This document discusses technologies for producing propylene from naphtha in an economic way with low capital and operating costs. It proposes a new catalytic process called Gasolfin that uses a graded fixed bed reactor system and optimized catalytic system to selectively crack naphtha into propylene with yields between 25-45%. This is an improvement over existing steam cracking and fluid catalytic cracking processes. The key advantages of the Gasolfin process are its ability to efficiently convert paraffinic naphtha feeds into propylene using a simple and low-cost fixed bed reactor design.
This document provides information about ThyssenKrupp Uhde's expertise in aromatics production. Some key points:
- ThyssenKrupp Uhde has over 60 years of experience in aromatics production and has developed various technologies, including the Morphylane® extractive distillation process.
- The main feedstocks for aromatics production are pyrolysis gasoline, reformate, and coke oven light oil. Process configurations depend on the feedstock composition and properties.
- Pyrolysis gasoline is typically used to produce benzene and/or benzene and toluene together. Reformate and coke oven light oil can be used to produce benzene, toluene
1) Fluid catalytic cracking (FCC) is a process that uses a catalyst to crack large hydrocarbon molecules in gas oils and residual stocks into smaller molecules to produce lighter products like gasoline.
2) The FCC process involves circulating hot catalyst between a reactor and regenerator. In the reactor, the catalyst cracks the large molecules into smaller ones like gasoline. Coke deposits on the catalyst and is burned off to reheat the catalyst in the regenerator.
3) FCC units produce additional gasoline from heavier fractions of crude oil to correct the imbalance between market demand for gasoline and excess heavy products from distillation. FCC is a critical process in many refineries.
This document discusses the development of a new third generation low NOx combustion promoter called CP® P by Grace Davison. Laboratory experiments were conducted to better understand NOx formation in FCC regenerators and the mechanisms of how low NOx promoters work. Based on improved mechanistic insights, CP® P was developed and shown in commercial field trials to deliver quick CO control and lower NOx emissions compared to competitors, meeting stricter EPA emission standards. The EPA now recognizes low NOx promoters as best demonstrated technology for reducing FCC unit NOx.
This presentation discusses FPC Combustion Catalyst from Fuel Technology Pty Ltd (FTPL). FTPL has been developing and manufacturing FPC for over 30 years. FPC is an additive that dissolves in diesel fuel and acts as a catalyst during combustion to improve efficiency. Independent testing has shown FPC can provide fuel savings of 2-8%, reduced maintenance costs, and lower emissions. When used in ships and power generators, customers can expect better performance while reducing fuel and maintenance expenses.
1) Self-assembled monolayer coated gold nanoparticles catalyze the aerobic oxidation of alpha-hydroxy ketones to aryl 1,2-diketones in water.
2) This provides an efficient one-pot synthesis of quinoxaline derivatives by in situ oxidation of alpha-hydroxy ketones and subsequent condensation with aryl 1,2-diamines in water.
3) 4-Aminothiophenol self-assembled monolayer coated gold nanoparticles were found to be an effective catalyst for these reactions, providing good to excellent yields of products under mild conditions in water.
This document presents a master's thesis project on recovering lignin-derived phenolics like guaiacol from biomass through hydrothermal conversion and downstream liquid-liquid extraction. The project aims to develop a laboratory-scale liquid-liquid extraction method using methyl isobutyl ketone as the organic solvent to recover guaiacol. The document outlines the experimental setup, procedure testing extraction at different temperatures and ratios. Results show extraction yield increases with higher solvent to feed ratios and temperature. Ternary diagrams of the extraction system are presented and liquid-liquid extraction is concluded to be an effective process for recovering phenolic compounds from lignin conversion aqueous streams.
Efficient and Re-usable SAPO Catalyst for the Selective Production of Furans ...pbpbms6
Selective production of furufral from hemicellulose and HMF from various C6 sugars (fructose, glucose, maltose, cellobiose, starch) are shown using solid acid catalyst, SAPO's.
The Isomalk-2SM process is a low-temperature light naphtha isomerization technology that uses a platinum-containing mixed metal oxide catalyst to effectively isomerize hydrocarbons at 120-140°C. It offers refiners a cost-effective option for various process configurations to produce an isomerate with a RON value of 81-93. Key advantages include high conversion rates, stability against impurities, no need for chloride or caustic additions, and a catalyst service life of over 10 years.
This document provides information about ThyssenKrupp Uhde's expertise in aromatics production. Some key points:
- ThyssenKrupp Uhde has over 60 years of experience in aromatics production and has developed various technologies, including the Morphylane® extractive distillation process.
- The main feedstocks for aromatics production are pyrolysis gasoline, reformate, and coke oven light oil. Process configurations depend on the feedstock composition and properties.
- Pyrolysis gasoline is typically used to produce benzene and/or benzene and toluene together. Reformate and coke oven light oil can be used to produce benzene, toluene
1) Fluid catalytic cracking (FCC) is a process that uses a catalyst to crack large hydrocarbon molecules in gas oils and residual stocks into smaller molecules to produce lighter products like gasoline.
2) The FCC process involves circulating hot catalyst between a reactor and regenerator. In the reactor, the catalyst cracks the large molecules into smaller ones like gasoline. Coke deposits on the catalyst and is burned off to reheat the catalyst in the regenerator.
3) FCC units produce additional gasoline from heavier fractions of crude oil to correct the imbalance between market demand for gasoline and excess heavy products from distillation. FCC is a critical process in many refineries.
This document discusses the development of a new third generation low NOx combustion promoter called CP® P by Grace Davison. Laboratory experiments were conducted to better understand NOx formation in FCC regenerators and the mechanisms of how low NOx promoters work. Based on improved mechanistic insights, CP® P was developed and shown in commercial field trials to deliver quick CO control and lower NOx emissions compared to competitors, meeting stricter EPA emission standards. The EPA now recognizes low NOx promoters as best demonstrated technology for reducing FCC unit NOx.
