CN103012220A - Method for preparing powdery Alpha-olefin sulfonate and preparation device - Google Patents
Method for preparing powdery Alpha-olefin sulfonate and preparation device Download PDFInfo
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- CN103012220A CN103012220A CN2012105502467A CN201210550246A CN103012220A CN 103012220 A CN103012220 A CN 103012220A CN 2012105502467 A CN2012105502467 A CN 2012105502467A CN 201210550246 A CN201210550246 A CN 201210550246A CN 103012220 A CN103012220 A CN 103012220A
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- 239000004711 α-olefin Substances 0.000 title claims abstract description 22
- 238000002360 preparation method Methods 0.000 title claims abstract description 16
- 238000000034 method Methods 0.000 title abstract description 12
- BDHFUVZGWQCTTF-UHFFFAOYSA-M sulfonate Chemical compound [O-]S(=O)=O BDHFUVZGWQCTTF-UHFFFAOYSA-M 0.000 title abstract description 5
- 238000001694 spray drying Methods 0.000 claims abstract description 72
- 239000000463 material Substances 0.000 claims abstract description 68
- 238000010438 heat treatment Methods 0.000 claims abstract description 33
- 238000005406 washing Methods 0.000 claims abstract description 13
- 238000000926 separation method Methods 0.000 claims abstract description 12
- 239000000203 mixture Substances 0.000 claims description 124
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 90
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 30
- 239000007788 liquid Substances 0.000 claims description 29
- 238000001035 drying Methods 0.000 claims description 27
- 239000000843 powder Substances 0.000 claims description 23
- 238000005507 spraying Methods 0.000 claims description 23
- 150000002148 esters Chemical class 0.000 claims description 19
- 239000002253 acid Substances 0.000 claims description 18
- 239000000428 dust Substances 0.000 claims description 18
- 238000004140 cleaning Methods 0.000 claims description 14
- 230000008676 import Effects 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 7
- 239000010865 sewage Substances 0.000 claims description 5
- 239000007921 spray Substances 0.000 claims description 5
- 238000004891 communication Methods 0.000 claims description 4
- 230000002411 adverse Effects 0.000 claims description 3
- 238000003860 storage Methods 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 10
- 238000003756 stirring Methods 0.000 abstract description 8
- 238000002156 mixing Methods 0.000 abstract description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 abstract 1
- 238000007605 air drying Methods 0.000 abstract 1
- 238000000889 atomisation Methods 0.000 abstract 1
- 238000010410 dusting Methods 0.000 abstract 1
- 235000011149 sulphuric acid Nutrition 0.000 abstract 1
- 239000001117 sulphuric acid Substances 0.000 abstract 1
- 239000000047 product Substances 0.000 description 19
- 230000004907 flux Effects 0.000 description 12
- 150000008053 sultones Chemical class 0.000 description 10
- 230000000737 periodic effect Effects 0.000 description 7
- 239000007787 solid Substances 0.000 description 7
- 238000006277 sulfonation reaction Methods 0.000 description 7
- 230000032683 aging Effects 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 238000006460 hydrolysis reaction Methods 0.000 description 6
- 238000006386 neutralization reaction Methods 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 239000003599 detergent Substances 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 238000012545 processing Methods 0.000 description 5
- 230000007062 hydrolysis Effects 0.000 description 3
- 230000003301 hydrolyzing effect Effects 0.000 description 3
- 239000000344 soap Substances 0.000 description 3
- 239000003945 anionic surfactant Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 239000012263 liquid product Substances 0.000 description 2
- 230000007246 mechanism Effects 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 239000006072 paste Substances 0.000 description 2
- -1 sodium alkyl benzene Chemical class 0.000 description 2
- 230000035882 stress Effects 0.000 description 2
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 2
- 229920000742 Cotton Polymers 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 1
- 239000013543 active substance Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229940077388 benzenesulfonate Drugs 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000004851 dishwashing Methods 0.000 description 1
- 230000003670 easy-to-clean Effects 0.000 description 1
- 239000003995 emulsifying agent Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 238000005187 foaming Methods 0.000 description 1
- 239000004088 foaming agent Substances 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 210000004209 hair Anatomy 0.000 description 1
- 239000008233 hard water Substances 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000006210 lotion Substances 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 238000012946 outsourcing Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 235000019633 pungent taste Nutrition 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000002453 shampoo Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000004753 textile Substances 0.000 description 1
- 239000000606 toothpaste Substances 0.000 description 1
- 229940034610 toothpaste Drugs 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 239000000080 wetting agent Substances 0.000 description 1
- 210000002268 wool Anatomy 0.000 description 1
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Abstract
The invention relates to a method for preparing powdery Alpha-olefin sulfonate and a preparation device and aims to achieve the purposes that the energy consumption is low, the device is compact in structure, the investment can be saved, and the operation is stable. The technical scheme is as follows: the method for preparing the powdery Alpha-olefin sulfonate comprises the following steps: 1), stirring, mixing and heating; and introducing dry air; 2), performing atomization; 3), performing primary separation, so that a powdery material enters a power bin; and 4), performing secondary separation, so that the powdery material enters the power bin, the secondary mixed gas flow is evacuated through an induced draft fan; and the heated dry air comes from evacuated tail gas of an air drying system or a nearby sulphuric acid plant. The device for preparing the powdery AOS (Alpha-olefin sulfonate) comprises a feeding device, a spray drying tower, a cyclone separation device and a de-dusting device and is characterized in that a feeding port and a dry air inlet are arranged at the top end of the spray drying tower, a mixed gas flow outlet is arranged on one side of the spray drying tower, and a washing outlet is arranged at the bottom of the spray drying tower.
