ECE/ENV/3S

ECONOMIC COMMISSION FOR EUROPE

LOW-AND NQN-WASYE TECH OkOGY

VOLUME 11

Summaries of Monographs 21 - 4.6

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- -- UNITED NATIONS

Geneva, 1981

- . L/ These s m a r i e s have been reproduced i n the forn i n vhicl? they m r e received

by the S e c r e t a r i a t ,

pege

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Vater Eystec closure i f i papcr r~i1I.z.

Recovery and r ecyc l ing of rimoniz contnined i n g x e s from a r x i o ~ ~ ~ u n Ei t rGte production.

Recovery of hydrochloric ;cid frog i n c i n e r a t i o n of clilorinr.ted i r r s te productc.

Recycling of \ ra te r fron nxmfcctu,-ing of nsbes tos/cemcnt p.;ccls znd p i p ~ s .

Recovery -mil r e c y c l i n c o f so iven t s f r o n v2pouTs o r i g i n a t i n g f r o n primin2 ccd p a i n t i n g of a luminim f o i l s .

Dry-phase n e u t r d i s a t i o n of cI lylatc , r C;cncrated ii> the production 43f styrene.

Hydrogen xrzshi~g by potassi7.m ccrbonzte ia c m o n i a 2roduction.

Pie c hani c a1 pee l i i 1 G o f ve ge C: ~ . . b l c s /f r u i t s . Descaling of metal ob jec t s by seam o f v ib ra t io i l / ab r~s ion .

Recycling of water i n the mmufactrming o f vood fibre pznels.

Surface treatment of p l a s t i c mc tc r i a l s i n a sulphochronis s o l u t i o n irith regenerat ion snd r ecyc l ing of the so lu t ion .

Extract ion of potato s t n r c h with recovery a ~ d use of p ro te ins i n internz.1 l i q u i d .

Production of m o n i m n i t r a t e uI th c o n t i n u o x c o n t r o l of the r e c c t i o n and degassing of t he r e s u l t i n g water vsgours.

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LGV- MTD - TTOIT-1 iiiS'1E T"TWO.X!(X

Production ijf t i t a n i m . lrhi'ce from i l n e n l t e S;J the sulphc?te me'A1od with re-processing o f '&he qucntitatiyIely aost important trr:ste products. '

STAGE OF D ~ E L O P I ~ Y P 0;' LC1 !- AIJ9 i?Gl?-~,fALTC --- TZCHITOSQGY

The thickening of su lphur i c cicid ~ G T decomTosition ald the processing of s t r o n g l y a c i d e f f l u e n t s t o i i 1 d s t r l a l Q~ISLJJI a r e implenented i n fu l l - s ca l e operat ion. has been v e r i f i e d on a serai-scale bcs i s .

The teclmolu2y 3f p r e c i p i t a t e d f e r r o w pigments

3EE)ORTING OEGlUTIZAT I O U

Federal t i i n i s t r y f o r Teclinical Development sild Investments of t h e CSSR.

DATE: OF REPORT

15 December 1979.

(a) ProcessiEg s t e p s

- Thickenifig of su lphur i c ac id f o r i lmen i t e deconposition.

- Thickening of s t r o n g l y ac id e f f l u e n t s a d t h e i r n e u t r a l i z a t i o n v i t h l i n e n i l k (processing of t he suspension t o i n d u s t r i a l m s U 4

- Processing of green v i t r i o l by a new technological method t o p r e c i p i t a t e d f e r rous p i p a n t s m d monL.m sulphate .

The range o f marketzble produc-cs from thc: mmufacturing process is exterlded t o include i n d u s t r i a l gypcm, sulplzuric ccid and s o l i d m o n i m sulphsze. occupation

ferrous p ime i l t s (yellow, r e d , b l ack ) Znvironneni;al problcne rre resolved and

of a g r i c u l t u r a l land f a r trzste disposal is no lonccr necded.

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REPCIRTIiTC- ORG~LTIZATIOU :

Cowiconsult , Consuitin, Zn@nocrs ancl Planncrs AS, Tclmikcrbyen 45, DK-2870, V i n u s . DEIXLFLFX. cquipmcnt f o r biogas y l s n t s . DkL"E OF REPOTX:

A nmbcr of otlicr firms also develop and scll

1G October 1573

Processing s t q s : d i g m t e r , irherr? i t is hcatecl t o c7- temncraturs of 50-60' and m i : c d with a c u l t u - c of thcrmw-dzilic 'oactcria. i n a scpa ra t c container . vi thdrztm f r o n t h e d i g c s t c r f o r Getratering ,and f i n d dis;?osal.

The s c b s t r a t c i s t ransfcrred t o an a i r - t i g h t ..

iI- thme as is. co l l ec t ed 3 iges t cd ma te r i a l i s 2 e r i o d i c a l l y

I!hterizls/energy r equ i r c r~cn t s : sw11cr than f o r m e s o ~ k i l i c c l i p s t i o n , m c l the c lwa te r ing i s e a s i e r too. necdcd f o r hza t inc .

Form znd mount; ai: r e s i d u a l s ,-cncratecl: pro&uct" w i l l be t h e digestcd sludge, which will bo Iroduced i n considerable amounts i n yoss ib l e f c t u r e f u l l - s c a l e p l a n t s I

The necessary d i g e s t e r volume is

T h c drvnlopcd methmc gas w i l l probably doli?rcr t h c energy

The only " r e s idua l

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(e) Forn and aaount of waste dischar,ce t o the environuent: The d iges t ed sludge vi11 g-.nzrally bc tis11 sliited f o r land a y p l i c a t i o n , as it,.iJill be a l z o s t conpletely f r c e of pathogenic organisas .

(f) I n t e s t n e a t reqxiremei:ts Inv2stnents vi11 be snaller thzn f o r mesophilic anaerobic d i g w t i o n b e t o thc smaller c'.igester voltune needed. p s .

Ener,gy reqt.irement;s w i l l 3e covered- by the sroduced n e t b n z Possibly, there w i l l e l s o bc surplus gas for other purposes.

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I?DUSTX

3523 - Plan t f o r t he processing of Lsed solvents .

C02PEllTIOUAL TSCIiiTOLOC-Y

D c s t n c t i o n , s n o c i a i d q o s i t . d i s t i l l a t i o n s l u 6 - p .

C i z T l t d i s t i l l e t i o n and des t ruc t ion of

LO?/ ITOI'Y-\IASTE 'TECSI'TOLOGY

I s o l a t i o n of a t t r az t ivc? cocq>oncnt (s) by wzy of d i s t i l l e t i o n , r e t i f i c a t i o n , and/or ex t r ac t ion . t o form 2 f u e l s u i t a b l e f o r s t e a n prcduction.

STAG3 OF DEVELOPI.%IX OF L/l3fl

Production i s s t i l l l a r p i y i n an e x p r i n e n t a l phase.

REPORTIiJG ORGANiZATiOB

Vanokon Petrokciaisk Vzd: Rps , Snavcvc j 25 , 54-71 S jh i e r sh , Demzrk. Telephone: (03)87.18.55.

The d i s t i l l a t i o n sludgz i s modified

Procsssing s t eps :

S t r i g T i ng + Dist i l la te treatment f i n i s h e d product ---? t i

4 ' f steam production sludge cornbustion ~-

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I k t e r i a l s / e n e r g r e q u i r e n e i ~ t s : 0.2 - 1 kg, water vayoujr,kg of prcduct , and. 0.25 Mdh/kg product.

Form and aaount or" r c s i c h a l s generated, 0.02 kg. of ashes (metal oxides and s i l i c i u n conFounds)/kg of raw matc r i a l (waste) (By simple d i s t i l l a t i o n t h e sludge w i l l t y y i c a l l y represent 20-50 Fer cent of t h e waste quan t i ty ) .

c 1 e m i rig.

Form and amomt of irastc discharge t o the environment: 30 ng of ciust/nm3 of i ' l ~ c gas and 500 e;r of so lven t s / t

4Fs

of rzir p a t e r i a l .

Investment r2quirmcnts and u n i t production cos t : Isvzstment rcqxirnment ii: s l a n t s with a capac i ty of 2,000 t of rzd Ioaterial gcr year : Vaiab2.e c o s t s :

j s i l l i o n D . h . 100 3 , k r / t .

Processing of desorbates fro= a c t i v e carbon f i l t e r . F in i sh ing and re-use of s p e c i a l Gistillate r e m m z x e , for i n s t ancz hydroxylterninsted polpirethan prepolymers . The process i s p a r t l y energy self-suTplying, (stcam Froduction from. conbustion of sludge).

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DzscaliEg or" s tc?el ' a i l l z t s by d?ot- 'olmting,

DATZ OF FEPORT

(a) Processing s t c p s

Thc shot-blest ing cons i s t s of y r o p s l l i n g n c t a l l i c grit against thc b i l l e t t o be treated, t o 2nsuTe Ci:: shatterin,rr of t he calamine l a y e r . T h i s oycrat ion takes i3lczcc i n an armomcd chamber. The d u s t i s vacuumci: t o a dc-<Lust zccw"1ator room before discharge, Thc grit d::ed with calitnine i s recycled. Tine s tandard technique i s t c t z l l g d i f f e r e n t s ince th desca l ing i s brought about by the ac t ion of the a c i d as $he b i l l e t s a r e dipi7ed i n succsssive baths.