This presentation discusses FPC Combustion Catalyst from Fuel Technology Pty Ltd (FTPL). FTPL has been developing and manufacturing FPC for over 30 years. FPC is an additive that dissolves in diesel fuel and acts as a catalyst during combustion to improve efficiency. Independent testing has shown FPC can provide fuel savings of 2-8%, reduced maintenance costs, and lower emissions. When used in ships and power generators, customers can expect better performance while reducing fuel and maintenance expenses.
1) Self-assembled monolayer coated gold nanoparticles catalyze the aerobic oxidation of alpha-hydroxy ketones to aryl 1,2-diketones in water.
2) This provides an efficient one-pot synthesis of quinoxaline derivatives by in situ oxidation of alpha-hydroxy ketones and subsequent condensation with aryl 1,2-diamines in water.
3) 4-Aminothiophenol self-assembled monolayer coated gold nanoparticles were found to be an effective catalyst for these reactions, providing good to excellent yields of products under mild conditions in water.
This document presents a master's thesis project on recovering lignin-derived phenolics like guaiacol from biomass through hydrothermal conversion and downstream liquid-liquid extraction. The project aims to develop a laboratory-scale liquid-liquid extraction method using methyl isobutyl ketone as the organic solvent to recover guaiacol. The document outlines the experimental setup, procedure testing extraction at different temperatures and ratios. Results show extraction yield increases with higher solvent to feed ratios and temperature. Ternary diagrams of the extraction system are presented and liquid-liquid extraction is concluded to be an effective process for recovering phenolic compounds from lignin conversion aqueous streams.
Efficient and Re-usable SAPO Catalyst for the Selective Production of Furans ...pbpbms6
Selective production of furufral from hemicellulose and HMF from various C6 sugars (fructose, glucose, maltose, cellobiose, starch) are shown using solid acid catalyst, SAPO's.
The Isomalk-2SM process is a low-temperature light naphtha isomerization technology that uses a platinum-containing mixed metal oxide catalyst to effectively isomerize hydrocarbons at 120-140°C. It offers refiners a cost-effective option for various process configurations to produce an isomerate with a RON value of 81-93. Key advantages include high conversion rates, stability against impurities, no need for chloride or caustic additions, and a catalyst service life of over 10 years.
This document summarizes the production of cumene, an important intermediate in phenol and acetone production. It discusses the history and various technologies used for cumene production, including solid phosphoric acid, AlCl3, and zeolite catalysts. Currently, over 80% of cumene is produced using zeolite catalyst technologies from companies like UOP, Badger Licensing, and CDTech. The document focuses on UOP's state-of-the-art Q-Max process using beta zeolite catalysts, which offers high cumene yields, regenerable catalysts, and lower production costs compared to older technologies.
With the demand for propylene outpacing the current supply levels, the supply assurance for propylene has become challenging. There are issues concerning the shortage of propylene and its impact on the industry. The paper discusses various feasible alternatives with emphasis on the production of GREEN propylene.
Propylene Production by Propane Dehydrogenation (PDH)Amir Razmi
In this article a description about different processes which are commercialized to produce propylene via Propane dehydrogenation were presented.
To receive more reports about cost estimation analysis and other reports (about the propylene and PDH ) contact the author.
Chemical Engineering Technology Profile ColumnFelipe Tavares
The document discusses propane dehydrogenation (PDH) as an economically attractive process for producing propylene from propane. PDH involves reacting propane over a platinum catalyst at around 650°C and atmospheric pressure to yield about 90% propylene. The process recovers hydrogen and purifies the propylene product. An economic analysis found that PDH yields high internal rates of return in the US and China due to low-cost propane from shale gas and imports, respectively, but is less favorable in South America and Europe.
This document discusses options for optimizing the hydrocarbon value chain by upgrading low value streams from petroleum refining. It presents two options for producing polyolefins like polypropylene and polyethylene from short residue: 1) via residue delayed coking and deep catalytic cracking or 2) via petcoke gasification. Both options can boost refining margins by generating higher value polymers without sacrificing conventional refinery outputs. The economics depend on factors like configuration, location, market access, economies of scale, and the differential in value between polymer products and feedstock.
The document discusses strategies for improving plant profitability via better utilization of existing assets with minimal capital investment. It examines product slate upgrading, debottlenecking existing technology, and technology upgrading. Case studies show how producers have used UOP technologies like Tatoray and PX-Plus processes along with adsorbent ADS-47 to upgrade production from gasoline to higher value aromatics with existing equipment. This allows producers to take advantage of market opportunities, increase capacity up to 92%, and maximize profitability.
This document is a report submitted by Siddharth Gupta for the partial fulfillment of the requirements for a Bachelor of Technology degree in chemical engineering. The report discusses the design of a reactor for the production of polyester (PET) and compares various routes employed for the esterification of PET. It provides details on the multi-stage PET production process including the reactions, operating conditions, and products of the primary esterifier, high polymerizer, wiped film reactor, and solid state polymerization reactor. The document analyzes the advantages of direct esterification of terephthalic acid over ester interchange for PET production.
Integration of Refining and Petrochem Industrybhartisharma0
This document discusses the integration of refinery and petrochemical operations at Bharat Petroleum Corporation Limited's Kochi Refinery in India. It outlines plans to expand the refinery's capacity from 190,000 to 310,000 barrels per day and construct a new petrochemical plant. A key part of the integration involves sourcing hydrogen, syngas and other utilities from a new "over the fence" gas supply operated through a build-own-operate model to minimize capital costs for both projects. The expansion aims to increase production of transportation fuels and petrochemical feedstocks like propylene to meet growing demand in India.
