Sulphuric Acid Manufacture

Southern African Pyrometallurgy 2006, Edited by R.T. Jones, South African Institute of Mining and Metallurgy, Johannesburg, 5-8 March 2006 1 Sulphuric Acid Manufacture W.G. Davenport University of Arizona, Tucson, Arizona, USA M.J. King Hatch, Perth, Australia B. Rogers Hatch, Mississauga, Ontario, Canada A. Weissenberger Hatch, Woodmead, South Africa Keywords: Pyrometallurgy, sulphuric acid, sulphur dioxide Abstract – The raw material for sulphuric acid manufacture is clean SO2 gas. It comes from (i) burning molten by-product sulphur; (ii) roasting or smelting metal sulphide concentrates, and (iii) decomposing contaminated organic chemical process sulphuric acid catalyst. Efficient gas cleaning is required for metallurgical and contaminated acid decomposition gases, especially the former. Sulphuric acid is made from SO2 gas by (i) oxidizing the SO2(g) to SO3(g) in contact with supported liquid-phase catalyst then (ii) reacting the resulting SO3(g) with the water component of 98.5 mass% H2SO4, 1.5 mass% H2O acid. This paper discusses the reasons for these process steps and indicates how acidmaking can be controlled and optimized. Special emphasis is placed on SO2(g) oxidation efficiency and how it is influenced by feed gas composition, feed gas temperature, catalyst composition, catalyst bed pressure, number of catalyst beds, and double versus single contact acidmaking. In addition, a review of various other treatment methods for SO2-bearing gases is provided. A brief description of each process is included along with commentary on their technical and economic applicability for use at metallurgical facilities. PART I: SULPHURIC ACID PRODUCTION FROM STRONG SO2 GAS Around 200 million metric tons of sulphuric acid is manufactured per year – most of it from strong SO2 (~10%) gas.1 South Africa produces and consumes around 3 million tons per year of sulphuric acid.2 A majority of the acid is used for making phosphate fertilizers, but it has a myriad of other uses. Raw Materials, Products The starting material for sulphuric acid manufacture is clean, dry SO2, 8 to 12% in O2, N2, SO2, CO2, SO3 gas. It is obtained: (a) by burning molten waste elemental sulphur (~70% of world production) (b) from high SO2 strength metallurgical off-gases (~20%) (c) by decomposing spent (used) sulphuric acid catalyst (~10%). 2 (a) and (c) beneficially make a useful product from waste. (b) beneficially removes SO2 from smelting and roasting off-gases. The product of sulphuric acid manufacture is liquid acid, 93 to 98% H2SO4, 2 to 7% H2O. Manufacturing Process Sulphuric acid manufacturing consists of: (a) gas cleaning and removal of H2O(g) by condensation (b) gas dehydration with sulphuric acid desiccant, i.e.: ~320 K H2O(g) + H2SO4(l) ‡ H2SO4(l) + H2O(l) [1] in strong slightly weakened acid acid DH = -80 MJ per kg-mole H2O(g) (c) oxidation of SO2 to SO3 in contact with supported liquid phase catalyst, i.e.: 700-900 K SO2(g) + ½ O2(g) ‡ SO3(g) [2] in SO2, O2, in feed gas or catalyst in SO3, SO2, N2 feed gas added to it O2, N2, gas in air DH = -100 MJ per kg-mole SO2(g) (d) reaction of (c)'s SO3 product with strong sulphuric acid to make strengthened sulphuric acid, i.e.: 350-380 K SO3(g) + H2O(l) ‡ H2SO4(l) [3] in SO3, SO2 in 1.5% H2O, in strengthened O2, N2, gas 98.5% H2SO4 sulphuric acid sulphuric acid DH = -130 MJ per kg-mole H2SO4(l) (e) mixing of (b)'s and (d)'s liquid products (+ water) to make the acid plant's range of products. Gas Cleaning The gas entering dehydration must be dust free (0.001 to 0.01 g/Nm3 of gas) to avoid plugging downstream SO2-oxidation catalyst. Dust is removed from the gas by a series of electrostatic precipitation and scrubbing steps. Metallurgical off-gas requires the most attention. Sulphur burning requires the least. Sulphuric acid catalyst decomposition gas is intermediate. 