seminar report on hydrogen

8/11/2019 Seminar Report on Hydrogen

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Separation and purification of hydrogen from refinery streams by membrane technology

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A Seminar Report

On

SEPARATION AND PURIFICATION OF HYDROGEN

FROM REFINERY STREAMS USING MEMBRANE

SEPARATION TECHNOLOGY

Project Report !"#mitte$ in Partia% F"%&i%%ment o&

t'e Re("irement! &or t'e A)ar$ t'e De*ree o&

INDE+

Sr. no. Contents Page no.

1

Introduction 2

2

Study Of Refinery Operations 4

Refinery !ydrogen management. "

4

#ethods for hydrogen separation and purification. $

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& 'ffect of product purity on hydrogen reco(ery . 1%

" Comparison bet)een (arious methods 11

* #embrane Separation 12

+ !ydrogen Selecti(e #embranes 14

$ Polymeric membranes 1"

1% Preparation Of Polyimide #embranes 1*

11 Shortcomings of )ith polyimide #embrane 1+

SEPARATION AND PURIFICATION OF HYDROGEN FROM REFINERY

STREAMS USING MEMBRANE SEPARATION METHOD

,-Intro$"ction.

Propertie! o& '/$ro*en.

,his interesting paper deals )ith ho) effecti(e separation and purification of hydrogen can

be by achie(ed scanning (arious alternati(es for the same .o need of getting astonished

after no)ing that about +% / of present )orld energy demand comes from fossil fuels0

since using hydrogen as fuel produces )ater as a byproduct unlie fossil fuels.

!ydrogen plays a (ery crucial role in industrial processes. !ydrogen burns in air )ith

a pale blue0 almost in(isible flame. !ydrogen is the lightest of all gases0 approimately one-

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fifteenth as hea(y as air. !ydrogen ignites easily and forms0 together )ith oygen or air0 an

eplosi(e gas .

Ener*/ !ydrogen has the highest combustion energy release per unit of )eight of any

commonly occurring material. ,his property maes it the fuel of choice for upper stages of

multi-stage rocets.

!ydrogen 3!2 is a colorless0 odorless0 tasteless0 flammable and nontoic gas at

atmospheric temperatures and pressures. It is the most abundant element in the uni(erse0 but

is almost absent from the atmosphere as indi(idual molecules in the upper atmosphere can

gain high (elocities during collisions )ith hea(ier molecules0 and become e5ected from the

atmosphere. It is still 6uite abundant on 'arth0 but as part of compounds such as )ater.

P'/!ica% propertie! )hen cooled to its boiling point0 -2&2.*" oC 3-422.$o7 hydrogen

becomes a transparent0 odorless li6uid that is only one-fourteenth as hea(y as )ater. 8i6uid

hydrogen is not corrosi(e or particularly reacti(e. 9hen con(erted from li6uid to gas0

hydrogen epands approimately +4% times. Its lo) boiling point and lo) density result in

li6uid hydrogen spills dispersing rapidly.

Man"&act"re ,he most common large-scale process for manufacturing hydrogen is

steam reforming of hydrocarbons0 in particular0 natural gas 3mostly methane. Other methods

used for hydrogen production methods include generation by partial oidation of coal or

hydrocarbons0 electrolysis of )ater0 reco(ery of byproduct hydrogen from electrolytic cells

used to produce chlorine and other products0 and dissociation of ammonia. !ydrogen is

reco(ered for internal use and sale from (arious refinery and chemical streams0 typically

purge gas0 tail gas0 fuel gas or other contaminated or lo)-(alued streams. Purification

methods include pressure s)ing adsorption 3PS:0 cryogenic separation and membrane gas

separation.

#any hydrogen gas users purchase it as a li6uid0 )hich can be (apori;ed as needed0

instead of producing it on their o)n site. 8i6uefaction of gaseous hydrogen is a multi-stage

process using se(eral refrigerants and compression< epansion loops to produce etreme cold.

:s part of the process0 the hydrogen passes through =ortho< para= con(ersion catalyst beds

that con(ert most of the =ortho= hydrogen to the =para= form. ,hese t)o types of diatomic

hydrogen ha(e different energy states. In =ortho= hydrogen0 )hich is the most common form

at room temperature0 the nuclei ha(e =anti-parallel= spins. In =para= hydrogen the nuclei ha(e

parallel spins. =Ortho= hydrogen is less stable than =para= at li6uid hydrogen temperatures. It

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spontaneously changes to the =para= form0 releasing energy0 )hich (apori;es a portion of the

li6uid. >y using a catalyst such as hydrous ferric oide to con(ert most of the hydrogen to the

more stable form during the li6uefaction process0 the li6uid hydrogen product can be stored

)ithout ecessi(e (ent loss.