Biomass to olefins cracking of renewable naphthapxguru
This document discusses cracking renewable naphtha produced from biomass to produce light olefins like ethylene and propylene. The biomass is first converted to a renewable naphtha fraction using a two-step process involving hydrodeoxygenation and hydrocracking. Comprehensive characterization of the renewable naphtha showed it consists mainly of paraffins suitable for steam cracking. Steam cracking this naphtha in a pilot plant yielded high amounts of ethylene (31 wt%) and propylene (17.5 wt%) while producing small amounts of byproducts. Experimental coking studies also showed this naphtha feed has attractive coking properties. Simulations predict higher run lengths compared to fossil n
Fundamentals of petroleum processing_ lecture7-1.pdfRobinsonA9
This document discusses various fuel refining processes including catalytic isomerization and polymerization. It provides details on catalytic isomerization of light hydrocarbons to improve gasoline octane. The document describes isomerization feedstocks, catalysts used, reaction conditions, and the process technology. It also summarizes the polymerization process for producing high-octane gasoline from olefin molecules and the visbreaking process for reducing viscosity of vacuum residues through mild cracking.
This document provides an abstract for a report on ethylene production. It discusses commercial steam cracking technologies used to produce ethylene from naphtha, ethane/propane, including developing technologies like gas-to-ethylene. It examines the costs of producing ethylene from different feedstocks and regional supply and demand. The abstract outlines the major commercial technologies, developments in different regions, and provides an overview of the steam cracking process used for natural gas liquids and naphtha.
This document discusses nitrogen removal from natural gas feedstock for chemicals production. It notes that nitrogen needs to be removed, as its presence would dilute reactants and increase costs. Cryogenic distillation is identified as the most economical method for large-scale nitrogen removal, as it is energy efficient and can process large volumes. Modern cryogenic nitrogen removal plants typically use a two-stage distillation process to produce high purity methane and nitrogen. They optimize energy usage to minimize operating costs. The document recommends upstream nitrogen removal for gas with over 3% nitrogen, as downstream separation would be less efficient. It also notes the importance of fully removing hydrocarbons from vented nitrogen due to environmental regulations.
The document summarizes several methods for the commercial production of propylene glycol. The traditional methods involve cracking naphtha into propene, oxidizing propene to propylene oxide, then hydrating the oxide to propylene glycol. Alternatively, propene can react with chlorine to form chlorohydrin intermediates, which are then dechlorinated to yield the oxide. More recent methods oxidize propene with hydrogen peroxide over a catalyst to directly form the glycol.
4.4 - "Thermophilic anaerobic digestion for increased biogas production and p...Pomcert
Thermophilic anaerobic digestion operates at temperatures over 50°C, offering benefits over mesophilic digestion such as increased biogas production and pathogen inactivation. These higher temperatures allow for greater degradation of organic matter and reduction in sludge volumes. Several countries have implemented thermophilic digestion at wastewater treatment plants to increase capacity, comply with biosolids regulations, and boost biogas production for energy. Operational experiences indicate improved dewaterability and stability though odors may occur if sludge is not cooled before further treatment.
This study piloted pyrolysis and gasification of abattoir solid wastes and reviewed using the wastes in boilers. Pyrolysis and gasification of dried paunch waste and DAF sludge were technically successful, producing char and syngas. However, waste processing fees of $65-90/tonne would be required for commercial viability. Co-combusting dewatered wastes in boilers could reduce costs. Thermal processing of wastes offers significant greenhouse gas reductions compared to current disposal methods.
This document provides an overview of the polymerization process used in petroleum refining to produce high octane gasoline. Polymerization involves combining light olefin gases like ethylene and propylene into higher molecular weight hydrocarbons using a phosphoric acid catalyst. It was widely used in the 1930s-40s but replaced by alkylation after WWII before making a comeback due to leaded gasoline phase outs. Polymerization occurs at 300-450°F and 200-1200 psi to polymerize olefins into gasoline blending components with octane numbers of 83-97. Safety risks include fires and runaway reactions due to cooling water loss or corrosion from phosphoric acid exposure.
Getting the Most Out of Your Refinery Hydrogen PlantGerard B. Hawkins
Getting the Most Out of Your Refinery Hydrogen Plant
Contents
Summary
1 Introduction
2 "On-purpose" Hydrogen Production
3 Operational Aspects
4 Uprating Options on the Steam Reformer
4.1 Steam Reforming Catalysts and Tube Metallurgy
4.2 Oxygen-blown Secondary Reformer
4.3 Pre-reforming
4.4 Post-reforming
5 Downstream Units
6 Summary of Uprating Options
7 Conclusions
AIR POLLUTION CONTROL IN THE SUGAR CANE INDUSTRYApril Smith
This document summarizes air pollution control technologies for the sugar cane industry. It discusses increasing emission standards that require technologies like wet scrubbers and electrostatic precipitators. It analyzes bagasse fly ash composition and compares control devices. Technologies like multicyclones and spray towers can achieve emissions below 120 mg/Nm3, while scrubbers and precipitators can achieve lower emissions. Larger boiler capacities decrease the annual cost of precipitators.
The document discusses technologies for large-scale methanol production from natural gas, focusing on achieving high single-line capacities above 10,000 metric tons per day. It describes how autothermal reforming (ATR) at low steam-to-carbon ratios is preferred for large plants, as it maximizes capacity and minimizes investment by producing synthesis gas in a compact reactor. ATR is followed by methanol synthesis using boiling water reactors or a combination of adiabatic and boiling water reactors. Developments aim to further reduce the steam-to-carbon ratio in ATR to increase capacity and lower capital costs.
This document summarizes the production of cumene, an important intermediate in phenol and acetone production. It discusses the history and various technologies used for cumene production, including solid phosphoric acid, AlCl3, and zeolite catalysts. Currently, over 80% of cumene is produced using zeolite catalyst technologies from companies like UOP, Badger Licensing, and CDTech. The document focuses on UOP's state-of-the-art Q-Max process using beta zeolite catalysts, which offers high cumene yields, regenerable catalysts, and lower production costs compared to older technologies.
