Download - Benzene XyleneChemicals 30052012

8/9/2019 Benzene XyleneChemicals 30052012

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Dr. Amalendu Datta – Advisor ProcessNOIDA / 30th May, 202

!"N#"N" $%&"N" '("MI'A&)


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!"N#"N" $%&"N" '("MI'A&)

• Ma*or source o+ !enene, -oluene and $ylenes is 'atalytice+ormin nit.• !enene can 1e roduced +rom -oluene and Other hiherAromatics 1y disroortionation reactions.


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!enene 'hemicals

'yclo (eane

!enene

"thyl !enene

)tyrene

Poly )tyrene

)tyrene !utadieneu11er

Acrylonitrile )tyrene!utadiene u11er

'arolactum

Nylon 4


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!enene5A!! &ummus 6lo1al7 P8D


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!enene5A!! &ummus 6lo1al7

Application

-o roduce hih9urity 1enene and hiher aromatics +rom toluene and heavier aromatics usin theDetol rocess.

Description

• 8eed and hydroen are heated and assed over the catalyst 57. !enene and unconvertedtoluene and/or ylene and heavier aromatics are condensed 527 and sta1ilied 537.

• -o meet acid :ash color seci+ications, sta1ilier 1ottoms are assed throuh a +ied91ed claytreater, then distilled 5;7 to roduce the desired seci+ication 1enene.•nconverted toluene and/or ylenes and heavier aromatics are recycled.

Economics

!asis o+ 00 MMy<"stimated investment, =/1sd 300

-yical utility re>uirements, er 11l +eed<"lectricity, ?@h .B8uel, MM!tu 0.3@ater, coolin, al ;0)team, I1 ;.;


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!enene5A!! &ummus 6lo1al7

Aromatic yield is CC.0 mol o+ +resh toluene or heavier aromatic chare. -yical yields +or

roduction o+ 1enene and ylenes are<-ye roduction !enene $ylene8eed, :tNon aromatics 3.2 2.3!enene 9999 .3-oluene ;E.3 0.E'B aromatics ;C. 0.3

'CFaromatics 99999 B.;Products, :t o+ +eed!eneneG E.E 34.C

'BaromaticsGG 99999 3E.EG.;H' minimum +reee ointGG.000 m nonaromatics maimum

Yield

-:elve lants :ith caacities ranin +rom a1out 2 million to 00 million allons er year have

1een licensed.

Commercial Plants

Technology Licensor

A!! &ummus 6lo1al


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"thyl !enene5!ader -echnoloy7 P8D


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"thyl !enene5!ader -echnoloy7

-o roduce ethyl1enene 5"!7 +rom 1enene and a olymer rade ethylene or an ethylene9rich

ethylene/ethane +eedstoc? usin the Mo1il/!ader "!Ma rocess and rorietary "on Mo1ilal?ylation and transal?ylation catalysts. -he technoloy can 1e alied in the desin o+rassroots units, uradin o+ eistin vaor9hase technoloy lants, or conversion o+aluminum chloride technoloy "! lants to eolite technoloy.

Application

Description"thylene reacts :ith 1enene in a li>uid9+illed al?ylation reactor 57 containin multile +ied91eds o+"on Mo1ils rorietary catalyst, +ormin "! and very small >uantities o+ olyethyl1enenes 5P"!7.

In the transal?ylation reactor 527, P"! is converted to "! 1y reaction :ith 1enene over "onMo1ilstransal?ylation catalyst. P"! and 1enene recovered +rom the crude "! enter the trans al?ylationreactor. "++luents +rom the al?ylation and transal?ylation reactors are +ed to the 1enene column 537,:here unreacted 1enene is recovered +rom crude "!. -he +resh 1enene +eedstoc? and a +raction o+the 1enene distillate are +ed to the lihts column 5;7 to re*ect liht imurities. -he lihts column1ottoms are returned to the 1enene column. -he 1ottoms +rom the 1enene column are +ed to the"! column 57 to recover "! roduct. -he 1ottoms +rom the "! column is +ed to the P"! column 547:here recycla1le al?yl1enenes are recovered as a distillate and dihenyl comounds are re*ected in

a 1ottoms stream that can 1e used as +uel.

a: materials and steam, tons er ton o+ "! roduct"thylene 0.244!enene 0.E3C)team, hih9ressure used .0)team, medium9and lo:9ressured enerated .;2

Utilities can be optimized for specific-site conditions.

