6471.117453126100211342464368105325748328560
415.8310.5170020537,26701531826599319285835227
510.5386.8160223559077676420276112013866965841
518.4352.618392552871809443633099222657666668
360.5278.9179219796606305396285110213866796060

A simulation run using Saehane software was conducted in order to investigate the performance of each individual element. It was observed that during the unit operation history, the performance of some membrane modules started to deteriorate with time due to scale formation and fouling deposition on the surface of the membranes. Cleaning therefore became necessary to improve the performance of the membranes. Cleaning gives a great improvement in both the quality and quantity of the permeate stream. This is evident from Figures 2,3,4,5,6, and 7 which show the improvement of membrane efficiency after chemical cleaning especially after three and six months of operation.

The cleaning agent, composed of 0.1% Sodium Triphosphate, 1% Na4 EDTA,s and 2% Citric Acid, was used for chemical cleaning to remove both organic and inorganic salts. Table 3 shows the overall properties for the influent streams from the arrays one and two, while Table 4 shows the theoretical results for each element using the program that was developed previously by the same authors [4]. Table 5 revealed the theoretical values for each element using Saehane software.


ArrayPressure barPermeate flow rate m3/hConcentrate flow m3/hPermeate TDS (ppm)Concentrate TDS (ppm)

114.877.282.819.214507
212.322.860.450.726164


ArrayEl. No.Feed Pressure barFeed m3/hPermeate m3/hRecoveryFeed TDS (ppm)Permeate TDS (ppm)

1114.8 13.31.20.093234212.4
214.312.11.20.096258014.6
313.810.91.10.101285317.2
413.49.81.00.106317020.4
513.18.81.00.111354224.5
612.97.80.90.117398229.6

2112.313.80.80.058450734.7
211.8130.70.056478240.6
311.312.30.70.053506147.5
410.811.60.60.950534255.6
510.4110.50.047562165.1
61010.50.50.044589776.5


ArrayEl. No.Feed Pressure barFeed m3/hPermeate m3/hRecoveryFeed TDS (ppm)Permeate TDS (ppm)

1115.513.91.20.093282.815.7
214.912.61.20.0933605.618.5
314.511.51.10.0963972.421.8
414.110.41.00.14392.525.8
513.79.31.00.1044877.130.8
613.48.40.90.1085440.037.0

2112.914.90.80.0536097.542.8
212.214.10.70.0516439.450.1
311.613.40.70.0486780.158.8
411.112.80.60.0447116.069.0
510.612.20.50.417443.281.1
610.211.70.40.0377757.995.6

The degradation of elements one and two for each vessel in the first array of the RO unit in Hartha power plant is attributed to the mechanical damage. This is due to the increasing of the permeate flux relative to the standard flux. Accordingly, the replacement of elements one and two or change of position relative to other elements is required to improve the permeate quality.

4. Conclusions

A simulation of the behavior of RO membranes was conducted using standard Saehane software and compared with predicted model that was developed by the authors. The results revealed that the reduction in water flow in both elements one and two in each vessel in the first array is attributed to the high permeate water flux through these two elements beyond the operation limits. Accordingly it is necessary to replace these two elements or change their position relative to other elements periodically.

References

  1. Technical Manual, Saehane Company, http://www.saehancsm.com/.
  2. M. Kurihara, H. Yamamura, and T. Nskanishi, “High recovery/high pressure membranes for brine conversion SWRO process development and its performance data,” Desalination, no. 125, p. 9, 1999. View at: Google Scholar
  3. K. AbdulSattar, S. Ismail, and A. A. Jassim, “Effect of different operation pressures for various membranes on the performance of RO plants,” Desalination, vol. 155, no. 3, pp. 287–291, 2003. View at: Publisher Site | Google Scholar
  4. K. AbdulSattar, S. Ismail, and A. A. Jassim, “Modeling of reverse osmosis systems,” Desalination, vol. 158, no. 1–3, pp. 323–329, 2003. View at: Publisher Site | Google Scholar
  5. S. El-Manharawy and A. Hafez, “Water type and guidelines for RO system design,” Desalination, vol. 139, no. 1–3, pp. 97–113, 2001. View at: Publisher Site | Google Scholar
  6. I. S. AL-Mutiz, M. A. AL-Ghunaimi, A. AL-Mutlag et al., “A comparison of theoretically calculated and actual chemical dose at water treatment plants,” in Proceedings of the 4th Gulf Water Conference, pp. 1–10, Manama, Bahrain, 1999. View at: Google Scholar

Copyright © 2010 Ala'a Abdulrazaq Jassim. This is an open access article distributed under the Creative Commons Attribution License, which permits unrestricted use, distribution, and reproduction in any medium, provided the original work is properly cited.


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