Transcription

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3 NTICE: Return r renew all Library Materials! The Minimum Fee tr eah Lst Bk is $ JUN? 7 1Q0Q The persn harging this material Is re^wisible fr its return t the library frm whih it was withdrawn n r befre the Latest Date stamped belw. T renew a1ite"pnfi»in!emet^sp8400 UNIVERSITY F ILLINIS LIBRARY AT URBANA-CHAMPAIGN L

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5 NFERENCE BM fngfneerfng LIBRAE UNIVERSITY F IlJ^ enter fr Advaned Cmpi UNIVERSITY F ILLINIS AT URBANA-CHAMPAIGN URBANA, ILLINIS THE AL FUTURE APPENDIX H Medium Btu Cal Gasifiatin

6 The persn harging this material is respnsible fr its return t the library frm whih it was withdrawn n r befre the Latest Date stamped belw. Theft, mutilatin, and underlining f bks are reasns fr disiplinary atin and may result in dismissal frm the University. UNIVERSITY F ILLINIS LIBRARY AT URBANA-CHAMPAIGN MAY 1 2 W MM *"*'» INTERUBRAKl APR 15 uj(u W81 L

7 Appendix H CAC Dument N. 163 Final Reprt The Cal Future: Enmi and Tehnlgial Analysis f Initiatives and Innvatins t Seure Fuel Supply Independene Mihael Rieber Center fr Advaned Cmputatin University f Illinis at Urbana-Champaign and Sha Lee S James Stukel Cllege f Engineering University f Illinis at Urbana-Champaign Advisr Jak Simn, Chief Illinis State Gelgial Survey Center fr Advaned Cmputatin University f Illinis at Urbana-Champaign Urbana, Illinis May 1975 This wrk was supprted by the Natinal Siene Fundatin (RANN), NSF Grant N. GI (A) 1.

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9 NGINEtKINti UBIWi Any pinins, findings, nlusins r remmendatins expressed in this publiatin are thse f the authr(s) and d nt neessarily reflet the views f the Natinal Siene Fundatin.

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11 THE AL FUTURE APPENDIX H Medium Btu Cal Gasifiatin Cntents: A Steam Press S. L. S fr Cal Gasifiatin M. Rieber Enmi Impat n the State f Illinis f the Medium Btu Cal Gasifiatin Demnstratin Faility at the University f Illinis at Urbana-Champaign S. L. S, M. Rieber, J. Stukel, et al A Prpsed Medium-Btu Cal Gasifiatin Demnstratin Plant fr the University f Illinis at Urbana-Champaign

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15 A STEAM PRCESS FR AL GASIFICATIN by S. L. S Prfessr f Mehanial Engineering University f Illinis at Urbana-Champaign

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17 , NARRATIVE* The bjetive f the prpsed researh prjet is t develp a medium Btu gasifier whih des nt require an xygen plant, d's i nt require any partiulate abatement devies t ahieve a lean prdut gas, prdues a prdut gas having a ntrllable 1L/C0 rati up t 95 perent H. (e.g., this rati an be adjusted fr immediate mthanatin) and des nt intrdue nitrgen int the gasifier. The purpse f the prpsed researh is t develp and arry ut «a test prgram t nfirm the hemial reatins whih ur under the nditins prpsed fr this gasifier, examine the variatin f the prduts f mbustin under the prpsed thermdynami nditin, nfirm that the gasifier des prdue a medium Btu gas, nfirm that there ar n aking prblems under the prpsed perating nditins, examine the impliatins f develping a medium Btu gasifier whih ntains an adjustable prprtin f H and, and nfirm the i:daptability f a pebble bed heater fr use in a gasifiatin press. A review f the mst advaned lw Btu gasifiatin presses indiates that they are basially air blwn systems whih prdue a gas having a higher heating value belw 200 Btu/sf [1-10].** In additin, many f these presses require extensive dust leaning systems. It has beeii pinted ut in the literature that any enrihment f lw Btu gas utilizing 0- results in a st penalty f $0.20/10 Btu as well as an energy penalty whih an be as high as 10 perent f the eletrial utput f the utility t whih gas is being supplied [11-12]. Studis have als shwn that lw Btu gas utilizatin is smewhat limited with *Us f dislsure i : prpsal data is subjet t the restritin r: the title page f tins prpsal. **N-.inibrs in brakets refer t entries in RliFCRLNCES.

18 heating values belw 200 Btu/sf beause f pipeline transprt limitatins. Gasifiatin installatin, having heating values abve 300 Btu/sf, hwever, are able t be transprted ver suffiiently lng distanes t allw muh greater flexibility. The disadvantages with this medium Btu gas in the past has been the requirement f 2 enrihment. The press whih is prpsed is able t supply a medium Btu gas (340 Btu/sf) withut requiring enrihment. Further, there 2 is n need fr any dust ntrl apparatus in the system. The gas leaving the gasifiatin system is virtually dust free. Finally, the H / rati in the prdut gas is mpletely variable fr the prpsed press. In fat, by perating at high pressures, the shift nversin step an be bypassed if a high Btu gas is desired. The press an als be run under perating nditins in whih n har is prdued withut the additin f xygen. A summary f the advantages and disadvantages fr the prpsed system is given belw. Advantages: 1. Sine al is never burned, the system an be designed t handle al with ash having a lw fusin pint by ntrlling the maximum temperature in the gasifir. 2. There is n nitrgen intrdued int- the reatr and hene there is n need t use pure xygen t ahieve a medium Btu * prdut gas. Tins nditin results beause steam is used bth as a ratant and as a heat sure in the reatr. Use f dislsure f prpsal data is subjet t the restritin n the title page f this prpsal

19 3. There is n inherent har frmatin in the prpsed system* beause f the amunt f exess steam used in the reatr. 4. The fuel gas mpsitin f the /H rati an be varied either in the initial design r during peratin t suit subsequent press needs, suh as methanatin, methanl prdutin, r hydrgenatin. 5. The \L prdued is saturated with water vapr whih prevents embrittlement f steel. 6. When n external heat sure is used in the auxiliary biler, there is n air pllutin frm the press. Fine fly ash prduts are remved with the ndensate. nly water treatment and water ling is required. 7. This al gasifiatin system an inrprate slid waste effiiently. When this is dne, air pllutin ntrl f the mbustin prduts f the slid waste in the biler might be needed. 8. Fr high sulfur al, the use f exess IL assures the frmatin f US (with the amunt f S frmatin being negligible). If the FLS prdued frm using al having a 5 perent sulfur ntent is treated t prdue elemental sulfur and H, this 1L an be reyled in the press t be used as part f the fuel gas. Fr this example, the \\^ prdued frm the sulfur press amunts t abut 2 perent f the ttal H in the gas. *Use f dislsure f prpsal data is subjet t the restritin n the title page f this prpsal.

