The document provides details on the material and energy balances, equipment needs, costs, and economic evaluation of a proposed corn starch production plant. Key points:
- Material and energy balances are presented to determine equipment size and energy requirements. The total estimated energy needed is 3,090,800 kWh/year.
- Major equipment needs and costs are listed, with a total purchased equipment cost of 710,000 ETB. The total fixed capital investment is estimated at 2,868,400 ETB.
- Production costs are estimated, including raw materials, utilities, labor, maintenance, etc. The total manufacturing cost is estimated to be 6,141,875 ETB + 3% of total production cost
In the plant, ammonia is produced from synthesis gas containing hydrogen and nitrogen in the ratio of approximately 3:1. Besides these components, the synthesis gas contains inert gases such as argon and methane to a limited extent. The source of H2 is demineralized water and the hydrocarbons in the natural gas. The source of N2 is the atmospheric air. The source of CO2 is the hydrocarbons in the natural gas feed. Product ammonia and CO2 is sent to urea plant. The present article intended the description of ammonia plant for natural gas based plants and the possible material balance of some section.
Standard Test for Smoke Point for Kerosene and Aviation Turbine fuel, ASTM 13...Student
Standard Test for Smoke Point for Kerosene and Aviation Turbine fuel, ASTM 1322-97, IP 57/95
The smoke point is the maximum flame height in millimeters at which kerosene will burn without smoking, tested under standard conditions, this test method provides an indication of the relative smoke producing properties of kerosene and aviation turbine fuels in a diffusion flame. The smoke point is related to the hydrocarbon type composition of such fuels. Generally the more aromatic the fuel the smokier the flame. A high smoke point indicates a fuel of low smoke producing tendency.
Prepared By Yasir Al-Beatiy
Computer Simulation of a Heat Exchanger using AspenAli Raza
A heat exchanger was simulated using Aspen Plus to heat Freon-12 from 240 K to 300 K using ethylene glycol at 350 K. The simulation specified the streams, calculated the heat transfer coefficients, determined the geometry of the exchanger including number of tubes, tube size and length, shell diameter, and baffles. The results of the simulation were examined to check if the design met the objectives of heating the Freon to the required temperature while maintaining a 10 K minimum approach and not exceeding pressure drop limits.
This document discusses various mass transfer separation processes used in chemical industries. It describes core separation processes like distillation, gas absorption, liquid-liquid extraction, drying, adsorption, crystallization and membrane separation. These processes are classified based on the phases involved (gas, liquid, solid) and the mechanism of separation - contact of immiscible phases, indirect contact of miscible phases through a membrane, direct contact of miscible phases, or use of surface phenomena. Examples of typical applications and separation processes are provided for different combinations of phases.
Project: Formaldehyde from methanol and airMehmoodIqbal7
1. The document describes the production of formaldehyde via the silver catalytic process. Formaldehyde is produced from methanol using a silver catalyst at high temperatures.
2. The reaction products are cooled and purified through absorption and distillation columns to separate the formaldehyde from unreacted methanol. Final products contain 37% formaldehyde solutions.
3. The silver catalytic process has advantages over alternative metal oxide processes in having lower costs, safer operations, higher yields, and more flexibility. Material and energy balances are required to design an optimal formaldehyde production process.
This document provides an overview of crystallization processes. It discusses how crystals form from solutions or melts via nucleation and growth. Primary and secondary nucleation are described. Mass transfer and population balance theories are used to model crystal growth rates and size distributions. The document outlines how continuous crystallizers like MSMPR systems operate and how residence time affects crystal size distribution. Methods for controlling crystal size like double draw-off, fines removal, and classified product removal are also summarized.
This document discusses reflux ratios in distillation columns. It defines total, minimum, and optimum reflux ratios. Total reflux uses all overhead vapor as reflux, allowing calculation of minimum required plates. Minimum reflux is the maximum ratio requiring infinite plates for desired separation. Optimum reflux minimizes total costs by balancing fixed costs that decrease with higher reflux against increasing operating costs.
Design of Methanol Water Distillation Column Rita EL Khoury
Methanol is an essential feed stock for the manufacture of many industrial products such as adhesives and paints and it is widely used as a solvent in many chemical reactions. Crude methanol is obtained from steam reforming of natural gas and then a purification process is needed since it contains smaller and larger degree of impurities.
The purification process consists of two steps: a topping column used to remove the low boiling impurity called the light ends; and the remaining water methanol mixture is transferred to another column called the refining column where it is constantly boiled until separation occurs. Methanol rises to the top while the water accumulates in the bottom.
This document focuses on methanol water separation. A detailed design study for the distillation column is conducted where the separation occurs at atmospheric pressure with a total condenser and a partial reboiler.
In the plant, ammonia is produced from synthesis gas containing hydrogen and nitrogen in the ratio of approximately 3:1. Besides these components, the synthesis gas contains inert gases such as argon and methane to a limited extent. The source of H2 is demineralized water and the hydrocarbons in the natural gas. The source of N2 is the atmospheric air. The source of CO2 is the hydrocarbons in the natural gas feed. Product ammonia and CO2 is sent to urea plant. The present article intended the description of ammonia plant for natural gas based plants and the possible material balance of some section.
Standard Test for Smoke Point for Kerosene and Aviation Turbine fuel, ASTM 13...Student
Standard Test for Smoke Point for Kerosene and Aviation Turbine fuel, ASTM 1322-97, IP 57/95
The smoke point is the maximum flame height in millimeters at which kerosene will burn without smoking, tested under standard conditions, this test method provides an indication of the relative smoke producing properties of kerosene and aviation turbine fuels in a diffusion flame. The smoke point is related to the hydrocarbon type composition of such fuels. Generally the more aromatic the fuel the smokier the flame. A high smoke point indicates a fuel of low smoke producing tendency.
Prepared By Yasir Al-Beatiy
Computer Simulation of a Heat Exchanger using AspenAli Raza
A heat exchanger was simulated using Aspen Plus to heat Freon-12 from 240 K to 300 K using ethylene glycol at 350 K. The simulation specified the streams, calculated the heat transfer coefficients, determined the geometry of the exchanger including number of tubes, tube size and length, shell diameter, and baffles. The results of the simulation were examined to check if the design met the objectives of heating the Freon to the required temperature while maintaining a 10 K minimum approach and not exceeding pressure drop limits.