3 Condensation and Dehydration Acid plants must be built and operated so that liquid sulphuric acid is not produced in unexpected locations in equipment and flues. The easiest way to ensure this is to remove all H2O(g) from catalytic SO2 oxidation input gas. It is removed by water-cooling condensation then dehydration with sulphuric acid desiccant. Typical H2O(g)-in-gas levels entering catalytic SO2 oxidation are ~50 mg H2O(g) per Nm3 of input gas. In sulphur burning acid plants, it is the sulphur combustion air that is dehydrated (with no prior condensation). Catalytic SO2 + ½ O2 ‡ SO3 Oxidation SO2 is oxidized to SO3 in preparation for H2SO4 making. The oxidation is done by blowing clean dry SO2 gas down through horizontal beds of Figure 1 catalyst. Industrially, the beds are typically 0.8 m thick and 10 m diameter. Figure 1: Photograph of catalyst pieces, courtesy Haldor Topsøe A/S http://www.haldortopsøe.com The outside diameter of the largest piece (far left) is 20 mm. Figure 2 is a stoichiometry-equilibrium curve for SO2 oxidation. It shows that the reaction goes almost to completion at 600 K but not at 1000 K. This indicates that raising reaction temperature to increase reaction rate is counter-acted by a large decrease in maximum attainable (equilibrium) SO3 production. This problem is overcome by using catalyst, which promotes rapid SO2 oxidation at cool temperatures (~700 K) where equilibrium SO3 production is efficient. The catalyst is molten V, K, Na, Cs, S, O solution on porous silica substrate. A simplified reaction scheme with this catalyst is: SO2 + 2V5+ + O2- ‡ 2V4+ + SO3 [4] ½ O2 + 2V4+ ‡ 2V5+ + O2- [5] which combine to give: SO2 + ½ O2 ‡ SO3 [2] Reactions [4] and [5] have lower activation energies than Reaction [5], giving rapid reaction at 700-900 K. 4 25 50 75 100 600 700 800 900 1000 Equilibrium temperature, K F E , equilibrium % S O2 o xidiz ed equilibrium curve Feed gas 10 volume% SO2 11 volume% O2 remainder = N2 1.2 bar equilibrium pressure Figure 2: Maximum percentage of SO2-in-feed-gas that can be oxidized when equilibrium is attained in a bed of Figure 1 catalyst. It decreases markedly with increasing temperature. The curve applies only to the specified conditions. Catalyst Temperature Limitations The V, K, Na, Cs, S, O catalyst must be molten for Reactions [4] and [5] to occur. It typically melts around 680 K, slightly cooler when it contains cesium ions. Unfortunately, it begins to lose its catalytic power above about 900 K due to the formation of unreactive vanadate ions and by non-reversible reaction with the silica substrate. Thus, SO2 oxidation must be done between ~700 and 900 K. The industrial implications of this are discussed below. H2SO4 Making In principle, H2SO4(l) can be made by reacting the SO3(g) from catalytic oxidation with water. However, Reaction [3] is so exothermic that the product of reacting strong SO3 with water would be hot H2SO4 vapour. Condensation of H2SO4(l) from this vapour is slow and expensive, so the SO2-water process is not used for strong gas. Instead, the SO3(g) is reacted with the H2O(l) in strong sulphuric acid. The small amount of H2O and the massive amount of H2SO4 in Reaction [3]'s input acid avoids this problem. The small amount of H2O limits the extent of the reaction. The large amount of H2SO4 warms only 25 K while it absorbs Equation [3]'s heat of reaction. The above sections describe the basic steps of sulphuric acid manufacture. The rest of Part I discusses: 5 (a) single- and multi-catalyst bed SO2 + ½ O2 ‡ SO3 oxidation (b) single and double contact acidmaking (c) optimization. Single- and Multi-Catalyst SO2 + ½ O2 ‡ SO3 Oxidation Figures 3 and 4 describe single catalyst bed SO2 oxidation. Figure 3 shows that warm SO2, O2, N2 gas descends the hot catalyst bed causing: (a) its SO2 to be oxidized (b) the gas to be heated by the exothermic oxidation reaction. Figure 3: 'Bed' of catalyst pieces for oxidizing SO2 to SO3. Industrial beds are 7-17 m diameter. Figure 4 describes this behaviour on Figure 2's stoichiometry-equilibrium curve graph. It shows that: (a) the gas warms as percent SO2 oxidation increases (b) maximum (equilibrium) SO2 oxidation is achieved at ~890 K with about 70% of the input SO2 having been oxidized to SO3. This demonstrates that only ~70% of input SO2 can be oxidized to SO3 in a single catalyst bed no matter how thick the bed. SO2 + 1/2O2 -> SO3 + heat CLEAN, DRY SO2 , O2 , N2 GAS ~700 K PARTIALLY OXIDIZED SO3 , SO2 , O2 , N2 GAS ~900 K 1/2 - 1 m 0.02 - 0.04 m 25 mm SILICA ROCK OR CERAMIC PIECES 25 mm SILICA ROCK OR CERAMIC PIECES STAINLESS STEEL SUPPORT GRID 10 - 12 MM CATALYST (FIGURE 1) STAINLESS STEEL 'CONVERTER' WALL 6 0 20 40 60 80 100 600 700 800 900 1000 Gas temperature, K F, % S O2 o xidiz ed Feed gas 10 volume% SO2 11 volume% O2 79 volume% N2 1.2 bar equilibrium pressure equilibrium curve heatup path 69.2% SO2 oxidized intercept 893.3 K 690 K feed gas Figure 4: First catalyst bed heat-up path, equilibrium curve and equilibrium intercept point. Only ~70% of input SO2 can be oxidized in a single catalyst bed. Multicatalyst bed oxidation with cooling between brings this up to 99+%, Figure 8. It can be deduced from this graph that a lower gas input temperature (say 670 K) will give a lower gas output temperature and a higher SO2 oxidation efficiency. The only practical way to circumvent this limitation is to use three or four sequential catalyst beds with gas cooling between, Figures 5 and 6. Figure 5: Schematic of single contact, 3 catalyst bed sulphuric acid plant. It is a single contact acid plant because it has only one H2SO4 making step. Note gas cooling between catalyst beds. It is this that permits additional SO2 oxidation in the next catalyst bed. 1ST CATALYST BED SO2 + 1/2O2 -> SO3 + heat 3RD CATALYST BED SO2 + 1/2O2 -> SO3 + heat 2ND CATALYST BED SO2 + 1/2O2 -> SO3 + heat IMPERVIOUS PLATE IMPERVIOUS PLATE GAS COOLING GAS COOLING HEAT ~890 K, ~70% SO2 OXIDIZED 700 K ~770 K, ~95% SO2 OXIDIZED 710 K 690 K SO2 , O2 , N2 GAS ~720 K, SO3 BEARING GAS TO COOLING & H2 SO4 MAKING ~98% SO2 OXIDIZED HEAT 7 60 70 80 90 100 600 700 800 900 1000 Gas temperature, K F, % S O2 o xidiz ed 2-3 cooldown 3 rd heatup 1-2 cooldown 2 nd heatup 1 st heatup 98.0% SO2 oxidized 94.2% SO2 oxidized 69.2% SO2 oxidized Figure 6: SO2 oxidation efficiency in Figure 5's three catalyst bed acid plant. The efficiency increases with each succeeding bed, but with diminishing gain. A 4th bed will further increase efficiency, but it is better to remove the gas's SO3 beforehand. This is the advantage of a double contact acid plant, Figure 7. Single Contact vs Double Contact Acidmaking Figure 5 is a schematic flowsheet of a single contact acidmaking plant. SO3 gas and 1.5% H2O, 98.5% H2SO4 acid are contacted only once. Figure 7 is a schematic flowsheet of a double contact plant. Figure 7: Schematic of 3-1 double contact acid plant. The increase in total SO2 oxidation after each bed is notable. Note the intermediate H2SO4 making step, bottom right. SO3 gas and 1.5% H2O, 98.5% H2SO4 acid are contacted twice with SO2 + ½ O2 ‡ SO3 oxidation between contacts. 1ST CATALYST BED SO2 + 1/2O2 -> SO3 + heat 3RD CATALYST BED SO2 + 1/2O2 -> SO3 + heat 2ND CATALYST BED SO2 + 1/2O2 -> SO3 + heat IMPERVIOUS PLATE IMPERVIOUS PLATE GAS COOLING GAS COOLING HEAT ~890 K, ~70% SO2 OXIDIZED 700 K ~770 K, ~95% SO2 OXIDIZED 710 K HEAT 690 K SO2 , O2 , N2 GAS 4TH CATALYST BED SO2 + 1/2O2 -> SO3 + heat GAS COOLING INTERMEDIATE H2SO4 MAKING, 99.9% SO3 REMOVAL AS H2SO4 GAS (l) WARMING ~700 K, SO3 BEARING GAS TO COOLING & FINAL H2 SO4 MAKING ~99.9% SO2 OXIDIZED IMPERVIOUS PLATE ~720 K, ~98% SO2 OXIDIZED 690 K 8 Advantage of Double Contact Acidmaking Figure 8 shows the advantage of double contact acidmaking. A four catalyst bed (4 – 0) single contact plant oxidizes only 99% of its feed SO2 causing 1% of the feed SO2 to leave in acid plant off-gas. The Figure 7 (3 – 1) contact plant, on the other hand, oxidizes 99.9% of its feed SO2, causing less than 0.1% of the feed SO2 to leave the acid plant. This is based on achieving equilibrium in each catalyst bed. It does so because the feed gas to its after H2SO4 making catalyst bed contains zero SO3 – allowing Reaction (2) to go almost to completion after intermediate H2SO4 making. 