20 , 9. The higher heating value f the fuel gas an be realizable in* sme appliatins sine the fuel gas des nt ause aid rrsin beause sulfur is remved in the press. 10.! Gas is prdued with an verall system effiieny f 60 t 70! i perent withut N' 2 dilutin r use f pure 0^ 11. Cal with a lw fusin temperature f ash (Illinis al has a sftening temperature between 2,250 F and 2,520 F with an average f 2,360 F) an be handled in the present system. ptins f reatr nfiguratins fr the prpsed press inlude: a. Fixed bed-an be designed fr peratin at temperatures belw that f ash fusin, Jb. Fluidized bed--an be designed fr temperatures belw that f ash fusin (gas bubbles in the fluidized bed ar nt as detrimental as in gasifiatin presses using xygen r air where shrt iruited xygen will burn with the fuel gas leaving the bed). Sputing bed-- fr high temperature peratin with slag remval, and d. Cylne entrained bed-at high temperature and slag remval. 12. Unless the tar is remved by preheating at a lw temperature (930 F),.the tar in the al is redued t and H 2> 13. 'The 1 perent nitrgen fund in the al is ither in an adsrbed r in a mbined frm suh "as CN and hydrides. These *Us f dislsure f prpsal data is subjet t the restritin n the title page f this prpsal.

21 j mpunds will be redued at the reatr nditin t N' 2 gas* r N (the latter being readily remved by disslving in the (ndensate). 14. A high system pressure is desirable beause the pwer nsumptin t pump water is less than' that fr mpressing the gas prdued fr transmissin and/r strage. Disadvantages: 1. The - in the raw fuel gas needs t be remved, althugh the 2 MEA absrptin press is mmerially available. This is a prblem mmn t mst gasifiatin presses. 2. Reatr steam injetin rates five times greater than thse used in urrent design may be required. All f this water is nt nsumed, hwever. Apprximately 40 t 50 perent mre water may be nsumed with this press under the wrst ase nditins. In additin t the water injeted int the reatr, ling water is als needed. 3. The pebble r refratry heater perating at high temperature with pebbles r parts underging alternate heating and ling will have similar prblems as in its appliatins in petrleum refineries. These refratry heaters are widely used in the petrleum industry. 4. The existene f a lwer heating value is a result f the 'hydrgen in the fuel gas. This heating value depends n the II / rati as in ther gasifiatin presses. 2 Use f dislsure f prpsal data is subjet t the restritin n the title pajj f this prpsal.

22 5. Fr the same transmissin pressure and pressure drp ver a* given distane, the present fuel gas alls fr a 50 perent greater pipe diameter than methane. It shuld be nted, hwever, that the medium Btu gas prdued in this press is ready fr mthanatin. The validity f the steam press f gasifiatin is explred, in a preliminary way, in the studies f Jensen [13] and f ppelt, t al.,[14] Bth f these studies used eletrial heating. *Us f dislsure f prpsal data is subjet t the restritin n the title page f this prpsal.

23 1 PRCESS DESCRIPTIN verview The present press gasifies al by reating it with steam at*-.temperatures f 2,000 t 3,000 F r higher withut the al ever ming int ntat with air r xygen. Indiret heating f the steam entering the reatr is amplished using a pebble bed heater whih utilizes a reyled fratin f the gas prdued fr heating the bed. Stak emissins frm the biler and heater are as lean as any gas fired system. Sine exess steam is used bth fr heating as well as fr gasifying the al, the sulfur in the al is remved in a liquid slutin. As a typial example, a 550 tns per day plant perating at a mderate pressure f 220 psi with a maximum steam temperature f 3,000 F, an estimated verall system effiieny arund 70 perent is attainable fr prduing a net f 15,700 sfm f gas at 340 Btu/sf. If prvisin is made fr stak gas treatment and slid waste is burned in the auxiliary biler part f the system, the system effiieny an be raised up t 86 perent with a 25,700 sfm utput. A desriptin f the majr elements f the prpsed press perating in a steady flw state is given belw. The system an als be perated as a bath press (see APPENDIX A). The mpressed air frm mpressr (2S), after passing thrugh the heat exhanger (29a), is fed thrugh a nzzle int the riser t lift the pebbles frm the regeneratr setin (lib) int a ylne whih separates the pebbles feeding the pebble regeneratr in setin (11a) frm the air. The air is then direted int the burner (14) whih *Us f dislsure f prpsal data is subjet t the restritin n the title page f this prpsal.

24 prdues a ht gas by burning a fratin f the reyled prdut fuel gas* t raise the pebbles (say, 0.5 inh mullite) t 3,500 F while the ht gas is led t 1,200 F and fed int turbine (Tl). The heated pebbles pass I n thrugh a thrat whih als serves as a gas seal int setin (lib) where superheated steam at 1,200 F is heated t 3,000 F. The design pressure, fr illustrative purpses, is 220 psi. Leakage f ither ht gas r steam is ntrlled by adjusting the pressures in (11a) and (lib). Steam heated t 3,000 F is fed int a sputed bed f al in the gasifier (19) while al is delivered under pressure. The air is taken int a turbine (T2) whih revers the pwer by driving a generatr r drives an air blwer t furnish additinal air if needed in biler (6); the air frm the turbine (T2) is near atmspheri fr the biler (6). Depending n the prperties f the al supplied, the gasifier (19) shwn in Fig. 1 an still be used. ther alternate reatrs suh as a nventinal fluidized bed uld als be used in (19). Additinal details are given in APPENDIX A. The system shwn in Fig. 2 desribes typial perating parameters fr a apaity f 550 tns per day f al, althugh it wuld be feasible t design a system apable f handling up t 10 t 20 times this amunt f al. While a 220 psi maximum pressure is used fr illustratin, the system an be designed t perate near atmspheri pressure; the simplifiatin wuld invlve the eliminatin f the turbine-mpressr. i A mtr-driven blwer wuld be suffiient fr this latter nfiguratin. The nvel features f the prpsed press inlude reating al with superheated steam under nditins f high exess steam and utilizing *Us f dislsure f prpsal data is subjet t the restritin n the title page f this prpsal. 8

25 a pebble bed nfiguratin t preheat the steam befre entering the re-* atr. The bed nfiguratin is nvel in that the pebbles ar heated by mbusting a fratin f the reyled gas prdued with air in ne setin f the pebble bed whih is islated frm the steam heating setin. The ability t ntrl the steam temperature entering the reatr allws fr a variable IL/ rati in the prdut gas. The ability t superheat the steam in the absene f air t high temperatures and t ntrl the amunt entering the reatr remves the neessity f an xygen plant t ahieve medium Btu gas. The use f gas t heat the pebble bed avids spalling f pebbles by partiulates. The majr mpnents f the system are available within urrent engineering pratie. Tnese inlude turbine-mpressr sets, pebble bed regeneratr, risers, ylnes, sputed beds, pak beds, r fluidized beds, bilers, and heat exhangers. Sine IIS is prdued instead f S0, sulfur is readily remved. The arrangement f these mpnents as well as 2 the perating nditins are believed t be nvel. The feasibility f the press using exess steam an be demnstrated by examining the reatins under equilibrium nditins. T generate U^ at 1,800 F, using stihimetri amunts f H 0, steam has t be heated 2 t abve 16,000 F. Beause the present inventin uses exess amunts f H as a heat transfer fluid, steam supplied at 2,500 F is suffiient t furnisli the needed heat f reatin. This exess 1^0 als displaes the hemial quil ibriun t a pint favring the frmatin f II S instead f S- whih is als desirable. Figure 2 is a diagrammati representatin f the prpsed system. *Us f dislsure f prpsal data is subjet t the restritin n the title page f this prpsal.

