CN1951915A - Sulfur trioxide gas jet sulfonation process and device for bisalkyl benzene - Google Patents
Sulfur trioxide gas jet sulfonation process and device for bisalkyl benzene Download PDFInfo
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- CN1951915A CN1951915A CN 200610102154 CN200610102154A CN1951915A CN 1951915 A CN1951915 A CN 1951915A CN 200610102154 CN200610102154 CN 200610102154 CN 200610102154 A CN200610102154 A CN 200610102154A CN 1951915 A CN1951915 A CN 1951915A
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Abstract
The invention discloses a sulfur trioxide gas injecting sulfonated technique of heavy alkylate benzene, which is characterized by the following: making composite gas of SO3/air into gas sprayer of SO3 gas injecting sulfonated reactor between 55 and 75 deg.c with spraying speed at 50-300m/s; entering heavy alkylate benzene into the SO3 gas injecting sulfonated reactor between 5 and 50 deg.c; setting the molar rate of heavy alkylate benzene and SO3 at 1.0-1.5:1; reacting heavy alkylate benzene and composite gas of SO3/air in the SO3 gas injecting sulfonated reactor for 1-5s; separating sulfonated product from non-reacted composite gas of SO3/air; cooling liquid phase under 40-80deg.c for 30-120min; hydrolyzing; neutralizing to obtain the product.
Description
Technical field
The present invention relates to a kind of technology and device thereof with each anion surfactant heavy alkylbenzene sulfonate of sulfur trioxide gas sulfonation of Heavy system.
Background technology
Heavy alkyl benzene (HAB) is the by product of producing in the detergent raw material alkylbenzene process, forms comparatively complexity, contains polyolefine, monoalkylated benzenes, dialkyl benzene, polyalkylbenzene, indane, tetralin, alkylnaphthalene, hexichol alkane and small amount of polar thing etc.Wherein very easily sulfonation of indane, tetralin and alkylnaphthalene, the difficult sulfonation of materials such as dialkyl benzene, polyalkylbenzene, but sulfonated bodies accounts for about 70%～90%.
Heavy alkylbenzene sulfonate has good reduction crude oil/water interfacial tension characteristic, and cheap, preparation technology is simple, be widely used in the every field of petroleum industry, as drilling well, oil recovery, crude oil demulsification, refining, and be three to adopt the main tensio-active agent that the displacement of reservoir oil, emulsified viscous oil, foam flooding are used.Along with the popularization of tertiary oil recovery, viscous oil recovery technology, the acute width of cloth of consumption of using tensio-active agent, especially heavy alkylbenzene sulfonate that recovers the oil increased in recent years.
At present, the technology of domestic production heavy alkylbenzene sulfonate mainly contains oleum method of sulfonation, SO
3Two kinds of gas membrane type sulfonation methods.The former is adopted by some middle-size and small-size producers mostly, and environmental pollution is quite serious, and production efficiency is low, and the quality instability of sulfonated product can not satisfy the requirement of ternary composite driving to the crude oil/water ultra low interfacial tension, and spent acid can't handle, and is eliminated gradually.The first half of the year in 2006, the continuous sulfonation full scale plant of sulfur trioxide gas membrane type that domestic first cover is produced heavy alkylbenzene sulfonate is gone into operation in grand celebration.Before this, domestic some unit is at SO
3Carried out the sulfonation test of heavy alkyl benzene on gas membrane-type sulfonation lab scale and the pilot plant.
SO
3The pattern of gas film sulfonation reactor is similar to shell-and-tube heat exchanger, (or otherwise) forms film from top to bottom at inside pipe wall to liquid state organics through the slit, sulfur trioxide gas also passes through in reaction tubes from top to bottom, and vigorous reaction takes place for the two, and reaction heat is removed by the water coolant of shell side.At present both at home and abroad many large-scale sulfonation producer mainly uses it for organic raw material such as sulfonated alkylbenzene, alpha-olefin, Fatty Alcohol(C12-C14 and C12-C18)/alcohol ether and produces sulfonic acid/Sulfates anion surfactant, SO
3Gas membrane type process for sulfonation technology is very ripe, according to incompletely statistics, and present domestic total SO
3Nearly hundred covers of membrane-type sulfonation device, overall throughput surpasses 120t/h, quality product near or surpass world level.