Economics


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'ycle lenths in ecess o+ +our and three years are eected +or the al?ylation and transal?ylationcatalysts resectively. Process e>uiment is +a1ricated entirely +rom car1on steel. 'aital investmentis reduced as a conse>uence o+ the hih activity and etraordinary selectivity o+ the al?ylationcatalyst and the a1ility o+ 1oth the al?ylation and transal?ylation catalysts to oerate :ith very lo:>uantities o+ ecess 1enene.

Catalyst

-he ethyl 1enene roduct contains less than 00m o+ 'B lus 'C imurities. Product urities

o+ CC.Cto CC.CCare eected.

Prodct !ality

Technology Licensor

-he !ader -echnoloy 'enter o+ @ashinton 6rou International, Inc.

Commercial Plants

)ince the commercialiation o+ the Mo1ill !ader "! technoloy in CB0, ;2 licenses have 1eenranted. -otal licensed caacity +or the "!Ma technoloy eceeds .2 million mty.

"thyl !enene5!ader -echnoloy7


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)tyrene 5A!! &ummus 6lo1al J OP7 P8D


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)tyrene 5A!! &ummus 6lo1al J OP7

Application-o roduce olymer9rade styrene monomer 5)M71y dehydroenatin ethyl1enene 5"!7

to +orm styrene usin the &ummus/ OP K'lassicK styrene rocess +or ne: lants and the&ummus/ OP K)MA-K rocess +or revams.

Description

In the 'lassic rocess, "! is catalytically dehydroenated to styrene in the resence o+ steam. -hereaction is carried out at hih temerature under vacuum.

• -he "! 5+resh and recycle7 and rimary steam are com1ined :ith suerheated steam, and themiture is dehydroenated in a multistae reactor system 57. An interheater reheats the rocess as1et:een staes. eactor e++luents are cooled to recover :aste heat and condense the hydrocar1onsand steam.• ncondensed o++as is comressed and is used as +uel. 'ondensed hydrocar1ons 527 are sent tothe distillation section. Process condensate 527 is stried to remove dissolved aromatics. A+ractionation train 53,;7 searates hih9urity styrene, unconverted "!, :hich is recycled, and therelatively minor reaction 1yroduct tar. -oluene is roduced 5,47 as a minor 1yroduct, and 1enene

547 is recycled to the al?ylator.-yical )M9roduct urity ranes +rom CC.B to CC.C. -he rocess rovides hih9roduct yield dueto a uni>ue com1ination o+ catalyst and oeratin conditions used in the reactors.-he )MA- rocess is the same ecet 1et:een the dehydroenation staesL oyen is introducedto artially oidie the hydroen roduced over a rorietary catalyst, to reheat the rocess as andto remove the e>uili1rium constraint +or the dehydroenation reaction. -he rocess achieves u to orreater than B0 "! conversion er ass.


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)tyrene 5A!! &ummus 6lo1al J OP7

Investment, .). "#tpy

5.). 6ul+'oast 1asis, 200,000 ty7 22a: materials consumtion, er metric ton o+ )M< 'lassic"thyl1enene .0;tilities, .). "#ton )M 3

Economics

Presently, 34 oeratin lants incororate the &ummus/OP styrene 'lassic technoloy. -hreeoeratin +acilities are usin the )MA- rocess technoloy. Many +uture units usin the )MA-rocess are eected to 1e retro+its o+ conventional units, since the technoloy is :ell suited +orrevams.

Commercial Plants

Technology Licensor

A!! &ummus 6lo1al J OP


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Footer can be customized13

I#9 !enene $ylene 'hemicals9-echni 'hennai "I-s

. @hat is the ma*or source 5re+inery rocess7 o+ !enene and9$ylene

. @hat do you et 1y al?ylatin !enene :ith "thylene

2. )tyrene is roduced 1y .o+ "thyl !enene.

