Project and Report (M.S.)--Virginia Polytechnic Institute and State University, 1991. / Vita. Abstract. Includes bibliographical references (leavese 77-78). Also available via the Internet.

Thesis (M. Sc.)--University of Hong Kong, 1993.

The electroplating industry has not evolved substantially over the years. Typically, the industry relies on experience as well as the common sense of its personnel to produce parts and to deal with any waste products that the plating process produces. With the heightened environmental awareness of the 1990s, past practices which produced acceptable treatment levels are no longer good enough. There are numerous methods for meeting the environmental laws of the 1990's. Technology can range from the simple to the complex. Several established methods for the electroplating industry are ion exchange, reverse osmosis, electrodialysis, ion flotation, sulfide precipitation and activated carbon. Internal waste reduction programs, discharging to publicly owned treatment works and zero discharge are as well viable options for the industry. With the combination of regulations and compliance scenarios facing today's etectroplating operations, it is necessary to define a protocol or methodology which will enable them to make economically feasible decisions as to what compliance option best fits with their corporate strategy. By doing so, the decision will allow them to continue to operate into the 21st century. The selection process must be flexible enough so that state of the art technologies are not the only solution. It must allow for multiperson evaluation of systems with multiattributes. This report represents the development and application of a methodology for evaluating different environmental compliance scenarios for the electroplating industry. The methodology was developed using the analytical hierarchy process, AHP. The strength of AHP lies in its ability to incorporate complex, multiattribute systems into a single decision making process which is robust enough to allow for multiperson evaluation. / Master of Science

No description available.