With the demand for propylene outpacing the current supply levels, the supply assurance for propylene has become challenging. There are issues concerning the shortage of propylene and its impact on the industry. The paper discusses various feasible alternatives with emphasis on the production of GREEN propylene.
Propylene Production by Propane Dehydrogenation (PDH)Amir Razmi
In this article a description about different processes which are commercialized to produce propylene via Propane dehydrogenation were presented.
To receive more reports about cost estimation analysis and other reports (about the propylene and PDH ) contact the author.
Chemical Engineering Technology Profile ColumnFelipe Tavares
The document discusses propane dehydrogenation (PDH) as an economically attractive process for producing propylene from propane. PDH involves reacting propane over a platinum catalyst at around 650°C and atmospheric pressure to yield about 90% propylene. The process recovers hydrogen and purifies the propylene product. An economic analysis found that PDH yields high internal rates of return in the US and China due to low-cost propane from shale gas and imports, respectively, but is less favorable in South America and Europe.
This document discusses options for optimizing the hydrocarbon value chain by upgrading low value streams from petroleum refining. It presents two options for producing polyolefins like polypropylene and polyethylene from short residue: 1) via residue delayed coking and deep catalytic cracking or 2) via petcoke gasification. Both options can boost refining margins by generating higher value polymers without sacrificing conventional refinery outputs. The economics depend on factors like configuration, location, market access, economies of scale, and the differential in value between polymer products and feedstock.
The document discusses strategies for improving plant profitability via better utilization of existing assets with minimal capital investment. It examines product slate upgrading, debottlenecking existing technology, and technology upgrading. Case studies show how producers have used UOP technologies like Tatoray and PX-Plus processes along with adsorbent ADS-47 to upgrade production from gasoline to higher value aromatics with existing equipment. This allows producers to take advantage of market opportunities, increase capacity up to 92%, and maximize profitability.
This document is a report submitted by Siddharth Gupta for the partial fulfillment of the requirements for a Bachelor of Technology degree in chemical engineering. The report discusses the design of a reactor for the production of polyester (PET) and compares various routes employed for the esterification of PET. It provides details on the multi-stage PET production process including the reactions, operating conditions, and products of the primary esterifier, high polymerizer, wiped film reactor, and solid state polymerization reactor. The document analyzes the advantages of direct esterification of terephthalic acid over ester interchange for PET production.
Integration of Refining and Petrochem Industrybhartisharma0
This document discusses the integration of refinery and petrochemical operations at Bharat Petroleum Corporation Limited's Kochi Refinery in India. It outlines plans to expand the refinery's capacity from 190,000 to 310,000 barrels per day and construct a new petrochemical plant. A key part of the integration involves sourcing hydrogen, syngas and other utilities from a new "over the fence" gas supply operated through a build-own-operate model to minimize capital costs for both projects. The expansion aims to increase production of transportation fuels and petrochemical feedstocks like propylene to meet growing demand in India.
Biomass to olefins cracking of renewable naphthapxguru
This document discusses cracking renewable naphtha produced from biomass to produce light olefins like ethylene and propylene. The biomass is first converted to a renewable naphtha fraction using a two-step process involving hydrodeoxygenation and hydrocracking. Comprehensive characterization of the renewable naphtha showed it consists mainly of paraffins suitable for steam cracking. Steam cracking this naphtha in a pilot plant yielded high amounts of ethylene (31 wt%) and propylene (17.5 wt%) while producing small amounts of byproducts. Experimental coking studies also showed this naphtha feed has attractive coking properties. Simulations predict higher run lengths compared to fossil n
Fundamentals of petroleum processing_ lecture7-1.pdfRobinsonA9
This document discusses various fuel refining processes including catalytic isomerization and polymerization. It provides details on catalytic isomerization of light hydrocarbons to improve gasoline octane. The document describes isomerization feedstocks, catalysts used, reaction conditions, and the process technology. It also summarizes the polymerization process for producing high-octane gasoline from olefin molecules and the visbreaking process for reducing viscosity of vacuum residues through mild cracking.
This document provides an abstract for a report on ethylene production. It discusses commercial steam cracking technologies used to produce ethylene from naphtha, ethane/propane, including developing technologies like gas-to-ethylene. It examines the costs of producing ethylene from different feedstocks and regional supply and demand. The abstract outlines the major commercial technologies, developments in different regions, and provides an overview of the steam cracking process used for natural gas liquids and naphtha.
This document discusses nitrogen removal from natural gas feedstock for chemicals production. It notes that nitrogen needs to be removed, as its presence would dilute reactants and increase costs. Cryogenic distillation is identified as the most economical method for large-scale nitrogen removal, as it is energy efficient and can process large volumes. Modern cryogenic nitrogen removal plants typically use a two-stage distillation process to produce high purity methane and nitrogen. They optimize energy usage to minimize operating costs. The document recommends upstream nitrogen removal for gas with over 3% nitrogen, as downstream separation would be less efficient. It also notes the importance of fully removing hydrocarbons from vented nitrogen due to environmental regulations.
The document summarizes several methods for the commercial production of propylene glycol. The traditional methods involve cracking naphtha into propene, oxidizing propene to propylene oxide, then hydrating the oxide to propylene glycol. Alternatively, propene can react with chlorine to form chlorohydrin intermediates, which are then dechlorinated to yield the oxide. More recent methods oxidize propene with hydrogen peroxide over a catalyst to directly form the glycol.