Description
Technical field
The present invention relates to a kind of preparation method and preparation facilities of tensio-active agent, specifically preparation method and the preparation facilities of powdery sulfonated α-olefin (hereinafter to be referred as AOS).
Technical background
Sulfonated α-olefin is a kind of anion surfactant of excellent property, has good water-soluble, whipability, wettability; There are good resistance to hard water, soil release characteristics good; Stable in acid-alkali medium, compatibleness is good; Have that toxicity is low, pungency is little and good biodegradability properties.Because the good performance of AOS, therefore in family with industrially all have a widely purposes.On personal-care supplies, can be used in the prescriptions such as Liquid soap, shampoo, toothpaste, body lotion, foam bath; On home washings, be applicable to dish washing detergent, heavy dirty laundry detergent, synthetic soap, liquid soap, wool, eider down clean-out system; Can be used in industry that letex polymerization emulsifying agent, oil three are adopted, the concrete density improving agent, raw cotton (or hair) washing, textile and paper wetting agent, farm chemical emulgent, foaming wall, fire-fighting are with foaming agent etc.
Domestic aspect anionic surfactant, the share of market of sodium alkyl benzene sulfonate (hereinafter to be referred as LAS) and polyoxyethylenated alcohol sodium sulfate (hereinafter to be referred as AES) is higher, LAS uses more in the heavy dirty powdered detergent of clothing usefulness, price is lower and more stable, Product Activity thing content 〉=96%, market sales volume is maximum.AES uses larger in the liquid product of personal care and home washings agent, Product Activity thing 70 ± 2%, and price is higher and fluctuation is larger, and market sales volume is taken second place.AOS can partly substitute LAS or AES in powdery and detergent product, price comparison is stable, Product Activity thing content 35 ± 1%, and market sales volume occupies the 3rd.AOS sells with the liquid product of low activity thing, packing and trucking costs are higher, this also is a high principal element of AOS product use cost, in the powdered detergent application facet, AOS is owing to needing larger energy consumption boil off a large amount of moisture ability powderings, so that the cost of manufacture of washing composition improves greatly.
AOS low activity the production of material is because the material state in its reaction mechanism and the process determines; After the reaction of alpha-olefin and sulphur trioxide except generating the hydroxyl sulfoacid that can directly be neutralized into alkenyl sulphonate, some sultone, and sultone must at high temperature be hydrolyzed and just can carry out neutralization reaction afterwards.The processing condition that hydrolysis reaction adopts in the industrial production are: 160～170 ℃ of temperature of reaction, pressure 0.5MPa, continuous hydrolysis 30 minutes.Because AOS concentration is gel state easily at 40% material when above, and concentration is higher, the viscosity of gel more greatly, increased the conveying difficulty, therefore, the concentration of AOS is controlled at about 35% in actual production process.
AOS about 70% is paste when just producing, and forms gradually the solid gel shape under the normal temperature, causes packing to use inconvenience, and suitability for industrialized production is not yet arranged so far.Aspect the dry powder process of the AOS of lower concentration, the drying process of external AOS product is comparatively advanced is the turbulent flow drying process of Chemithon company of the U.S. and the vacuum knifing drying process of gondola Ballestra company, but these two kinds of methods all exist investment large, the shortcomings such as energy consumption is large are difficult to apply.In addition, the patent gazette of " drying process of a kind of spray-drying tower and α olefin sulfonate thereof " by name of Zhongqingwuchan Zhejiang Chemical Co., Ltd.'s application discloses a kind of spray-drying tower, employing arranges along wall wind, unit for cleaning wind and tower wall refrigerating unit, make spray-drying tower in drying process, be difficult for producing wall sticking phenomenon, easy to clean.With this device fabrication AOS product, drying efficiency obtains certain raising, but because drying is since 30～40% AOS, so energy consumption is larger.
Summary of the invention
The objective of the invention is to overcome the deficiency that the above-mentioned background technology exists, a kind of preparation method and preparation facilities of improved powdery sulfonated α-olefin are provided, and this device and method should have that energy consumption is low, compact equipment, reduced investment, by product sultone are few, system is easy to control, stable characteristics.