This document discusses various mass transfer separation processes used in chemical industries. It describes core separation processes like distillation, gas absorption, liquid-liquid extraction, drying, adsorption, crystallization and membrane separation. These processes are classified based on the phases involved (gas, liquid, solid) and the mechanism of separation - contact of immiscible phases, indirect contact of miscible phases through a membrane, direct contact of miscible phases, or use of surface phenomena. Examples of typical applications and separation processes are provided for different combinations of phases.
Project: Formaldehyde from methanol and airMehmoodIqbal7
1. The document describes the production of formaldehyde via the silver catalytic process. Formaldehyde is produced from methanol using a silver catalyst at high temperatures.
2. The reaction products are cooled and purified through absorption and distillation columns to separate the formaldehyde from unreacted methanol. Final products contain 37% formaldehyde solutions.
3. The silver catalytic process has advantages over alternative metal oxide processes in having lower costs, safer operations, higher yields, and more flexibility. Material and energy balances are required to design an optimal formaldehyde production process.
This document provides an overview of crystallization processes. It discusses how crystals form from solutions or melts via nucleation and growth. Primary and secondary nucleation are described. Mass transfer and population balance theories are used to model crystal growth rates and size distributions. The document outlines how continuous crystallizers like MSMPR systems operate and how residence time affects crystal size distribution. Methods for controlling crystal size like double draw-off, fines removal, and classified product removal are also summarized.
This document discusses reflux ratios in distillation columns. It defines total, minimum, and optimum reflux ratios. Total reflux uses all overhead vapor as reflux, allowing calculation of minimum required plates. Minimum reflux is the maximum ratio requiring infinite plates for desired separation. Optimum reflux minimizes total costs by balancing fixed costs that decrease with higher reflux against increasing operating costs.
Design of Methanol Water Distillation Column Rita EL Khoury
Methanol is an essential feed stock for the manufacture of many industrial products such as adhesives and paints and it is widely used as a solvent in many chemical reactions. Crude methanol is obtained from steam reforming of natural gas and then a purification process is needed since it contains smaller and larger degree of impurities.
The purification process consists of two steps: a topping column used to remove the low boiling impurity called the light ends; and the remaining water methanol mixture is transferred to another column called the refining column where it is constantly boiled until separation occurs. Methanol rises to the top while the water accumulates in the bottom.
This document focuses on methanol water separation. A detailed design study for the distillation column is conducted where the separation occurs at atmospheric pressure with a total condenser and a partial reboiler.
Packed columns are used for distillation, gas absorption, and liquid-liquid extraction. They have continuous gas-liquid contact through a packed bed, unlike plate columns which have stage-wise contact. Packed columns depend on good liquid and gas distribution, and have lower holdup but higher pressure drop than plate columns. This document provides details on packed column components, design procedures such as selecting packing and determining height, and examples of absorption and stripping processes in packed columns.
Desalination of Sea Water using Membrane technologyChandni Sinha
The document discusses various desalination methods for obtaining fresh water from seawater. It begins by introducing the importance of desalination given increasing fresh water scarcity. There are two main types of desalination processes: thermal and membrane. Thermal processes involve boiling saline water to produce distilled water, while membrane processes use semi-permeable membranes to separate fresh water from salt water. The document then goes into detail about various thermal and membrane desalination methods, including multi-stage flash distillation, reverse osmosis, and nanofiltration. It also discusses factors involved in membrane development and selection.
This document discusses heat exchangers, including their types, advantages, disadvantages, and applications. It describes the main types of heat exchangers as shell and tube, double pipe, plate type, and finned tube. Shell and tube heat exchangers are the most widely used due to their lower cost compared to plate type and ability to handle higher pressures than double pipe. Plate type heat exchangers offer higher efficiency but higher initial cost. Heat exchangers are commonly used in chemical, petrochemical, food, and other industrial processes to transfer heat between fluids.
The document provides an overview of unit operations in chemical engineering. It defines unit operations as basic steps that involve physical changes like separation, crystallization, evaporation. Examples of common unit operations are given like heat transfer, evaporation, drying, absorption. Different types of unit operations are classified. Key aspects of specific unit operations like heat transfer, drying, evaporation and distillation are described in further detail. The document highlights the importance of understanding the physical laws governing each unit operation for effective analysis and design of chemical processes.
The document describes the Semi-Implicit Method for Pressure Linked Equations (SIMPLE) algorithm for coupling pressure and velocity in computational fluid dynamics. It involves the following steps:
1. An initial guess for pressure and velocity is made.
2. Momentum equations are solved to get updated velocity fields.
3. A pressure correction equation is derived from the continuity equation and solved to update pressure.
4. Pressure and velocities are corrected and the process is iterated until convergence is achieved.
Under-relaxation factors are applied to the pressure and velocity corrections to improve convergence. Variations like SIMPLER use the discretized continuity equation directly to obtain pressure instead of a pressure correction step.
Hydrogen has many potential industrial applications but faces challenges in production, storage, and safety. It is primarily produced through steam methane reforming, which accounts for 48% of global hydrogen. Other methods include electrolysis and gasification of fossil fuels or biomass. Hydrogen is used in various industrial processes but storage remains an issue due to its low density. Further development is needed to establish hydrogen as a sustainable energy carrier.
In many cases, the drying of mater
ials is the fina l operation i n manufac turing process
carried out immediately prior to pack ag ing and dispatch . Drying refer s to final
removal o f water, and the operation follow s e vapo ration , filtration or crystallization .
This document discusses options for distilling dilute ethanol to produce 99.5% ethanol. It analyzes pressure swing distillation versus azeotropic distillation, with benzene as a common entrainer. Preliminary simulations show pressure swing distillation yields the desired product composition with less ethanol loss. A three-column system is also considered but deemed too costly. The document outlines objectives of determining the optimal distillation method, finalizing a process flow diagram, performing safety and economic analyses, and achieving a 5% annual ROI.
Shortcut Methods of Distillation Design
0 INTRODUCTION/PURPOSE
1 SCOPE
2 ESTIMATIONOF PLATEAGE AND REFLUX
REQUIREMENTS
2.1 Generalized Procedure for Nmin and Rmin
2.2 Equation based Procedure for Nmin and Rmin
3 PREDICTION OF OVERALL PLATE EFFICIENCY
4 SIZING OF MAIN PLANT ITEMS
4.1 Column Diameter
4.2 Surface Area of Condensers and Reboilers
FIGURES
1 NON-IDEAL EQUILIBRIUM CURVE
2 AT A GLANCE CHART BASED ON FENSKE,
UNDERWOOD
3 PLATE EFFICIENCY CORRELATION OF O’CONNEL
Cyclones and hydrocyclones use centrifugal force and gravity to separate mixtures without filters. Contaminated gas or liquid enters tangentially and spins, forcing heavier particles to the outer wall. Lighter particles spiral up the center and exit at the top while heavier particles exit at the bottom. They are commonly used to remove particulates in industrial processes like mining, drilling, and wastewater treatment. Operating parameters like geometry and flow characteristics determine separation size and efficiency. They have low costs but reduced performance with non-ideal mixtures.