4.4 - "Thermophilic anaerobic digestion for increased biogas production and p...Pomcert
Thermophilic anaerobic digestion operates at temperatures over 50°C, offering benefits over mesophilic digestion such as increased biogas production and pathogen inactivation. These higher temperatures allow for greater degradation of organic matter and reduction in sludge volumes. Several countries have implemented thermophilic digestion at wastewater treatment plants to increase capacity, comply with biosolids regulations, and boost biogas production for energy. Operational experiences indicate improved dewaterability and stability though odors may occur if sludge is not cooled before further treatment.
This study piloted pyrolysis and gasification of abattoir solid wastes and reviewed using the wastes in boilers. Pyrolysis and gasification of dried paunch waste and DAF sludge were technically successful, producing char and syngas. However, waste processing fees of $65-90/tonne would be required for commercial viability. Co-combusting dewatered wastes in boilers could reduce costs. Thermal processing of wastes offers significant greenhouse gas reductions compared to current disposal methods.
This document provides an overview of the polymerization process used in petroleum refining to produce high octane gasoline. Polymerization involves combining light olefin gases like ethylene and propylene into higher molecular weight hydrocarbons using a phosphoric acid catalyst. It was widely used in the 1930s-40s but replaced by alkylation after WWII before making a comeback due to leaded gasoline phase outs. Polymerization occurs at 300-450°F and 200-1200 psi to polymerize olefins into gasoline blending components with octane numbers of 83-97. Safety risks include fires and runaway reactions due to cooling water loss or corrosion from phosphoric acid exposure.
Getting the Most Out of Your Refinery Hydrogen PlantGerard B. Hawkins
Getting the Most Out of Your Refinery Hydrogen Plant
Contents
Summary
1 Introduction
2 "On-purpose" Hydrogen Production
3 Operational Aspects
4 Uprating Options on the Steam Reformer
4.1 Steam Reforming Catalysts and Tube Metallurgy
4.2 Oxygen-blown Secondary Reformer
4.3 Pre-reforming
4.4 Post-reforming
5 Downstream Units
6 Summary of Uprating Options
7 Conclusions
AIR POLLUTION CONTROL IN THE SUGAR CANE INDUSTRYApril Smith
This document summarizes air pollution control technologies for the sugar cane industry. It discusses increasing emission standards that require technologies like wet scrubbers and electrostatic precipitators. It analyzes bagasse fly ash composition and compares control devices. Technologies like multicyclones and spray towers can achieve emissions below 120 mg/Nm3, while scrubbers and precipitators can achieve lower emissions. Larger boiler capacities decrease the annual cost of precipitators.
The document discusses technologies for large-scale methanol production from natural gas, focusing on achieving high single-line capacities above 10,000 metric tons per day. It describes how autothermal reforming (ATR) at low steam-to-carbon ratios is preferred for large plants, as it maximizes capacity and minimizes investment by producing synthesis gas in a compact reactor. ATR is followed by methanol synthesis using boiling water reactors or a combination of adiabatic and boiling water reactors. Developments aim to further reduce the steam-to-carbon ratio in ATR to increase capacity and lower capital costs.
International Conference on NLP, Artificial Intelligence, Machine Learning an...gerogepatton
International Conference on NLP, Artificial Intelligence, Machine Learning and Applications (NLAIM 2024) offers a premier global platform for exchanging insights and findings in the theory, methodology, and applications of NLP, Artificial Intelligence, Machine Learning, and their applications. The conference seeks substantial contributions across all key domains of NLP, Artificial Intelligence, Machine Learning, and their practical applications, aiming to foster both theoretical advancements and real-world implementations. With a focus on facilitating collaboration between researchers and practitioners from academia and industry, the conference serves as a nexus for sharing the latest developments in the field.
We have compiled the most important slides from each speaker's presentation. This year’s compilation, available for free, captures the key insights and contributions shared during the DfMAy 2024 conference.
6th International Conference on Machine Learning & Applications (CMLA 2024)ClaraZara1
6th International Conference on Machine Learning & Applications (CMLA 2024) will provide an excellent international forum for sharing knowledge and results in theory, methodology and applications of on Machine Learning & Applications.
A SYSTEMATIC RISK ASSESSMENT APPROACH FOR SECURING THE SMART IRRIGATION SYSTEMSIJNSA Journal
The smart irrigation system represents an innovative approach to optimize water usage in agricultural and landscaping practices. The integration of cutting-edge technologies, including sensors, actuators, and data analysis, empowers this system to provide accurate monitoring and control of irrigation processes by leveraging real-time environmental conditions. The main objective of a smart irrigation system is to optimize water efficiency, minimize expenses, and foster the adoption of sustainable water management methods. This paper conducts a systematic risk assessment by exploring the key components/assets and their functionalities in the smart irrigation system. The crucial role of sensors in gathering data on soil moisture, weather patterns, and plant well-being is emphasized in this system. These sensors enable intelligent decision-making in irrigation scheduling and water distribution, leading to enhanced water efficiency and sustainable water management practices. Actuators enable automated control of irrigation devices, ensuring precise and targeted water delivery to plants. Additionally, the paper addresses the potential threat and vulnerabilities associated with smart irrigation systems. It discusses limitations of the system, such as power constraints and computational capabilities, and calculates the potential security risks. The paper suggests possible risk treatment methods for effective secure system operation. In conclusion, the paper emphasizes the significant benefits of implementing smart irrigation systems, including improved water conservation, increased crop yield, and reduced environmental impact. Additionally, based on the security analysis conducted, the paper recommends the implementation of countermeasures and security approaches to address vulnerabilities and ensure the integrity and reliability of the system. By incorporating these measures, smart irrigation technology can revolutionize water management practices in agriculture, promoting sustainability, resource efficiency, and safeguarding against potential security threats.
Introduction- e - waste – definition - sources of e-waste– hazardous substances in e-waste - effects of e-waste on environment and human health- need for e-waste management– e-waste handling rules - waste minimization techniques for managing e-waste – recycling of e-waste - disposal treatment methods of e- waste – mechanism of extraction of precious metal from leaching solution-global Scenario of E-waste – E-waste in India- case studies.
