CN105622468A - Method for continuous production of petroleum sulfonate by micro chemical technology - Google Patents
Method for continuous production of petroleum sulfonate by micro chemical technology Download PDFInfo
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- C07C303/00—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides
- C07C303/32—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides of salts of sulfonic acids
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C309/00—Sulfonic acids; Halides, esters, or anhydrides thereof
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Abstract
A method for continuous production of petroleum sulfonate by a micro chemical technology includes the steps: a diluted petroleum fraction and diluted liquid sulfur trioxide continuously pass through a micro channel reactor integrating micro reaction and micro heat exchange and are subjected to reaction and heat exchange in the micro channel reactor, and then petroleum sulfonate is generated; and the obtained petroleum sulfonate is cooled in a subsequent micro channel heat exchanger further, outflows, and then enters a neutralizing salifying work section. The method is mainly characterized in that the reactants sulphur trioxide and petroleum fraction are subjected to reaction at a low mass ratio of 0.15-0.2, and the reaction device comprises the micro channel reactor and the micro channel heat exchanger. The micro chemical technology provides a technical support for continuous production of petroleum sulfonate with ten thousand ton grade industrial scale.
Description
Technical field
The present invention relates to liquid phase SO3The method of sulfonated petroleum fraction, particularly relates to macro work technology and produces the method (namely adopting the method that microreactor produces petroleum sulfonate continuously) of petroleum sulfonate continuously.
Background technology
Oil is the one-level strategic resource of relation national energy security, but oil recovery is generally relatively low at present. Petroleum sulfonate owing to raw material sources are wide, interfacial activity is strong and crude oil compatibility is good, good water solubility, less costly, it is believed that be the surface active agent for tertiary oil recovery of most commercial promise. Long distillate oil SO3Liquid phase sulfonation production petroleum sulfonate is quick strong exothermal reaction, and existing process route mainly adopts the continuous sulfonation method of autoclave liquid phase. This technique is run at low temperature 0��5 DEG C, and low temperature energy consumption is big. Owing to the microcosmic in reactor mixes uneven, the wide sulfonating agent concentration making the employing of this technique higher of residence time of material distribution; Additionally, sulfonating reaction heat is derived by external heat exchanger, in course of reaction, local temperature is high and mix uneven, causes unstable product quality.
CN101318112A describes employing hypergravity and liquid phase SO3Sulfonation technology prepares the method for anionic surface active agent for displacement of reservoir oil. At reaction temperature-10��50 DEG C, a certain proportion of distillate and sulfonating agent is made to react in supergravity reactor, simultaneously, product is made to circulate 20��70min in circulation stirring still and supergravity reactor, the active matter content of preparation reaches more than 40%, and supergravity reactor can strengthen mixing of materials. But its technique exists material back-mixing, two kinds of operator schemes all cannot solve quick, the original position removal problem of sulfonating reaction heat, and adopts outer loop back flow reaction product method to remove partial reaction heat.
Patent 201010206998 takes the lead in disclosing the technique of microreaction technology synthetic petroleum sulfonate, in single micro passage reaction, completes the exploitation of laboratory lab scale craft, obtain preferably effect. But when applying this technique and carrying out producing amplification, for promoting that in microreactor, material is evenly distributed, reaction velocity is 2.5-10 times of lab scale craft, now, in single microreactor, exchange capability of heat is not enough, cause reaction temperature higher, in active matter content and active matter, single disulfonate ratio is slightly lower, therefore, patent 201110397157 proposes classification process for sulfonation, heat of reaction is dispersed in two-stage microreactor, and strengthen original position shifting heat to reduce sulfonating reaction temperature, thus improving activity concentration and single sulfonic acid selectivity, increase active matter tensile property. Above-mentioned two patent gained activity concentration is up to 50%, and in active matter, monosulfonate concentration is 70 �� 2%, and active matter makes oil water interfacial tension be stably maintained at 10-2mN��m-1Order of magnitude level. Two pieces patent is devoted to by strengthening reacting replacing heat adjustment product slates, but reaction side thermal resistance is big, reaction time is short, moving hot speed limited, for improving single sulfonic acid selectivity further, we are by reducing reaction raw materials temperature, to control reaction temperature rising (patent 201210122668.4), working in coordination with by moving heat with original position, it is achieved the Effective Regulation of product structure, monosulfonate concentration is higher than 75%.