The lotr p o l l u t i o n technique r cqu i r e s a small quan t i ty o f s i t , corresponding t o the cunount nccessary t o renew g r i t l o s t i n r ecyc l ing (1.8 ltg) . The s tandard techEique reqvircs water and

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9 l i t r e s of su lphur i c acid.

TJnlilcc s tnn<a,rcl t c c ~ h i i q u ~ , the lo.ii pol_lutiol? 'iechciqw c l i d n a t s s 2.11 aqueous i rnstcs ca rn j ing snspen3zd n a t t e r and ac id . On t he o the r Iiend, i t r c s u l t s i n the formation of dvst (qwnGity ;u;cleterrained) a disclr?ar,-o of s i t Jrhich correoponds ?io r ecyc l ing lo s ses (1.8 kg p z r t o n of b i l l e t s dsscalcd) and iz noisc l e v e l of 80 dec ibe l s ttro metres mzy.

Pollv.ticn concrol uec?s1ues r e p i r e d for compiicnce with existing s tandarcis

The dust produced i s vacuumed i n t o a de-chst accumils tor room and the s o l i d iras'ics i x c sent i n t o an a r c furzacc.

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(e ) Forn and amount of waste discharge t o t h z envirorment

T h e p o l l u t i o n , a f te r dz-dusting, i s reduced t o 22 x of dxst T e r ton of b i l l e t s nanufactvred. dec ibe l s 2.t ttro a e t r e s , All s o l i d trastes a r c dXscharg2d. s tacdard technique, OR t h e contranj , ar"ter n e u t r a l i z a t i o n p o l h t i o n by ap2ov.s irastes i s s t i l l 8 kg of susyni'icd- and. cxydicable lllatter and 0.1 k i l o ecpito:: p r t o n .

Investment rcquirenents and unit production c o s t s

The noise l c v e l rzncains a t 30 I n the

(f)

The nccessary invostment f o r t he 1011 Fo l lu t ion tcchniqv.5 is 543,OCO Francs (1973 I h n c s ) as opposed t o 100,COO Francs f o r t h e standard technique, r e s p c t i v e l y 96 Franc;; and 152 ~ P r m c s (1978 Francs).

Diverse e:rl)ensas per t o n of b i l l c t s descaled zre

8 GTIER SIGTXPICUl ASECTS 03' LOT:]- AID IT0JlT-Vl~STE TEcKp(T0LOC;Y

Amelioration of workring cor,ditions r?xce;,,t for noise factor.

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The e lcc t rophores i s q e r a t i o n ( anp l i ca t ion of pa in t by e l e c t r o l y s i s ) i s t:ic mnc as t r i th th? stan62rd technique, The r i n s e oratcrs undergo u l t r a f i l t r a t i o n , trllick sepa ra t e s t he 7.rater from the p a i n t i t contains . The p a i n t i s re--ae& f o r e l cc t rophores i s , idxi.1~ the 7:ratcr i s recycled f o r r i n s i n g .

For t h e treatment of a 1,000 n2 su r face , the lorr p o l i u t i o n techl ique reyvires 28.75 !:$ of p i n t ( a p i n s t 52.5 kg € o r the standm3 tesliniq.clc), 0.5 n7 of vater (against 30 a?) and 1.6 G J f o r t h e necessary elcctr ic i t ' J f o r t'nc nevr c i r c u i t ~LIEI?S.

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P o l l u t i o n con5rol mces~rcs -.. exis t i i?g s t a n k r d s : i!om.

required for compliance ~~4th

Form and zzoimt of a-rastc discharge t o th2 emironmelt

3 o f trater f o r t!?c Nom f o r thc ~ O V ?ol lut ioi i technique, 50 m standard technique (containing 3.7 kc of suqendcd matter aiid liavin,- 32 lcg or" chemical OFJ~CC,~ dcmnd and a Cronomced c o l o ~ r ) .

Investment roquireoezlts and un i t procluction cos t s

552,000 Frt.ncs (1980 Francs) . Production c o s t s f o r 1,OCO m2 of t r c a t c d suxfscc : I, 257 Francs f cr thc lorr p o l l u t i o n teclmdqLlc ; 1,182 F r a m s f o r the standard technique. Without cleWeciation __ _ _ -- - these f i g u c s becone: 1,167 and 1,182 Francs,

8. OTHER SIGiTiFICAXT ASPZCTY Or L/IW -

The u l t r a f i l t r a t i o n can be appl icd t o both e l s t r o p h o r e s i s proccsscs: c a t i o n i c and an ion ic

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J u l y . 1980

(b) i l a t e r i e l s and ecer,ay requi~Pments

thanks to the automation of the rcercerizer t h z t r equ i r e s l e s s rwte r f o r r i n s e s (15.7 G J per ",on of thread aercerizeci as opposed t o 19.5 G J ) .

Soda end we ttiriz agent conoimption are considernbly reduced: of pure sods, 5.5 !:g o f vettin: agent per ton of thrcad, a,-cinst 470 kz and 8.5 kg r e spec t ive ly ,

Eren . r i t h tile e i ' z g r a t o r the l o ~ i go l lu t ion techniqcc usc?s less energy,

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173 kg

( c ) For?? 2nd mount o f residv.els zenerzted

Anti-goilukion measures: n e u t r d i z a t i o n of the scch v i t h hydrochloric ac id : ton a t 22” Ea.“.

.525 1 3 p e r ton a t 2C0 bum6 against i,‘>53 1s per

( e ) Fom m d m o u t o f m s t c discharGe to the envi romznt

Reduction o f the rate o f m s t e discharge (l3m3 aga ins t 8 G m 3 per ton o f th read) , reduction of the chemicd. ax;l/%sn dcnrtnd i n the waste discharge (13 Zca ageins t 22), reduct ion o f salinity (1.52 2rg o f dissolved sGJAs-agEinst ->2d) .--.-------------

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Investment requirenents and uni t - p roduc t ion . cas t

8.

In 19’77, l,4.3O,OCrJ Francs for the l o v pollukion process as opposed to 1,133,CC; Francs for the standzrd technique. Divers2 expenses per ton o f tnread mercerized: 1,329 m c s ( i n 1977) f o r the low p o l l u t i o n technique, against 2,000 Francs for the stGndard technique . OTREB SIGlTiFICABT ASPECTS OF L/bWI!

The modern mercerizer used, mentioned .above, allows the- use or” less manpower

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In the low p o l l a t i o n process, the r in se t i s te r i s recycled; heretofore it vzs discharged i n t o the senage system.

?ne mdi ;rater, a f t e r having been centr i fuged i n the stendard process i n order t o separate the su in t , i s g radua l ly dr ied off. Various intermediate by-yroducts are inc inera ted i n a chzmber yrovidi i .? the necessary s t e m f o r the tra%er treatment phase.

Tlctzr consvantion i s 2 r.13 per ton ins tead o f 7.5.

( e ) FOEI and mount 05 residu,-.ls generated

Aqueous TrasteS dia2.ppez.Y completely f i t h the lo!r ??cllution

The 1 3 ~ ~ i>ollxtioI2 technique ,?..llo.crs the technique, 0 .5 1% o f dust p e r ' b n . reduct ion of the SC

(d )

?uo t h tec!miq_ues b i - i ~ abou 1 atmospheric g o l l u t i o n ol

&LSdiarg$ci from 2 . k ~ t o 1.5 kg per ton.

Po l lu t ion c o n t x l nep.sures required f o r compliance u i t h e x i s t i l% s tanclards

KO add i t iona l mna,suxes zre required v i t h the l o i r Fol lu t ion

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process except f o r tl-,e t reatnenr, or" fumes from the boilei- .

( e ) Form and m o u n t o f imstc cliscl:arge t o the envimnnent

Vi tk the stacdzrd pr3cess, t h e chemical oxygen 2emznd of the r e s idua l water a f t e r cen t r i fuga t ion (4.5 m3/tons) i s jcjo Q; wastes (1.8 m 3 / t ) a r i trez.r;eci by a p u r i f i c a t i o n s t a t i o n .

rir-se

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These aqunous rrastes ciisappear vit i i the low po l lu t ion process. The dus t (9.5 kg/t) and the SG f i l t r a t ion .

( f ) In- e s h e n t requirenents an unit production c > s t s

(1 .5 kg/t) a r e discharged tri t i iout 2

(Telcing i n t o account the 2 u r i f i c a t i o n s ta t ion t h a t vo:zld have t o have been i n s t e l l e d v i t h the standard process) . 15,030 ,GGC Francs f o r the 107,- po l lu t ion technique, j2,5CG , O W Francs f o r the standart! technique. Diverse expenses per ton 02 TI001 l:2wsh?d i n 1977: f o r the stnndcrd technique, i!ithout k k i n g i n t o account r e c e i p t s from the sale 01 s u i n t (185 Trancs) o r f e r t i l i z e r (no figure availo'ule at t h i s time).

Investments:

135 Francs f o r the l a r g o l l u t i o n tecilnique and l7C Francs

None.

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tized

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- - ( c ) ~ o m and mount o f r e s idua l s generated

The mnufzcturii-< imter i s pniZiec1 Sefore bein& discharged in to the ri-er. There are 3 kg of suspeaded 2nd oxydiza5le ma%xer pez to i l o f pz:.oer nanufacta-ed, aga ins t E ,1 k~ i n t;in standard tec:ulic;ue.