by Wong Suk Ying. / Thesis submitted in: November 2001. / Thesis (M.Phil.)--Chinese University of Hong Kong, 2002. / Includes bibliographical references (leaves 144-157). / Text in English; abstracts in English and Chinese. / by Wong Suk Ying. / Acknowledgments --- p.i / Abstract --- p.ii / Contents --- p.v / List of Figures --- p.x / List of Tables --- p.xvi / Chapter 1. --- INTRODUCTION --- p.1 / Chapter 1.1 --- Electroplating Industry in Hong Kong --- p.1 / Chapter 1.1.1 --- Typical stages in electroplating process --- p.1 / Chapter 1.1.1.1 --- Pre-treatment --- p.1 / Chapter 1.1.1.2 --- Electroplating --- p.3 / Chapter 1.1.1.3 --- Post-treatment --- p.3 / Chapter 1.1.2 --- Typical characteristics of wastestreams from electroplating industry --- p.3 / Chapter 1.2 --- Chemical Specific Approach against Toxicity Based Approach --- p.6 / Chapter 1.3 --- Ecotoxicological Study on Electroplating Effluent --- p.7 / Chapter 1.4 --- Toxicity Identification Evaluation --- p.8 / Chapter 1.4.1 --- Phase I: Toxicity Characterization --- p.9 / Chapter 1.4.2 --- Phase II: Toxicity Identification --- p.10 / Chapter 1.4.3 --- Phase III: Toxicity Confirmation --- p.12 / Chapter 1.5 --- Toxicity Identification Evaluation on Electroplating Effluent --- p.14 / Chapter 1.6 --- Selection of Organisms for Bioassays --- p.15 / Chapter 1.6.1 --- Organism used for toxicity identification evaluation --- p.17 / Chapter 2. --- OBJECTIVES --- p.20 / Chapter 3. --- MATERIALS AND METHODS --- p.21 / Chapter 3.1 --- Source of Samples --- p.21 / Chapter 3.2 --- Toxicity Identification Evaluation: Phase I Baseline Toxicity Test --- p.21 / Chapter 3.2.1 --- Microtox® test --- p.23 / Chapter 3.2.2 --- Growth inhibition test of a marine unicellular microalga Chlorella pyrenoidosa CU-2 --- p.25 / Chapter 3.2.3 --- Survival test of a marine amphipod Hylae crassicornis --- p.28 / Chapter 3.2.4 --- Survival test of a marine shrimp juvenile Metapenaeus ensis --- p.31 / Chapter 3.3 --- Toxicity Identification Evaluation: Phase I Toxicity Characterization --- p.34 / Chapter 3.3.1 --- pH adjustment filtration test --- p.35 / Chapter 3.3.2 --- Aeration test --- p.36 / Chapter 3.3.3 --- C18 solid phase extraction test --- p.37 / Chapter 3.3.4 --- EDTA chelation test --- p.38 / Chapter 3.3.5 --- Graduated pH test --- p.40 / Chapter 3.4 --- Toxicity Identification Evaluation: Phase II Toxicity Identification --- p.41 / Chapter 3.4.1 --- Filter extraction test --- p.41 / Chapter 3.4.2 --- Total metal content analysis --- p.42 / Chapter 3.5 --- Toxicity Identification Evaluation: Phase III Toxicity Confirmation --- p.43 / Chapter 3.5.1 --- Chemicals --- p.44 / Chapter 3.5.2 --- Mass balance test --- p.44 / Chapter 3.5.3 --- Spiking test --- p.44 / Chapter 4. --- RESULTS --- p.46 / Chapter 4.1 --- Chemical Characteristics of the Electroplating Effluent Samples --- p.46 / Chapter 4.2 --- Toxicity Identification Evaluation: Phase I Baseline Toxicity --- p.46 / Chapter 4.2.1 --- Toxicity of electroplating effluent samples on Microtox® test --- p.46 / Chapter 4.2.2 --- Toxicity of electroplating effluent samples on growth inhibition test of microalga Chlorella pyrenoidosa CU-2 --- p.46 / Chapter 4.2.3 --- Toxicity of electroplating effluent samples on survival test of amphipod Hyale crassicornis --- p.52 / Chapter 4.2.4 --- Toxicity of electroplating effluent samples on survival test of shrimp juvenile Metapenaeus ensis --- p.52 / Chapter 4.3 --- Toxicity Identification Evaluation: Phase I Toxicity Characterization --- p.52 / Chapter 4.3.1 --- Toxicity Characterization of electroplating effluent samples using Microtox® test --- p.56 / Chapter 4.3.2 --- Toxicity Characterization of electroplating effluent samples using microalgal growth inhibition test of Chlorella pyrenoidosa CU-2 --- p.59 / Chapter 4.3.3 --- Toxicity Characterization of electroplating effluent samples using survival test of amphipod Hyale crassicornis --- p.65 / Chapter 4.3.4 --- Toxicity Characterization of electroplating effluent samples using survival test of shrimp juvenile Metapenaeus ensis --- p.68 / Chapter 4.4 --- Toxicity Identification Evaluation: Phase II Toxicity Identification --- p.73 / Chapter 4.4.1 --- Metal analysis on the electroplating effluents --- p.75 / Chapter 4.4.2 --- Effect of filter extraction test on toxicity recovery of the electroplating effluent samples --- p.75 / Chapter 4.4.2.1 --- Microtox® test --- p.75 / Chapter 4.4.2.2 --- Growth inhibition test of microalga Chlorella pyrenoidosa CU-2 --- p.75 / Chapter 4.4.2.3 --- Survival test of amphipod Hyale crassicornis --- p.81 / Chapter 4.4.2.4 --- Survival test of shrimp juvenile Metapenaeus ensis --- p.90 / Chapter 4.4.3 --- Effect of filter extraction test on metal ions recovery of the electroplating effluent samples --- p.90 / Chapter 4.5 --- Toxicity Identification Evaluation: Phase III Toxicity Confirmation --- p.96 / Chapter 4.5.1 --- Mass balance test results on Microtox® test --- p.96 / Chapter 4.5.2 --- Mass balance test results on survival test of amphipod Hyale crassicornis --- p.104 / Chapter 4.5.3 --- Spiking test results on Microtox® test --- p.106 / Chapter 4.5.4 --- Spiking test results on survival test of amphipod Hyale crassicornis --- p.113 / Chapter 5. --- DISCUSSION --- p.118 / Chapter 5.1 --- Toxicity Identification Evaluation: Phase I Baseline Toxicity --- p.118 / Chapter 5.2 --- Toxicity Identification Evaluation: Phase I Toxicity Characterization --- p.119 / Chapter 5.2.1 --- pH adjustment filtration test --- p.119 / Chapter 5.2.2 --- Aeration test --- p.120 / Chapter 5.2.3 --- C18 solid phase extraction test --- p.120 / Chapter 5.2.4 --- EDTA chelation test --- p.120 / Chapter 5.2.5 --- Graduated pH test --- p.121 / Chapter 5.3 --- Toxicity Identification Evaluation: Phase II Toxicity Identification --- p.122 / Chapter 5.3.1 --- Metal analysis on the electroplating effluents --- p.122 / Chapter 5.3.2 --- Effect of filter extraction test on toxicity and metal ions recovery of the electroplating effluent samples --- p.123 / Chapter 5.3.3 --- Comparison between the concentrations of the metal ions in the electroplating effluent samples with the Technical Memorandum on standards for effluent discharged --- p.124 / Chapter 5.3.4 --- Comparison between the concentrations of the metal ions in the electroplating effluent samples with the toxicity of the metal ions reported in the literature --- p.124 / Chapter 5.3.4.1 --- Microtox® test --- p.126 / Chapter 5.3.4.2 --- Microalga --- p.126 / Chapter 5.3.4.3 --- Amphipod --- p.126 / Chapter 5.3.4.4 --- Shrimp --- p.126 / Chapter 5.4 --- Toxicity Identification Evaluation: Phase III Toxicity Confirmation --- p.131 / Chapter 5.4.1 --- Mass balance test on Microtox® test --- p.132 / Chapter 5.4.2 --- Mass balance test on survival test of amphipod Hyale crassicornis --- p.133 / Chapter 5.4.3 --- Spiking test on Microtox® test --- p.133 / Chapter 5.4.4 --- Spiking test on survival test of amphipod Hyale crassicornis --- p.134 / Chapter 5.5 --- Toxicity of the Metal Ions Identified as the Toxicants in the Electroplating Effluent --- p.135 / Chapter 5.5.1 --- Copper --- p.135 / Chapter 5.5.2 --- Nickel --- p.137 / Chapter 5.5.3 --- Zinc --- p.138 / Chapter 5.6 --- Summary --- p.140 / Chapter 6. --- CONCLUSIONS --- p.142 / Chapter 7. --- REFERENCES --- p.144 / Chapter 7.1 --- APPENDIXES --- p.158

