WO2009065485A2 - Procédé et usine de production d'acide sulfurique - Google Patents

Procédé et usine de production d'acide sulfurique Download PDF

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Publication number
WO2009065485A2
WO2009065485A2 PCT/EP2008/009193 EP2008009193W WO2009065485A2 WO 2009065485 A2 WO2009065485 A2 WO 2009065485A2 EP 2008009193 W EP2008009193 W EP 2008009193W WO 2009065485 A2 WO2009065485 A2 WO 2009065485A2
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WO
WIPO (PCT)
Prior art keywords
acid
absorber
drying tower
sulfuric acid
plant
Prior art date
Application number
PCT/EP2008/009193
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English (en)
Other versions
WO2009065485A3 (fr
Inventor
Karl-Heinz Daum
Wolfram Schalk
Wolfgang Götz
Original Assignee
Outotec Oyj
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from DE102007058144A external-priority patent/DE102007058144A1/de
Application filed by Outotec Oyj filed Critical Outotec Oyj
Priority to MX2010005600A priority Critical patent/MX2010005600A/es
Priority to CN200880114711A priority patent/CN101848857A/zh
Priority to AU2008328289A priority patent/AU2008328289B2/en
Publication of WO2009065485A2 publication Critical patent/WO2009065485A2/fr
Publication of WO2009065485A3 publication Critical patent/WO2009065485A3/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/69—Sulfur trioxide; Sulfuric acid
    • C01B17/74—Preparation
    • C01B17/76—Preparation by contact processes
    • C01B17/80—Apparatus
    • C01B17/806—Absorbers; Heat exchangers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8603—Removing sulfur compounds
    • B01D53/8609—Sulfur oxides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/69—Sulfur trioxide; Sulfuric acid
    • C01B17/74—Preparation
    • C01B17/76—Preparation by contact processes
    • C01B17/765—Multi-stage SO3-conversion
    • C01B17/7655—Multi-stage SO3-conversion with intermediate absorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/302—Sulfur oxides

