EP0000707A1 - Procédé et installation pour séparer l'anhydride sulfureux de courants gazeux avec obtention d'acide sulfurique selon le procédé aux oxydes d'azote - Google Patents

Procédé et installation pour séparer l'anhydride sulfureux de courants gazeux avec obtention d'acide sulfurique selon le procédé aux oxydes d'azote Download PDF

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Publication number
EP0000707A1
EP0000707A1 EP7878100388A EP78100388A EP0000707A1 EP 0000707 A1 EP0000707 A1 EP 0000707A1 EP 7878100388 A EP7878100388 A EP 7878100388A EP 78100388 A EP78100388 A EP 78100388A EP 0000707 A1 EP0000707 A1 EP 0000707A1
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zone
acid
nitrogen
gas
pretreatment
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EP7878100388A
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German (de)
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EP0000707B1 (fr
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Volker Dr. Fattinger
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Novartis AG
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Ciba Geigy AG
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    • 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
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides

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  • the invention further relates to an improved system for carrying out the method according to the invention, which is based on that described in the above-mentioned DT-OS 26 09 505.
  • the process according to the invention also works in the denitrification and in the absorption zone with sulfuric acid of 70-85% by weight H 2 SO 4 , preferably with an acid between 72 and 80% by weight. % H 2 SO 4 (absorption acid).
  • nitrogen oxide-sulfuric acid plants can be loaded with larger amounts of gas if higher nitrogen oxide losses in the exhaust gas of the plant are permitted. Because of the In order to keep the air clean, it is necessary to operate nitrogen oxide-sulfuric acid plants with the lowest possible nitrogen oxide concentrations in the exhaust gas. In Germany, for example, a maximum limit for nitrogen oxides of 400 ppm is often set. A comparison between the performance of different nitrogen oxide-sulfuric acid processes must assume the same nitrogen oxide concentrations in the exhaust gas from the plants.
  • Sulfuric acid which is produced by this type of process, is therefore said to be a "strong" acid with a. Content of more than 70% by weight, but preferably more than 72% by weight of H 2 SO 4 .
  • the known nitrogen oxide-sulfuric acid processes deliver only limited amounts of sufficiently concentrated sulfuric acid per m 3 of reaction space when processing moist gases with an SOn content of less than 6% by volume and at temperatures below 60 ° C.
  • Modern Petersen tower systems produce 4 to 6 vol% of gases SO 2 less than 150 kg of a sulfuric acid with 73% by weight H 2 SO 4 .
  • gases with such a low SO 2 content when regenerating the solid or liquid sorbent gases are formed which contain S0 2 in varying amounts with concentrations of often only a few percent by volume and have a relatively high water content.
  • a "relatively high” water content is to be regarded as one which exceeds 50% of the weight of the SO 2 contained in the gas per m 3 , for example in the presence of 100 g SO 2 / m 3 over 50 g H 2 O / m 3 is.
  • Exhaust gases with a relatively low S0 2 content also arise when waste sulfuric acid is split, because a considerable proportion of the oxygen is consumed by the fuel in the cracking furnace.
  • the invention now solves the problem of ensuring a concentration of nitrogen oxides in the cleaned exhaust gases which is below the still permissible maximum concentration at which discharging the exhaust gases into the ambient air is permitted.
  • Another object of the invention is to improve the method described at the outset in the processing of SO 2 -containing gases, in particular also those of low SO 2 concentration, below 6% by volume SO 2 .
  • the space-time consumption of 78% sulfuric acid significantly, preferably to be increased to more than double that previously achievable, preferably to further reduce the volume of the reaction spaces previously required in the process according to DE-OS 26 09 505, and to achieve these improvements largely independently of the water content of the inlet gases.
  • Another object of the invention is to keep the sum of the volumes of the filling spaces of the reaction apparatus serving as treatment zones as low as possible.
  • the invention further aims to reduce the heat requirement of the system mentioned.
  • a nitrogen-oxygen compound (as defined in more detail below) is introduced into the pretreatment zone in such an amount that the contact of the SO 2 -containing gas stream with thin acid in this zone always contains the nitrogen-oxygen compound in the zone corresponds to at least 0.8 g of N 2 (in the form of said compound) per mole of SG 2 's contained in the gas stream to be treated.
  • the moisture content of the gases when they enter the system consisting of the reaction zones mentioned at the outset, as described in DE-OS 26 09 505, should be at least 5 g H 2 0 per m 3 gas.
  • the gas entering the inventive system may at times only traces of SO 2, but then again included from time to time, some, for example 2 to 5% by volume of S0 second
