CN1053174C - Method for sulfonating liquid state organics by gas phase sulfur trioxide and its equipment - Google Patents
Method for sulfonating liquid state organics by gas phase sulfur trioxide and its equipment Download PDFInfo
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- CN1053174C CN1053174C CN96107060A CN96107060A CN1053174C CN 1053174 C CN1053174 C CN 1053174C CN 96107060 A CN96107060 A CN 96107060A CN 96107060 A CN96107060 A CN 96107060A CN 1053174 C CN1053174 C CN 1053174C
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Abstract
The present invention relates to a method for sulfonating and sulfatizing liquid state organic matters and devices thereof. The liquid state organic matters comprise benzene, alkylbenzene containing carbon atom numbers C7 to C18, fat alcohol ether containing C8 to C20 and alpha-olefin containing C8 to C30. The liquid state organic matters and gas mixture containing sulfur trioxide are simultaneously and respectively sprayed from the central spraying holes of nozzles and the annular space of the nozzles into a circulating reactor for a sulfonation reaction; circulating flow is formed both at the inner parts and the outer parts of a flow guiding cylinder in the reactor, and enhances heat transfer and mass transfer; reacting heat is sunk through cooling mediums in jacket type or close winding coil type flow guiding cylinders, and/or reactor jackets and/or a circular cooler. Because the contact areas of reacting objects in two phases are large, and positioning time at a centralization heat sinking area is short, the reacting effect is good.
Description
The present invention relates to a kind of method and equipment thereof with the gas phase sulfur trioxide sulfonating liquid state organics.
At present, the sulphonating agent that is used for sulfonating liquid state organics has the vitriol oil, oleum and sulphur trioxide etc.During with the vitriol oil or oleum sulfonation, owing to generate the carrying out that water is unfavorable for sulfonation reaction during reaction, sulfuric acid is excessive often for this reason, the spent acid amount is bigger after the sulfonation, pollute, and be that sulphonating agent then can be avoided above-mentioned shortcoming with sulphur trioxide, but its processing method at present, only limit to the organic sulfonation of macromolecule, especially be subjected to thermo-responsive organic sulfonation, certain degree of difficulty is arranged on the implementation for the small molecular weight organism.Sulfonation reactor commonly used at present has still formula, falling film type etc.The alternate contact area of still formula sulfonation reactor is little, and transmission effect is poor, and production efficiency is low; Falling film type sulfonation reactor complex structure, the operational condition harshness, during especially for some quick strong exothermal reaction, still difficulty is avoided local superheating, reduces the selectivity of reaction.Through China Patents Information Center's retrieval, retrieve some background technologies (seeing China Patents Information Center's search report) about sulfonation reaction.Wherein, in the patent documentation of CN85109591A, narrated a kind of benzene sulfonated injection circulation reactor that is used for, the steam of benzene is at a high speed to spray into reactor and by the sulfonation of the institute of the sulfate liquid in the device, its nozzle is a mono-layer tube, only is used for spraying benzene vapor, the jet velocity height, the guide shell top must be baffled, and this invention mainly solves the plant issue of the vitriol oil and benzene reaction.Also having in the patent documentation of US3935237, introduce a kind of method with gas phase sulfur trioxide sulfonating liquid state toluene, is that the sulphur trioxide segmentation is fed multistage still formula stirred reactor sulfonating liquid state toluene, but its complex technical process, to implementing to bring certain degree of difficulty.
The purpose of this invention is to provide a kind of method and equipment thereof with the gas phase sulfur trioxide sulfonating liquid state organics.This method technology is simple, pollution-free, is easy to promotion and implementation.This equipment can make the contact area between the two phase reaction thing big, and short in the concentrated heat release zone residence time, and reaction effect is good, sulphur trioxide specific absorption height.
Method of the present invention realizes by following manner.