SO
3There is following problem in the gas film sulfonation reactor when being used for sulfonation of Heavy:
(1) the easy coking in film sulfonation reactor top influences liquid film uniform at the film sulfonation reactor inwall, thereby makes sulfonated product quality instability, especially shows the ability difference that reduces the crude oil/water interfacial tension.This is that the different sulfonation activity of forming differ bigger because the composition of heavy alkyl benzene is comparatively complicated on the one hand, as: the difficult sulfonation of materials such as dialkyl benzene, polyalkylbenzene, the very easily sulfonation of indane, tetralin and alkylnaphthalene; Be because the interior liquid film temperature of film sulfonation reactor reaches peak value on film sulfonation reactor top on the other hand, easily side reactions such as sulfonation component generation oversulfonate and oxidation of part in the heavy alkyl benzene, even the carbonization coking phenomenon appears.In addition, material is longer relatively in the residence time of film sulfonation reactor.
(2) viscosity of heavy alkyl benzene and sulfonated products thereof is higher, at SO
3Gas film sulfonation reactor lower semisection liquid film is too thick, influences sulphonation rate and quality product.
(3) with short production cycle, must often stop and clean.Influence the work-ing life of film sulfonation reactor on the one hand, substandard product is increased, production cost increases.
In addition, SO
3Also there is complex structure in the gas film sulfonation reactor, and apparatus processing, manufacturing accuracy and setting accuracy are had relatively high expectations, and investment cost is big; Turndown ratio is little, and processing condition are strict, is not suitable for the shortcomings such as situation of frequent start-stop car.
Summary of the invention
The purpose of this invention is to provide a kind of constant product quality, the long SO 3 gas jetting process for sulfonation and the device thereof that are used to prepare heavy alkylbenzene sulfonate of production cycle.
The SO of heavy alkyl benzene of the present invention
3The operation steps of gas injection process for sulfonation is as follows:
By the aerial concentration of volume percent of sulphur trioxide is 3～20%, is preferably in 6～15%, with SO
3/ air mixed becomes mixed gas also after filtering, and mixed gas enters SO
3The gas jet of gas blowing type sulfonation reactor, SO during air inlet body nozzle
3/ air gas mixture temperature is between 55～70 ℃, and in 50m/s～300m/s scope, heavy alkyl benzene enters SO from the gas speed of gas jet ejection
3Temperature during the gas blowing type sulfonation reactor is controlled between 5 ℃～50 ℃, heavy alkyl benzene and SO
3Mol ratio be controlled at 1.0～1.5: between 1, heavy alkyl benzene and SO
3/ air gas mixture is at SO
3Reacting in the gas blowing type sulfonation reactor, is 1～5 second in the intravital reaction times of reactor still, sulfonation reaction product and unreacted SO
3/ air gas mixture is from SO
3After the product outlet of gas blowing type sulfonation reactor is discharged, carry out gas-liquid separation, liquid phase is after cooling, continue reaction 30～120min down at 40～80 ℃, the water that under agitation adds heavy alkylbenzene sulfonic acid weight 0.5%～1.5% then, at 40～80 ℃ of following hydrolysis 10min～90min, promptly obtain the finished product heavy alkylbenzene sulfonate with alkaline solution pH6～9 that neutralize.
Aforesaid SO
3Be by combustion sulphur method, oleum acid gas formulation or liquid SO
3The method of evaporation preparation.
Aforesaid alkali is organic basess such as mineral alkalis such as sodium hydroxide, potassium hydroxide, ammonium hydroxide, magnesium hydroxide, calcium hydroxide and monoethanolamine, diethanolamine, trolamine, tetraalkylammonium hydroxide.
In order to realize the present invention, provide a kind of SO that is exclusively used in the preparation heavy alkylbenzene sulfonate
3The gas blowing type xanthator, it is by nozzle, the reactor kettle is formed, it is characterized in that nozzle comprises gas jet, the liquid distribution chamber, atomizing mouth, heavy alkyl benzene inlet and mixed gas inlet, gas jet communicates with the mixed gas inlet and is fixed in top, liquid distribution chamber, the heavy alkyl benzene inlet is positioned at the lateral bottom of liquid distributor, atomizing mouth is fixed in the liquid distribution chamber, the gas jet bottom enters in the atomizing mouth, the atomizing mouth top is an opening, the position of atomizing mouth top in the liquid distribution chamber is higher than the position of heavy alkyl benzene inlet in the liquid distribution chamber, nozzle is fixed in reactor kettle top, the atomizing mouth bottom enters in the reactor kettle, and there is the product outlet reactor kettle lower end.