Definitions

  • This invention relates to a process and a plant for producing sulfuric acid from a gas containing sulfur dioxide, wherein the sulfur dioxide is catalytically oxidized in a converter to obtain sulfur trioxide, wherein the sulfur trioxide produced thereby preferably is absorbed in concentrated sulfuric acid in an intermediate absorber and the residual gas preferably is again supplied to a catalytic conver- sion stage, and wherein the sulfur trioxide produced then is absorbed in concentrated sulfuric acid in a final absorber.
  • sulfuric acid usually is effected by the so-called double absorption process as it is described in Winnacker/K ⁇ chler, Chemischetechnik:ificate und Kunststoff, Vol. 3: Anorganische Grundstoffe, Swiss effort, pp. 64 to 135.
  • Sulfur dioxide (SO 2 ) obtained as waste gas of metallurgical plants or by combustion of sulfur is converted to sulfur trioxide (SO 3 ) in a multistage converter by means of a solid catalyst, e.g. with vanadium pentoxide as active component.
  • the SO 3 obtained is withdrawn after the contact stages of the con- verter and supplied to an intermediate absorber or after the last contact stage of the converter to a final absorber, in which the gas containing SO 3 is guided in counterflow with concentrated sulfuric acid and is absorbed in the same.
  • the sulfur dioxide is obtained from waste gases of metallurgical plants, e.g. from the pyrometallurgical production of non-ferrous metals, e.g. from the calcination of sulfidic ores, the thermal decomposition of metal sulfates or alkali sulfates or from the processing of contaminated waste sulfuric acid by thermal decomposition, the gases initially are cleaned from impurities which might impair the quality of the sulfuric acid or impede the catalytic conversion to sulfur triox- ide.
  • the waste gas cleaned in this way then is dried in a drying tower with con- centrated sulfuric acid of e.g. 94-96 % H 2 SO 4 (the sulfuric acid concentration each is indicated in percent by weight), i.e.
  • the sulfur trioxide which in the subsequent converter is produced from sulfur dioxide and oxygen by catalytic oxidation, is absorbed in absorbers into concentrated sulfuric acid of e.g. 98.5 % H 2 SO 4 , with its concentration increasing in the process.
  • the residual gas is again supplied to a catalytic conversion stage, and in a final absorber the sulfur trioxide produced is liberated from the remaining SO 3 .
  • the final absorber is operated with concentrated sulfuric acid in the same way as the intermediate absorber, with the concentration of the sulfuric acid increasing here as well.
  • the water required for forming sulfuric acid from SO 3 and H 2 O and for dilution to about 98.5 % H 2 SO 4 is in part obtained from the gas/air humidity absorbed in the drying tower.
  • the rest is supplied to the intermediate absorber and/or the final absorber as process water.
  • the concentration of the sulfuric acid is kept constant.
  • a similar arrangement is used in plants for producing sulfuric acid on the basis of elementary sulfur.
  • air is dried in the drying tower and the oxygen con- tained therein is used for the combustion/oxidation of elementary sulfur to SO 2 - containing gas.
  • this sulfur dioxide then is catalytically converted to sulfur trioxide as described above and subsequently absorbed in the intermediate and final absorbers and converted to sulfuric acid.
  • Fig. 1 shows the acid-side circuitry of a typical conventional arrangement of the drying and absorption towers.
  • the gas-side circuitry is not shown.
  • Tables indicate the process parameters in conduits 1 to 14. In so far, Table 1 indicates the process parameters for a circuitry as shown in Fig. 1.
  • SO 2 -containing gas is supplied to the drying tower TT via a non- illustrated conduit, which gas is guided in counterflow with the sulfuric acid supplied via conduit 1 , which has a concentration of 96 % H 2 SO 4 .
  • the SO 2 - containing gas is dried thereby, and the steam contained therein leads to a dilution of the sulfuric acid which is withdrawn from the bottom of the drying tower TT via conduit 2 and supplied to an acid circulation tank T1.
  • the sulfuric acid is supplied by means of the pump P1 via conduit 3 to an acid cooler C1 , in which the acid temperature is decreased from 81 0 C to 65°C. With this temperature, the sulfuric acid then is again supplied to the drying tower TT via conduit 1.
  • the acid circuit of the drying tower TT is defined thereby.
  • a partial stream of the sulfuric acid is supplied as so-called crossflow acid via conduit 4 to an acid circulation tank T2 of the intermediate absorber circuit.
  • the quantity of the partial stream is controlled via a control valve V (LIC) on the basis of a level measurement in the acid circulation tank T1.
  • Sulfuric acid is supplied to the intermediate absorber ZA via conduit 5, which in the intermediate absorber ZA is guided in counterflow with SO 3 -containing gas from the non-illustrated converter in which the sulfur dioxide was converted to sulfur trioxide.
  • the sulfur trioxide is absorbed in the sulfuric acid and increases its concentration to about 99 %.
  • the sulfuric acid is withdrawn from the bottom of the intermediate absorber and supplied to the acid circulation tank T2 of the intermediate absorber circuit.
  • the sulfuric acid which for level control was diluted with the partial stream from the drying tower circuit supplied via conduit 4, is delivered via conduit 7 through the acid cooler C2 and into conduit 5.
  • a partial stream of the acid is branched off via conduit 8 into the pump receiver of the drying tower circuit, in order to adjust the concentration of the drying tower acid.
  • the quantity of the partial stream is adjusted via a control valve V (QIC) on the basis of a concentration measurement in conduit 1 .
  • Sulfuric acid with a concentration of 98.5 % which is guided in counterflow with SO 3 -containing gas and absorbs the SO 3 , is supplied to the final absorber EA via conduit 9.