This method with the gas phase sulfur trioxide sulfonating liquid state organics, this liquid state organics includes benzene, carbonatoms is C
7～C
18Alkylbenzene, C
8～C
20Fatty alcohol-ether, C
8～C
30Alpha-olefin, adopt injection circulation reactor, be provided with guide shell in this reactor, the below of this guide shell is provided with the double tubular nozzle, above-mentioned a kind of liquid state organics is sprayed in the reactor from the center of orifices of nozzle, and the gas mixture that makes trioxygen-containing sulphur is that also spraying into simultaneously in ring week of above-mentioned liquid state organics injection stream carried out sulfonation reaction in the reactor from the annular space spray orifice of nozzle, and in this reactor, form cycling stream, temperature of reaction is 0 ℃～100 ℃, sulphur trioxide concentration of volume percent in the described sulphur trioxide gas mixture is 2%～20%, all the other are rare gas element or exsiccant air, adding the interior described sulphur trioxide of reactive system and the mol ratio of liquid state organics is 0.2～2.0: 1, and the spouting velocity of described liquid state organics is 10～40m/s.
The employed equipment of this method is injection circulation reactor, be provided with guide shell in the housing of this reactor, below guide shell, be provided with the double tubular nozzle, liquid state organics sprays in the reactor from the center of orifices of nozzle, the gas mixture of trioxygen-containing sulphur sprays in the reactor from the annular space spray orifice of nozzle simultaneously, the liquid state organics of high-velocity jet is broken for gas phase the small bubbles of many size appropriateness, form in reactor by the density difference inside and outside spouting of liquid and the guide shell simultaneously and circulate, thereby increase substantially the reactor inner transmission matter, heat-transfer effect, tail gas is discharged by reactor head.This method can combine injection circulation reactor and recycle pump, outer loop water cooler, reaction solution is drawn by reactor bottom, can make its part through recycle pump, outer loop water cooler, again in the nozzle Returning reactor, can be equipped with the outer loop water cooler of different heat transfer area according to the requirement of reaction conditions, thereby in time shift out reaction heat to keep definite temperature of reaction.
In described method with the gas phase sulfur trioxide sulfonating liquid state organics, described liquid state organics is a toluene, temperature of reaction is 0 ℃～10 ℃, sulphur trioxide concentration of volume percent in the described sulphur trioxide gas mixture is 6～9%, all the other are the exsiccant air, the mol ratio that described sulphur trioxide and described toluene add in this reactive system is 0.3～0.4: 1, and the spouting velocity of described toluene is 15～25m/s.
In described method with the gas phase sulfur trioxide sulfonating liquid state organics, described liquid state organics is a dodecylbenzene, temperature of reaction is 54 ℃～56 ℃, sulphur trioxide concentration of volume percent in the described sulphur trioxide gas mixture is 4～9%, all the other are the exsiccant air, the mol ratio that described sulphur trioxide and described dodecylbenzene add in this reactive system is 1.00～1.05: 1, and the spouting velocity of described dodecylbenzene is 20m/s.
In described method with the gas phase sulfur trioxide sulfonating liquid state organics, described liquid state organics is C
14～C
16Alpha-olefin, temperature of reaction is 35 ℃～45 ℃, the sulphur trioxide concentration of volume percent in the described sulphur trioxide gas mixture is 3.5～6.5%, all the other are the exsiccant air, described sulphur trioxide and described C
14～C
16The mol ratio that adds in this reactive system of alpha-olefin be 1.05～1.15: 1, described C
14～C
16The spouting velocity of alpha-olefin be 20m/s.
In described method with the gas phase sulfur trioxide sulfonating liquid state organics, described liquid state organics is C
12～C
14Fatty alcohol-ether, temperature of reaction is 30～33 ℃, the sulphur trioxide concentration of volume percent in the described sulphur trioxide gas mixture is 2.5～5.5%, all the other are the exsiccant air, described sulphur trioxide and described C
12～C
14The mol ratio that adds in this reactive system of fatty alcohol-ether be 1.01～1.05: 1, described C
12～C
14The spouting velocity of fatty alcohol-ether be 20m/s.
The utility model is described in further detail below in conjunction with accompanying drawing.
Fig. 1 is the interface chart of injection circulation reactor, recirculation cooler
Fig. 2 is the synoptic diagram with injection circulation reactor of close drum tubular type guide shell
Fig. 3 is the hollow jacketed type guide shell synoptic diagram in the injection circulation reactor
Fig. 4 is the nozzle synoptic diagram
As Fig. 1, Fig. 2, shown in Figure 4, equipment with the gas phase sulfur trioxide sulfonating liquid state organics includes injection circulation reactor 1, this injection circulation reactor 1 is to be provided with the guide shell 9 that two ends are opening in reactor shell, below this guide shell 9, be provided with nozzle 2, these nozzle 2 structures are double tubular, be formed with center of orifices 21 on its injector head, annular space spray orifice 22, this nozzle has two imports, be respectively the liquid state organics import 23 that communicates with described center of orifices 21, the sulphur trioxide combi inlet port 24 that communicates with described annular space spray orifice 22, be provided with tail gas outlet 25 at the top of described reactor shell, on described reactor shell diapire, be provided with reaction solution outlet 26.