Aforesaid nozzle can be on reactor kettle top with 2～60 uniform distribution.
Can also be fixed with guide shell in the aforesaid reactor kettle, the atomizing mouth bottom enters in the guide shell.
When carrying out sulfonation reaction, heavy alkyl benzene enters the liquid distribution chamber by the heavy alkyl benzene inlet, enters atomizing mouth through the overflow of atomizing mouth top again, flows downward SO then along the atomizing mouth inwall
3/ air gas mixture enters gas jet, SO by the gas phase inlet
3/ air gas mixture sprays in the reactor kettle with the heavy alkyl benzene contact and from atomizing mouth reacts sulfonation reaction product heavy alkylbenzene sulfonic acid that obtains and unreacted SO
3/ air gas mixture flows out from the product outlet.
Compare with existing membrane-type sulfonation technology, the SO 3 gas jetting process for sulfonation and the device of heavy alkyl benzene of the present invention have the following advantages:
(1) constant product quality, and the ability of the product reduction crude oil/water interfacial tension of injection process for sulfonation production is better than the product of membrane-type sulfonation explained hereafter.This is owing to the sulphonation rate difference of different process for sulfonation to different components in the heavy alkyl benzene, the peak value of sulfonation temperature is lower than film sulfonation reactor in the jet sulfonation reactor, and material is short than film sulfonation reactor in the residence time of jet sulfonation reactor, therefore, easy sulfonation material (as indane, tetralin, alkylnaphthalene etc.) in the heavy alkyl benzene is difficult for taking place side reactions such as oversulfonate and oxidation in jet sulfonation reactor, the composition of active ingredient more helps reducing the crude oil/water interfacial tension in the product that the injection process for sulfonation makes.
(2) principle of jet sulfonation reactor is to utilize flow at high speed phase (SO
3Therefore/air gas mixture) make liquid phase (heavy alkyl benzene) be dispersed into small drop, be very suitable for containing wax, be difficult for film forming, easily coking, (for example: sulfonation heavy alkyl benzene) be subjected to organism such as thermo-responsive.
(3) jet sulfonation reactor is simple in structure than film sulfonation reactor, and facility investment is few, operation and easy to maintenance, and turndown ratio is big, and the production cycle is long.
Description of drawings
Fig. 1 is a structural representation of the present invention
As shown in the figure, the 1st, heavy alkyl benzene inlet, the 2nd, mixed gas inlet, the 3rd, gas jet, the 4th, liquid distribution chamber, the 5th, atomizing mouth, the 6th, guide shell, the 7th, reactor kettle, the 8th, product outlet.
Embodiment
Embodiment 1: the sulfonation of heavy alkyl benzene
SO
3The gas blowing type sulfonation reactor is by nozzle, the reactor kettle is formed, nozzle is by gas jet 3, liquid distribution chamber 4, atomizing mouth 5, heavy alkyl benzene inlet 1 and mixed gas inlet 2 are formed, gas jet 3 communicates with mixed gas inlet 2 and is fixed in 4 tops, liquid distribution chamber, heavy alkyl benzene inlet 1 is positioned at liquid distributor 4 lateral bottoms, atomizing mouth 5 is fixed in the liquid distribution chamber 4, gas jet 3 bottoms enter in the atomizing mouth 5, atomizing mouth 5 tops are openings, the position of atomizing mouth 5 tops in liquid distribution chamber 4 is higher than the position of heavy alkyl benzene inlet 1 in liquid distribution chamber 4, nozzle is fixed in reactor kettle 7 tops, atomizing mouth 5 bottoms enter in the reactor kettle 7, and there is product outlet 8 reactor kettle 7 lower ends.
