EP1339676A1 - Method for photochemical sulphochlorination of gaseous alkanes - Google Patents
Method for photochemical sulphochlorination of gaseous alkanesInfo
- Publication number
- EP1339676A1 EP1339676A1 EP01978529A EP01978529A EP1339676A1 EP 1339676 A1 EP1339676 A1 EP 1339676A1 EP 01978529 A EP01978529 A EP 01978529A EP 01978529 A EP01978529 A EP 01978529A EP 1339676 A1 EP1339676 A1 EP 1339676A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- chlorine
- alkane
- mole
- sulfur dioxide
- moles
- 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.)
- Withdrawn
Links
- 238000000034 method Methods 0.000 title claims abstract description 27
- 150000001335 aliphatic alkanes Chemical class 0.000 title claims abstract description 20
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims abstract description 36
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 21
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 claims abstract description 20
- 229910052753 mercury Inorganic materials 0.000 claims abstract description 20
- 235000019398 chlorine dioxide Nutrition 0.000 claims abstract description 4
- OSVXSBDYLRYLIG-UHFFFAOYSA-N chlorine dioxide Inorganic materials O=Cl=O OSVXSBDYLRYLIG-UHFFFAOYSA-N 0.000 claims abstract description 4
- 238000006552 photochemical reaction Methods 0.000 claims abstract description 3
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical group C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 24
- 238000006243 chemical reaction Methods 0.000 claims description 23
- 239000000460 chlorine Substances 0.000 claims description 21
- 239000000203 mixture Substances 0.000 claims description 18
- 229910052801 chlorine Inorganic materials 0.000 claims description 17
- 239000007789 gas Substances 0.000 claims description 14
- 239000007788 liquid Substances 0.000 claims description 12
- 229910052738 indium Inorganic materials 0.000 claims description 8
- APFVFJFRJDLVQX-UHFFFAOYSA-N indium atom Chemical compound [In] APFVFJFRJDLVQX-UHFFFAOYSA-N 0.000 claims description 8
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 5
- -1 alkanesulfonyl chlorides Chemical class 0.000 claims description 5
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims description 5
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims description 5
- 238000002347 injection Methods 0.000 claims description 5
- 239000007924 injection Substances 0.000 claims description 5
- 238000004519 manufacturing process Methods 0.000 claims description 4
- 125000004432 carbon atom Chemical group C* 0.000 claims 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 abstract 1
- 239000004155 Chlorine dioxide Substances 0.000 abstract 1
- 235000010269 sulphur dioxide Nutrition 0.000 abstract 1
- 239000004291 sulphur dioxide Substances 0.000 abstract 1
- 239000012359 Methanesulfonyl chloride Substances 0.000 description 13
- QARBMVPHQWIHKH-UHFFFAOYSA-N methanesulfonyl chloride Chemical compound CS(Cl)(=O)=O QARBMVPHQWIHKH-UHFFFAOYSA-N 0.000 description 13
- GYHNNYVSQQEPJS-UHFFFAOYSA-N Gallium Chemical compound [Ga] GYHNNYVSQQEPJS-UHFFFAOYSA-N 0.000 description 7
- 229910052733 gallium Inorganic materials 0.000 description 7
- 239000012043 crude product Substances 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 238000009434 installation Methods 0.000 description 3
- 238000012432 intermediate storage Methods 0.000 description 3
- 239000012429 reaction media Substances 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000013021 overheating Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 230000005855 radiation Effects 0.000 description 2
- 241000393496 Electra Species 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 125000004390 alkyl sulfonyl group Chemical group 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000002019 doping agent Substances 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000000295 emission spectrum Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- 238000005286 illumination Methods 0.000 description 1
- PNDPGZBMCMUPRI-UHFFFAOYSA-N iodine Chemical compound II PNDPGZBMCMUPRI-UHFFFAOYSA-N 0.000 description 1
- 229910052740 iodine Inorganic materials 0.000 description 1
- 239000011630 iodine Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 230000037452 priming Effects 0.000 description 1
- 238000006862 quantum yield reaction Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000004645 scanning capacitance microscopy Methods 0.000 description 1
- 238000005204 segregation Methods 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C303/00—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides
- C07C303/02—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides of sulfonic acids or halides thereof
- C07C303/04—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides of sulfonic acids or halides thereof by substitution of hydrogen atoms by sulfo or halosulfonyl groups
- C07C303/10—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides of sulfonic acids or halides thereof by substitution of hydrogen atoms by sulfo or halosulfonyl groups by reaction with sulfur dioxide and halogen or by reaction with sulfuryl halides
-
- 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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
- B01J19/12—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing electromagnetic waves
- B01J19/122—Incoherent waves
- B01J19/123—Ultraviolet light
-
- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
- B01J2219/0873—Materials to be treated
- B01J2219/0881—Two or more materials
- B01J2219/0883—Gas-gas
Definitions
- the present invention relates to the field of alkane sulfonyl chlorides and more particularly relates to the manufacture of these compounds by photochemical sulfochlorination of gaseous alkanes at ambient temperature.
- This process which essentially consists in reacting a gaseous mixture of alkane, sulfur dioxide and chlorine in the presence of ultraviolet light supplied by a mercury lamp, is characterized in that the mixture contains a strong excess of sulfur dioxide by compared to the alkane and that liquid sulfur dioxide is injected into the reaction zone to keep the temperature thereof constant.
- An installation for implementing this method is also described in the aforementioned patents, the content of which is incorporated here by reference. Compared to the photochemical processes of the prior art, described in the work by F. ASINGER "Paraffins, Chemistry and Technology", Pergamon Press 1968, p.520 et seq.
- indium-doped lamps have a much longer life than gallium-doped lamps and, like the latter, are not subject to slow segregation of the dopant in the lower parts of the lamp.