  • an S0 2 -containing gas stream contains 8% by weight or more of SO 2 , it is more economical to remove its S0 2 content by catalytic oxidation to SO 3 using the contact process.
  • the improved system of reaction zones in which the method according to the invention is carried out, can be charged with a SO 2 -containing gas, which can be a known type of exhaust gas, for example, chimney gas or a roasting gas, as used in the combustion of fuels low sulfur content or when roasting sulfur-containing ores, for example in the production of copper, or in other industrial processes, in particular also a gas which is produced in the preconcentration of exhaust gases to increase their sulfur content.
  • gases usually contain between 0.4 and 5% by volume of sulfur in the form of SO 2 , i.e. insufficient amounts of SO 2 for the contact process.
  • Exhaust gases which are processed in the system according to the invention should preferably have an S0 2 content of at least 0.2% by volume.
  • the gas stream is conveyed through the entire system of the reaction zones in the process according to the invention by a fan which is located either at the inlet end of the system or, preferably, after the outlet end thereof, which produces a slight excess pressure or a slight suction pressure in the gas lines of the system.
  • a fan which is located either at the inlet end of the system or, preferably, after the outlet end thereof, which produces a slight excess pressure or a slight suction pressure in the gas lines of the system.
  • About 0.01 to 0.1 atm are sufficient for the transport of the gas to be treated through the system.
  • the pressure used in practice is not sufficient to carry out a pressure synthesis of the type described in US Pat. No. 2,184,707 by E. Berl, which requires an excess pressure of at least 3, but in practice 10 to 50 atm.
  • Nitrogen-oxygen compounds are those compounds which normally occur or are used in the nitrogen oxide process, that is to say N0, N0 2 , N 2 0 3 , nitrose or nitric acid and, if appropriate, also solid "chamber crystals". Nitrous acid is immediately oxidized to nitric acid in the nitrogen oxide process or releases N203 or forms nitrose with sulfuric acid.
  • Gaseous substances which contain nitrogen-bound nitrogen are therefore NO- or N0 2 - orN 2 O 3 -. gases, liquid substances are in particular nitric acid itself or sulfuric acid containing nitrous oxide.
  • the nitrogen-oxygen compound is preferably introduced in the form of nitrous acid-containing thin acid flowing to the pretreatment zone, which originates from the SO 2 processing zone.
  • Nitric acid can also be introduced into the thin acid flowing to the pretreatment zone in order to generate or increase the nitrogen-oxygen compound content therein.
  • the concentration of nitrogen, which is brought into the pretreatment zone in an oxygen-bound form, should not be higher per mole of SO 2 in the gas stream than an amount of nitrogen-oxygen compound corresponding to 11.2 g of N 2 .
  • the acid dewatering zone and the pretreatment zone are preferably connected in series in a thin acid circuit.
  • the thin acid from the acid dewatering zone advantageously flows directly into the pretreatment zone via a gas-liquid cap.
  • Thin acid emerging from the pretreatment zone can be brought into contact with the exhaust gases from the nitrogen oxide absorption zone in the acid dewatering zone, and the resulting sulfuric acid with nitrogen oxide it has taken up from the exhaust gases and a slightly increased H 2 SO 4 content can be reintroduced directly into the pretreatment zone.
  • the H 2 SO 4 concentration of the acid coming into contact with the SO 2 -containing gas stream in the pretreatment zone is preferably kept lower than the H 2 SO 4 concentration of the acid in the SO 2 processing zone.
  • the method according to the invention makes it possible to manage with less than 100 m3 of filling space per Nm 3 / sec of SO 2 gas to be cleaned and also to reduce the heat requirement of the system.
  • the presence of nitrogen-oxygen compounds in the pretreatment zone causes an unexpectedly strong chemical reaction in this zone, e.g. is recognized by an increase in the acid outlet temperature, which occurs as soon as the addition of the nitrogen-oxygen compound is started.
  • the nitrogen-oxygen compounds can e.g. be brought into the pretreatment zone in the form of sulfuric acid containing nitroses.
  • nitric acid or to introduce nitrogen oxide-containing gases from catalytic ammonia combustion into the pretreatment zone. Thanks to the low concentration of sulfur acid in the pretreatment zone and because of the presence of S0 2 in the same, no nitrous is taken up by the sulfuric acid in the pretreatment zone; on the contrary, nitrous sulfuric acid, which is added to the pretreatment zone, quickly loses its nitrogen oxide content by releasing gaseous nitrogen oxides.
  • the gas stream After the pretreatment, the gas stream enters the denitrification zone. It has been found that the preloading of the gas with nitrogen oxides does not noticeably hinder the denitrification as long as the amount of nitrogen-oxygen compound present in the pretreatment zone does not exceed the above-mentioned amount corresponding to 11.2 g nitrogen per mole SO 2 of the gas stream.
  • the overall system is significantly intensified and it is not necessary to maintain temperatures above 65 ° C. at any point in the system when processing gases containing about 1% by weight of SO 2 .
