The document summarizes the energy balance for a mixer and reactor used in a chemical process. It provides equations and tables to calculate the heat of reactions, input and output enthalpies, heat generated, and cooling water requirements. The key reactions and temperatures at each stage are described. Exothermic reactions occur in the reactor, generating heat that must be removed by cooling water. Mass and energy balances are performed to calculate the required cooling water flow.
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.
The document describes a proposed process to produce 50,000 metric tons per year of dimethyl ether (DME) through the catalytic dehydration of methanol. Key aspects of the process include:
- Methanol and recycled methanol will be mixed, vaporized, and sent to a fixed bed reactor operating at 350°C to produce DME and water.
- The reactor effluent will be cooled and separated into DME product and a stream of methanol and water using two distillation columns.
- The project tasks involve developing a process flow diagram, performing material balances, equipment sizing and costing, estimating capital and operating costs, and evaluating the economic viability of the process.
The document summarizes the energy balance for a mixer and reactor used in a chemical process. It provides equations and tables to calculate the heat of reactions, input and output enthalpies, heat generated, and cooling water requirements. The key reactions and temperatures at each stage are described. Exothermic reactions occur in the reactor, generating heat that must be removed by cooling water. Mass and energy balances are performed to calculate the required cooling water flow.
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.
The document describes a proposed process to produce 50,000 metric tons per year of dimethyl ether (DME) through the catalytic dehydration of methanol. Key aspects of the process include:
- Methanol and recycled methanol will be mixed, vaporized, and sent to a fixed bed reactor operating at 350°C to produce DME and water.
- The reactor effluent will be cooled and separated into DME product and a stream of methanol and water using two distillation columns.
- The project tasks involve developing a process flow diagram, performing material balances, equipment sizing and costing, estimating capital and operating costs, and evaluating the economic viability of the process.
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.
The document discusses various technologies for producing ethylbenzene and styrene including liquid-phase zeolite-catalyzed and aluminum chloride processes for ethylbenzene production and catalytic dehydrogenation for styrene. It also covers developing technologies like a process using ethane and benzene and Exelus' process using methanol and toluene. The document provides economic analyses of different production routes and supply/demand forecasts for various regions.
The document provides background information on the proposed Carbon Plus Corporation activated carbon manufacturing project in Quezon Province, Philippines. It discusses the need for the project due to the growing demand for activated carbon and lack of local suppliers. The company aims to produce activated carbon from abundant local coconut shells to service the purification needs of various local industries in a more affordable, sustainable manner. It introduces the company vision to be a leading local activated carbon supplier through quality products, job creation and customer satisfaction.
This document discusses enthalpy balances in distillation. It defines enthalpy and provides enthalpy-concentration diagrams. Equations for total and individual enthalpy balances are presented for the rectifying and stripping sections. The document describes how to solve the equations using an iterative approach with enthalpy data. It also discusses how to calculate the feed enthalpy parameter q using enthalpy values. An example problem calculates q for a benzene-toluene mixture.
(LTS) Low Temperature Shift Catalyst - Comprehensive OverviewGerard B. Hawkins
The document discusses low temperature shift catalysts used in hydrogen production plants. It describes the purpose of low temperature shift catalysts in further converting carbon monoxide to carbon dioxide to improve hydrogen yield and remove impurities. It then covers the chemistry, typical operating conditions, factors influencing catalyst activity like temperature profile and poisons, and byproduct formation issues. The document promotes the VSG-C111/112 series as superior catalysts, highlighting their resistance to poisons like sulfur and chloride, low methanol byproduct formation, high activity, and strength properties.
This is great Presentation with 3D effects which is all about production of ammonia from natural gas.
I am damn sure you will be getting everything here searching for.
its better to download it and then run in powerpoint 2013.
1. Ammonia is industrially synthesized from nitrogen and hydrogen through the Haber process. It is produced on a large scale, exceeding 130 million tonnes annually.
2. The synthesis of ammonia is an equilibrium reaction that is exothermic and favored by high pressure and low temperature. Industrial production occurs at 400-500°C and 150-300 atmospheres using an iron catalyst.
3. Haber optimized the process by implementing a recycling system to increase space-time yield, improving economic production. His recycling design is still used as the basis for industrial ammonia synthesis.