This document describes an experiment conducted by students to measure the density and specific gravity of various liquids using a hydrometer. The introduction provides background on hydrometers and how they are used to determine density and specific gravity. The experimental procedures involve filling a cylinder with the test liquid, inserting the hydrometer, and recording the point where the liquid meets the stem. The student then answers discussion questions about density and specific gravity measurements in oil industry, how hydrometers work, differences between density and relative/specific gravity, API gravity, and sources of error in their results.
batch distillation, multi stage batch distillationKarnav Rana
This document discusses batch distillation. It begins by contrasting batch and continuous distillation, noting that batch distillation is useful when small amounts of products with varying compositions are needed. The key difference is that batch distillation involves no continuous feed or product withdrawal. Rayleigh's equation is then derived and explained, providing a critical third equation to solve batch distillation problems using material balances. Graphical and numerical integration techniques are presented for using Rayleigh's equation to determine unknown values like the final liquid amount.
This experiment involves conducting a saponification reaction between sodium hydroxide (NaOH) and ethyl acetate (Et(Ac)) in a continuous stirred tank reactor (CSTR) to determine the effect of residence time on conversion. A calibration curve will be prepared to relate conductivity measurements to conversion values for the 0.1M NaOH and 0.1M Et(Ac) reaction. The objectives are to determine conversion, the reaction rate constant, and the effect of residence time on conversion.
Astm method for distillation of petroleum products at atmospheric pressureStudent
This document summarizes an experiment to determine the boiling range of kerosene using ASTM distillation. The experiment involves heating a 100mL gasoline sample in a distillation flask and measuring the temperature and volume percent distilled at intervals. A plot of the results shows the boiling range is 54-180°C. The document discusses how boiling range indicates a fuel's composition and properties, and how it affects safety, performance, and tendency to be explosive. Factors like vapor losses and condenser efficiency can impact the accuracy of the results.
HNO3 MANUFACTURING WITH PROCESS FLOW DIAGRAMUsama Pervaiz
Here are two ways expenses are minimized in the Ostwald process:
1. The heat generated by the exothermic reactions is utilized to maintain the high temperature needed for the ammonia oxidation reaction, reducing energy costs.
2. Platinum-rhodium alloy is used as the catalyst. Platinum is very expensive but using it in an alloy with less costly rhodium allows the use of less platinum, lowering material costs.
This document discusses various processes used to remove mercaptans from petroleum products. It begins by explaining that mercaptans cause foul odors and corrosion and need to be removed. Then it describes processes that include caustic scrubbing, solutizer extraction, doctor treating using lead compounds, copper chloride sweetening, merox extraction, and sulfuric acid treatment. The doctor treating process reacts mercaptans with lead compounds to form disulfides. Merox extraction oxidizes mercaptans to disulfides using a catalyst. Sulfuric acid treatment and clay treatment can also remove olefins, gums and improve product properties.
This document discusses factors that affect manufacturing costs, including direct costs that vary with production rate, fixed costs that do not vary with production rate, and general expenses. It then provides equations to estimate total manufacturing cost based on these factors. An example calculation is shown for a nitric acid plant. Manufacturing costs are estimated based on raw material, utility, labor, and fixed capital investment costs. Percentages of total cost accounted for by each cost category are also calculated.
This document summarizes a project to design and model a solid oxide fuel cell (SOFC) system using HYSYS simulation software. The design follows a 7-level process design hierarchy outlined by Douglas. The SOFC system is fueled by natural gas and pressurized air, producing most of its electricity through two SOFC units with the remainder from two turbines. Key components of the SOFC process include methane, oxygen, hydrogen, and carbon dioxide. The economic analysis of the final design shows an after-tax rate of return of 8.5%, making it a potentially attractive investment.
Packed columns are used for distillation, gas absorption, and liquid-liquid extraction. They have continuous gas-liquid contact through a packed bed, unlike plate columns which have stage-wise contact. Packed columns depend on good liquid and gas distribution, and have lower holdup but higher pressure drop than plate columns. This document provides details on packed column components, design procedures such as selecting packing and determining height, and examples of absorption and stripping processes in packed columns.
Desalination of Sea Water using Membrane technologyChandni Sinha
The document discusses various desalination methods for obtaining fresh water from seawater. It begins by introducing the importance of desalination given increasing fresh water scarcity. There are two main types of desalination processes: thermal and membrane. Thermal processes involve boiling saline water to produce distilled water, while membrane processes use semi-permeable membranes to separate fresh water from salt water. The document then goes into detail about various thermal and membrane desalination methods, including multi-stage flash distillation, reverse osmosis, and nanofiltration. It also discusses factors involved in membrane development and selection.
This document discusses heat exchangers, including their types, advantages, disadvantages, and applications. It describes the main types of heat exchangers as shell and tube, double pipe, plate type, and finned tube. Shell and tube heat exchangers are the most widely used due to their lower cost compared to plate type and ability to handle higher pressures than double pipe. Plate type heat exchangers offer higher efficiency but higher initial cost. Heat exchangers are commonly used in chemical, petrochemical, food, and other industrial processes to transfer heat between fluids.
The document provides an overview of unit operations in chemical engineering. It defines unit operations as basic steps that involve physical changes like separation, crystallization, evaporation. Examples of common unit operations are given like heat transfer, evaporation, drying, absorption. Different types of unit operations are classified. Key aspects of specific unit operations like heat transfer, drying, evaporation and distillation are described in further detail. The document highlights the importance of understanding the physical laws governing each unit operation for effective analysis and design of chemical processes.
The document describes the Semi-Implicit Method for Pressure Linked Equations (SIMPLE) algorithm for coupling pressure and velocity in computational fluid dynamics. It involves the following steps:
1. An initial guess for pressure and velocity is made.
2. Momentum equations are solved to get updated velocity fields.
3. A pressure correction equation is derived from the continuity equation and solved to update pressure.
4. Pressure and velocities are corrected and the process is iterated until convergence is achieved.
Under-relaxation factors are applied to the pressure and velocity corrections to improve convergence. Variations like SIMPLER use the discretized continuity equation directly to obtain pressure instead of a pressure correction step.
