Kinetics of Hydroprocessing

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INDIAN OIL CORPORATION LIMITED

2012

Study Of Kinetics of

Hydro-Processing ofVegetable oil[Type the document subtitle]

I O C L R & D FA R I D A B A D S E C - 1 3 A , HA R Y A N A , I N D I A


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K I N E T I C S O F H Y D R O - P R O C E S S I N G O F V E G E T A B L E - O I L

Project Completed By:-

Atul-Goel Deepak Pandey

B.Tech B.TechSummer Training Report Summer Training Report

July-2012 July-2012


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A C K N O W L E D G E M E N T

Apart from the efforts of myself, the success of any project depends largely on the

encouragement and guidelines of many others. I take this opportunity to express my gratitude

to the people who have been instrumental in the successful completion of this project. I

would like to show my greatest appreciation to Mr.B.Ravi Kumar, SRO (AE&TD). I can't

say thank you enough for his tremendous support and help. Without his encouragement and

guidance this project would not have materialized. I wish to express my sincere gratitude to

Mr. Sarvesh Kumar, SRM (AE&TD), for his initial support and guidance. I would also like to

thank Mr. Alok Sharma, CRM (AE&TD), for allowing me to work in this department and

helping me to gain profound knowledge about various key elements. I also record my sincere

thanks to the entire staff of Refining Technology-II Department and Library for their

cooperation and guidance in successful out coming of this report. At last I would like to

express my thanks to the IOCL R&D Training and Placement Department for allowing me to

undergo my training at their organization.

.


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S U M M A R Y

The project assigned was to study the kinetics of hydro-processing of vegetable oil. The

mixture of mustard oil with diesel was made to run at different operating condition of

temperature, pressure and composition. The kinetic model for the reaction was proposed.

It was observed that the hydrogenation of vegetable oil proceeded through two different

reaction that are decarboxylation and hydro deoxygenation. The two side reaction of reverse

water gas reaction and methanation reaction were also observed.

The rate equation for different model like power law and Langmuirhinshelwood mechanism

were calculated. The decarboxylation and hydro-deoxygenation reaction were observed first

order with respect to vegetable oil. Methanation reaction was found to behave first order with

respect to carbon mono-oxide.

The mechanism and the rate determining step in the reaction were also proposed at the end of

the report.


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A B B R E V I A T I O N


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F I G U R E S


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C O N T E N T S

I. Company Profile

II. Introduction

III. Extraction Of Jatropha Oil

IV. Experimental Method And Set-Up

V. Experimental Investigation Of Rate of Hydrogenation Reactions

VI. Quality of Product Obtained

VII. Mathematic Model Of Trickle-Bed

VIII. Conclusion

Reference

Appendix A

Appendix B

Appendix C


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1 . C O M P A N Y P R O F I L E

1. COMPANY OVERVIEW

Indian Oils world class R&D centre, established in 1972, has state-of-the-art facilities & hasdelivered pioneering results in lubricants technology, refining process, pipeline

transportation, bio-fuels & fuel-efficient appliances.

Over the past three decades, Indian Oil R&D Centre has developed over thousands offormulations of lubricating oils and greases responding to the needs of Indian industry and

consuming sectors like Defence, Railways, Public Utilities and Transportation. The Centre

has also developed and introduced many new lubricant products to the Indian market like

multigrade railroad oils.

Focused research in the areas of lubricants and grease formulations, fuels, refining processes,

biotechnology, additives, pipeline transportations, engine evaluation, tribological and

emission studies, and applied metallurgy has won several awards. The R&D Centres

activities in refining technology are targeted in the areas of fluid catalytic cracking (FCC),

hydroprocessing, catalysis, residue upgradation, distillation simulation and modelling, lube

processing, crude evaluation, process optimization, material failure analysis and remaining

life assessment and technical services to operating units.

In FCC, apart from process optimization and catalyst evaluation the accent is on the

development of novel technologies aimed at value addition to various refinery streams.