As Fig. 1, Fig. 2, shown in Figure 3, guide shell 9 can be the individual layer vertical barrel type, also can be hollow jacketed type or close drum tubular type.
The barrel of described guide shell is hollow chuck 27 as shown in Figure 3, and this chuck has heat-eliminating medium import and export 28,29, draws outside the described injection circulation reactor by pipeline respectively.
As shown in Figure 2, the barrel of described guide shell 9 is made of close wound coil, and the heat-eliminating medium import and export of this coil pipe is drawn outside the described injection circulation reactor by pipeline respectively.
As shown in Figure 2, the housing of injection circulation reactor 1 is generally round shape, and its outer wall can be provided with or not be provided with chuck 11, has heat-eliminating medium import and export 30,31 on the chuck 11.
Described nozzle can be one or more.Described guide shell also can be one or more.In use, following combination can be arranged: adopt 1 nozzle and 1 guide shell; Or adopt a plurality of nozzles and 1 guide shell; Or adopting a plurality of nozzles and a plurality of guide shell, the quantity of nozzle is more than or equal to the quantity of guide shell.
As shown in Figure 1 and Figure 2, equipment with the gas phase sulfur trioxide sulfonating liquid state organics also includes outer loop water cooler 4, also be provided with circulation fluid outlet 32 on the diapire of described injection circulation reactor 1, connect Y-tube by pipeline, the other two-port of this Y-tube connects liquid state organics input tube and recycle pump 5 inlets respectively, these recycle pump 5 outlets, by the reaction solution import of the described outer loop water cooler 4 of pipe connection, the outlet of the reaction solution of this outer loop water cooler 4 is by the liquid state organics import 23 of the described nozzle 2 of pipe connection.Outer loop water cooler 4 can adopt any type of recuperator.
Technical process of the present invention is illustrated in conjunction with Fig. 1, Fig. 2, Fig. 4.Liquid state organics sprays in the injection circulation reactor 1 from the center of orifices 21 of nozzle 2, simultaneously, the gas mixture 8 of trioxygen-containing sulphur also sprays in the injection circulation reactor 1 from the annular space spray orifice 22 of nozzle 2, at the strong cycling stream of guide shell 9 inside and outside formation, improved device inner fluid mechanics situation, strengthen heat transfer and mass transfer, also be convenient to shift out a large amount of reaction heat of quick generation.Tail gas 10 after the sulfonation is discharged from tail gas outlet 25.The reaction solution of being drawn by the bottom is divided into two strands, one is as reaction product 3, take away from reaction solution outlet 26, another strand is as circulating reaction liquid 7, discharge from circulation fluid outlet 32, and,, after cooling, return in the injection circulation reactor 1 by nozzle 2 again by recycle pump 5 warp let-off outer loop water coolers 4 with after fresh organic liquor 6 is mixed.As shown in Figure 1, water coolant or other heat-eliminating medium enter heat exchanger from the cooling medium inlet 33 of outer loop water cooler 4, discharge from heat-eliminating medium outlet 34.The reaction heat of process can take out by the three approach partition, promptly passes through jacketed type or close drum tubular type guide shell, reactor jacket, outer loop water cooler, adopts water coolant or other heat-eliminating medium to take away reaction heat.Because of the contact area between the two phase reaction thing is big, and short in the concentrated heat release zone residence time, reaction effect is good, sulphur trioxide specific absorption height.
Tail gas after the sulfonation generally can reach emission standard.Organic smog content is to be no more than 1.8 mg/litre, SO
3Content is no more than 50ppm.But, can take method in common, as filtration method, electric dust collection, centrifugal separation, solvent absorption etc. because the organic raw material difference of using is carried out organic smoke treated as need.
