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Dr. Amalendu Datta – Advisor Process NOIDA / 30th May, 202

  !"N#"N" $%&"N" '("MI'A&)

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

•  Ma*or source o+ !enene, -oluene and $ylenes is 'atalytic e+ormin nit. •  !enene can 1e roduced +rom -oluene and Other hiher Aromatics 1y disroortionation reactions.

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!enene 'hemicals

'yclo (eane

!enene

"thyl !enene

)tyrene

Poly )tyrene

)tyrene !utadiene u11er 

Acrylonitrile )tyrene !utadiene u11er 

'arolactum

Nylon 4

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!enene5A!! &ummus 6lo1al7 P8D

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!enene5A!! &ummus 6lo1al7

 Application

-o roduce hih9urity 1enene and hiher aromatics +rom toluene and heavier aromatics usin the Detol rocess.

Description

•  8eed and hydroen are heated and assed over the catalyst 57. !enene and unconverted toluene and/or ylene and heavier aromatics are condensed 527 and sta1ilied 537.

•  -o meet acid :ash color seci+ications, sta1ilier 1ottoms are assed throuh a +ied91ed clay treater, then distilled 5;7 to roduce the desired seci+ication 1enene. •nconverted toluene and/or ylenes and heavier aromatics are recycled.

Economics

!asis o+ 00 MMy< "stimated investment, =/1sd 300

-yical utility re>uirements, er 11l +eed< "lectricity, ?@h .B 8uel, MM!tu 0.3 @ater, coolin, al ;0 )team, I1 ;.;

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!enene5A!! &ummus 6lo1al7

Aromatic yield is CC.0 mol o+ +resh toluene or heavier aromatic chare. -yical yields +or

roduction o+ 1enene and ylenes are< -ye roduction !enene $ylene 8eed, :t Non aromatics 3.2 2.3 !enene 9999 .3 -oluene ;E.3 0.E 'B aromatics ;C. 0.3

'CFaromatics 99999 B.; Products, :t o+ +eed !eneneG E.E 34.C

'BaromaticsGG 99999 3E.E G.;H' minimum +reee oint GG.000 m nonaromatics maimum

Yield 

-:elve lants :ith caacities ranin +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 !enene5!ader -echnoloy7 P8D

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"thyl !enene5!ader -echnoloy7

-o roduce ethyl1enene 5"!7 +rom 1enene and a olymer rade ethylene or an ethylene9rich

ethylene/ethane +eedstoc? usin the Mo1il/!ader "!Ma rocess and rorietary "on Mo1ilal?ylation and transal?ylation catalysts. -he technoloy can 1e alied in the desin o+ rassroots units, uradin o+ eistin vaor9hase technoloy lants, or conversion o+ aluminum chloride technoloy "! lants to eolite technoloy.

 Application

Description "thylene reacts :ith 1enene in a li>uid9+illed al?ylation reactor 57 containin multile +ied91eds o+ "on Mo1ils rorietary catalyst, +ormin "! and very small >uantities o+ olyethyl1enenes 5P"!7.

In the transal?ylation reactor 527, P"! is converted to "! 1y reaction :ith 1enene over "onMo1ils transal?ylation catalyst. P"! and 1enene recovered +rom the crude "! enter the trans al?ylation reactor. "++luents +rom the al?ylation and transal?ylation reactors are +ed to the 1enene column 537, :here unreacted 1enene is recovered +rom crude "!. -he +resh 1enene +eedstoc? and a +raction o+ the 1enene distillate are +ed to the lihts column 5;7 to re*ect liht imurities. -he lihts column 1ottoms are returned to the 1enene column. -he 1ottoms +rom the 1enene column are +ed to the "! column 57 to recover "! roduct. -he 1ottoms +rom the "! column is +ed to the P"! column 547 :here recycla1le al?yl1enenes are recovered as a distillate and dihenyl comounds 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 !enene 0.E3C )team, hih9ressure used .0 )team, medium9and lo:9ressured enerated .;2

Utilities can be optimized for specific-site conditions.