- the subject of the invention is therefore a process for the manufacture of alkanesulfonyl chlorides by the photochemical reaction of an alkane with chlorine and sulfur dioxide, optionally in the presence of hydrogen chloride, characterized in that use is made as light source a medium pressure mercury lamp doped with indium.
- the process according to the invention relates more particularly to the sulfochlorination of methane which is the most difficult alkane to sulfochlorinate, but it also applies to all gaseous alkanes under the chosen temperature and pressure conditions.
- the proportions of the reactants in the gas mixture subjected to light radiation can vary between the following limits:
- this pressure can range from 1 to 15 relative bars and is preferably between 8 and 12 relative bars.
- the reaction temperature generally between 10 and 90 ° C, depends on the working pressure chosen. It is for example around 60 ° C for 10 bar absolute and around 80 ° C for 15 bar absolute. As in the process described in patents FR 2 578 841, FR 2 595 095 and FR 2 777 565, the temperature is kept constant by injection of liquid SO 2 into the reaction zone.
- Indium-doped medium-pressure mercury lamps to be used in accordance with the process according to the invention are well known and are described, for example, in the work by M. Déribeau entitled “Iodine Lamps - Lodide Lamps", Editions DUNOD, 1965, p.67, as well as in the book “Sources de Lumière” of the French Lighting Association (AFE) in LUX Editions, 1992, p.134, or finally in “Techniques d'Utilisation des Photons” "by JC André and A. Bernard Vannes, Editions ELECTRA / EDF, 1992, pp. 157-168. The content of these works is incorporated here by reference.
- Such lamps sold by the companies SILITRO / SCAM or HERAEUS, re-emit more than 70% of their light energy in the form of radiation of wavelengths between 400 and 475 nm.
- Figures 1, 2 and 3 attached show respectively the emission spectrum of a 750 watt medium pressure mercury lamp, that of a gallium doped medium pressure mercury lamp of the same power and that of a mercury lamp medium pressure of the same power doped with indium.
- the light energy emitted by the medium-pressure mercury lamp (Figure 1) is distributed in the form of lines between 220 and 750 nm and that emitted by the gallium-doped lamp ( Figure 2) between 400 and 430 nm while, for the indium doped lamp (figure 3), most of the energy emitted is concentrated in the 400 to 460 nm region.
- the illumination of the reaction medium with a medium-pressure mercury lamp doped with indium is much more homogeneous than with a conventional mercury lamp .
- the method according to the invention can be implemented in an installation similar to that described in patent FR 2 578 841.
- Such an installation essentially comprising means for supplying the reagents, a photochemical reactor and means for separating the products from the reaction is represented by the diagrammatic drawing of attached FIG. 4.
- the inputs 1, 2 and 3 are respectively those of the alkane, sulfur dioxide and chlorine which are introduced in the gaseous state into a mixer 4 provided with an agitator to homogenize the gas mixture. ; for safety reasons, a premixer of Cl 2 and SO 2 is preferably provided at 4 '.
- the gas mixture passes from the mixer 4 via the line 5 into the reactor 6 in which it is distributed uniformly by means of a 5 'ramp with orifices.
- Another similar ramp 7 is also placed along the height of the reactor to introduce the liquid SO 2 intended for adjusting the temperature.
- a light source 8 passes through the reactor in a manner known per se.
- a tube 11 carries the liquid product, formed in the reactor 6, to a separator 12 from which the liquid phase, that is to say the crude alkanesulfonyl chloride, descends into an intermediate storage 13, while the residual gases pass through a pipe 14 in a second separator 15.
- This separator is optionally provided with a cooler 15 'to bring the SO 2 , arriving, to the liquid state; the liquid SO 2 containing chlorine is recovered in an intermediate storage 16.
- a fraction of SO 2 is recycled by the pipes 17 and 17 ′ via the pump 18 and the ramp 7 in the reactor 6.
- Another fraction of SO 2 , coming from 16, goes through line 19 in the heater 20 and from there through 19 'to the supply of the mixer 4.
- the HCI is evacuated via line 21 to treatment devices not shown.
- the intermediate storage 13 From the bottom of the intermediate storage 13 there is a pipe 22 to apparatuses for purifying the alkanesulfonyl chloride produced which, not forming the subject of the invention, are not shown here.
- the following examples illustrate the invention without limiting it.
- methanesulfonyl chloride (CH3SO 2 CI) was prepared using a medium pressure mercury lamp as the light source. This 750 watt lamp was placed axially in a 50 liter capacity reactor 6.
- the gas mixture prepared in 4 contained for one mole of methane, 6.25 moles of sulfur dioxide, 0.83 mole of chlorine and 0.417 mole of hydrogen chloride. This gas mixture was fed to the reactor at a rate of 5.75 Nm ⁇ / hour. The pressure in the reactor being fixed at 9 bars above the atmosphere, the temperature was adjusted to 65 ⁇ 2 ° C by injection, by means of the ramp 7, of 5.1 kg / h of liquid SO 2 .
- the gaseous effluent, arriving by 14 in the second separator 15 had the following volume composition:
- this gaseous effluent was 6.57 Nm 3 / h and contained the gaseous SO 2 resulting from the evaporation which served to cool the reaction.
- the temperature in the separator 15 was kept below 32 ° C.
- methanesulfonyl chloride was prepared by replacing the conventional mercury lamp with a gallium doped lamp of the same electrical power (750 W).
- the hourly flow rate of the feed gas mixture had to be brought to 6.86 Nm 3 / hour.
- the pressure in the reactor being fixed at 9 bars above the atmosphere, the temperature was adjusted to 65 ⁇ 2 ° C by injection, by means of the ramp 7, of 7.5 kg / h of sulfur dioxide liquid.
- the gaseous effluent, arriving by 14 in the second separator 15 had the following volume composition:
- the productivity of methanesulfonyl chloride was 3.58 kg / kW.
- methanesulfonyl chloride was prepared by replacing the conventional mercury lamp with an indium doped lamp of the same electrical power (750 W).