  • process water is supplied to the bottom of the intermediate absorber ZA and of the final absorber EA 1 in order to again dilute the sulfuric acid to the desired value of 98.5 %. This is effected on the basis of concentration measurements in conduits 5 and 9.
  • a simplification of the acid-side circuitry can be effected by combining several tower circuits.
  • Such a conventional arrangement of the drying and absorption towers and the acid-side circuitry thereof is shown in Fig. 2.
  • the gas-side circuitry in turn is not shown. O ⁇
  • sulfuric acid with a concentration of about 98.5 % H 2 SO 4 is supplied to the drying tower TT via conduit 1.
  • the sulfuric acid is withdrawn from the bottom of the drying tower TT and supplied to the acid circulation tank T1 provided for all tower circuits in common.
  • the sulfuric acid is supplied via conduits 3, 4.1 and 4.2 to the acid coolers C1 and C2, from which it is supplied via conduits 1 , 6 and 9 to the drying tower TT, the intermediate absorber ZA and the final absorber EA.
  • the product is discharged via conduit 13 and supplied to a non-illustrated product cooler.
  • Such circuitry is particularly useful for plants which can also be used for the combustion of elementary sulfur, since the drying tower here is operated with air.
  • this circuitry cannot be used due to the high solubility of sulfur dioxide in the circulating sulfuric acid of the drying tower.
  • the concentration of the dissolved SO 2 then is reduced by mixing with the acids from the intermediate and final absorbers, but is in part expelled (stripped) again in the further course at the final absorber, so that the SO 2 then leaves the plant in the chimney gas and thus leads to inadmissible emissions.
  • this circuitry impairs the water balance, as in particular when processing gases with low SO 2 contents the amount of water introduced into the drying tower is too high as compared with the absorbed amount of SO 3 in the intermediate absorber. This can lead to the fact that the desired concentration of the common circuit of 98.5 % H 2 SO 4 can no longer be maintained. Therefore, this circuitry is hardly employed in practice.
  • FIG. 3 Another alternative is the combination of the acid circuits of intermediate absorber and final absorber, as it is shown in Fig. 3.
  • the drying tower TT forms a separate circuit.
  • the acid-side circuitry is shown.
  • the main components of the plant again are the same as in Figures 1 and 2, so that in so far the same reference numerals are used.
  • Table 3 indicates the process parameters for the circuitry as shown in Fig. 3.
  • the sulfuric acid formed in the intermediate absorber ZA is supplied via conduit 6 to a common acid circulation tank T2 for the absorber towers ZA, EA.
  • the sulfuric acid is supplied via conduits 7, 11 to the acid coolers C2 and C3 and then via conduits 5, 9 to the intermediate absorber ZA and to the final absorber EA, respectively.
  • product sulfuric acid is withdrawn from the plant and supplied to a non-illustrated product cooler.
  • This circuitry consists in that the pump and acid coolers for the common absorber circuit can be identical. However, the drying tower pump P1 and the associated cooler C1 still are different. Like in the circuitry shown in Fig. 1 , the crossflow acid from the drying tower TT is supplied to the acid circulation tank T2 of the absorbers ZA, EA as 94 to 96 % sulfuric acid. Even if this cross- flow quantity is relatively small, there still exists the above-described problem of the sulfur dioxide dissolved therein. This SO 2 is partly expelled in the final absorber EA and hence reduces the turnover and increases the emission. With increasing SO 2 content of the feed gas, the solubility thereof increases and intensifies the described effect. Due to the stricter requirements for a minimization of emissions, this actually advantageous circuitry therefore can no longer be employed. Summary of the Invention
  • the inlet concentration of the acid in an absorber is about 97.3 to 98.4 % H 2 SO 4 .
  • this first absorber is the intermediate absorber of such a plant. It is, however, possible here that the intermediate absorber also is divided into several individual absorbers, as is the case e.g. in DE 59 701 328. In the case of such a division, intermediate absorber each is understood to be the entire aggregate, constructed of several individual partial absorbers.
  • the fundamental difference of the present invention with respect to the circuitry shown in Fig. 3 consists in that the feed acid to the intermediate absorber no longer has the conventional acid concentration of typically 98.5 % H 2 SO 4 , but that the intermediate absorber is operated with a lower concentration of in par- ticular 97.5 to 98.2 % H 2 SO 4 .
  • the amount of circulating acid must virtually be increased linearly. This leads to the fact that the flooding point would be exceeded when using conventional ceramic fillers. In such cases, one is therefore forced to considerably increase the towers for hydraulic reasons, even if the mass transfer does not require the same.
  • the amount of circulating acid thus can be reduced considerably by maintaining the required outlet concentration. Due to the lower circulating amount, the intermediate absorber can be configured with a substantially reduced diameter, since the distance to the flooding point is increased. At the same time, the lower circulating amount leads to the fact that the pump capacity can be reduced considerably. In turn, this leads to the fact that the capacity of all circulating pumps can be adapted to that of the drying tower.
  • a partial stream of the sulfuric acid withdrawn from the drying tower is branched off and admixed only to the inflow of the intermediate absorber as crossflow acid, in accordance with a preferred aspect of the invention, inde- pendent of whether starting gas containing sulfur dioxide or air with concen- trated sulfuric acid is dried in the drying tower.
  • the crossflow acid from the drying tower has a concentration of 93 to 97 % H 2 SO 4 , preferably 95.5 to 96.5 % H 2 SO 4 and in particular about 96 % H 2 SO 4 .