Hydrogen has many potential industrial applications but faces challenges in production, storage, and safety. It is primarily produced through steam methane reforming, which accounts for 48% of global hydrogen. Other methods include electrolysis and gasification of fossil fuels or biomass. Hydrogen is used in various industrial processes but storage remains an issue due to its low density. Further development is needed to establish hydrogen as a sustainable energy carrier.
In many cases, the drying of mater
ials is the fina l operation i n manufac turing process
carried out immediately prior to pack ag ing and dispatch . Drying refer s to final
removal o f water, and the operation follow s e vapo ration , filtration or crystallization .
This document discusses options for distilling dilute ethanol to produce 99.5% ethanol. It analyzes pressure swing distillation versus azeotropic distillation, with benzene as a common entrainer. Preliminary simulations show pressure swing distillation yields the desired product composition with less ethanol loss. A three-column system is also considered but deemed too costly. The document outlines objectives of determining the optimal distillation method, finalizing a process flow diagram, performing safety and economic analyses, and achieving a 5% annual ROI.
Shortcut Methods of Distillation Design
0 INTRODUCTION/PURPOSE
1 SCOPE
2 ESTIMATIONOF PLATEAGE AND REFLUX
REQUIREMENTS
2.1 Generalized Procedure for Nmin and Rmin
2.2 Equation based Procedure for Nmin and Rmin
3 PREDICTION OF OVERALL PLATE EFFICIENCY
4 SIZING OF MAIN PLANT ITEMS
4.1 Column Diameter
4.2 Surface Area of Condensers and Reboilers
FIGURES
1 NON-IDEAL EQUILIBRIUM CURVE
2 AT A GLANCE CHART BASED ON FENSKE,
UNDERWOOD
3 PLATE EFFICIENCY CORRELATION OF O’CONNEL
Cyclones and hydrocyclones use centrifugal force and gravity to separate mixtures without filters. Contaminated gas or liquid enters tangentially and spins, forcing heavier particles to the outer wall. Lighter particles spiral up the center and exit at the top while heavier particles exit at the bottom. They are commonly used to remove particulates in industrial processes like mining, drilling, and wastewater treatment. Operating parameters like geometry and flow characteristics determine separation size and efficiency. They have low costs but reduced performance with non-ideal mixtures.
This document describes an experiment conducted by students to measure the density and specific gravity of various liquids using a hydrometer. The introduction provides background on hydrometers and how they are used to determine density and specific gravity. The experimental procedures involve filling a cylinder with the test liquid, inserting the hydrometer, and recording the point where the liquid meets the stem. The student then answers discussion questions about density and specific gravity measurements in oil industry, how hydrometers work, differences between density and relative/specific gravity, API gravity, and sources of error in their results.
batch distillation, multi stage batch distillationKarnav Rana
This document discusses batch distillation. It begins by contrasting batch and continuous distillation, noting that batch distillation is useful when small amounts of products with varying compositions are needed. The key difference is that batch distillation involves no continuous feed or product withdrawal. Rayleigh's equation is then derived and explained, providing a critical third equation to solve batch distillation problems using material balances. Graphical and numerical integration techniques are presented for using Rayleigh's equation to determine unknown values like the final liquid amount.
This experiment involves conducting a saponification reaction between sodium hydroxide (NaOH) and ethyl acetate (Et(Ac)) in a continuous stirred tank reactor (CSTR) to determine the effect of residence time on conversion. A calibration curve will be prepared to relate conductivity measurements to conversion values for the 0.1M NaOH and 0.1M Et(Ac) reaction. The objectives are to determine conversion, the reaction rate constant, and the effect of residence time on conversion.
Astm method for distillation of petroleum products at atmospheric pressureStudent
This document summarizes an experiment to determine the boiling range of kerosene using ASTM distillation. The experiment involves heating a 100mL gasoline sample in a distillation flask and measuring the temperature and volume percent distilled at intervals. A plot of the results shows the boiling range is 54-180°C. The document discusses how boiling range indicates a fuel's composition and properties, and how it affects safety, performance, and tendency to be explosive. Factors like vapor losses and condenser efficiency can impact the accuracy of the results.
HNO3 MANUFACTURING WITH PROCESS FLOW DIAGRAMUsama Pervaiz
Here are two ways expenses are minimized in the Ostwald process:
1. The heat generated by the exothermic reactions is utilized to maintain the high temperature needed for the ammonia oxidation reaction, reducing energy costs.
2. Platinum-rhodium alloy is used as the catalyst. Platinum is very expensive but using it in an alloy with less costly rhodium allows the use of less platinum, lowering material costs.
This document discusses various processes used to remove mercaptans from petroleum products. It begins by explaining that mercaptans cause foul odors and corrosion and need to be removed. Then it describes processes that include caustic scrubbing, solutizer extraction, doctor treating using lead compounds, copper chloride sweetening, merox extraction, and sulfuric acid treatment. The doctor treating process reacts mercaptans with lead compounds to form disulfides. Merox extraction oxidizes mercaptans to disulfides using a catalyst. Sulfuric acid treatment and clay treatment can also remove olefins, gums and improve product properties.
This document discusses factors that affect manufacturing costs, including direct costs that vary with production rate, fixed costs that do not vary with production rate, and general expenses. It then provides equations to estimate total manufacturing cost based on these factors. An example calculation is shown for a nitric acid plant. Manufacturing costs are estimated based on raw material, utility, labor, and fixed capital investment costs. Percentages of total cost accounted for by each cost category are also calculated.
This document summarizes a project to design and model a solid oxide fuel cell (SOFC) system using HYSYS simulation software. The design follows a 7-level process design hierarchy outlined by Douglas. The SOFC system is fueled by natural gas and pressurized air, producing most of its electricity through two SOFC units with the remainder from two turbines. Key components of the SOFC process include methane, oxygen, hydrogen, and carbon dioxide. The economic analysis of the final design shows an after-tax rate of return of 8.5%, making it a potentially attractive investment.
The topic of our presentation is Cost of production. So, we have come to know that how the firm is working systematically with all its process and methods .The firm has different units to the production of dairy products, which has its own automatic machines for its output. we discovered that the functioning of each product is very smoothly which is easier for the production incharges to put the tags ,logos ,prices and detailing on the packaging. The manager of the dairy firm had practically explained and showed the graphical data from 2015-20 about the revenue ,profits ,losses ,expenses and investment, expenditure . the manager had also said that how these were ranging and how the firm got their product familiar and popular to their consumer. As their product were reaching at the maximum level, their TRP got high through the consumer’s taste and preference.