Heavy alkyl benzene (average molar mass: 265) under 25 ℃ with the flow velocity of 15kg/h continuously by SO
3The heavy alkyl benzene inlet 1 of gas blowing type sulfonation reactor enters liquid distribution chamber 4, through entering atomizing mouth 5 through atomizing mouth 5 top overflows again, flows downward SO along atomizing mouth 5 inwalls then again
3/ air (volume ratio 15%) mixed gas under 55 ℃ by SO
3The gas phase inlet 2 of gas blowing type sulfonation reactor enters gas jet 3, and the gas speed that sprays from gas jet 3 is 158m/s, SO
3/ heavy alkyl benzene raw materials components mole ratio 1.1: 1, SO
3/ air gas mixture sprays in the reactor kettle with the heavy alkyl benzene contact and from atomizing mouth reacts, at 5 seconds intravital reaction times of reactor still, sulfonation reaction product that obtains and unreacted SO
3/ air gas mixture is from SO
3After the product outlet 8 of gas blowing type sulfonation reactor is discharged, carry out gas-liquid separation, liquid phase is after cooling, continue reaction 40min down at 45 ℃, under agitation add 2.0kg/h water then, at 45 ℃ of following hydrolysis 15min, then with the sodium hydroxide solution pH8 heavy alkylbenzene sulfonic acid sodium that gets product that neutralizes.
Embodiment 2: the sulfonation of heavy alkyl benzene
Heavy alkyl benzene (average molar mass: 345) under 45 ℃ with the flow velocity of 10kg/h continuously by SO
3The liquid phase inlet 1 of gas blowing type sulfonation reactor enters liquid distribution chamber 4, through entering atomizing mouth 5 through atomizing mouth 5 top overflows again, flows downward SO along atomizing mouth 5 inwalls then again
3/ air (volume ratio 6%) mixed gas under 65 ℃ by SO
3The gas phase inlet 2 of gas blowing type sulfonation reactor enters gas jet 3 from the fast 238m/s of being of the gas of gas jet 3 ejections, SO
3/ heavy alkyl benzene raw materials components mole ratio 1.2: 1, SO
3/ air gas mixture sprays in the reactor kettle (7) with the heavy alkyl benzene contact and from atomizing mouth reacts, and the reaction times of (7) is 3 seconds in the reactor kettle, sulfonation reaction product that obtains and unreacted SO
3/ air gas mixture is from SO
3After the product outlet 8 of gas blowing type sulfonation reactor is discharged, carry out gas-liquid separation, liquid phase is after cooling, continue reaction 60min down at 60 ℃, under agitation add 0.8kg/h water then, at 65 ℃ of following hydrolysis 30min, then with the aqua calcis pH9 heavy alkyl benzene calcium sulfonate that gets product that neutralizes.
Embodiment 3: the sulfonation of heavy alkyl benzene
Heavy alkyl benzene (average molar mass: 320) under 40 ℃ with the flow velocity of 9.5kg/h continuously by SO
3The liquid phase inlet 1 of gas blowing type sulfonation reactor enters liquid distribution chamber 4, through entering atomizing mouth 5 through atomizing mouth 5 top overflows again, flows downward SO along atomizing mouth 5 inwalls then again
3/ air (volume ratio 4%) mixed gas under 60 ℃ by SO
3The gas phase inlet 2 of gas blowing type sulfonation reactor enters gas jet 3 from the fast 193m/s of being of the gas of gas jet 3 ejections, SO
3/ heavy alkyl benzene raw materials components mole ratio 1.15: 1, SO
3/ air gas mixture sprays in the reactor kettle (7) with the heavy alkyl benzene contact and from atomizing mouth reacts, and the reaction times of (7) is 4 seconds in the reactor kettle, sulfonation reaction product that obtains and unreacted SO
3/ air gas mixture is from SO
3After the product outlet 8 of gas blowing type sulfonation reactor is discharged, carry out gas-liquid separation, liquid phase is after cooling, continue reaction 20min down at 70 ℃, under agitation add 1.1kg/h water then,, get product with the triethanolamine solution pH6 that neutralizes then at 55 ℃ of following hydrolysis 30min.