3. @hat is the )tyrene Monomer urity o1taina1le 1y &ummus/OP 'lassic )tyrene rocess

. @hat is the conversion er ass o+ "thyl !enene to )tyrene


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Polystyrene 5OP7 P8D


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-he N)''IOP olystyrene rocess roduces a :ide rane o+ olystyrene 5P)7 rades.6eneral9urose or KcrystalK olystyrene 56PP)7 is a clear, amorhous olymer used:idely in ac?ain o+ +ood, comact dis?s, etc. @hen more imact resistance isre>uired +or items li?e comuter and television housins, oly1utadiene ru11er is

incororated into the olystyrene matri to roduce hih9imact or Kru11er9modi+iedKolystyrene 5(IP)7. -he technoloy is also caa1le o+ roducin a +amily o+ remiumhih9strenth, hih9loss (IP) resins that can 1e su1stituted +or more eensive

Acrylonitrile9!utadiene9)tyrene resins 5A!)7 in many alications.

Polystyrene 5OP7

Application

Description

-he rocess involves continuous, 1ul?9hase olymeriation o+ styrene usin acom1ination o+ thermal and chemical initiation. A tyical unit desin consists o+ searatereaction trains +or 6PP) and (IP) rades, :hich have 1een otimied +or each resintye. -he 6PP) reactor train is caa1le o+ roducin numerous rades o+ 6PP) that

rane +rom lo: molecular :eiht, hih9+lo: rades to hih9molecular9:eiht, heat9resistant rades. -he (IP) reactor train includes a rorietary reactor desin that ivesunrecedented control over the distri1ution o+ ru11er throuh the olystyrene matri.-he e++icient distri1ution o+ ru11er means that this rocess can roduce a iven olymerstrenth :ith less ru11er than is re>uired 1y other technoloies. -his rocess can alsorecisely control the sie o+ ru11er articles, do:n to less than one micron in diameter.


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)mall ru11er articles result in hih9strenth (IP) resins :ith smooth, lossy +inishes that rival the

mechanical roerties and sur+ace +inish o+ A!). -he 6PP) and (IP) reactor sections each containseveral olymeriation reactors in series, t:o9stae devolatiliation and a alletiin line. -hedevolatiliation e>uiment is desined to deliver olystyrene roduct :ith a concentration o+ residualtotal volatile material 5-M7 o+ less than 00 :t9m. 'ommon e>uiment includes sections +or +eedrearation, )M recovery, :ater removal and 1ul?9resin handlin.

Polystyrene 5OP7

Description $Contd.%

Economics!asis< 0,000 ty 6PP) F 0,000 ty (IP), .). 6ul+ 'oast7

Investment, .). "&tpy 300a: material consumtion, er metric ton o+ 6PP))tyrene 0.CCC9.00Ea: material consumtion, er metric ton o+ (IP))tyrene 0.C2490.C;Bu11er 0.0290.04;tilities, .). =/ton P) 3.4

Nion )teel 'hemical 'o.5N)''7,currently oerates t:ounits in Qimitsu, Raan, :ith a

total olystyrene caacity o+ 200,000 ty. N)'' roduces more than 0 di++erent radeso+ 6PP) and (IP), includin a +amily o+ remium, hih9er+ormance (IP) resins thathave success+ully dislaced A!) in certain alications.

Commercial Plants

Technology Licensor OP


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'ycloheane 5I8P,I8PNA7 P8D

' l h 5I8P I8PNA7


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'ycloheane 5I8P,I8PNA7

Application

Produce hih9urity cycloheane 1y li>uid9hase catalytic hydroenationo+ 1enene.

Description-he main reactor 57 converts essentially all the +eed isothermally in the li>uid hase ata thermodynamically +avora1le lo: temerature usin a continuously in*ected solu1lecatalyst. -he catalysts hih activity allo:s use o+ relatively lo: hydroen artial ressure, :hichresults in +e:er side reactions, e.., isomeriation or hydrocrac?in. -he heat o+ reactionvaories cycloheane roduct and, usin umaround circulation throuh an echaner, alsoenerates steam 527. @ith the heat o+ reaction 1ein immediately removed 1y vaoriation,accurate temerature control is assured.