- the hourly flow rate of the feed gas mixture had to be brought to 8.82 Nm 3 / hour.
- the pressure in the reactor being fixed at 9 bars above the atmosphere, the temperature was adjusted to 65 ⁇ 2 ° C by injection, by means of the ramp 7, of 9.64 kg / h of sulfur dioxide liquid.
- the gaseous effluent, arriving by 14 in the second separator 15 had the following volume composition:
- the methane flow rate at the outlet 21 of the separator 15 was 0.326 Nm 3 / hour.
- the quantity introduced in 1 being 1.038 Nm 3 / h, the conversion of methane was therefore 68.6%.
- For chlorine, the conversion was 88%.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Electromagnetism (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Toxicology (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention concerns a method for making an alkanesulphonyl chloride by photochemical reaction of an alkane with chlorine and sulphur dioxide, which consists in using as light source an indium-doped medium-pressure mercury lamp.
Description
PROCEDE DE SULFOCHLORATION PHOTOCHI IQUE D'ALCANES GAZEUX PROCESS FOR PHOTOCHEMIC SULFOCHLORINATION OF GASEOUS ALKANES
La présente invention concerne le domaine des chlorures d'alcanesulfonyle et a plus particulièrement pour objet la fabrication de ces composés par sulfochlora- tion photochimique des alcanes gazeux à la température ambiante.The present invention relates to the field of alkane sulfonyl chlorides and more particularly relates to the manufacture of these compounds by photochemical sulfochlorination of gaseous alkanes at ambient temperature.
Etant donné l'utilité industrielle des chlorures d'alcanesulfonyle, en particulier du chlorure de méthanesulfonyle, la fabrication de ces composés a fait l'objet de plusieurs procédés consistant notamment en la sulfochloration photochimique d'alcanes avec le chlore et le dioxyde de soufre. Parmi ces procédés connus, un procédé particulièrement performant pour la sulfochloration photochimique des alcanes gazeux à la température ambiante comme le méthane est celui décrit dans les brevets FR 2 578 841 et FR 2 595 095.Given the industrial utility of alkanesulfonyl chlorides, in particular methanesulfonyl chloride, the manufacture of these compounds has been the subject of several processes consisting in particular of the photochemical sulfochlorination of alkanes with chlorine and sulfur dioxide. Among these known processes, a particularly efficient process for the photochemical sulfochlorination of gaseous alkanes at room temperature such as methane is that described in patents FR 2,578,841 and FR 2,595,095.
Ce procédé qui consiste essentiellement à faire réagir un mélange gazeux d'alcane, de dioxyde de soufre et de chlore en présence de lumière ultraviolette fournie par une lampe au mercure, est caractérisé en ce que le mélange contient un fort excès de dioxyde de soufre par rapport à l'alcane et que du dioxyde de soufre liquide est injecté dans la zone de réaction pour maintenir constante la température de celle-ci. Une installation pour la mise en œuvre de ce procédé est également décrite dans les brevets précités dont le contenu est incorporé ici par référence. Par rapport aux procédés photochimiques de la technique antérieure, décrits dans l'ouvrage de F. ASINGER "Paraffines, Chemistry and Technology", Pergamon Press 1968, p.520 et suivantes et dans le brevet FR 2 246 520, le procédé des brevets FR 2 578 841 et FR 2 595 095 présente l'avantage de n'exiger l'introduction d'aucun produit étranger dans le milieu réactionnel et de former ce dernier unique- ment avec ses constituants obligatoires, à savoir l'alcane, le dioxyde de soufre et le chlore. D'autre part, ce procédé permet d'obtenir de bonnes conversions et des rendements satisfaisants aussi bien par rapport à l'alcane que par rapport au chlore. En outre, contribuant à une meilleure absorption des photons par le chlore et à une élimination très aisée de la chaleur de réaction, ce procédé conduit à d'excellents rendements quantiques et évite toute surchauffe du milieu réactionnel.This process which essentially consists in reacting a gaseous mixture of alkane, sulfur dioxide and chlorine in the presence of ultraviolet light supplied by a mercury lamp, is characterized in that the mixture contains a strong excess of sulfur dioxide by compared to the alkane and that liquid sulfur dioxide is injected into the reaction zone to keep the temperature thereof constant. An installation for implementing this method is also described in the aforementioned patents, the content of which is incorporated here by reference. Compared to the photochemical processes of the prior art, described in the work by F. ASINGER "Paraffins, Chemistry and Technology", Pergamon Press 1968, p.520 et seq. And in patent FR 2 246 520, the process of the patents FR 2 578 841 and FR 2 595 095 has the advantage of not requiring the introduction of any foreign product into the reaction medium and of forming the latter only with its compulsory constituents, namely the alkane, the dioxide of sulfur and chlorine. On the other hand, this process makes it possible to obtain good conversions and satisfactory yields both with respect to the alkane and with respect to the chlorine. In addition, contributing to a better absorption of photons by chlorine and to a very easy elimination of the heat of reaction, this process leads to excellent quantum yields and avoids any overheating of the reaction medium.
Les performances de ce procédé ont ensuite été améliorées selon le brevet FR 2 777 565, en utilisant comme source lumineuse une lampe au mercure dopée au gallium. Il a été montré que, par rapport à une lampe au mercure d'égale puissance, l'emploi d'une telle source lumineuse permet d'obtenir une productivité du réacteur nettement supérieure, ainsi qu'une amélioration du rendement et de la sélectivité de la réaction.The performance of this process was then improved according to patent FR 2 777 565, using as a light source a mercury lamp doped with gallium. It has been shown that, compared to a mercury lamp of equal power, the use of such a light source makes it possible to obtain a significantly higher reactor productivity, as well as an improvement in the yield and the selectivity of the reaction.