  • the concentration of the cross- flow acid is adjusted in that process water is admixed to the bottom of the drying tower or to the sulfuric acid withdrawn from the drying tower.
  • process water is admixed to the inflow of the intermediate absorber in accordance with a preferred aspect of the invention.
  • the amount of said process water is adjusted by a concentration control.
  • the strongly SO 2 -containing crossflow acid from the drying tower thereby is guided to the top of the intermediate absorber together with the circulating acid.
  • This drying tower acid thus is prevented from mixing with the circulating acid of the final absorber, and an additional SO 2 emission, as it would occur with a circuitry as shown in Fig. 3, thus is avoided.
  • the SO 2 dissolved in the crossflow acid of the drying tower is expelled at the top of the intermediate absorber and supplied with the gas to the second catalytic conversion stage and converted to SO 3 .
  • the acid circuits of the intermediate absorber and of the final absorber are combined.
  • the acid outflow of the intermediate absorber and of the final absorber correspondingly is supplied to a common acid circulation tank.
  • process water preferably is also admixed to the bottom of the intermediate absorber.
  • dilute acid e.g. from plants corresponding to DE 10 2007 047 319, Fl 2007 0054 or EP 177 839, instead of the process water.
  • This dilute acid can originate both from an alternative process step to the final absorber, from a further gas cleaning stage downstream of the final absorber, or from a plant completely independent of the described sulfuric acid plant.
  • the process of the invention is the more advantageous for the operation of the plant the higher the concentration of the SO 2 content in the feed gas.
  • the feed gas in the converter for converting the sulfur dioxide includes 6.5 to 30 vol-% SO 2 , preferably > 12 vol-% SO 2 .
  • the process is particularly suitable for application in connection with a process for the catalytic conversion of high-percentage SO 2 -containing gases, as it is described in DE 102 49 782 A1.
  • the amount of heat to be dissipated at the acid coolers remains constant. With a reduced amount of circulating acid, this means that the temperature difference must increase. With a constant temperature of the acid charged to the towers, the inlet temperature of the acid into the acid coolers therefore is increased and is above 90 0 C in accordance with the invention.
  • the acid coolers can easily process acids even in this temperature range, but just as the associated acid conduits they can be reduced in size due to the reduced amount of circulating acid.
  • This invention also relates to a plant for producing sulfuric acid from a gas containing sulfur dioxide, which can be used for the process described above and includes a drying tower for drying the SO 2 -containing gas or air, a converter for the catalytic conversion of the sulfur dioxide to sulfur trioxide, an absorber and preferably a further stage for cleaning the gas from SO 2 , preferably a further absorber (final absorber) for the absorption of the sulfur trioxide in concentrated sulfuric acid, wherein the acid is circulated in the drying tower and in the ab- sorber(s).
  • the absorbers include a common acid circuit, whereas the drying tower has a separate acid circuit, from which a crossflow conduit is branched off, which is connected with the acid supply conduit of the one absorber.
  • a process water supply conduit is connected with the acid supply conduit of the intermediate absorber in accordance with a development of the invention.
  • mixing is effected in a mixing tank, preferably with a static mixer, e.g. in a mixing line of the pipe conduit.
  • the process water supply conduit is connected with the bottom of the drying tower. Adjusting the acid concentration at the inlet of the intermediate absorber thus is effected indirectly by adjusting the concentration of the crossflow acid and by the amount thereof, which is admixed to the circulating acid of the intermediate absorber. Alternatively, the amount of water can also be supplied in the form of dilute acid, whereby a dilute acid supply conduit completes or replaces the process water supply conduit.
  • the control of the process water feed stream is effected by means of a control means on the basis of the acid concentration in the acid supply conduit of the intermediate absorber.
  • the flow control of the crossflow acid is effected on the basis of the level in the drying tower.
  • the low acid inlet concentration in the intermediate absorber no longer represents the azeotropic concentration and consequently no longer has the lowest total vapor pressure. While both the H 2 SO 4 vapor pressure and the SO 3 partial pressure are decreasing with a concentration lower than the azeotropic concen- tration, the H 2 O partial pressure is increasing. This does not lead to a reduction of the SO 3 absorption, but can possibly lead to a slightly increased formation of mist.
  • mist filters therefore are provided downstream of the intermediate absorber, which prevent the apparatus from being affected by acid condensation and hence corrosion.
  • the acid circuits of the drying tower, the intermediate absorber and the final absorber are operated by means of acid pumps, which due to the circuitry of the invention can each have the same capacity (delivery rate), although the acid flow rates to the towers are very different. At the same time, the sum of all deliv- ery rates to the towers is smaller than in the prior art.
  • Fig. 1 schematically shows a conventional plant for producing sulfuric acid with an illustration of the acid circuit (double absorption plant).
  • Fig. 2 schematically shows another conventional plant for producing sulfuric acid with an illustration of the acid circuit.
  • Fig. 3 schematically shows a further conventional plant for producing sulfuric acid with an illustration of the acid circuit.
  • Fig. 4 schematically shows a preferred embodiment of a plant of the invention for producing sulfuric acid with an illustration of the acid circuit in a double absorption plant
