Evaluation of capital cost data: Part 9: Liquid waste disposal with emphasis on chemical treatment

Capital cost correlations are given for chemical feed systems, chlorination, ozone disinfection, ultraviolet light disinfection, ion exchange, flocculation, and carbon adsorption. Most of the correlations are accurate to ± 30%, expressed in Canadian dollars and adjusted to a Marshall and Swift value of 1000. Details as to what components are included in the cost are given. Data are given for the labour and material costs to create a working process module. To put the current data into perspective, several hundred sources of cost data were analyzed. The major correlations are compared, on a consistent basis, with current data.     

Evaluation of capital cost data: Part 8: Liquid waste disposal with emphasis on biological treatment

Capital cost correlations are given for aeration basins, mechanical aerators, diffused aeration, conventional activated sludge process, extended aeration, contact stabilization, oxidation ditch, rotating biological contactor, trickling filter, aerobic lagoons, facultative lagoon, aerated lagoons and liners. Most of the correlations are accurate to ±30%, expressed in Canadian dollars and adjusted to a Marshall and Swift value of 1000. Details as to what components are included in the cost are given. Data are given for the labour and material costs to create a working process module. Data for oxidation ditches are accurate to ±50%. To put the current data into perspective, several hundred sources of cost data were analyzed. The major correlations are compared, on a consistent basis, with current data.     

Evaluation of capital cost data: Gas moving equipment

Capital cost correlations are given for gas moving equipment. Correlations available in the literature and current data are compared on a consistent basis. Forty-three graphs show the relative magnitude of the different correlations and the recommended correlation for each type of equipment is summarized in a table. Some data on the costs of installing gas moving equipment are given.     

Evaluation of capital cost data: Liquid moving equipment

Capital cost correlations are given for liquid moving equipment. Correlations available in the literature and current data from suppliers, contractors, consultants and industry are compared on a consistent basis. Forty-three graphs show the relative magnitudes of the different correlations, and the recommended correlation for each type of equipment is given. Some factors are given on the costs of installing liquid moving equipment.     

Evaluation of capital cost data: Heat exchangers

Capital cost correlations are given for heat exchangers and furnaces. Correlations available in the literature and current data are compared on a consistent basis. Forty-six graphs show the relative magnitude of the different correlations and the recommended correlation for each type of equipment is summarized in a table. Some data on the costs of installing heat exchange equipment are given.     

Evaluation of capital cost data: Heat exchangers

Capital cost correlations are given for heat exchangers and furnaces. Correlations available in the literature and current data are compared on a consistent basis. Forty-six graphs show the relative magnitude of the different correlations and the recommended correlation for each type of equipment is summarized in a table. Some data on the costs of installing heat exchange equipment are given.     

Evaluation of capital cost data: Offsite utilities (Supply)

Capital cost correlations are given for units supplying utilities: steam, refrigeration, cooling and treated water, electricity. Correlations available in the literature and current data are compared on a consistent basis. Thirty-two graphs show the relative magnitudes of the different correlations, and the recommended correlation for each type of equipment is given. Some factors are given on the costs of installing the package units.     

Evaluation of capital cost data: Drives

Capital cost correlations are given for electric and gasoline motors, steam, gas and combustion-gas driven turbines, power transmission units and power converters. Correlations available in the literature and current data are compared on a consistent basis. Thirty-eight graphs show the relative magnitudes of the different correlations and the recommended correlation for each type of equipment is summarized in a table.     

Evaluation of capital cost data: Onsite utilities (industrial gases)

Capital cost correlations with capacity or with total investment are given for units supplying onsite industrial gases: compressed air, oxygen, nitrogen, inert atmospheres, high purity hydrogen, synthesis gas, ozone and acetylene. Costs are also given for units to remove carbon dioxide and water from gas streams. Correlations available in the literature and current data are compared. Graphs show the relative magnitudes of the different correlations, and the recommended correlation for each type of equipment is given. Some unit usages are given for producing some of the gases.     

Economics of occupational cotton dust control in cottonseed oil mills

An economic analysis of the total cost for various dust control systems for a 500 ton/day model cottonseed oil mill has been performed. All cost data have been adjusted to reflect May 1981 prices. Cost data are presented for the dust collection system, cyclone(s), baghouse(s) and prime air mover(s) for each major processing area at 3 different air-to-cloth ratios. Data were obtained for equipment and installation costs from mills using the various devices and/or complete systems wherever possible. In cases where these data were not available, estimates were obtained from several firms that manufacture and install similar equipment. At the recommended air-to-cloth ratio of 20:1, the initial capital cost was estimated as $707,900, the annual operating expenses as $226,490 and the life cycle cost as $607,510.     

NCE引进焚烧炉国产化

通过对日本日铁化学工程公司（简称NCE）引进的焚烧炉国产化改造,炉钢壳和炉砖在国内进行制作及采购。更新投用后设备运行正常,焚烧装置各项指标达标可控,同时国产化改造节约了投资费用,节省了时间,取得了较好成效。     

Desalting seawater and brackish water: a cost update

This report is a second update of costs, originally presented in ORNL/TM-5070, which gave cost estimates for desalting seawater and brackish water based upon first quarter 1975 costs. The first update was based upon 1977 costs. The specific input to the report includes two earlier U.S. Department of Energy reports, recent work sponsored by the U.S. Office of Water Research & Technology, and new equipment and operating cost input from major equipment suppliers and users.

Cost estimates are given for desalting seawater by distillation and reverse osmosis, and for desalting brackish water by reverse osmosis and electrodialysis. The report includes the cost of generating steam and electrical energy on site using coal-fired boilers as well as oil-fired boilers, and dual purpose nuclear/electric seawater distillation plants. The energy costs for both reverse osmosis and electrodialysis are based upon the availability of electricity at a fixed rate. Cost data were computed as a function of plant size, and include both capital costs and construction costs which are considered as typical. These assumptions are used to develop the reference cases of total water cost. The manner of presentation is such, however, that the costs can be easily adjusted to reflect local conditions.     