Il a maintenant été trouvé qu'on peut encore améliorer ce procédé en utilisant comme source lumineuse une lampe au mercure dopée à l'indium. En effet, par
rapport à une lampe au mercure dopée au gallium, l'emploi d'une lampe au mercure dopée à l'indium permet, à puissance égale, d'améliorer encore la répartition de l'énergie lumineuse dans le réacteur ainsi que la productivité, le rendement et la sélectivité.It has now been found that this process can be further improved by using an indium-doped mercury lamp as the light source. Indeed, by compared to a mercury lamp doped with gallium, the use of a mercury lamp doped with indium allows, at equal power, to further improve the distribution of light energy in the reactor as well as the productivity, yield and selectivity.
Outre leur meilleur rendement lumineux, les lampes dopées à l'indium présentent une longévité largement supérieure à celle des lampes dopées au gallium et ne sont pas sujettes, comme ces dernières, à une lente ségrégation du dopant dans les parties basses de la lampe.In addition to their better light output, indium-doped lamps have a much longer life than gallium-doped lamps and, like the latter, are not subject to slow segregation of the dopant in the lower parts of the lamp.
L'invention a donc pour objet un procédé de fabrication de chlorures d'alcanesulfonyle par réaction photochimique d'un alcane avec du chlore et du dioxyde de soufre, éventuellement en présence de chlorure d'hydrogène, caractérisé en ce que l'on utilise comme source lumineuse une lampe au mercure moyenne pression dopée à l'indium.The subject of the invention is therefore a process for the manufacture of alkanesulfonyl chlorides by the photochemical reaction of an alkane with chlorine and sulfur dioxide, optionally in the presence of hydrogen chloride, characterized in that use is made as light source a medium pressure mercury lamp doped with indium.
Le procédé selon l'invention vise plus particulièrement la sulfochloration du méthane qui est l'alcane le plus difficile à sulfochlorer, mais il s'applique également à tous les alcanes gazeux dans les conditions de température et de pression choisies.The process according to the invention relates more particularly to the sulfochlorination of methane which is the most difficult alkane to sulfochlorinate, but it also applies to all gaseous alkanes under the chosen temperature and pressure conditions.
Selon l'alcane de départ, les proportions des réactifs dans le mélange gazeux soumis au rayonnement lumineux peuvent varier entre les limites suivantes :Depending on the starting alkane, the proportions of the reactants in the gas mixture subjected to light radiation can vary between the following limits:
et sont de préférence choisies comme suit : and are preferably chosen as follows:
On opère de préférence sous une pression supérieure à la pression atmosphérique. Généralement, cette pression peut aller de 1 à 15 bars relatifs et est, de préférence, comprise entre 8 et 12 bars relatifs. It is preferably carried out under a pressure higher than atmospheric pressure. Generally, this pressure can range from 1 to 15 relative bars and is preferably between 8 and 12 relative bars.
La température réactionnelle, généralement comprise entre 10 et 90°C, dépend de la pression de travail choisie. Elle est par exemple d'environ 60°C pour 10 bars absolus et d'environ 80°C pour 15 bars absolus. Comme dans le procédé
décrit dans les brevets FR 2 578 841 , FR 2 595 095 et FR 2 777 565, la température est maintenue constante par injection de SO2 liquide dans la zone réactionnelle.The reaction temperature, generally between 10 and 90 ° C, depends on the working pressure chosen. It is for example around 60 ° C for 10 bar absolute and around 80 ° C for 15 bar absolute. As in the process described in patents FR 2 578 841, FR 2 595 095 and FR 2 777 565, the temperature is kept constant by injection of liquid SO 2 into the reaction zone.
Les lampes au mercure moyenne pression dopées à l'indium à utiliser conformément au procédé selon l'invention sont bien connues et sont décrites, par exemple, dans l'ouvrage de M. Déribéré intitulé "Lampes à Iode - Lampes à lodures", Editions DUNOD, 1965, p.67, ainsi que dans l'ouvrage "Sources de Lumière" de l'Association Française d'Eclairage (AFE) aux Editions LUX, 1992, p.134, ou enfin dans "Techniques d'Utilisation des Photons" de J.C. André et A. Bernard Vannes, aux Editions ELECTRA/EDF, 1992, pp. 157-168. Le contenu de ces ouvrages est incorporé ici par référence. De telles lampes, commercialisées par les Sociétés SILITRO/SCAM ou HERAEUS, réémettent plus de 70 % de leur énergie lumineuse sous forme de radiations de longueurs d'onde comprises entre 400 et 475 nm. Les figures 1 , 2 et 3 annexées montrent respectivement le spectre d'émission d'une lampe au mercure moyenne pression de 750 watts, celui d'une lampe au mercure moyenne pression de même puissance dopée au gallium et celui d'une lampe au mercure moyenne pression de même puissance dopée à l'indium. L'énergie lumineuse émise par la lampe au mercure moyenne pression (figure 1 ) est répartie sous forme de raies entre 220 et 750 nm et celle émise par la lampe dopée au gallium (figure 2) entre 400 et 430 nm alors que, pour la lampe dopée à l'indium (figure 3), l'essentiel de l'énergie émise est concentrée dans la zone de 400 à 460 nm. Outre un gain de rendement d'énergie lumineuse utile (environ 28 % par rapport au gallium), l'éclairement du milieu réactionnel avec une lampe au mercure moyenne pression dopée à l'indium est beaucoup plus homogène qu'avec une lampe au mercure classique. Ceci contribue à un amorçage de la réaction mieux réparti dans le volume réactionnel et, en favorisant les transferts thermiques, permet d'atténuer les surchauffes locales liées à l'énergie de la réaction; on observe donc une meilleure sélectivité. Par rapport à la lampe dopée au gallium, la productivité est améliorée de 23 % et la sélectivité par rapport au chlore est supérieure à 90 %.Indium-doped medium-pressure mercury lamps to be used in accordance with the process according to the invention are well known and are described, for example, in the work by M. Déribéré entitled "Iodine Lamps - Lodide Lamps", Editions DUNOD, 1965, p.67, as well as in the book "Sources de Lumière" of the French Lighting Association (AFE) in LUX Editions, 1992, p.134, or finally in "Techniques d'Utilisation des Photons" "by JC André and A. Bernard Vannes, Editions ELECTRA / EDF, 1992, pp. 157-168. The content of these works is incorporated here by reference. Such lamps, sold by the companies SILITRO / SCAM or HERAEUS, re-emit more than 70% of their light energy in the form of radiation of wavelengths between 400 and 475 nm. Figures 1, 2 and 3 attached show respectively the emission spectrum of a 750 watt medium pressure mercury lamp, that of a gallium doped medium pressure mercury lamp of the same power and that of a mercury lamp medium pressure of the same power doped with indium. The light energy emitted by the medium-pressure mercury lamp (Figure 1) is distributed in the form of lines between 220 and 750 nm and that emitted by the gallium-doped lamp (Figure 2) between 400 and 430 nm while, for the indium doped lamp (figure 3), most of the energy emitted is concentrated in the 400 to 460 nm region. In addition to a gain in useful light energy efficiency (around 28% compared to gallium), the illumination of the reaction medium with a medium-pressure mercury lamp doped with indium is much more homogeneous than with a conventional mercury lamp . This contributes to a priming of the reaction better distributed in the reaction volume and, by favoring the heat transfers, makes it possible to attenuate the local overheating linked to the energy of the reaction; better selectivity is therefore observed. Compared to the gallium doped lamp, the productivity is improved by 23% and the selectivity with respect to chlorine is greater than 90%.