Economics

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'ycle lenths in ecess o+ +our and three years are eected +or the al?ylation and transal?ylationcatalysts resectively. Process e>uiment is +a1ricated entirely +rom car1on steel. 'aital investment is reduced as a conse>uence o+ the hih activity and etraordinary selectivity o+ the al?ylation catalyst and the a1ility o+ 1oth the al?ylation and transal?ylation catalysts to oerate :ith very lo: >uantities o+ ecess 1enene.

Catalyst 

-he ethyl 1enene roduct contains less than 00m o+ 'B lus 'C imurities. Product urities

o+ CC.Cto CC.CCare eected.

Prodct !ality 

Technology Licensor 

-he !ader -echnoloy 'enter o+ @ashinton 6rou International, Inc.

Commercial Plants

)ince the commercialiation o+ the Mo1ill !ader "! technoloy in CB0, ;2 licenses have 1een ranted. -otal licensed caacity +or the "!Ma technoloy eceeds .2 million mty.

"thyl !enene5!ader -echnoloy7

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)tyrene 5A!! &ummus 6lo1al J OP7 P8D

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)tyrene 5A!! &ummus 6lo1al J OP7

 Application -o roduce olymer9rade styrene monomer 5)M71y dehydroenatin ethyl1enene 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 revams.

Description

In the 'lassic rocess, "! is catalytically dehydroenated to styrene in the resence o+ steam. -he reaction is carried out at hih temerature under vacuum.

•  -he "! 5+resh and recycle7 and rimary steam are com1ined :ith suerheated steam, and the miture is dehydroenated in a multistae reactor system 57. An interheater reheats the rocess as 1et:een staes. eactor e++luents are cooled to recover :aste heat and condense the hydrocar1ons and steam. • ncondensed o++as is comressed and is used as +uel. 'ondensed hydrocar1ons 527 are sent to the distillation section. Process condensate 527 is stried to remove dissolved aromatics. A +ractionation train 53,;7 searates hih9urity styrene, unconverted "!, :hich is recycled, and the relatively minor reaction 1yroduct tar. -oluene is roduced 5,47 as a minor 1yroduct, and 1enene

547 is recycled to the al?ylator. -yical )M9roduct urity ranes +rom CC.B to CC.C. -he rocess rovides hih9roduct yield due to a uni>ue com1ination o+ catalyst and oeratin conditions used in the reactors. -he )MA- rocess is the same ecet 1et:een the dehydroenation staesL oyen is introduced to artially oidie the hydroen roduced over a rorietary catalyst, to reheat the rocess as and to remove the e>uili1rium constraint +or the dehydroenation reaction. -he rocess achieves u to or reater than B0 "! conversion er ass.

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)tyrene 5A!! &ummus 6lo1al J OP7

Investment, .). "#tpy 

5.). 6ul+'oast 1asis, 200,000 ty7 22 a: materials consumtion, er metric ton o+ )M<   'lassic "thyl1enene .0; tilities, .). "#ton )M 3

Economics

Presently, 34 oeratin lants incororate the &ummus/OP styrene 'lassic technoloy. -hree oeratin +acilities are usin the )MA- rocess technoloy. Many +uture units usin the )MA- rocess are eected to 1e retro+its o+ conventional units, since the technoloy is :ell suited +or revams.

Commercial Plants

Technology Licensor 

A!! &ummus 6lo1al J OP

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Footer can be customized13

I#9 !enene $ylene 'hemicals 9-echni 'hennai "I-s

. @hat is the ma*or source 5re+inery rocess7 o+ !enene and 9$ylene 

. @hat do you et 1y al?ylatin !enene :ith "thylene 

2. )tyrene is roduced 1y .o+ "thyl !enene.

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

. @hat is the conversion er ass o+ "thyl !enene to )tyrene 

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Polystyrene 5OP7 P8D

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