  • the highest acid temperature is required for the irrigation of the denitrification zone.
  • Working at relatively low temperatures means saving heat energy and also has the major advantage that comparatively cheap materials can be used.
  • Sulfuric acid plants according to the invention can e.g. be made of PVC or PVC-coated material. It is possible to create a system made entirely of plastic, which can produce a very pure acid.
  • the pretreatment zone is used to intensify the SO2 processing.
  • the pre-treatment zone also takes on the function of gas drying.
  • the use of the pretreatment zone as a gas drying device makes the process particularly suitable for processing very moist gases containing SO 2 . Balancing the water balance of the system according to the invention is particularly important in the case of weak S0 2 contents of the gases to be processed. Under weakly S0 2 -containing gases are understood at a content of 5 vol .-% SO 2. Thanks to the invention it is possible to work also S0 2 -containing gases, the moisture content above a molar ratio of H 2 O: is 1: SO 2 of the second This is an essential advantage of the method because the removal of moisture from large exhaust gas streams is only possible with considerable energy and cost.
  • the moisture content of the gases which can be processed in the system according to the invention can be up to 20 to 60 or even more g H20.
  • the sulfuric acid in the pretreatment zone absorbs water from the gas stream.
  • the sulfuric acid diluted in this way is fed to a gas-liquid contact apparatus which is located on the gas side at the end of the system.
  • the exit gases of nitrogen oxides absorption 'zone are dry and therefore suitable to avoid the waste acid water.
  • the nitrogen oxide content in the acid leaving the pretreatment zone is so low that the dry exhaust gases leaving the system can be safely used as water removal agents in the acid drainage zone. They can then be loaded with steam through the chimney, as they are practically free of nitrogen oxides.
  • Gas-liquid reactors connected in series are used in the system according to the invention, each of which is traversed by a gas stream and an acid stream.
  • reaction apparatuses known in process engineering such as bubble columns, bubble layers and in particular also packed towers, are suitable for this purpose.
  • the concentration of gaseous nitrogen oxides is reduced to: is above 1% by volume, with entry gases with a higher SO 2 content, the nitrogen oxide concentration in the gas phase should be above 2% by volume.
  • the invention therefore distinguishes between denitrification and nitrogen oxide absorption, any free space that is not filled with packing material is avoided as far as possible. Only the combination of the measures of the invention makes it possible to intensify a tower system to the extent described, ie to increase its yield even when processing gases with less than 6% by volume S0 2 content to such an extent that daily production of 300 kg 78% sulfuric acid per m 3 filling space and more can be achieved.
  • the system for carrying out the process according to the invention is preferably designed or steered in such a way that the reaction space for nitrogen oxide absorption is at least the same or, at best, larger than the sum of the reaction spaces for denitration and SO 2 processing. Otherwise nitrogen oxides are lost for the implementation of the method. Because nitrogen oxide absorption primarily depends on the gas volume and not on the concentration of nitrogen oxides in the gas. Due to the above design of the reaction spaces, the overall system can be kept significantly smaller than the known systems for processes of the type described in the introduction.
  • the S0 2 content should preferably not be less than 0.2% by volume.
  • the upper limit of the residence time of the gas between the exit from the denitrification zone and the entry into the first nitrogen oxide absorption tower can be less than 30 seconds .
  • the temperature of the nitrous acid to be introduced into the denitrification zone is preferably kept constant by appropriate regulation of the additional indirect preheating of this acid.
  • the content of nitrose in the thin acid in the above-mentioned cycle due to the dissolution of nitrogen oxides in this acid in the S0 2 processing zone should not exceed 0.03% by weight calculated as HNO 3 .
  • the concentration of the acid flowing out of the denitrification zone can be kept constant by adding thin acid or water to this zone, thereby keeping the supply of water to the system as low as possible.
  • the process according to the invention makes it possible to process entry gases into the denitrification zone, the temperature of which is below 60 ° C. Entry gases, the temperature of which is less than 45 ° C, can still be processed to sulfuric acid despite an S0 2 content of only 1 to 1.5%.
  • the variation of the nitrous acid quantity, which is fed to the denitrification zone is used in the tower system as a regulating means for the ratio NO: N0 2 in the gas before the latter enters the nitrogen oxide absorption zone, and not the addition which is usually customary in tower systems Water.
  • This control system according to the invention makes it possible to automate a tower system.