KuberTENes Birthday Bash Guadalajara - K8sGPT first impressionsVictor Morales
K8sGPT is a tool that analyzes and diagnoses Kubernetes clusters. This presentation was used to share the requirements and dependencies to deploy K8sGPT in a local environment.
CHINA’S GEO-ECONOMIC OUTREACH IN CENTRAL ASIAN COUNTRIES AND FUTURE PROSPECTjpsjournal1
The rivalry between prominent international actors for dominance over Central Asia's hydrocarbon
reserves and the ancient silk trade route, along with China's diplomatic endeavours in the area, has been
referred to as the "New Great Game." This research centres on the power struggle, considering
geopolitical, geostrategic, and geoeconomic variables. Topics including trade, political hegemony, oil
politics, and conventional and nontraditional security are all explored and explained by the researcher.
Using Mackinder's Heartland, Spykman Rimland, and Hegemonic Stability theories, examines China's role
in Central Asia. This study adheres to the empirical epistemological method and has taken care of
objectivity. This study analyze primary and secondary research documents critically to elaborate role of
china’s geo economic outreach in central Asian countries and its future prospect. China is thriving in trade,
pipeline politics, and winning states, according to this study, thanks to important instruments like the
Shanghai Cooperation Organisation and the Belt and Road Economic Initiative. According to this study,
China is seeing significant success in commerce, pipeline politics, and gaining influence on other
governments. This success may be attributed to the effective utilisation of key tools such as the Shanghai
Cooperation Organisation and the Belt and Road Economic Initiative.
CHINA’S GEO-ECONOMIC OUTREACH IN CENTRAL ASIAN COUNTRIES AND FUTURE PROSPECT
Propylene
1. On-demand propylene from naphtha
T
oday, steam crackers are
still the leading source of
propylene. The next larg-
est source of propylene comes
from refineries. However, the
share in propylene production
by these sources is decreasing.
On-purpose technologies have
been gaining ground rapidly
over the last 10 years. Current
front runners among on-pur-
pose technologies are propyl-
ene dehydrogenation (PDH)
and coal-to-olefins (CTO). The
main difference between con-
ventional propylene production
and on-purpose technologies is
feedstock: conventional technol-
ogies use mostly oil or naphtha,
whereas on-purpose produc-
tion technologies use propane
and coal.
The US market is experienc-
ing a substantial increase in
availability of naphtha with the
advent of very light tight oils.
This will be exacerbated by the
implementation of CAFE stand-
ards. These aim to reduce US
gasoline consumption by 2.5
million b/d. In Europe, export
refineries are experiencing
similar trends, combined with
the fact that over the past five
years US gasoline production
A new catalytic process targets economic production of propylene from
naphtha at relatively low capital and operating costs
BART DE GRAAF and RAY FLETCHER Inovacat B.V.
ANGELOS LAPPAS Chemical Process and Energy Resources Institute of the Center for Research andTechnology
www.digitalrefining.com/article/1001395 PTQ Q2 2017 1
has started to meet US gaso-
line demand. A substantial sur-
plus in naphtha and gasoline is
starting to emerge. Distressed
naphthas can be a very cheap
feedstock for petrochemical
production.
Propyleneproductionprocesses
Steam cracking utilises what is
likely the most severe condi-
tions of any chemical process
in industry. When sufficient
heat is supplied, molecules will
start to ‘fall apart’ into free rad-
icals. Steam cracking involves
networks of many different
free radical reactions, includ-
ing initiation, propagation and
termination steps. Cracking
light naphtha feeds in a steam
cracker produces high yields
of ethylene due to the free
radical chemistry involved.
Selectivities towards propylene
can be improved by reducing
the severity of operation but
steam crackers are not designed
to operate at propylene-to-eth-
ylene ratios much larger than
one.
Catalytic cracking creates a
pathway for molecules that
allows for a lower energy bar-
rier for the reactions to pro-
ceed. This requires an affinity
of the reactant for the cata-
lytic site and the creation of an
intermediary product that will
crack into the desired prod-
ucts. The lower energy barrier
means that reactions already
occur at a lower temperature.
This reduces energy losses
and helps to steer selectivity
to the most desired products.
Thermal cracking products
show a higher selectivity
towards ethylene, whereas cat-
alytic cracking occurring at
gentler temperatures favours
larger olefins such as propyl-
ene and butylene.1
Selectivities
can be optimised using zeo-
litic catalysts. Optimising the
pore geometry and affinity to
the intermediates may strongly
influence the selectivity
towards desired products.
Process design can help to
increase selectivities further.
Fluid catalytic cracking (FCC)
of naphtha has been commer-
cialised under various names
and is sometimes also applied
as a secondary riser added to a
conventional FCC unit. One of
the main challenges in this pro-
cess is the heat imbalance: there
is a gap between the highly
2. 2 PTQ Q2 2017 www.digitalrefining.com/article/1001395
sive ethane has replaced naph-
tha in steam crackers which has
resulted in a large decline in
propylene production in these
units. Inexpensive propane
has also been a benefit to PDH
operations.
Worldwide there are approxi-
mately 30 PDH units. The main
challenges of PDH unit opera-
tion are catalyst breakage and
transport from unit to unit,
chromium content of catalyst,
and limited possibility for turn-
down. These units tend to run
either at full capacity or are
idled.
Gasolfin catalysis
Naphtha is an attractive feed-
stock for propylene production.
Existing processes can convert
naphtha into 15-20% propylene.
Steam crackers cracking naph-
tha at high severity yield about
15% propylene. FCC processes
can produce up to 20% propyl-
ene, with some claims of up to
22%. Significant optimisation
of the catalyst and process con-
ditions are required to achieve
these propylene yields when
cracking naphtha.