!ydrogen is no)n as =fuel of the future1due to its abundance and its non-polluting

combustion products. 8ess has been said about the fact that other forms of energy must be

used to produce the hydrogen )hich )ill be used as fuel. #ost hydrogen is bound up in

compounds such as )ater or methane0 and energy is re6uired to brea the hydrogen free from

these compounds0 then separate0 purify0 compress and< or li6uefy the hydrogen for storage

and transportation to usage points. 9idespread production0 distribution and use of hydrogen

)ill re6uire many inno(ations and in(estments to be made in efficient and en(ironmentally-

acceptable production systems0 transportation systems0 storage systems and usage de(ices.

.?se of hydrogen as an energy source could help to address issues related to energy including

global climate change and local air pollution. #oreo(er0 hydrogen is abundantly a(ailable in

the uni(erse and possesses the highest energy content per unit of )eight compared to any of

the no)n fuels. 0 demand for hydrogen energy and production has been gro)ing in the

recent years. #embrane separation process is an attracti(e alternati(e compared to other

technologies such as pressure s)ing adsorption and cryogenic distillation. ,his paper reports

different types of membranes used for hydrogen separation from hydrogen-rich mitures. 9e

)ill be studying about current research has been focused on nonpolymeric materials

such as metal0 molecular sie(ing carbon0 ;eolites0 and ceramics. !igh purity of hydrogen is

obtainable through dense metallic membranes and especially palladium and its alloys0 )hich

are highly selecti(e to hydrogen. ,hin membranes )ould not only reduce the cost of materials

but also increase the hydrogen flu. #etal alloys or composite metal membranes ha(e been

used for hydrogen purification. !o)e(er0 metallic membranes are sensiti(e to some gases

such as carbon monoide and hydrogen sulfide. ,herefore0 ceramic membranes0 inert to

poisonous gases0 are desirable. Inorganic microporous membranes offer many ad(antages

o(er thin-film palladium membranes. #ore importantly0 in microporous membranes0 the flu

is directly proportional to the pressure0 )hereas in palladium membranes0 it is proportional to

the s6uare root of the pressure. 9e )ill comprehend the ad(antages and disad(antages of

different membranes and )ould bring out the best.

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2-St"$/ O& Re&iner/ Operation!

: (ie) of refinery operation is depicted abo(e @,2A.#anaging current

hydrogen infrastructure and planning for future re6uirements re6uires careful selection of the

best combination of reco(ery0 epansion0 efficiency impro(ements0 purification and ne) !2

supply options. 8et us ha(e )hat actually happens in refinery pertaining to hydrogen.

,he chart abo(e sho)s ho) comprehensi(e )or is carried out in a refinery.,he crude oil as

a feed gi(es )ide (ariety of products right from 8PB to )aes that counts to 1" products.

,his carries a great attention to refinery operations.:nd hydrogen flo) carries an appreciable

and crucial importance.9e )ould go to a depth to study hydrogen flo) in refinery soon.

. Re&iner/ '/$ro*en mana*ement

Refering to the )ide importance of hydrogen in energy demand 0managing its flo) is

)orthy effort.

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7ollo)ing are the )ays of hydrogen sources in a refinery 3,,4-,he latter diagram sho)s the

units )hich re6uire hydrogen for their subse6uent processes.

FIGURE 2 . So"rce! O& H/$ro*en in Re&iner/

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FIGURE 5. Steam Re&ormin* Proce!!

Steam reforming process- ,he process aims at pure hydrogen production from natural gas as

feed .,he feed may also contain refinery off gases.,he natural gas contains sulfur )hich

deteriorates catalyst acti(ity hence is to be remo(ed .the feed is is first desulfurised

con(erting sulfur to hydrogen sulfide.esulfurisation is carried out using hydrogen and in

presence of #o


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!ydrogen management has become a priority in current refinery operations and )hen

planning to produce lo)er sculpture gasoline and diesel fuels. ue to increased hydrogen

consumption 7or hydrotreating0 additional hydrogen is needed for processing hea(y crudes.

o)adays more purities of hydrogen are re6uired to achie(e product (alue

impro(ements and increase the catalyst life0 in short cost consideration come into picture.