Submitted in fulfilment of the requirements of the egree of Master of Technology: Chemical Engineering, Durban University of Technology, 2011. / The South African electroplating industry generates large volumes of hazardous waste water that has to be treated prior to disposal. The main source of this waste water has been the rinse system. Conventional end-ofpipe waste water treatment technologies do not meet municipality standards. The use of technologies such as membranes, reverse osmosis and ion exchange are impractical, mainly due to their cost and technical requirements. This study identified source point reduction technologies, close circuiting of the electroplating process, specific to the rinse system as a key development. Specifically the application of a low flow counter current rinse system for the recovery of the rinse water in the plating bath was selected. However, the recovery of the rinse tank water was impeded by the low rates of evaporation from the plating bath, which was especially prevalent in the low temperature operating plating baths. This master’s study proposes the use of an induced draft evaporative cooling tower for facilitation of evaporation in the plating bath. For total recovery of the rinse tank water, the rate of evaporation from the plating bath has to be equivalent to the rinse tanks make up water requirements. A closed circuit plating system mathematical model was developed for the determination of the mass evaporated from the plating bath and the cooling tower for a specified time and the equilibrium temperature of the plating bath and the cooling tower. The key criteria in the development of the closed circuit plating system model was the requirement of minimum solution specific data as this information is not readily available. The closed circuit plating system model was categorised into the unsteady state and steady state temperature regions and was developed for the condition of water evaporation only. The closed circuit plating system model was programmed into Matlab and verified. The key factors affecting the performance of the closed circuit plating system were identified as the plating solution composition and operational temperature, ambient air temperature, air flow rate and cooling tower iv packing surface area. Each of these factors was individually and simultaneously varied to determine their sensitivity on the rate of water evaporation and the equilibrium temperature of the plating bath and cooling tower. The results indicated that the upper limit plating solution operational temperature, high air flow rates, low ambient air temperature and large packing surface area provided the greatest water evaporation rates and the largest temperature drop across the height of the cooling tower in the unsteady state temperature region. The final equilibrium temperature of the plating bath and the cooling tower is dependent on the ambient air temperature. The only exception is that at low ambient air temperatures the rate of water evaporation from the steady state temperature region is lower than that at higher ambient air temperatures. Thus the model will enable the electroplater to identify the optimum operating conditions for close circuiting of the electroplating process. It is recommended that the model be validated against practical data either by the construction of a laboratory scale induced draft evaporative cooling tower or by the application of the induced draft evaporative cooling tower in an electroplating facility.