Cracking of olefinic feeds
occurs readily via carbenium
ion mechanisms. For paraffinic
and naphthenic feeds, super
acid cracking is required. This
mechanism accurately describes
the initial stages of cracking
paraffins.2
However, crack-
ing of light paraffinic feeds
at temperatures below steam
cracking has been proven to
be rather challenging in exist-
ing processes and conversion is
limited. Therefore, to enhance
conversion of paraffinic and
naphthenic feeds, the Gasolfin
catalytic system has two dis-
tinct functionalities: in the first
step a pre-conditioning of the
endothermic deep conversion
of naphtha needed to produce
high propylene yields and the
very low coke make produced
by naphtha cracking.
There are a limited number
of FCC units operating world-
wide using these technologies.
Whereas secondary riser tech-
nology benefits from the much
more stable FCC heat balance,
it pays a penalty in selectivities
due to the presence of faujasites
in the catalyst mix which boosts
hydrogen transfer reactions.
A second challenge in current
fluidised cracking processes is
the high degree of back-mixing
reducing selectivities towards
propylene.
Addition of ZSM-5 additive
to the FCC unit is a simple
and effective way to increase
propylene yields. The propyl-
ene yield achievable utilising
ZSM-5 is a function of feed-
stock, FCC design and base
catalyst composition. ZSM-5
additives may be a relatively
cheap option to incrementally
increase propylene yields in
various refineries.
At present, the conversion of
methanol to propylene is com-
mercially unattractive due to
methanol and propylene prices.
The process starting with the
conversion of coal to metha-
nol, followed by methanol to
propylene, is commercially fea-
sible. The CTO process comes
at a high environmental price:
14-20 tonnes of CO2
is emitted
for every tonne of propylene
produced. Additionally, sub-
stantial amounts of wastewater
are produced. The environmen-
tal challenges make this pro-
cess less attractive compared to
competitive processes.
PDH technology has in recent
years begun to gain increasing
importance. Many PDH units
have been built over the past
five years, especially in China.
Typically, these units have a
capacity between 300 000 t/y
and 660 000 t/y of propylene.
In the US recently, one 750 000
t/y unit came online and a sec-
ond one is expected to start up
this summer.
The recent large surpluses in
natural gas liquids have bene-
fited both steam crackers and
PDH units. Relatively inexpen-
C2= C3= C4=
15
25
20
10
5
Yield,wt%
0
Catalyst System 2
Catalyst System 3
Catalyst System 1
Figure 1 Effect of catalytic system on olefin yields at total conversion for
constant naphtha feed and operating conditions.The Gasolfin process
makes use of a catalytic system that will be optimised as a function of feed
composition
3. feed molecules occurs, followed
by cracking over a second com-
ponent of the catalytic system.
Controlling reaction condi-
tions are critical in this pro-
cess. The graded bed promotes
the initial cracking step while
suppressing side reactions.
Optimising temperature and
hydrocarbon partial pressure
are key to steering selectivities
to maximum propylene or max-
imum aromatisation mode, or
any selectivities in between.
Testing of a variety of feed-
stocks over the Gasolfin cat-
alytic system has shown
propylene selectivities between
25% and 45%. Selectivities
depend on feed type. Different
yield patterns are achieved
while processing paraffinic vs
olefinic feeds. Propylene or aro-
matic yields may be optimised
for each feed stock modification
of operating conditions and
composition of the catalytic
system.
For the composition of the
catalytic system, a few consid-
erations are important: what are
the expected variations in feed
composition and what is the
range of desired product selec-
tivities? Changing the catalytic
system will result in different
olefin yields, and there is sub-
stantial room for optimisation
(see Figure 1; note that in all cat-
alytic systems a catalytic crack-
ing component was present,
with the intrinsic cracking activ-
ity of system 1 being the largest
and system 3 being the lowest).
Gasolfin process design
Minimising back-mixing is a
key to maximum propylene
yield. Fluid bed or fast fluid-
ised riser operations always
involve a substantial amount
of back-mixing. While this may
www.digitalrefining.com/article/1001395 PTQ Q2 2017 3
be preferential for feed distri-
bution, it does limit propylene
yield by increasing the likeli-
hood of propylene consuming
reactions such as oligomerisa-
tion and aromatisation. Limited
back-mixing is a typical fea-
ture of fixed bed operations.
Optimisation of catalyst layout
and functionalities in such a
fixed bed enables the cracking
of every type of naphtha feed
including paraffins.
Even though FCC is widely
used in refining, this type of
operation is easily the most
complex type of reactor oper-
ated today. Capital investment
cost of a FCC is approximately
$500 million. The capital invest-
ment for a steam cracker with
its exotic metallurgy is one of
the most expensive reactors in
the chemicals industry. In the
chemicals industry as a whole,
the most common type of reac-
tor used is fixed bed which is
also the least expensive type of
reactor.
When designing a new pro-
cess, it is essential to mini-
mise risk. The simplest type of
reactor with the easiest mode
of operation has the highest
chance of being successful at
start-up. Therefore, the Gasolfin
process has been designed with
reactors consisting of graded
fixed beds. All other equip-
ment required in the process is
standard equipment commer-
cially proven in many chemical
plants and refineries.
Feedstock selection
The Gasolfin catalytic system
has been tested with a wide
range of naphtha feeds, includ-
ing highly paraffinic, olefinic
and naphthenic feeds (see
Figure 2). The process does not
convert aromatic components.
All feedstocks are readily con-
verted into propylene and aro-
matics, depending on catalyst
composition and process condi-
tions. For example, for a typical
FCC gasoline, feed selectivities
of the primary products range
from 28% propylene to 72%
aromatics. For paraffinic feeds,
up to 45% propylene selectivity
has been obtained in testing.