A vaor9hase +ied91ed +inishin reactor 537 comletes the catalytic hydroenation o+any residual 1enene. -his ste reduces residual 1enene in the cycloheane roductto very lo: levels.Deendin on the urity o+ the hydroen ma?e9u as, the sta1iliation sectionincludes either an &P searator 5;7 or a small sta1ilier to remove the liht ends.A rime advantae o+ the li>uid9hase rocess is its su1stantially lo:er cost comared to vaorhase rocesses< investment is articularly lo: 1ecause a sinle, ineensive main reactorcham1er is used comared to multile91ed or tu1ular reactors used in vaor hase rocesses.uench as and unreacted 1enene recycles are not necessary and 1etter heat recovery enerates1oth the cycloheane vaor +or the +inishin ste and a reater amount o+ steam. -heseadvantaes result in lo:er investment and oeratin costs. Oerational +lei1ility and relia1ilityare ecellentL chanes in +eedstoc? >uality and +lo:s are easily handled. )hould the catalyst 1edeactivated 1y +eed >uality usets, +resh catalyst can 1e in*ected :ithout shuttin do:n.


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'ycloheane 5I8P,I8PNA7

.0E ? o+ cycloheane is roduced +rom ? o+ 1enene.

Yield

Economics

!asis< 200,0009ta cycloheane comle, I)!& 2000 6ul+ 'oast location :ith P)A hydroen is E.4million =.). 'atalyst cost is =.). 2/metric ton o+ roduct.

Technology Licensor

I8P,I8PNA


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'arolactum 5)NIA !PD )..A7 P8D


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'arolactum 5)NIA !PD )..A7

A rocess to manu+acture carolactam +rom nitration9 rade toluene. 8i1er9

rade +la?ed or molten carolactam and :hite ammonium sul+ate crystals are roduced.

Application

Description

-oluene and air are +ed to the reactor 57 in :hich the oidation to 1enoic acid is carriedout at 40H' and 0 atm. -he reaction roduct is a 30 solution o+ 1enoic acid in toluene lus asmall >uantity o+ 1yroducts. 8ractionation 527 searates unconverted toluene +or recycle, ure1enoic and a 1ottom +raction o+ heavy 1yroducts.

!enoic acid is hydroenated under ressure in resence o+ alladium catalyst in a series o+continuous stirred tan? reactors 537 at E0H' and 4 atm. 'onversion is comlete in a sinle ass.'ycloheane9car1oylic acid is 1lended :ith oleum and +ed to a multistae reactor 5;7 :here it isconverted to carolactam 1y reaction :ith nitrosylsul+uric acid.-his acid is roduced in a conventional ammonia oidation lant, :here the nitroen oides area1sor1ed in oleum. eactor e++luent is diluted :ith :ater 57, and unconverted cycloheanecar1oylic acid is recycled to the rocess, :hile the lactam solution +lo:s to the crystalliation lant547 :here it is neutralied :ith ammonia. Ammonium sul+ate crystallies at 1ottom and the to

oranic layer o+ carolactam is recovered and uri+ied throuh a t:o solvent 5toluene and :ater7etraction 5E7 and a continuous +ractionation 5B7.

-oluene!enoicAcid

'yloheane'ar1oylicAcid

Nitrosylsul+uric

Acid

'arolactum

5'(27'5O7N(

N%&ON 4

Polymeriation240S',;hrs,N2 Atmoshere

40S'

0atm

170', 4atm, Pd catalyst[H2]Nitrogen Oxide

Oleum

! Ferban !erman#


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$ased on a %0"000&t'# batter# limits 'lant" (. )uro'e"1%%0*n+estment" ,-t'# 200/#'ical ra material and utilit# reuirements"'er g o ca'rolactam*/oluene" g 1.0

4mmonia" g 1.156ulur" g 0.%0

H#drogen" Nm3 0.0 4mmonium sulate" g" credit8 3.98)lectricit#" (: 0.06team" g 11.0Fuel gas" Nm3 0.29(ater" cooling" m3 0.;0(ater" c:illed" m3 0.13

'arolactum 5)NIA !PD )..A7

Economics

20,OOO9ty)NIA !PD +actory in -orviscosa, ItalyL B0,0009ty ANI' +actory in Man+redonia, ItalyLeansion to BB,0009ty "&"'-O'(IMPOM +actory in 'hirchi?, ))L 0,0009ty lant,)hi*iahuan, 'hina.

Commercial Plants

Technology Licensor )NIA !PD )..A., eclusive contractor< )NAI'O "nineerin )..A.


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Footer can be customized23

I#92 !enene $ylene 'hemicals9-echni NOIDA "I-s

. @hat do you understand 1y 6PP) and (IP)

2. 'ycloheane is roduced 1y o+ !enene.

