The cement industry is one of the most intensive energy consumers in the industrial sectors. The energy consumption represents 40% to 60% of production cost. Additionally, the cement industry contributes around 5% to 8% of all man-made CO2 emissions. Physiochemical and thermochemical reactions involved in cement kilns are still not well understood because of their complexity. The reactions have a decisive influence on energy consumption, environmental degradation, and the cost of cement production. There are technical difficulties in achieving direct measurements of critical process variables in kiln systems. Furthermore, process simulation is used for design, development, analysis, and optimization of processes, when experimental tests are difficult to conduct. Moreover, there are several models for the purpose of studying the use of alternative fuels, cement clinker burning process, phase chemistry, and physical parameters. Nonetheless, most of them do not address real inefficiency taking place in the processes, equipment, and the overall system. This paper presents parametric study results of the four-stage preheater dry Rotary Kiln System (RKS) with a planetary cooler. The RKS at the Mbeya Cement Company (MCC) in Tanzania is used as a case study. The study investigated the effects of varying the RKS parameters against system behaviour, process operation, environment, and energy consumptions. Necessary data for the modelling of the RKS at the MCC plant were obtained either by daily operational measurements or laboratory analyses. The steady-state simulation model of the RKS was carried out through the Aspen Plus software. The simulation results were successfully validated using real operating data. Predictions from parametric studies suggest that monitoring and regulating exhaust gases could improve combustion efficiency, which, in turn, leads to conserving fuels and lowering production costs. Composition of exhaust gases also depends both on the type of fuel used and the amount of combustion air. The volume of exit flue gases depends on the amount of combustion air and infiltrating air in the RKS. The results obtained from the study suggest a potential of coal saving at a minimum of about , which approximates to 76,126 tons per year at the current kiln feed of 58,000 kg·h⁻¹. Thus, this translates to a specific energy saving of about 1849.12 kJ·kgcl⁻¹, with relatively higher clinker throughput. In this vein, process modelling provides effective, safe, and economical ways for assessing the performance of the RKS.
1. Introduction
There are several process parameters in a cement rotary kiln system, which should be studied in order to observe trends that may indicate problems and provide necessary mean data for process analysis. The most important kiln controlling parameters are clinker production rate, fuel flow rate, specific heat consumption, secondary air temperature, kiln feed-end temperature, preheater exhaust gas temperature, ID fan pressure drop, kiln feed-end percentage oxygen, percentage downcomer oxygen, primary air flow rate, specific kiln volume loading, specific heat loading of burning zone cross-section area, and cooler air flow rate including temperature, pressure, and oxygen profile of the preheater [1–4]. However, the principal control variables are burning zone solid material temperature typically aimed at ; feed-end gas temperature typical at ; and feed-end oxygen typical at 2% [1]. Control is managed by adjustments of kiln feed, fuel flow rate, and ID fan speed [1].
A process simulation software is used for the description of different processes in flow diagrams. The objectives of simulation models are to deliver a comprehensive report of material and energy streams, determine the correlation between the reaction and separation systems, study how to eliminate wastes and prevent environmental pollution, evaluate plant flexibility to changes in feedstock or product policy, investigate the formation and separation of by-products and impurities, optimize the economic performance of the plant, validate the process instrumentation, and enhance process safety and control.
Cement production processes involve complex chemical and physical reactions during the conversion of raw materials to the final product. Moreover, the clinker burning process, which has a decisive influence on energy consumption and the cost of cement production, involves the combustion reaction of fossil fuel and a complex heat exchange between solids from raw materials and hot combustion gases [2, 3]. It also involves mixing, as well as separation of solid and fluids at various compositions, temperatures, and pressures. Therefore, following these complex issues which contribute to the inefficient energy use and emissions in cement kiln systems, there is a strong need to use computer-aided modelling to simplify the work of analyses. Other studies have tried to vary fuel properties, primary- and secondary air settings, and fuel feed location to study the effect of the operational setting on refuse-derived fuel, where the results show a good applicability of the presented modelling procedure [2–5].
Cement manufacturing is a high volume and energy intensive process, and according to the authors in [6, 7], the price of consuming large amounts of nonrenewable resources and energy (principally thermal fuels and electrical power) in those plants contributes to about 40% to 60% of the total manufacturing cost. In addition, the cement plants are also intensive in terms of CO2 and other effluent emissions. For that reason, sustainability can be viewed as a broad and complex concept in the cement industry sector, as it includes a variety of key issues, such as (i) efficiency of resource and energy use, (ii) reduced emissions, (iii) health and safety protection, and (iv) competitiveness and profitability, which are essential for its economic survival and social acceptance [8].
The term “cement” includes a range of substances utilized as binders or adhesives, even though the cement produced in the greatest volume and most widely used in concrete for construction is Portland cement. Cement plants basically consist of three manufacturing parts: (i) raw material and fuel supply preparation, (ii) clinker production (commonly named as the pyroprocessing part), and (iii) intergrinding and blending of cement clinker with other active ingredients to produce the required types of cement.
The cement manufacturing process starts by handling a mix of raw materials: (i) naturally occurring limestone, which is the source of calcium, (ii) clay minerals and (iii) sand, which are the sources of silicon and aluminium, and (iv) iron-containing components. The raw materials are ground and mixed together in controlled proportions to form a homogeneous blend, termed as a raw meal or raw-mix, with the required chemical composition.
Raw meal is then subjected to the continuous, high temperature operations in the pyroprocessing part of the plant, namely the rotary kiln system (RKS). The progressive increase of temperature along RKS initiates a series of consecutive reactions of raw meal, ranging from the evaporation of free water to the decomposition of raw materials and the combination of lime and clay oxides. This means that raw meal passes through a series of functional zones where it is dried, preheated, calcined, and sintered to produce clinker minerals, which, in turn, form the semifused pellets of cement clinker. Regarding the type of pyroprocessing employed in RKS, the overall technology for cement production can be roughly divided into (i) the dry process, (ii) the wet process and its modification, (iii) the semidry process, and (iv) the semiwet process. Each of the enumerated processes are characterized by different raw material preparations and different configurations of RKS, and in practice, they have to be selected according to consideration given to properties of raw materials and costs of fuel and electricity, as well as conditions of location, etc. The major technologies in use today, including their configurations, respective temperature, and functional zones inside the RKS, are illustrated in Figure 1 [9–11].