Depending on the feed and
desired flexibility, the process
will consist of two or more
reactors with varying graded
beds. (A minimum of two reac-
tors will be required for con-
tinuous operations while one
C2= C3= C4=
30
40
35
25
20
15
10
5
0
Yield,wt%
Naphtha 2
Naphtha 3
Naphtha 1
Figure 2 Effect of feedstock on olefin yields at total conversion for constant
catalyst composition and operating conditions
4. reactor is off-line for regenera-
tion.) Generally, the most prof-
itable feeds are light straight
run (LSR) and delayed coker
naphthas (DCN).
Economics and benefits
The price of the feed is an
important variable in operat-
ing costs. Gasolfin converts
gasoline and naphthas into
petrochemicals. As discussed
in previous sections, naphtha
prices are expected to come
under pressure due to the
increase in light feed produc-
tion containing high fractions
of light straight run naphthas
(especially in the US),3
and a
reduction in gasoline use by
increasing fuel efficiency and
increased demand for elec-
tric cars.4
Competitive feeds
such as propane and coal face
different challenges. Propane
prices are expected to increase
slightly due to increased
demand, and environmental
challenges for CTO will make
it unlikely to gain much trac-
tion outside of China.
Open literature evaluations
of operating expenses on the
basis of feedstock costs for
CTO, PDH and steam cracking
are made more challenging by
the differences in attributing
the benefits of the by-prod-
ucts for each process. The esti-
mated operating margin for
each technology when taking
into account the prices of the
respective feedstocks and prod-
ucts for each process, together
with their manufacturing costs,
are shown in Figure 3. Naphtha
cracking via the Gasolfin pro-
cess clearly passes the profita-
bility hurdle.
The capital costs of the
Gasolfin process are limited
due to the simple process lay-
out and operation. The process
consists essentially of a feed
preheat section, a series of fixed
beds reactors, an aromatics
extraction unit, and a product
rectification section. Due to the
simple design and operation,
this process is much less expen-
sive to build and operate than
next best available technolo-
gies. The capital costs are in
the range of $60-100 million for
a 5-15 000 b/d (feed) unit, less
than half the costs of competi-
tive propylene producing tech-
nologies. As process conditions
are rather mild, operating costs
are at least 30% less than for
steam cracking or PDH units.
Steam crackers and PDH
units have a typical minimum
size to allow for profitable
operation, and have limited
possibilities for turndown. This
makes the decision to build a
new PDH unit dependent on
the possibility to sell the excess
propylene readily. The Gasolfin
process starts at a smaller size
and can comfortably bear a
smaller economy of scale due
to savings in energy and other
operational costs. The 70%
turndown ratio is much larger
than the 25% span for stand-
ard propylene production pro-
cesses. The process lends itself
well to the operator desiring to
incrementally increase propyl-
ene yield. Probably one of the
biggest advantages is the flex-
ibility of the process: the same
process can be used in maxi-
mum propylene mode, maxi-
mum aromatics mode or any
operational point in between.
Conclusions
Naphtha will remain a cheap
feed for making petrochemicals.
This makes naphtha a prime
feedstock for the growing pro-
pylene market. On-demand
propylene technologies have
thus far shunned naphtha as
a feedstock. The Gasolfin pro-
cess fills this gap. Next to low
capital and operational costs,
the biggest advantages of the
process are flexibility in prod-
4 PTQ Q2 2017 www.digitalrefining.com/article/1001395
H1 2014 H2 2014 H1 2015 H2 2015 H1 2016 H2 2016
Half years
1200
1400
1000
800
600
400
200
0
−200
−400
Operatingmargin,USD/t
MTO/MTP
Naphtha cracker (EU)
PDH
Propylene price
Inovacat Gasolfin
Figure 3 Propylene price and operating margins of various propylene
manufacturing processes for 2014-2016. Data have been derived from Platts,
Plastics Information Europe, HIS, ICIS and OPIS
5. ucts and the operational range
of the process, especially if a
standard size PDH unit is eco-
nomically unfeasible.
References
1 Greenfelder B S,Voge H H, Good G M,
Catalytic and thermal cracking of pure
hydrocarbons, Industrial and Engineering
Chemistry, 1949 (41) 2573.
2 Haag W O, Dessau R M, Proceedings
of8thInternationalCongressonCatalysis,
Berlin, 1984, Vol. II, 305, Dechema,
Frankfurt am Main.
3 www.eia.gov/analysis/studies/
petroleum/lto/?src=home-b6
4 www.bp.com/en/global/corporate/
energy-economics/energy-outlook.html
Bart de Graaf is a Consultant in the
refining and petrochemical industry.
He previously worked in research
and technical sales with Akzo Nobel/
Albemarle Catalyst Company and
www.digitalrefining.com/article/1001395 PTQ Q2 2017 5
Angelos Lappas is Research Director
of the Chemical Process and Energy
Resources Institute of the Center
for Research and Technology Hellas
(CPERI/CERTH) and is director of CPERI
laboratory that operates pilot and bench
scale facilities that are recognised as
unique on an international scale. He has
published 89 ISI papers, has presented
at 139 conferences, has authored
three books and contributed chapters
in seven additional books, and holds a
PhD in chemical engineering from the
University of Thessaloniki, Greece.
Johnson Matthey Process Technologies.
He has authored several papers on
various processes and the catalysis and
chemistry involved, and holds a MSc
in chemical engineering from Twente
University and a PhD in heterogeneous
catalysis from the University of
Amsterdam.
Ray Fletcher is a leading process
technology developer and Co-Founder
of Inovacat BV, a Netherlands based
petrochemical technology innovation
company. More than 28 years of hands-
on refinery operations include 22 years
of direct operating, troubleshooting,
optimisation and catalysis experience
with most FCC unit designs spanning
nearly all refining companies.The author
of 45 journal articles, he holds a bachelor
of science degree in chemical engineering
from the University of Washington.
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