Embodiment 1: the sulfonation of toluene
Adopt device flow process shown in Figure 1 to carry out the sulfonation of toluene.The housing internal diameter of injection circulation reactor is 300mm, and height overall is 4000mm.Draft tube diameter is 200mm, and height is 2000mm.Guide shell is the individual layer vertical barrel type.The fresh toluene flow that enters system is 251/h, and the gas mixture of trioxygen-containing sulphur 6～9% (v/v) (all the other are dry air) is with 25Nm
3The flow of/h is entered in the injection circulation reactor 1 by nozzle clearance, send into outer loop water cooler 4 coolings-5 ℃～+ 5 ℃ with the fresh toluene that enters system through recycle pump 5 by the circulating reaction liquid that this reactor bottom is drawn, speed with 15～25m/s enters this reactor through the nozzle center hole then, keeps reactor temperature at 0 ℃～10 ℃.The mol ratio that described sulphur trioxide and toluene add in this reactive system is 0.3～0.4: 1.Para-isomeride accounts for 84～86% in the toluenesulphonic acids that reaction produces, and meta-isomer is not more than 1.1%, and does not have the spent acid generation.Sulphur trioxide concentration in the tail gas that reactor is discharged is not more than 0.04% (v/v).
Embodiment 2: the sulfonation of dodecylbenzene
Injection circulation reactor geomery and outer loop water cooler are with embodiment 1.Described liquid state organics is a dodecylbenzene, temperature of reaction is 54 ℃～56 ℃, sulphur trioxide concentration in the described sulphur trioxide gas mixture is 4～9% (v/v) (all the other are the exsiccant air), the mol ratio that described sulphur trioxide and described dodecylbenzene add in this reactive system is 1.00～1.05: 1, and the spouting velocity of described dodecylbenzene is 20m/s.The Witco 1298 Soft Acid quantum of output is 40Kg/h.
Embodiment 3: the sulfonation of alpha-olefin
Injection circulation reactor geomery and outer loop water cooler are with embodiment 1.Described liquid state organics is C
14～C
16Alpha-olefin, temperature of reaction is 35 ℃～45 ℃, the sulphur trioxide concentration in the described sulphur trioxide gas mixture is 3.5～6.5% (v/v) (all the other are the exsiccant air), described sulphur trioxide and described C
14～C
16The mol ratio that adds in this reactive system of alpha-olefin be 1.05～1.15: 1, described C
14～C
16The spouting velocity of alpha-olefin be 20m/s.Organism is C
14～C
16The alpha-olefin inlet amount be 40Kg/h, in the product unreacted reactant content less than 5%, SO in the tail gas after the sulfonation
3Content is 30ppm.
Embodiment 4: the sulphating of fatty alcohol-ether
Injection circulation reactor geomery and outer loop water cooler are with embodiment 1.Described liquid state organics is C
12～C
14Fatty alcohol-ether, temperature of reaction is 30～33 ℃, the sulphur trioxide concentration in the described sulphur trioxide gas mixture is 2.5～5.5% (v/v) (all the other are the exsiccant air), described sulphur trioxide and described C
12～C
14The mol ratio that adds in this reactive system of fatty alcohol-ether be 1.01～1.05: 1, described C
12～C
14The spouting velocity of fatty alcohol-ether be 20m/s.At the machine thing is C
12～C
14The fatty alcohol-ether inlet amount be 35kg/h.Unreacted reactant content is less than 5% in the product.SO in the tail gas after the sulfonation
3Content is 30ppm.
It is that sulphonating agent can fast reaction speed that the present invention adopts sulphur trioxide, avoid because of pollution and equipment corrosion problem with sulfuric acid sulfonation brought, have the injection circulation reactor of forcing internal recycle and have the outer loop water cooler and adopt, make reactant in injection circulation reactor, form the intensive internal recycle, reactant is in complete admixture, the reaction heat energy that SO 3 sulfonated liquid state organics is produced in time shifts out, basically concentration of reactants difference and temperature head have been eliminated, be applicable to put back by force fast and should be particularly useful for being subjected to thermo-responsive organic reaction, and help the industrialization and the serialization of process, thereby guarantee the quality of reaction product.Processes and apparatus of the present invention is simple, and control is convenient, and sulphur trioxide transformation efficiency height is pollution-free, is easy to promotion and implementation.