( d )

2o l lu t ion r e x l t s so l c ly from rzirr 2 ~ 5 c o o l i p ? m t e r .

Po l lu t ion cont ro l measures required for compliance with ex i s t ing stendards.

In the l o r j pol lut ior , tec!mique, s ince tile po l lu t ion produced i s d l ov and cocforins t o the cont rac t noims, no measures zre necessary.

( e ) Fo-mi and aiount o f irsste d i sc la rge t o the envi roment

Same a s under ( c ) . (f) In1jesi;ment requirements ~l . r?c~ i m i p o d u c t i o n c o s t s __ I .- - -- --.I-

The necesszqr investment for the l o v po l lu t ion technique i s 800 , O K r r ancs , conpared t o l ,5C!O ,QGO for the s tanderd technique iP a s b n d a r d treatment solutio11 had been en2loyed. are r e spec t ive ly 7.3 Francs and 7.0 Prz.ncs per ton o L P _napex' ?reduced.

OTIBI? SIG1TIFIGA€lT BSECTS GF L(m

Production c o s t s

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Profound modif icat ion o f comportment o f personnel.

Winis th re de 1 '?b,vironnement e t du ZxIre de Vie Di rec t ion de l a PrGvention des Pol lu t ions 14 Boulevzrd du G5ndre.l L c d e r c 92521 "ITeuillj.-sur-Seinc Cedex, 3rcnce

August 1980

(a) ProcessirG s t eps

The synthesis o f mmonim n i t r a t e i s c a r r i e d out i n bozh techniques thro-Gh a n i t r i c ac id r e a c t i o n on the ammonia. place, vapour i s i'orncd, containing a sclall moun t or" cmmonia. i n the formerly used process t i e vspour lias discharged, i t ; i s now washed i n n i t r i c ac id , which p3rmits recuperet ion and recycl ing o f the ammonia t h a t i t contains .

When tke r e a c t i o n takes :l'liereas

('0) Materials and ecergy requirencnts

Each ton ol" ammonium ni t rz , te msnufcctured requi res :

0213 kg of m o n i a for the lm: n o l l u t i o n technique ( zzz ins t 215.5 kg)

-787 ks o f r i t r i c a c i d f o r t h c lorr n o l l u t i o n technique (no chm,nc)

05.58 G J for the v e n t i l a t o r a-nJ supplcnertary pmps .

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( d ) Po l lu t ion cont ro l measures reopired for compliance with e x i s t i q stendzrds . .

No measures a r e necessary, bv.t a p a r t o f the vapour i s condensed i n order to recover the heat i t contains.

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Fom and amount o f waste disclnrge to the envimnment

Atmospheric discharges :

9 . 3 5 1% of mineral nitroZen foT the l o v p o l l u t i o n technique (aga ins t 1.5 19)

Discharges in to m t e r :

Outflo7.r : 0.271113 (no clxnge)

00.4 kg o f mineral nii;raGen for thc l o u p o l l u t i o n teclmiqu? (aga ins t 1 . 6 kg).

(f) I n v e s t ” requirements and unit production c o s t s

Supplenentaxy icvestment: j50,C)GO Francs i n 1976 f o r r?n annml production o f 152,090 tons. ...

Production cos t (without deprec ia t ion) f o r a ton o f ,.su;lonim~ n i t r a t e vias 2.11 Francs less i n 1-379 €or the low p o l l u t i o n techniqua.

_ . .--. - - . --..- _ - -. .” . 3. OTflER SIC-iTE’IC\ITT ASE’ECTS OP L / W ! -

ITone .

30 of chlor inated waste moducts

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C Oi!fl~'W.!? I G N A L TI? CPLTGLijGY

Incine r a t ion of ch lo r ina t ed 1.4 as t e s followed by n e u t r a l i z a t i c n

Inc ine ra t ion of chlor inated wastes fc.llo.cled by recovery of hydrochloric acid.

€ $ i n i s t i r e d+ 1IXnvironnenent e t du Cadre de Vie Direc t ion de l a Pre'vention des Po l lu t ions 14, Boulevard GBn4ral Leclerc 9 2 5 21. Neuilly- sar-Se im C e dex , France

DATB OF REPORT

August 1980

PROCESS 2ESCRI'PTiOW OF L/NhlT AKil DEI.TTIFICATI3W OF DImEEWCES C C l G " D TO CO??VEBTIONAL TZCEiOLOGY

(a) Processing s t e p s

The tox ic chlor inated v a s t e s a re inc ine ra t ed i n an oven. oombustion gases are f i r s t uater-cooled i n a closed c i r c u i t , then the hydrochlor ic acid t h a t they contain i s absorbed i n water t o give a inarketable acid solut ion. cool ing water c i r c u l a t e s i n ax open c i r c u i t and, because i t takes on acid, must be neu t r a l i zed before discharge. I n both processes, the gases a re neu t r a l i zed i n soda before being discharged i n t o the atmosphere. source of po l lu t ion i n the standard technique.

The

I n the standard process, the

me discharge of the coolir,g water i s the p r inc ipa l

(b) Materials and energy requirements

Per ton o f v a s t e , both processes require 65 kg of soda. The low p l l u t i o n techniqce r equ i r e s no l i n e (as opposed t o 550 kg) , and r equ i r e s 3 9-13 or" water ( aga ins t 65.5 m 3 ) and (2.608 G J ( a g a i n s t 0.298 GJ). /J

(d) Pol lu t ion con t r a1 r easu res required for com9liance v i t h e x i s t i n g s t andazd s

Ro measures a re n e c e s s a r j ef ter the n e u t r s l i z a t i o n s .

- -

( e ) T o m an2 amount of waste d i scha rh i t o the environrent

The wastes emitted are those described i n s e c t i o n C.

Investment r eqa i r enen t s and u n i t production c o s t s

InvestKent f o r l o u poll7ition process: 1G,OCO,OCO ) . Production c o s t I;er tm t r e z t e d :

( f )

l?,COO,CGO -- f r ancs ( aga ins t

181 f r ancs ( aga ins t 322.0 f r a n c s ) .

8. OEER SIGi"1CAlTT b.SFECTS GF L/I?:!T

None. i

-.

31. Recycling of v a t e r from manufacturing of asbestos/cement Danels and ci-ces (Summary of monograph ZFJPJ?. 2/5/Add. 31)

1.

2.

3.

4.

DJEUSTRY

3699 - i"lanufacturing of non-netall ic z i n e r a l products with the exception of petroleurn and coal de r iva t ives .

COI'TVZBTIOMAL ~ C B T S L O G ' !

Manufacturing of asbestos-cement panels arid pipes water used i n mmuf ac tur ing, a f t e r decm.tin2. :'>

Manufacturing of asbestos-cement panels and piTes water used i n thn process.

with discharge of

with r ecyc l ing o f the

__-__-__1__--"------ 1ndu-s-tFial -dfveloperrt- for ~ a r ~ i ~ ~ - r e c ~ ~ c ~ ~ ~ ~ - - ~ I n d u s t r i a l t e s t i n g for complete recycl ing.

5.

6.

7,

- FiE PORT DTG OR GAI? 12 AT I G i i

Ministzre de 1'Environnement e t du Cadre de Vie Di rec t ion de l a Privent ion des Po l lu t ions 14, Boulevard de Ce'n4ral Leclerc, 92521 Neuilly-sur-Seine Cedex, Prance

DATE OF FEPORT

August 1980 e

PROCXSS DESCRIPTION OF L/lRPT Aim DEXTDICATIOJT OF DDmmNmS CBIQARED TO COJTVENTIOJTAL 'IECHf.TGLOGY

(a) Processing s t eps

The asbestos and the cement are mixed i n water. The r e s u l t i n g mixture i s placed on a c l o t h r o l l i n g a t high speed, i s drained there and forms a t h i n lPye r t h a t serves as a base f o r the panels and pipes.

The water drained o f f i n both processes i s decanted twice.

The residue from the f irst decanting i s recycled; second i s a l s o recycled i n the lot i po l lu t ion process, while i t i s discharged i n the standard process.

t h a t from the

( b ) Mater ia ls and egergy requirements

Water consumption i s p resen t ly 0.80 m3 F e r ton of asbestos-cement with the lov ? o l l u t i o n process. process.

It i s 6.1 a3 with the standard It should drop t o about 0.4 m3 by 1983.

.. . r

,>

i 1.

( c ! Form and mount ol' r e s i d u a l s genzrated

low po l lu t ion process) . _.

Pollt i t ion c o n t r c l Teas'nes req;ired for c c r p l i a c e with euistiz; stan?.ard s

( d )

Anti-pollat ion measures : condensation CY residue..-. _ _ - _ _

( e ) Porn ar,d m o m t of r..,aste discharge t> the environment

7 The discharge of t i i s tes i s reduead t s 9.~15 1173 frJEI 5.7 iW E r ton of asbestos-cement, and the susp-ended and oxidizable matters a r e reduced t o 8.5 g ,and 14 g r e s r e c t i v e l y ( ags ins t 2,460 g a d 215 g ) .

Residue discharged i s 18 kiz; F e r ton o f asbestos-cement for the 1 c t ~ - po l lu t ion process es cp9osed t o 41 kg previcusly.