Technical scheme provided by the invention is:
A kind of preparation method of powdery sulfonated α-olefin may further comprise the steps:
1), mixes by volume pump input mix and blend tank respectively from the AOS acid esters (sulfonated products of alpha-olefin) of sulfonating gas liquid/gas separator with from the liquid caustic soda of storage tank, and the material in the mix and blend tank is heated; Pass into simultaneously the dry air of heating at spray-drying tower, the temperature of dry air is 150～400 ℃, and flow changes according to the variation for the treatment of capacity and drying air temperature;
2), after the material in the mix and blend tank stops through 1～30min, open the mix and blend bottom valve, material sprays into spray-drying tower and atomizes;
3), when material sprays into spray-drying tower, mixed airflow enters primary cyclone by mixed airflow outlet, mixed airflow is through after the flash liberation, isolated pulverulent material enters the powder storehouse by pipeline;
4), the one-level mixed airflow outlet by primary cyclone enters secondary cyclone and carries out secondary separation through the mixed airflow of flash liberation; Isolated pulverulent material enters the powder storehouse by pipeline, and isolated mixed gas flows to into sack cleaner, through emptying by induced draft fan after the dedusting;
The dry air of described heating is from the emptying tail gas of air dryer systems or near vitriol works.
Described liquid caustic soda is the sodium hydroxide solution (massfraction) of 25%～50% concentration.
The mol ratio of described AOS acid esters and sodium hydroxide is 1:1.1～1.5.
The atomizer nozzle form of described spray-drying tower is air-flowing type or pressure type or centrifugal.
Dry air after the described heating with the atomizing after material in spray-drying tower, contact in the mode of following current or adverse current.
The temperature of the heating material in the described mix and blend tank is 150～200 ℃; The type of heating of described mix and blend tank is steam heating or electrically heated.
A kind of device for preparing powdery AOS comprises the feeding unit, spray-drying tower, cyclone separator and the cleaning apparatus that sequentially are communicated with by pipeline; The top that it is characterized in that described spray-drying tower is provided with opening for feed and the dry air import that is communicated with feeding unit, the side of spray-drying tower is provided with the mixed airflow outlet of connecting cyclonic separator, and the bottom of spray-drying tower is provided with the washing outlet of Sewage treatment systems;
Described feeding unit comprises mix and blend tank and the AOS acid esters pipeline and the liquid caustic soda pipeline that are communicated with the mix and blend tank respectively by two pipelines that are equipped with pneumatic adjusting valve and volume pump;
Described cyclone separator comprises primary cyclone and secondary cyclone, the primary cyclone opening for feed is connected to the mixed airflow outlet of spray-drying tower by pipeline, the one-level mixed airflow on primary cyclone top exports the opening for feed that is connected to secondary cyclone by pipeline, and the top of secondary cyclone is provided with the mixed gas spout; The bottom of described primary cyclone, secondary cyclone is equipped with the product outlet that is connected to the powder storehouse by pipeline.
The stress reaction tank that described mix and blend tank is jacketed, the bottom is provided with bottom valve, and the bottom valve outlet directly is communicated with the import on spray-drying tower top by pipeline.
Described spray-drying tower comprises tubular main unit for dryer, spraying gun, mixed airflow outlet and the washing outlet of hollow, and described spraying gun is connected to the main shaft top of spray-drying tower.
Described cleaning apparatus comprises by the sack cleaner of pipeline communication and induced draft fan; The import of described sack cleaner is connected to the mixed airflow outlet of secondary cyclone, and the outlet of described sack cleaner is communicated with induced draft fan and flows by the mixed gas after the dedusting with emptying; The bottom of sack cleaner is provided with the dust collection mouth.
Described spray-drying tower is air-stream spraying drying tower or pressure spray drying tower or centrifugal spray drying tower.
The present invention compared with prior art has following outstanding advantages and positively effect:
1) greatly reduce dried material initial moisture content (from 65% be reduced to 30% and below), decrease dry energy consumption (can save the energy consumption for drying more than 50%).
2) because the raising of material content (concentration) will reduce much when neutralization, hydrolysis, drying plant volume and the processing power of output are than lower concentration (35%) equally, investment cost reduces (can save 50% above facility investment expense) greatly.
3) because the reducing of equipment volume and processing power, equipment takes up an area the space and also greatly reduces, and running cost also greatly reduces (the 50% above equipment of can saving takes up an area the space, the equipment running cost of saving more than 50%).
4) because the reaction heat that neutralization produces is converted to the heat of partial hydrolysis reaction needed, also reduced energy consumption.
5) less investment of the present invention, not high to equipment requirements, all appts that disposes, equipment and device are the matured product of outsourcing, install simple and easyly, and for ease of maintenaince, simultaneity factor is stable, is easy to control.