IndianOil's R&D Centre is fully equipped to provide technical support to commercial

hydrocracker units in the evaluation of feed stocks and catalysts, optimization of operatingparameters, evaluation of licensors' process technologies, development of novel processes

and simulation models.

Material failure analysis and remaining life assessment of refinery equipment and

installations is a highly specialized service being provided by the R&D Centre to the

refineries of IndianOil as well as other companies.

With a vision of evolving into a leader as technology provider through excellence in

management of knowledge, technology and innovation, IndianOil has launched IndianOil

Technology Ltd. The new subsidiary markets the intellectual properties developed by

IndianOil R&D Centre.

In todays dynamic business environment, innovation through a sustained process of

Research & Development (R&D) is the only cutting edge tool for organisation to thrive. With

emphasis on development & speedy commercialisation of globally competitive products,

process & technologies, the focus has now shifted from R&D to RD&D (Research,

Development & Deployment).


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Figure 1.

INDMAX, a hallmark technology developed by the Centre for maximisation of LPG and

light distillates from refinery residue, has been selected by IndianOil for setting up a 4 million

metric tonnes per annum (MMTPA) INDMAX unit as a part of the 15 MMTPA integrated

refinery-cum-petrochemicals complex at Paradip, as well as at Bongaigaon Refinery &

Petrochemicals Ltd. (BRPL). The Centre has also licensed its Diesel Hydrotreating

technology to these two refineries. These successes have catapulted IndianOil R&D into the

elite league of multinational technology licensors.

Standing in the company of six worldwide technology holders for Marine Oils, with the

second global OEM (original equipment manufacturer) approval by Wartsila, Switzerland,

IndianOil's SERVO Marine Oils are now technically qualified to cater to the lubrication

requirements of more than 90% of the world's marine engine population. In the power-

generation segment, the newly developed SERVO Marine K-Series was approved by Yanmar

Co. Ltd. of Japan for use in their engines operating on distillate fuels.

The R&D Centre continues to provide significant support to the IndianOil Group refineries in

product quality improvement, evaluation of catalysts and additives, health assessment ofcatalysts, material failure analysis, troubleshooting and in improving overall efficiency of

operations. In-house developed FCC models are not only being used in IndianOil refineries

for process optimisation but a similar model has also been sold to a multinational company.

IndianOil has formed a joint venture company, Indo Cat Pvt. Ltd., with Intercat, USA, for

manufacturing 15,000 tonnes per annum of FCC (fluidised catalytic cracking) catalysts &

additives in India, for catering to rising global demand.

As a step towards ensuring energy security for the nation, IndianOil has launched several

initiatives to exploit alternative sources of energy such as Hydrogen and Bio-fuels.

Subsequent to commissioning India's first experimental H-CNG (Hydrogen-Compressed

Natural Gas) dispensing unit at the R&D Centre campus at Faridabad, demonstration projects

are underway on use of H-CNG blends in heavy and light vehicles. IndianOil is also setting

up India's first commercial H-CNG dispensing station at one of its retail outlets in Delhi in

the year 2008 for fuelling experimental vehicles running on H-CNG blends as well as on pure

Hydrogen. IndianOil R&D is also working on production, storage, transportation, distribution

& commercialization of Hydrogen as an alternative fuel.

Bio-fuels, besides spearheading commercialisation of Ethanol-Blended Petrol in the country,

Indian Oil has been in the forefront of technology development for Bio-diesel production

from various edible and non-edible oils and its application in vehicles. Pioneering studies by

Indian Oils R&D Centre established that Bio-diesel produced from Jatropha seeds were at

par with that produced from vegetable oils. In the past few years, the R&D Centre has studied

the entire value chain of Bio-diesel, starting from Jatropha plantation to field trials on


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passenger cars, light commercial vehicles and railway locos in collaboration with several

vehicle manufacturers, railways and state transport undertakings.

Figure 2.

Indian Oil along with its subsidiary Indian Oil Technologies Ltd. has been engaged in

successful marketing of in house developed technologies, technical services & training not

only in India but abroad too.