26 A gas- fired pebble bed heater (r ther frm f erami heater suh as* Rht Muhl-B. and W. Cmpany system) heats the steam frm T as delivered frm the biler-superheater t T. This steam is used t bth heat and gasify the al in the reatr. The gas prdued tgether with the exess steam at T enters the ler in whih the gas is quenhed and steam is ndensed while heating the water, steam, and air fr mbustin. The utput gas ntaining prinipally IL,,., and H S, passes thrugh absrbers t remve sulfur and C0~ t prdue a fuel gas having a higher? heating value f 340 Btu/sf independent f the prprtin f in the gas. The heat absrbed is determined by the heat f reatin and equilibrium based n the data in Table 1 (Basi Reatins), the speifi heat f the al and the mpsitin f its ash. It is seen frm Reatin (2) that 3,235 Btu/lb-C is absrbed r 970 Btu/lb H is prdued frm the C. Reatins (7) and (8) shw 932 Btu/lb S absrbed frm the pyrite reatins 2 r 14,940 Btu/lb 1-L frm the S. Hene, fr a al f 95 perent C and 5 perent S, 3,120 Btu/lb fuel will be absrbed. This figure is inreased by the frmatin f in Reatin (1), as well as by the dempsitin f sulfates and arbnates in the ash. Reatins (1) and (2), in Table 1, are, in effet, the utilizatin f C t redue II. Sine, in the present press, this is the nly bjetive in the reatr, this press affrds great flexibility in determining the prprtins f H- and in the gas prdued. Mst nventinal gasifiatin presses try t bth supply heat by mbustin and amplish this reduing press at the same time in the reatr. As a result, the rati f H. t is muh lwer than fr the prpsed press. APPLLN'DIX A inludes the patent appliatin f *Use f dislsure f prpsal data is subjet t the restritin n the title page f this prpsal.

27 S. L. S f the high-pressure burninglss water gas press f al gasifi-* atin, n whih the present prpsal is based. While n deisin has yet been reahed as t the status f its patent, the infrmatin presented here and in the appendies is prprietry. APPENDIX C is a signed py f prvisins f the DISCLSURE SUBMISSIN NDITINS. Hls f dislsure f prpsal data is subjet t the restritin n the title page f this prpsal.

28 SYSTEM PARAMETERS The Q's in Fig. 2 dente the heat transferred at eah lement f* the press; the W's dente wrk input, all fr 1 lb-mle f II intp the reatr. A range f design and perating nditins shwing the influene f variables in different ases fr the system in Fig. 2 is given in Table 2. Table 2 als shws the range f hie f mpsitin f fuel gas prdued via prper seletin f design parameters. The lumn entitled "Typial Labratry Experiment" gives data f the prpsed labratry wrk shwing its usefulness in demnstrating the validity f the system in Fig. 1. The data in Table 2 are gruped under design parameters, energy relatins, flw quantities, prdut mpsitins, and perfrmane parameters. Cases illustrated shw the flexibility f the design f the system t ver a wide range f situatins. Calulatins were based n heat f reatins and hemial equilibria as given in Table 1. Flw relatins in Table 2 rrespnd t the diagram in Fig. 1. The items in Table 2 are further nted as fllws: Item 1: Carbn input C** is that reated with 1 lb-mle f H.. Fr T** tns per day f 12,000 Btu/lb al, multiply extensive quantities in table by T**/C** t btain per minute values. Case (6) shws that the system an be designed t handle lw fusin temperature ash in a fluidized reatin. Item 2: Maximum temperature is that at the inlet t the reatr as prdued by the pebble heater. The steam is supplied *Us f dislsure f prpsal data is subjet t the restritin n the title page f this prpsal. *M)mpsi t in f sulfates and arbnates in ash absrbs additinal amunt f heat.

29 as a heat sure as well as a ratant. A greater amunt* f heat r steam may be needed depending n prperties f ash** in al. Item 3: Quenhing temperature is that leaving the reatr int I the ler where rapid ling will lead t frzen equilibrium nditin. The fuel gas mpsitin an be mdulated by this temperature and arbn input, (Items 16 and 17). Item 4: The system pressure f 10 atm has been hsen fr thse equilibria where st r har frmatin urs at muh higher pressures (allwable pressures in parenthesis). Fr Cases 5 and 6, the pressures were determined frm the nditin where n arbn is left in the prdut. Hene, the system an be designed fr n arbn left-ver while satisfying ther nditins. Where there is n exess f HJ3 suh as in several nventinal gasifiatin systems, the ase f n arbn left-ver urs nly at zer pressure r at exess?. Item 5: H nverted by equilibrium reatins f different ases are given. ne (1) minus this amunt is eventually n- densed and reyled, exept apprximately 1 perent f water vapr remains with the prdut gas as saturdated vapr. Hydrgen in the prdut gas des nt ause erabrittlmnt f steel when it -is saturated with water vapr. In the ndensr, flyash arried ver serves as ndensatin nulei and will nt ause air pllutin. HJse f dislsure f prpsal data is subjet t the restritin n the title pig f this prpsal. 'Dempsitin f sulfates and arbnates in ash absrbs additinal amunt f heat

30 Item 6 and Item 7: Ninety perent heat exhanger effetiveness was taken,* I whih is attainable within enmial designs. Item 8: The heat t ling water is the net ndenser heat remval. Cling water requirement is determined frm this item. Nte that high maximum steam temperature and lw quenhing temperature means a mre effiient system and lwer ling water demand r thermal pllutin. Fine flyash, frming ndensatin nulei, is remved with the. ndensate. Item 9: The pump wrk shws that it is enmial t pump water t generate steam at the desired gas supply pressure than t pump the gas. Item 10: The blwer wrk fr pumping the air required in mbustin was alulated fr the intermittent heating system f the pebble heater and an air pressure f 30 inhes water wuld be suffiient. Fr the steady flw system, air at the system pressure an be prdued with a turb-mpressr unit, with the turbine revering the larger part f the mpressr wrk and n signifiantly greater net wrk input is expeted. Item 11: The fratin f gas prdued is burned with air t heat the pebble heater. Hene, the pebble r refratry heater is never expsed t arbn r al, thus aviding spalling *Us f dislsure f prpsal data is subjet t the restritin n the title page f this prpsal.