When carrying out the plant-scale petroleum sulfonate of ton and producing, (containing acid sludge) is affected by sulfur trioxide Feedstock fluctuation, under there is no independent pump control equipment, micro-response system more difficult stable operation of classification process for sulfonation, cause reaction continuity to be tested. Additionally, pumping unit lift is limited, raw material sulfur trioxide can be carried acid sludge secretly and enter micro-response system on the one hand, although activity concentration is high when reactant sulfonating agent and raw oil charge ratio are slightly higher on the other hand, but also has the sulfonic acid that reduces a lot and generate, formed and be less susceptible to be dissolved in the product of reaction system and be deposited in micro-response system, during long-play, system pressure drop can be gradually increased, until flow is lower than assumed load, it is impossible to meets normal production.
Therefore, macro work technology produces the technique that petroleum sulfonate must be taked to update continuously, to adapt to existing production status.
Summary of the invention
For guaranteeing the micro passage reaction continuous production for ton scale petroleum sulfonate, it is proposed to techniques below method.
The method includes: by the sulfan of the petroleum distillate of dilution and dilution continually by a micro passage reaction integrating micro-reaction and micro-heat exchange, and reaction and heat exchange in micro passage reaction, generate mahogany acid, mahogany acid flows out after cooling further in a follow-up micro channel heat exchanger, enter back into neutralization Cheng Yan workshop section, generate petroleum sulfonate. Being characterized mainly in that of the method, makes reactant sulfur trioxide and petroleum distillate react in low-mass ratio 0.15��0.2 scope; Reaction heat, by industrial circulating water removal major part, obtains the mahogany acid that temperature is 30��55 DEG C; Another of the method is characterized mainly in that, consersion unit is only made up of a described micro passage reaction and an independent micro channel heat exchanger.
In method of the present invention, the mass ratio of reactant sulfur trioxide and petroleum distillate refers to the quality of pure sulfur trioxide and the ratio of pure fraction oil quality in the petroleum distillate of dilution in the sulfonating agent of dilution, namely all disregarding the quality of diluent or solvent, this solvent includes the dichloroethanes reclaimed. Mass concentration after the dilution of reactant sulfur trioxide and petroleum distillate respectively 20��30% and 50% (identical with the patent 201010206998.2,201110397157.9 of applicant). When described petroleum distillate is selected from low boiling fraction such as diesel oil distillate, the reaction in low-mass ratio 0.15��0.18 is interval of reactant sulfur trioxide and petroleum distillate, when described petroleum distillate is selected from high boiling range fraction such as wax oil fraction, the reaction in mass ratio 0.18��0.2 is interval of reactant sulfur trioxide and petroleum distillate. Micro passage reaction integrates micro-reaction and micro-heat exchange, and micro-reaction refers to and the petroleum distillate of described dilution and the sulfan of dilution carry out microcosmic mixing the micro-chemical engineering unit operation reacted; Micro-heat exchange in method refers to that the material that micro-reaction gained includes mahogany acid carries out micro-chemical engineering unit operation of in-situ heat exchange. The micro-reaction of micro-chemical engineering unit operation carries out on a series of and that line interlacing is integrated micro-reaction channel with micro-heat exchanger channels with micro-heat exchange, this is reaction channel and micro-heat exchanger channels composition micro passage reaction slightly, and it is arbitrary known size between 0.1-2.0mm that micro-reaction channel and micro-heat exchanger channels have equivalent diameter.
In method of the present invention, being made up of the micro-system producing mahogany acid micro passage reaction and micro channel heat exchanger, the pressure drop of this micro-system is 0��0.5MPa, it is preferable that run under 0��0.2MPa pressure drop. This parameter can reduce the requirement to raw material pump, reduces power consumption simultaneously.
In method of the present invention, the diluent of petroleum distillate and sulfur trioxide is dichloroethanes, the recyclable recycling of solvent dichloroethanes. When adopting recycling design diluent liquid sulfur trioxide raw material, the sulfan of dilution settles contained acid sludge in advance before entering micro passage reaction, and the acid sludge regularly gone out by gravitational settling is directly discharged in the connection pipeline between reaction workshop section and neutralization Cheng Yan workshop section together flow out with product mahogany acid, enter follow-up neutralization Cheng Yan workshop section, react with gained mahogany acid with ammonia for nertralizer, this reaction carries out in existing any feasible known device, such as titanium material homogenizer.