Embodiment 4: the sulfonation of heavy alkyl benzene
Heavy alkyl benzene (average molar mass: 305) under 35 ℃ with the flow velocity of 46kg/h continuously by SO
3The liquid phase inlet 1 of gas blowing type sulfonation reactor enters liquid distribution chamber 4, through entering atomizing mouth 5 through atomizing mouth 5 top overflows again, flows downward SO along atomizing mouth 5 inwalls then again
3/ air (volume ratio 13%) mixed gas under 65 ℃ by SO
3The gas phase inlet 2 of gas blowing type sulfonation reactor enters gas jet 3 from the fast 169m/s of being of the gas of gas jet 3 ejections, SO
3/ heavy alkyl benzene raw materials components mole ratio 1.2: 1, SO
3/ air gas mixture sprays in the reactor kettle (7) with the heavy alkyl benzene contact and from atomizing mouth reacts, and the reaction times of (7) is 4 seconds in the reactor kettle, sulfonation reaction product that obtains and unreacted SO
3/ air gas mixture is from SO
3After the product outlet 8 of gas blowing type sulfonation reactor is discharged, carry out gas-liquid separation, liquid phase is after cooling, continue reaction 70min down at 60 ℃, under agitation add 0.9kg/h water then, at 55 ℃ of following hydrolysis 40min, then with the magnesium hydroxide solution pH7 heavy alkylbenzene sulfonic acid magnesium that gets product that neutralizes.
Claims (9)
1, a kind of SO 3 gas jetting process for sulfonation of heavy alkyl benzene is characterized in that comprising the steps:
By the aerial concentration of volume percent of sulphur trioxide is 3～20%, is preferably in 6～15%, with SO
3/ air mixed becomes mixed gas also after filtering, and mixed gas enters SO
3The gas jet of gas blowing type sulfonation reactor, SO during air inlet body nozzle
3/ air gas mixture temperature is between 55～70 ℃, and in 50m/s～300m/s scope, heavy alkyl benzene enters SO from the gas speed of gas jet ejection
3Temperature during the gas blowing type sulfonation reactor is controlled between 5 ℃～50 ℃, heavy alkyl benzene and SO
3Mol ratio be controlled at 1.0～1.5: between 1, heavy alkyl benzene and SO
3/ air gas mixture is at SO
3Reacting in the gas blowing type sulfonation reactor, is 1～5 second in the intravital reaction times of reactor still, sulfonation reaction product and unreacted SO
3/ air gas mixture is from SO
3After the product outlet of gas blowing type sulfonation reactor is discharged, carry out gas-liquid separation, liquid phase is after cooling, continue reaction 30～120min down at 40～80 ℃, the water that under agitation adds heavy alkylbenzene sulfonic acid weight 0.5%～1.5% then, at 40～80 ℃ of following hydrolysis 10min～90min, promptly obtain the finished product heavy alkylbenzene sulfonate with alkaline solution pH6～9 that neutralize.
2, the SO 3 gas jetting process for sulfonation of a kind of heavy alkyl benzene as claimed in claim 1 is characterized in that described SO
3Be by combustion sulphur method, oleum acid gas formulation or liquid SO
3The method of evaporation preparation.
3, the SO 3 gas jetting process for sulfonation of a kind of heavy alkyl benzene as claimed in claim 1 is characterized in that described alkali is mineral alkali or organic bases.
4, the SO 3 gas jetting process for sulfonation of a kind of heavy alkyl benzene as claimed in claim 3 is characterized in that mineral alkali is sodium hydroxide, potassium hydroxide, ammonium hydroxide, magnesium hydroxide or calcium hydroxide.
5, the SO 3 gas jetting process for sulfonation of a kind of heavy alkyl benzene as claimed in claim 3 is characterized in that organic bases is monoethanolamine, diethanolamine, trolamine or tetraalkylammonium hydroxide.
6, the SO 3 gas jetting process for sulfonation of a kind of heavy alkyl benzene as claimed in claim 1 is characterized in that the aerial concentration of volume percent of described sulphur trioxide is 6～15%.