31 f the pebbles by the st partiles and ersin by the* slag. Nte that higher maximum steam temperature means greater demand in the pebble heater; this is beause a superheater utlet f 1,200 F has been hsen arding! t urrent engineering pratie. Higher superheater utlet temperature will redue this demand. Item 12: The fratin f gas t the biler, if used, will eliminate air pllutin mpletely. 'Hie nly envirnment impat will be treatment f reyled water and supply f make-up water fr the press and the ling water regeneratin. If, as is nted with Item 7, external sure f heat is used, suh as slid waste, the gasifiatin effiieny will be greatly imprved. As a matter f fat, this system is the nly ne whih effetively nverts slid waste t fuel gas, as nted in Item 27 (fr system with lw maximum temperature) as muh as 30 perent f the heat needed in gasifiatin an be supplied frm slid waste. Item 13: The number f mles air fr mbustin in Items 6 and 7 fr eah ase is given. The air is preheated in the ler and in heat exhangers revering heat frm the mbustin prdut leaving the heater and the biler. Nte that even thugh air instead f xygen is used in this gasifiatin press, there is n nitrgen dilutin f the fuel gas. Item 14: The greater effiieny f greater T and lwer T is seen in r e and Item 15: the greater amunt f fuel gas prdued by given arbn input. *Use f dislsure f prpsal data is subjet t the restritin n the title page f this prpsal.

32 J4. Item 16 and Item 17: The press an be adjusted t prdue a gas f desired* prprtin f and I!. Case 1 r nearly 3 t 1!L and is desirable fr mthanatin. Still higher an be used fr prduing methanl. Higher perentage f H- than Case 6 an prdued fr hydrgen fuel systems, r hydrgenatin. Item 18: Mles f t be absrbed may be nsidered a disadvantage f the system. The press is, hwever, rutine; ne f these is, the MEA (mn-ethanl amine) system. Item 19 and Item 20: Calulatins frm equilibria f II S shw an imprtant advantage f the present system: Beause f exess f IL and W, S0 2-7 (suh as frm sulfates in the ash) (less than 10 f ILS) and S (less than 1/100 f II S) are bth negligible in the m. gasifiatin prdut; the H-S is readily remved in suh as the Girbtl r Stretfrd presses with revery f H. t the fuel gas. In anther way f speaking, S in al (als in pyrite frm) als ntributes t the prdutin f 1L (see Table 1). Item 21 and Item 22: The higher heating value (HI IV) and the lwer heating value (LI1V) f the final fuel gas is given. The LHV is appliable t usages where H frm mbustin is nt ndensed. The differene is nearly 45 Btu/sf, even when 90 perent f IL and 10 perent f is prdued. Nte als that II! IV is at least in part realizable in bilers beause aid rrsin is n lnger a nern. Use f dislsure f prpsal data is subjet t the restritin n the title page f this prpsal.

33 Item 23 and I tri 24: Th pff;.i. ; ^ I / / i.. eff"ieny range shws A eff "iny. is I better than thse reprter! p are C0 "'I,CtitiVC - N tc - *» «a" mparable r EVe " th ffi "enis based n L V *.,«* f fi? p 70 perent f the ht- <-v ' "euher an be handled in ther gasifinti sasitiatin ruw «. presses. LHV The effiieny wuld be <~ bc9s -. 8 at2er ^ slid waste is available zer st, and better yet if,h dispsal. h System is "edited fr Vast,»aste Hie general feature ure f n,i the present press ls i, se equilibria f «" H the hial and hn at varius temperatures ures and m- pressures. Fr the water gas reatins m anf),,,., equilibrium, W and (3) f i, le f and a mle f n., w have: 2 at 1 5 J C0 2 + (2 - a 2. 2a s ) R, + (a a, 2a 5-2) ^ +,.,.' with a mle f rc in «.i * 5 m the frm f st r har Th,.,. -a temperature and pressures sl a < - x 1, whih wnin ' i- *» tl the ase f svpni 5CVeral nventinal 2asifintin««S - urs at nly, er prssure ** W,,.. ^^ "" '"^ Tak th f inhing f a as at K (1740«F) at 10 atm a - n i, ' F- Case 2 f Table ludj 2,, hwever a - e; / ' k-, " S00t f ' atin urs niv * ^'.pressures, fr these H tw values f, h ' *» '0 atm prest bll d P - Ul ' bjs^ n 1 mle f C: 3 S " "^-ie f C will be lef. *" fml0 "1 «"*»*- the restritin n

34 Quenhing Cnventinal Press Pint B in Fig F Present Press Pint A in Fig F H 2 in (a ) Prdut Mles C (st, har) 1 mle 0.1** 5 mles H Fuel Gas H perent r higher* 54.5 perent r lwer Sulfur n H2 S /n S Hene, the present press may give a fuel gas f 10 perent and 90 perent H_ r 25 perent and 75 perent IL in ase 1, Table 2, withut the dilutin by nitrgen even thugh air is used in the heat generatin. Mrever, exess supply f steam eliminates har frmatin. Beause air r xygen will be present in the riginal input t prdue the heat f reatin. **Expt when xygen is in exess. ***Us f dislsure f prpsal data is subjet t th restritin n the title page f this prpsal.

35 Plant Design and peratin While different ases in Table 2 may be regarded as illustrating the nsequene f seleting different design parameters, they als illustrate the range f peratin and adjustment with the input variables suh as al mpsitin, availability f slid waste, and the desired fuel gas mpsitin. Table 3 illustrates tw typial design nditins fr a gasifiatin plant f an utput f 18,000 sfm gas f 340 Btu/sf HIW. The fuel supply is 500 tns per day f al as speified in the ase (A) and 330 tns per day f al and 281 tns per day f slid waste in the ther (B). Anther view f this table is that it gives the perating nditins f a given gasifiatin plant at tw different fuel supply nditins. Nte that 5 perent f S in the al may prdue an additinal 2 perent f the fuel gas.

36 PRPSED STUDY The prpsed study nsists f tw phases. Phase 1 inludes {he* verifiatin f the press as a viable means fr gasifiatin, a detailed gas and ndensate analysis and the determinatin f design parameters fr a gasifiatin plant (Table 4). This will be nduted in the Mehanial Engineering Labratry n benh sale equipment with available steam supply and eletri heating. Referene tests will be made with arbn fr the mparisn f a wide range f al samples. A preliminary design f a pilt plant is in Phase 2. Phase 1: Wrk in this stage will be nduted ver a perid f 12 mnths. Fr nduting the tests, the 150 psig gasifiatin system shwn in Fig. 5 is t be nstruted. A shemati f this system is shwn in Fig. 4. Available steam supply in the Mehanial Engineering Labratry at 150 psi and 375 F will be nneted t the experimental setup via 2-inh valve n the steam main. The steam, after passing thrugh a reduing valve, will be heated in an available eletri heater pwered by a 20 kw d pwer supply. As shwn in Fig. 5, the desirable steam temperature is btained by mixing f the streams at high and lw temperatures. Fr tests with 3,000 F steam fr the reatr, a flw f 0.75 lb per minute an be maintained. The refratry (magnesia brik) lined reatr ntains a bttm layer f spheres f mullite (limited t 3,340 F) r ther refratries (suh as fused magnesia fr up t 4,000 F) fr distributing the steam flw int the al bed f lump al r al dust fr fluidized bed tests. These refratry spheres will be 0.5 inhes in diameter r 0.25 inhes in diameter fr btaining knwledge *Us f dislsure f prpsal data is subjet t the restritin n the title page f this prpsal.