Technique effect
The present invention is under low reaction thing sulfur trioxide with distillate charge ratio, higher product mahogany acid (salt) concentration of relatively still reaction technique and surface tension characteristics value can be obtained, simultaneously, sulfur trioxide consumption relatively still reaction technique reduces by 38.5��50% (with autoclave consumptions 0.325 for benchmark), the minimizing of sulfur trioxide material consumption amount significantly reduces the generation neutralizing reaction workshop section inorganic salt by-product, controls to provide strong technical support for subsequent treatment and cost of material.
Accompanying drawing explanation
Fig. 1, microsystem device and flow process, wherein: 1-micro passage reaction, 2-micro channel heat exchanger, 3-acid sludge settlement separator; A-flux oil, B-sulfonating agent, F1-effusion meter, F2-effusion meter, C1-circulating cooling water waterborne, C2-cooling water return, P-goes to neutralize workshop section.
Detailed description of the invention
The present invention is specifically addressed by following limiting examples.
Equipment and flow process: following enforcement takes the microsystem device shown in Fig. 1 and flow process to carry out. Microsystem device is made up of a micro passage reaction and an independent micro channel heat exchanger. In version identical with the microreactor related in the patent 201010206998 of applicant and patent 201110397157 or micro-heat exchanger, on scale yardstick, micro passage reaction and micro channel heat exchanger in device have done parallel processing and amplifying, and parallel two set switchings use. In this device, micro passage reaction (1) is made up of a series of and that line interlacing is integrated micro-reaction channel and micro-heat exchanger channels, this carries out micro-reaction and two micro-chemical engineering unit operations of micro-heat exchange on reaction channel and micro-heat exchanger channels slightly respectively, and it is arbitrary known size between 0.1-2mm that micro-reaction channel and micro-heat exchanger channels have equivalent diameter; Micro passage reaction takes the reaction-heat exchange pattern of cross-flow. Micro channel heat exchanger (2) involved by this device is independent heat transmission equipment, and Main Function is that micro channel heat exchanger takes countercurrent heat-transfer form in order to reduce product temperatur further.
The sulfur trioxide pipeline of micro-system is pre-configured with the separator (3) of a sedimentation acid sludge. This separator designs has a middle part charging aperture, a top discharge mouth (clear liquid), and a bottom drain hole. Wherein, middle part charging aperture is sulfur trioxide supplied materials mouth, top discharge mouth connects the micro passage reaction in microsystem device, bottom discharge mouth is then connected on the product exit pipeline of micro channel heat exchanger (reaction workshop section and the connection pipeline neutralized between Cheng Yan workshop section, such as Fig. 1) by valve. The bottom of this separator is designed to conical hopper shape, and middle part charging aperture upper edge designs a sloping baffle, so that contained acid sludge is deposited to bottom in raw material sulfur trioxide, periodic exhaustion also neutralizes acid sludge, it is to avoid increase resistance in its access arrangement.
Process and operation: adopting the sulfonating agent prepared in advance and petroleum distillate is raw material, respectively through pipeline transport pump, and adopt industrial flow meter to control flow, then access micro-system through valve. Before two reaction masses are cut microsystem device, first according to Microsystems Design Load Regulation sulfonated oil flow, sulfonation dosage presses in the material little range intervals regulation and control than 0.15��0.2, both are first squeezed into a little time in still, after stability of flow balances, more respectively sulfonated oil and sulfonating agent are switched in micro passage reaction (MCR). It is recirculated cooling water that reaction moves thermal medium, and because micro-heat exchanger channels integrated in micro passage reaction is minute yardstick, the passage in micro channel heat exchanger is also minute yardstick, and cooling water inlet pipe road domestic demand arranges filter, removes impurities in water and avoids blocking microchannel; The upper coolant-temperature gage of recirculated cooling water is determined by public work, and it is 15��25 DEG C that application claims cools down coolant-temperature gage waterborne, less than 30 DEG C, to increase driving force of heat transfer (temperature difference). After sulfonating reaction completes in micro passage reaction (MCR), product enters further heat exchange in micro channel heat exchanger (MCHE) immediately. Sulfonated products after heat exchange enters product storage tank or goes to neutralize workshop section.
Sample and analyze: respectively at pipeline place, the bottom sampling mahogany acid of microsystem device outlet and caldron process, with generation petroleum sulfonate and inorganic salt in the ammonia that mass concentration is 23%, with pH value 8��10 for neutralizing reaction end. Neutralizing sample adopts the complete analysis method (gravimetric method) of extract and separate and evaporation operation to analyze active matter, unsulfonated oil, inorganic salt and volatile content; Chromatography qualitative activity thing is the concentration of single double; two polysulfonates with unsulfonated oil ratio and active matter; Oil water interfacial tension adopts to rotate and drips interfacial tensimeter TX500C mensuration.