Indian Oil has, till date, invested close to Rs. 1,000 crore in setting up world-class facilities atits R&D Centre for building world-class capabilities in analytical services, engines, test rigs

and pilot plants for all major refinery processes, catalyst characterisation & development, etc.

It plans to invest about Rs. 500 crore during the period 2007-12 to maintain its leadership in

downstream R&D activities in the hydrocarbon sector. While continuing with cutting edge

R&D in the core areas of lubricants formulations, refinery process technologies and pipeline

transportation, the thrust would now be on commercialising the developed technologies and

initiating research in new frontier areas such as petrochemicals, residue gasification, coal-to-

liquid, gas-to-liquid, alternative fuels, synthetic lubricants, nano-technology, etc. Through

these R&D initiatives, IndianOil will continuously enhance value for all its stakeholders


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2 . I N T R O D U C T I O N

This chapter discusses the basic principles involved in processing of crude oil and hydro-

processing of vegetable oil.

CRUDE OIL

Crude oil, The Black-Diamond for the world

formed due to decaying activity of the micro-

organism on the buried dead plants and animals.

The life couldnt be imagined without it.

Crude oil, complex mixture of paraffins, olefins,

aromatics, long chained carbon atom varying from

C1-C100. Around 700 refineries across the globe

are working 247 to meet the demand of its

product.

The figure 2-1 shows the regional share of world

refining, with Americas making big bite.

The extraction and refining of crude oil to finished product is a complex process. The

extracted crude oil is being purchased on the basis of API gravity and its sulphur content.

Then it is made to pass through a de-Salter removing the metals and mud from the crude.

Then the crude oil is distillated in an atmospheric distillation column, where the product cuts

are collected on the basis of their boiling point. The light ends separated are hydro-treated to

remove the sulphur content in it and to bring them below the desired limit.

FIGURE 2-0-2 SCHEMATIC REFINIG OF CRUDE OIL

The heavy end left below need to be converted to light end products for this any one of the

two techniques mentioned are used FCC: Fluid catalyzed cracking

Hydro-Cracking

C

FIGURE 2-0-1 REGIONAL SHARES OFWORLD REFINING


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The fig.2-3 shows the product obtained per barrel

of crude oil

Figure 2-0-3 products per gallon of crude oil

FIGURE 2-4 CRUDE OIL REFINING PRODUCTS


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BIO DIESEL

Diesel being a fossil fuel, rising demand of it has always raised an unanswered question of

what if, if not diesel?

The answer to this if had been bio-diesel. But because of the higher viscosity of the bio-

diesel produced and the modification in the engine it required it has lost its ground Ref[1].

The production of bio-diesel is carried out by treating vegetable oil with methanol, namely

trans-etherification reaction is order to produce the bio-diesel and glycerol.

The glycerol and ester produced are separated. Glycerol is recovered and sold to

pharmaceutical industries, ester being used as bio-diesel. The major advantage of using bio-diesel over the conventional fuel is that they produce comparatively less harmful products

like CO, CO2 and H2O in comparison to SOx and NOx.

FIGURE 0-5: FLOW SHEET FOR BIO-DIESEL

PRODUCTION


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The pre-requisite for using bio-diesel is to make major changes in the engine and these

changes could not be attained in a day. This limitation of bio-diesel has lead to strict norm by

the government to not to dope the diesel with vegetable oil by not more than 5% (w/w) Ref[2].

VEGETABLE OIL HYDRO-PROCESSING

After bio-diesel loosing it ground the hydro-processing of vegetable oil has started gaining

momentum. Many industries have already started commercializing this technology. The

vegetable oil is made to react with hydrogen at the refining hydro processing temperature and

pressure that is 360C and 55bar pressure the product obtained are C0, C02 and nC-18

paraffin.

FIGURE 0-6 HYDRO-PROCESSING REACTION OF VEGETABLE OIL REF [3 ].

The vegetable is doped with either the diesel which is about to be de-sulpharised or mixed

with heavy fraction of crude oil and send for hydro-treating.