Description of drawings
Fig. 1 is AOS spray drying unit system construction drawing of the present invention.
Wherein: 1 is the AOS acid esters; 2 is liquid caustic soda; 3 is the first pneumatic adjusting valve; 4 is the second pneumatic adjusting valve; 5 is the first volume pump; 6 is the second volume pump; 7 is the mix and blend tank; 8 dry airs for heating; 9 is spray-drying tower; 10 is Sewage treatment systems; 11 is primary cyclone; 12 powder storehouses; 13 is secondary cyclone; 14 is sack cleaner; 15 is the dust collection mouth; 16 is induced draft fan; 17 is the tail gas evacuation port.
Embodiment
Below in conjunction with accompanying drawing invention is described further.
Thinking of the present invention is the initial concentration that farthest improves dried material, reduces the energy consumption of powdery AOS product; It is even at first to make AOS acid esters after the sulfonation and liquid caustic soda carry out short mix in the mix and blend tank, when mixing mixing, finish hydrolytic process, the neutralization reaction liberated heat just in time can be used as the heat energy of hydrolytic process, has so also reduced the energy expenditure of hydrolytic process; Because temperature is high, the time is short, and material is still paste, can enter smoothly spray-drying tower; Material is atomized into the less droplet of particle diameter in spray-drying tower, contact with pre-heated dry air again, mixing of materials sinks at the bottom of the drying tower again to droplet to spraying gun during, also can further be hydrolyzed and neutralization reaction, finish simultaneously dry technological process.Because initial concentration is more than 70%, neutralizing hydrolysis processing unit volume and processing power require and can greatly reduce, and cost of investment greatly reduces; And the AOS acid esters is with after liquid caustic soda mixes, and the heat that neutralization produces both can be used as the thermal source of hydrolysis reaction, had improved again the temperature that material enters drying tower, and dry required energy consumption also just greatly reduces.
Referring to Fig. 1, the present invention includes feeding unit, spray-drying tower 9, cyclone separator and cleaning apparatus by pipeline communication, described feeding unit is connected with spray-drying tower respectively with cyclonic separator, the bottom of described spray-drying tower is provided with washing outlet, and described washing outlet is connected to Sewage treatment systems 10; The side of spray-drying tower is provided with the mixed airflow outlet, and the mixed airflow outlet is communicated to cyclonic separator 11, carries the import on the pipeline communication spray-drying tower top of dry air 8.
Mix and blend tank 7 and by two pipelines that are communicated with and are equipped with respectively pneumatic adjusting valve and volume pump with the mix and blend tank; AOS acid esters 1 from the sulfonating gas liquid/gas separator enters mix and blend tank 7 by the first pneumatic adjusting valve 3, the first volume pump 5 successively; Liquid caustic soda 2 from storage tank enters the mix and blend tank by the second pneumatic adjusting valve 4, the second volume pump 6 successively; Described mix and blend tank 7 is the stress reaction tank of jacketed, and the bottom is provided with bottom valve, and the bottom valve outlet is connected directly to spray-drying tower 9 by pipeline.
Spray-drying tower comprises tubular main unit for dryer, spraying gun, mixed airflow outlet and the washing outlet of hollow; Described spraying gun is connected to the main shaft top of spray-drying tower, and described mixed airflow outlet is connected to cyclonic separator.The washing outlet of described spraying drying tower bottom is connected to Sewage treatment systems 10; Described spray-drying tower side is provided with the mixed airflow outlet, and this mixed airflow outlet is connected to cyclonic separator by pipeline.
Cyclone separator comprises primary cyclone 11 and secondary cyclone 13.Described primary cyclone opening for feed is communicated with the mixed airflow outlet of spray-drying tower; The top of primary cyclone is provided with the outlet of one-level mixed airflow, and the opening for feed of secondary cyclone is connected to the outlet of one-level mixed airflow, and the top of secondary cyclone is provided with the mixed gas spout.The lower part outlet of primary cyclone, secondary cyclone is equipped with the product outlet 12 that is connected to the powder storehouse by pipeline.
Cleaning apparatus comprises sack cleaner 14 and induced draft fan 16.The import of described sack cleaner is connected to the mixed airflow outlet of secondary cyclone 13, and the outlet of sack cleaner is connected to induced draft fan 16, and the mixed gas stream that secondary cyclone produces is by emptying by evacuation port 17 after the sack cleaner dedusting.The sack cleaner bottom is provided with dust collection mouth 15.