Claims (9)
1, a kind of method with the gas phase sulfur trioxide sulfonating liquid state organics is characterized in that this liquid state organics includes benzene, carbonatoms is C
7～C
18Alkylbenzene, C
8～C
20Fatty alcohol-ether, C
8～C
30Alpha-olefin, adopt injection circulation reactor, be provided with guide shell in this reactor, the below of this guide shell is provided with the double tubular nozzle, above-mentioned a kind of liquid state organics is sprayed in the reactor from the center of orifices of nozzle, and the gas mixture that makes trioxygen-containing sulphur is that also spraying into simultaneously in ring week of above-mentioned liquid state organics injection stream carried out sulfonation reaction in the reactor from the annular space spray orifice of nozzle, and in this reactor, form cycling stream, temperature of reaction is 0 ℃～100 ℃, sulphur trioxide concentration of volume percent in the described sulphur trioxide gas mixture is 2%～20%, all the other are rare gas element or exsiccant air, adding the interior described sulphur trioxide of reactive system and the mol ratio of liquid state organics is 0.2～2.0: 1, and the spouting velocity of described liquid state organics is 10～40m/s.
2, the equipment that claim 1 method is used, it is characterized in that this equipment includes injection circulation reactor (1), this injection circulation reactor is to be provided with the guide shell that two ends are opening (9) in reactor shell, below this guide shell, be provided with nozzle (2), this nozzle (2) structure is a double tubular, be formed with center of orifices (21) on its injector head, annular space spray orifice (22), this nozzle has two imports, be respectively the liquid state organics import (23) that communicates with described center of orifices (21), the sulphur trioxide combi inlet port (24) that communicates with described annular space spray orifice (22), be provided with tail gas outlet (25) at the top of described reactor shell, on described reactor shell diapire, be provided with reaction solution outlet (26).
3, equipment according to claim 2, it is characterized in that: the barrel of described guide shell can be the straight tube of individual layer, hollow chuck or close wound coil constitutes, and the heat-eliminating medium of described hollow chuck or close wound coil is into and out of all drawing outside the described injection circulation reactor (1) by pipeline respectively.
4, equipment according to claim 2 is characterized in that: described nozzle (2) is one or more, and described guide shell (9) is one or more.
5, equipment according to claim 2, it is characterized in that: this equipment also includes outer loop water cooler (4), also be provided with circulation fluid outlet (32) on the diapire of described injection circulation reactor (1), connect Y-tube by pipeline, the other two-port of this Y-tube, connect liquid state organics input tube and recycle pump (5) inlet respectively, this recycle pump (5) outlet is by the reaction solution import of the described outer loop water cooler of pipe connection (4), and the reaction solution outlet of this outer loop water cooler (4) is by the liquid state organics import (23) of the described nozzle of pipe connection (2).
6, the method with the gas phase sulfur trioxide sulfonating liquid state organics according to claim 1, it is characterized in that: described liquid state organics is a toluene, temperature of reaction is 0 ℃～10 ℃, sulphur trioxide concentration of volume percent in the described sulphur trioxide gas mixture is 6～9%, all the other are the exsiccant air, the mol ratio that described sulphur trioxide and described toluene add in this reactive system is 0.3～0.4: 1, and the spouting velocity of described toluene is 15～25m/s.
7, according to the described method of claim 1 with the gas phase sulfur trioxide sulfonating liquid state organics, it is characterized in that described liquid state organics is a dodecylbenzene, temperature of reaction is 54 ℃～56 ℃, sulphur trioxide concentration of volume percent in the described sulphur trioxide gas mixture is 4～9%, all the other are the exsiccant air, the mol ratio that described sulphur trioxide and described dodecylbenzene add in this reactive system is 1.00～1.05: 1, and the spouting velocity of described dodecylbenzene is 20m/s.
8, according to the described method of claim 1, it is characterized in that described liquid state organics is C with the gas phase sulfur trioxide sulfonating liquid state organics
14～C
16Alpha-olefin, temperature of reaction is 35 ℃～45 ℃, the sulphur trioxide concentration of volume percent in the described sulphur trioxide gas mixture is 3.5～6.5%, all the other are the exsiccant air, described sulphur trioxide and described C
14～C
16The mol ratio that adds in this reactive system of alpha-olefin be 1.05～1.15: 1, described C
14～C
16The spouting velocity of alpha-olefin be 20m/s.