3. @hat is the temerature and ressure +or oidation o+ -olueneto !enoic Acid

;. @hat is the temerature and ressure +or roduction o+'ycloheane 'ar1oylic acid

. @hat is Nylon4

Nylon 4 4 5Polyheamethylene adiamide7


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Nylon 4,4 5Polyheamethylene adiamide7Made +rom (eamethylene Diamine and Adiic acid as sho:n inthe diaram 1elo:.

$enzene48

(O9'95'(27;9'9O(

(2N95'(2749 N(2

@ater

• -he reactants are heated and :ater is removed tillolymeriation is comlete.

• -he temerature is increased to 2E09300S' a+ter :hich theressure is raised to 20si.

•-he ressure is +urther reduced to atmosheric ressure termit +urther removal o+ :ater

•A+ter 3 hours Nylon 44 is etruded under nitroen ressurethrouh a 1ottom valve o+ the autoclave.

N2

N%&ON 44

)innin o+ Nylon 4,4


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/:e c:i's o n#lon 'ol#mer are ed t:roug: a :o''er 4" into a s'inning +essel $" on anelectricall# :eated grid 'erorated 'late8


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$ylene 'hemicals

P9$ylene -erehthalic Acid Polyester

Dimethyl -erehthalate

O9$ylene Phthalic Anhydride

-oluene !enoic Acid

P $ l 5" M 1il 'h i l7 P8D


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P9$ylene 5"on Mo1il 'hemical7 P8D

P $ylene 5"on Mo1il 'hemical7


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P9$ylene 5"on Mo1il 'hemical7

-he selectively convert toluene to hih9urity 5C0F7 araylene9rich 5P$7 ylenes and 1eneneusin "on Mo1ils technoloies licensed under the name PMa.

Application

Description

• Dry toluene +eed and hydroen9rich recycle as are umed throuh +eed/e++luent

echaners and chare heater and into the PMa reactor 57. )elective toluenedisroortionation 5)-DP7 occurs in the vaor hase to roduce the araylene9rich

ylene and 1enene co9roduct.• !yroduct yields are small. eactor e++luent is cooled 1y heat echane and li>uid roducts aresearated +rom the recycle as. (ydroen9rich as +rom the searator 527 is recycled 1ac? to thereactor toether :ith ma?eu hydroen. &i>uid roduct is stried o+ remainin liht as in thesta1ilier 537 and sent to roduct +ractionation. nconverted toluene is recycled to etinction.-:o technoloy versions are licensed under the name PMa. One version involves catalyst 5"M922007, :hich is co?e selectivated in9situ and the other version uses catalyst 5M-P$7 in :hich theselectivation is rovided 1y retreatment durin catalyst manu+acture.!oth technoloies rovide sini+icantly hiher selectivity and loner oeratin cycles than other)-DP technoloies. Oeratin costs associated :ith do:nstream recovery are also reduced 1y thehih araylene urity +rom PMa.Oeratin conditions< PMa oerates at lo:er start9o+9cycle temeratures and lo:er hydroen tohydrocar1on recycle ratios than other )-DP technoloies, resultin in loner cycles and lo:erutilities. !y eliminatin the in9situ selectivation ste, the M-P$ version o+ this technoloy results insimli+ied oeration and lo:er caital costs. -he PMa catalysts 1oth o++er lon oeratin cycles

and are reenera1le.

P $ylene 5"on Mo1il 'hemical7


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P9$ylene 5"on Mo1il 'hemical7

-here are eiht M)-DP units 5redecessor technoloy to PMasm7 and three commercial units

usin the PMa technoloy.-he +irst t:o PMaunits utilied the M-P$catalyst and started u inCC4 and CCE at 'halmette e+inins &ouisiana e+inery and Mo1il 'hemicals !eaumont lant,resectively. -he third unit, usin "M92200technoloy,started u in CCB at "onMo1ils!ayto:n'hemical Plant.

Commercial Plants

Technology Licensor

"onMo1il'hemical 5retro+it alications7L I8P 5rassroots alications7.

Phthalic Anhydride5@ac?er 'hemie 6m1(7 P8D


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Phthalic Anhydride5@ac?er 'hemie 6m1(7 P8D

Pthalic Anhydride5@ac?er 'hemie 6m1(7


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Pthalic Anhydride5@ac?er 'hemie 6m1(7

-o roduce hthalic anhydride 5PA7 +rom o9ylene, nahthalene or mitures o+ 1oth +eedstoc?s usina +ied91ed vaor hase rocess, oriinally ?no:n as the von (eyden Process.