Adopt said apparatus to prepare the method for powdery AOS, may further comprise the steps:
1) starts spray-drying tower 9, after passing into the dry air 8 of heating, open the stirring mechanism of mix and blend tank 7, AOS acid esters 1 and liquid caustic soda 2 are squeezed into the mix and blend tank through pneumatic adjusting valve, volume pump respectively, begin simultaneously the material in the mix and blend tank is heated;
2) mixed material is opened the mix and blend bottom valve after stopping after a while, and material enters spray-drying tower 9 and atomizes;
3) when material sprays into, mixed airflow enters primary cyclone 11 by the mixed airflow outlet, and mixed airflow is through after the flash liberation, and isolated pulverulent material enters the powder storehouse by pipeline;
4) the one-level mixed airflow outlet by primary cyclone enters secondary cyclone 13 and carries out secondary separation through the mixed airflow of flash liberation, and isolated pulverulent material enters the powder storehouse by pipeline; The mixed gas of second-stage separator flows to into sack cleaner 14, and through emptying by induced draft fan 16 after the dedusting, 15 in the dust collection mouth of bag-type dust bottom needs periodic cleaning.
The dry air of described heating is from the emptying tail gas of air dryer systems or near vitriol works, and the temperature of dry air is 150～400 ℃, and flow changes for the size according to treatment capacity; As recommendation, the temperature of dry air is 200～350 ℃.
The concentration of described liquid caustic soda is 25%～50% sodium hydroxide solution (massfraction).
The mol ratio of described AOS acid esters and sodium hydroxide is 1:1.1～1.5.
Described spray-drying tower is air-stream spraying drying tower or pressure spray drying tower or centrifugal spray drying tower (form of nozzle of spraying gun wherein is air-flowing type or pressure type or centrifugal).
Dry air after the described heating with the atomizing after material in spray-drying tower, contact in the mode of following current or adverse current.
The Heating temperature of material is 150～200 ℃ in the described mix and blend tank; As recommendation, Heating temperature is 160～190 ℃.
The type of heating of material is steam heating or electrically heated in the described stirred pot.
The residence time of material is 1～30min in the described stirred pot; As recommendation, the residence time is 20～30min.
Mix and blend tank of the present invention, spray-drying tower, cyclone separator, sack cleaner, induced draft fan, pneumatic adjusting valve, volume pump and miscellaneous equipment are all selected conventional equipment.
The centrifugal spray drying tower that powdery AOS produces in the LPG-100 model carries out; Open centrifugal spray drying tower, pass into the dry air of heating, 300 ℃ of the inlet temperatures of dry air, flow is 1000m
3/ min, open the stirring of mix and blend tank, the aging AOS acid esters later of sulfonation is 200kg/h by the pneumatic adjusting valve adjust flux, squeeze into the mix and blend tank by volume pump, simultaneously liquid caustic soda is 100kg/h by the pneumatic adjusting valve adjust flux, squeezes into the mix and blend tank by volume pump, passes into again steam the material of mix and blend tank is heated, Heating temperature is 190 ℃, and the concentration of liquid caustic soda is 32%; Behind the mixed material stop 30min, open the mix and blend bottom valve, material enters centrifugal spray drying tower and carries out centrifugal spray drying; Mixed airflow enters primary cyclone by the mixed airflow outlet, and mixed airflow is through after the flash liberation, and the isolated pulverulent material of institute enters the powder storehouse through outlet; One-level mixed airflow outlet by primary cyclone enters secondary cyclone and carries out secondary separation through the mixed airflow of flash liberation, and the isolated pulverulent material of institute enters the powder storehouse through outlet; The mixed gas of second-stage separator flows to into sack cleaner, through emptying by induced draft fan after the dedusting, and the dust collection mouth periodic cleaning of bag-type dust bottom.
Gained AOS product solid content is 98.4%, and actives is 93.2%, and total sultone content is 4mg/kg.
The centrifugal spray drying tower that powdery AOS produces in the LPG-100 model carries out; Open centrifugal spray drying tower, pass into the dry air of heating, 350 ℃ of the inlet temperatures of dry air, flow is 800m
3/ min, open the stirring of mix and blend tank, the aging AOS acid esters later of sulfonation is 170kg/h by the pneumatic adjusting valve adjust flux, squeeze into the mix and blend tank by volume pump, liquid caustic soda is 120kg/h by the pneumatic adjusting valve adjust flux simultaneously, squeeze into the mix and blend tank by volume pump, passing into simultaneously steam heats the material of mix and blend tank, Heating temperature is 170 ℃, the concentration of liquid caustic soda is 25%, behind the mixed material stop 20min, open the mix and blend bottom valve, material enters centrifugal spray drying tower and carries out spraying drying; Mixed airflow enters primary cyclone by the mixed airflow outlet, and mixed airflow is through after the flash liberation, and the isolated pulverulent material of institute enters the powder storehouse through outlet; One-level mixed airflow outlet by primary cyclone enters secondary cyclone and carries out secondary separation through the mixed airflow of flash liberation, and the isolated pulverulent material of institute enters the powder storehouse through outlet; The mixed gas of second-stage separator flows to into sack cleaner, through emptying by induced draft fan after the dedusting, and the dust collection mouth periodic cleaning of bag-type dust bottom.