Boiler Efficiency Improvement through Analysis of Lossesijsrd.com
Thermal is the main source for power generation in India. The percentage of thermal power generation as compare to other sources is 65 %. The main objective of thermal power plant is to fulfill the energy demands of the market and to achieve these demands; plant requires technical availability with the parts reliability and maintenance strategy. This paper deals with the determination of current operating efficiency of Boiler and calculates major losses for Vindhyachal Super thermal power plant (India) of 210 MW units. Then identify the causes of performance degradation. Also find the major causes of heat losses by Fault Tree Analysis (FTA) and recommends its appropriate strategy to reduce major losses. The aim of performance monitoring is continuous evaluation of degradation i.e. decrease in performance of the steam boiler. These data enable additional information which is helpful in problem identification, improvement of boiler performance and making economic decisions about maintenance schedule.
2016.12.14 DryFining Coal Gen presentation FINALSandra Broekema
The document summarizes 6 years of operating experience with DryFining, a coal drying process. It has upgraded 1000 tons per hour of lignite coal since 2009, reducing moisture from 38% to 30% by weight. This has increased the coal's heating value and reduced emissions while improving the net plant heat rate by 4.5%. Case studies show the process can increase generation capacity at coal plants and reduce capital and operating costs. The process provides more flexible, efficient fuel enhancement that benefits both new and existing coal-fired power facilities.
The objective of this applied research is to compare the values of the different exergoeconomic variables of the Open Cycle Gas Turbine (OCGT) calculated during summer atmospheric conditions to the values obtained from the simulation of the plant using design conditions.
This document proposes replacing the conventional diesel generator and battery-based power system used by EthioTelecom with a hybrid system incorporating a fuel cell, microturbine, and DC/DC converter. It analyzes the technical specifications and performance of the system components, models the new system, and compares the costs, emissions, and reliability to the conventional system. The analysis finds that the hybrid system has lower operating costs, reduced emissions, higher reliability, and a payback period of around 6 years, making it a more sustainable option for telecom power in Ethiopia.
This document contains information about thermodynamic properties and processes. It includes a table with temperature and enthalpy values for water and ammonia. It also contains exam questions on various thermodynamic cycles and concepts like the Otto cycle, diesel cycle, refrigeration, and gas turbines. Key topics covered include ideal gas processes, heat engines, refrigerators, availability analysis, and the first and second laws of thermodynamics.
This document provides procedures for conducting a Gross Turbine Cycle Heat Rate (GTCHR) test on a steam turbine. The test is used to measure the overall efficiency of the turbine cycle and its auxiliaries. Key steps include operating the unit at a steady load and temperature conditions, collecting instrumentation data like steam and water temperatures and pressures, and calculating the turbine cycle heat rate in kcal/kWh based on enthalpy values and steam and water flows. The test report includes computation of main steam, reheat, and extraction steam flows along with the final heat rate value.
This document contains exercises and problems related to cost accounting concepts like economic order quantity, reorder point, safety stock, and ABC analysis. Exercise 8.1 provides production scheduling details. Exercise 8.2 calculates order quantities based on forecast demand. Other exercises calculate EOQ, carrying costs, order costs under different scenarios. Problems calculate optimal order size, number of production runs, economic order quantity, and reorder point considering usage patterns and costs.
This document outlines the design of a process to produce 50,000 metric tons per year of 99.5% dimethyl ether (DME) from methanol. Key aspects of the design include using 259.6 kmol/hr of 99% methanol feed, a single reactor with catalyst operating at 250°C and 80% conversion, and two distillation columns to separate DME and methanol. Economic analysis shows a negative net present value over 10 years, indicating the design is not financially viable based on the assumptions.
This document contains instructions for a Thermal Engineering exam. It has 12 questions divided into two sections. The first section has 6 questions on topics like Orsat apparatus, coal combustion analysis, steam properties, Rankine cycle, boiler types and trials. The second section has questions on second law of thermodynamics, heat pumps, available energy, diesel cycle analysis, internal combustion engines, and their systems. Students are instructed to answer questions by section in separate answer books. Diagrams, tables, and calculators may be used. Data should be assumed if necessary.
1. The document provides information on cost allocation for an engineering company across different departments.
2. Equations are set up to calculate the costs of Stores and Maintenance departments, with Stores costs calculated to be Rs. 1,045 and Maintenance costs calculated to be Rs. 905.
3. Overhead rates are then calculated for different departments based on the cost allocations to Machining, Assembly and Finishing departments.
This document discusses standard costing and variance analysis. It contains:
1) An explanation of how standards are used in budgeting and the standard-setting process.
2) Descriptions of direct material, direct labor, and factory overhead variances and how they are calculated.
3) Examples showing the calculation of price, quantity, rate, efficiency, flexible budget, and volume variances.
The overall purpose is to explain how to analyze variances between actual and standard costs.
This document discusses various methods for estimating capital costs for chemical engineering projects. It describes different types of cost estimates ranging from order-of-magnitude to detailed estimates. It also covers adjusting costs based on changes in equipment capacity and time. Methods like Lang factors, module cost approach, and total plant cost estimates are outlined. Factors like materials, pressure, and temperature that influence capital costs are also addressed.
Airah Natural Refrigerants Special Interest Group Sydney 30 October 2008rhysemo
The document discusses the benefits of transcritical CO2 cooling and heating systems in office buildings and meat processing plants. It provides several key benefits:
1) Significant reduction in primary energy consumption and electrical energy use compared to traditional HVAC systems due to the higher efficiency of CO2 systems.
2) Reduced cooling water consumption and elimination of Legionella bacteria and HFC fugitive gas emissions.
3) Significant decreases in greenhouse gas emissions from reduced energy use.
4) Potential energy savings of 45-50% in meat processing plants by recovering waste heat from cooling, heating, and freezing processes.
Airah Natural Refrigerants Special Interest Group Sydney 30 October 2008rhysemo
The document discusses the benefits of transcritical CO2 cooling and heating systems in office buildings and meat processing plants. It finds that such systems can significantly reduce primary energy consumption, electrical energy use, cooling water use, and greenhouse gas emissions compared to traditional HVAC systems. This is due to the improved efficiency of CO2 as a refrigerant and the ability to provide both heating and cooling from one system. The document also recommends considering total energy inputs and parasitic loads when selecting compressor equipment.
- The document discusses Mayekawa Mfg. Co., Ltd.'s NH3/CO2 refrigeration system called "NewTon". It aims to provide energy conservation and comply with environmental regulations by using natural refrigerants.