  • U.S. Patent 1,882,447 to H.F. Merrian includes the denitrification zone, a product denitrification tower and an actual denitrator.
  • dry gas from a sulfuric acid contact system is introduced into the Merrian product denitrification tower together with nitrous acid-containing sulfuric acid, water-from the acid being taken up in the dry gas stream in this tower, which at the same time also Nitrogen oxides absorbed from the acid.
  • moisture from the gas stream entering this zone is absorbed by the thin acid flowing through it.
  • FIG. 1 The embodiment of the system according to the invention shown in FIG. 1 comprises seven reactors connected in series and serving as treatment zones, which are shown in the drawing as packing layers sprinkled with acid. For the sake of brevity, they are referred to below as "towers".
  • a gas stream to be treated in the system according to the method according to the invention which, in addition to nitrogen, also contains about 10% by volume of oxygen, a content of SO 2 which is at least temporarily too high for discharging into the ambient air and a considerable content of water vapor, for example 4% by volume ; is introduced via the line 102 at the lower end of the packing layer contained in the tower 1 and is fed from the top end thereof from the tower 1 via the gas line 22 to the lower end of the packing layer in a denitrification tower 2.
  • the gas stream passes via line 32 to the upper end of a first S0 2 processing tower 3 of the SO 2 processing zone and flows downward through the packed layer of the tower 3 via gas line 42 to the lower end of the packed layer of a second S0 2 processing tower 4 and in the latter.
  • the gas flow flows through this packing layer upwards and is passed from the upper end of the tower 4 of the SO 2 processing zone via the gas line 52 to the upper end of a first tower 5 of the nitrogen oxide absorption zone, the packing layer of which it flows through from top to bottom.
  • the gas stream is sucked off by the fan 67 from the lower end of this packing layer and is pressed via line 62 into the packing layer located in the second absorption tower 6 from bottom to top.
  • the tower 7 is arranged directly above the tower 1 and its interior is separated from that of the tower 1 by a gas-liquid seal 77, which prevents gas from line 72 entering the tower 7 below its packing layer t into the space of the tower 1 above can get from the packing layer and thus into the gas line 22.
  • each packing layer can be equipped with an additional acid cycle. However, these circuits are not shown in the drawing to simplify the illustration.
  • the pumps 25, 35, 45, 55, 65 and 75 are used to transport the sprinkling acid to the packed layers of the towers 2, 3, 4, 5, 6 and 7.
  • the acid flowing out of the packed layer of the Tu 7 passes through the gas Liquid seal 77 'on the packed layer of the tower 1.
  • the heat exchangers 24 and 74 serve to heat the acids which flow through the lines 23 and 73 into the corresponding packed layers of the towers 2 and 7, respectively.
  • the heat exchangers 34, 44 and 64 serve to cool the acids which flow through the lines 33, 43 and 63 onto the corresponding packing layers of the towers 3, 4 and 6, respectively.
  • towers 3 and 4 to the SO 2 processing zone, which is sprinkled with a thin acid of less than 70% by weight H 2 SO 4 which is circulated through the packed layers of these two towers.
  • the concentration in towers 3 and 4 is approximately 65% by weight H 2 SO 4 .
  • Tower 4 is at the end of the S0 4 processing zone. It has been found that the acid already takes up appreciable amounts of nitrogen oxides at the end of this zone.
  • the thin acid flowing out of the packing layer of the tower 1 into the sump 71 of this tower is now conveyed by the pump 75 via line 73 through the heat exchanger 74 heating the acid and further through line 73 into the upper end of the tower 7, the packing layer of which represents the acid dewatering zone.
  • the separated from the thin acid circuit of the S0 2 processing zone thin acid circuit for the pretreatment zone via line 73 is now closed in that the thin acid, which is sprinkled on the upper end of the tower 7 on the packing layer, through the latter layer and through the the lower end of the tower 7 gas-liquid seal 77 flows back into the packing layer located in the tower 1 below.
  • the amount of water absorbed by this acid during its circulation in the packed layer of the tower 1 is thus passed directly to the end of the system, i.e. led into the packed layer of the tower 7 and released there to the exhaust gas of the system supplied via line 72.
  • the amount of water released can be controlled, as a result of which a desired concentration of the acid in the circuit via the packed layers of the. Towers 7 and 1 can be set. As already explained above, the acid flowing out of the packing layer of the tower 7 passes directly to the packing layer of the tower 1 via the gas seal 77.
  • the concentration of the acid in the circuit over the packed layers of the towers 7 and 1 is approximately 60% by weight H 2 SO 4 .
  • the concentration of the acid in the SO 2 processing zone (packing layers 3 and 4) is 65% by weight H 2 SO 4 .
  • the gas stream to be treated preferably has a temperature of approximately 40 ° C.
  • 108 denotes a device for the catalytic oxidation of ammonia.
