Publication: Magyar Közlöny
Issue: MK-2004-172 (Year: 2004, Number: 172)
Era: 2004-2010
Section: Melléklet a 2004. évi CVII. törvényhez
Paragraph Index: 252

9. Ge ne ral op ti ons for re duc ti on of sulp hur emis si ons are: (i) Energy ma na ge ment me a su res:* (a) Energy sav ing The ra ti o nal use of energy (imp ro ved energy ef fi ci en cy/pro cess ope rat ion, co ge ne ra ti on and/or de mand-si de ma na ge ment) usu ally re sults in a re duc ti on in sulp hur emis si ons. (b) Energy mix In ge ne ral, sulp hur emis si ons can be re du ced by inc re a sing the pro port ion of non-com bus ti on energy so ur ces (i.e. hyd ro, nuc le ar, wind, etc.) to the energy mix. Ho we ver, furt her en vi ron men tal im pacts have to be con si de red. (ii) Tech no lo gi cal op ti ons: (a) Fuel swit ching The SO2 emis si ons du ring com bus ti on are di rectly re la ted to the sulp hur con tent of the fuel used. Fuel swit ching (e.g. from high- to low-sulp hur co als and/or li qu id fu els, or from coal to gas) le ads to lo wer sulp hur emis si ons, but the re may be cer ta in rest ric ti ons, such as the ava i la bi lity of low-sulp hur fu els and the adap ta bi lity of exis ting com bus ti on sys tems to dif fe rent fu els. In many ECE co unt ri es, some coal or oil com bus ti on plants are be ing rep la ced by gas-fi red com bus ti on plants. Du al-fu el plants may fa ci li ta te fuel swit ching. (b) Fuel cle a ning Cle a ning of na tu ral gas is sta te-of-the-art tech no logy and wi dely app li ed for ope ra ti o nal re a sons. Cle a ning of pro cess gas (acid re fi ne ry gas, coke oven gas, bi o gas, etc.) is also sta te-of-the-art tech no logy. De sulp hu ri za ti on of li qu id fu els (light and midd le frac ti ons) is sta te-of-the-art tech no logy. De sulp hu ri za ti on of he a vy frac ti ons is tech ni cally fe a sib le; ne vert he less, the cru de pro per ti es sho uld be kept in mind. De sulp hu ri za ti on of at mosp he ric re si due (bot tom pro ducts from at mosp he ric cru de dis til la ti on units) for the pro duc ti on of low-sulp hur fuel oil is not, ho we ver, com monly prac ti sed; pro ces sing low-sulp hur cru de is usu ally pre fe rab le. Hyd ro-crac king and full con ver si on tech no logy have mat ured and com bi ne high sulp hur re ten ti on with imp ro ved yi eld of light pro ducts. The num ber of full con ver si on re fi ne ri es is as yet li mi ted. Such re fi ne ri es typi cally re co ver 80 per cent to 90 per cent of the sulp hur in ta ke and con vert all re si du es into light pro ducts or ot her mar ke tab le pro ducts. For this type of re fi ne ry, energy con sump ti on and in vest ment costs are inc re a sed. Typi cal sulp hur con tent for re fi ne ry pro ducts is gi ven in table 1. TABLE 1 Sulphur content from refinery products [S content (per cent)] Typi cal pre sent va lu es An ti ci pa ted fut ure va lu es 0.1 0.05 0.1 0.01 0.05–0.3 < 0.05 0.1–0.2 < 0.1 0.2–3.5 < 1 0.5–1.0 < 0.5 3.0–5.0 < 1 (co as tal are as) < 2 (high seas) Cur rent tech no lo gi es to cle an hard coal can re mo ve app ro xi ma tely 50 per cent of the inor ga nic sulp hur (de pen ding on coal pro per ti es) but none of the or ga nic sulp hur. More ef fec ti ve tech no lo gi es are be ing de ve lo ped which, ho we ver, in vol ve hig her spe ci fic in vest ment and costs. Thus the ef fi ci en cy of sulp hur re mo val by coal cle a ning is li mi ted com pa red to flue gas de sulp hu ri za ti on. The re may be a co unt ry-spe ci fic op ti mi za ti on po ten ti al for the best combination of fuel cleaning and flue gas cleaning. (c) Ad van ced com bus ti on tech no lo gi es The se com bus ti on tech no lo gi es with imp ro ved ther mal ef fi ci en cy and re du ced sulp hur emis si ons inc lu de: flu i di zed-bed com bus ti on (FBC): bubb ling (BFBC), cir cu la ting (CFBC) and pres su ri zed (PFBC); in teg ra ted ga si fi ca ti on com bi ned-cyc le (IGCC); and combined-cycle gas turbines (CCGT). Sta ti o na ry com bus ti on tur bi nes can be in teg ra ted into com bus ti on sys tems in exis ting con ven ti o nal po wer plants which can inc re a se ove rall ef fi ci en cy by 5 per cent to 7 per cent, le ad ing, for examp le, to a sig ni fi cant re duc ti on in SO2 emis si ons. Ho we ver, ma jor al te ra ti ons to the existing furnace system become necessary. 