( f ) Investment requirement and x n i t produckion c o s t s - -

Investment neccsszqr t o put the low po l lu t ion process i n t o s5rvice: 5,50C,OOO francs.

Diverse add i t iona l expenses for the low po l lu t ion technique p r t o n of asbestos-cement. 2.63 francs.

None. . - .

. . . _ _ _ _ _ . _ , .~ , _. . .-. . r , . , ___ . .~ . ..... " . -- . .. _. - . . .

. . . - .. . -. .

. .

. .

32. Recovery and recycl ing or" s e lven t s from vamurs o r i q i n a t i n g from miminrS

y m o n o graph GTVj!iP. 215/A&3.32 .d naintin:J; of alxninrum foils

1.

2.

3 .

4.

5 .

6 .

'9.

I1TDUsm.Y

3819 - Nanufzctuzing of metal products , machines and n a t e r i a l .

C O'lTVEliiTIOlIAL TECHiVOLCCFf

Priming and lacquering aluminium f o i l . discharge of solvent v a p u r s e i n t o the atmospnere.

Hot a i r drying o f lacquer ,

Priming and lacquering aluainium f o i l . Recovery of vapour with ac t iva t ed carbon. co l l ec t ed , d i s t i l l a t i o n a d recycl ing.

Hot air drying of lacquer. Eecovenj of solvents

STAGE OF DEVXLOTNEJT OF L/WT

I n d u s t r i a l development.

RE PORT DTG ORGMTIZATIO?I

MinistBre de 1'Enviromement e t du Cadre de Vie Di rec t ion de l a Prevention des Po l lu t ions 14, Boulevard du GQn6rz.l Leclerc

~ -- 92521 Beuilly-sur-Se i n s Cedex, France - -

DATE OF REPORT

August 1980.

PROCESS DESCRIPTIOX OF L / W ~ T A ~ D LDEDTTLFICATIC)N OF DIFFEFEETCES C O ~ " TO CONVENTIOi?AL TECHITCLOGY

(a) Processing s t e p s

I n the low po l lu t ion technique the solvent vapours emitted during the hot a i r drying of the lacquer a re recovered with ac t iva t ed carbon.

The ac t iva t ed carbon, i n a second o p r a t i o n , i s steam cleaned. The solvent vapour a d water vapour mix i s sen t i n t o a d i s t i l l i n g

obtained are recycled t o the workroom where the lacquer i s prepared. I n the standard process the solvent vapours from the drying of the l acque r are discharged d i r e c t l y i n t o the atmosphere without t reatment .

- column af ter condensation. Af t e r condensation, the solvents

%nergy nee2s a re irlcreased by 1j.j GJ Fer tm o f s c lven t ilsec? i n o rde r t o produce the mgour necess2ry fcr cleaning the actiTJated czrbon m d the d i s t i l l a t i a n 3f che recovered so lz t ion .

- -_ ._ -

( c ) Forrn and !x€ resi$l:als gemrntct? I -

Ths waste prcduced i s x,ade up of ketonic m d e t h y l i c solvenr, vapours.

With the low p c l l u t i o n tecl-xiqus, 30 kg s$--s~l.vent v a p u r s LE ’

released. i n t o the a tmsphere F s r tcn 01 solvent used. Vith the standard technique the quan t i ty of t h i s waste re leas& i s 73@ ;q.

Fol lu t ion con t ro l neasures required f c r cgnpliance with e x i s t i n g s tzndards . - . .-

.

(d)

30 add i t iona l x i t i - p o l l x t i s n neasures are required tcj reduce r e s idua l po l lu t ion s ince i t i s v e r y lo:,.

F o r 3 and amount o f r.!ast<? discnarge t o the envi ronmnt . .

(9)

The wastes discharged i n t o the envircnment equal the wastes produced s ince t h s r e i s no add i t iona l treatment. .

( f ) Investment requirement and mit ?production c a s t s ._ _.

The necessary investnent for the i n s t a l l a t i o n of the low po1luti.cn process vas 3.G5 n i l l i o n francs, i n 197.3 ?rm,cs.

-- ,Production c o s t s pe.r ton 02 .solvznt used have d r o p p d from 7,096 francs t o 6,969 francs i f one includes c a l c u l a t i o n s for the solvents recovered, without tdcing i n to account amort izat ion o f the investment (l9SC f r a n c s ) ,

This i s . t h e f i r s t i n d u s t r i a l app l i ca t ion of the recovery of ketonic solvent vapours, general ly considered as a d i f f i c u l t procedure. A s the technical r e s u l t s were pos i t i ve 2.s f a r as the reduct ion o f po l lu t ion i s concerned and the economic r e s u l t s shculd be sa . t isfactory given the expected increase i n the p r i c e s of p t r o l e u m based solvents , the use 03 t h i s process should be extended t o a c t i v i t i e s enploying the sane t y p s of products .

43. Dry-Dhase n e c t r a l i e a t i o n of a l k y l a t e s g3n5rated ir! the production o f s";em (Swnolary o f nonogrzph E.W/%P .2/5/Add.33)

1,

2.

3.

4.

5 .

6.

7.

INDUSTRY

35ao - Chsmical industry and manufacturipg o f ahenical products, pe troleuiii ana coal de r iva t ives and F l a s t i c an5 rubber Froducts.

CO"?ION-4L 'ECETOLOGY

V e t n e u t r a l i z a t i o n of the a l k y l a t e s resu l t i rg from ths m s n u f a c t w i r ? of e thylbenzeEe . LO\<!- AID XON-'dASTE '23 CBJOLOGY

Dry n e u t r a l i z a t i o n of the a l k y l a t e s r e s u l t i r g from the manufacturing o f e thylbenzene

STAG OF DZVELOPT~NT OF L/JWT

P i l o t stage

REPORTING ORGAIiIZATIOX

Ministkre de 1'Environnerent e t du Cadre de Vie D i r e c t i o n de l a Pre'vention des PoElLztions 14, Boulevard du GQn6ral Leclerc 92521 Neuilly-sur-Seine Cedsx, France

I

DATE OF RETORT

Augus t 1980.

PROCESS DESCRIPTION OF L/WT AM) IDDZEUTIFICATION OF D ~ R E N C E S CCTPP~TD - TO CONVENTIO!SAL TZCHl\iOLOGY

(a) Processi,ag s t e p s

I n the low p o l l u t i o n technique, the e l i m i n a t i o n of the sal-ts and impur i t i e s of the s o l u t i o n o f e thylbemene obtained by a n ethylene r e a c t i o n on the benzene is c a r r i e d out without water.

The s o l u t i o n is neu t r a l i zed i n a m o n i a , then f locu la t ed a d decafitad, The sediment is centr i fuged and vacuum dried. obtained can be used t o manufacture mixed f e r t i l i z e r s ,

The s o l i d r e s idue

I n the standard technique, a f t e r ammonia n e u t r a l i z a t i o n , the s o l u t i o n i s washed i n water, then soda, and water again. and s t r ipped while r e s idue , waste gas and water a r e discharged i n t o the environment.

Wastes a r e f l o c u l a t e d

; -/

i

( b ) Matasials and energy r e q u i r m s n t s _ _ _ _ - - - -- .-.. - - - _ ... - _ _ _t__.__p._ . - ...... - . . .. .

The low p o l l u t i o n technique does not r o c u i r e -dater (as opposed t o the standard technigile :

T.he mount o f o thz r rim' rcater ia ls used i s i d e n t i c a l (0.27 t of e thylene, 0.745 t of be,nzane, 7 kg o f c a t a l y s t s , 3.5 kg of a m o n i a per ton of etkylbenzei%). The outpat shecld, however, be iaproved by 1 t o 2 pe r cer?t i n the lorr p o l l u t i o n process.

DifTerences i n energy meds a r e not y e t ava i l ab le .

Form and anount o f r e s i d u a l s senerated

1.5~13 p r t on or" e t h y l b e m ~ m ) - . - _

( c ) .._ .-

The lo...~ p o l l u t i o n technique does not prodice wastes, as s o l i d r e s iduss a r e used i n q t h e r aFp l i ca t ions ( f e r t i l i z e r manufacturing). 'rl&t$s produccd i n the staEdard technique a r e salts (ammonium and aluninium chlor ide ) , alaminium hydroxide, hydro-cabons dissolved i n water.

P o l l u t i o n con t ro l measures required for corcpliance with e x i s t i n g standards

~ . - .- -"

(a)

IJO a n t i p o l l u t i o n rCeasures are cecessary (ne vastes).

(e)' Form and mount o f waste discharge t o the environment 4

No wastes a r e discharged i n t o the envi roment .

( f ) Investment- requirements and u n i t production c o s t s _. -

Measures taken i n the low p o l l u t i o n process of waste n e u t r a l i z a t i o n m o u n t t o 5.25 m i l l i o n Francs (1979), whereas the cost o f a physicochemical treatment s t a t i o n i s estimated a t 4 m i l l i o n Francs (1976)

. . . .. - - .. . .. ..-

Production c o s t s a r e not y e t ava i l ab le ( recent process) .

8 , OTHER SIGNIFICAI\IT ASPECTS OF L f W T

This low p o l l u t i o n technique 'can be extended to o the r production processes u s i n g acid c a t a l y s t s .