Application

Description

Air is heated and loaded :ith evaorated 57 o9ylene and/or nahthalene. -he hydrocar1on/airmiture enters a multitu1ular reactor 527 containin catalyst. An aitated salt melt removes the heato+ reaction and maintains constant temerature conditions. eaction heat enerates hih9ressuresteam. Modern lants oerate :ith o9ylene +eedstoc? loadins o+C0900 gl'm( air. eactor e++luent

as is recooled in a as cooler 537 1e+ore art o+ the PA vaor is condensed to a li>uid in the recondenser 5;7 and is continuously dischared to the crude PA tan? 57. -he remainder o+ a1out 4 PAlm( in the reaction as is condensed as solid su1limate in s:itch condensers 547 on seciallydesined +inned tu1es.-he s:itch condensers are eriodically cooled and heated in a discontinuous oeration o+ anautomated s:itchin cycle usin heat trans+er oil circuits. Durin the heatin hase, solid PA ismelted +rom the condenser tu1es and dischared as a li>uid to crude PA tan?. "++luent as is vented

to the atmoshere a+ter :ater scru11in and/or incineration. -he crude PA is thermally retreated 5E7and then +ed to the vacuum distillation system. &o: 1oilin 5&!7 imurities are removed in the lihtscolumn 5B7 as &! residues. -he hih91oilin 5(!7 residue +rom the ure PA column 5C7 is sent to theresidue 1oil9out vessel +or PA recovery. Pure PA o1tained as a distillate can 1e stored either in themolten state or +la?ed and 1aed

)ecial hih9er+ormance catalysts oidie o9ylene as :ell as oidiin nahthalene, o9yleneand mitures o+ 1oth +eedstoc?s in any roortions. All catalysts are rin9shaed.

Catalyst

Phthalic Anhydride5@ac?er 'hemie 6m1(7


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Phthalic Anhydride5@ac?er 'hemie 6m1(7

092 ? PA +rom 00 ? o+ ure o9yleneL CE9CC ? PA +rom 00 ? o+ ure nahthalene.

Yield

"cellent enery utiliation and minimied o++as volume are due to hih hydrocar1on/air ratio. Plantscan 1e desined to oerate indeendently o+ eternal o:er suly and eort electric enery or (Psteam.

Economics

Commercial Plants

More than 0 lants :ith tyical roduction caacities o+ 20,0009E,000 ty, :ith a maimum caacityo+ ;0,000 ty, have 1een desined and 1uilt 1y &uri.

Technology Licensor

@ac?er 'hemie 6m1(L eclusive contractor< &uri 0 6as 'hemie 6m1(.

O9$ylene is oidied :ith air to Phthalic Anhydride in resence o+2O catalyst at 3009;00S' and 92atm

Dimethyl -erehthalate56-' -echnoloy7 P8D


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Dimethyl -erehthalate56-' -echnoloy7 P8D

Dimethyl -erehthalate56-' -echnoloy7


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-o increase caacity and reduce enery usae o+ eistin or rassroots dimethyl terehthalate

5DM-7 roduction +acilities usin variations o+ 6-9DM- rorietary technoloy.

Application

Description

-he common roduction method o+ DM- +rom araylene and methanol is throuh successive

oidations in +our ma*or stes< oidation, esteri+ication, distillation and crystalliation. Amiture o+ 9ylene and methyl 9toluate 5MPl7 is oidied :ith air usin a heavy9metal catalyst.All oranics are recovered +rom the o++ as and recycled to the system. -he acid miture +rom the

oidation is esteri+ied :ith methanol and roduces a miture o+ esters. -he crude ester miture isdistilled to remove all heavy 1oilers and residue roducedL lihter esters are recycled to theoidation section. a: DM- is then sent to the crystalliation section to remove DM- isomers andaromatic aldehydes.-he technoloy imrovements enhance the traditional rocessin in each section. -he adatationsinclude< chanes in rocess con+iurations and oeratin conditions, alteratin the searationschemes, revisin the recovery arranement, increasin the value o+ the 1yroducts and reducinthe overall lant recycles.