  • the nitrogen oxides formed are cooled in the heat exchanger 104 and then flow through the column 110 from bottom to top. That part of the nitrogen oxides which is not absorbed in the column 110 reaches the main gas stream of the installation via line 112 and line 102.
  • thin acid can be passed from the sump 71 of the tower 1 into the column 110 via the valve 106.
  • the thin acid saturated with nitrogen oxides passes through the sump 101 and line 115 to the pump 116 and via line 117 and valve 118 into the upper end of the packing layer of the tower 3.
  • the tower 1 - tower 7 - heat exchanger 74 through lines 115 and 117 As already mentioned, thin acid withdrawn via line 73 is replaced by thin acid flowing in via compensating line 133.
  • the nitrogen-oxygen connection of the pretreatment zone is carried out by additional spraying of the packing layer of the tower 1 with sulfuric acid containing nitrose, which flows from the transfer line 5 L for the latter from the sump 51 of the first Nitrogen oxide absorption tower 5 branched off via the line 123 and the upper end of the packed layer of the tower 1 is supplied.
  • a liquid which contains nitrogen-bound nitrogen especially also in the form of nitric acid and is taken from a special container 80, into the packed layer of the tower 3 sprinkled with thin acid from tower 4 via line 33 the SO 2 processing zone at the top of the latter.
  • the low-nitrosic acid from the denitrification tower 2 flows through the absorption zone (towers 6 and 5), and the nitrous acid formed there flows from the packed layer of the tower 5 into the sump 51, in part also via the line 82 and the valve 56 into the container 80.
  • nitric acid can be fed through line 83 into container 80 to compensate for the normal nitrogen oxide losses of the system.
  • the pump 85 is started and becomes strongly nitrous - and / or sulfuric acid containing nitric acid flows via valve 46 and line 37 into the packed layer of tower 3.
  • the pretreatment tower 1 is now charged with part of the liquid which contains oxygen-bound nitrogen by completely or partially closing valve 46 in the system according to FIG. 4 while valve 86 is opened.
  • the strongly nitrous and / or nitric acid-containing sulfuric acid conveyed by the pump 85 is conducted from the container 80 via the line 78 to the packed layer of the tower 1.
  • valve 46 can be closed completely.
  • the overall system is significantly intensified and it is not necessary, for example, in the plant according to FIG. 1 when processing approximately 1% by volume S0 2 -containing gases warm up anywhere in the system to temperatures above 65 ° C to ensure sufficient denitrification and complete S0 2 processing in the overall system.
  • Working at relatively low temperatures means saving heat energy and also has the major advantage that comparatively cheap materials can be used.
  • nitrogen oxide-containing acid is introduced into the layer of the tower 1, significantly more SO 2 can be obtained without increasing the nitrous content of the acid in the sump and without increasing the nitrogen oxide content of the system exhaust gases.
  • the nitrous content of the acid in the sump-51 is 2% by weight, calculated as HN0 3 (100% nitric acid).
  • the acid in the sump 41 contains 0.3% by weight of oxygen-bound nitrogen, calculated as HN0 3 .
  • the heated acid reaches the layer of the tower 7 via line 73 and releases water vapor to the dry exhaust gases from the nitrogen oxide absorption zone there, as also described above.
  • the acid cools down to approx. 50 ° C and returns to the layer of tower 1.
  • acid which is bound to acid Contains nitrogen, via the valve 76 to layer 1, the level in the sump 71 rises and a corresponding amount of acid flows back via line 133 into the sump 31 and thus into the circuit of the SO 2 processing zone (towers 3 and 4).
  • the rest is nitrogen.
  • the nitrogen oxides absorbed in the layers of the absorption towers 5 and 6 are passed with the acid via the sump 51 through the pump 25 via the lines 54 and 23 to the layer of the denitrification tower 2, in which these nitrogen oxides are reacted with SO 2 as NO in get the gas stream, which leaves the tower 2 through line 32.
  • the more nitrogen oxides in the gas stream the better the S02 processing in the layers of towers 3 and 4.
  • nitrous acid is passed into the layer of the denitrification tower 2 per Nm 3 of gas.
  • nitric acid is passed from the container 91 via the pump 27 and the valve 28 via the line 36 and via the valve 26 to the layer of the depositing tower 2.
  • about a third of the nitrogen oxide-containing acid which circulates from the sump 41 of the tower via the lines 33 and 43 in the SO 2 processing zone is then branched to about 30 to 40 ° C. after heating in the heat exchanger 34 and via the Line 30 and the valve 76 are introduced into the tower 1 at the upper end thereof and its packing layer is sprinkled with this branched acid in addition to the thin acid flowing down from the tower 7.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
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  • Environmental & Geological Engineering (AREA)
  • Analytical Chemistry (AREA)
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EP78100388A 1977-07-21 1978-07-13 Procédé et installation pour séparer l'anhydride sulfureux de courants gazeux avec obtention d'acide sulfurique selon le procédé aux oxydes d'azote Expired EP0000707B1 (fr)