Le procédé selon l'invention peut être mis en œuvre dans une installation similaire à celle décrite dans le brevet FR 2 578 841. Une telle installation comprenant essentiellement des moyens d'alimentation des réactifs, un réacteur photochimique et des moyens pour séparer les produits de la réaction est représentée par le dessin schématique de la figure 4 annexée.The method according to the invention can be implemented in an installation similar to that described in patent FR 2 578 841. Such an installation essentially comprising means for supplying the reagents, a photochemical reactor and means for separating the products from the reaction is represented by the diagrammatic drawing of attached FIG. 4.
Sur ce dessin, les entrées 1 , 2 et 3 sont respectivement celles de l'alcane, du dioxyde de soufre et du chlore que l'on introduit à l'état gazeux dans un mélangeur 4 muni d'un agitateur pour homogénéiser le mélange gazeux ; pour des raisons de sécurité, un prémélangeur de Cl2 et SO2 est de préférence prévu en 4'. Le mélange gazeux passe du mélangeur 4 via la conduite 5 dans le réacteur 6 dans lequel
il est distribué uniformément au moyen d'une rampe 5' à orifices. Une autre rampe similaire 7 est placée également suivant la hauteur du réacteur pour introduire le SO2 liquide destiné au réglage de la température. Le réacteur est traversé de manière connue en soi par une source lumineuse 8. En haut du réacteur 6 part une canalisation 9 vers une pompe 10, permettant de recycler une fraction de l'effluent du réacteur vers la canalisation 5 en vue de la prédilution des réactifs venant de 4. Une tubulure 1 1 conduit le produit liquide, formé dans le réacteur 6, vers un séparateur 12 d'où la phase liquide, c'est-à-dire le chlorure d'alcanesulfonyle brut, descend dans un stockage intermédiaire 13, tandis que les gaz résiduels passent par une conduite 14 dans un second séparateur 15. Ce séparateur est éventuellement muni d'un refroidisseur 15' pour ramener le SO2, arrivant, à l'état liquide ; le SO2 liquide contenant du chlore, est récupéré dans un stockage intermédiaire 16. Une fraction de SO2 est recyclée par les canalisations 17 et 17' via la pompe 18 et la rampe 7 dans le réacteur 6. Une autre fraction de SO2, venant de 16, passe par la canalisation 19 dans le réchauffeur 20 et de là par 19' vers l'alimentation du mélangeur 4.In this drawing, the inputs 1, 2 and 3 are respectively those of the alkane, sulfur dioxide and chlorine which are introduced in the gaseous state into a mixer 4 provided with an agitator to homogenize the gas mixture. ; for safety reasons, a premixer of Cl 2 and SO 2 is preferably provided at 4 '. The gas mixture passes from the mixer 4 via the line 5 into the reactor 6 in which it is distributed uniformly by means of a 5 'ramp with orifices. Another similar ramp 7 is also placed along the height of the reactor to introduce the liquid SO 2 intended for adjusting the temperature. A light source 8 passes through the reactor in a manner known per se. At the top of the reactor 6 there is a line 9 towards a pump 10, making it possible to recycle a fraction of the effluent from the reactor to line 5 with a view to prediluting the reagents coming from 4. A tube 11 carries the liquid product, formed in the reactor 6, to a separator 12 from which the liquid phase, that is to say the crude alkanesulfonyl chloride, descends into an intermediate storage 13, while the residual gases pass through a pipe 14 in a second separator 15. This separator is optionally provided with a cooler 15 'to bring the SO 2 , arriving, to the liquid state; the liquid SO 2 containing chlorine is recovered in an intermediate storage 16. A fraction of SO 2 is recycled by the pipes 17 and 17 ′ via the pump 18 and the ramp 7 in the reactor 6. Another fraction of SO 2 , coming from 16, goes through line 19 in the heater 20 and from there through 19 'to the supply of the mixer 4.
En haut du séparateur 15, le HCI est évacué par la conduite 21 vers des appareils de traitement non représentés. Du bas du stockage intermédiaire 13 part une conduite 22 vers des appareils de purification du chlorure d'alcanesulfonyle produit qui, ne faisant pas l'objet de l'invention, ne sont pas représentés ici. Les exemples suivants illustrent l'invention sans la limiter.At the top of the separator 15, the HCI is evacuated via line 21 to treatment devices not shown. From the bottom of the intermediate storage 13 there is a pipe 22 to apparatuses for purifying the alkanesulfonyl chloride produced which, not forming the subject of the invention, are not shown here. The following examples illustrate the invention without limiting it.