37 f the heating and ling harateristis f these refratry spheres.* The flw velities will be belw 5 fps. The harge f 6 t 10 lbs f arbn r al will permit a running time f abut ne hur. The temperature will be mnitred by thermuples (TC) lated at varius pints. i The perating pressure f the reatr is redued t slightly abve atmspheri pressure suh that the gas delivered is nearly atmspheri fr analysis. Adjustments will be made fr varius utlet temperatures T fr e quenhing and ling. The nditin inside the reatr will be bserved thrugh view prts. The gas flw will be measured by a wet test meter and its heating value will be determined with a Junkers alrimeter. The referene test will be that made n labratry grade haral hips. Tests and adjustments and rretins will be made t reah a lwer heating value f abve 200 Btu/sf ( is nt remved in this stage). Frm that pint n, al samples will be tested fr the ability t ahieve a heating value f suh a magnitude. These results will determine whether the prgram will preed any further. The aquisitin f hrmatgraph will be fr gas analysis and the ling needs will be determined by weighing the ling water flw. Reatin rates will be determined by different running time and different sizes f bathes. ptimum temperatures f inlet steam (T ) and utlet gas (T ) will enable us t reevaluate the prpsed system and its design nditins. Determinatin will be made n the reatin rate, heat transfer relatins fr the desired quenhing nditins, ndenser peratin, and ash and ndensate analyses. Bath testing will still be neessary and extensive al and ash analyses will be perfrmed. The apparatus shwn *Use f dislsure f prpsal data is subjet t the restritin n the title page f this prpsal.

38 in Fig. 5 may develp a standard tl fr evaluating al fr the present* press f gasifiatin. This stage will evlve int a ntinuing labratry funtin f ntrl tests fr pilt plant referene and al press evaluatin. Phase 2: Based n the design infrmatin btained abve, design f the pilt demnstratin plant will be made. Further tests will inlude using the gas prdued in Phase 1 equipment t test the pebble bed, the effet f thermal yling f the pebbles f mullite r magnesia (fr bth peridi system and steady flw system), and mpnent needs. Cal lk and al feed systems and ash lk and ash dispsal systems will be designed and speified. Design will als be made n the H-S and - absrptin system. A prpsal fr a pilt r demnstratin plant will be mpleted in this perid fr beginning f installatin by mid Table 4 is an utline f the prpsed time shedule and sh;vs verlapping f stages and phases. The present prpsal vers Phase 1 and the design stage f Phase 2. *Us f dislsure f prpsal data is subjet t the restritin n the title page f this prpsal.

39 REFERENCES 1. Karnavas, J. A., Larsa, P. J., and Pelzarski, E. A., "ATGAS-Mltn-Irn Cal Gasifiatin," presented at 1972 A.G.A Syntheti Pipeline GAs Sympsium, tber 30, Larsa, P. J. and MGarvy, R. J., "fuel Gas frm Mlten- Irn Cal Gasifiatin," presented at Clean Fuel frm Cal Sympsium at the Institute f Gas Tehnlgy, Chiag, 111., September 10-14, Huebbr, J., "Cal Gasifiatin: State f the Art," Heating/Piping/Air Cnditining, (1973), January. 4. Hegarty, W. P. and Mdy, B. E., "Evaluating the Bi-Gas SNG Press," Chemial Engineering Prgress, 69, N. 3, pp (Marh 1973). 5. "Gas Manufatured," Kirk-thmr Enylpedia f Chemial Tehnlgy, Send Ed., Vl. 10, pp Franswrth, J. F., et al., "Prdutin f Gas frm Cal by the Kpper- Ttzek Press," presented at Clean Fuel frm Cal Sympsium at Institute f Gas Tehnlgy, Chiag, 111., September 10-14, Frney, A. J. and MGe, J. D., "The Synthan Press Researh Result and Prttype Plant Design," prsnted at the Furth A.G.A Syntheti Pipeline Gas Sympsium, tber 30-31, Leding, J. W. and Tsars, C. L., "IGT U-Gas (Clean Utility Gas) Press," presented at Clean Fuels frm Cal Sympsium at the Institute f Gas Tehnlgy, Chiag, 111., September 10-14, Arher, D. H., t al., "Cal Gasifiatin fr Clean Pwer Prdutin," presented at Clean Fuels frm Cal Sympsium at Institute f Gas Tehnlgy, Chiag, 111., September 10-14, Banhik, I. N., "The Winkler Press fr the Prdutin f Lw Btu Gas frm Cal" presented at Clean Fuels frm Cal Sympsium at Institute f Gas Tehnlgy, Chiag, 111., September 10-14, "Cal Tehnlgy: Key t Clean Energy," Annual Reprt 1973/74, ffie f Cal Researh, U.S. Department f the Interir..2. Squires, A. M., "Clean Fuels frm Cal Gasifiatin," Siene, Vl. 184, April 19, 1974, pp Jensen, 0., "A New Eletri Press fr the Carbnizatin f Nn- Cking Bituminus Cal," J. Inst. Fuel, 23, (1950). 4. pplt, W. II., Kanps, T. W., Grnhvd, C. H., Kub, W. R., and MMur.tri, R., "Prdutin f Crude Ammnia-Synthesis Gas frm Nrth Pakta Lignite in Annular-Retrt Gasifir "US ' Bureau f Mines Reprt N. 52D7 (1957).