  • Fig. 5 schematically shows a plant for producing sulfuric acid in accordance with another preferred embodiment of the invention with an illustration of the acid circuit.
  • Fig. 4 shows a first embodiment of the present invention.
  • the same main components as used in the description of the prior art shown in Figures 1 to 3 are designated with the same reference numerals.
  • ref- erence is also made to the above description.
  • the invention does, however, not only relate to the preferred embodiment in a double absorption plant, which is only cited as an example generally known to one of skill in the art.
  • sulfuric acid with a concentration of 96 wt-% is supplied to the drying tower TT via conduit 1.
  • the sulfuric acid is guided in counterflow with non-illustrated S ⁇ 2 -containing gas or air, in order to dry the same by absorbing water.
  • the sulfuric acid diluted in this way is supplied to the acid circulation tank T1 of the drying tower circuit.
  • the sulfuric acid is guided via conduit 3 through the acid cooler C1 and again supplied to the top of the drying tower TT via conduit 1.
  • Part of the sulfuric acid is branched off from conduit 3 and via conduit 4 supplied as crossflow acid to a mixing tank M, in which it is mixed with sulfuric acid of the absorber circuit, which is supplied via conduit 8, and with process water supplied via conduit 14.1 or alternatively with dilute acid.
  • the flow rates of the crossflow acid supplied from the drying tower TT via conduit 4 to the circulating acid of the absorber circuit, and of the stream of process water or of dilute acid are controlled on the basis of a concentration measurement in the acid supply conduit 5 of the intermediate absorber ZA such that in the inflow of the intermediate absorber ZA an acid concentration of 98 ⁇ 0.2 % H 2 SO 4 is obtained.
  • the sulfuric acid is guided in counterflow with gas containing sulfur trioxide, which was produced by converting the SO 2 - containing gas from the drying tower TT in a non-illustrated converter.
  • the crossflow acid from the drying tower TT can have a relatively high content of sulfur dioxide, which then gasses out in the intermediate absorber ZA and is supplied from the same to a further catalytic conversion stage and converted into sulfur trioxide, before it is supplied to the final absorber EA.
  • process water can be introduced into the bottom of the intermediate absorber ZA, in order to adjust the acid, which is withdrawn from the intermediate absorber ZA via conduit 6, to a desired value of e.g. 98.4 % H 2 SO 4 .
  • the acid is supplied to an acid circulation tank T2 common to the two absorber towers ZA and EA and supplied from the same by means of two pumps P2 and P3 of the same capacity via the conduits 7 and 11 to the acid coolers C2 and C3, which in turn have the same capacity.
  • the acid cooled in this way is supplied to the top of the final absorber EA and via conduit 8 to the pump receiver of the drying tower TT.
  • another partial stream is supplied to the mixing tank M and then to the top of the intermediate absorber ZA.
  • the product conduit 13 the acid not required for circulation is drawn in as product from the plant and supplied to a non-illustrated product cooler.
  • mist filters are provided, which prevent the apparatus from being affected by acid condensation.
  • Fig. 5 shows a variant of the plant circuitry in accordance with the invention, which largely corresponds to the plant as shown in Fig. 4.
  • the process water is not directly introduced via conduit 14.1 into the mixing tank M, but into the bottom of the drying tower TT, in order to adjust the concentration of the acid withdrawn from the drying tower TT and hence of the crossflow acid, which is mixed with the acid of the absorber circuit via the mixing chamber M.
  • This circuitry has the advantage that a static mixer can be used in the mixing chamber M 1 or the mixing chamber can be configured as a mixing line in the pipe conduit, where, however, only acids are suitably mixed with each other and admixing water can lead to problems.
  • Table 1 refers to the plant circuitry as shown in Fig. 1 , where in the converter for producing SO 3 , which is not shown in the drawing, a metallurgical gas with a content of 10 vol-% SO 2 was supplied, which was previously dried in the drying tower
  • Table 2 refers to the plant circuitry as shown in Fig. 2, wherein sulfur dioxide was produced by combustion of elementary sulfur and a feed gas with a concen- tration of 11.8 vol-% SO 2 was supplied to the converter not illustrated in the drawing.
  • a feed gas with a concen- tration of 11.8 vol-% SO 2 was supplied to the converter not illustrated in the drawing.
  • air is dried with sulfuric acid.
  • Table 3 refers to a plant circuitry as shown in Fig. 3, wherein a metallurgical gas with an SO 2 concentration of 12 vol-%, which was previously dried in the drying tower TT, was supplied to the converter not shown in the drawing.
  • Tables 4.1 to 4.3 refer to the plant circuitry as shown in Fig. 4, where in Table 4.1 a metallurgical gas with an SO 2 concentration of 8 vol-%, which was previously dried in the drying tower TT, was supplied to the converter not shown in the drawing. In Table 4.2, a metallurgical gas with an SO 2 concentration of 12 vol-% was supplied to the converter, whereas in Table 4.3 a metallurgical gas with an SO 2 concentration of 18 vol-% was supplied to the converter.
  • Table 5 refers to a plant circuitry as shown in Fig. 5, wherein a metallurgical gas with an SO 2 concentration of 18 vol-%, which was previously dried in the drying tower TT, was supplied to the converter not shown in the drawing.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Inorganic Chemistry (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Chemical & Material Sciences (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Treating Waste Gases (AREA)
  • Catalysts (AREA)
  • Gas Separation By Absorption (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)
  • Drying Of Gases (AREA)