- NewTon uses a prefabricated package for the NH3 refrigeration cycle that is tested and assembled in the factory prior to shipping. This allows for quicker onsite installation and minimizes NH3 charge.
- Performance data shows NewTon provides significant power reductions of 19-41% compared to previous HCFC-22 systems in various cold storage applications. It also has higher energy efficiency factors compared to HCFC-22 freezer systems.
This document appears to be a question paper for an engineering thermodynamics exam consisting of multiple choice and numerical problems. It covers topics like thermodynamic equilibrium, Carnot cycle efficiency, ideal gas properties, vaporization enthalpy, adiabatic saturation temperature, gas turbine cycle analysis, heat pumps, refrigeration, steam power cycles, psychrometrics, and Maxwell relations. The problems involve calculations related to compression, expansion, heat transfer, work, efficiency, and using properties from thermodynamic tables and charts.
Design and Simulation of Divided Wall Column - Design of the ColumnHariKirant29
The document summarizes the design and simulation of a divided wall column for separating reformate into benzene, toluene, and p-xylene. It includes the reformate composition, literature review on divided wall columns, material and energy balances, minimum number of trays calculation, Aspen simulation, materials selection, and a cost analysis. The divided wall column consists of a prefractionator with 13 trays separating to a side draw and a main column with 9 + 10 trays achieving high purity products within specifications. The simulation matches the material balances with less than 1% difference. The total capital cost is estimated at $1.67 billion with a payback period of 2.8 years.
2. 6. Energy balance on dryer
• Solid matter in Dry starch and wet starch = 2441 kg/day
• Initial air condition = T= 20o
C (h0=30kJ/kg), and 50% RH, H1 =0.0074 kg of water/ kg dry air
• Product temperature when it leaves drier =450
c
• Heated air entering in to the drier = 400
C at 25% RH, enthalpy of in let air (ha1)
ha1=71Kj/kg dry air, where RH= relative humidity
• Enthalpy required to heat the air = ha1 – h0 = 71-30 = 41kJ/kg
• Air temperature leaving the drier = 35 0
C
• Latent heat of vaporization at 0 0
C = 2507KJ/kg
• Specific heat of air (Cp,a) = 0.24 + 0.46 (H)
• Specific heat of solid matter of the product (Cp,e) =2.32 kJ/kg0
c
• Specific heat of water (Cw) = 4.2 kJ/kg0
C
• Energy estimated to be released in order to dry the starch.
• Feed temperature = 250
C
• H1& H2 is absolute humidity of air
• A = is flow rate of air
• Enthalpy of Feed = hwe
• Enthalpy of product = hde
• Enthalpy of inlet air = ha1
• Enthalpy of out let air = ha2
A(H2-H1)= 2441-1666 = 775 kg /day ........................................1
mwet starch(hwe) + A (ha1) = mdry starch (hde) + A (ha2) ---------------------------- [2]
1.hwe = Cpstarch* ΔT + W1 .CpH2O. ΔT
hwe = 1.75 kJ/kg0
C (250
c) + 0.25(4.2)( 250
c)
hwe=70 kJ/kg
3. 2. hde = CpstarchΔT + Ws2*CpH2O * ΔT
hde = 1.75 kJ/kg (45) + 0.052(4.2)(45)
hde = 88.75 kJ/kg
3. ha2 = Cs ΔT + λ H2
ha2 = (0.24 +0.46H2) (35) + 2507.4H2
ha2 = 8.4 +2523.5H2---------------------------------------------- [3]
Inserting eq. 3 in eq.2
2441(70) + A (71.0) = 1666(88.75) + A (8.4 +2523.5H2)
170,870+A (71.0) =147,857+ 2523.5AH2----------------------- [4]
Taking Eq. [1] and inserting it in eq. [4]
from Eq. [1]
AH2=775+AH1=775+A( 0.012 Kg/ kg dry air)
then Eq. [4]
170870+A (71.0) =147,857+ 2523.5(775+A( 0.012 ))
170870+A (71.0) =147,857+1,302,050.3+A(30.2)
A=3,1196 kg/day
Inserting A in eq.1
A (H2 - H1) =775 kg/day
H2=(775 +31196 *0.012) /31196
H2=0.0368 Kg/ kg dry air
Inserting H2 in eqution3.
ha2 = 8.4 + 2523.5 (0.0368kg/kg dry air)
ha2 = 101.37kJ/Kg
4. Table 6.1: Specification Equipments
Equipments quantity type capacity Power needed
for driving
Centrifuge Separator 1 Vertical Cylinder 0.186m3
/hr 65kw/hr
Dryer 2 Flash pan type 4.04m2
125kwhr
Heat Exchanger 3 Plate type 0.5m2
75kw/hr
Pump 3 centrifuge 0.396m3
/hr 1.5kwhr
Air filter 1 Vertical Basket 10m3
/hr 50kw/hr
Belt conveyer 1 horizontal 3m 15kw/hr
Packing machine 1 general 25packets/min 95kw/hr
Total 426.5kw/hr
Source; Coulson and Sinnot volume-6 and www.machte.com
5. The total annual total energy consumption to drive each equipment’s, assuming the will be 300
working days.
=426.5kw/hr *24hr *300
=3,070800kw/year
Also by approximation for lighting and other related services around 20,000kw per year
consumed. Therefore the total electric energy consumed is the sum total energy needed for
equipments and for lighting.
=3,070800kw +20,000kw
= 3090800kw/year
Process flow diagram
6. 7. ECONOMIC EVALUATION OF THE PROJECT
7.1 PLANT CAPACITY AND PROPOSED LOCATION
Based on the market study, the envisaged plant is proposed to have annual production capacity of
500 tones. The plant will operate in a single shift of 8 hours a day, and for 300 days a year.
CORN STARCH is mainly consumed by the Pharmaceutical industry, food industry , textile
industry….. The location for the plant is a compromise between the availability of major raw
material corn/ maize and market for the finished product starch and modified starch. The
availability of the basic infrastructure like electricity, water, and road which are vital for the
smooth operation of the plant.
7.2. Estimation of equipment costs
Assuming new equipment is similar to a base item where cost data is available, Equation below
explains the equipment cost estimation process, where EPC is Equipment Purchased Cost, Q and
QO are the new and base equipment capacities, respectively, and a is the exponent of the power
law function given by the user. By default, this exponent is set as 0.6 for estimating new
equipment cost (Whiteside, 2007 and Harriso, 2003).The cost of major equipment was evaluated
based on cost data on 1997, 2000 and 2004 and bring back to equivalent cost to 2014 applying
cost index techniques.