During the hydro-processing process many reaction take place simultaneously

1.

2.

3.

The reactions of our concerned are those which directly produce n-paraffin the major

component of the diesel. The consumption of hydrogen in a particular reaction plays an

important role in deciding the price of the bio-diesel. The reaction which consumes least

amount of hydrogen is R3.

The aim of this project is to propose the kinetic model for the above reaction. And study the

effects of various operating condition on the yield of each of the reaction, the project also

discuss the quality of the diesel produced.


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Extraction of jatropha oil

Jatropha oil can be extracted from the seeds by three ways. They are:

Mechanically

Chemically

Enzymatically

Here is a chart that describes the process of oil extraction from the seeds, Jatropha oil

extraction chart

Below are some of the methods that are usually followed to extracts the oils from jatropha

seeds.

Oil Presses

Oil presses method is used to extract the oil using simple mechanical devices. It is also done

manually. The most commonly used oil presses method is the Bielenberg ram press method.

Bielenberg ram press method is a simple traditional method that uses simple devices to

extract the oils. With the help of this method 3 liters of oil can be obtained with 12 kg of

seeds.

Oil Expellers

Oil expellers method is also use for jatropha oil extraction. The most commonly used method

is the Sayari oil expeller method. This method is also called as Sundhara oil expeller. Komet


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oil expellers are also used. These sayari oil expellers was developed in Nepal and is a diesel

operated one. Now it is developed in Tanzania and Zimbabwe mainly for the production

jatropha oil. Heavy oil expellers are made of heavy cast iron and the light ones are made up

of iron sheets. Electricity driven models are also available.

Komet oil expeller is a single oil expeller machine that is used not only to extract the jatropha

oil as well for the preparation of the oil cakes.

Traditional MethodsTraditional methods are used in the rural and developing areas for extracting the oils.

Traditional methods are simple and the oil is extracted by hand using simple equipment.

Hot oil extraction

The process of extracting the oil at high pressure is called as hot oil extraction method. Since

jatropha oil can regulate the operating temperature it is extracted using the hot oil extraction

method.

Then the cold oil extraction method it is easy to extract the oil from the hot oil extraction

since the oil flows more easily due to higher viscosity. And the press cake that remains afterextracting the oil also have less oil content which might be 3 to 7 % approximately. These

two reasons make the oil press method very interesting.

During the oil extraction method many stuffing of the seeds are converted into gum like

substances and some non organic substances. These are unwanted products and so they have

to be refined.

Modern Concepts

Modern methods are followed to extract more oils from the jatropha seeds. In these modern

concepts chemical methods like aqueous enzymatic treatment is used. The maximum yield byfollowing this modern method is said to be about 74/5.

The main idea in researching the modern concepts is to extract a greater percentage of oil

from the jatropha seeds.


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4 . E X P E R I M E N T A L S E T U P A N D M E T H O D S

The chapter describe about the experimental set up on which the major part of the project was

carried out, various techniques that were used in analysis of the product are also discussed in

brief.

EXPERIMENTAL SET UP

The experiment was carried out at laboratory scale reactor. The reactor was typical Trickle

bed reactor, throughout the project reactor is assumed to be ideal fixed bed plug flow reactor.

The schematic diagram of the micro-reactor unit

Fig: 2.1 Schematic Dig of experimental set-up, HPS-high pressure separator, LPS-low

pressure separator, GC-gas chromatography, PDT-product.

The reactor was charged with activated Ni-Mo catalyst, the reactor had ID-12mm and length

of 1.5-m. The reactor was charged with 20cc of catalyst, the glass beads were placed above

and below the catalyst. Three electrically heated coils surrounded the catalyst, the Pt-based

Gas

FEED

REACTOR

PRODUCT

HPS

GAS

LPS

GC

PDT

GAS


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thermostat were arranged to measure both the skin temperature and the temperature inside the

bed.