EXEMPLE 1 (comparatif)EXAMPLE 1 (comparative)
Dans le dispositif décrit précédemment, on a préparé du chlorure de métha- nesulfonyle (CH3SO2CI) en utilisant comme source lumineuse une lampe au mercure moyenne pression. Cette lampe de 750 watts était placée axialement dans un réacteur 6 de 50 litres de capacité.In the device described above, methanesulfonyl chloride (CH3SO 2 CI) was prepared using a medium pressure mercury lamp as the light source. This 750 watt lamp was placed axially in a 50 liter capacity reactor 6.
Le mélange gazeux, préparé en 4, contenait pour une mole de méthane, 6,25 moles de dioxyde de soufre, 0,83 mole de chlore et 0,417 mole de chlorure d'hydrogène. Ce mélange gazeux était alimenté au réacteur au débit de 5,75 Nm^/heure. La pression dans le réacteur étant fixée à 9 bars au-dessus de l'atmosphère, la température était réglée à 65 ± 2°C par injection, au moyen de la rampe 7, de 5,1 kg/h de SO2 liquide.The gas mixture, prepared in 4, contained for one mole of methane, 6.25 moles of sulfur dioxide, 0.83 mole of chlorine and 0.417 mole of hydrogen chloride. This gas mixture was fed to the reactor at a rate of 5.75 Nm ^ / hour. The pressure in the reactor being fixed at 9 bars above the atmosphere, the temperature was adjusted to 65 ± 2 ° C by injection, by means of the ramp 7, of 5.1 kg / h of liquid SO 2 .
La quantité horaire de chlorure de méthanesulfonyle brut, recueilli après détente dans le stockage 13, était de 2,5 kg. A la pression atmosphérique et à la température ambiante, ce produit brut présentait la composition pondérale suivante :
The hourly quantity of crude methanesulfonyl chloride, collected after expansion in storage 13, was 2.5 kg. At atmospheric pressure and at room temperature, this crude product had the following composition by weight:
L'effluent gazeux, arrivant par 14 dans le second séparateur 15 présentait la composition volumique suivante :The gaseous effluent, arriving by 14 in the second separator 15 had the following volume composition:
Le débit de cet effluent gazeux était de 6,57 Nm3/h et contenait le SO2 gazeux issus de l'evaporation ayant servi au refroidissement de la réaction. Afin de recueillir le dioxyde de soufre à l'état liquide sous 4 bars de pression relative, la température dans le séparateur 15 était maintenue au-dessous de 32°C.The flow rate of this gaseous effluent was 6.57 Nm 3 / h and contained the gaseous SO 2 resulting from the evaporation which served to cool the reaction. In order to collect the sulfur dioxide in the liquid state under 4 bars of relative pressure, the temperature in the separator 15 was kept below 32 ° C.
Le débit de méthane à la sortie 21 du séparateur 15 était de 0,278 Nm3/heure. La quantité introduite en 1 étant de 0,68 Nm3/h, la conversion du méthane a donc été de 59 %. Pour le chlore, la conversion s'est élevée à 88 %. Les résultats ont conduit aux rendements et sélectivité suivants en chlorure de méthanesulfonyle produit :The methane flow rate at the outlet 21 of the separator 15 was 0.278 Nm 3 / hour. The quantity introduced in 1 being 0.68 Nm 3 / h, the conversion of methane was therefore 59%. For chlorine, the conversion was 88%. The results led to the following yields and selectivity for methanesulfonyl chloride produced:
Ramenée à la puissance de la lampe au mercure moyenne pression, la productivité en chlorure de méthanesulfonyle a été de 2,55 kg/kW.
EXEMPLE 2 (comparatif) Reduced to the power of the medium pressure mercury lamp, the productivity of methanesulfonyl chloride was 2.55 kg / kW. EXAMPLE 2 (comparative)
Dans le même appareillage qu'à l'exemple 1 , on a préparé du chlorure de méthanesulfonyle en remplaçant la lampe au mercure classique par une lampe dopée au gallium de même puissance électrique (750 W).In the same apparatus as in Example 1, methanesulfonyl chloride was prepared by replacing the conventional mercury lamp with a gallium doped lamp of the same electrical power (750 W).
Afin d'avoir le même taux de conversion du chlore qu'à l'exemple 1 (88 %), le débit horaire du mélange gazeux d'alimentation a dû être amené à 6,86 Nm3/heure. La pression dans le réacteur étant fixée à 9 bars au-dessus de l'atmosphère, la température a été réglée à 65 ± 2°C par injection, au moyen de la rampe 7, de 7,5 kg/h de dioxyde de soufre liquide.In order to have the same chlorine conversion rate as in Example 1 (88%), the hourly flow rate of the feed gas mixture had to be brought to 6.86 Nm 3 / hour. The pressure in the reactor being fixed at 9 bars above the atmosphere, the temperature was adjusted to 65 ± 2 ° C by injection, by means of the ramp 7, of 7.5 kg / h of sulfur dioxide liquid.
La quantité horaire de chlorure de méthanesulfonyle brut, recueilli après détente dans le stockage 13, était de 3,54 kg. A la pression atmosphérique et à la température ambiante, ce produit brut présentait la composition pondérale suivante :The hourly quantity of crude methanesulfonyl chloride, collected after expansion in storage 13, was 3.54 kg. At atmospheric pressure and at room temperature, this crude product had the following composition by weight:
L'effluent gazeux, arrivant par 14 dans le second séparateur 15 présentait la composition volumique suivante :The gaseous effluent, arriving by 14 in the second separator 15 had the following volume composition:
Le débit de cet effluent gazeux, contenant le SO2 gazeux issu de l'evaporation ayant servi au refroidissement de la réaction, était de 8,3 Nm3/h. Afin de recueillir le dioxyde de soufre à l'état liquide sous 4 bars de pression relative, la température dans le séparateur 15 était maintenue au-dessous de 32°C.