Embodiment 1
Diesel oil is the production of raw material:
With mass concentration be 50% diesel oil based flux oil for raw material, micro-system respectively raw oil be 1000,1200, commissioning test under the traffic load of 1400kg/h, raw oil flow is controlled by effusion meter, correspondingly, by the sulfonating agent SO that mass concentration is 25%3Solution is with flow 400kg/h, 450kg/h, 450kg/h material controlling respectively, the i.e. mass ratio (SO of reactant sulfur trioxide and petroleum distillate3/ Oil) it is 0.2,0.19,0.16. Under above-mentioned raw materials oil load and reactant ratio, adopt first set micro system equipment, micro passage reaction in equipment has the parallel multi-channel of 1.25mm equivalent, and the drag overall characteristics design value of this set micro-system is 0.08MPa/ (2000kg/h water). In course of reaction, micro passage reaction and micro channel heat exchanger all cool down water for heat transferring medium with plant circulation, and cooling water accesses reactor and heat exchanger parallel, and flow is non-interference, cooling water temperature 24��28 DEG C. Reaction temperature is measured point and is positioned in the connecting tube between micro passage reaction and micro channel heat exchanger, and final drop temperature is measured point and is positioned on micro channel heat exchanger outlet. The drop measurement point of micro-system includes flux oil import and sulfonating agent import, lays respectively at micro passage reaction two inlet tube front position. Under above-mentioned different load, amount to operation 120 hours, the flow of reactant petroleum distillate and charging SO continuously3/ Oil mass is than measured value, and micro-system resistance, reaction temperature and drop temperature are shown in table 1, and the operation result such as table 1 shows.
Gained mahogany acid enters and neutralizes Cheng Yan workshop section, with generation petroleum sulfonate and inorganic salt in the ammonia that mass concentration is 23%, with system pH 8��10 for neutralizing reaction end.
In process conditions shown in table 1, reaction temperature is substantially distinguished from still reaction technique (referring to table 3 still reaction technique), reaches 50-60 DEG C, and the temperature of charge in micro channel heat exchanger is higher than drop temperature, is more than 40 DEG C. Under this reaction temperature, in diesel oil based raw material, gum level is low, will not too much produce colloid sulfonated products, and micro passage reaction can long period stable operation.
In the reaction result shown in table 1, in product except key component, all the other are volatilizable part, the moisture that the solvent brought into including raw material and N-process are brought into. After deduction solvent, active matter (petroleum sulfonate), unsulfonated oil and inorganic salt content the activity concentration calculated reaches 48.9��53.8%. And list sulfonic acid concentrations reaches 79��85%, higher than classification process for sulfonation, simultaneously also above autoclave production technology. Show, at low SO3Under/Oil charge-mass ratio, active matter content does not reduce, and single sulfonated bodies is higher simultaneously.
The process conditions of table continuous sulfonation of diesel oil in 1,120 hours and operation result
Embodiment 2
Wax oil is the production of raw material:
By effusion meter, the wax oil base flux oil that concentration is 50% is controlled flow run under 1200kg/h load, by the sulfonating agent SO that concentration is 25wt.%3Solution is with flow 450��480kg/h material controlling, and namely reactant sulfur trioxide is 0.19��0.2 with the mass ratio of petroleum distillate. Wax oil sulfonation production takes direct switching, uninterrupted with diesel oil sulfonation production. Being affected by wax oil mobility, micro passage reaction adopts the more another set of equipment of number of channels, and to reduce the flow resistance under same load, the drag characteristic design load of this cover system is 0.05MPa/ (2000kg/h water). Meanwhile, for reducing reaction temperature, except cooling water inlet temperature is reduced to about 20 DEG C, the charge-mass ratio of reactant sulfur trioxide and wax oil foundation stone oil distillate control and diesel oil based technique for producing raw material quite, namely above-mentioned 0.19��0.2. It is as shown in table 2 that wax oil based raw material oil produces 55 hours continuous service datas of petroleum sulfonate.
Gained mahogany acid enters and neutralizes Cheng Yan workshop section, with generation petroleum sulfonate and inorganic salt in the ammonia that mass concentration is 23%, with system pH 8��10 for neutralizing reaction end.
