The document summarizes Sameer Israni's research on methanol steam reforming in a palladium-silver membrane reactor. Key points:
1) Experiments and modeling were conducted to understand the effects of various species on hydrogen flux through Pd-Ag membranes during methanol steam reforming. Surface poisoning was found to be the main cause of reduced flux.
2) A packed bed membrane reactor with a single Pd-Ag fiber was tested and modeled. Higher temperatures and pressures led to increased hydrogen utilization and productivity.
3) A 3D model was developed to simulate large-scale multi-fiber membrane reactors and understand the effects of design parameters on productivity.
Manufacturing of ammonia using haber's processrita martin
Ammonia is a colourless pungent smelling gas used mostly in production of fertilizers. It is widely manufactured by Haber process from nitrogen (N2) and hydrogen (H2)
Purpose
Key to good performance
Problem Areas
Catalysts, heat shields and plant up-rates
Burner Guns
Development of High Intensity Ring Burner
Case Studies
Conclusions
Steam Reforming - The Basics of reforming, shapes and carbon:
Steam Reforming Catalysis :
Chemical reactions
Catalyst shape design
Catalyst chemistry
Carbon formation and removal
Why have a Secondary Reformer ?
Need nitrogen to make ammonia
Wish to make primary as small as possible
Wish to minimise methane slip since methane is an inert in the ammonia synthesis loop
Other methods of achieving this
Braun Purifier process
Can address all these with an air blown secondary
Manufacturing of ammonia using haber's processrita martin
Ammonia is a colourless pungent smelling gas used mostly in production of fertilizers. It is widely manufactured by Haber process from nitrogen (N2) and hydrogen (H2)
Purpose
Key to good performance
Problem Areas
Catalysts, heat shields and plant up-rates
Burner Guns
Development of High Intensity Ring Burner
Case Studies
Conclusions
Steam Reforming - The Basics of reforming, shapes and carbon:
Steam Reforming Catalysis :
Chemical reactions
Catalyst shape design
Catalyst chemistry
Carbon formation and removal
Why have a Secondary Reformer ?
Need nitrogen to make ammonia
Wish to make primary as small as possible
Wish to minimise methane slip since methane is an inert in the ammonia synthesis loop
Other methods of achieving this
Braun Purifier process
Can address all these with an air blown secondary
DEACTIVATION OF METHANOL SYNTHESIS CATALYSTS
CONTENTS
1 INTRODUCTION
2 THERMAL SINTERING
3 CATALYST POISONING
4 REACTANT INDUCED DEACTIVATION
5 SUMMARY
TABLES
1 DEACTIVATION PROCESSES ON METHANOL SYNTHESIS CATALYSTS
2 MELTING POINT, HUTTIG AND TAMMANN TEMPERATURES OF COPPER, IRON AND NICKEL
3 SINTERING RATE CONSTANTS CALCULATED INLET AND OUTLET SIDE STREAM UNIT FOR VULCAN VSG-M101
4 COMPARISON BETWEEN CALCULATED S∞ AND DISCHARGED MEASUREMENTS ON VULCAN VSG-M101
5 EFFECT OF POSSIBLE CONTAMINANTS AND POISONS ON CU/ZNO/AL2O3 CATALYSTS FOR METHANOL SYNTHESIS
6 GUARD SCREENING TEST RESULTS ON METHANOL MICRO-REACTOR. EFFECT OF DEPOSITED METALS ON METHANOL ACTIVITY
FIGURES
1 THE HΫTTIG AND TAMMANN TEMPERATURES OF THE COMPONENTS OF A SYNTHESIS CATALYST
2 A SCHEMATIC REPRESENTATION OF TWO CATALYST SINTERING MECHANISMS
3 SIDE STREAM DATA FOR VULCAN VSG-M101. INLET TEMPERATURE 242 OC, PRESSURE 1500 PSI, GAS COMPOSITION 6% CO, 9.2% CO2, 66.9% H2, 2.5% N2 AND 15.4% CH4, SPACE VELOCITY 17,778 HR-1. MEAN OUTLET TEMPERATURE 280 OC
4 TEMPERATURE DEPENDENCE OF THE RATE OF SINTERING
5 MECHANISM OF SULFUR RETENTION
6 CORRELATION OF SULFUR CAPACITY WITH TOTAL SURFACE AREA
7 EFFECT OF DEPOSITED (NI+FE) PPM ON METHANOL SYNTHESIS CATALYST ACTIVITY
8 DISCHARGED (FE + NI) DEPOSITION LEVELS ON METHANOL SYNTHESIS PLANT SAMPLES
9 EPMA ANALYSIS OF DISCHARGED LABORATORY SAMPLE OF POISONED VULCAN VSG-M101
10 THE EFFECT OF CO2 ON SYNTHESIS CATALYST DEACTIVATION
REFERENCES
Carbon Dioxide to Chemicals and Fuels Course Material.