40 i Tabi 1 Basi Reatins (Multiply kal/g-ml by 1,800 t get Btu/lb-Ml) nnj Equilibrium Cnstants. between 800 K and 1,200 K, Gasifiatin: ' (1) C H t + H kal/g-mle 1 *10 K l = l *10 < P W=? ' 641 " 7 ' 230/T ( K) (2) C + 2H 2 (. t C0 2 21l (3) + H 0,, t H v Cfi) 2 2 lf w K = lg (P P /P P,,^) = /T 10 H2 C()2 C0 (. K) Cmbustin: (4) C + (5) + 2 t C t C (6) H 2 + ~0 2 Z H Z H., (g) Sulfur: (7) H 2 S * H 2 + S (8) FeS + H 2 f * Fe + US (9) 3H 2 + S0 2 t H 2 S + 2H * h K s - I *i p ( H s p /ps2 h 2 Ph > = " ". "fw (10) + M 2 S * S + H 2-35 K C0S " P S P../ P C0 P!I 2 S " 0316

41 : TabJe 2 Summary f Prdut and '.inr^y Relatins f Press >f (based n 1 lb-mle f Steam at Reatr Inlet, 1,200 F at Superheater utlet (T ), 100 F Cndenser Temperature (T )) pe$1gn i C*»es Para-ters: S Typial labratry Eipert.vnt 0) C«rb9n Input. C*. 1b-Mt (?) K9i1r.tr* Temperature, F V 0) Quenhing Trperatun V -F («) System Pressure, P. atm (Allable) (5) H,0 Cnverted, lb-tla.» S S 0.3$ S00 2S X C 1-1C (70) (12) (23) (27) (3) (6) 0.S S fnerv Re latins (6) lief t t Pebble Neater (7) (B) (90S Efftlw.es:,) Q Btu a Eletri M Heater Net Heat t Eiler (90X Effetiveness) Q ba. Heat 10 3 Btu t Cling Water Q^, 10 3 Btu 6.46 S (9) Purp Wrk, w, Btu 7? (10) Blwer Wrk, w_, Btu (33 Inh H-0 equivalent) Flw Q entities: \ (ID Fratin f Gas t Pebble Heater (12) Fratin f Gas t Biler* (13) Hles f Air S es (14) Hles Fuel Gas Generated (15) Mles Fuel Gas (Generated with External Heat) (0.468) (0.496) (0.428) Prdut C-Psitins: * (0.356) (0.454) (0.302) (16) Fuel Gas:. S ; (17) (18) (15) Fuel Gas: H 2, S Hles - t be Absrbed n'h 2 5/''S0 2.' (20) N il 2 S /; 'C0S S5 250 Perfrrne Pa rasters: (21) Higher Keating Value (H-iV, ttu/sf) *(22) le*r Heating Value (IHV). Ttu/sf m (23) Effiuiiy, MHV (withut External Heat) *{24) Effiieny. HMV (with External Heat), I e S6< 3 > (25) Effiieny, LHV (wlti.ut External Kat), I S (26) Effiieny. U'V (with Extrnel I'at), M.S C5< 3 > (27) I Waste Heat Utlllubl Fr P Ins f Cil per Pay f 1?.0C0 Gtu/lb, Multiply Extensive Quantities by */C* t btain f'ls per Minute Steam Supplied 78 Nt Remved Kay use e* tenia I lu-a ("sure "suh as slid wjste; (3) Externil Heat Ht Chjrgel.

42 Table 3 Typial Design Cnditins fr 18,000 sfm Gas f 3«10 Btu/sf (IlilV) A. Cal Gasifiatin (Air Pllutin Cntrl nt Needed) (Crrespnding t Case (1) f Table 2) Fuel: 500 Tns/Day f Cal f 12,000 Btu/lb 9% Ash; 5% Sulfur j! Gas Prdued: 25%, 75% hl Water: 158 gpra Cnverted 146 gpm Treated and Reyled 3,700 gpn Cling Water (30 F Temp. Rise) Air: 41,620 sfm, 93 hp Net. Pebble Heater: 2.13 x 10 8 Btu/hr, 11,700 sfm Fuel Gas Biler: 1.03 x 10 8 Btu/hr : 5,760 sfm Fuel Gas Raw Gas Treatment: C0 2 Remved: 9,900 sfm H 2 S Remved: 330 sfm Giving: 21 Tens Sulfur/Day 330 sfm H 2 Effiieny: 73% (HIV), 65% (LHV) B. Cal Gasifiatin with Burning f Slid Waste whih May Need Air Pllutin Cntrl (Crrespnding t Case (6) f Trble 2) Fuel: 330 Tns/Day f C;:? f 12,000 Btu/lb 9% Ash, 5% Sulfur 231 Tns/Day f Slid Waste f 6,000 Btu/lb Gas Prdued: 11%, 89% H i. Water: 125 gpm Cnverted 156 gpm Treated and Reyled 4,000 gpsi Caling Water 0 e F Tssn. Rise) Air: 32, 00 J sfm, 43 hp Net Pebble Heater: 10 8 Btu/hr, 3,350 sfm Fuel Gas Biler: 1.41 x 10 Btu/hr, Heat frm Slid Waste Burning Raw Gas Treatment: Remved: 9,100 <f.:. H S KMvd: 2\V sfm Giving: 1J Tns Su3fur/D:.y Effiiytiy: 78% (HilV), :,:". (i.!!v) 220 jefm IK,

43 evaluatin) 0' (0 w n k C) V 1-4 S.'i t L t tests I "-N 1 1 r-. 1 >> E f- r~» en H 1 l I 1 J_ t l I i i 3- (N H CM H i-h 1 CT> ntrl f ativity press /-> 1 1 CN 1 C 1»H 1 1 * H 1 P P 1 1 V rh 1 t-t H 1 w P C M P H A. J_ (0 l ft l l CX) 1 u 1 &4 l r- TJ 0) t. t-- <T> a, r-\ k 04 b ip. Q) H 3, TJ 1 IT) ^f CM 0) H JG i + CN 0) H e H H H CD 01 H 3 00 H t>» tinuing al 4_ C T) t <U 10 CD p 0) e ftj a. e CD P ip p CD 6 H <D Q P P «H CQ a, H (U(L, in t-«h t f0 CM CM <D V a) CD 10 t fu f0 r0 x: -m -C x: h 00 ^ a«

44 fu>1 C»*.?l.*'w f 'w Mr 1rr.-> lr,t\ f wrj f.»» US P*' till y zi>:':; :.'\ ; ;i;;' : 1^ N -: 5«t thrift / i-lc:': : :!;:":';;!:ii>i:22 \/ '3-1 "'"". A.«> -v. l i *.."r'--:-"*.u" 4 >V / j.»* MjS s H-S *«*»«1 Presvjr* Cntrls 10* ifn f«el*ci; \ PetM* Riser J :<::- E'll;,,!:;,;..:!);:^ iiiiill H.'.^r Ht«r C«idei>i«' JL_JH -8L-, H*t»r 10* 9«r» t F Mrtf>tJtt<< 300»t<. n «p*» rii,. «,,»- - SW»tM r«"'"s- - '- '-' ""' «- "

45 «T 5» 1,200 F (-).^0,11- Pebble bed Heater2Burner }!«J(),M M. Reatr Cal v»/ 1 Exhaust H,.() Ash n lf J_ i J Available / 01 «/>»3 Biler _AAAJ Burner ru-r- Feed Pump Water _» ( P L ) w p va- Air 1 Available ( B ) -«Air -f 1 A1r Blwer w Cl Water Pump J* U Tl-F 'P i *-' /<^N -F Ash, Cndensate, fr 1 Treatment H? S Absrptin t (Girbtl) *S C0 2 - Absrptin (MEA) H*. () *May be replaed by external sure M 2 Air Cmb. Prdut H 2.(C0) Figure 2 Basi System