6-' -echnoloy o++ers comlete imlementation o+ the technoloy and overall lant revie:s +orselective imrovements to reduce oeratin and overall roduction costs. )ome searateimrovements availa1le are<. Oidation otimiation reduces 1yroduct +ormation, thus lo:erin 9ylene consumtion2. ecoveries o+ 1yroducts +or sale such as methyl 1enoate 5Me!7 and acetic and +ormic acid3. Imroved esteri+ier reactor desin ena1les hiher throuhuts and imroves methanol usae



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;. "nhanced isomer removal minimies DM- losses. Imroved crystalliation schemes +or reduced enery, lo:ers methanol handlin and losses,

imroves urity and oeratin +lei1ility4. Interation o+ steam usae in the lant +or considera1le savins on oeratin costsE. Oeratin revie:s to reduce oeratin do:ntime and etend online +actorsB. Advanced control models +or imroved oera1ility.

Description$contd.%

Economics

!ased on rocess modi+ications, an eistin DM- lant can increase roduction :ith an investment

o+ =200 to =400/ton/yr o+ additional caacity. A ne: lant :ill have an investment reduction o+ a1out20 e>uiment cost. a: material consumtion er ton o+ roduct 5:ith the comlete modi+ication7is 40 ton o+ araylene and 340 ton o+ methanol.

Commercial Plants 6-9DM- technoloy is used 1y seven DM- roducers

Technology Licensor 6-' -echnoloy 'or.

-erehthalic Acid 5Deussa A67 P8D


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-erehthalic Acid 5Deussa A67 P8D

-erehthalic Acid 5Deussa A67


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Application

-o roduce +i1er9rade terehthalic acid 5P-A7 +rom dimethyl terehthalate 5DM-7.

Production o+ terehthalate +rom 9ylene and methanol are +ound under the dimethyl

terehthalate descrition7. DM- and the amount o+ methanol9+ree :ater +rom column 5E7needed +or the hydrolysis is mied in a miin vessel 57 and trans+erred to hydrolysis

reaction column 527 :here DM- is hydrolyed to terehthalic acid.-he +ormed methanol is stried o++ :ith steam +rom the evaorator 547. -he reaction miture +romthe hydrolysis is cooled do:n 1y +lash distillation in crystalliers 537. A+ter centri+uin 5;7, the P-Ais dried 57 and assed on to storae.-he +iltrate is recycled 1ac? to evaorator 547. )triin vaor o+ the hydrolysis reactor 527 isdistilled in a column 5E7 :here methanol9+ree :ater o1tained as 1ottom roduct is recycled tomiin vessel 57. -o roduct is searated in a second column 5B7 into the methanol overheadthat is recycled to the DM- lant and :aste:ater 1ottom is sent to incineration.

Description



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!asis is a 30,0009ty P-A lant, @est 6erman conditions, Decem1er2000,includin comressorstation, incinerator +or :aste:ater and o++ as, hot9oil heatin system and catalyst reeneration<Investment< 6erman conditions,Includin DM- roduction, DM/ty ,300a: materials and utilities consumtion, er ton o+ roduct<9$ylene,? EMethanol, ma?eu, ? 40@ater,demineralied,? 008uel,6R .;

Roint P-Aand DM- roduction in one lant is ossi1le.


Economics

Commercial Plant

-he rocess is licensed in -ai:an :ith a 200,0009ty lant.

Ullmann)s Encyclopedia of &ndstrial Chemistry* ol.A24, CB,. C3920;.

+eference

Technology Licensor

Deussa A6.

I#93 !enene $ylene 'hemicals


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Footer can be customized3%

9-echni 'hennai "I-s

. @hat is Nylon44

2. P9$ylene can 1e made throuh -oluene .

3. @hat is the oeratin ressure and temerature in PhthalicAnhydride eactor

;. Production o+ DM- involves com1ined oidation andesteri+ication ..-rue/+alse

. 8i1er rade -erehthalic Acid can 1e made 1y o+ DM-.

