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WO2008151758A2 - Procédé et appareil pour mélanger des gaz - Google Patents

Procédé et appareil pour mélanger des gaz Download PDF

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Publication number
WO2008151758A2
WO2008151758A2 PCT/EP2008/004510 EP2008004510W WO2008151758A2 WO 2008151758 A2 WO2008151758 A2 WO 2008151758A2 EP 2008004510 W EP2008004510 W EP 2008004510W WO 2008151758 A2 WO2008151758 A2 WO 2008151758A2
Authority
WO
WIPO (PCT)
Prior art keywords
gas
gas flow
converter
ring
conduit
Prior art date
Legal status (The legal status 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 status listed.)
Ceased
Application number
PCT/EP2008/004510
Other languages
English (en)
Other versions
WO2008151758A3 (fr
Inventor
Karl-Heinz Daum
Wolfram Schalk
David Cachero Ventosa
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Metso Corp
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
Application filed by Outotec Oyj filed Critical Outotec Oyj
Priority to AU2008261290A priority Critical patent/AU2008261290B2/en
Priority to CN200880019767.1A priority patent/CN101679037B/zh
Priority to MX2009013478A priority patent/MX340510B/es
Publication of WO2008151758A2 publication Critical patent/WO2008151758A2/fr
Publication of WO2008151758A3 publication Critical patent/WO2008151758A3/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

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
    • C01B17/803—Converters
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/10—Mixing gases with gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/30—Injector mixers
    • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
    • B01F25/313—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit
    • B01F25/3132—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit by using two or more injector devices
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
    • B01J8/0461—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical annular shaped beds
    • B01J8/0469—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical annular shaped beds the beds being superimposed one above the other
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0492—Feeding reactive fluids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0496—Heating or cooling the reactor
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00194—Tubes