34* HydroKen waship? by notassiim carbonate i n amnonia croduct ion (Sunnary of monograph 3€lV/!:rP.2/~/Add.3d)

1.

2.

3.

4.

5 -

6 .

7.

IXDUSTRY

3511.- Chemical i ndus t ry and manufacturirg of chemical products, petroleum and coa l d e r i v a t i v e s and p l a s t i c and r u b b e r products.

C 0 ~ " T I O I J A L TECH?IOLGGY

Washirg of hydrogen i n amonium carbonate t o e l h i z t e carbon dioxide and to^ o b t a i n hydrogen of adequate p u r i t y f o r arimonia synthesis .

LObI- AID XOiWdA.Sm E.? CEXOLOGY

Washing of hydrogen i n potassium carbonate t o e l i n i n a t e the carbon dioxide contained i n hydrogen.

STAGE OF DEVZLOPTBNT OF L/WT

I n d u s t r i a l development.

FEPOETING ORGAETIZATIO!i

Ministgre d5 1YEnvironnemect e t du Cadre de Vie i a i r ec t ion de l a PrGvention des Po l iu t ions 14, Boulevard du GQne'ral Leclerc 92521 Neuilly-sur-Seine Cedex, France

DATE OF REPORT

A u g u s t 1980.

PR3CZSS DESCRIPTION OF L/WT AND IDENTIFICATION OF DIFFZRENCES COIQARED TO COhmPliTIOlTAL TECENOLOGY

,

(a ) Processing s t e p s

I n the low p o l l u t i o n technique, the cracked hydrogen containing 29 t o 22 p e r cent o f carbon dioxide i s washed i n a s o l u t i o n of potassium carbonate. The s o l u t i o n con ta in i rg carbon dioxide is heated i n a n exchanger where the input cracked gas y i e l d s heat.

Then it i s t r e a t e d i n a column containing n i t rogen and i t i s regenerated. Wastes a r e made of carbon dioxide and nitrogen.

In the standard technique, the cracked gas i s washed i n pressurized water, then i n ammonium carbonate. The s o l u t i o n of carbonate i s r e s t o r e d by steam heat ipg and carbon dioxide is discharged but i t i s accompanied with ammonia which i s a source of po l lu t ion .

( b ) H a t e r i a l s and eniFgy requirsmcnts

The low pol l j t i .cn techniquz reqtl ires; besi8es cracked gas; n i t rogen , vhich can 'ne r,rmi.?,ed by c t h i r un i t s of %'3- y lan t .

I n t'm standard tschnique, a m o n i a i s nscessary to c,orcpensate f o r losses alzd to r e c o n s t i t u t e amonim c a r b o x t e (3 k g / t of ammonia produced).

0.C3 and 1 .24 GJ of en=.rgy y e r t on a r e raquired r e spec t ive ly .

Form zn4 amcunt o f r e s i d u a i s , rsrsrzted

The ;qastas prodace3 by th-. low pollutior? process and i n - t h e u n i t as a whole (washicg acd m o n i a syn thes i s ) contain 0.03 kg *of ammocia i n s o l u t i o n pe r ton of a m o n i s produced.

In the standard technique: 0.03 kg of gaseous a m o n i s .

To l lu t ion control measures required for cool.plisnce w i t h e x i s t i n g standards -

The a n t i p o l l u t i o c z?s;?suros required by th s stan6ard t e c h i q u e c o n s i s t i n e i i n i n a t i n g azu?.onia from the discharges by usirg a t reatmezt s t a t i o n which would prodme aimnoniun sulphate . I n the low p o l l u t i o n technique, no neasuros a r e necessary.

Form and amount of waste discharge to th? envirornent -

The wastes discharged i n t o the enrcrironnient have the following c h a r a c t e r i s t i c s pe r t o n of a m o n i a produced:

( c )

3.3 kg of m o n i a i n s o l u t i o n and ,

(d)

(e )

_- S tanaard Low po-lfutlon'--- ___ - . - . .__." ~ - ... __.. -- "- -

t e chniqus technique

Water: Equitox 10 eq * 490 eq hmonia 0.03 kg 3.3 -4g

Air : . h o nia 0 0.03 kg

Investment requirements and mit production cos t

Investment for the low p o l l u t i o n technique: Froduction cos t p e r t on o f armonia:

(f)

16 n i l l i o n francs (1979). 4.5 francs,

A t r e a h i e n t s t a t i o n would have cos t 2,640,000 f r a m s . ir, t h s s k ? d a r d technique, the production cos t p e r t on of a m o n i a i s 22.5 F. The treatment s t a t i o n would have r e s u l t e d i n a n a d d i t i o n a l cos t of: 7 f r ancs , conpensated by the s a l e s of amnonium sulphate (3.5 f r a n c s ) ,

OTEfEB SIGNIFICANT I-SECTfj Ok L/Y;F!?

The low p o l l u t i o n technique allows s u b s t a n t i a l energy savipg through steam saving. The low pollution- process i s perfected and i s used i n s e v e r a l u n i t s ; i t can be extended t o all .a"onia syn thes i s un i t s .

. 3 5 . EechanicaE oetl ir!! o f v s c e t a b l a s / f r u i t s

(SuTsary of monograph E?W/"'P .2/5/iidd.35)

1 I.

2.

3 .

4.

5.

6 .

7 -

INDijST2iY

3113 - Manufacturing of foods tu f f s , dr inks and tobacco.

P e e l i r e of vegetables through a chemicomechanical process before conservation.

LOV- aLm ~ T O U - W A S ~ m CEINOLOGY

Pee l ing of vegetables through a mechanical process before conservation.

STACE OF DWSL~PPEJTP QF L/N~JT

I n d u s t r i a l development.

REPORT IXG ORGAXIZAT I O N

Ministgre de 1'Enviromement e t du Cadre de Vie Di rec t ion de l a Prdvention des Po l lu t ions 14, Boulevard du GBnBral Leclerc 92521 Heuilly-sur-Seine Cedex, France

DATE OF m?ORT

A u g u s t 1980

PROCESS DZSCRIPTIO8T OF L / W MID IDENTIFICAT13N OF DIFZTmNCES COMPARED TO COI~VEXTIONAL TECHNOLOGY

(a) Processing s t e p s

I n the standard technique, the washed tubers a r e peeled i n a peeling-machine composed o f abrasive r o l l s , wi th water. The waste water containing peel ings i s f i l t e r e d and re-ryc&d a t the p e e l i r g s tage: the f i l t e r contains only peel ipgs o f l e s s than 5 mm and i t i s p e r i o d i c a l l y cleaned. Peel ings r e t a i n e d by f i l t e r a r e sen t f o r dumping.

Then tub3rs a r e t inned.

I n the standard technique, the washed tubers are dipped i n t o a soda so lu t ion , then peeled and dipped i n t o a c i t r i c a c i d s o l u t i o n f o r

. neu t ra l i za tior,,

Waste water contains soda, c i t r i c a c i d and peelings.

...

X a t e r i a l s and e n e r g requirements -_ * - -- .- - . - . . . -- -. . .

Fora a$ amourt of r e s i d u s i s generated

The wastes.pr3dacz.l 33- the l o i i pol1uti.cn technique a r e made of tuber trastes and a c i d n i t r i c : which a r e contained ic the water discharged, Peelxngs rntained by the f i l t a r a r e s e n t f o r duwing .

For each ton of tubers t r e a t e d , 5 E? of wastes are produced, which contain 1 5 kg of tubi?r wastas and 1 PG of c i t r i c a c i d ; p e e l i r g s a r e s e n t for d m p i r g .

IT? the standarci t e c h n i q w , wastes amount t o 25 m 3 , contairdng 170 kg o f p e e i i r g s , 5 kg o f soda, an6 6 kg of c i t r i c acid.

P o l l n t i o n con t ro l irieasures required f D r compliance wi th ~ e x i s t i r g standards

No a d d i t i o n a l a n t i p o l l u t i o n measures a r e necessary t o meet e x i s t i r q requirements.

Form and amount of waste discharge t o the environuent -

The wastes discharged i n t o tke environment a r e ider i t rcal t o those Froduced during manufactwirg.

Investment requiremsnts and u n i t production c o s t s

In 1979, th2 low p l l u t i o n techr-ique r equ i r ed a n i n v e s b t n t of 280,000 francs (as opposed t o 50,000 f r a n c s f o r the s tandard technique ) . Variable e q e n s e s pe r ton of products t r e a t e d anount t o 160 F/ t i n the low p o l l u t i o n technique a g a i n s t t e chnique .

. -

170 kg of

- - . - .- - I .-

F/t i n t h s s tandard

8 . OTHER SIGhTIFICkhT ASPECTS OF L/Ni:i"

Apart from p o l l u t i o n reduct ion, the low p o l l u t i o n technique ensures a n improved output and a higher q u a l i t y of products.

The technique usirg the.4escr ibed equipment can be extended only t o f r u i t o r ' vege tab le s which ar+ compact ar,d s o l i d .

a.

2 .

3.

4.

5.

6 ,

7.

IHDUSTRY

3819 - Mamfaztur i rg of mzta l ob jec t s , machines a d material..

C O m ? T I n u L T5CEXCLXY

P i c k l i r a of d ie c a s t p a r t s of brass i n n i t r i c a c i d .