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CH906277 1977-07-21
CH9062/77 1977-07-21

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EP0000707A1 true EP0000707A1 (fr) 1979-02-21
EP0000707B1 EP0000707B1 (fr) 1981-10-14

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EP78100388A Expired EP0000707B1 (fr) 1977-07-21 1978-07-13 Procédé et installation pour séparer l'anhydride sulfureux de courants gazeux avec obtention d'acide sulfurique selon le procédé aux oxydes d'azote

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EP (1) EP0000707B1 (fr)
JP (1) JPS5423074A (fr)
AT (1) AT372297B (fr)
AU (1) AU528089B2 (fr)
BR (1) BR7804686A (fr)
DD (1) DD137192A5 (fr)
DE (1) DE2830215A1 (fr)
ES (1) ES471906A1 (fr)
FI (1) FI782254A (fr)
IN (1) IN150428B (fr)
IT (1) IT7850389A0 (fr)
PL (1) PL112097B2 (fr)
ZA (1) ZA784132B (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2961409A1 (fr) * 2010-06-22 2011-12-23 Air Liquide Procede de purification d'un gaz de combustion
WO2014083982A1 (fr) * 2012-11-30 2014-06-05 千代田化工建設株式会社 Procédé et dispositif de désulfuration pour dispositif de production d'acide sulfurique
WO2020002472A1 (fr) 2018-06-28 2020-01-02 Basf Se Utilisation d'alkynylthiophènes en tant qu'inhibiteurs de nitrification