PRODUCT ANALYSIS TECHNIQUES

Gas Chromatography:

The common technique to analyze the compounds which can vaporize without

decomposition. Gas chromatography consists of two phase, the mobile phase (or "movingphase") is a carrier gas, usually an inert gas such as helium or an un-reactive gas such

as nitrogen.

Thestationary phase is a microscopic layer of liquid or polymer on an inert solid support,

inside a piece of glass or metal tubing called a column. The gaseous compounds being

analyzed interact with the walls of the column, which is coated with different stationary

phases. This causes each compound to elute at a different time, known as the retention

time of the compound. The temperature inside the column is generally controlled by the

heaters. Based on the retention time of each component its composition in sample is

calculated.

CATALYSIS

The first introduction of the word catalysis was by Berzelius in 1836, while Ostwald

presented the first correct definition of a catalyst in 1895. He described a catalyst as a

substance that changes the rate of a chemical reaction without itself appearing in the

products. The reaction of hydro-processing is a typical heterogeneous solid catalyzed reaction

carried in trickle bed reactor.

A catalyst accelerates a chemical reaction. It does so by forming bonds with the reacting

molecules (i.e. adsorption), such that they can react to a particular product, which detaches

itself from the catalyst (i.e. desorption), and leaves the catalyst unaltered so that it is ready to

interact with the next set of molecules. In fact, we can describe the catalytic reaction as a

cyclic event in which the catalyst participates and is recovered in its original form at the end

of the cycle. A catalyst cannot alter the chemical equilibrium of a given reaction; it only

creates a favourable reaction pathway. This is done by decreasing the activation barrier

(Ea,cat) compared to the gas phase reaction (Ea, gas) and thus increasing the reaction rate.

Consequently, the reaction can take place at lower temperatures and pressures, which

decreases costs and amounts of energy for e.g. a chemical plant. Furthermore, if for a certain

reaction different paths are possible that lead to various products, the catalyst can selectively


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decrease the activation energy of one of the possible reaction paths, thereby altering the

selectivity of the reaction. In general a successful catalyst increases the yield of the desired

product while decreasing that of other products, which has advantages for both economic and

environmental reasons.

Figure 0-1: Potential energy diagram for a heterogeneous catalytic reaction (solid line), i.e.

reaction of A and B to form AB, compared with the non-catalytic gas-phase reaction (dashed

line). The presence of a catalyst lowers the activation energy (Eact) considerably.

NI-MO CAT ALYST

The catalyst used in our project to carry hydro-treating reaction is a Ni-Mo catalyst.


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4. EXPERIMENTAL INVESTIGATION OF RATE OF HYDROGENATION REACTIONS

The chapter summarizes the path followed during the hydro-processing of vegetable oil.

The proposed mechanism in literature estimates the production of CO2,CO and H2O

directly from vegetable oil. But it became difficult to account for the moles of carbon mono-

oxide.

As there is no fixed mechanism in the literature regarding the conversion of vegetable oil to

carbon mono-oxide.

And the same could be commented as there was no trending graph for production of CO2

from vegetable oil. As depicted in the graph shown below.

Fig 4.1 Moles CO,CO2 and H2O V/S Moles Of VO Following A Direct Production Path

with the number of hit and trial

0.0017254290.011694570.017129189 0.0192924650

0.0365183110.071347203

0.165795511

0

0.185

0.315

0.63

0

0.1

0.2

0.3

0.4

0.5

0.6

0.7

0 0.05 0.1 0.15 0.2

Molesofproduct

Moles of VO initially

CO2 v/s VO

CO v/s VO

H2O v/s VO


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# Proposed Mechanism

#Moles of CO2 V/S moles of VO

#Moles of H2O V/S moles of VO

0.001725429

0.052430896

0.086836597

0.187266364

0

0.02

0.04

0.06

0.08

0.1

0.12

0.14

0.16

0.18

0.2

0 0.05 0.1 0.15 0.2

MolesofCO

2produced

Moles of VO initial

CO2 V/s VO

CO2 V/s Vo

Linear (CO2 V/s Vo)