'rude -erehthalic Acid 5-PA7 Production


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'rude -erehthalic Acid 5-PA7 Production


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Puri+ied -erehthalic Acid 5P-A7 Production

/:ere are to 'rimar# met:ods o crude /B4 'uriication. /:e irst" described:ere" is b# direct 'roduction o iber&grade /B4 or 'uriied tere':t:alic acidB/48.n t:e 'roduction o iber&grade /B4 rom crude /B4" t:e crude acid isdissol+ed under 'ressure in ater at 229 to 279@


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P"- Melt Phase Polymeriation

B)/ resin is manuactured b# t:e esteriication o B/4 it: et:#lene gl#col andloss o ater " or b# t:e trans&esteriication o >=/ it: et:#lene gl#col and losso met:anol. $ot: reactions occur at 100 to 190@ < in t:e 'resence o a catal#st.$is 2&:#drox#et:#l8 tere':t:alate is 'roduced as an intermediate. /:isintermediate t:en undergoes 'ol#condensation under +acuum at 10 to 20@ <

abo+e t:e melting 'oint o B)/ 25;@


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P"- )olid )tate Polymeriation

/:e inal ste' in B)/ resin manuacture is a solid state 'ol#merization'rocess. /:is ste' raises t:e tem'erature o t:e solid 'ellets to Dustbelo t:e melting 'oint in t:e 'resence o a dri+ing orce to urt:er t:e'ol#merization. 6olid stating increases t:e inal .C. rom 0.72 to 1.05. talso 'roduces a 'ol#mer it: lo acetalde:#de content.

Polyethylene -erehthalate


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Polyethylene -erehthalate is 'roduced rom ethylene lycol and dimethyl terehthalate

or terehthalic acid. /:e ormer is a transesteri+ication reaction" :ereas t:e latter is an esteri+ication reaction. In dimethyl terehthalate rocess" >=/ and excess et:#lene gl#col are reacted in t:e melt at 190E200@< it: a 1asic catalyst. Methanol


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TRANSESTERIFICATION SYSTEM

POD'-

8""D DM-

"-(%&"N"6&%'O&

M"-(ANO&'O&MN

REACTOR

2

REACTOR

1

REACTOR

3

REACTOR

4

("A- "$'(AN6"("A-"$'(AN6"

("A-"$'(AN6"

("A-"$'(AN6"

'OND"N)"

M"-(ANO&

ROCESS FLOW SCHEME

ROCESS FLOW SCHEME

P"- P"PO&%M"I#A-ION "A'-O )%)-"M


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P"- P"PO&%M"I#A-ION "A'-O )%)-"M

POD'-

8""D !("-

"-(%&"N"6&%'O&

REACTOR

2

REACTOR

1

REACTOR

3

REACTOR

4

("A- "$'(AN6"

'OND"N)"

-O A'M)%)%-"M

-O A'M

)%)%-"M

'OND"N)"

-hin 8ilm eactor


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8""D

!&AD"))'AP

-(" -(IN8I&M)8A'"

6&%'O&

D"I'"6"N"A-")-(IN 8I&M

A6I-A-O

PO&%M" POD'-

8""D

PO&%M" POD'-

6&%'O&

-(IN 8I&M"A'-O

DI)' IN6"A'-O

DI)') @I-((O&") 8O6"N"A-IN6-(IN 8I&M

8""D

One o t:e most im'ortant c:aracteristics o B)/ isreerred to as Intrinsic iscosity C8

http://en.wikipedia.org/wiki/Intrinsic_viscosityhttp://en.wikipedia.org/wiki/Intrinsic_viscosityhttp://en.wikipedia.org/wiki/Intrinsic_viscosity


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reerred to as Intrinsic iscosity C8

/:e intrinsic +iscosit# range o B)/

Fiber grade0.50 E 0.70 d-g /extile0.72 E 0.% d-g /ec:nical" tire cord

Film grade0.;0 E 0.70 d-g $oB)/ biaxiall# oriented B)/ ilm80.70 E 1.00 d-g 6:eet grade or t:ermoorming

$ottle grade0.70 E 0.7 d-g (ater bottles lat80.7 E 0.9 d-g


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Footer can be customized5%

-echni NOIDA "I-s

. @hat is the oeratin ressure and temerature in -erehthalic

Acid eactor

2. @hat is the oeratin ressure and temerature in "steri+cationo+ -erehthalic acid

3. "steri+ication 5-PA7 and -ransesteri+ication 5DM-7 eactions

are carried out in a series o+ .

;. @hat is the ma*or hysical characteristic roerty +orevaluation o+ olyester roduct

. @hat is the ressure in 8inishin eactor o+ P"-


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