2004/172. szám * Op ti ons (i) (a) and (b) are in teg ra ted in the energy struc tu re and po li cy of a Party. Imp le men ta ti on sta tus, ef fi ci en cy and costs per sec tor are not con - si de red here. Flu i di zed-bed com bus ti on is a com bus ti on tech no logy for bur ning hard coal and brown coal, but it can also burn ot her so lid fu els such as pet ro le um coke and low-gra de fu els such as was te, peat and wood. Emis si ons can ad di ti o nally be re du ced by in teg ra ted com bus ti on cont rol in the sys tem due to the ad di ti on of lime/li mes to ne to the bed ma te ri al. The to tal ins tal led ca pa city of FBC has re a ched app ro xi ma tely 30,000 MWth (250 to 350 plants), inc lu ding 8,000 MWth in the ca pa city rang e of gre a ter than 50 MWth. By-pro ducts from this pro cess may ca u se prob lems with res pect to use and/or disposal, and further development is required. The IGCC pro cess inc lu des coal ga si fi ca ti on and com bi ned-cyc le po wer ge ne ra ti on in a gas and ste am tur bi ne. The ga si fi ed coal is burnt in the com bus ti on cham ber of the gas tur bi ne. Sulp hur emis si on cont rol is achi e ved by the use of sta te-of-the-art tech no logy for raw gas cle a ning fa ci li ti es upst re am of the gas tur bi ne. The tech no logy also exists for he a vy oil re si du es and bi tu men emul si ons. The ins tal led ca pa city is pre sently abo ut 1,000 MWel (5 plants). Com bi ned-cyc le gas-tur bi ne po wer sta ti ons using na tu ral gas as fuel with an energy ef fi ci en cy of app ro xi ma tely 48 per cent to 52 per cent are cur rently being planned. (d) Pro cess and com bus ti on mo di fi ca ti ons Com bus ti on mo di fi ca ti ons com pa rab le to the me a su res used for NOx emis si on cont rol do not exist, as du ring com bus ti on the or ga ni cally and/or inor ga ni cally bo und sulp hur is al most comp le tely oxi di zed (a cer ta in per cen ta ge de pen ding on the fuel pro per ti es and com bus ti on technology is retained in the ash). In this an nex dry ad di ti ve pro ces ses for con ven ti o nal bo i lers are con si de red as pro cess mo di fi ca ti ons due to the in jec ti on of an agent into the com bus ti on unit. Ho we ver, ex pe ri en ce has shown that, when app lying the se pro ces ses, ther mal ca pa city is lo we red, the Ca/S ra tio is high and sulp hur re mo val low. Prob lems with the furt her uti li za ti on of the by-pro duct have to be con si de red, so that this so lu ti on sho uld usu ally be app li ed as an intermediate measure and for smaller units (table 2). (e) Flue gas de sulp hu ri za ti on (FGD) pro ces ses The se pro ces ses aim at re mo ving al re a dy for med sulp hur oxi des, and are also re fer red to as se con da ry me a su res. The sta te-of-the-art tech no lo gi es for flue gas tre at ment pro ces ses are all ba sed on the re mo val of sulp hur by wet, dry or se mi-dry and catalytic chemical processes. To achi e ve the most ef fi ci ent pro gram me for sulp hur emis si on re duc ti ons be y ond the energy ma na ge ment me a su res lis ted in (i) abo ve a com bi na ti on of tech no lo gi cal op ti ons iden ti fi ed in (ii) above should be considered. In some ca ses op ti ons for re du cing sulp hur emis si ons may also re sult in the re duc ti on of emis si ons of CO2, NOx and ot her pollutants. In pub lic po wer, co ge ne ra ti on and dist rict he a ting plants, flue gas tre at ment pro ces ses used inc lu de: lime/li mes to ne wet scrub bing (LWS); spray dry ab sorp ti on (SDA); Well man Lord pro cess (WL); am mo nia scrub bing (AS); and com bi ned NOx/SOx re mo val pro ces ses (ac ti va ted car bon pro cess (AC) and com bi ned ca taly tic NOx/SOx removal). In the po wer ge ne ra ti on sec tor, LWS and SDA co ver 85 per cent and 10 per cent, res pec ti vely, of the ins tal led FGD capacity. Se ve ral new flue gas de