98.5 99 99.5 100 0 1 2 3 Beds before intermediate H2SO4 making - beds after F total , % S O2 o xidized after all catalyst beds 4 - 0 1 - 3 2 - 2 3 - 1 690 K input gas, all beds Figure 8: SO2 oxidation efficiencies after all catalyst beds. 4 – 0 is a single contact plant with four catalyst beds. 3 – 1 is a double contact plant with three beds before intermediate H2SO4 making and one bed after intermediate H2SO4 making etc. The superior performance of double contact acid plants is notable. The optimum performance of the 3 – 1 arrangement is also notable. Final Comments Sulphuric acid manufacture is most efficient when the acid plant is run continuously with ultra clean feed gas and ultra efficient dehydration. Cool catalyst bed input gas temperatures (with low melting point Cs-enhanced catalyst) also help. They increase SO2 oxidation efficiency and avoid destructive overheating of the catalyst. Acid plants are now being designed to capture every last MJ of energy. This endeavour should not, however, be allowed to interfere with continuous plant operation especially with metallurgical plants – where the valuable product is metal, not acid. 9 PART II: OTHER TREATMENT METHODS FOR SO2 BEARING GASES Lower strength (0.5 – 5 vol.% SO2) gases are not continuously treated in traditional contact-type acid plants. Their low SO2 strength requires a noneconomical amount of supplemental fuel to be burned to maintain the catalyst beds at optimum SO2 oxidation temperatures. In addition, the complexity and capital cost of acid production may not be justified for low tonnage applications. Site-specific factors may not favour direct sulphuric acid production, e.g., remote sites with poor or negative acid netbacks. Therefore, many alternative SO2 treatment methods have been developed. Most technologies have evolved as a result of the requirements of a number of industries and their specific process and regulatory mandates. SO2 removal utilizing treatment methods other than contact acid plant technology is common in petroleum, power generation, incineration, as well as pulp and paper and is continuing to become more common in metallurgical installations. Each industry has specific process characteristics and scrubbing needs. Many of the technical problems encountered in the past with scrubbing are the result of the misapplication of a scrubbing process. For example, a limestone slurry scrubber that works well on the steady, weak SO2 strength gas generated in a coal-fired boiler will not be suitable for the stronger, fluctuating gas produced by metallurgical processes. The selection of an SO2 scrubbing technology is usually a difficult task due to the large number of processes available (about 80 are presently commercially active). Some of them include: a) Scrubbing, producing by-products and/or wastes: o Direct Lime Slurry o Direct Limestone Slurry o ‘Dry’ sorbent, including spray drying and circulating dry scrubbers o Once-through Sodium o Magnesium Oxide o Various Dual Alkali processes o Seawater o Ammonia b) Regenerable processes producing high strength SO2 gas streams for further treatment in a contact acid plant or similar o Absorption/regeneration of SO2 in amine solutions o Wellman-Lord o Non-amine, organic scrubbing (e.g. Solinox®) c) Other acid producing processes such as: o Sulfacid® o Peroxide scrubbing o Petersen-Fattinger process o WSA (Wet gas Sulphuric Acid) 10 Several of the above processes have been used in the metallurgical industry in South Africa, including the following installations: Table I: Summary of South African metallurgical SO2 treatment processes Location Process Gases Treated Gas Volume Nm3/h Inlet SO2 Concentration vol.