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4127075A1 (de) * 1991-08-16 1993-02-18 Nymic Anstalt Verfahren zum reinigen von belasteten abgasen von verbrennungsanlagen
DE4129166A1 (de) * 1991-09-03 1993-03-04 Nymic Anstalt Verfahren zur reinigung von rauchgas
CN112246081A (zh) * 2020-09-30 2021-01-22 浙江蓝星环保设备有限公司 一种烟气脱硝装置

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB270988A (en) * 1926-10-12 1927-05-19 Hugo Petersen Improvements in and relating to the manufacture of sulphuric acid
DE467587C (de) * 1928-01-11 1928-10-29 Erich Rothammel Verfahren zur Benutzung einer Gloverapparatur zur ausschliesslichen Erzeugung von Schwefelsaeure
US1822447A (en) * 1928-01-16 1931-09-08 Gen Chemical Corp Manufacture of hso from weak so, gas
FR911236A (fr) * 1945-06-04 1946-07-02 Procédé et installation pour la fabrication combinée d'acide nitrique et d'acide sulfurique, notamment très concentrés
FR2032512A5 (en) * 1969-01-15 1970-11-27 Cimadevilla Jose Pure, concentrated sulphuric acid prodn
FR2303760A1 (fr) * 1975-03-10 1976-10-08 Ciba Geigy Ag Procede de separation de l'anhydride sulfureux de courants gazeux avec obtention d'acide sulfurique selon le procede aux oxydes d'azote

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB270988A (en) * 1926-10-12 1927-05-19 Hugo Petersen Improvements in and relating to the manufacture of sulphuric acid
DE467587C (de) * 1928-01-11 1928-10-29 Erich Rothammel Verfahren zur Benutzung einer Gloverapparatur zur ausschliesslichen Erzeugung von Schwefelsaeure
US1822447A (en) * 1928-01-16 1931-09-08 Gen Chemical Corp Manufacture of hso from weak so, gas
FR911236A (fr) * 1945-06-04 1946-07-02 Procédé et installation pour la fabrication combinée d'acide nitrique et d'acide sulfurique, notamment très concentrés
FR2032512A5 (en) * 1969-01-15 1970-11-27 Cimadevilla Jose Pure, concentrated sulphuric acid prodn
FR2303760A1 (fr) * 1975-03-10 1976-10-08 Ciba Geigy Ag Procede de separation de l'anhydride sulfureux de courants gazeux avec obtention d'acide sulfurique selon le procede aux oxydes d'azote

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2961409A1 (fr) * 2010-06-22 2011-12-23 Air Liquide Procede de purification d'un gaz de combustion
WO2014083982A1 (fr) * 2012-11-30 2014-06-05 千代田化工建設株式会社 Procédé et dispositif de désulfuration pour dispositif de production d'acide sulfurique
WO2020002472A1 (fr) 2018-06-28 2020-01-02 Basf Se Utilisation d'alkynylthiophènes en tant qu'inhibiteurs de nitrification

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Publication number Publication date
DD137192A5 (de) 1979-08-22
ZA784132B (en) 1979-07-25
EP0000707B1 (fr) 1981-10-14
PL112097B2 (en) 1980-09-30
JPS5423074A (en) 1979-02-21
ATA526278A (de) 1983-02-15
DE2830215A1 (de) 1979-02-22
AU3820178A (en) 1980-01-24
BR7804686A (pt) 1979-04-17
ES471906A1 (es) 1979-10-01
AU528089B2 (en) 1983-04-14
FI782254A (fi) 1979-01-22
PL208578A1 (pl) 1979-04-23
IT7850389A0 (it) 1978-07-20
IN150428B (fr) 1982-10-02
AT372297B (de) 1983-09-26

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