National Centre for Catalysis Research (NCCR, IIT Madras), considered for the first on-line course the topic of Carbon dioxide to Chemicals and Fuels. NCCR has learnt many such lessons which are necessary for the researchers to understand and also have a complete comprehension of the limitations.
Need to remove poisons prior to entering downstream catalyst beds, including
Pre reformers
Primary reformers
HTS
LTS
Note : no Secondary - poisons do not stick as temperature is too high
Note that methanator is a purification step
Removes CO and CO2 which poisons synthesis catalyst
Introduction and Theoretical Aspects
Catalyst Reduction and Start-up
Normal Operation and Troubleshooting
Shutdown and Catalyst Discharge
Nickel Carbonyl Hazard
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
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.
DEACTIVATION OF METHANOL SYNTHESIS CATALYSTS
CONTENTS
1 INTRODUCTION
2 THERMAL SINTERING
3 CATALYST POISONING
4 REACTANT INDUCED DEACTIVATION
5 SUMMARY
TABLES
1 DEACTIVATION PROCESSES ON METHANOL SYNTHESIS CATALYSTS
2 MELTING POINT, HUTTIG AND TAMMANN TEMPERATURES OF COPPER, IRON AND NICKEL
3 SINTERING RATE CONSTANTS CALCULATED INLET AND OUTLET SIDE STREAM UNIT FOR VULCAN VSG-M101
4 COMPARISON BETWEEN CALCULATED S∞ AND DISCHARGED MEASUREMENTS ON VULCAN VSG-M101
5 EFFECT OF POSSIBLE CONTAMINANTS AND POISONS ON CU/ZNO/AL2O3 CATALYSTS FOR METHANOL SYNTHESIS
6 GUARD SCREENING TEST RESULTS ON METHANOL MICRO-REACTOR. EFFECT OF DEPOSITED METALS ON METHANOL ACTIVITY
FIGURES
1 THE HΫTTIG AND TAMMANN TEMPERATURES OF THE COMPONENTS OF A SYNTHESIS CATALYST
2 A SCHEMATIC REPRESENTATION OF TWO CATALYST SINTERING MECHANISMS
3 SIDE STREAM DATA FOR VULCAN VSG-M101. INLET TEMPERATURE 242 OC, PRESSURE 1500 PSI, GAS COMPOSITION 6% CO, 9.2% CO2, 66.9% H2, 2.5% N2 AND 15.4% CH4, SPACE VELOCITY 17,778 HR-1. MEAN OUTLET TEMPERATURE 280 OC
4 TEMPERATURE DEPENDENCE OF THE RATE OF SINTERING
5 MECHANISM OF SULFUR RETENTION
6 CORRELATION OF SULFUR CAPACITY WITH TOTAL SURFACE AREA
7 EFFECT OF DEPOSITED (NI+FE) PPM ON METHANOL SYNTHESIS CATALYST ACTIVITY
8 DISCHARGED (FE + NI) DEPOSITION LEVELS ON METHANOL SYNTHESIS PLANT SAMPLES
9 EPMA ANALYSIS OF DISCHARGED LABORATORY SAMPLE OF POISONED VULCAN VSG-M101
10 THE EFFECT OF CO2 ON SYNTHESIS CATALYST DEACTIVATION
REFERENCES
Carbon Dioxide to Chemicals and Fuels Course Material.
National Centre for Catalysis Research (NCCR, IIT Madras), considered for the first on-line course the topic of Carbon dioxide to Chemicals and Fuels. NCCR has learnt many such lessons which are necessary for the researchers to understand and also have a complete comprehension of the limitations.