LOV- AlaD NONJdASTE 'IT Ci?3?OLOGY

Descaling o f d i e cas t p a r t s of brass by vibra t ion .

STAGE OF D3VTLOPi%W OF L/IWT

I n d u s t r i a l d a v e l o p e n t . REPORTING 0RGAI.IIZBT IC??

Ministkre de 1'Errrironnement e t du Cadre de Vie D i r e c t i o n de l a Pre'vestion des P o l l u t i o n s 14, boulevard du GQneral Leclerc 92521 Neui l ly-surSeine Cedex, France .

PROCESS DESCRIPTION OF L/NF?I! A D D E N T I F I G A T I O N OF DIFFEXENCES COPPARED TO COHVESTIOITAL TECIilVOLOGY

Processing s t eps

I n the low p o l l u t i o n technique, the brass p a r t s t o be t r e a t e d are f i rs t placed ir, a v i b r a t i o n apparatus with abrasive glass marbles and s l i g h t l y a c i d addi t ive . i n a second apparatus for e tch ing with s t e e l b a l l s and bas ic add i tk i e , then they a r e dr ied .

In the standard technique, the p a r t s are dipped i n t o n i t r i c ac id , r i n sed , dipped again into ac id , r insed again and dried.

After r insiri i , the .par ts a r e placed

Mate r i a l s and energy requirements

The l o w p o l l u t i o n process requi res reagents (10 kg per ton of p a r t s ) and water ( 2 m 3 / t ) whereas the standard technique r e q u i r e s 250 kg of n i t r i c a c i d and 40 m 3 of water pe r ton of p a r t s t r ea t ed .

The low p o l l u t i o n process requires . 0.43 G J o f e l e c t r i c i t y , as opposed to 0.25 G J f o r the standard technique.

1

The wastss Froduced by ths low F o l l u t i o n p o c s s s a r e made of used E Ltks of acid r eagen t s , y,-!:ich ar? s e c t f o r 2 2 t c x i f i c a t i o n ; the' r i n s e water xhi:k is x i x 3 with 5k.e bafhs of basic reagnnts: tt.e miut;crs i s then stored. f o r pf-T con t ro l , i ' i ltereci t o e l b i n a t e hpaxry p a r t i c l e s an3 s c n t back i n t o ths c i r c u i t .

IC the standard technique, trastes cons i e t .>c w?d baths of n i t r i c a c i d containing copper an3 z i a c , r i n s e water, and n i t r i c vapour which i s discharged i n t o the atmosyhere.

(a) Pollclt ion con t ro l mtasmes re2uired f o r conpliance with e x i s t i x standards

The low p o l l u t i o n process does not r equ i r e a n t i p o l l u t i o n meastires , whereas the standard techrique makes i t necessary t o yrovide f o r d e t o x i f i c a t i o n of nitric t;r;ths, soda n e u t r a l i z a t i o n of a t r i c vapour, and treatment of r i n s e water.

-

. _ . -

( e ) Fom and mount of waste d i s c h a g s t o the environment

The wastes discharged i n t o the e w i r o r n e n t hzve the f o l l o w b g c h a r a c t e r i s t i c s , p e r t o n of p a r t s t r e a t e d :

S t m d a r d Low p o l l u t i o n technique te chnio ue

Outflow I J i t r i c ac id High content Mone

8 kg 0.@75 kg WATER I Copper _ - . ( z inc (Ikeak a c i d (reagent)

5.5 Kb7 ~

No ne

AIR X i t r i c vapour 50 t o 40 p e r . c e r t - ~ None of the n i t r i c a c i d used

(f) Investment requirements and u n i t production cos t s

The necessary investment amounted to 265,000 f r ancs i n 1979 f o r the low p o l l u t i o n process , as opposed t o 516,000 f r ancs f o r the s tandard technique ( cos t of the- treatment s t a t i o n ) .

5. OTHER SIGNIFICANT ASPZCTS OF L/Yfl

'I

!

A s opposed t o thc? s tancard technique, the low p o l l u t i o n process does noT tend t o e l imina te surface d e f e c t s , which demands more careful machining.

The aspec t of t he p r t s may g i v e r i s e t o sone reluctance and check f u r t h e r development of th is process which is, however, economically and environmentally ve ry a t t r a c t i v e .

7 I.

2.

39

4.

5 .

r 6.

7.

Inclustr ia l d e v e l o p E " .

I l i n i s t e r s iik 1'Envirornement e t du Ca&rs ds Vie D i r e c t i o n d.5 l a Prbveztion des P o l l c t i o n s 14, 3oulsvard OU &r,Sral Leclsrc 92521 Xeuillg-sur-Seine Cede-, Frmse

BCCESS DESCBIPTION OF L / W T AT,?) DENTIFICBTION OF DIFFE;IEI\ICES C O I P - ! TO COlTVEETTI3ItAL TESZlOOLOCY

(a) P rocess i r e s t eps

In the 10t.r p o l l u t i o n technique, the water necessary for maiufacturing c i r c u l a t e s i n a closed c i r c u i t snci the f l u i d lased t o trm-sFOrt the f i b r e s i s i t s e l f thrt f i n a l effluent. exac t ly equal t o the mount t h a t evaporates dur ing mandac tu r ing i s i n t r d u c e d i n t o the closed c i r c u i t . technique water taken f r o n E r i v e r i s used f o r t r a n s p o r t i w the f i b r e s ; i t is then separatsd for the most p a r t during the d i f f e r e n t s tages of nanufacturing m.3 i s discharged, fall. of f i b r e s soluble wood cmpouniis (resins and sugars) i n t o the r i v e r .

Wi;T a quant i ty of ?.rater

01?1 the ccntraz'y, i n the standard

(b ) Mate r i a l s w-3 energy requirements

I n the low p o l l u t i s n technique, the consmpt ion of m a t e r i a l s is considerably reduced: pane l s nanufacturerf, as ogposed t o 30,rJoo l i t r e s ir, the standard technique, and 1 ton of wood i s required, a8 opposed t o 1.06 tons i n the standard technique.

Energy 90 x 10 joules .

130 l i f r e s of water a r e required p e r ton of

1'

onsmpt ion i n the low 3 o l l u t i o n technique i s over 8

( e ) ? o r 2 a4 9:;1;7wt 02 uasze dischzrge t o tk,e environment

The waste disshZrge3. i s iden t i ca l t o the waste produced.

( f ) Investment requirezents acd unit p r d z c t i o n c o s t s

me 1cv Fol lu t i cn tes-b,ir,ue recrj;ir?d e-2.5 mil l ign f r m c (1% fraixs) investDent, whereas a stmdard t r e a t ” so lu t ion applied t o tin2 i n i t i a l ..;anilfsc.t7ning proc5ss would have required a 5 n i l l i o n f r a n c (1958 frmcs) i n v e s b e n t .

3- SIGIXE’ICABT ASPZCTS GF L/X!K!

Tne loti pollutior, technique is more e f f i c i e n t tnzn a s t a d z r d t r e s t m n t solution an5 F e r n i t s i? g-reater technical adap tab i l i t y i n nanufsc twing , given the p o s s i b i l i t y of uti l izir ,- toxic products.

8 .

i

- - _._ . . , .- . - .. .. . _I .

, r r ;300 - C h m i c s l inclcstry pe t ro l e -m m 3 coa l d e r i v a t i v e s an3 p l a s t i c a d rubber p r d u c t s .

maz-af.-ct-nin; of chen ic s l pr3ductss,

2. CO!TVEIJTIO?T_o_L TEC3lTOLOG-f

P ick l ing of ABS p l a s t i c n a t t e r ir, a sulfochrorxic sol-tion.

4.

Pick l ing of ABS plast ic : m a k t e r i n a suifochroclic so lu t ion with r e s t o r h t i o n and recycling of the solct ion.

I n d u s t r i a l devalopncnt.

I? inis t&re dc I'EnvironneEent e t 31; Cacire de Vie D i rec t ion de l a Prdventior, d e s Pol l i i t ions 14, I3oulevar6 du Gne'rsl Leclers 92521 N e u i l l y - s w 9 e i n c Cedex, France

6.

A u g u s t 1986.

(a) Processing s t e p s

The p i c k l i n g o p e r a t i o n ~ i t s e l f i s i d e n t i c a l : 2 bzsket c o n t a i n k g the p l a s t i c p a r t s i s diFped i n t o a ba th of concentrated sulfuric a c i d and chromic a c i d t h a t ensures descaling.

Whereas i n the s t a n d a d technique the bath i s sen t , t o a d e t o x i f i c a t i o n s t a t i o n when i t i s used, t h a t i s t o sax when the Cr3+ i o n concentrat ion reaches 50 g/l , i n the low p o l l u t i o n process the ba th i s r e s t c r e d by e l e c t r o d i a l y s i s 2nd recycled i n order t o x a i n t s i n the Cr3+ concentrat ion a t between 20 g and 30 g/l , Tne ba th i s only sen t t o the d e t o x i f i c a t i o n s t a t i o n once a year.

(b) Platerials 2nd energy requirements

1 Tfie r e s t o r a t i o n of t he ba th a l l D w s a r educ t ion of s u l f u r i c ac id c @ n s m g t i o n from 12.5 kg/100 n2 descaled t o 3.3 kg. znd the consumption of chroEic acid from 13 kg/100 m2 desczled t o 3.5 kg.