Some refineries solely depend on catalytic reformers as a main source of hydrogen. #ultiple

hydro treating units run for hydrogen either by reducing throughput0 managing intermediate

tan age logistics0 or running catalytic reformer optimally to satisfy do)nstream hydrogen

re6uirements.

!ydrogen purity upgrade can be achie(ed through some hydrotreaters by absorbing

hea(y hydrocarbons. Critical control of hydrogen partial pressure in hydro processing

reactors is difficult )hich affects catalyst life0 charge rate.

!ere for us steam methane reformer utili;es refinery off gas as a feed and in addition

natural gas. !ydrogen partial pressure carries attention.

!ydrogen distribution system includes follo)ing units

1. !ydrocracers

2. !ydrodesulphuri;ation

. Isomerisation

,he follo)ing flo) sheet depicts the flo) of hydrogen in a refinery 364

!ydrogen containing streams go through (arious steps lie purification0 reco(ery units 0sulfur

remo(al steps.

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$%-$+ /

*& / +& /

FIGURE 7 . Sc'ematic o& '/$ro*en net)or8

,he diagram sho)s hydrogen flo) in a refinery .It is re6uired by cat reformer0 isomerisation

and !S units also by hydrocracer. Purified hydrogen is recycled in net)or. ,he

purification step may be using membrane unit or PS: unit.

7- Met'o$! &or '/$ro*en !eparation an$ p"ri&ication

,he follo)ing are three important methods to separate hydrogen from a miture.

1. #embrane Separations

2. Pressure s)ing adsorption

. cryogenic separations

,he selection of the best of abo(e depends upon follo)ing factors

1. 'conomics

2. fleibility

. future epansion

4. eco friendliness

&. 'nergy re6uirements

1. 7or membranes separations )e )ill deal )ith after)ards

2. 7or pressure s)ing adsorption

,he impurities are adsorbed at higher partial pressures and then are desorbed

:t lo)er partial pressure.,he impurity partial pressure is reduced by s)inging the

adsorber pressure from feed pressure to the tail gas pressure.:lso a high purity purge of

!2 supply

!2 plant !ydrocracer

!2purification !2 reco(ery

Isomerisation

fuel

!SCatalytic reformer

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hydrogen is used .(ery less hydrogen is adsorbed.,he process proceeds in a cyclic

manner. : series of adsorbers can be used for the purpose.'ach adsorb undergoes same

set of process steps.

: min. pressure ratio for hydrogen separation re6uired is approimately 41 bet)een

the feed and tail gas.,he optimum feed pressure for PS: in refinery is 2%%-4%% psi.

9-E&&ect o& pro$"ct p"rit/ on '/$ro*en reco:er/

!ere )e see as )e try for higher purity the reco(ery is reduced linearly and (ice (ersa

FIGURE 9 .E&&ect o& p"rit/ on reco:er/ o& '/$ro*en

,he economics of PS: process depends upon the ability to of tail gases to use at lo)er

pressures.Proper selection of adsorbent is re6uired concerned to its life.

7ollo)ing are the steps carried out in a adsorber unit 374

1. :dsorption Process

2. Co-Current epressuri;ation Process

. Counter-Current epressuri;ation Process

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4. Purge Process

&. Counter-Current Repressuri;ation Process

7or cryogenic separations

,hese are a loe temperature separation processes )hich uses the (olatility difference in

components in a fro;en state.,he simplest cryogenic process is partial condensation.,he

feed is cooled in a multipass heat echanger.,he feed at almost %%-2%%% psig an

ambient temp. is fed to cryogenic unit.,he unit condenses ma5ority of C2

hydrocarbons.,he t)o phase miture is then again cooled to get the pure

hydrogen.,he li6uid hydrocarbon is then throttled to (apori;e and thus separated.

;- Compari!on #et)een :ario"! met'o$! %i!te$ a#o:e i! reporte$ 3;4

TABLE No- , Compari!on o& t'e Met'o$!

features :dsorption #embranes cryogenics

!2 purity $$.$ / $%-$+ / $%-$" /

!2 reco(ery *&-$2 / +&-$& / $%-$+ /

7eed pressure 1%-4% barg 2%-1"% barg &-*& barg

7eed !2

content

E4% / 2&-&% / E1% /

!2 product

pressure

7eed pressure FF feed pressure FF 7eed


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7actors PS: #embrane Cryogenic

7eed pretreatment o Hes Hes

7leibility ery high !igh :(erageReliability !igh !igh :(erage

>y-product o Possible Hes

'ase Of Operation :(erage !igh lo)

TABLE No- 2 Compari!on o& :ario"! met'o$!

efore catching a depth let us see )here are the membranes ad(antageous

and )here are they disad(antageous.