Need to remove poisons prior to entering downstream catalyst beds, including
Pre reformers
Primary reformers
HTS
LTS
Note : no Secondary - poisons do not stick as temperature is too high
Note that methanator is a purification step
Removes CO and CO2 which poisons synthesis catalyst
Introduction and Theoretical Aspects
Catalyst Reduction and Start-up
Normal Operation and Troubleshooting
Shutdown and Catalyst Discharge
Nickel Carbonyl Hazard
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
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.
Multiphase flow modelling of calcite dissolution patterns from core scale to reservoir scale - Jeroen Snippe, Shell, at UKCCSRC specialist meeting Flow and Transport for CO2 Storage, 29-30 October 2015
Pore scale dynamics and the interpretation of flow processes - Martin Blunt, Imperial College London, at UKCCSRC specialist meeting Flow and Transport for CO2 Storage, 29-30 October 2015
Passive seismic monitoring for CO2 storage sites - Anna Stork, University of Bristol at UKCCSRC specialist meeting Geophysical modelling for CO2 storage, monitoring and appraisal, 3 November 2015
Numerical Modelling of Fracture Growth and Caprock Integrity During CO2 Injection, Adriana Paluszny - Geophysical Modelling for CO2 Storage, Leeds, 3 November 2015
Research Coordination Network on Carbon Capture, Utilization and Storage Funded by National Science Foundation in USA - A.-H. Alissa Park, Columbia University - UKCCSRC Strathclyde Biannual 8-9 September 2015
Packed Bed Reactor for Catalytic Cracking of Plasma Pyrolyzed Gasijsrd.com
Packed bed reactors play vital role in chemical industries for obtaining valuable product, like steam reforming of natural gas, ammonia synthesis, sulphuric acid production, methanol synthesis, methanol oxidation, butadiene production, styrene production. It is not only used for production but also used in separation process like adsorption, distillation and stripping section. Packed bed reactors are work horse of the chemical and petroleum industries. Its low cost, and simplicity makes it first choice to any chemical processes. In our experimental work vacuum residue is used as a feed which is pyrolyzed in the primary chamber with the help of plasma into hydrogen and hydrocarbon gases which is feed stream to the Ni catalyst containing packed bed reactor called catalytic cracker. Ni loading in the catalyst about 70 % is used to crack or decompose lower molecular hydrocarbon in to hydrogen to maximize the energy content per mass flow of gas steam and also to minimize the carbon dioxide equivalent gases at outlet of the reactor. Since cracking is surface phenomena so the catalyst play important role in designing of reactor shape. Parallel Catalytic packed bed with regeneration and deactivation can be used for commercial production of clean fuel.
Long term safety of geological co2 storage: lessons from Bravo Dome Natural CO2 reservoir - Marc Hesse, University of Texas at Austin, at UKCCSRC specialist meeting Flow and Transport for CO2 Storage, 29-30 October 2015
Great news for Emmishield!
First test from the European Commission Improof Project shows that great benefits as energy savings, protection increase, cleaner air emissions.
Conclusions:
more uniform heat transfer,
increased run lenghts,
improved product selectivities,
longer lifetime of the furnace,
big energy savings,
production increase.
Emmishield works!!!!
Study of Polymer-Coating on Various Types of Carbon Supports to Enhance Platinum Utilization Efficiency in Polymer Electrolyte Membrane Fuel Cell Electrocatalysts
The project will focus on synthesis of hexagonal structured pure phases of compositions: BaM1/3Ti2/3O3-δ and BaM1/6Ti5/6O3-δ, where M= Sc, In and Fe via different methods such as Solid state sintering and wet chemical route. The ultimate goal is to finding structure – functionality relationships within these proton and mixed conducting systems. A substantial effort will focus on search for and fabrication of new materials although the main part of the work will concentrate on detailed structural characterisation (rietveld refinement), impedance spectroscopy, infrared spectroscopy and thermogravimetric analysis.
Master Thesis Total Oxidation Over Cu Based Catalystsalbotamor
The evolution in the oxidation state of Cu and Ce in a benchmark catalyst is studied
under different conditions: temperature programmed reduction with propane and hydrogen,
and isothermal reduction with propane and hydrogen.