7, device as the SO 3 gas jetting process for sulfonation of each described a kind of heavy alkyl benzene of claim 1-6 is by nozzle, reactor kettle (7) is formed, it is characterized in that nozzle is by gas jet (3), liquid distribution chamber (4), atomizing mouth (5), heavy alkyl benzene inlet (1) and mixed gas inlet (2) are formed, gas jet (3) communicates with mixed gas inlet (2) and is fixed in top, liquid distribution chamber (4), heavy alkyl benzene inlet (1) is positioned at the lateral bottom of liquid distributor (4), atomizing mouth (5) is fixed in the liquid distribution chamber (4), gas jet (3) bottom enters in the atomizing mouth (5), atomizing mouth (5) top is an opening, the position of atomizing mouth (5) top in liquid distribution chamber (4) is higher than heavy alkyl benzene inlet (1) position in liquid distribution chamber (4), nozzle is fixed in reactor kettle (7) top, atomizing mouth (5) bottom enters in the reactor kettle (7), and there is product outlet (8) reactor kettle (7) lower end.
8, the device of the SO 3 gas jetting process for sulfonation of a kind of heavy alkyl benzene as claimed in claim 7, it is characterized in that described nozzle on reactor kettle (7) top with 2～60 uniform distribution.
9, the device of the SO 3 gas jetting process for sulfonation of a kind of heavy alkyl benzene as claimed in claim 7 is characterized in that described reactor kettle (7) internal fixing has guide shell (6), and atomizing mouth (5) bottom enters in the guide shell (6).
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| CNB2006101021547A CN100427464C (en) | 2006-11-10 | 2006-11-10 | Sulfur trioxide gas jet sulfonation process and device for bisalkyl benzene |
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| CN100427464C CN100427464C (en) | 2008-10-22 |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101811993A (en) * | 2010-05-05 | 2010-08-25 | 中国日用化学工业研究院 | Process for preparing fatty acid ester sulfonate |
| CN102513210A (en) * | 2011-12-16 | 2012-06-27 | 江苏科行环境工程技术有限公司 | Sulfur trioxide Spraying device |
| CN101423482B (en) * | 2008-11-27 | 2012-07-25 | 中国日用化学工业研究院 | Integrated method of sulphonation and neutralization reaction |
| CN103861544A (en) * | 2012-12-17 | 2014-06-18 | 中国石油化工股份有限公司 | Impinging stream reactor and application thereof |
| CN110526840A (en) * | 2019-09-19 | 2019-12-03 | 南雄市汉科化工科技有限公司 | Synthesize the preparation process and reaction unit of dodecyl Biphenyl Ether disulfonic acid sodium salt |
| CN110526840B (en) * | 2019-09-19 | 2024-06-04 | 南雄市汉科化工科技有限公司 | Preparation process and reaction device for synthesizing sodium dodecyl diphenyl ether disulfonate |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1120038C (en) * | 1999-04-30 | 2003-09-03 | 大庆石油管理局 | Alkyl benzene sulfonate surfactant, its preparation method and application in tertiary oil recovery |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101423482B (en) * | 2008-11-27 | 2012-07-25 | 中国日用化学工业研究院 | Integrated method of sulphonation and neutralization reaction |
| CN101811993A (en) * | 2010-05-05 | 2010-08-25 | 中国日用化学工业研究院 | Process for preparing fatty acid ester sulfonate |
| CN102513210A (en) * | 2011-12-16 | 2012-06-27 | 江苏科行环境工程技术有限公司 | Sulfur trioxide Spraying device |
| CN103861544A (en) * | 2012-12-17 | 2014-06-18 | 中国石油化工股份有限公司 | Impinging stream reactor and application thereof |
| CN103861544B (en) * | 2012-12-17 | 2016-07-27 | 中国石油化工股份有限公司 | A kind of impact flow reactor and application thereof |
| CN110526840A (en) * | 2019-09-19 | 2019-12-03 | 南雄市汉科化工科技有限公司 | Synthesize the preparation process and reaction unit of dodecyl Biphenyl Ether disulfonic acid sodium salt |
| CN110526840B (en) * | 2019-09-19 | 2024-06-04 | 南雄市汉科化工科技有限公司 | Preparation process and reaction device for synthesizing sodium dodecyl diphenyl ether disulfonate |
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Effective date of registration: 20190319 Address after: 312369 No. 19 Wei three road, Hangzhou Bay Economic and Technological Development Zone, Shangyu District, Shaoxing, Zhejiang Patentee after: Zhongguang chemical Shaoxing Co., Ltd. Address before: No. 34, Wen Yuan Lane, Taiyuan, Shanxi Province Patentee before: Chinese Daily Use Chemical Industry Research Inst. |