Gained AOS product solid content is 98.8%, and actives is 93.6%, and total sultone content is 8mg/kg.
The pressure spray drying tower that powdery AOS produces in the YPG-100 model carries out, and the opening pressure spray-drying tower passes into the dry air of heating, 220 ℃ of the inlet temperatures of dry air, and flow is 700m
3/ min, open the stirring of mix and blend tank, the aging AOS acid esters later of sulfonation is 200kg/h by the pneumatic adjusting valve adjust flux, squeeze into the mix and blend tank by volume pump, liquid caustic soda is 80kg/h by the pneumatic adjusting valve adjust flux simultaneously, squeeze into the mix and blend tank by volume pump, passing into simultaneously steam heats the material of mix and blend tank, Heating temperature is 180 ℃, the concentration of liquid caustic soda is 42%, behind the mixed material stop 25min, open the mix and blend bottom valve, material enters pressure spray drying tower and carries out spraying drying; Mixed airflow enters primary cyclone by the mixed airflow outlet, mixed airflow is through after the flash liberation, the isolated pulverulent material of institute enters the powder storehouse through outlet, one-level mixed airflow outlet by primary cyclone enters secondary cyclone and carries out secondary separation through the mixed airflow of flash liberation, and the isolated pulverulent material of institute enters the powder storehouse through outlet; The mixed gas of second-stage separator flows to into sack cleaner, through passing through induced draft fan emptying (17), the dust collection mouth periodic cleaning of bag-type dust after the dedusting.
Gained AOS product solid content is 96.2%, and actives is 92.2%, and total sultone content is 6mg/kg.
Embodiment 4
The pressure spray drying tower that powdery AOS produces in the YPG-100 model carries out, and the opening pressure spray-drying tower passes into the dry air of heating, 250 ℃ of the inlet temperatures of dry air, and flow is 400m
3/ min, open the stirring of mix and blend tank, the aging AOS acid esters later of sulfonation is 160kg/h by the pneumatic adjusting valve adjust flux, squeeze into the mix and blend tank by volume pump, liquid caustic soda is 80kg/h by the pneumatic adjusting valve adjust flux simultaneously, squeeze into the mix and blend tank by volume pump, passing into simultaneously steam heats the material of mix and blend tank, Heating temperature is 160 ℃, the concentration of liquid caustic soda is 32%, behind the mixed material stop 20min, open the mix and blend bottom valve, material enters pressure spray drying tower and carries out spraying drying; Mixed airflow enters primary cyclone by the mixed airflow outlet, mixed airflow is through after the flash liberation, the isolated pulverulent material of institute enters the powder storehouse through outlet, one-level mixed airflow outlet by primary cyclone enters secondary cyclone and carries out secondary separation through the mixed airflow of flash liberation, and the isolated pulverulent material of institute enters the powder storehouse through outlet; The mixed gas of second-stage separator flows to into sack cleaner, through emptying by induced draft fan after the dedusting, and the dust collection mouth periodic cleaning of bag-type dust bottom.
Gained AOS product solid content is 96.8%, and actives is 92.6%, and total sultone content is 10mg/kg.
Embodiment 5
The air-stream spraying drying tower that powdery AOS produces in the GPQ-100 model carries out, and opens the air-stream spraying drying tower, passes into the dry air of heating, 200 ℃ of the inlet temperatures of dry air, and flow is 600m
3/ min, open the stirring of mix and blend tank, the aging AOS acid esters later of sulfonation is 200kg/h by the pneumatic adjusting valve adjust flux, squeeze into the mix and blend tank by volume pump, liquid caustic soda is 70kg/h by the pneumatic adjusting valve adjust flux simultaneously, squeeze into the mix and blend tank by volume pump, passing into simultaneously steam heats the material of mix and blend tank, Heating temperature is 180 ℃, the concentration of liquid caustic soda is 48%, behind the mixed material stop 28min, open the mix and blend bottom valve, material enters the air-stream spraying drying tower and carries out spraying drying; Mixed airflow enters primary cyclone by the mixed airflow outlet, mixed airflow is through after the flash liberation, the isolated pulverulent material of institute enters the powder storehouse through outlet, one-level mixed airflow outlet by primary cyclone enters secondary cyclone and carries out secondary separation through the mixed airflow of flash liberation, and the isolated pulverulent material of institute enters the powder storehouse through outlet; The mixed gas of second-stage separator flows to into sack cleaner, through emptying by induced draft fan after the dedusting, and the dust collection mouth periodic cleaning of bag-type dust bottom.
Gained AOS product solid content is 95.7%, and actives is 92.0%, and total sultone content is 5mg/kg.