sulp hu ri za ti on pro ces ses, such as elect ron beam dry scrub bing (EBDS) and Mark 13A, have not yet pas sed the pi lot stage. Tab le 2 shows the ef fi ci en cy of the abo ve-ment io ned se con da ry me a su res ba sed on the prac ti cal ex pe ri en ce gat he red from a lar ge num ber of imp le men ted plants. The imp le men ted ca pa city as well as the ca pa city rang e are also ment io ned. Des pi te com pa rab le cha rac te ris tics for se ve ral sulp hur aba te ment tech no lo gi es, lo cal or plant-spe ci fic inf lu en ces may lead to the exclusion of a given technology. Tab le 2 also inc lu des the usu al in vest ment cost ran ges for the sulp hur aba te ment tech no lo gi es lis ted in sec ti ons (ii) (c), (d) and (e). Ho we ver, when app lying the se tech no lo gi es to in di vi du al ca ses it sho uld be no ted that in vest ment costs of emis si on re duc ti on me a su res will de pend amongst ot her things on the par ti cu lar tech no lo gi es used, the re qu i red cont rol sys tems, the plant size, the ex tent of the re qu i red re duc ti on and the ti me-sca le of plan ned ma in te nan ce cyc les. The tab le thus gi ves only a bro ad rang e of in vest ment costs. In vest ment costs for ret ro fit ge ne rally ex ce ed tho se for new plants. 2004/172. szám TABLE 2 Emissions of sulphur oxides obtained from the application of technological options to fossil-fuelled boilers Uncontrolled emissions Additive injection Wet scrubbinga Spray dry absorptionb Reduction efficiency (%) up to 60 up to 90 Energy efficiency (kWel/103 m3/h) 0.1-1 6-10 3-6 Total installed capacity (ECE Eur) (MWth) 194,000 16,000 Type of by-product Mix of Ca salts and fly ashes Gypsum (sludge/waste water) Mix of CaSo3 * 1/2 H2O and fly ashes Specific investment (cost ECU(1990)/kWel) 20-50 60-250 50-220 mg/m3 c g/kWhel mg/m3 c g/kWhel mg/m3 c g/kWhel mg/m3 c g/kWhel Hard coald 1,000-10,000 3.5-35 400-4,000 1.4-14 < 400 <1.4 < 400 < 1.4 (< 200, 1% S) < 0.7 (< 200, 1% S) < 0.7 Brown coald 1,000-20,000 4.2-84 400-8,000 1.7-33.6 < 400 <1.7 < 400 < 1.7 (< 200, 1% S) <0.8 (< 200, 1% S) <0.8 Heavy oild 1,000-10,000 2.8-28 400-4,000 1.1-11 < 400 <1.1 < 400 <1.1 (< 200, 1% S) <0.6 (< 200, 1% S) <0.6 Ammonia scrubbingb Wellman Lorda Activated carbona Combined catalytica Reduction efficiency (%) up to 90 Energy efficiency (kWel/103 m3/h) 3-10 10-15 4-8 Total installed capacity (ECE Eur) (MWth) 2,000 1,300 Type of by-product Ammonia fertilizer Elemental S Sulphuric acid (99 vol.%) Elemental S Sulphuric acid (99 vol.%) Sulphuric acid (70 wt.%) 2004/172. szám Specific investment (cost ECU(1990)/kWel) 230-270e 200-300 e 280-320 e f 320-350 e f mg/m3 c g/kWhel mg/m3 c g/kWhel mg/m3 c g/kWhel mg/m3 c g/kWhel Hard coald < 400 < 1.4 < 400 < 1.4 < 400 < 1.4 < 400 < 1.4 (< 200, 1% S) < 0.7 (< 200, 1% S) < 0.7 (< 200, 1% S) < 0.7 (< 200, 1% S) < 0.7 Brown coald < 400 < 1.7 < 400 < 1.7 < 400 < 1.7 < 400 < 1.7 (< 200, 1% S) < 0.8 (< 200, 1% S) < 0.8 (< 200, 1% S) < 0.8 (< 200, 1% S) < 0.8 Heavy oild < 400 < 1.1 < 400 < 1.1 < 400 < 1.1 < 400 < 1.1 (< 200, 1% S) < 0.6 (< 200, 1% S) < 0.6 (< 200, 1% S) < 0.6 (< 200, 1% S) < 0.6 a For high sulphur content in the fuel the removal efficiency has to be adapted. However, the scope for doing so may be process-specific. Availability of these processes is usually 95%. b Limited applicability for high-sulphur fuels. c Emission in mg/m3 (STP), dry, 6% oxygen for solid fuels, 3% oxygen for liquid fuels. d Conversion factor depends on fuel properties, specific fuel gas volume and thermal efficiency of boiler (conversion factors (m3/kWhel, thermal efficiency: 36%) used: hard coal: 3.50; brown coal: 4.20; heavy oil: 2.80). e Specific investment cost relates to a small sample of installations. f Specific investment cost includes denitrification process. The table was established mainly for large combustion installations in the public sector. However, the control options are also valid for other sectors with similar exhaust gases. 2004/172. szám IV. Control techniques for other sectors

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