Abstract

Lorsque de l'acide sulfurique est produit à partir d'un gaz qui contient du dioxyde de soufre, le dioxyde de soufre est catalytiquement oxydé dans un convertisseur pour obtenir du trioxyde de soufre. Le dioxyde de soufre produit est ainsi absorbé dans de l'acide sulfurique concentré dans un absorbeur intermédiaire et le gaz résiduel est éventuellement de nouveau alimenté vers une étape de conversion catalytique. Le trioxyde de soufre produit peut alors être absorbé dans de l'acide sulfurique concentré dans un absorbeur final. Pour simplifier la configuration de l'usine et également la régulation des gaz d'alimentation avec une teneur élevée en SO2, conformément à l'invention, la concentration d'entrée de l'acide vers l'absorbeur intermédiaire est d'environ 97,3 à 98,4 % de H2SO4.
PCT/EP2008/009193 2007-11-23 2008-10-31 Procédé et usine de production d'acide sulfurique WO2009065485A2 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
MX2010005600A MX2010005600A (es) 2007-11-23 2008-10-31 Proceso y planta para producir acido sulfurico.
CN200880114711A CN101848857A (zh) 2007-11-23 2008-10-31 生产硫酸的方法和装置
AU2008328289A AU2008328289B2 (en) 2007-11-23 2008-10-31 Process and plant for producing sulfuric acid