#embranes are gaining attention since their

1. 8o) energy consumption

2. #ild process conditions

. :bsense of additi(es

4. Possibility to combine )ith other technology

&. easy to scale up

#embranes )itness disad(antages as

1. 8o) lifetime

2. 7ouling tendency

. 8o) selecti(ity

Performance of membrane is decided in terms of flo) through and selecti(ity of membrane.

Selecti(ity is the difference in permeabillities of miture components or the relati(e ease of

separation.

7eed retentate

#embrane----------------------------------------------------------------------------------------------------------------

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Permeate

FIGURE ; . Mem#rane "nit Nomenc%at"re

Selecti(ity factor is defined this )ay

9here y: and y> are fractions of components : and > in the permeate and a and beare

fractions of components : and > in the feed.

!igher the selecti(ity better is the separation of the selecti(e species.

Permeability is defined as0

P J 7lu K,hicness of membrane

Partial pressure difference.

Mec'ani!m! o& tran!port

Bas Separation mechanisms,here are t)o main membrane permeation mechanisms namely through dense membranes

and the other is through porous membranes .,he dense are highly selecti(e and gi(e less flu

,he porous are less selecti(e and gi(e high flu.

T'e $en!e mem#rane mec'ani!m

,he solution


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6- H/$ro*en Se%ecti:e mem#rane!

,hese are categori;ed into

1. Polymeric membranes

2. Inorganic membranes

Includes carbon0 Silica0 Ceramic0 Meolite membranes

. #ied #atri #embranes

4. #etallic membranes

Inor*anic mem#rane! .

a Carbon membranes

,hese are of t)o types namely molecular sie(ing and surface diffusion membranes.molecular

sie(ing membranes are not commercially a(ailable.,heir selecti(ities are 4-2%.,he

performance of these membranes deteriorate )hen attaced by ammonia

0chloroflourocarbons and hydrogen sulfide.carbon membranes are operated bet)een &%%-

$%% O C.,hese are (ery brittle and difficult to pacage. :nd price of carbon still high.

b Ceramic membranes :re constructed by combining metal and nonmetal in form of an

oide0nitride or carbide.,hey are both porous and dense.Operating temp. is 2%%-"%% O C.

,he porous ceramic membrane has a t)o layer structure0membrane itself and a thicer porous

supporting layer.,he mechanism is solution diffusion.!ydrogen selecti(ity is higher.7lues

are also higher.,hese separating membranes are prepared from alumina0;irconia0silica.

Meta%%ic mem#rane! )hen high purity hydrogen is re6uired )e can opt for these

membranes at the epense of cost.palladium and palladium-alloy are etremely selecti(e to

the only hydrogen.hydrogen flo) is described by solution diffusion. If palladium

mambranes are eposed at lo)er temp. they are damaged because hydrogen gets loced

inside the palladium lattice.: solution to this problem is doping it )ith sil(er or

copper.Operating temp. range of palladium alloy membranes is %%-"%% O C.: ma5or

disad(antage of palladium membranes is their high sensiti(ity to chemicals such as

S0Cl0CO.,hese chemicals poison membrane surface and reduce hydrogen flu by 2%-1%% /

e(en.,he commercial a(ailability is still limited.

8et us loo into metallic membranes )ith an appreciable length as they are specially

employed )hen $$.$ &/ purity is desired.

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Palladium and its alloys as )ell as nicel0platinum and the metals in group III- of periodic

table are all permeable to !2.Palladium and alloys are )idely studied due to their high

permeability0their chemical compatibility )ith many hydrocarbon containing streams.

:gain if )e plot a graph of 3PfeedNPpermeate (


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abo(e the glass transition temperature.glassy membranes are highly selecti(e and gi(e a

lo)er flu0)hereas rubbery gi(e re(erse condition.

S'ortcomin*! o& po%/meric mem#rane! .