Definitions

  • the present invention relates to a process for mixing two gases of different temperature and/or composition in a converter for producing SO 3 from an SO 2 - containing gas, and to an apparatus for performing this process.
  • the present invention is concerned with the production of sulfuric acid.
  • sulfuric acid mostly is produced by the so-called double absorption process, which is described in Ullmann's Encyclopedia of Industrial Chemistry, 5 th edition, Vol. A25, pp. 635 to 700.
  • a starting gas containing sulfur dioxide is at least partly reacted with oxygen in a plurality of successive contact stages of a converter corresponding to the formula
  • the produced gas containing sulfur trioxide then is supplied to an absorber and converted there to sulfuric acid.
  • the oxidation of the sul- fur dioxide to sulfur trioxide is effected in the presence of a catalyst, which usually contains vanadium pentoxide as active component and has a working range of about 380 to 640 0 C. While at temperatures above 640 0 C an irreversible damage of the vanadium pentoxide catalyst occurs, the same is inactive at temperatures below 380 0 C. As the process is strongly exothermal, the gas inlet temperature into the contact stage must be about 400 0 C.
  • the reaction is not initiated, whereas at a much higher iniet temperature the temperature rises so much during the process that the catalyst is damaged. It is, however, possible to also use other catalysts which allow a higher working temperature, as is known e.g. from EP 1 047 497 B1 or DE 100 23 178 A1.
  • the reaction is performed in several stages, between which the process gas each is cooled by means of integrated heat exchangers, in order to achieve a suitable gas inlet temperature for the next contact stage.
  • such converter includes four to five contact stages, and in the above-mentioned double absorption process the process gas having passed through a number of, e.g.
  • the process gas supplied to the converter suffers from frequent fluctuations of the quantity and SO 2 concentration. While in conventional converters the SO2 concentration usually is restricted to about 12 vol-% due to the high temperatures achieved in the first step of catalysis, the process described in DE 102 49 782 A1 provides for using higher SO 2 concentrations by recirculating SO 3 -containing gas. This recirculation limits the reaction in the first contact stage and as a result the heat generated there.
  • a first, SO 2 - containing gas flow is introduced into the converter through a central supply pipe and passed through an integrated heat exchanger arranged around the central supply pipe, that a second gas flow is supplied via a ring conduit arranged in the converter directly before or after the integrated heat exchanger, from which the second gas flow is discharged through a plurality of openings and is fed into the first gas flow, so that it mixes with the same, and that the gas mixture obtained then is supplied to a contact stage of the converter, in which the SO 2 is at least partly converted to SO 3 on a catalyst.
  • the second gas Via the ring conduit, the second gas thus is fed into the first gas at a plurality of points, so that an excellent mixing is achieved.
  • the second gas flow which for instance is SO 2 -containing gas of low tempera- ture
  • a higher pressure with respect to the mixture is available, whereby the pressure loss can also be increased and/or controlled.
  • the mixing and the mixing quality can be adjust or controlled. If the second gas is recirculated sulfur trioxide, its pressure can be in- creased by means of a blower or the like, so that here as well a higher pressure - A -
  • the pressure loss in the mixing device is optimised, to get sufficient turbulence and mixing quality without much pressure loss.
  • the first gas flow includes more than 13 vol-% SO 2 and the second gas flow 3 to 40 vol-% SO 3 , preferably 5 to 25 vol-% SO 3 , in accordance with a development of the invention.
  • the first gas stream also can contain SO 3 , e. g. 1 to 10 vol-% SO 3 , but preferably contains less than 1 % SO 3 .
  • the gas flow in the mixing chamber can be guided e. g. by guiding plates or by the gas inlet of the ring conduit, so that e. g. a stream like a swirl in the mixing chamber results.
  • the temperature at the inlet of the first contact stage of the converter is regulated in accordance with the invention by means of a second gas flow, which includes up to 30 vol-% SO 2 , preferably up to 12 vol-% SO 2 - and has a temperature of O to 400 0 C, preferably 80 to 300 0 C, more preferably 100 to 12O 0 C.
  • This gas flow can be passed around the usual heat exchanger as a bypass for increasing the temperature of the first gas, so that it has a higher pressure than the first gas.
  • devices for controlling or regulat- ing the pressure e.g. blowers or throttle valves or flow resistors can be incorporated, whereby mixing can be controlled in addition.
  • the volume flow rate of the second gas flow is smaller than that of the first gas flow and is 20 to 60%, preferably ⁇ 50% and more preferably ⁇ 30 % of the first gas flow.
  • An inventive apparatus for mixing two gases in a converter for producing SO 3 from an SO 2 -containing gas which can be used in particular for performing the process described above, includes a supply conduit for a first gas which is introduced into the converter and is passed through an integrated heat exchanger, which is arranged around the central supply conduit, a ring conduit for a second gas, which is arranged in the converter directly before or after the heat exchanger in a mixing chamber, wherein the ring conduit includes a plurality of openings for the dis- charge of second gas into the mixing chamber.
  • the first gas is introduced into the converter from above or below and upon deflection passed through the integrated heat exchanger, which preferably is arranged around the central supply conduit, and then enters the mixing chamber arranged above the heat exchanger. It 1 however, is possible that the gas is introduced from above or below into the heat exchanger in a straight way without deflection.
  • the ring conduit also preferably is arranged around the central supply conduit for the first gas. Beside a simple guidance of the flow, this results in a compact construction of the converter and the mixing means.
  • the holes in the ring conduit are facing the heat exchanger.
  • the second gas flow preferably is discharged from the ring conduit in downward direction. If the second gas flow should cocurrently be fed into the first gas flow, the holes in the ring con- duit are facing away from the heat exchanger, so that the second gas flow is discharged from the ring conduit in upward direction.
  • corresponding openings which can be designed as bores, slots or the like, are provided both on the lower surface and on the upper surface or at the sides of the ring conduit. The openings can be provided in several rows one beside the other, in order to increase the quantity of the second gas flow to be supplied.
  • the openings have an angle of 20 to 70°, particularly preferably 30 to 60° with respect to the vertical.
  • the openings can have a different size or shape, e.g. in dependence on the distance from the supply conduit. It is also possible to vary the openings or the gas flow around or from the openings by further installations, e.g. baffle plates, welding seams, etc. This variation can also concern only individual openings or individual groups of openings. It is furthermore possible to provide a closing device for individual openings or groups of openings, so as to have a regulation or control means in particular in partial load operation.
  • two to seven, in particular three concentric ring conduits are provided, from which the second gas is discharged.
  • the quantity of the second gas flow also can be increased thereby.
  • the ring conduits may be located at different vertical levels.
  • the ring conduits are connected with a common supply conduit for the second gas in accordance with the invention. It was found to be advantageous that the common supply conduit for the second gas is at least partly guided around the central supply conduit for the first gas and that a plurality of downwardly guided connecting conduits connect the supply conduit with the ring conduits.
  • the second gas can simultaneously be introduced into the converter at several points, wherein a preferred symmetric configuration of the converter and hence a preferred symmetric guidance of the flow is achieved.
  • What is essential for the invention is the rather uniform mixing of the gases and the uniform distribution in the converter, for which purpose it is possible to depart from the symmetry, if necessary.
  • the connecting conduits are each connected with all ring conduits via supply ports, in order to provide for an easier supply.
  • the plant has conduits for supplying gases to the mixer, which can be adjusted or controlled for the volume flow rate of the gas stream and/or pressure and/or pressure loss inside the con- duit.
  • This control can be done with blowers or the like and/or devices for control pressure loss, e. g. buffles, nozzles or flow resistors.
  • Fig. 1 shows a schematic sectional view of a converter for producing SO 3 from an SO 2 -containing gas with an apparatus for mixing gases in accordance with an embodiment of the present invention with illustrated gas flows,
  • Fig. 2 shows the region of introduction of the second gas flow into the first gas flow
  • Fig. 3 shows a partial top view of ring conduits of the apparatus in accor- dance with the invention
  • Fig. 4 shows a section through a ring conduit along line IV-IV of Fig. 3.
  • the converter 1 for converting SO 2 to SO 3 as shown in Fig. 1 includes a total of five contact stages K1 to K5, in which a catalyst, in particular a catalyst containing vanadium pentoxide is provided, in order to convert the SO 2 to SO 3 .
  • the SO 3 -containing gas obtained is supplied to a non-illustrated heat recovery plant and the intermediate absorption, in order to at least partly remove the sulfur trioxide from the process gas.
  • the SO 2 - containing process gas then is again supplied to the converter at the bottom, in order to pass through the contact stages K4 and K5.
  • the present invention primarily is intended to be realized in the first region of the converter 1 with the contact stages K1 to K3, so that the following description is restricted to this region.
  • the mixing method of the present invention may also be realized in the second region of the converter (contact stages K4 and K5).
  • SO 2 -containing gas which flows through the supply conduit from the top to the bottom and is deflected at its lower end by 180° by means of a baffle plate 3, is supplied to the converter 1 via a central supply conduit 2.
  • the first gas traverses a first heat exchanger WT1 , which in particular constitutes a tubular heat exchanger, from the bottom to the top and is discharged into a mixing chamber 4 arranged above the heat exchanger WT1.
  • a second gas which for instance is recirculated SO 3 -containing process gas or SO 2 -containg gas of lower temperature than the first gas, likewise is introduced into the mixing chamber 4 via a supply conduit 5 and adjoining connecting conduits 6, which via supply ports 7 are connected with ring conduits 8 extending around the central supply conduit 2, and mixes with the first gas.
  • the supply con- duit 5 here is guided around the central supply conduit 2 e.g. outside the converter 1 , for instance as a three-quarter circle, wherein the connecting conduits are downwardly branched from the supply conduit 5 and enter the converter 1.
  • the ring conduits 8, from which the second gas is discharged, are provided directly after the integrated heat exchanger WT1 , i.e. without interconnection of further apparatuses.
  • additional e.g. cold or warm S ⁇ 2 -containing gas can be supplied and mixed with the SO 3 containing gas before entering the converter 1.
  • the gas mixture then flows through the first contact K1 and subsequently is passed through the integrated heat exchanger WT1 , in order to cool the temperature of the process gas increased as a result of the exothermal reaction in the contact stage K1 to a temperature of about 400 0 C suitable for entering a second contact stage K2 and at the same time heat the SO ⁇ -containing first gas supplied through the central supply conduit 2.
  • the process gas Upon traversing the second contact stage K2, the process gas in turn is passed through an integrated heat exchanger WT2, in order to be cooled to an inlet temperature of about 400 0 C suitable for the third contact stage K3, and upon passing through this third contact stage K3 is withdrawn from the converter 1 via an outlet 10 and supplied to an intermediate ab- sorption plant.
  • the above described structure including the deflection of the first gas flow prior to entering the first heat exchanger WT1 is preferred for a converter comprising plural heat exchangers.
  • the apparatus for mixing the first and second gases is shown in detail.
  • the first gas enters the first heat exchanger WT1 from below and then is discharged into the mixing chamber 4.
  • the second gas is fed into the ring conduits 8, from which it is discharged into the mixing chamber 4 in downward direction via a plurality of openings 11 (cf. Fig. 4).
  • the openings 11 here are arranged in several rows of holes possibly arranged offset with respect to each other, so that the second gas is fed into the first gas as a plurality of small flows and can easily mix with the first gas due to the resulting turbulences promoted by the countercurrent feeding.
  • corresponding openings can also be provided on the upper surface of the ring conduits 8 in addition or alternatively to the openings 11 provided on the lower surface of the ring conduits 8, in order to cocur- rently feed the second gas into the first gas.
  • the mixing of the two gas flows is performed before the gas enters the converter.
  • the structure of the mixing chamber 4 and the ring conduits 8 is provided prior to the mixed gas entering the converter 1.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Inorganic Chemistry (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