46 i a " l a g «0.05 Quenhing at 1340 F, p < 100, t give 2Z~Z, 721 H in Fuel Gas u 10 t give 107;, 90% H 2 in Fuel Gas ' Based n 1 Kle f C / 0.1Y a^ = a * fratin f riginal C 5 S,. - y^s^ Hle H,0/M1e X; j^5^ _ 10' i. CL 10 a Temperature, K 1G00 Figure 3 Equilibrium Relatins f C-H 2 Reatin

47 150 psig 375 F TC Eletri Heater ~20 kw TC Reatr --Cal Cal & Ash Analyses Ash T«T = 1500 F l 5_ TC TC *j Flw Weighing Water ^ Ash, Cndensate fr Analysis H 2,, C0 2, h' 2 S, S Gas Analysis Calrimetry Figure A Phase 1 System

48 Marh 12, 1975 Additinal nte t CR Prpsal N. U50233GA "A Steam Press fr Cal Gasifiatin" by S. L. S, Prfessr f Mehanial Engineering University f Illinis at Urb ana-champaign Urbana, Illinis Presentatin f further details n the basi knwledge and experimental fats n the steam press fr al gasifiatin appears warranted (1) & ( at this time. The experimental basis f the prpsed system has been presented in the fllwing referenes: Jensen, "A new eletri press fr the arbnizatin f nn-king bituminus al," J. Inst. Fuel 22 C 129 >» 54 " 5 (Experiment at 1000 C steam, briquetted al, prdued 500 Btu/sf gas) 2. W. H. ppelt, T. W. Kemps, C. H. Grnhvd, W. R. Kube, and R. MMurtrie, "Prdutin f rude ammnia-synthesis gas frm Nrth Dakta lignite in an annular-retrt gasifier," U.S. Bur. f Mines, Rept. Invest (1957). (Experiment with steam at atmspheri pressure, heated eletrially prdued 300 Btu/sf gas) 3. J.' L. Jhnsn, "Kinetis f bituminus al har gasifiatin with gases ntaining steam and hydrgen," Advanes in Chemistry Series, N. 131, Cal Gasifiatin, the Amerian Chemial Siety (1974), , Qnn v (Measured reatin rate f steam and al heated t 1900 F in a lsed hamber) 4 "Eletrially heated f luidized-bed reatr," Chera. Eng. News 42 (45) 68-9 (1964); als W. M. Gldberger, J. E. Hanivay, Jr., Ind B. G. Langstn, "The eletrthermal fluidized bed, Chem. Eng. Prg. 61 (2), 63-7 (1965). Bth referenes 1 and 2 arried ut gasifiatin f al suessfully with steam alne and at atmspheri pressure where the steam density is belw Ibm/eu. ft. beause f superheating by the eletri energy. (1) At 3000 F even at 10 atm. the density is abut 0.07 lbm./u. ft. Therefre even if ne bases his estimatin n the idea f ntat density alne, the illustrated test nditin. is mre than enugh t prdue. the desired reatin.

49 It is readily shwn, frm rrelating the data in Ref. 3 that the reatin rate nstant f steam-arbn reatin is given by a kineti frequeny fatr f 140 m/se and an ativatin energy f 3A.1 kal/g-mle. The rate f arbn nversin in mass per unit *-. «' time fr given surfae area and steam density is readily mputed. Fr a surfae temperature f 1540 K (2300 F) and a steam pressure f 10 atm., and a partile size f lmra, a reatin rate f 120 kg/se fr eah tn (900kg) f arbn is maintained. (. The heat f the abve reatin is supplied by the steam suspending the partiles via ndutin and nvetin maintained by a differene between the steam temperature and the arbn surfae temperature, and enhaned by relative mtin between the partile and the steam (see, fr instane, S. L. S, "Fluid Dynamis f Multiphase Systems," Blaisdell, 1967, p. 22). Fr a relative velity f 1.5 ra/se in the abve numerial example, all the heat f reatin is supplied by the steam at a temperature f 1612 K (2440 F). Hene the reatin rate an be sustained by the heat supplied by the steam. At the lwer temperatures, a lwer temperature differene than in this example will be needed t supply the heat f reatin. The relative mtin prdued in a sputing bed r a fluidized bed is desirable fr inreasing the (4) rate f heat transfer frm steam. The abve analysis shws that the suess f gasifiatin f al is dependent n: partile size (r slid surfae area), residene time, reatin rate whih is a funtin f temperature, the gas phase density, the relative velity f phases, and the nentratin f the reatant. The reatr design is a result f balaning all these fatrs. Based n the reatin rate as determined in Ref. 3 in the abve, the fratin (5) reated and the gas temperature vs. time is shwn in Fig. Al. This means that a residene time f 20 minutes is needed fr lmra. al at steam temperature f 3240 F at the inlet- and a pressure f 35 atm., r 70 min. at 10 atm. Even the latter residene time is quite suitable fr a 500 tn/day plant beause that means a primary reatr f 7.5 ft. inside diameter and 80 ft. high hlding 25 tns f al. The size an be redued if we design at 35 atm. but the balane is in the st f mahinery and related mpnents (mpressr and turbine, et. and the the design f the pebble bed heater) vs. the size f reatr and ther pressure vessels. Referene 4 shws the desirability f relative mtin and that lw vapr density at high temperature is nt the nly ntrlling fatr. (4) We have nt yet settled n a fluidized bed r a sputing bed. The sputing bed, if prperly designed, is useful beause its ntributin t the ntrlled residene time and greater relative mtin than an rdinary fluidized bed. It shuld be mplemented by a settling hamber fr the fines in the al t mplete the reatin. The pebble bed heater is perhaps nt as muh a prblem as an xygen plant. The fail-safe feature f the prpsed press is unmathed by (2) thers. f1. f f.

50 -3- The design has nt been finalized with regard t using a mving pebble bed heater r several fixed pebble beds with swithing. With regard t a mving pebble bed, the writer has industrial experiene f design f risers in atalyti rakers where the nditins are (5) similar t a mving pebble bed. It an be seen that beause f high gas vissity at the high perating temperature and the gas density prdued by the pressurized peratin will redue attritin f the pebbles in mparisn t perating a pebble bed heater at atmspheri (2) pressure. There is the disadvantage f the need fr valving in using fixed» pebble beds, but their nstrutin fr high temperature and pressures is well knwn. In the 1950 f s, air t prdue Mah 5 in a wind tunnel was heated t abve 3500 F in a magnesia pebble bed heater. The (2) pebbles were intermittently heated by ht gas at 4500 F frm an il burner and at slightly abve atmspheri pressre, and blwn with air at 50 atm. r higher. The greatest advantage is that by swithing amng several fixed bed heaters, the heating yle f pebbles an be arried ut near atmspheri pressure, thus there is saving in the mahinery fr air mpressin. Steam pressures f 35 atm. r higher an be readily designed fr with the attendant advantages even fr a small plant. Cal lks will als be pressurized with steam. In this, ase, air mpressin is entirely eliminated; mtr driven air blwers will be suffiient. Nte that the steam pressure is ahieved by pumping water, whih nsumes nly a fratin f the energy required by gas mpressin.