This document summarizes the key properties, production, and uses of urea. It discusses that urea has a molecular weight of 60.05 and formula of NH2·CO·NH2. It is used primarily as a solid or liquid fertilizer but also in resins, animal feed, and other applications. Urea production involves compressing ammonia and carbon dioxide in an autoclave, then processing the liquid effluent through flash drums to form an aqueous urea solution or molten urea that is prilled into granules. The main raw materials are ammonia and carbon dioxide.
This document describes a design project report on adipic acid produced by students Shivika Agrawal, Nikhil Nevatia, and Satish Pillai. It includes chapters on the introduction to adipic acid, market analysis of global and Indian demand and production capacity, a comparison of production processes and selection of a process, material and energy balances, equipment design, and a cost estimation. The main points are that adipic acid is mainly used to produce nylon 6,6 and has a global demand of 3.3 million metric tons growing at 3-5% annually, with China as the largest importer and Europe the largest market. India currently imports its requirements of adipic acid.
Urea Dust & Ammonia Emission Control Prill Tower Project at Al BayroniAli Akbar
This document summarizes a presentation given about a project to control urea dust and ammonia emissions from a prilling tower at an urea plant in Saudi Arabia. The project involved installing an air cleaning unit with acid wash scrubbers to absorb urea dust and ammonia from the exit air stream. The absorbed materials were then sent to a crystallization unit to produce ammonium sulfate as the final product. The project successfully reduced urea dust and ammonia emissions below international standards and produced a new fertilizer product. It provided lessons learned for other plants seeking to control emissions from prilling towers.
Toluene is an aromatic hydrocarbon that is a colorless, flammable liquid with a benzene-like odor. It is insoluble in water but soluble in organic solvents. Toluene's main uses are as a precursor to benzene in chemical production, as an octane booster in gasoline, and as an industrial solvent. It is emitted from facilities involved in crude oil and natural gas extraction and petroleum refining.
The document discusses key concepts in multicomponent distillation including:
- Key components are chosen to indicate separation and are always distributed between products.
- The Fenske equation is used to determine minimum number of stages assuming constant relative volatility, while the Underwood method determines minimum reflux ratio.
- The Gilliland correlation estimates actual number of stages given operating reflux from minimum values.
Methanol is the simplest alcohol and can be used as an alternative fuel or chemical feedstock. It is produced via a four step process: feed purification using desulphurization; steam reforming of natural gas over nickel catalysts at high pressures and temperatures; methanol synthesis over copper catalysts in a reactor; and methanol purification through distillation. Methanol production facilities are located globally and the demand for methanol is increasing in countries like India at 7-8% annually.
This document outlines the production of acetic acid by a company with the following organizational structure and directors:
- The company will produce acetic acid using methane as a raw material through two reactor processes. Acetic acid is separated from the products in a separator.
- Key factors in selecting a plant site include availability of raw materials, utilities, land, and minimizing environmental impact from effluent disposal. Three potential sites are identified and evaluated.
- Equipment for the process is designed including reactors, separator, heater and cooler. A process flow diagram is presented along with cost analysis and profitability calculations showing the project has positive net present value.
Calculation guidelines for Rotary Dryer.pdfEd Ryan Ruales
The document outlines the design procedure for a rotary dryer used to dry fertilizer from 5% to 1.5% moisture content. The key steps are:
1) Performing mass and heat balance calculations to determine moisture evaporated, dry solid mass, and total heat duty of 4.4 MJ/hr.
2) Sizing the dryer using the heat duty to calculate required air flow of 14.8 kg/hr, diameter of 2.3 m, volumetric heat transfer coefficient of 398 kJ/hr-m3-K, and length of 18 m.
3) Checking that the outlet air humidity is below saturation and selecting design parameters like number of flights based on sol
Haiku Deck is a presentation tool that allows users to create Haiku style slideshows. The tool encourages users to get started making their own Haiku Deck presentations which can be shared on SlideShare. In just a few clicks, users can design beautiful, minimalist slideshows.
Final Year Project - Production of Aniline from Ammonolysis of Phenol Ismail Zahoor
A process for preparing aniline by direct amination of phenol with ammonia in the vapor phase in the presence of a solid, heterogeneous catalyst. It has been discovered that significant process improvement are obtained if the phenol feed to the reaction is vaporized in the absence of substantial amounts of ammonia.