Lors du mélange de deux gaz de températures et/ou de compositions différentes dans un convertisseur pour produire du SO3 à partir d'un gaz contenant du SO2, un premier courant gazeux contenant du SO2 est introduit dans le convertisseur par un conduit d'alimentation central et amené à traverser un échangeur de chaleur intégré disposé autour du conduit d'alimentation central et traversé par le premier courant gazeux de la partie inférieure à la partie supérieure. Un second courant gazeux est introduit par un conduit annulaire agencé au-dessus de l'échangeur de chaleur intégré et à partir duquel le second courant gazeux est déchargé par une pluralité d'ouvertures et introduit dans le premier courant gazeux, de telle sorte que les deux courants gazeux se mélangent. Ensuite, le mélange gazeux obtenu est adressé à un étage de contact du convertisseur dans lequel le SO2 est, au moins partiellement, converti en SO3 sur un catalyseur.
PCT/EP2008/004510 2007-06-13 2008-06-06 Procédé et appareil pour mélanger des gaz Ceased WO2008151758A2 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
AU2008261290A AU2008261290B2 (en) 2007-06-13 2008-06-06 Process and apparatus for mixing gases
CN200880019767.1A CN101679037B (zh) 2007-06-13 2008-06-06 混合气体的方法和装置
MX2009013478A MX340510B (es) 2007-06-13 2008-06-06 Proceso y aparato para mezclar gases.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102007027881.2 2007-06-13
DE102007027881A DE102007027881B4 (de) 2007-06-13 2007-06-13 Verfahren und Vorrichtung zur Mischung von Gasen