Theoretical waste minimisation opportunities and options for electroplating were sought from the literature. Their suitability under the specific site conditions of a chromium electroplating plant were evaluated using the results of a waste minimisation audit (audit). The audit showed that many waste minimisation practices were already in place. These included counter current flowing rinse systems, multiple use of rinses and recycling of the drag-out solution back into the plating solution. Two types of information were collected during the audit, namely new chemical monitoring (concentration levels of sodium, iron, zinc, copper, lead, chromium and nickel and conductivity, total dissolved solids and pH) and flow rate data and existing data (composition of the process solutions, products and waste outputs, and raw materials, workpieces and utility inputs). The data were analysed using four established waste minimisation techniques. The Scoping Audit and the Water Economy Assessment results were determined using empirically derived models while the Mass Balancing and the True Cost of Waste results were obtained through more detailed calculations. The results of the audit showed that the three most important areas for waste minimisation were water usage, effluent from rinse water waste streams and nickel consumption. Water usage has the highest waste minimisation potential followed by nickel. Dragged-out process chemicals and rinse water consumption contribute to ranking the effluent stream the most important waste minimisation opportunity identified by the True Cost of Waste Analysis. Potential financial savings were roughly estimated to be in the order of R 19949 and R 126603 for water and nickel respectively. Intervention using only "low cost-no-cost" waste minimisation measures was recommended as a first step before contemplating further focus areas or technical or economical feasibility. / Thesis (M.Sc.)-University of KwaZulu-Natal, Pietermaritzburg, 2004.

A chromium plating line used by a local company was monitored to identify any potential waste minimisation opportunities. Plating of the workpiece surface is carried out by immersing the workpiece in seven process (treatment) solutions including nickel and chromium plating baths. Between each process step the workpieces are rinsed. The chromium plating process was evaluated using the results of a waste minimisation audit. This involved gathering data on the composition, flow rates and costs of the inputs of the process. Two types of data were collected namely new and existing data. The new data included chemical monitoring (concentration levels of Ni, Cr, Na, S, B, P, Si, Fe, Cu, Zn, Pb as well as conductivity, TDS, SS and pH measurements) and water usage data. The existing data included raw materials, utility inputs, composition of process solutions and product outputs. The data were analysed using three established waste minimisation techniques. The Water Economy Assessment (a form of Monitoring and Targeting) results were determined using an empirically derived model. The Water Balance and True Cost of Waste results were obtained through more detailed calculations using the results of the chemical analysis. The results from the audit showed that the water usage on the chromium plating line has the highest waste minimisation potential. The True Cost of Waste analysis showed there is no significant chemical wastage in the effluent stream. The potential savings of the effluent stream was negligible (approximately R10 for 238 days). Drag-out calculations were also performed and showed that the drag-out volumes were in good agreement with the typical volumes found in the metal finishing industry. Intervention using simple lowcost and no-cost waste minimisation opportunities were recommended as a first step before contemplating further focus areas for technical or feasibility studies. / Thesis (M.Sc.)-University of KwaZulu-Natal, Pietermaritzburg, 2009.

published_or_final_version / Environmental Management / Master / Master of Science in Environmental Management