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# Moles of propane V/S Vo

#Moles of HC V/S moles of VO

0.070389577

0.0310948160.028932256

0

0.01

0.02

0.03

0.04

0.05

0.06

0.07

0.08

0 0.05 0.1 0.15 0.2

MolesofH2OviaHDO

Moles of VO initial

H2O via HDO

H2O via HDO

0.01607096

0.029492131

0.061695992

0.011731596

0.005182469 0.004822043

0

0.01

0.02

0.03

0.04

0.05

0.06

0.07

0 0.05 0.1 0.15 0.2

Molesofpropanevia

Moels of VO initially

decarboxylation

HDO


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#Moles of CO2 V/S moles of CO reverse water gas shift reaction

#Moles of CH4 V/S moles of CO methanation reaction

0.048212881

0.088476392

0.185087976

0.035194789

0.015547408 0.014466128

0

0.02

0.04

0.06

0.08

0.1

0.12

0.14

0.16

0.18

0.2

0 0.05 0.1 0.15 0.2

MolesofHC

via


HC via

decarboxylation

HC via

HDO

0.036518311

0.071347203

0.165795511

0

0.02

0.04

0.06

0.08

0.1

0.12

0.14

0.16

0.18

0 0.05 0.1 0.15 0.2

MolesofCOformed

Total moles of CO2 formed

moles of CO2 v/s CO

moles of CO2 v/s CO


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#Assuming 50%error in water estimation via HDO

#Moles of propane V/S Vo 50% error in water estimation via HDO

0.020147667

0.038969092

0.09005001

0

0.01

0.02

0.03

0.04

0.05

0.06

0.07

0.08

0.09

0.1

0 0.02 0.04 0.06 0.08 0.1 0.12 0.14 0.16 0.18

MolesofCH4formed

Total moles of CO formed

CH4 V/S CO

CH4 V/S CO

0.1823

0.309

0.632

0

0.1

0.2

0.3

0.4

0.5

0.6

0.7

0 0.02 0.04 0.06 0.08 0.1 0.12 0.14 0.16 0.18

MoleofwaterviaHDO


H2O V/S VO

H2O V/S VO


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#Moles of HC V/S moles of VO 50% error in water estimation via HDO

#Kinetic order for de-carboxylation Rxn assuming first order kinetics (k=0.803479 sec-1

)

W/Fao (Kg/moles) Cao(moles/volume) Conversion Rate constant

0.01607096

0.029492131

0.061695992

0.030383333

0.0515

0.105333333

0

0.02

0.04

0.06

0.08

0.1

0.12

0 0.05 0.1 0.15 0.2

Molesofpropaneformmed


Moles of propane v/s moles of vo with 50%

error in water estimation

decarboxylation

HDO 50% error

0.016070960.029492131

0.061695992

0.09115

0.1545

0.316

0

0.05

0.1

0.15

0.2

0.25

0.3

0.35

0 0.05 0.1 0.15 0.2

MolesofH

C


Moles of HC v/s moles of VO

decarboxylation

HDO 50%error


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10.19157 0.05 0.344818 0.829787

5.822268 0.1 0.361497 0.77054

2.837434 0.2 0.368544 0.81011

#Kinetic order for HDO Rxn assuming first order kinetics(k=1.848858 sec

-1

)


10.19157 0.05 0.65083 2.064837

5.822268 0.1 0.6385 1.747589

2.837434 0.2 0.626227 1.734147

#Kinetic order for methanation Rxn assuming first order kinetics(k=1.437302 )