EPC = Co (Q/Qo) a
Where, EPC= Cost of purchased equipment
Co= cost of base line equipment
Q= capacity purchased equipment
Qo= capacity baseline equipment
Calculating using above equation the equipment’s costs as summarized in table 7.1
Table 7.1: Specification and costs of the major equipment’s
7. No Name Size Unit Unit cost
($)
Total ($)
1 Raw material
storage
77(m3
) 1 2000 40000
2 Steeping tank 9.3(m3
) 3 1500 90000
3 De germination 6 (m3
) 1 3500 70000
4 Grinding 2ft? 1 1200 24000
5 Centrifuge 2m(diameter) 1 1200 24000
6 Separation unit 2m(diameter) 1 500 10000
7 Dryer 4tf2
2 3500 140000
8 Modification
tank
1.5(m3
) 2 2500 100000
9 Storage tank 10.5(m3
) 1 1000 20000
Tota
l
710,000 ETB
Source; A=coulsen and Sinnot volume-6, B= www.machte.com and www.alibaba.com,
C=Whitesides, W., 2007,D= Plant design and Economics, fourth edition
Estimation of total capital investment Cost
SINCE WE KNOW THE COSTS OF PURCHASED EQUIPMENT:
PEC = 25% OF FCI(FIXED CAPITAL INVESTMENT)
SO WE CAN CALCULATE THE FCI AND IT WILL BE
710,000 ETB /0.25 = 2,840,000 ETB
Items Cost (ETB)
Purchased Equipment costs (FCI) 710,000
Installation 9%FCI 255,600
Processing piping 8%FCI 227,200
Instrumentation7% FCI 198,800
Electrical 10% FCI 284,000
Buildings 6% FCI 170,400
8. Yard improvements 3% FCI 85,200
Auxiliary Facility 25%FCI 710,000
Total Direct Costs (DC) 2,641,200
Total Indirect Costs (IC):
Engineering 8% FCI 227,200
Construction 10% FCI 284,000
Total Indirect costs (IC) 511,200
Other Costs (OC)
Contractor’s Fee 3% FCI 85,200
Contingency 5% FCI 142,000
Total other costs (OC) 227,200
Fixed Capital Investment (FCI) Costs 2,868,400 ETB
Working capital (25%FC) 573,680
Total capital investment (TCI) 3,442,080
Estimation of total production or operation cost (TPC)
The production cost divide into manufacturing costs and general expenses cost. Total production
cost is the sum manufacturing and general expenses.
1.1.1. MANUFACTURING COSTS (MC)
MC =Direct Manufacturing Costs (DMC) +Fixed Manufacturing Costs (FMC) + Plant over
head cost (POC)
i. Direct manufacturing cost (DMC)
Direct production costs are calculated and equal the sum of the following items as specified
within the processes: Raw materials, operating Labor, direct supervisor and clerical labor,
Laboratory, Utilities and operating supplies.
9. Raw materials (CRM): two different major raw materials are used in the corn starch production
process in this project for economic purposes: corn/maize and water. Itemized raw material costs
are summarized and listed in Table 7.2
Table 7.2: Raw materials
Raw materials unit cost (ETB/kg) Annual amount (kg/year) Annual cost (ETB/year)
Corn /maize 5 819,600Kg/year 4,098,000
Water(m3
) 0.86 ETB 1,393.2 (m3
) 1200
Total 4,099,200
Source: material balance on steeping section 5.1
Utilities (CUT): three different utilities are examined in the CORN STARCH production process
in this project for economic purposes: electricity, Lubricating oil and cooling water. Itemized
utility costs are summarized and listed in Table 7.3.
10. Table 7.3 Utility costs for sodium bicarbonate production
Utility unit cost (ETB/unit) Annual amount Annual cost(ETB)
Electricity (Kw/year) .45 3090800 1390860
Lubricating oil (lt.) 6.2 4838.75 30,000
water (m3
) 4.3 *10-3
2786400kg/year 240
Total 1421100 ETB
Sources: materials and energy balance calculation section 5.1and 5.2
Operating Labor (COL)
The plant requires 35 workers, and their annual expenditure, including fringe benefits, is
estimated at Birr 336,960 ETB. For details see Table 7.4 below.
Table 7.4 Manpower requirement and annual labor cost
Sr.
No.
Description Req.
No.
Salary, (Birr)
Monthly Annual
1 Plant manager 1 4,500 54,000
2 Secretary 1 1000 12,000
3 Accountant 1 1200 14,400
4 Production head 1 1,800 21,600
5 Operator 6 6,000 72,000
6 Assistant
operators
3 3,600 43,200
7 Mechanic 1 1,200 14,400
8 Electrician 1 1200 14,400
9 Store keeper 1 500 6,000
10 Purchaser 1 1000 12,000
11 Sales man 1 1000 12,000
12 Personnel 1 900 10,800
13 Time keeper 1 400 4,800
15 Driver 2 700 16800
11. 17 Guard 2 500 6,000
18 Cleaner 1 400 4,800
Sub-total 25 22,300 280,800
Employee benefit
(10% BS)
2808
Total 336,960 ETB
Direct supervisor and clerical labor (CSC); the cost of supervisor and clerical labor is estimated
CSC = aSCCOL ( aSC = 0.18)
=18% of operating labor (COL)
= 0.18 *336,960= 60,653
Maintenance and repairs (CMR)
CMR = aMRFCI (aMR = 0.06)
= 0.06 * fixed capital investment (FCI)
=0.06*2,868,400
= 172,104
Laboratory charges (CLC)
CLC = aLCCOL (aLC = 0.15)
=15% of operating labor (COL)
=0.15*336,960
=50,544
Patents/royalties, CPR= aPRTPC (aLC = 0.03)
= 0.03TPC
Direct production cost (DMC)
DMC=CRM + CUT + 1.33 COL+ 0.03 TPC + 0.069 FCI
= 4,917,720+578,080 +1.33*336,960 +0.069*$2,868,400 +0.03TPC
=6,141875 +0.03TPC
12. ii. Fixed Manufacturing Costs (FMC).
This costs the sum of depreciation, insurance and taxes
The depreciation (DEP) item is calculated using a straight-line depreciation method,
considering a salvage value fraction (f) of the fixed capital investment (FCI), which is assumed
10 % in this analysis by default. The depreciation period (n) is set to ten years by default.