Embodiment 6
The air-stream spraying drying tower that powdery AOS produces in the GPQ-100 model carries out, and opens the air-stream spraying drying tower, passes into the dry air of heating, 280 ℃ of the inlet temperatures of dry air, and flow is 500m
3/ min, open the stirring of mix and blend tank, the aging AOS acid esters later of sulfonation is 160kg/h by the pneumatic adjusting valve adjust flux, squeeze into the mix and blend tank by volume pump, liquid caustic soda is 85kg/h by the pneumatic adjusting valve adjust flux simultaneously, squeeze into the mix and blend tank by volume pump, passing into simultaneously steam heats the material of mix and blend tank, Heating temperature is 170 ℃, the concentration of liquid caustic soda is 32%, behind the mixed material stop 20min, open the mix and blend bottom valve, material enters the air-stream spraying drying tower and carries out spraying drying; Mixed airflow enters primary cyclone by the mixed airflow outlet, and mixed airflow is through after the flash liberation, and the isolated pulverulent material of institute enters the powder storehouse through outlet; One-level mixed airflow outlet by primary cyclone enters secondary cyclone and carries out secondary separation through the mixed airflow of flash liberation, and the isolated pulverulent material of institute enters the powder storehouse through outlet; The mixed gas of second-stage separator flows to into sack cleaner, passes through induced draft fan through after the dedusting) emptying, the dust collection mouth periodic cleaning of bag-type dust bottom.
Gained AOS product solid content is 97.4%, and actives is 92.8%, and total sultone content is 7mg/kg.
Can be found out that by above embodiment the present invention is when guaranteeing powdery AOS quality product, the remaining amount of sultone also has remarkable reduction (being reduced to 4-10mg/kg).
Claims (10)
1. the preparation method of a powdery sulfonated α-olefin may further comprise the steps:
1), mixes by volume pump input mix and blend tank respectively from the AOS acid esters of sulfonating gas liquid/gas separator with from the liquid caustic soda of storage tank, and the material in the mix and blend tank is heated; Pass into simultaneously the dry air of heating at spray-drying tower, the temperature of dry air is 150～400 ℃;
2), after the material in the mix and blend tank stops through 1～30min, open the mix and blend bottom valve, material sprays into spray-drying tower and atomizes;
3), when material sprays into spray-drying tower, mixed airflow enters primary cyclone by mixed airflow outlet, mixed airflow is through after the flash liberation, isolated pulverulent material enters the powder storehouse by pipeline;
4), the one-level mixed airflow outlet by primary cyclone enters secondary cyclone and carries out secondary separation through the mixed airflow of flash liberation; Isolated pulverulent material enters the powder storehouse by pipeline, and isolated mixed gas flows to into sack cleaner, through emptying by induced draft fan after the dedusting;
The dry air of described heating is from the emptying tail gas of air dryer systems or near vitriol works.
2. the preparation method of a kind of powdery sulfonated α-olefin according to claim 1 is characterized in that described liquid caustic soda is the sodium hydroxide solution of concentration 25%～50%.
3. the preparation method of a kind of powdery sulfonated α-olefin according to claim 2, the mol ratio that it is characterized in that described AOS acid esters and sodium hydroxide is 1:1.1～1.5.
4. the preparation method of a kind of powdery sulfonated α-olefin according to claim 3 is characterized in that the material after dry air and the atomizing after the described heating contacts in the mode of following current or adverse current in spray-drying tower.
5. the preparation method of a kind of powdery sulfonated α-olefin according to claim 4 is characterized in that the temperature of heating material in the described mix and blend tank is 150～200 ℃; The type of heating of mix and blend tank is steam heating or electrically heated.
6. a device for preparing the powdery sulfonated α-olefin comprises the feeding unit, spray-drying tower (9), cyclone separator and the cleaning apparatus that sequentially are communicated with by pipeline; The top that it is characterized in that described spray-drying tower is provided with opening for feed and the dry air import that is communicated with feeding unit, the side of spray-drying tower is provided with the mixed airflow outlet of connecting cyclonic separator, and the bottom of spray-drying tower is provided with the washing outlet that is communicated with Sewage treatment systems (10);
Described feeding unit comprises mix and blend tank (7) and AOS acid esters (1) pipeline and liquid caustic soda (2) pipeline that are communicated with the mix and blend tank respectively by two pipelines that are equipped with pneumatic adjusting valve and volume pump;
Described cyclone separator comprises primary cyclone (11) and secondary cyclone (13), the primary cyclone opening for feed is connected to the mixed airflow outlet of spray-drying tower by pipeline, the one-level mixed airflow on primary cyclone top exports the opening for feed that is connected to secondary cyclone by pipeline, and the top of secondary cyclone is provided with the mixed gas spout; The bottom of described primary cyclone, secondary cyclone is equipped with the product outlet that is connected to powder storehouse (12) by pipeline.
7. a kind of device for preparing the powdery sulfonated α-olefin according to claim 6 is characterized in that the stress reaction tank that described mix and blend tank is jacketed, and the bottom is provided with bottom valve, and the bottom valve outlet directly is communicated with the import on spray-drying tower top by pipeline.