%, dry basis Start-up Date Lonmin Platinum Sodium-lime, concentrated mode dual alkali Electric furnace and converter 200 000 2 2003 Impala Platinum Sulfacid® Electric Furnace 50 000 1 2002 Anglo Platinum, Waterval Smelter PetersenFattinger Electric Furnace 65 000 0.5 - 1 2002 Scrubbing Table II presents an overview of some common commercial scrubbing processes grouped into their general class. It must be noted that there are several variations of each class. The key features of these processes are summarized below: · Lime slurry and limestone scrubbing is suitable for relatively low SO2 concentrations and moderate collection efficiencies. They have very high liquid circulation rates, can often be designed for zero effluent discharge, and can produce a marketable quality of gypsum. · Spray drying and circulating dry scrubbers are applicable to hot gases with a significant amount of evaporative capacity. SO2 absorption occurs as water evaporates leaving behind a dry mixture of sulphate and sulphite solids. Because final collection occurs in a baghouse (or ESP), there is no segregation of process and CaSO3/CaSO4 solids. · While there are several types of dual alkali processes in operation, they all use a soluble scrubbing agent (usually sodium or aluminum based), which is regenerated by reaction with another alkali (usually calcium based). These processes offer the advantages of solution scrubbing, a solid by-product and the ability to handle higher strength SO2 gases. These advantages come at the cost of a more complex process. · Once through sodium processes use soda ash or caustic and produce a solution of soluble sodium salts. They are simple and effective, but use a costly reagent, and have a liquid effluent. Seawater scrubbers are actually a form of this, making use of natural alkalinity in seawater (sodium bicarbonate). 11 A number of decisions are required to select and define the most appropriate scrubbing technology for any given application. Key considerations in the selection process are as follows: · Process operating conditions; of particular importance are SO2 concentrations and the nature of fluctuations. Lime/limestone systems are typically limited to fairly weak gas of less than 6 000 to 8 000 ppm SO2 and can be adversely affected by rapid changes in concentration. Temperature and water content impact the evaporative capacity of the gas and, therefore, the ability to achieve a water balance with zero water discharge. · Performance requirements; outlet SO2 targets in terms of concentration and efficiency needed to achieve this target. · Disposal issues; both solid waste characteristics/disposal costs and wastewater issues need to be comprehended as part of the process selection. · Process reliability/availability; many SO2 scrubbing systems have incurred significant downtime, usually due to scaling. · Operating versus capital costs, particularly as they relate to reagent, disposal and power costs. · Site specific factors; there are usually a number of specific issues at each facility that require consideration. Existing equipment and auxiliary facilities, availability of reagents, water treatment facilities and disposal/re-use of by-products. Many scrubbers produce a material that can be marketed, partially off-setting the operating cost of the scrubber and more importantly, eliminating waste disposal problems. The most common saleable by-product is gypsum for use in cement or wallboard manufacture. Nearly 75% of the gypsum produced by flue gas desulphurization (FGD) in the United States is used in wallboard. Another, less common, saleable by-product is ammonium sulphate (NH4)2SO4 produced by scrubbing SO2 bearing gases with ammonia. The process is typically used for treating tail gases from contact type acid plants associated with fertilizer production facilities. Table II: Overview of Scrubbing Processes Process Reagents ByProducts Principal Reactions (H2O Not Always Shown) Applicable Inlet SO2 (ppm) Proven Efficiency (%) Order of Magnitude Capital Cost US$/Nm3/h Order of Magnitude Operating Cost US$/t SO2 Typical Scrubbing Vessel Lime Slurry CaO CaSOx CaO + SO2 = CaSO3 2H2O + CaSO3 + ½O2 = CaSO4▪2H2O <100-10 000 90-97 100-150 175 Open Spray Tower Limestone Slurry CaCO3 CaSOx (gypsum) CaCO3 + SO2 = CaSO3 + CO2 2H2O + CaSO3 + ½O2 = CaSO4▪2H2O 1000-6 000 ~95 100-150 150 Open Spray Tower Spray Drying – Lime CaO CaSOx ½H2O + CaO + SO2 = CaSO3▪½H2O 2H2O + CaSO3 + ½O2 = CaSO4▪2H2O ><100-3 000 90-95 125-200 200 Spray Tower + Bag-house Dual Alkali (Lime Sodium) CaO NaOH Na2CO3 