1. Operating temp. :re limited to $%- 1%% O C.

2. ,hey ha(e limited chemical resistance to !Cl .SO0CO2

. 8o) mechanical strength

4. !igh sensiti(ity to s)elling

&.:chie(able purity is lesser than $$.$ /

:d(antages of polymeric membranes

1. :re a(ailable in cheaper rates

2. 8onger life

. 'asy processibility

To remo:e t'e a#o:e mentione$ $ra)#ac8! o& po%/meric mem#rane! )e "!e

1.>lending techni6ue

2.Chemical crosslining

.fabricate mied matri membranes

A> B%en$in* tec'ni("e .

Is a special techni6ue to optimi;e hydrogen and CO2 separation performance of polymeric

membranes.,he important consideration here is polymer miscibility.: miscible polymer

blend system indicates good interaction among the constituent polymers.8i et al.0 described

blending of cellulose acetate and polyethylene glycol 3P'B.,his increases permeability of

CO2 due interaction of CO2 and P'B. CO2 permeability decreases to 4.$ from ". !o)e(er its

selecti(ity increases to 4.& from 2.&.

Recently 0hosseini et al.0studied blend system of matrimid and polyben;emida;ole3P>I

each of )hich ehibit intrinsic selecti(ity of .+.blending of the components in 1 ratio

results in selecti(ity of $.4.this gain in selecti(ity is due to hydrogen bond formationin interchin spacing of blend system. >ut this all is achie(ed at the epense of reduced

permeability.

B>c'emica%Cro!!%in8in* 9e )ould come across this later in polyimide membranes.

C> Mi?e$ Matri? Mem#rane! .

,hese are potent hybrid membranes comprised of polymer )ith embedded inorganic

particles to enhance the stability of membrane under harsh operating conditions .Bui(er et

al .0 fabricated polysulfone


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there is poor interfacial adhesion bet)een the organic and inorganic phases. :lso the

fabrication cost is high so carry less attention.

o) )e come across a ne) class of membranes i.e. Polyimide membranes

9e )ill emphasi;e

1 Preparation polyimide membrane

2 ra)bacs of polyimide membranes i.e. plastici;ation

eal )ith plastici;ation using

aChemical crosslining

b,hermal annealing

,@- Preparation po%/imi$e mem#rane 354

FIGURE 6 . preparation o& po%/imi$e mem#rane

,he synthesis of soluble "7: based polyimides ia a t)o step polycondensation reaction.

:n e6uimolar amount of dianhydrides and diamines is reacted in #P .,he reaction is

carried out in a 1%% ml flas )ith a ,eflon stir bar at room temp.for 1+ hrs. in presence of

nitrogen purge. ,he dianhydrides and diamines react to form a polyamic acid solution. ,his

solution is then chemically imidi;ed )ith e6uimolar amounts of acetic anhydride and

triethylamine.,his gi(es )ater out as a byproduct.

,,- Pro#%em )it' po%/imi$e mem#rane

P%a!ticiation

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In glassy polymeric membranes the problem is of plastici;ation .Plastici;ation is

an increase in the segmental motion of polymer chains0due to the presence of one or more

sorbates 0such as permeability of both components increases and the selecti(ity decreases.:s

a result of increase in mobility the fre6uency of gap openings and their a(erage si;e

increase. Polyimides are )idely used due to their attracti(e selecti(ity0 permeability.,heir use

for natural gas and hydrocarbon separation is still limited by plastici;ation induced

selecti(ity losses in feeds )ith significant partial pressures of CO2 and CD hydrocarbons.

,he degree of crosslin can be controlled by amt. of carboylic acid incorporated in

polymer bacbone.,he crosslining reactions occur at temp. belo) the glass transition

temp.Its important to no) about plastici;ation pressure and is the minimum in permeation

isotherm. : figure gi(en belo) eplains a permeation isotherm.)hen pressure is belo) 1&

atm 354 -,he permeability decreases due to saturation of the 8angmuir sites. :bo(e 1& atm

the permeability increases as the polymer chain mobility increases due to plastici;ation by

dissol(ed CO2.,his has been reported in 354

1% 2% % 4&%%%

4%%

4%%

Perm %%

perm %% barrers

2%%

barrers 2%%

1%%

1% 2% % 4%

CO2 pressure 3atm

FIGURE = .E&&ect o& pre!!"re on permea#i%it/

Cro!!%in8in* reaction!

D !OC!2C!2O!

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D !2O ----------------- 3monoesterification

!OC!2C!2O

2 product ---------------- 3,ransesterification

!OC!2C!2O o

Cro!! %in8in* reaction!