51 Si t ' U 1 - ~ $ s

52

53

54

55 ENMIC IMPACT N THE STATE F ILLINIS F THE MEDIUM BTU AL GASIFICATIN DEMNSTRATIN FACILITY AT THE UNIVERSITY F ILLINIS AT URBANA-CHAMPAIGN Mihael Rieber Researh Prfessr Center fr Advaned Cmputatin tber, 19 74

56

57 ENMIC IMPACT N THE STATE F ILLINIS F THE MEDIUM BTU AL GASIFICATIN DEMNSTRATIN FACILITY AT THE UNIVERSITY F ILLINIS AT URBANA-CHAMPAIGN A. Intrdutin The imprtane f al t the State f Illinis an be seen by mparing the value f al prdutin t the value f all ther mineral prdutin in the state. In 1969, al as a perent f ttal value was 42.4 perent. In 19 70, it was 46,6 perent. Unfrtunately, Illinis al prdutin des nt math its reserve psitin. Arding t the Natinal Petrleum Cunil, Illinis ntains 15.2 perent f the estimated ttal reserves f al in the United States. In 19 71, Illinis al prdutin was nly 10.6 perent f ttal U.S. al prdutin. Furthermre, the use f al has been delining relatively in almst every area f fuel nsumptin. Part f the prblem is transprtatin, part f the prblem is air pllutin ntrl, and part f the prblem is that al in its natural frm is learly the least flexible f all fssil fuels. Beause it is slid and ntains substantial amunts f waste, al invlves greater diffiulty at every stage f the use press. It is mre diffiult t extrat, transprt and handle in nsumptin than either il r gas. Furthermre, after mbustin an ash residue remains that reates a dispsal prblem. As a result, al is used in its 'U.S. Bureau f Mines, Minerals Yearbk 1970, Vl. 2, Table I, p. 235.

58 - 2 - natural frm nly when it is heaper than ther fuels. Mrever, the use f al in its natural frm indiates that the enmies f sale in al handling are suh that nly large users find that they an heaply verme the st disadvantages. This fat largely explains the nentratin f al use amng large nsumers f fuel. Inreasingly, industrial, mmerial and gvernment establishments have restrited their use f al. It has lng been a desire f the al industry t verme these drawbaks by develping enmially viable tehniques fr manufaturing syntheti il and gas frm al. It has als been argued that the impending exhaustin f dmesti nventinal il and gas supplies wuld make the need fr suh synthesis inevitable. The al gasifiatin prpsal is a plan t design, nstrut, and perate a al gasifiatin plant whih wuld use high sulfur Illinis al t supply the University f Illinis' Abbtt Pwer Plant. This plant wuld use tns f al per day t prdue a medium Btu gas. Fr mst industrial firms and institutins, generating either eletriity, heat r bth, the gasifiatin faility will nstitute a demnstratin plant. Fr large systems, suh as an eletri utility, it will serve as a pilt plant. Thus, the faility will serve as a demnstratr in a learning press invlving the majr natural resure f the State f Illinis and ther majr al states. It is a lng step twards satisfying three als: first, Prjet Independene; send, air pllutin

59 - 3 - ntrl regulatins; and third, a revitalizatin f al mining in the high sulfur bituminus al distrits, a majr energy sure east f the Mississippi. B. Cal in the State f Illinis The prblem faing the State f Illinis an be seen in Table I. Here it an be seen that 1970 ttal prdutin, as a perent by sulfur ntent, des nt math the reserves f al that exist within the state. The imbalane has been further aggravated by air pllutin ntrl regulatins, whih mean that fr the years after 1970, al prdutin is weighted even mre heavily tward the lw sulfur end while the perentage f reserves in eah sulfur ategry remains the same. It may be nted in passing that fr the 1.5 t 1.99 sulfur ntent ategry, reserves are negligible while prdutin is indiated at 6.3 perent. This apparent disrepany urs beause washing f al, as part f the prdutin press, lwers the sulfur ntent f the al smewhat. The table indiates that it is learly within the interest f the state t d everything pssible t enable prdutin f its high sulfur al reserves. Table II indiates the level f sulfur ntent fr al shipped t majr users. It must be pinted ut again that the data are fr As air pllutin ntrl regulatins tightened, the state is less able t nsume 3.5 perent sulfur al in its eletri utilities r 2.8 perent sulfur al in ther setrs. This will ause a drain n what little lw sulfur al exists within the state and will lse markets fr Illinis al.

60 TABLE I Distributin f Illinis Cal Prdutin and Reserves by Sulfur Cntent Sulfur Cntent 1970 Ttal Prdutin ' Reserves (Perent, Weight) (Perent) (Perent) (2) ver TTAL (1) (2) Cmpiled by Illinis State Gelgial Survey. Department f Health, Eduatin and Welfare, Cntrl Tehniques fr Sulfur xide Air Pllutants. January 1969, Table 4.2, p

61 TABLE II Illinis: Average Sulfur Cntent f Cal Shipped, Eletri Utilities 3.5 Perent Cke and Gas Plants 0.8 Perent ther Industrial and Retail 2.8 Perent All ther 2.8 Perent Exprts Sure: U.S. Bureau f Mines, Minerals Yearbk, 1970, Vl. I, Table 41, p. 384.

62 - 4 - C. The Medium Btu Cal Gasifiatin Plant The prpsed al gasifiatin plant, in additin t supplying heat and pwer fr the University, has a number f speifi uses. First, it will demnstrate the use f Illinis high sulfur al in a manner that is well within air pllutin ntrl regulatins. Additinally, it may be nted that the al supplied t the gasifier need nt have muh prir preparatin. Send, the plant will demnstrate t industry, large mmerial and gvernment mplexes, and small utilities, a methd f using al t generate press heat and steam, eletri pwer and, if the al gasifier is lse t the establishment, the gas an be used fr air nditining purpses. Third, fr larger utilities, the plant will serve as a pilt plant fr medium Btu gasifiatin. Furth, the gasifiatin plant an serve as a training site fr Illinis' persnnel (Envirnmental Prtetin Ageny and Illinis Cmmere Cmmissin) wh will be respnsible fr future hearings relating t the ertifiatin f al gasifiatin plant. Fifth, the plant will serve as a test base fr future experimentatin. Beause the plant prdues a medium Btu gas, a number f speial features arise. First, the gas an be piped abut 25 miles. This demnstrates siting flexibility t future users. Send, it need nt use pure xygen in the gasifiatin press. Therefre, nstrutin sts and perating sts are lwer. Third, the use f muh auxiliary equipment is eliminated. And