CaSOx (gypsum) 2NaOH + SO2 = Na2SO3 + H2O H2O + Na2SO3 + SO2 = 2NaHSO3 2NaHSO3 + Ca(OH)2 = Na2SO3 + CaSO3▪½H2O + 1½ H2O Na2SO3 + Ca(OH)2 = 2NaOH + CaSO3 1 200- 150 000 + 99+ 125-175 175 Tray or Packed Tower Dual Alkali (Dowa) CaCO3 Al2(SO4)3 CaSO4▪ 2H2O Al2O3 Al2(SO4)3 + 3SO2 + 3/2 O2 = 2Al2(SO4)3 2Al2(SO4)3 + 3CaCO3 = Al2(SO4)3▪Al2O3 + 3CaSO4 + 3CO2 1 000-25 000 85-98 150 190 Tray or Packed Tower Once Through Seawater NaHCO3 (CaO) Na2SO3 Na2SO4 2NaHCO3 + SO2 = Na2SO3 + 2CO2 + H2O Na2SO3 + ½O2 = Na2SO4 up to ~2 000 ~98 very site specific 60-120 Tray or Packed Tower Once Through Sodium NaOH Na2CO3 Na2SO3 Na2SO4 2NaOH+SO2 = Na2SO3+H2O Na2SO3 + ½O2 = Na2SO4 ><100- 10 000+ 99+ 40-80 350-480 Tray or Packed Tower 13 Regenerable Processes Amine absorb/desorb (Cansolv® 3 and TurboSOx® 4) use amines to absorb SO2 gas in a packed or tray tower absorber. The SO2 rich amine is transferred to a desorb column and steam heated to strip high purity SO2 gas and water vapour from the amine. The lean amine is returned to the absorber. The high strength SO2 is cooled to condense water vapour and ducted to another facility, e.g. acid plant for additional processing to make sulphuric acid. Amine absorb/desorb is well suited for treating gases with a wide range of fluctuating SO2 concentrations, but is logistically difficult for applications without an on-site acid plant or similar. The process utilizes solution-based absorption and should be reliable, although there are comparatively few installations at present. Other regenerable processes have a similar configuration, and similar implementation issues. Other Sulphuric Acid Processes Sulfacid® Process SO2, H2O and O2 react in an activated carbon catalyst to form H2SO4 in the Donau Carbon5 Sulfacid® process (Figure 9). The product of the process is weak (><20% H2SO4) sulphuric acid. Multiple activated carbon beds arranged in parallel are often used. The acid making reaction for the Sulfacid® process is as follows: SO2 + 2 1 O2 + nH2O ‡ H2SO4 ∙ (n-1)H2O [6] The process can treat feed gases with: · less than 1 volume% SO2 · a minimum 7 volume% O2, and · a maximum of 30 mg/Nm³ of dust minimizing activated carbon fouling. Figure 9: Sulfacid® process for removal of SO2. Feed gases are mixed with steam (if required) in the mixing chamber before entering the reactor holding the activated carbon catalyst. ACTIVATED CARBON MIXING CHAMBER HOLDING TANK STEAM (IF REQUIRED) WATER SO2 BEARING TAIL GAS CLEAN GAS TO ATMOSPHERE ><20%H2SO4 TO MARKETOR DILUTION IN ACID PLANT 14 Sulphuric acid is formed from the oxidation of SO2 in the presence of H2O and activated carbon. The acid formed on the activated carbon is washed into a holding tank where it is pumped to the acid plant’s acid circulation system for dilution or sold to customers. Sulfacid®’s advantages are its relatively low capital and operating cost and production of H2SO4. Its main disadvantage is that its acid product strength is weak ><20% H2SO4 making it difficult to sell to off-site customers. About 50 Sulfacid® plants are presently in operation. Peroxide Scrubbing Lurgi Metallurgie and Süd-Chemie developed the Peracidox®6 process specifically to remove residual SO2 from tail gases from double absorption sulphuric acid plants. The process uses hydrogen peroxide (H2O2) to oxidise SO2 to sulphuric acid: SO2 (g) + H2O2 (aq) ‡ H2SO4 (aq) [7] Scrubbing is achieved by direct contact in a counter-current spray tower. The peroxide reacts with SO2 in the first chamber and overflows to the second chamber. The bleed acid concentration is ~50% H2SO4, which can be recycled to the acid plant as dilution water or sold as a by-product should a market exist. A basic flow schematic is provided in Figure 10. Figure 10: Peracidox® process flow schematic. 