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.
The document discusses various technologies for producing ethylbenzene and styrene including liquid-phase zeolite-catalyzed and aluminum chloride processes for ethylbenzene production and catalytic dehydrogenation for styrene. It also covers developing technologies like a process using ethane and benzene and Exelus' process using methanol and toluene. The document provides economic analyses of different production routes and supply/demand forecasts for various regions.
The document provides background information on the proposed Carbon Plus Corporation activated carbon manufacturing project in Quezon Province, Philippines. It discusses the need for the project due to the growing demand for activated carbon and lack of local suppliers. The company aims to produce activated carbon from abundant local coconut shells to service the purification needs of various local industries in a more affordable, sustainable manner. It introduces the company vision to be a leading local activated carbon supplier through quality products, job creation and customer satisfaction.
This document discusses enthalpy balances in distillation. It defines enthalpy and provides enthalpy-concentration diagrams. Equations for total and individual enthalpy balances are presented for the rectifying and stripping sections. The document describes how to solve the equations using an iterative approach with enthalpy data. It also discusses how to calculate the feed enthalpy parameter q using enthalpy values. An example problem calculates q for a benzene-toluene mixture.
(LTS) Low Temperature Shift Catalyst - Comprehensive OverviewGerard B. Hawkins
The document discusses low temperature shift catalysts used in hydrogen production plants. It describes the purpose of low temperature shift catalysts in further converting carbon monoxide to carbon dioxide to improve hydrogen yield and remove impurities. It then covers the chemistry, typical operating conditions, factors influencing catalyst activity like temperature profile and poisons, and byproduct formation issues. The document promotes the VSG-C111/112 series as superior catalysts, highlighting their resistance to poisons like sulfur and chloride, low methanol byproduct formation, high activity, and strength properties.
This is great Presentation with 3D effects which is all about production of ammonia from natural gas.
I am damn sure you will be getting everything here searching for.
its better to download it and then run in powerpoint 2013.
1. Ammonia is industrially synthesized from nitrogen and hydrogen through the Haber process. It is produced on a large scale, exceeding 130 million tonnes annually.
2. The synthesis of ammonia is an equilibrium reaction that is exothermic and favored by high pressure and low temperature. Industrial production occurs at 400-500°C and 150-300 atmospheres using an iron catalyst.
3. Haber optimized the process by implementing a recycling system to increase space-time yield, improving economic production. His recycling design is still used as the basis for industrial ammonia synthesis.
This document summarizes the key properties, production, and uses of urea. It discusses that urea has a molecular weight of 60.05 and formula of NH2·CO·NH2. It is used primarily as a solid or liquid fertilizer but also in resins, animal feed, and other applications. Urea production involves compressing ammonia and carbon dioxide in an autoclave, then processing the liquid effluent through flash drums to form an aqueous urea solution or molten urea that is prilled into granules. The main raw materials are ammonia and carbon dioxide.
This document describes a design project report on adipic acid produced by students Shivika Agrawal, Nikhil Nevatia, and Satish Pillai. It includes chapters on the introduction to adipic acid, market analysis of global and Indian demand and production capacity, a comparison of production processes and selection of a process, material and energy balances, equipment design, and a cost estimation. The main points are that adipic acid is mainly used to produce nylon 6,6 and has a global demand of 3.3 million metric tons growing at 3-5% annually, with China as the largest importer and Europe the largest market. India currently imports its requirements of adipic acid.
Urea Dust & Ammonia Emission Control Prill Tower Project at Al BayroniAli Akbar
This document summarizes a presentation given about a project to control urea dust and ammonia emissions from a prilling tower at an urea plant in Saudi Arabia. The project involved installing an air cleaning unit with acid wash scrubbers to absorb urea dust and ammonia from the exit air stream. The absorbed materials were then sent to a crystallization unit to produce ammonium sulfate as the final product. The project successfully reduced urea dust and ammonia emissions below international standards and produced a new fertilizer product. It provided lessons learned for other plants seeking to control emissions from prilling towers.
Toluene is an aromatic hydrocarbon that is a colorless, flammable liquid with a benzene-like odor. It is insoluble in water but soluble in organic solvents. Toluene's main uses are as a precursor to benzene in chemical production, as an octane booster in gasoline, and as an industrial solvent. It is emitted from facilities involved in crude oil and natural gas extraction and petroleum refining.