66 PIJ of energy a r e necessary per 100 m2 descaled f o r e l e c t r o d i a l y s i s .

Since the nuxber o f t i n e s ti?? ba ths are sznt t o the de tox i f i ca t ion cent= i s reduced by 4, t h e risks of accidental noll-Jtion are reduced by as nuzh.

7

3121 - Food indus t ry ,

2, CONVENTIOITf i ECXY9LOGY

1 Ex t r ac t ion of po ta to skzrch without recovery of p r o t e i n s i n the i n t e n d vegetat ion water.

3. Low- -!a NOTJ-WASm EcmTi3Lcc-Y

Ex t rac t ion of po ta to s t a r c h witin r e c o v e n and v a l o r i z a t i o n of p r o t e i n s i n the i n t e r n a l veget2.tion water.

4. STAGE 'OF DEVELOP~ET OF L/TWT i f

I n d u s t r i a l development.

i 5. 3 E P O R T I I J G O R G ~ ~ I ~ ~ ! l I Q ~ ~

~ ? i

FEnistkre de IfEnvironnenent e t du C d r e 6e Vie Di rec t ion de l a M v e n t i o n des P o l l u t i o n s 14, Boulevard du S n 6 r a l Laclesz 92521 Ne-dl ly-su-Seine Cadex, Frm.ce

'\

6 . DATE OF FEPORT

'7. PROCESS DESCRIPTION IIF L/NWT BID mEETTUFICBTIOW OF I)"BCES C O M € " TO COISVENTIIIIJAL TECBJOLOGY

(a) Processing s t s p s

Coagulation followed by cen t r i fuga t ion of t i e proteir ,s contained i n the i n t e r n a l vegetat ion water p e m i t s them t o be sepsrated from the water whereas with thf- standard techniqze the vegetat ion water, s t i l l fa1 of p r o t e i n s , vas discharged i n t o the r i v e r d t e r having been s tored f o r i? month.

(b) E a t e r i a l s and energy requirements

Mater ia l needs a r e i d e n t i c z l i n both processes: and 14.5 m3 of water gel- ton o f po ta to starch.

5 tons of po ta toes

The l o i ~ p o l l u t i o n process r e q u i r e s 0.80 G J of e l e c t r i c i t y and 1.25 GJ stean power, compared t o 0.30 G J and 0.17 GJ f o r the standard proce ss.

Although t h i s techriique i s slrez<y o?e ra t iomi i t m y s t i l i maergo imorovenents tl-,at :.4E pcrz i t m i nc rezse i n th s eff ic izncy of t hc resavery znd va lo r i z r t i on of the prodac t e recoacrsd.

. . , . .---. .. .. . . ...- -... . . . _". ...- . . . - .

" i / 3 6 ,

page 36

49 *

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F J "

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7.

LO+-- &XI rJOiJ-VAST ZCHXOLOGY

Froicstion. of a.cznonixl n i t r z t e with 2 i r e c t v e r i f i c a t i o n o f the r e a c t i o n 2nd- deSu5blin.g o f the water va?om ext rac ted . 4 n-

E i a i s t ~ r e de 1fEnviromement et; c?u Cadre de Vie 9 i r e c t i o n de 12 PrGventior, des Tol lu t ions 14, Boulevzrd d a C4nGral Leclerc 92521 Ne-&.lly-slx-Seine Cedex, Frqmce

(a) Processing s t e p s

li~ the low p s l l u t i o n technique, the v 3 r i f i c a t i o n of tht- r eac t ion of the two basic a lenan t s (concentrated n i t r i c ac id an& w c n i a ) i s carriec? out through the in t emed i - of the pH v l a l y s i s of the r e s idua l water co l l ec t ed a t the end of the process , tkLs water h a v i w or ig ina l l j - been containad in the n i t r i c ac id and obtained by evaporation of the amnonitin n i t r a t e so lu t ion followed. by condensation.

L?. the lcl t r p o l l u t i o n tachnique, the aimoniQrC n i t r a t e l d e n wstcr V W o U : a

pesses through a de'cubb1t.r before condensation which l i ? i t s the n i t r a t e bubbles ca r r i ed by tha vapour.

\

.

,

Additionzl r e c e i p t s Gue t o 2 2 increase i n t!?.e c w t i t y of n i t r a t 2 orcduced or" 1.7 p e r cent ecyiz1 8C0,OOC f r v l c a p e r yczr (1980 f runcs ) . *

This technique' a110 :~~ c l o s e r v e r i f i c a t i o n of tl-s c k m i c a l r e a c t i o n s t h s t take place dar ing prodcction and t hx gives a b e t t e r n a t e r i a l y i e l d and l e s s pollrrt ion. the chernical s ec to r ,

Tnis p r i n c i p l e shculd be extended t a o ther procedures ir.

\

41. Deuineral izat ion oi beet, , juice v i t h re -use ci" e l u a t e s .

(Sulinnar?. of nonograiph EFJbJP,2/5/Add ,41)

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2.

31

4.

5 *

6 .

7 .

C O E m * T IC iUL m CETCLXX

Demineralization of beet juice with discharge of e l u t e s .

La%'-- BRri) 1~01?4lkST?2 '?ECEmJOi;Y

D e a b e r a l i z a t i o n of beet j u i ce with va lor iza t ion of e l u a t e s

I n d u s t r i a l . developnent . mPORTDX ORGMIZA'7IOB

PUistb:e de 1'Environnexent e t du Cadre de Vie Direction de l a Pr6vention des Pollutions 14 Boulevard du 68nkrel Leclerc 92521 Ncdilly-sar-Seine Cedex, France

DATE OF i i i 0 R T

Augris t 1980.

r rocess ing s teTs

The demineralization e32ates are separated from the o t h e r e f f l u e n t s . are Concentrated by evaporation and then c r y s t a l l i z e d Centrifugation permits the separation of salts t h a t a r e marketed as f e r t i l i z e r and the Iilother l i p o r , rich i n proteins , t h a t is riarketed f o r a im1 feed.

After having been hordogenized, these e lua t e s

Conversely, in the standard technique, the e f f luen t s used i n the recovery of the resins are n ixed v i t h o ther water , sent t o a holding pool an& then discharged i n t o the environment.

H a t e r i a l s and energy requirements

The non-polluting technique requi res the s m e smount of salt as the standard technique (16 kg per ton of deaineral ized b e e t s ) ,

On the other hand i t requi res l e s s \rater because of the condensation of evaporated water and i t s recycl ing (0.375 n3 agains t 0.850). more energy (520 EIJ as opposed t o 9 NJ).

Zovever, i t consumes a g r e a t d e a l

‘ .

c., .

! E q m V / 3 6 cage 41

( 2 ) I n v e s t m n t req-i:rmmts mi^ ~ i n ~ t proi!xction cost:

The ceccssary b v c s t n e n t f e r the non-polluting technique is ’3,OOO,GOO f r m c s (1-973 f r a n c s ) as oppose2 t o 7,500,000 f r m c s f o r the si;aiidard tec’hiiqcie i f a stmrlard m d e l SioloGical treatnent s t a t io r , i s erqioyed. expenses per ton of dcninsraLized beets f o r the non-polluting teclinique m d f o r the treatment s t a t i o n , but the c o s t of the g o r , - ~ o l h t i r r g - p ~ c c y ~ is ccz,iier?satad 23: 32. .~ mdCetiqg c2 “112 az-L~l-Fze3 cl:;z~as, tile recdi?tc Tor v k ~ c . ar? 6.5 f r a s - : ~ : T T k-n of ~ e ~ z ~ z z a 7 - i z e d 3e3t-3.

There are 12 franc;; d iverse

!

..... .- . . . . _ . . . -. . . .

. . . . . . - . . . . . . .

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1.

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-. 3 .

4.

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7 .

1120; a p i c u 1 hi znl was t e . 9200 - Treatment of s o l i d c i t y iiaste a n d . f o r e s t a 1 znd

The cocventional processes are only aypl iccble i n the p r i o r process phase, but n c t i n t h e s to red f u e l production phese; Y i i s is a c o q l e t e l y nerr technology and. consecyently t h e r e i s no cocvent ional techwlogy e x i s t b g i n t h i s l a t t e r aspect .

?XI - QR UCX-lJliS'IT TXWWLOGY

Production of vegetdole fuel bio-transforEed fr3a solid c i t y residTJals and f o r e s t a l and a g r i c u l t u r a l vas t e

ajn SORIA ( S p i n ) t he re i s a model i n s t e l l a t i o n (PIBZDA Fzctory) with az m n u z l gro&.,Iction of 6,000 ut/year of conhust ible b r i q u e t s , t h a t has been punning for 10 years .

The Conrpany Sociedad Combustible Vegetables Biotransformdos S.A. (COFWESA) has programed the i n s t a l l a t i o n of a series of p l a n t s i n Spain and vc~1-ious E u r o p e a coun t r i e s , the first of which w i l l be i n s t a l l e d i n S S T ~ ~ L G O TIE C 0 I ~ O S Z I . A (Spain) rri th capac i ty , i n t h e iirst phase, f o r 20,000 nt /year of co rhus t ib l e products.

Tlie process is f u l l y consol idated in t r e a t n e n t of f o r e s t a l , agx-icL i t u r a l and c i t y vas t e . Tlie process i s i i3 t 5e stzl;e of research and developnent t o treat the sludge froci the waste weter p u r i f i c a t i o n process.