50% H2O2 reacts with SO2 forming a 50% H2SO4 solution that is sent to the contact plant or market. Tail gases can be as low as 20 ppm SO2. H2SO4 vapour and SO3 are also removed from the feed gas stream. The advantages of the Peracidox® process include it’s simplicity, small footprint, high SO2 removal efficiency and low capital cost. Its biggest disadvantages are its high operating cost due to peroxide and its relatively low acid strength product (~50% H2SO4). For these reasons the Peracidox® process is most suited for acid plant tail-gas treatment where SO2 concentrations are consistently low or only temporarily high (e.g. during acid plant start-up). In FEED GAS 50% H2O2 PROCESS WATER TAIL GAS 50% H2SO4 CIRCULATING PUMP MIST ELIMINATOR 15 this case Peracidox® is economical because peroxide consumption is small and its initial capital costs are low. Petersen-Fattinger Process The chemistry of this process is based on the lead chamber process commonly used in the early 1900’s. SO2 and H2O bearing feed gases are contacted in a series of packed towers with 65% H2SO4 containing nitrosyl sulphuric acid (NOHSO4) to promote the formation of H2SO4 from SO2, O2 and H2O7. The acidmaking reaction generates NO(g) and NO2(g), which are subsequently reabsorbed into higher strength acid to form more acid catalyst. Nitric acid must be added to ensure correct levels of NOHSO4 are present for catalysis. Product acid is in the form of 70-76% H2SO4 with some nitrosyl present. The process advantages are its relatively high strength acid product (76% H2SO4) and low operating cost. Its disadvantages are its materials of construction sensitivity, presence of NOx in tail gas, presence of nitrosyl compounds in its product acid and, currently, only one large-scale commercial installation. WSA (Wet gas Sulphuric Acid) Haldor Topsøe’s WSA (Wet gas Sulphuric Acid)8 process treats wet, low SO2 concentration (0.2% - 6% SO2) gases. SO2 bearing gases are first cooled and cleaned in a gas cleaning plant before being heated, sent through a converter for catalytic oxidation of SO2 to SO3 and passing through a glass tube condenser where H2O in the gas combines with SO3 to produce strong (98% H2SO4) sulphuric acid. A basic flow diagram is provided in Figure 10. Figure 10: WSA process flow schematic. A natural gas burner is used to provide supplemental heat for catalytic SO2 oxidation. Heat generated in the catalyst beds during catalytic SO2 oxidation is recovered in a molten salt circulation system, which is used to heat incoming feed gas. 16 WSA’s advantages are its strong acid product (98% H2SO4) and its ability to treat wet, SO2 bearing gases ranging from 1.4% SO2 to 6.5% SO2 while oxidizing 98-99%9 of its incoming feed gas SO2. Its only disadvantage for metallurgical application is a limited number of installations. Final Comments Sulphur dioxide streams tend to fall into two categories – low strength and high strength. High strength gases (>5% SO2) are treated in contact type acid plants, where the total SO2 tonnage justifies the expense and complexity. Low strength gases (0 - 2% SO2) are typically treated in scrubbers with neutralizing agents producing various by-products, e.g. gypsum, or waste streams for disposal. Peracidox® and Sulfacid® processes are efficient at removing SO2 from gases, but produce weak H2SO4 making their use less widespread. The WSA process has the ability to produce strong 98% H2SO4 while treating a wide range of low SO2 strength (1.4% – 6.5%) gases making it an attractive process. Its use will likely continue to increase. REFERENCES 1. W.G. Davenport, M.J. King, Sulfuric Acid Manufacture, Analysis, Control and Optimization, Elsevier Science, 2005. 2. I. Robinson, N. Van Averbeke, A.J. Harding, J.A.G. Duval, P. Mwape, J.W. Perold, E.J. Roux, South Africa’s Mineral Industry 2003/2004, Department: Minerals and Energy Republic of South Africa, 2004, pp. 192. 3. http://www.cansolv.com 4. http://www.turbosonic.com 5. http://www.dcffm.de 6. http://www.outokumpu.com 7. V. Fattinger and W. Jäger, A Two-Stage Process Combination for the Production of Sulfuric Acid or Oleum with Next to Zero SO2 Emissions, Sulphur 98Conference Preprints Volume 2, British Sulphur, 1998, pp. 157-170. 8. http://www.topsøe.com 9. A. Kristiansen, Topsøe Wet gas Sulphuric Acid (WSA) Technology for Fixation of SO2 in Off-gases in the Metallurgical Industry, 2005, pp. 12.