8. a kind of device for preparing the powdery sulfonated α-olefin according to claim 7 is characterized in that described cleaning apparatus comprises sack cleaner (15) and the induced draft fan (17) by pipeline communication; The import of described sack cleaner is connected to the mixed airflow outlet of secondary cyclone, and the outlet of described sack cleaner is communicated with induced draft fan and flows by the mixed gas after the dedusting with emptying; The bottom of sack cleaner is provided with dust collection mouth (16).
9. a kind of device for preparing the powdery sulfonated α-olefin according to claim 8, it is characterized in that described spray-drying tower comprises tubular main unit for dryer, spraying gun, mixed airflow outlet and the washing outlet of hollow, described spraying gun is connected to the main shaft top of spray-drying tower.
10. a kind of device for preparing the powdery sulfonated α-olefin according to claim 9 is characterized in that described spray-drying tower is air-stream spraying drying tower or pressure spray drying tower or centrifugal spray drying tower.
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| CN103480163A (en) * | 2013-09-22 | 2014-01-01 | 浙江赞宇科技股份有限公司 | Device for removing dioxane from ethoxylation alkyl sulfate through centrifugal spray |
| CN104003912A (en) * | 2014-05-30 | 2014-08-27 | 湖南丽臣奥威实业有限公司 | Preparation method for shower gel type alpha-alkenyl sulphonate and application thereof |
| CN104447422A (en) * | 2014-12-05 | 2015-03-25 | 浙江赞宇科技股份有限公司 | Production technology and device for comprehensive recovery and utilization of alpha-alkenyl electrostatic acid |
| CN104451714A (en) * | 2014-12-05 | 2015-03-25 | 浙江赞宇科技股份有限公司 | Production process and production device for preparing industrial additives from electrostatic acid and application thereof |
| CN105254540A (en) * | 2015-10-30 | 2016-01-20 | 嘉兴赞宇科技有限公司 | Preparation method and device for powdery fatty acid methyl ester sodium sulfonate |
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| CN107954905A (en) * | 2017-12-01 | 2018-04-24 | 北京恒聚化工集团有限责任公司 | A kind of preparation method of alpha-alkene sulfonate |
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| CN104003912A (en) * | 2014-05-30 | 2014-08-27 | 湖南丽臣奥威实业有限公司 | Preparation method for shower gel type alpha-alkenyl sulphonate and application thereof |
| CN104003912B (en) * | 2014-05-30 | 2015-11-18 | 湖南丽臣奥威实业有限公司 | A kind of preparation method of body wash type α olefin sulfonate and application thereof |
| CN104447422B (en) * | 2014-12-05 | 2016-09-07 | 浙江赞宇科技股份有限公司 | The production technology of a kind of α-thiazolinyl electrostatic acid comprehensive reutilization and device |
| CN104447422A (en) * | 2014-12-05 | 2015-03-25 | 浙江赞宇科技股份有限公司 | Production technology and device for comprehensive recovery and utilization of alpha-alkenyl electrostatic acid |
| CN104451714A (en) * | 2014-12-05 | 2015-03-25 | 浙江赞宇科技股份有限公司 | Production process and production device for preparing industrial additives from electrostatic acid and application thereof |
| CN104451714B (en) * | 2014-12-05 | 2017-02-22 | 浙江赞宇科技股份有限公司 | Production process and production device for preparing industrial additives from electrostatic acid and application thereof |
| CN105254540B (en) * | 2015-10-30 | 2017-03-22 | 嘉兴赞宇科技有限公司 | Preparation method and device for powdery fatty acid methyl ester sodium sulfonate |
| CN105254540A (en) * | 2015-10-30 | 2016-01-20 | 嘉兴赞宇科技有限公司 | Preparation method and device for powdery fatty acid methyl ester sodium sulfonate |
| CN105460993A (en) * | 2016-01-13 | 2016-04-06 | 大连科林能源工程技术开发有限公司 | Dry environment-friendly treating and solid salt recycling system for high-concentration salt-containing waste water |
| CN107954905A (en) * | 2017-12-01 | 2018-04-24 | 北京恒聚化工集团有限责任公司 | A kind of preparation method of alpha-alkene sulfonate |
| CN107954905B (en) * | 2017-12-01 | 2020-06-09 | 北京恒聚化工集团有限责任公司 | Preparation method of α -olefin sulfonate |
| CN109019639A (en) * | 2018-06-07 | 2018-12-18 | 亚泰电化有限公司 | The purifying plant of by-product sal glauberi in a kind of sodium peroxydisulfate production process |
| CN109019639B (en) * | 2018-06-07 | 2021-03-16 | 亚泰电化有限公司 | Purification device of by-product sodium sulfate decahydrate in sodium persulfate production process |
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