The document discusses key concepts in multicomponent distillation including:
- Key components are chosen to indicate separation and are always distributed between products.
- The Fenske equation is used to determine minimum number of stages assuming constant relative volatility, while the Underwood method determines minimum reflux ratio.
- The Gilliland correlation estimates actual number of stages given operating reflux from minimum values.
Methanol is the simplest alcohol and can be used as an alternative fuel or chemical feedstock. It is produced via a four step process: feed purification using desulphurization; steam reforming of natural gas over nickel catalysts at high pressures and temperatures; methanol synthesis over copper catalysts in a reactor; and methanol purification through distillation. Methanol production facilities are located globally and the demand for methanol is increasing in countries like India at 7-8% annually.
This document outlines the production of acetic acid by a company with the following organizational structure and directors:
- The company will produce acetic acid using methane as a raw material through two reactor processes. Acetic acid is separated from the products in a separator.
- Key factors in selecting a plant site include availability of raw materials, utilities, land, and minimizing environmental impact from effluent disposal. Three potential sites are identified and evaluated.
- Equipment for the process is designed including reactors, separator, heater and cooler. A process flow diagram is presented along with cost analysis and profitability calculations showing the project has positive net present value.
Calculation guidelines for Rotary Dryer.pdfEd Ryan Ruales
The document outlines the design procedure for a rotary dryer used to dry fertilizer from 5% to 1.5% moisture content. The key steps are:
1) Performing mass and heat balance calculations to determine moisture evaporated, dry solid mass, and total heat duty of 4.4 MJ/hr.
2) Sizing the dryer using the heat duty to calculate required air flow of 14.8 kg/hr, diameter of 2.3 m, volumetric heat transfer coefficient of 398 kJ/hr-m3-K, and length of 18 m.
3) Checking that the outlet air humidity is below saturation and selecting design parameters like number of flights based on sol
Haiku Deck is a presentation tool that allows users to create Haiku style slideshows. The tool encourages users to get started making their own Haiku Deck presentations which can be shared on SlideShare. In just a few clicks, users can design beautiful, minimalist slideshows.
Final Year Project - Production of Aniline from Ammonolysis of Phenol Ismail Zahoor
A process for preparing aniline by direct amination of phenol with ammonia in the vapor phase in the presence of a solid, heterogeneous catalyst. It has been discovered that significant process improvement are obtained if the phenol feed to the reaction is vaporized in the absence of substantial amounts of ammonia.
The document discusses hydrogen production via steam reforming of natural gas. Steam reforming involves four steps: reforming, shift conversion, gas purification, and methanation. It produces hydrogen at high efficiency and is the lowest cost production method currently available. However, it also produces carbon dioxide as a byproduct. Newer steam reforming plants use pressure swing absorption to produce 99.99% pure hydrogen. While steam reforming is an efficient process, it contributes to carbon dioxide emissions, so methods to capture and store the CO2 are being investigated.
This document summarizes the results of a network monitoring software evaluation project. It describes the project preparation, introduction, and three phases: research on paid and open source solutions, meetings with stakeholders to understand requirements, and implementation and testing of several solutions. In phase one, over a dozen potential solutions were researched. Phase two involved meetings with IT teams and departments to determine needs. In phase three, solutions like Zabbix, LibreNMS, Nagios, Zenoss, and others were implemented and tested. A final section scores and compares leading candidates like Zabbix, LibreNMS, Nagios, and Zenoss (the overall winner) based on weighted criteria.
Linde compact methane reformer for H2 productionSteve Wittrig
Hydro-Chem has developed a new line of hydrogen generators called HYDROPRIME® based on steam methane reforming technology. HYDROPRIME® units provide hydrogen capacities from 0.3 to 0.9 MM SCFD at ultra-high purity levels and 200 psig pressure. They offer advantages over traditional hydrogen supply methods like higher efficiency and reliability, lower emissions, and easier installation and maintenance.
The document depicts the process of transcription and translation. It shows DNA being unwound and copied into mRNA by RNA polymerase. The mRNA then leaves the nucleus and binds to ribosomes for translation. Transfer RNA molecules deliver amino acids to the ribosome according to the mRNA codons. The amino acids are linked together to form a polypeptide chain.