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
DE102007056933 2007-11-23
DE102007056933.7 2007-11-23
DE102007058144.2 2007-11-30
DE102007058144A DE102007058144A1 (de) 2007-11-30 2007-11-30 Verfahren und Anlage zur Herstellung von Schwefelsäure

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WO2009065485A2 true WO2009065485A2 (fr) 2009-05-28
WO2009065485A3 WO2009065485A3 (fr) 2009-07-30

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AU (1) AU2008328289B2 (fr)
CL (1) CL2008003420A1 (fr)
MX (1) MX2010005600A (fr)
PE (1) PE20091297A1 (fr)
WO (1) WO2009065485A2 (fr)

Cited By (5)

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Publication number Priority date Publication date Assignee Title
EP2578301A4 (fr) * 2010-06-04 2014-11-05 Showa Co Ltd Procede de decomposition/elimination utilisant un materiau photocatalytique
WO2016096867A1 (fr) * 2014-12-19 2016-06-23 Outotec (Finland) Oy Procédé et installation pour une production énergétiquement efficace, améliorée d'acide sulfurique
CN109879255A (zh) * 2019-04-27 2019-06-14 招远市招金金合科技有限公司 一种硫铁矿制酸系统生产精制硫酸的系统及方法
US10633251B2 (en) 2015-11-06 2020-04-28 Haldor Topsøe A/S Method and plant design for reduction of start-up sulfur oxide emissions in sulfuric acid production
WO2021254627A1 (fr) 2020-06-18 2021-12-23 Outotec (Finland) Oy Procédé et installation de production d'acide sulfurique

Families Citing this family (1)

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Publication number Priority date Publication date Assignee Title
US9849419B2 (en) * 2014-05-09 2017-12-26 Outotec (Finland) Oy Process and plant for the production of liquid acid

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US4591494A (en) * 1983-02-03 1986-05-27 C-I-L Method and apparatus for making sulphuric acid
US5028396A (en) * 1982-06-11 1991-07-02 Chemetics International Company, Ltd. Apparatus formed of high silicon chromium/nickel in steel in the manufacture of sulpheric acid
WO2005095272A2 (fr) * 2004-03-12 2005-10-13 Outokumpu Technology Oy Procede et installation de production d'acide sulfurique

Patent Citations (3)

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Publication number Priority date Publication date Assignee Title
US5028396A (en) * 1982-06-11 1991-07-02 Chemetics International Company, Ltd. Apparatus formed of high silicon chromium/nickel in steel in the manufacture of sulpheric acid
US4591494A (en) * 1983-02-03 1986-05-27 C-I-L Method and apparatus for making sulphuric acid
WO2005095272A2 (fr) * 2004-03-12 2005-10-13 Outokumpu Technology Oy Procede et installation de production d'acide sulfurique

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* Cited by examiner, † Cited by third party
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EP2578301A4 (fr) * 2010-06-04 2014-11-05 Showa Co Ltd Procede de decomposition/elimination utilisant un materiau photocatalytique
WO2016096867A1 (fr) * 2014-12-19 2016-06-23 Outotec (Finland) Oy Procédé et installation pour une production énergétiquement efficace, améliorée d'acide sulfurique
US10150671B2 (en) 2014-12-19 2018-12-11 Outotec (Finland) Oy Process and plant for improved energy-efficient production of sulfuric acid
US10633251B2 (en) 2015-11-06 2020-04-28 Haldor Topsøe A/S Method and plant design for reduction of start-up sulfur oxide emissions in sulfuric acid production
CN109879255A (zh) * 2019-04-27 2019-06-14 招远市招金金合科技有限公司 一种硫铁矿制酸系统生产精制硫酸的系统及方法
WO2021254627A1 (fr) 2020-06-18 2021-12-23 Outotec (Finland) Oy Procédé et installation de production d'acide sulfurique

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MX2010005600A (es) 2010-09-07
CL2008003420A1 (es) 2009-12-18
AU2008328289B2 (en) 2012-08-23
PE20091297A1 (es) 2009-09-18
AU2008328289A1 (en) 2009-05-28
CN101848857A (zh) 2010-09-29

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