9, according to the described method of claim 1, it is characterized in that described liquid state organics is C with the gas phase sulfur trioxide sulfonating liquid state organics
12～C
14Fatty alcohol-ether, temperature of reaction is 30～33 ℃, the sulphur trioxide concentration of volume percent in the described sulphur trioxide gas mixture is 2.5～5.5%, all the other are the exsiccant air, described sulphur trioxide and described C
12～C
14The mol ratio that adds in this reactive system of fatty alcohol-ether be 1.01～1.05: 1, described C
12～C
14The spouting velocity of fatty alcohol-ether be 20m/s.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96107060A CN1053174C (en) | 1996-07-12 | 1996-07-12 | Method for sulfonating liquid state organics by gas phase sulfur trioxide and its equipment |
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|---|---|---|---|
| CN96107060A CN1053174C (en) | 1996-07-12 | 1996-07-12 | Method for sulfonating liquid state organics by gas phase sulfur trioxide and its equipment |
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| CN1143064A CN1143064A (en) | 1997-02-19 |
| CN1053174C true CN1053174C (en) | 2000-06-07 |
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| CN96107060A Expired - Fee Related CN1053174C (en) | 1996-07-12 | 1996-07-12 | Method for sulfonating liquid state organics by gas phase sulfur trioxide and its equipment |
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|---|---|---|---|---|
| CN1298682C (en) * | 2004-04-29 | 2007-02-07 | 中国石油天然气股份有限公司 | Sulphonation reaction producing technology and equipment thereof |
| CN101585786B (en) * | 2009-07-09 | 2012-05-23 | 江南大学 | Method of using SO<3>-air mixture to produce alkylphenol sulfonic acid and salts thereof via film sulfonator sulfonated alkylphenol |
| CN101670225B (en) * | 2009-10-19 | 2012-01-18 | 浙江赞宇科技股份有限公司 | Sulfonated tail gas cycle-absorption method and cycle-absorption system |
| CN101966419A (en) * | 2010-09-01 | 2011-02-09 | 浙江赞宇科技股份有限公司 | Sulfur trioxide tail gas treating device in sulfonation reaction |
| CN104471123B (en) * | 2012-07-12 | 2016-09-28 | 陶氏环球技术有限责任公司 | Utilize the method that gaseous sulfur trioxide prepares carbon fiber |
| CN102731307B (en) * | 2012-07-17 | 2014-09-03 | 江苏同禾药业有限公司 | Preparation method of ethyl 6-oxo-8-chloro-caprylate |
| CN104174352A (en) * | 2014-09-04 | 2014-12-03 | 吉林化工学院 | Internal loop airlift reactor for refined white oil experiment |
| CN104557622B (en) * | 2014-12-18 | 2017-02-08 | 中国石油天然气股份有限公司 | Sulfonation reaction method and device |
| CN109438295B (en) * | 2018-11-29 | 2021-05-28 | 浙江秦燕科技股份有限公司 | Method for preparing CLT acid sulfonate by continuous reaction |
| CN112619566B (en) * | 2021-01-19 | 2022-04-12 | 山西潞安化工有限公司 | Multistage jet loop reactor for preparing ethylene by oxidative coupling of methane |
| CN112808181B (en) * | 2021-01-19 | 2022-04-08 | 山西潞安化工有限公司 | Jet loop reactor for preparing ethylene by oxidative coupling of methane |
| CN115337764A (en) * | 2022-07-29 | 2022-11-15 | 赞宇科技集团股份有限公司 | Alpha-sodium alkenyl sulfonate tail gas falling film absorption and recycling system and treatment process |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85109591A (en) * | 1985-12-30 | 1987-06-24 | 西北大学 | Circulating fluid benzenesulfonating reactor |
| US5136008A (en) * | 1990-08-25 | 1992-08-04 | Bayer Aktiengesellschaft | Polyurethane containing acryloyl or methacryloyl groups, and a process for their production and their use |
-
1996
- 1996-07-12 CN CN96107060A patent/CN1053174C/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85109591A (en) * | 1985-12-30 | 1987-06-24 | 西北大学 | Circulating fluid benzenesulfonating reactor |
| US5136008A (en) * | 1990-08-25 | 1992-08-04 | Bayer Aktiengesellschaft | Polyurethane containing acryloyl or methacryloyl groups, and a process for their production and their use |
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