July 1yGO.

( z ) Processing s t e p s

"lie ratr nateriols , f o r e s t a l and a p i c u l t u r a l vas t e (branches, l eaves , t runks, s trw, 3 t a l k s , e t c . ) and- s o l i d c i t y r e s i d u a l s a r e f i r s t sub jec t t o a process where the metal f r w t i o n , g l a s s and i n e r t n a t t e r i s separnted, then suitably chopped o r

c r d i e c t and 2x2 sub j e c t t o 3, con t ro l l ed aerobic f e r n e n t a t i m , based on choice fungus and. bac te r i a -cu lk res -9 .%hat z r c S a m a t c? prqor’u-ion of 5 ?e r c e n t , The necessary over- t .arnin~s a r e =de TO achie-la opsiniuii i e r o b i c c i s condi t ions u n t i l ;?

1. dinogeneous LZSS i s a’ctai.-ed.

This Q.SS i s then introciucec? i n t c t he d iges to r s 7,liiez-e i t is su3 ; jx t ed co an m s c r o b i c f ernen t e t i o n , T.rlrich c o n s t i t u t e s t he key ?base of the process, wi th nev anaerobic b a c t e r i r s tocks . m e v o r k prc;cess laats f o T aparoximztely one ireel: *

a d f e m e n t z t i o n i s kepi; con t ro l l ed at 2 t e q e r s t a r e of 1-5 t o 2 5 ~ .

After t h o soli? iit;s fro::i t h s d iges to r h s passed .through soccGssive s i z e x l $ c 5 i c z 2 x 5 grinding ghaaes OG t o the br iqi ie t mmf2,c:ture; addeti,, as thas:, aTe ?reduced i n the hac-teriz neta3olisn.

One icg of f u e l is obtained f o r e-rery 2*5 kg of rav rmterial t r e a t e d , trith a c a l o i i f i c ?mer of L: ,300 15.~~1. hunic?ity and a maxi.mr.1 5 Fer cent of asliss .

i t then goes n 3 binder products hcve to be

Tw3 per c e n t

(3) Naterials and energ7 reqyired

0.2 kWk per ton produced.

Fora and mount 02 residunls generated

Gx?q themetallLC i n e r t w t t e r and glass of the s o l i d c i t y trastc used m d t he ash f n n the corabustion of res idues produced i n s e l e c t i o n of . s i z e s , - . that are use4 i n - t h e product

( c )

.. - . - ~ final. -&rying%iIn. ~ . - -

i

.-

ECE/ENV/36 page 44

3. Low- and non-T;rzs ts t e c h o l o e s '

Anaerobic-aeroSic 5 i o l a g i c a l t reatnen t giving nethaae as a Sy-prodUct t o be used f o r thermal eaei-gr production.

4. STAGE OF DG'w?ZLOPl~EXT .OF L/Ii!!T

Thirteen full s c a l e p l a n t s i n operation o r under construct ion e

(z) "ocessing s t e p s

Organic waste \raters frolc the i n d w t r y are t r e a t e d with anaerobic microorganism Tor recovery or" methane. this way is then t r e a t e d wi th aerobic n i c roo rgmisns f o r achieving a very good e f f l u e n t quality.

The vater t r e a t e d i n

The a e r o b i c a l l y produced excess biosludge i s recycled t o t he anaerobic s t e p h e r e it i r : d iges t ed t o Iilethane.

The recovery of netinan2 i s about 300 l/kg COD treated.

(h) Materials and enerGy reqyired

Tl?e process w i l l consme on ly sl;lall amounts of e l e c t r i c a l energy f o r t he operation. About 0.15 Mlhlkg o r g m i c mterial t r e a t e d .

(e) Form and mount of vaste discharge t o the environment

"lie BOD reduction is wre thv l 99 p e r cei3t. 5

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E CE/X?lV/ 3 6 page 46

D r y barking has been c u t i n t o operntion a t more t'nm ten f a c i l i t i e s in t he TJSSR.

D r y "arlring yrovicles s i g n S i L a n t c o s t savings a 4 s t only because of t he exclxsion of t he treatment of ve t bark and bark containing .iiaste m t e r b u t als:, because of the higher ezergy content of t he dry bark. Bark-fired boilers c2-n provide up t o 20 p e r cen t of a f a c i l i t y ' s s tean requirements . In t'nose cases where the cpp l i ca t ion 0; dry barking is n o t desirzble, due t o a n e c e s s i t y t o obtain 2 very high degree of bark removal,

most of t he Sark (UT t o YG p e r cen t is removed by the d r ~ nethod baking ciln be performed i n izro

whereas the f i n a l ba rk in5 i s accomplished by v e t barking. co~iii,ined uethod r e s u l t s i n 2. s u b s t a n t i a l reduction of irater requirements comparecl t o convcn t i o n a l wet barking.

In such a combined nethod,

The

/'

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49

bt t h e vxi-ious stnzcs of potrole 'm r e l i n i n g , 2 nca'oei- of cmdefisates

t1icrw.l zi2d c r t a l x t i c crsckers ooking u n i t all con ta i s a liigil d e g r w 02 hydrosen sulphide and z z " l a . terqierahre ~ 2 6 - pressure and transformed i n t o thiosulphates d i i c h ?.re tken d i z c h a ~ ~ s i 2:ito t he c z n z s

. are ,'on.ieiL. The condens?.tes Ti-om the vacuuo d i s t i l b t i o n u n i t , the tke hydrocracker, and the clels-yed

rl'hesz condensztcz are ctib jectec! t o a oxidizet iog a t e levated

Sul$iide containing condensates are t r e e t e d by means of d i s t i l l a t i o n

ST:'SZ GF DZV-L9?i.EIiT OF Lhi!!E

5 . . rii=PGE?' ETC- G I G i G I Z 2 IQiT

The USSR S t a t e Cormittee f o r Science m d Techolo,T.

..

,

. - .

D i s t i l l a t i o n of sulp~ide-con'~aininC condensates .rakes i t poss ib l e t o p r d u c e h y d r o p n sulphide and arumnia 2s proGucts. The d i s t i l l a t i o n u n i t ~ l l o v s %he production of 35-37 p e r cen t g ~ s c o u s mon1.z and

Tlie e f f l u e n t f r o n t h e d i s t i l l a t i o n u n i t contains 50-100 ng/l of hydrogen sulphide and around 500 w/l 02 m"ia . anit o r disck.losseC. Lqto the sever.

p e r cen t h y h o p n su1phiG.e.

5''hi.c ireste ?rater iz ei%her xx& in %lie pre-treztmsct

...

1.

2 .

3.

4 -

59

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3530 - Petreleuin ;-ef i n i n g

CoT.nrcIkT IOI.TJ.5 "ZCETOIGGY

The d i i f i c u l t i e s e:icau:lterd i n t h e coriven ticnzl pmcess of hy6ro- desulphurizat lon a r e Ciuc t o t h e deposi t ion on the c a t a l y c t of t'ne hezvies t f r a c t i o n s of the feed s tocli (irith high metal concentration ) .

"PORT EG @RG?-iTIZl.-T IXT

The USSR S t a t e Corz i t t ee fsr Sciexce and. Technolo€V.

DATE OF TG?ORT

15 A v . p s t 1979

-- PR0CT:"S i)%SIFTIOPIT OF L/WT "D IDEiTT~ICBTIC1~- 'IF D m T T m S

The r e s idue i s de-asohalted wi t i i l i g h t gasol ine (v i rg in gasol ine vith init ial b o i l i n g ?oir,t 22-24O': mc? with end bc i l i% po in t 62-65°C) i n s tandard ex t r ac t ion c o l u m s a t a temperature of 14O-16OoC ?ad a d i l u t i o n r a t i o of 3.5-5/1. The content of ash i n the de-asphalted o i l (its y i e l d s f o r v ~ . c u u ~ re s idue is 85-75 p e r c e n t ) compared with the feed s tock vi11 be 2-4 times less and i ts carbon r e s idue about 1.5-2 tiaes less. The content 02 aspha l t ines is 93-95 p e r cen t less and the viLcd.';2 5C-7; cenc l a s s . The de-aspfialted o i l is hydrodesul$mrized i n tile f i x e d bed, In addi t ion 2-7 per c e n t of the feed is in the f a n of a nev product - ye t ro l eun a s p h z l t i t e - containing 60-CO p e r c e n t asThaltenes, 10-20 per cent of r e s i n and 10-20 p e r c e n t of oil. Softening p o i n t i s 140-180"C. I l l e a s y b l t i t e is easily pcnrriered and does n o t agglomerzte i n s torage. The product can be used f o r t h e r n o ~ l ~ ~ ~ r o i s o l a t i o n of heat lxibea and i n combiEatior, v i th vacuurs resiclue i t czn be used t o b r i q u e t t e c o a l f i n e s and t o produce bitumens of d i f f e r e n t trade marksr ?*.le t r e a t i n g very heavy p e t r o l m u rich i n E e t a l s , the pro&uct c m be b c i n e r n t e i ! i n a s p e c i a l b o i l e r p l a n t t o pro&uce v a n a d h a and n i c k e l .

-.&- CoI5?p D TO - -.--,-- COi" I"TC?@ ..F-%iLLS . _ . - - .

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