Makalah ini membahas tentang sintesis asetanilida dari anilin dan asam asetat glasial melalui reaksi substitusi nukleofilik. Reaksi ini melibatkan anilin sebagai nukleofil dan asam asetat glasial sebagai elektrofil. Mekanisme reaksinya terdiri atas dua tahap yaitu adisi nukleofil pada gugus asam karboksilat dan terbentuknya keadaan zat antara.
Aniline is a benzene derivative with an amino group substituted in place of one hydrogen atom. It undergoes various reactions due to both its amino and benzene functional groups. Reactions of the amino group include salt formation, alkylation, acylation, reaction with acetaldehyde, and the carbylamine reaction. Reactions of the benzene ring include oxidation, halogenation, sulfonation, nitration, and the Hofmann Martius rearrangement. Aniline and its derivatives have many pharmaceutical applications as intermediates for drugs like sulfonamides, paracetamol, and herbicides. It is also used to synthesize polymers with interesting redox and acid-base properties.
2. İÇERİK
• ANİLİN ve ÖZELLİKLERİ
• KULLANIM ALANLARI
• KAPASİTE
• PROSES AKIŞ DİYAGRAMI
• EKONOMİK ANALİZ
a. Sabit Sermaye Maliyeti Kestirimi
b. Toplam Sermaye Maliyeti Kestirimi
c. Üretim Maliyeti Kestirimi
d. Karlılık Analizi
• SONUÇ ve TARTIŞMALAR
4. ANİLİNİ TANIYALIM
• FİZİKSEL VE KİMYASAL ÖZELLİKLERİ
• Anilin; renksiz, oldukça rahatsız edici kokulu,
yağsız bir sıvıdır.
• Işık ve hava etkisiyle yükseltgenerek
kahverengileşir.
• Suda çok az çözünür. ( 3,6 g /100 ml 18ºC’de)
• Etanol, benzen, kloroform ve başlıca organik
çözücülerle karışır.
5. FİZİKSEL VE KİMYASAL ÖZELLİKLER
Özellikler Değer Özellikler Değer
Kimyasal formülü C6H5NH2 Kırılma indisi n20 1,585
Molekül Ağırlığı 93,12 g/mol Yanma Isısı 3389,72 kJ/mol
Özgül Ağırlığı 1,022 g/l Gizli Buharlaşma Isısı 478,55 J/g
Kaynama Noktası 184 - 186 ºC Parlama Noktası (Kapalı
Kapta)
70 - 76ºC
Donma Noktası -6,3 ºC Parlama Noktası (Açık
Kapta)
75,5 ºC
Alevlenme Noktası (Kapalı Kap) 70 ºC Kritik Sıcaklık 425,6 ºC
Kendiliğinden Tutuşması
Noktası
371 ºC Kritik Basınç 5,30 MPa
Viskozite (20 ºC'de) 4,423 poise
7. TOKSİKOLOJİK ÖZELLİKLER
• Anilin solunduğunda, deri ile temasında ve
yutulduğunda toksik bir maddedir.
• Gözlerde irritasyon, yaşarma, görüşte
bulanıklık, fotofobiye neden olabilmektedir.
Korneaya zarar verebilmektedir.
• Yutulduğunda, hemoglobin ve
methemoglobini etkiler. Mesleki sinir
sisteminde asfeksiye neden olur.
• Suda yaşayan canlılar için son derece
zararlıdır.
13. Ekipman Parametre Değer Gerekli Veriler
P-101 Pompası
Giriş basıncı 1 atm
W= 0,00578 kW
Çıkış basıncı 1,5 atm
P-102 Pompası
Giriş basıncı 1,5 atm
W= 0,043 kW
Çıkış basıncı 5 atm
C-101 Kompresörü
Giriş sıcaklığı 298 K
W= 3,791 kW
Çıkış sıcaklığı 369,76 K
C-102 Türbini
Giriş basıncı 5 atm
W= -0,378 kW
Çıkış basıncı 1 atm
C-103 Türbini
Giriş basıncı 5 atm
W= -0,98 kW
Çıkış basıncı 1 atm
V-101 Faz ayırıcı
Hacim 0,062 m3
Dikey
konumlandırılmıştır.