Neste estudo, a sorção e recuperação de íons metálicos de resíduos sólidos industriais provenientes de uma indústria de galvanoplastia situada no Rio de Janeiro (Brasil) foram investigadas através da utilização de duas resinas comerciais de troca iônica: Lewatit VPOC 1800 (fortemente ácida, tipo gel) e Lewatit VPOC 1960 (fortemente básica, tipo gel), produzidas pela Lanxess-Bayer Chemicals. As características físico-quimicas das resinas e do lodo galvânico foram determinadas. Os estudos de sorção das resinas foram conduzidos em batelada e em coluna. Baseado nesses estudos, os parâmetros de sorção e das curvas de ruptura foram determinados. Os estudos de equilíbrio e cinética de sorção também foram realizados. O resíduo de galvanoplastia era composto pelos metais: Cu2+, Fe3+, Al3+, Ni2+ e Cr3+. A capacidade de sorção qe das resinas Lewatit VPOC 1800 variou entre 0,1-1,9 mg g-1 para Cu2+, 0,01-0,6 mg g-1 para Fe3+ e 0,2-0,4 mg g-1 para Al3+. Enquanto que para a resina Lewatit VPOC 1960, os valores de qe variou entre 0,01-0,4 mg g-1 para Cu2+ e 0,01 0,2 mg g-1 para Fe3+ dependendo da concentração do metal e do tempo de contato. A capacidade de sorção para a resina Lewatit VPOC 1960 foi restrita para íons Cu2+ e Fe3+ os quais formam complexos aniônicos com íons Cl-. O modelo de Freundlich foi o mais adequado para descrever o equilíbrio de troca iônica de ambas as resinas. Já em relação ao mecanismo de sorção, o modelo pseudo-segunda ordem tipo 1 foi o mais aplicável. O ponto de ruptura das resinas Lewatit VPOC 1800 e Lewatit VPOC 1960 em relação aos íons Cu2+ocorreu quando passou através da coluna, 1860 cm3 e 2220 cm3 de solução de resíduo sólido respectivamente (20 g de resina, 100 mg L-1 de íons Cu2+, vazão de 60 cm3 min-1). Os íons metálicos Cu2+, Fe3+, Al3+, foram dessorvidos em alta proporção da resina Lewatit VPOC 1800 passando pela coluna solução aquosa de H2SO4 2,4 mol L-1. Já os metais Cu2+ e Fe3+ foram eluídos da resina Lewatit VPOC 1960 com solução aquosa de HCl 2,0 mol L-1. A recuperação seletiva de Cu2+ não foi alcançada porque Cu2+ e Fe3+ precipitam na mesma faixa de pH / In the present study, the sorption and recovery of metal ions from industrial solid residues proceeding from galvanoplasty industry (Rio de Janeiro, Brazil) was investigated by using two commercial ion exchange resins Lewatit VPOC 1800 (strong acid, gel type) and Lewatit VPOC 1960 (strong basic, gel type) produced by Lanxess - Bayer Chemicals. The physical-chemical characteristics of the resins and galvanic sludge were determined. The studies of sorption of the resins were conduced under batch and column conditions. Based on these studies the sorption parameters and the breakthrough curves for both resins were determined. Studies of equilibrium and kinetic of the sorption were also performed. The electroplating residue were composed of the metals Cu2+, Fe3+, Al3+, Ni2+ and Cr3+. The sorption capacity qe of the resin Lewatit VPOC1800 varied between 0.1-1.9 mg g-1 to Cu2+, 0.01-0.6 mg g-1 to Fe3+ and 0.2-0.4 mg g-1 to Al3+. While for the resin Lewatit VPOC1960 the values of qe varied between 0.01-0.4 mg g-1 to Cu2+ and 0.01-0.2 mg g-1 to Fe3+ depending of the metal concentration and contact time. The sorption capacity for Lewatit VPOC1960 was restricted to ions Cu2+ and Fe3+ that to form anionic complexes with chloride. The Freudlich model was more adequate to describe the ion exchange equilibrium for both resins and the sorption mechanism was compliant to the kinetic model of pseudo second order type 1. The breakpoint to Cu2+ occurred after passing 1860 cm3 and 2220 cm3 of residue solution through the resins Lewatit VPOC1800 and Lewatit VPOC1960, respectively (20 g of the resin, 100 ppm of Cu2+, flow rate of 60 cm3 min-1). The metals Cu2+, Fe3+ and Al3+ were desorbed on high proportion of the Lewatit VPOC1800 through passing a aqueous solution H2SO4 2.4 mol L-1. Already the metals Cu2+ and Fe3+ were eluted to Lewatit VPOC1960 with HCl aqueous solution 2.0 mol L-1. The selective recuperation of the Cu2+ was not reach because the Cu2+ and Fe3+ precipitated on similar pH