Le débit de méthane à la sortie 21 du séparateur 15 était de 0,26 Nm3/heure. La quantité introduite en 1 étant de 0,8 Nm3/h, la conversion du méthane a donc été de 67 %. Pour le chlore, la conversion s'est élevée à 88 %. The flow rate of this gaseous effluent, containing the SO 2 gas resulting from the evaporation which served to cool the reaction, was 8.3 Nm 3 / h. In order to collect the sulfur dioxide in the liquid state under 4 bars of relative pressure, the temperature in the separator 15 was kept below 32 ° C. The methane flow rate at outlet 21 of separator 15 was 0.26 Nm 3 / hour. The quantity introduced in 1 being 0.8 Nm 3 / h, the conversion of methane was therefore 67%. For chlorine, the conversion was 88%.
Les résultats ont conduit aux rendements et sélectivités suivants en chlorure de méthanesulfonyle produit :The results led to the following yields and selectivities of methanesulfonyl chloride produced:
Ramenée à la puissance de la lampe au gallium, la productivité en chlorure de méthanesulfonyle a été de 3,58 kg/kW.Reduced to the power of the gallium lamp, the productivity of methanesulfonyl chloride was 3.58 kg / kW.
EXEMPLE 3EXAMPLE 3
Dans le même appareillage qu'à l'exemple 1 , on a préparé du chlorure de méthanesulfonyle en remplaçant la lampe au mercure classique par une lampe dopée à l'indium de même puissance électrique (750 W).In the same apparatus as in Example 1, methanesulfonyl chloride was prepared by replacing the conventional mercury lamp with an indium doped lamp of the same electrical power (750 W).
Afin d'avoir le même taux de conversion du chlore qu'à l'exemple 1 (88 %), le débit horaire du mélange gazeux d'alimentation a dû être amené à 8,82 Nm3/heure. La pression dans le réacteur étant fixée à 9 bars au-dessus de l'atmosphère, la température a été réglée à 65 ± 2°C par injection, au moyen de la rampe 7, de 9,64 kg/h de dioxyde de soufre liquide.In order to have the same chlorine conversion rate as in Example 1 (88%), the hourly flow rate of the feed gas mixture had to be brought to 8.82 Nm 3 / hour. The pressure in the reactor being fixed at 9 bars above the atmosphere, the temperature was adjusted to 65 ± 2 ° C by injection, by means of the ramp 7, of 9.64 kg / h of sulfur dioxide liquid.
La quantité horaire de chlorure de méthanesulfonyle brut, recueilli après détente dans le stockage 13, était de 4,55 kg. A la pression atmosphérique et à la température ambiante, ce produit brut présentait la composition pondérale suivante :The hourly quantity of crude methanesulfonyl chloride, collected after expansion in storage 13, was 4.55 kg. At atmospheric pressure and at room temperature, this crude product had the following composition by weight:
L'effluent gazeux, arrivant par 14 dans le second séparateur 15 présentait la composition volumique suivante :
The gaseous effluent, arriving by 14 in the second separator 15 had the following volume composition:
Le débit de cet effluent gazeux, contenant le SO2 gazeux issu de l'evaporation ayant servi au refroidissement de la réaction, était de 7,49 Nm3/h. Afin de recueillir le dioxyde de soufre à l'état liquide sous 4 bars de pression relative, la température dans le séparateur 15 était maintenue au-dessous de 32°C.The flow rate of this gaseous effluent, containing the SO 2 gas resulting from the evaporation which served to cool the reaction, was 7.49 Nm 3 / h. In order to collect the sulfur dioxide in the liquid state under 4 bars of relative pressure, the temperature in the separator 15 was kept below 32 ° C.
Le débit de méthane à la sortie 21 du séparateur 15 était de 0,326 Nm3/heure. La quantité introduite en 1 étant de 1 ,038 Nm3/h, la conversion du méthane a donc été de 68,6 %. Pour le chlore, la conversion s'est élevée à 88 %.The methane flow rate at the outlet 21 of the separator 15 was 0.326 Nm 3 / hour. The quantity introduced in 1 being 1.038 Nm 3 / h, the conversion of methane was therefore 68.6%. For chlorine, the conversion was 88%.
Les résultats ont conduit aux rendements et sélectivités suivants en chlorure de méthanesulfonyle produit :The results led to the following yields and selectivities of methanesulfonyl chloride produced:
Ramenée à la puissance de la lampe à indium, la productivité en chlorure de méthanesulfonyle a été de 4,65 kg/kW. Le tableau suivant résume les résultats des exemples précédents :Reduced to the power of the indium lamp, the productivity of methanesulfonyl chloride was 4.65 kg / kW. The following table summarizes the results of the previous examples:
Claims
1. Procédé de fabrication de chlorures d'alcanesulfonyle par réaction photo- chimique d'un alcane avec du chlore et du dioxyde de soufre, éventuellement en présence de chlorure d'hydrogène, caractérisé en ce que l'on utilise comme source lumineuse une lampe au mercure moyenne pression dopée à l'indium.1. Method for manufacturing alkanesulfonyl chlorides by photochemical reaction of an alkane with chlorine and sulfur dioxide, optionally in the presence of hydrogen chloride, characterized in that a lamp is used as the light source medium pressure mercury doped with indium.
2. Procédé selon la revendication 1 dans lequel on opère sous une pression allant de 1 à 15 bars relatifs, de préférence comprise entre 8 et 12 bars relatifs.2. Method according to claim 1 wherein one operates under a pressure ranging from 1 to 15 relative bars, preferably between 8 and 12 relative bars.