Synthesis and study of new nonionic polyether water clarifier for oily wastewater

In order to solve the problem of oily wastewater treatment in Shengli Oilfield, tert-butyl phenol (TP) series nonionic polyether water clarifiers were synthesized by polymerization with p-tert-butyl phenol (PTBP) as the initiator. The water clarifiers were characterized by Fourier-transform infrared spectroscopy (FT-IR) and the interfacial tension test was carried out. The TP series of water clarifiers effect were evaluated by the oil content and suspension content in the clean water experiments. In addition, the effects of dosage and temperature on the water effect were discussed through the control variable method. The experimental results showed that the oil removal rate of TP6 can reach 95% and the suspension removal rate can reach 92% when the dosage of water clarifier was 40 mg/L, the cleaning water temperature was 55°C, and the cleaning water time was 30 min. The oily wastewater colour after cleaning was clear and transparent with the TP series of water clarifiers, and the effect was better than with commercial water clarifiers.     

Natural gas viscosity estimation using density based models

Accurate value determination of natural gas viscosity plays a key role in its management as it is one of the most important parameters in natural gas engineering calculations. In this study, a comprehensive model is suggested for prediction of natural gas viscosity in a wide range of pressures, temperatures, densities and compositions. The new model can be applicable for gases containing heptane plus and non‐hydrocarbon components. It is validated by the 2011 viscosity data from 18 different gas mixtures. Compared to existing similar models and correlations, its results are quite satisfactory. © 2012 Canadian Society for Chemical Engineering     

Status of reverse osmosis desalination technology

Reverse osmosis (RO), a relatively new technology, is gradually becoming an established and economical method for demineralization of saline waters. Over 50 commercial plants ranging in size from 50,000 gpd to 2 million gpd (2 mgd) are producing fresh quality water for municipal and industrial uses from brackish water sources. The U.S. Congress has authorized construction of a 100 mgd plant in Yuma, Arizona to demineralize otherwise unusable high salinity irrigation return flows as part of the Colorado River Salinity Control. Engineering design and operation details together with cost information on some commercial plants and the planned 100 mgd plant will be presented.A review of the plant operation data indicates that is imperative for the plant owners and equipment suppliers to place due emphasis on providing adequate feed water pretreatment facilities and trained plant operation personnel to ensure trouble-free operation and to achieve furthur economy in desalting costs.Significant advances have been made in the development of RO process for sea water desalination. Soaring energy costs are providing incentive for plant owners to prefer RO plants (up to 100,000 gpd) over vapor compression distillation hardware. Results of the Federal Government Desalting R & D Programs clearly indicate that RO desalting costs will be at least 20–30% lower than distillation.     

Economic aspects of membrane processes

Care must be exercised, in predicting operating costs for membrane desalination systems for electricity, labor, chemicals, etc. The assumptions made in establishing unit costs can greatly affect the predicted operating cost and hence the ultimate investment decision. The use of data estimating the quantities of chemicals, power, etc., expected to be used per unit of production can assist in predicting costs, as then site-specific cost data can be used. The fact that 0.2 pounds of acid per kgal of permeate is required in a Florida RO plant is more useful for predicting operating costs of an RO plant on the Island of Anegata than is the fact that acid costs at the Florida plant are $0.03/kgal of water produced. Data based on units rather than costs are presented for seven RO facilities and one ED facility in this paper for use in this type of analysis.     

新型变压吸附技术的开发和应用

简要介绍了新型两段法变压吸附高效气体分离技术开发的背景及意义，详细介绍了该技术在脱碳、提氢、提纯CO、制氧领域中的应用。该技术的开发成功，极大地简化了工艺流程，既节省动力设备购置费、运行费和设备维护费，又大幅提高了装置稳定性、安全性和可靠性。     

改良型道尔澄清桶的设计理论基础及应用

阐述了国内盐水澄清桶的设计现状，探讨了设计澄清桶的理论基础，即颗粒沉降速度的求取；介绍了改良型道尔澄清桶的设计特点、若干实用的技术数据及其在青岛海晶化工集团有限公司的使用效果。     

Optimum Values of Process Parameters of the “Wet Limestone Flue Gas Desulfurization System”

In this article the method of cost optimization of the “Wet Limestone Flue Gas Desulfurization System” is presented. The optimization calculations include process and cost models. The process model describes the most important stage of SO₂ removal that runs in the absorber and in the holding tank. It includes absorption of sulfur dioxide, oxidation of SO^2–₃, dissolution of limestone, and crystallization of gypsum. The model was applied to calculate indispensable parameters for estimating costs and then to minimize capital and operating costs. Costs of all important equipment were estimated, such as SO₂ removal systems with the absorber and the holding tank, reagent feed system with the ball mill and dewatering gypsum slurry system. Optimum values of the process parameters for different conditions of running flue gas desulfurization system were found. The process and cost model can be useful when designing the wet limestone FGD systems and carrying out economic analysis of the flue gas desulfurization plants.     

Optimal selection of major equipment in dual purpose plants

Simulation of different operational conditions with the aid of a computer program is one of the best ways of assisting decision-makers in the selection of the most economic mix of equipment for a dual purpose plant. Using this approach this paper deals with the economic comparison of plants consisting of MSF desalinators and combustion gas or back pressure steam turbines coupled to low capacity electric power generators. The comparison is performed on the basis of the data made available by the OPTDIS computer program and the results are given in terms of yearly cost of production as the sum of capital, manpower, maintenance, fuel and chemical costs.