Çap 0,27 m
Yükseklik 1,08 m
Ekipman boyutlandırma özeti
14. Ekipman Parametre Değer Gerekli Veriler
R-101 Faz ayırıcı
Hacim 60,71 m3
Yatay konumlandırılmıştır.Çap 2,684 m
Yükseklik 10,736 m
E-101 Isı değiştirici
Giriş sıcaklığı 47,5 ºC
Alan= 2,7 m2
Çıkış sıcaklığı 253 ºC
E- 102 Isı değiştirici
Giriş sıcaklığı 250 ºC
Alan= 1,75 m2
Çıkış sıcaklığı 49,1 ºC
E- 103 Isı değiştirici
Giriş sıcaklığı 185 ºC Alan= 1,015 m2
Çıkış sıcaklığı 25 ºC
T-101 Distilasyon Kolonu
Alan 0,015 ft2
Çap 0,043 m
Kaynatıcı debisi 270,1 kg/h
Yoğuşturucu debisi 4969,3 kg/h
Raf sayısı 15 raf
18. • Malzeme; dökme demir
• Fm = 1
• İşletme sınırları; T= 77 F, P= 7,35 psig
• F0=1 alınmıştır. MBF= 1’dir*.
• Santrifüj pompası için;
• S= C/F = 1,45*22,04 = 31,958 gpm*psig
• Bu S değeri için α = 0,17 seçilmiştir.
• 𝐶 = 𝐶0
𝑆
𝑆0
𝛼
= 0,39 × 103 31,958
10
0,17
= 475$
• 475$ < 200.000$ olduğundan MF2 alınır. Burada MF2= 3,38’ dir.
• Güncellenmiş çıplak modül maliyeti = UF (BC) (MBF+MF-1)
• Güncellenmiş çıplak modül maliyeti = 5,03* 475* (1+3,38-1) = 8.075$
• Kompresör hesabı pompa gibidir.
• *Bolat, E., Salt İ., Salt, Y., Duranoğlu D., Açıkalın K., Dilmaç Ö.F., (2012-
2013), Yıldız Teknik Üniversitesi Proses Tasarımı Ders Notları, İstanbul.
19. • Reaktörün maliyeti, basınçlı kap hesaplamaları kullanılarak
hesaplanmıştır.
• D= 2,684 m= 8,806 ft >1,2 m olduğundan yatay konumlandırılmıştır.
• L= 35,223 ft
• Basınçlı kap için cihaz maliyeti:
• 𝐶 = 𝐶0
𝐿
𝐿0
𝛼 𝐷
𝐷0
𝛽
• Yatay kap için bulunan değerler (Bolat, E., 2012):
• 𝐶0 = 600 𝐿0 = 4,0 𝐷0 = 3,0 𝛼 = 0,78 𝛽 = 0,98
• BC= 600x(35,223/4,0)0,78x(8,806/3,0)0,98= 9.405$
• Cihaz maliyeti 200.000 $’ın altında olduğundan MF2 değeri alınır (Bolat,
E., 2012)
• 𝑀𝐹2 = 3,18
• Malzeme olarak karbon çeliği seçildi. Fm=0; Fd=0; Fs=1. MBF=1 alınmıştır.
• Güncellenmiş kurulmuş cihaz maliyeti = 5,03x9405x(1+3,18-1)= 150.436 $
• Faz ayrıştırıcısı hesabı da reaktör gibidir.
23. Kaynaklar Sabit Sermaye Yüzdesi Maliyetler ($)
Kurulmuş cihaz fiyatı % 35 240.214
Proses borulama % 15 84.075
Alet-teçhizat % 12 36.032
Yapı ve konum geliştirme % 12 28.825
Servisler % 30 72.064
Dış hatlar % 10 24.021
Fiziksel Tesis Toplamı 485.231
Fiziksel Tesis Toplam Yüzdesi
Mühendislik ve yapım % 35 169.830
Öngörülmeyen olaylar % 20 97.046
Boyut faktörü % 5 24.261
Toplam Sabit Sermaye 776.368
24.
25. • Sabit sermaye maliyeti toplam sermayenin
%80’ini oluşturmaktadır.
• Toplam sermaye maliyeti;
• 𝟕𝟕𝟔. 𝟑𝟔𝟖 ×
𝟏𝟎𝟎
𝟖𝟎
= 𝟗𝟕𝟎. 𝟒𝟔𝟎 $ olarak
bulunur.