In service data shown in table 2, wax oil based raw material oil solution flow is on a declining curve, it is cyclic fluctuation (decision of production process operating mode) mainly due to sulfonating agent flow, when causing wax oil sulfonation, temperature is gradually increased, so that gum components generation sulfonation in wax oil, micro-system resistance increases. Sulfonating agent fluctuation is mainly due to it containing the higher acid sludge impurity of toughness, and producing continuously that application macro work technology is carried out by this acid sludge produces negative effect. Therefore, the present invention proposes sulfonating agent supplied materials is carried out pretreatment, namely settles the pretreatment of acid sludge so that it is contained minute quantity acid sludge does not enter micro-system.
Table 1 and table 2 show: the pressure drop of diesel oil sulfonation system is lower than wax oil sulfonation system, and stability is also better than wax oil reaction system; Diesel oil sulfonating reaction temperature-controllable is at 50-60 DEG C, and wax oil sulfonating reaction temperature then reaches 60-70 DEG C. In wax oil sulfonated products, unsulfonated oil concentration is higher, still has more reactant not to be sulfonated. According to the present invention, sulfonating reaction thing SO3Consumption reduces, the SO of saving3The sulfonation production again of unsulfonated oil can be continued on for.
The process conditions of table 2, wax oil based raw material oil sulfonation production petroleum sulfonate continuously and operation result
Comparative example 1
The bavin of caldron process, wax oil produce petroleum sulfonate:
The raw oil of caldron process and micro-Chemical Engineering Technology same concentrations and sulfonating agent. In caldron process, the reaction-ure feeding ratio that diesel oil based flux oil is raw material is 0.3, and the reaction-ure feeding ratio that wax oil base flux oil is raw material is 0.33, and reaction heat removes with low temperature cold saline. The product of this technique of sampling analysis is constituted, and is listed in table 3.
Comparative example and comparative example service data, the present invention is under less reaction-ure feeding ratio, Product Activity substrate concentration, single sulfonic acid selectivity are above prior art level, wherein, all quite a lot of compared with caldron process with single sulfonic acid selectivity with the Product Activity substrate concentration that diesel oil is raw material.
Table 3, caldron process bavin, wax oil sulfonation operation result
The present invention is micro-Chemical Engineering Technology provides technical guarantee for the continuous prodution of ton commercial scale petroleum sulfonate.
Claims (8)
1. the method that macro work technology produces petroleum sulfonate continuously, it is characterized in that: by the petroleum distillate of the sulfan of dilution and dilution continually by a micro passage reaction, and react with low-mass ratio in micro passage reaction, generate mahogany acid, gained mahogany acid flows out after cooling further in a follow-up micro channel heat exchanger, goes to neutralize Cheng Yan workshop section and obtains petroleum sulfonate.
2. method according to claim 1, wherein, low-mass ratio refers to the ratio of described sulfan and petroleum distillate, and value is 0.15��0.2.
3. method according to claim 1, wherein, described micro passage reaction integrates micro-reaction and micro-heat exchange, and micro-reaction refers to and the petroleum distillate of described dilution and the sulfan of dilution carry out microcosmic mixing the micro-chemical engineering unit operation reacted; Micro-heat exchange refers to that the material that micro-reaction gained includes mahogany acid carries out micro-chemical engineering unit operation of in-situ heat exchange.
4. method according to claim 3, wherein, the micro-reaction of micro-chemical engineering unit operation carries out on a series of and that line interlacing is integrated micro-reaction channel with micro-heat exchanger channels with micro-heat exchange; The micro passage reaction that micro-reaction channel and micro-heat exchanger channels composition is described, and to have equivalent diameter be arbitrary known size between 0.1-2mm.
5. method according to claim 1, wherein, the system producing mahogany acid being made up of micro passage reaction and micro channel heat exchanger, its operation pressure drop is 0��0.5MPa.
6. method according to claim 1, wherein, the diluent of petroleum distillate and sulfan is dichloroethanes, the recyclable recycling of dichloroethanes; When adopting recovered solvent dichloroethanes dilution sulfur trioxide, the sulfan of dilution settles contained acid sludge in advance before entering micro passage reaction, and regularly the acid sludge of sedimentation is directly discharged in the mahogany acid material of outflow micro channel heat exchanger, go to neutralize Cheng Yan workshop section with mahogany acid.