Publications (2)

Publication Number Publication Date
WO2008151758A2 true WO2008151758A2 (fr) 2008-12-18
WO2008151758A3 WO2008151758A3 (fr) 2009-06-11

Family

ID=39827729

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2008/004510 Ceased WO2008151758A2 (fr) 2007-06-13 2008-06-06 Procédé et appareil pour mélanger des gaz

Country Status (7)

Country Link
CN (1) CN101679037B (fr)
AU (1) AU2008261290B2 (fr)
CL (1) CL2008001718A1 (fr)
DE (1) DE102007027881B4 (fr)
MX (1) MX340510B (fr)
PE (1) PE20090270A1 (fr)
WO (1) WO2008151758A2 (fr)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102745654A (zh) * 2012-07-31 2012-10-24 阳谷祥光铜业有限公司 一种烟气制酸的转化装置、对其升温的系统及方法
CN108046221B (zh) * 2017-12-12 2020-10-02 中国恩菲工程技术有限公司 一种冶炼烟气制酸的方法
WO2025140972A1 (fr) * 2023-12-28 2025-07-03 Metso Metals Oy Procédé et installation de production de gaz contenant du trioxyde de soufre

Family Cites Families (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2104858A (en) * 1935-01-23 1938-01-11 Gen Chemical Corp Manufacture of sulphuric acid
DE966833C (de) * 1951-10-10 1957-09-12 Basf Ag Vorrichtung zur Herstellung schwefeltrioxydhaltiger Gase
DE1151341B (de) * 1961-03-21 1963-07-11 Schmidt Sche Heissdampf Einrichtung an Zusatzfeuerungen zum Einfuehren und Mischen des frischen Heizgases invon Abgasen niederer Temperatur durchstroemten Abgaskanaelen
DE1926239U (de) * 1964-01-31 1965-11-04 Uhde Gmbh Friedrich Vorrichtung zum mischen von gasen unterschiedlicher dichte.
US3661165A (en) * 1970-07-21 1972-05-09 Nat Distillers Chem Corp System for mixing gases and sparger valve for accomplishing same
DE7242602U (fr) * 1972-11-20 1976-04-29 Hoogovens Ijmuiden B.V., Ijmuiden (Niederlande)
US4152407A (en) * 1977-02-02 1979-05-01 Warren Fuchs Process and apparatus for exothermic reactions
CA1159229A (fr) * 1980-09-19 1983-12-27 John Mcfarland Convertisseur
US5480620A (en) * 1994-08-17 1996-01-02 Cameron; Gordon M. Catalytic converter
DE19800800C2 (de) 1998-01-13 2001-05-23 Metallgesellschaft Ag Verfahren zur Herstellung von Schwefelsäure
DE10023178A1 (de) 2000-05-11 2001-11-15 Mg Technologies Ag Verfahren zum katalytischen Umsetzen von Gasen mit hohem Gehalt an SO¶2¶
DE10249782A1 (de) * 2002-10-24 2004-05-06 Outokumpu Oyj Verfahren und Anlage zur Herstellung von Schwefelsäure aus schwefeldioxidreichen Gasen
DE10359744A1 (de) * 2003-12-19 2005-07-14 Uhde Gmbh Verfahren und Vorrichtung zum Eindüsen von Sauerstoff in einen Synthesereaktor

Also Published As

Publication number Publication date
DE102007027881A1 (de) 2008-12-18
PE20090270A1 (es) 2009-03-19
DE102007027881B4 (de) 2012-02-16
CN101679037A (zh) 2010-03-24
AU2008261290B2 (en) 2013-07-04
AU2008261290A1 (en) 2008-12-18
CL2008001718A1 (es) 2008-08-01
CN101679037B (zh) 2015-03-04
MX2009013478A (es) 2010-01-18
WO2008151758A3 (fr) 2009-06-11
MX340510B (es) 2016-07-11

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