Analytical methods used involve operando X-ray absorption spectroscopy (XAS) in
transmission mode at the Cu K edge and Ce LIII edge, as well as online mass spectrometry
(MS) at the outlet of the reactor.
ICWES15 -Comparative Absorption of Copper from Synthetic and Real Wastewater ...
Methanol Steam Reforming in Pd-Ag Membrane Reactor for High Purity Hydrogen Generation
1. Methanol Steam Reforming in a Pd-Ag Membrane Reactor: Experiments & Modeling Sameer H. Israni (Advisor : Prof. Michael P. Harold) Acknowledgement: Support by NSF CTS-0521977
2.
3.
4.
5.
6.
7.
8.
9.
10.
11.
12.
13.
14.
15.
16. Results – Parameters Estimated Estimated binding energies correspond well with literature reported values K 0 H (kJ/mol) K H2 3.33e-10 -58.46 K H2O 1.54e-10 -49.12 K CO2 3.67e-15 -106.2 K CO 6.38e-11 -88.42 K CH3OH 1.69e-16 -123.3 K I 3.77e+38 418.9 K II 4.44e+29 328.8
17. Results – Gas mixtures No major interactions between species Temperature ( o C) Pressure (bars) CH 3 OH (mole %) CO (mole %) CO 2 (mole %) H 2 O (mole %) Experimental % drop in H 2 flux Simulated % drop in H 2 flux 225 3 20 3 10 20 89 ± 3 92.2 250 3 20 3 10 20 84 ± 3 90.2 250 5 20 3 10 20 76 ± 3 83.7 300 5 20 3 10 20 77 ± 3 84.4 225 3 5 10 25 5 85 ± 3 87.4 250 3 5 10 25 5 80 ± 3 86.4 250 5 5 10 25 5 78 ± 3 81.3 300 5 5 10 25 5 75 ± 3 79.8
18.
19.
20.
21.
22. Kinetic Parameters obtained from PBR data Membrane permeability obtained from pure gas permeation results Membrane Inhibition Factor Obtained from experiments & modeling PBMR Model
24. PBR Results Temperature profile at center of PBR 250 C, 5 bars CH 3 OH + H 2 O CuO/ZnO/Al 2 O 3 Catalyst
25. Kinetic Parameters obtained from PBR data Membrane permeability obtained from pure gas permeation results Membrane Inhibition Factor Obtained from experiments & modeling PBMR Model
30. PBMR – Simulation Results Fraction of membrane surface sites covered by species other than hydrogen 300 C, 5 bars Rate limiting step H 2 flux through membrane Surface Poisoning = 0.5) implies that 50 % of membrane surface poisoned
Pd membranes selectively allow passage of hydrogen Membrane reactors description For past 50 yrs membrane purifiers /reactors used in remote locations These systems use self supported Pd ~100 microns Comparison
- The overall objective is to study methanol steam reforming in membrane reactors - The study is divided into 3 parts - 1st part deals with understanding how the H2 flux thru the membr is affected by the other reactants and products of MSR - In the 2nd part I have carried out MSR in packed bed reactor and single fibre PBMR - I have also a model to try and simulate the experimental results - Finally using these results I have developed a model to simulate large scale multi-fiber PBMRs
- one of the 1st things I do when i synthesize these membr is to test them for their pure H2 flux -so basically i subject one side of the membr to pure H2 and measure the flow thru it -what i have plotted here is H2 flux versus at diff temps - the x-axis is ... -since the flux is linear wrt to this parameter – the membr exhibits what is known as Sieverts type of bhavior and the rate limiting step is diffusion of H atom -Now when I subjected the membr to pure He at diff press and temps there was no flow thru the membr -
- the results i showed you were for pure H2 - when there is a mixture of gases the H2 flux goes down (even when u compare the results at the same partial pressure differences) - the main reason for this decrease is due to the other species adsorbing on the Pd surface and basically decreasing the surface area available for H2 adsorpition - - when
- appartus in a furnace
- pepple et al, --> used the commercial BASF catalyst - the only thing I had to change
![Palladium based membranes ,[object Object],Non-porous Gas Mixture Pd Membrane Pure H 2](data:image/gif;base64,R0lGODlhAQABAIAAAAAAAP///yH5BAEAAAAALAAAAAABAAEAAAIBRAA7)