3. Procédé selon la revendication 1 ou 2 dans lequel la température réac- tionnelle est comprise entre 10 et 90°C et maintenue constante par injection de SO2 liquide dans la zone réactionnelle.3. Method according to claim 1 or 2 wherein the reaction temperature is between 10 and 90 ° C and kept constant by injection of liquid SO 2 into the reaction zone.
4. Procédé selon l'une des revendications 1 à 3 dans lequel l'alcane est le méthane, le mélange gazeux alimenté au réacteur comprenant 1 à 12 moles de dioxyde de soufre, 0,1 à 1 mole de chlore et 0,1 à 0,6 mole de chlorure d'hydrogène par mole de méthane.4. Method according to one of claims 1 to 3 wherein the alkane is methane, the gas mixture fed to the reactor comprising 1 to 12 moles of sulfur dioxide, 0.1 to 1 mole of chlorine and 0.1 to 0.6 moles of hydrogen chloride per mole of methane.
5. Procédé selon la revendication 4 dans lequel le mélange gazeux contient 5 à 7 moles de dioxyde de soufre, 0,7 à 0,9 mole de chlore et 0,4 à 0,5 mole de chlorure d'hydrogène par mole de méthane.5. The method of claim 4 wherein the gas mixture contains 5 to 7 moles of sulfur dioxide, 0.7 to 0.9 mole of chlorine and 0.4 to 0.5 mole of hydrogen chloride per mole of methane .
6. Procédé selon l'une des revendications 1 à 3 dans lequel l'alcane contient au moins 2 atomes de carbone, le mélange gazeux alimenté au réacteur comprenant 7 à 14 moles de dioxyde de soufre et 0,1 à 1 mole de chlore par mole d'alcane.6. Method according to one of claims 1 to 3 wherein the alkane contains at least 2 carbon atoms, the gas mixture supplied to the reactor comprising 7 to 14 moles of sulfur dioxide and 0.1 to 1 mole of chlorine per mole of alkane.
7. Procédé selon la revendication 6 dans lequel le mélange gazeux contient7. The method of claim 6 wherein the gas mixture contains
10 à 13 moles de dioxyde de soufre et 0,7 à 0,9 mole de chlore par mole d'alcane. 10 to 13 moles of sulfur dioxide and 0.7 to 0.9 mole of chlorine per mole of alkane.
Applications Claiming Priority (3)
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FR0015260A FR2817258B1 (en) | 2000-11-27 | 2000-11-27 | PROCESS FOR THE PHOTOCHEMICAL SULFOCHLORINATION OF GASEOUS ALKANES |
FR0015260 | 2000-11-27 | ||
PCT/FR2001/003143 WO2002042260A1 (en) | 2000-11-27 | 2001-10-11 | Method for photochemical sulphochlorination of gaseous alkanes |
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EP1339676A1 true EP1339676A1 (en) | 2003-09-03 |
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CA (1) | CA2429848A1 (en) |
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AR056857A1 (en) | 2005-12-30 | 2007-10-24 | U3 Pharma Ag | DIRECTED ANTIBODIES TO HER-3 (RECEIVER OF THE HUMAN EPIDERMAL GROWTH FACTOR-3) AND ITS USES |
JP5250199B2 (en) * | 2006-11-22 | 2013-07-31 | 日本曹達株式会社 | Method for producing trichloromethanesulfonyl chloride |
EP2459523A2 (en) * | 2009-07-30 | 2012-06-06 | Dow Global Technologies LLC | Improved process for the sulfochlorination of hydrocarbons |
TWI630916B (en) | 2009-11-13 | 2018-08-01 | 第一三共歐洲公司 | Materials and methods for treating or preventing her-3 associated diseases |
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US2709155A (en) * | 1952-11-12 | 1955-05-24 | Exxon Research Engineering Co | Photochemical sulfo-chlorination |
US2683076A (en) * | 1952-11-20 | 1954-07-06 | Standard Oil Dev Co | Recovery of gases in the sulfochlorination of hydrocarbons |
US2665305A (en) * | 1952-11-20 | 1954-01-05 | Standard Oil Dev Co | Treatment of sulfonyl chlorides |
DE2326414C2 (en) * | 1973-05-24 | 1982-02-25 | Bayer Ag, 5090 Leverkusen | Process for the production of m-chlorobenzenesulphonic acid chloride and m-dichlorobenzene |
JPS5221495B2 (en) * | 1974-03-28 | 1977-06-10 | ||
DE2544552C2 (en) * | 1975-10-04 | 1986-03-27 | Bayer Ag, 5090 Leverkusen | Alkyl sulfonic acid phenyl ester mixtures, processes for their preparation and their use |
EP0194931B1 (en) * | 1985-03-14 | 1989-11-15 | Societe Nationale Elf Aquitaine (Production) | Process and apparatus for the photochemical sulfochlorination of gaseous alkanes |
FR2777565B1 (en) * | 1998-04-21 | 2000-05-19 | Atochem Elf Sa | PROCESS FOR PHOTOCHEMICAL SULFOCHLORINATION OF GASEOUS ALKANES |
-
2000
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2001
- 2001-10-11 CA CA002429848A patent/CA2429848A1/en not_active Abandoned
- 2001-10-11 US US10/432,714 patent/US20040050683A1/en not_active Abandoned
- 2001-10-11 JP JP2002544396A patent/JP2004520281A/en not_active Withdrawn
- 2001-10-11 EP EP01978529A patent/EP1339676A1/en not_active Withdrawn
- 2001-10-11 KR KR10-2003-7007037A patent/KR20030062357A/en not_active Application Discontinuation
- 2001-10-11 WO PCT/FR2001/003143 patent/WO2002042260A1/en not_active Application Discontinuation
- 2001-10-11 CN CNA018222056A patent/CN1487918A/en active Pending
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JP2004520281A (en) | 2004-07-08 |
AU2002210635A1 (en) | 2002-06-03 |
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FR2817258B1 (en) | 2003-01-10 |
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