Equation 6.4 is used to calculate depreciation:
DEP=
= ………………2,868,400*(1-
0.1)/10
258,156
FMC = CTI + CDEP = 0.32 FCI +CDEP
= 0.32*2,868,400 +258,156
13. =1,176,044
7.4.2 GENERAL EXPENSES (GE)
GE = Administrative Cost (AC) +Other Costs (OC)
Administrative (AC) expenses include costs for executive and clerical wages, office supplies,
engineering and legal expenses, upkeep on office buildings, and general communications.
Other costs (OC); includes distribution, selling, research and development costs
GE=Administrative Cost (AC) +Other Costs (OC) =50 %( operating labor + supervision +
Maintenance)
Administration costs (CAD)
CAD = aAD (COL +CSC + CMR); (aAD = 0.15)
CAD = aAD (COL + 0.18COL + 0.06 FCI) = 0.177 COL + 0.009 FCI
Distribution and sales costs (CDS)
CDS = aDS TPC =0.11 TPC ; (aDS = 0.11)
R&D (CRD)
CRD = aRD TPC = 0.05 TPC ; (aRD = 0.05)
Financing costs=0.04 FCI
GE =CAD +CDS +CRD +CF
GE = 0.177 COL + 0.009 FCI + 0.11TPC + 0.05TPC + 0.04 FCI
GE = 0.177 COL + 0.049 FCI + 0.16TPC
= 0.177*336,960 +0.049*2,868,400+0.16TPC
=200,194 +0.16TPC
TPC = MC + GE = (DMC+ FMC ) + (AC +OC)
TPC = CRM+CUT +1.33 COL+ 0.03 TPC+ 0.069 FCI + 0.032 FCI +CDEP +0. 708 COL + 0.032
FCI + 0.177 COL + 0.009FCI + 0.16 TPC
TPC = 1.24(CRM+CUT +CDEP) + 2.74 COL + 0.23 FCI
14. = 1.24*(4,917,720+578,080 +258,156) +2.74*336,960 + 0.23*2,868,400
=$1,369,503.8……(6,717,908 ETB)
Therefore;
DMC=6,141875 +0.03TPC
=6,141875 + 0.03 *6,717,908
= 6,343,412
GE=200,194 +0.16TPC
=200,194 +0.03*6,717,908
= 401,731
Unit Cost Analysis
The unit costs for corn starch production are calculated as the quotient of the annual operating
cost divided by the annual production rate.
Unit cost (ETB/kg) =
= = 6,717,908 /500,000 /
=13.5 ETB/kg
Corn starch selling Price
In order to conduct the profitability analysis, the selling price for corn starch must be first
identified. From local?26? market of the current corn starch price is 15?? per kilogram and
international selling price is $0.76 per kilogram of corn starch. So the unit corn starch price per
15. kilogram is calculated and equals ETB13.5/kg. For profitability let it will sell with current local
market value.
Profitability Analysis
According to the projected income statement, the project will start generating profit in the first
year of operation. Important ratios such as profit to total sales, net profit to equity (Return on
equity) and net profit plus interest on total investment (return on total investment) show an
increasing trend during the life-time of the project. To calculate the gross profit let we calculate
the sales value per annual.
i. Sales (Sales Revenue)
Sales= unit cost * annual capacity
=13.3??$/kg*500,000kg/year
6750000 ETB /year if 14
7,000,000 ETB
ii. Gross profit (GP)
Gross profit (GP) = Sales – TPC
=7,000,000-$8,717,908
=880,496.2 32,092 = 282092
iii. Netprofit (NP)
Net profit=Gp-[sales –TPC]*tax rate
=Gp-Gp*0.35
=Gp [1-0.35]
= 282092*0.65
=183,360 ETB
16. iv. Turn over Ratio
Turnover ratio is defined as the ratio of gross annual sales to the fixed-capital investment where
the product of the annual production rate and the average selling price of the commodities are the
gross annual sales figures. The reciprocal of the turnover ratio is sometimes defined as the
capital ratio or the investment ratio. Turnover ratios of up to 5 are common for some business
establishments and some are as low as 0.2. For the chemical industry, as a very rough rule of
thumb, the ratio can be approximated as 1.
Turnover=
7,000,000 /2,868,400
=
= 2.444
So, our project acceptable to establishment since turn ratio between the maximum and minimum
range [0.2-5]
17. 7.61 PAYBACK PERIOD
The payback period is a simple indicator measuring how long it takes to recover the initial
investment in the corn starch production plants. When choosing among a few mutually exclusive
projects, the project with the quickest payback is preferred. The payback period is calculated as
the quotient of the total capital investment divided by the net profit as shown in equation below.
Payback period =
8,717,908/183,360 = 36?????
=
=3.6years
1.1.1. CASH FLOW
Table 7.5: cash flow of sodium bicarbonate Production
Year Fixed
capital
Working
capital
sales Total
operating
cost
Gross
profit
Depreciation Taxes N
-2 -1,661,404 0 0 0 0 0 0 0
18. -1 - 1,661,404 0 0 0 0 0 0 0
0 0 -415,351 0 0 0 0 0 0
1 0 0 2,250,000 1,369,503.8 880,496.2 149,526.4 308,173.7 5
2 0 0 2,250,000 1,369,503.8 880,496.2 149,526.4 308,173.7 5
3 0 0 2,250,000 1,369,503.8 880,496.2 149,526.4 308,173.7 5
4 0 0 2,250,000 1,369,503.8 880,496.2 149,526.4 308,173.7 5
5 0 0 2,250,000 1,369,503.8 880,496.2 149,526.4 308,173.7 5
6 0 0 2,250,000 1,369,503.8 880,496.2 149,526.4 308,173.7 5
7 0 0 2,250,000 1,369,503.8 880,496.2 149,526.4 308,173.7 5
8 0 0 2,250,000 1,369,503.8 880,496.2 149,526.4 308,173.7 5
9 0 0 2,250,000 1,369,503.81 880,496.2 149,526.4 308,173.7 5
10 0 0 2,250,000 1,369,503.8 880,496.2 149,526.4 308,173.7 5
Source: “Economic evaluation report” and “Cash flow analysis report” from Plant design and
Economics for chemical engineers, Fourth edition and Sinnott, 1993 and sodium bicarbonate
production data.
7.62BREAKEVEN POINT ANALYSIS (BEP)
Breakeven point is the point when total annual production cost equals total annual sales. That is
the point where profit equals zero. The breakeven point is determined from the relation:
BEP =
Where Sup=Selling price per unit of production
Vcup = Variable costs per unit of production
vcup=
=
=2.71$/kg