7. the method according to claim 1 or 6, wherein, the mass concentration of the petroleum distillate of dilution and the sulfan of dilution respectively 50% and 20��30%.
8. method according to claim 1, wherein, neutralizes Cheng Yan workshop section and reacts with mahogany acid for nertralizer with ammonia, and this reaction carries out in existing any feasible known device.
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| CN201410581757.4A CN105622468A (en) | 2014-10-27 | 2014-10-27 | Method for continuous production of petroleum sulfonate by micro chemical technology |
| PCT/CN2014/090450 WO2016065662A1 (en) | 2014-10-27 | 2014-11-06 | Continuous petroleum sulfonate production method using micro-chemical technology |
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| CN201410581757.4A CN105622468A (en) | 2014-10-27 | 2014-10-27 | Method for continuous production of petroleum sulfonate by micro chemical technology |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109456303A (en) * | 2018-11-20 | 2019-03-12 | 武汉联续流化学科技有限公司 | The method that micro passage reaction continuously synthesizes sulfuric acid vinyl ester and sulfuric acid 4- ethylene methacrylic ester |
| CN111704561A (en) * | 2020-05-18 | 2020-09-25 | 中国日用化学研究院有限公司 | Method for preparing alkyl diphenyl ether sulfonate by sulfonating liquid-phase sulfur trioxide |
| CN113549209A (en) * | 2021-08-05 | 2021-10-26 | 四川鸿鹏新材料有限公司 | Method for continuously producing AEO (aerated Acoustic Acrylonitrile) and AES (atomic emission Spectrometry) by using microchannel reactor and microchannel system |
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| US3956372A (en) * | 1973-11-02 | 1976-05-11 | Marathon Oil Company | Process for the production of petroleum sulfonate |
| CN101318112A (en) * | 2008-07-18 | 2008-12-10 | 北京化工大学 | Method for preparing anionic surface active agent for displacement of reservoir oil |
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| CN102295586A (en) * | 2010-06-23 | 2011-12-28 | 中国科学院大连化学物理研究所 | Method for synthesizing petroleum sulfonate in micro reactors |
| CN103130690A (en) * | 2011-12-02 | 2013-06-05 | 中国科学院大连化学物理研究所 | Method of producing petroleum sulfonate by micro reaction system grading sulfonation |
| CN103373945A (en) * | 2012-04-23 | 2013-10-30 | 中国科学院大连化学物理研究所 | Method for regulating and controlling product distribution in process of producing mahogany petroleum sulfonate through micro-reaction system |
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2014
- 2014-10-27 CN CN201410581757.4A patent/CN105622468A/en active Pending
- 2014-11-06 WO PCT/CN2014/090450 patent/WO2016065662A1/en active Application Filing
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| US3956372A (en) * | 1973-11-02 | 1976-05-11 | Marathon Oil Company | Process for the production of petroleum sulfonate |
| CN101318112A (en) * | 2008-07-18 | 2008-12-10 | 北京化工大学 | Method for preparing anionic surface active agent for displacement of reservoir oil |
| CN102190605A (en) * | 2010-03-03 | 2011-09-21 | 北京中石大节能科技发展有限责任公司 | Petroleum sulfonate anionic surfactant and preparation method thereof |
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| CN103373945A (en) * | 2012-04-23 | 2013-10-30 | 中国科学院大连化学物理研究所 | Method for regulating and controlling product distribution in process of producing mahogany petroleum sulfonate through micro-reaction system |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109456303A (en) * | 2018-11-20 | 2019-03-12 | 武汉联续流化学科技有限公司 | The method that micro passage reaction continuously synthesizes sulfuric acid vinyl ester and sulfuric acid 4- ethylene methacrylic ester |
| CN111704561A (en) * | 2020-05-18 | 2020-09-25 | 中国日用化学研究院有限公司 | Method for preparing alkyl diphenyl ether sulfonate by sulfonating liquid-phase sulfur trioxide |
| CN111704561B (en) * | 2020-05-18 | 2023-03-03 | 中国日用化学研究院有限公司 | Method for preparing alkyl diphenyl ether sulfonate by sulfonating liquid-phase sulfur trioxide |
| CN113549209A (en) * | 2021-08-05 | 2021-10-26 | 四川鸿鹏新材料有限公司 | Method for continuously producing AEO (aerated Acoustic Acrylonitrile) and AES (atomic emission Spectrometry) by using microchannel reactor and microchannel system |
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|---|---|
| WO2016065662A1 (en) | 2016-05-06 |
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