32. • COM = (CRM+CUT +CWT)* 1,23+0,304 FCI+2,73 COL
• COM = (3.198.801+441.280 +4.020)*
1,23+0,304* 776.368+2,73* 51.156
• COM = 4.857.915 $/yıl
33.
34. 𝑑 𝑘
𝐷𝐷𝐵
= 2 𝑛 𝐹𝐶𝐼𝐿 −
𝑗=0
𝑗=𝑘−1
𝑑𝑗 (Bolat, E., 2012)
Arazi hariç sabit sermaye (FCIL ) 776.368-28.825= 747.543 $
Hurda değeri (Sn) 0
Ekipman ömrü (n) 10 yıl
Amortismana tabi yıl (k) 7 yıl
Hesaplamalarda Gerekli Veriler
36. Hesaplamalarda Gerekli Veriler
Toplam Sabit sermaye yatırımı (FCIL) 747.543 $
Toplam arazi maliyeti (L) 28.825 $
Hurda değeri (Sn) 0
İşletme Sermayesi (W) 194.092 $
Yıllık satış geliri (R) 2000,53*2500 $ = 5.001.325 $/yıl
COMd 4.761.646 $
Vergilendirme oranı (t) 0.30
Proje ömrü 10 yıl
Toplam yatırım 970.460 $
Son yıl yatırım değeri 222.917 $
38. İndirgenmemiş nakit akışın geri ödeme süresi 5,57 yıl
Toplam nakit durumu (CCP) 8,75.105 $
Toplam nakit oranı (CCR) 18,44/9,7 = 1,9
Yatırım geri dönüş hızı (ROROI) % 11,7
40. İndirgenmiş geri ödeme süresi
(DPBP)
8,94 yıl
Net bugünkü değer (NPV) 1,42.105 $
Bugünkü değer oranı (PVR)
Pozitif nakit akışlar/ Negatif nakit
akışlar
11,12/9,7 = 1,15
41. SONUÇ ve TARTIŞMALAR
• Bu projede anilin, nitrobenzenin katalitik hidrojenasyonu ile üretilmektedir.
Üretim esnasında optimum verim sağlanması çalışılmıştır. Hedefler
doğrultusunda çevreci ve verimli bir üretim gerçekleştirilmiştir.
• Proseste 5,8 yılda kara geçilebilmektedir. Bu da prosesin uygulanabilir
olduğunu göstermektedir. Bu karın elde edilebilmesi için nitrobenzen ve
hidrojen maliyetinin mümkün olduğunca minimum tutulması gerekmektedir.
Ayrıca işçi masrafları da maliyeti çok artırmaktadır. Otomasyon sistemlerinin
yaygın kullanımı hem üretimin daha hatasız gerçekleşmesini sağlayacak hem
de işçi giderlerinin oldukça azalmasını sağlayacaktır. Üretim Çin’de
gerçekleştirilerek işçi masrafı en aza indirilebilir. Bu önerilerin bir veya birkaçı
uygulanarak daha karlı bir üretim yapılabilir.
• Proseste atık su ve atık hidrojen tekrar bir membran sisteminden geçirilerek
gerek servis akımı gerekse besleme akımı olarak kullanılabilir. Bunun için
uygun bir membran sistemi geliştirilebilir.
• Atık su arıtma tesisinde biyolojik arıtma sisteminden faydalanılabilir.
• Reaktör akışkan yataklı tercih edilip verim daha da artırılabilir.
• Sonuç olarak anilin üretimi uygulanabilir bir prosestir. Ülkemizdeki anilin
ihtiyacını karşılamak ve bu alanda dışarı bağımlılığı azaltmak için böyle bir
tesis kurulmalıdır.
42. • Bolat, E., Salt İ., Salt, Y., Duranoğlu D., Açıkalın K., Dilmaç Ö.F.,
(2012-2013), Yıldız Teknik Üniversitesi Proses Tasarımı Ders
Notları, İstanbul.
• http://www.chemeng.queensu.ca/courses/CHEE332/files/CEP
CI_2014.pdf
• http://turkish.alibaba.com/product-gs/nitrobenzene-
1677382249.html
• http://www.ika.rwth-aachen.de/r2h