10.19157 0.0391767 0.551714 1.574486

5.822268 0.0874532 0.546189 1.356989

2.837434 0.1980774 0.543139 1.38043

# Conversion data for reverse water gas shift reaction.

Moles of CO2 Conversion


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0.048213 0.757439

0.088476 0.806398

0.185088 0.895766

#Conversion v/s moles of CO2

#Summary of rate constant

Reaction Order Rate constant Rate determining step

Decarboxylation 1st

wrt VO 0.803479

HDO 1st

wrt VO 1.848858

Methanation 1st

wrt CO 1.437302

Reverse water gas shift

reaction

Kp 0.063

0.7574388870.8063982010.895765974

1.416501587

1.641951811

2.261116655

0

0.5

1

1.5

2

2.5

0 0.05 0.1 0.15 0.2

conversion

Moles of CO2

Conversion v/s moles of CO2

conversion v/s moles of CO2

ln(1-Xa) v/s moles of CO2


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#PONA

Composition Aromatics Olefins Saturates Naphthalene

100%PRDHDS 17.9 0 82.1 12.8

5%MOSLX+95%PRDHDS 15.1 0 84.9 13.5

10%MOSLX+90%PRDHDS 15.4 0 84.6 13.3

20%MOSLX+80%PRDHDS 15.9 0 84.1 13.2

#PONA

# Conclusion from PONA analysis

17.915.1 15.4 15.9

82.184.9 84.6 84.1

12.8 13.5 13.3 13.2

0

10

20

30

40

50

60

70

80

90

0 0.05 0.1 0.15 0.2

Mg/lit???


Aromatics

Saturates

Napthalenes


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The aromatics increases, with increase in the moles of vegetable oil doped

Where as there is decrease in moles of saturates and naphthalene with increase in

vegetable oil doped.


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3. MATHEMATIC MODEL FOR TRICKLE BED

This chapter summarizes the mathematical model for trickle bed as follows:

Figure a. Sketch showing the resistances involved in the G/L reaction on a catalyst

surface.

Graphically we show the resistances as in Fig. a. We can then write the following general rate

equations:


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Kinetics of Hydroprocessing

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Getting the Measure of Corrosion - Emerson Electric...hydroprocessing increasingly important. Hydroprocessing units help the refining industry meet global demand for cleaner fuels,

KHABAROVSK REFINERY HYDROPROCESSING PROJECT PLANT SAFETY

Hydroprocessing Catalysts from The Chevron and ... - · PDF fileEditor’s Note: Although this is only the second special issue of the Catalagram ® dedicated solely to hydroprocessing,

Hydroprocessing of Crude Jatropha Oil Using Hierarchical ... · Hydroprocessing of triglyceride yields straight chain hydrocarbons of 15-20 carbon range. The process involves reaction

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Production of Renewable Diesel through the Hydroprocessing

1. CONSOLIDATION OF HYDROPROCESSING VESSEL DESIGN · PDF fileCONSOLIDATION OF HYDROPROCESSING VESSEL DESIGN- ... I would like to express my sincere thanks to BITS Pilani ... Hydraulic

Hydroprocessing Catalyst Evaluation

Transition Metal Phosphides Catalysts for the Hydroprocessing … · 2017. 5. 10. · Transition Metal Phosphides Catalysts for the Hydroprocessing of Triglycerides to Green Fuel

Hydroprocessing: Hydrotreating& Hydrocracking

HYDROPROCESSING OF PALM OIL FOR SECOND …

Frameworks for Naphthalene Hydroprocessing

Utilization of waste spent hydroprocessing catalyst ... · PDF fileUtilization of waste spent hydroprocessing catalyst: development of a process for full recovery of deposited metals

Technical Paper About Refinery Hydroprocessing Technology Selection.Pdf

Hydroprocessing : Hydrocracking & Hydrotreating - Astra Energy

CELESTIA™: A REVOLUTIONARY NEW HYDROPROCESSING … · From a kinetics perspective, Celestia is most effective when used in high-pressure applications. Consequently, the initial

University of Groningen Catalytic hydroprocessing of bio

Catalytic Hydroprocessing of Microalgae-Derived Biofuels ...thefutureenergy.org/wp-content/uploads/2016/06/Catalytic... · Catalytic hydroprocessing of microalgae-derived ... Catalytic

X4500 SERIES HYDROPROCESSING - Welcome to hte · optimization to a range of hydroprocessing applications. It is optimized for high-pressure applications in trickle-bed and up-flow

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Kinetics of Hydroprocessing

Text of Kinetics of Hydroprocessing