,he :>: containing copolyimide films )ere crosslined )ith 'thylene glycol under

solid state conditions 354-In first step the carboylic acid groups react )ith a large ecess of

ethylene glycol to form a monoesterified film.,hen polymer chains are crosslined by

pulling (acuum on the film at ele(ated temperature to set free the ethylene glucol from a

transesterfication reaction.:ctually sample films are soaed in 'B at 1*% O C for 12 hrs

under nitrogen purge.acuum line is used to reco(er 'B.,hen temperature is raised to 22% O

C.

Ionic Cro!!%in8in* .

Ionically crosslined copolyimides are deri(ed from :>: containing structures and

obtained by coordinating a multi(alent cation )ith the carboylate ion.: 2%/ ecess of

stoichiometric amount of aliminium acetylacetonate0)as added to ,!7 solution.,he films

)ere dried at 1% O C under full (acuum for 24 hrs to complete crosslining.,he

ad(antage of process is during the crosslining reaction (olatile acetylacetone is set free.

Conc%"!ion .

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:fter ha(ing gone through thourough study of hydrogen re6uirement in the refinery or other

refineries 0 )e get an idea of ho) important is hydrogen as a current source of energy or fuel.

!ydrogen is a green fuel 0gets importance )hen eco friendly results are anticipated.

!ere in the articles of the paper 0)e initially studied (arious processes for separation of

hydrogen.9e conclude all are e6ually important methods0they are useful under (ariable

conditions .One may applicable or affordable for one but may not be other method

affordable for that pre(ailing condition.#embrane separation methods gi(e high purity

hydrogen but at the epense of cost of membranes 0they are compact 0less space re6uired for

operation. Some membranes are not commercially a(ailable due to some of their

shortcomings.So )e need thorough o(er(ie) of membranes to be used herein and

economically (iable process is brought about for the same.

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Re&erence! .

1 :sim 8aee6 Lhan0 :ngels Cano Odena 0>iot;a Butierre;0 Cristina #inguillon 0

Q!ydrogen separation and purification using polysulfone acrylate ;eolite mied matri

#embranes. 0ournal of #embrane sciences 0&%0 4%-"%02%1%

2 ..!oollday0 .!u..8.Ling 0H.9ang 0Q:n o(er(ie) of hydrogen production

technologies. 0Catalysis ,oday0 1$ 0244-2"%02%%$

ohn a(id 9ind0 QImpro(ing Polyimide #embrane Resistance to Carbon ioide

Plastici;ation in atural Bas Separations0Ph. 3,ech. ,hesis0 ,he ?ni(ersity of ,eas

:t :ustin0ecember 0 2%%2

4 . StTcer0 #. 9hysall0 B.U. #iller 0 :nt)erp0 >elgium0 Q% Hears of PS:

,echnology for !ydrogen Purification0 +-1101$$+

& 8u Shao0>ee ,ing 8o)0 ,ai Shung Chung 0 Q Polymeric #embranes for thehydrogen economy Contemporary approaches and prospects for the future . 0 ournal

of #embrane Sciences 02* 01+-" 02%%$

" itin Patel0 >ill >aade 0 :ir Products0 ?S:0 8eong 9ah 7ong0 :ir Products0 :sia

:nd inay Lhurana 0,echnip N Cofleip0 ?S: .0 QCreating alue ,hrough Refinery

!ydrogen #anagement. "-+02%%

* Oy(ind !atle(i0 Sabina L. Bade0 #atthe) L. Leeling0 Paul #. ,hoen0 :.P.

a(idson . ouglas 9ay0QPalladium and palladium alloy membranes for hydrogen

separation and production !istory0 fabrication strategies0 and current performance.0

Separation and Purification ,echnology0 *0 &$-"40 2%1%

+ Ruth :. a(is 0itin #. Patel0 QRefinery !ydrogen #anagement 0 :ir Products

Chemicals Inc.0 P,U Spring0 2%%4

$ S.C.:.Lluiters.0 Status re(ie) on membrane systems for hydrogen

separationIntermediate report '? pro5ect #IBR'H '& 02%%1

1% Seyed Saeid !osseini 0#ay #ay ,oeh 0 ,ai Sung Chung 0Q!ydrogen separation and

Purification in membranes of miscible polymer blends )ith Interpenetration net)ors

Polymer $40 1&$4-1"%02%%+

11 S)en 7ritsch0 Lrupp ?hde Bmb! 0ortmund0 Bermany0QSteam Reformer >ased

!ydrogen Plant Optimisation0 2-0 2%%%

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seminar report on hydrogen

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