CN107522755A - A kind of method that light APG is prepared using loop reactor - Google Patents

A kind of method that light APG is prepared using loop reactor Download PDF

Info

Publication number
CN107522755A
CN107522755A CN201710835247.9A CN201710835247A CN107522755A CN 107522755 A CN107522755 A CN 107522755A CN 201710835247 A CN201710835247 A CN 201710835247A CN 107522755 A CN107522755 A CN 107522755A
Authority
CN
China
Prior art keywords
apg
loop reactor
product
reactor
bleaching
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
CN201710835247.9A
Other languages
Chinese (zh)
Inventor
毛锦生
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
WUXI GREEN APPLE ENGINEERING PROSPECTING DESIGN INSTITUTE
Original Assignee
WUXI GREEN APPLE ENGINEERING PROSPECTING DESIGN INSTITUTE
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by WUXI GREEN APPLE ENGINEERING PROSPECTING DESIGN INSTITUTE filed Critical WUXI GREEN APPLE ENGINEERING PROSPECTING DESIGN INSTITUTE
Priority to CN201710835247.9A priority Critical patent/CN107522755A/en
Publication of CN107522755A publication Critical patent/CN107522755A/en
Pending legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07H—SUGARS; DERIVATIVES THEREOF; NUCLEOSIDES; NUCLEOTIDES; NUCLEIC ACIDS
    • C07H1/00—Processes for the preparation of sugar derivatives
    • C07H1/06—Separation; Purification
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07H—SUGARS; DERIVATIVES THEREOF; NUCLEOSIDES; NUCLEOTIDES; NUCLEIC ACIDS
    • C07H15/00—Compounds containing hydrocarbon or substituted hydrocarbon radicals directly attached to hetero atoms of saccharide radicals
    • C07H15/02—Acyclic radicals, not substituted by cyclic structures
    • C07H15/04—Acyclic radicals, not substituted by cyclic structures attached to an oxygen atom of the saccharide radical
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/582—Recycling of unreacted starting or intermediate materials

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Biochemistry (AREA)
  • Biotechnology (AREA)
  • General Health & Medical Sciences (AREA)
  • Genetics & Genomics (AREA)
  • Molecular Biology (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Detergent Compositions (AREA)

Abstract

The invention belongs to sugar derivatives preparation field, disclose a kind of method that light APG is prepared using loop reactor, this method includes putting into bed material material into loop reactor, and the bed material material is set to be circulated in the Bleaching reactor of loop reactor, controlling reaction temperature and pressure, it is continuously added to circulate feed back, liquid caustic soda and bleaching agent by entry mixers, and after keeping described reaction condition for a period of time, product is continuously removed.Preparation method of the present invention is easy and effective, greatly shortens the drift color time of product, product stability is good, and obtained product remaining oxygen and color and luster are significantly better than prior art.

Description

A kind of method that light APG is prepared using loop reactor
Technical field
The present invention relates to sugar derivatives preparation field, is that one kind prepares light alkyl using loop reactor specifically The method of glucosides.
Background technology
APG (alkyl polyglucosides, APG for short), it is the processing product with renewable starch and grease Glucose and fatty alcohol are raw material, and one point is lost under the catalytic action of acid by the light base of the hemiacetal of glucose and the light base of fatty alcohol New non-ionic surfactants obtained from sub- water.Its surface-active is stronger, there is abundant, fine and smooth and stable foam, decontamination Ability is strong, nontoxic to human body, nonirritant, and resistance to alkali ability is strong, and thickening effect is notable, is cooperateed with yin, yang, nonionic compounding Effect is good, and has the performance characteristics such as sterilization, biodegradable rapid thorough, raising enzyme activity.It is a kind of alternative LAS, AES, AEO etc. prepare various chemicals, the great hair of detergent as commercial auxiliaries or as main active matter and cosurfactant The new non-ionic surfactants of exhibition prospect.
The preparation of APG product mainly by synthesizing, dealcoholysis, drift colour cell into.In general, existed using long-chain fatty alcohol Under the conditions of acidic catalyst is existing directly and glucose response, APG and water are generated, is removed as early as possible using vacuum and nitrogen The water of dereaction generation.In building-up process, in order to obtain desired product distribution, fatty alcohol is often significantly excessive, free The presence of fatty alcohol significantly affects the performance of product, application.So need to carry out it dealcoholation treatment using kestner long-tube evaporator, one As film evaporator is rotated into using falling film evaporator and belt scraping plate.After removing fatty alcohol, the active material of APG is direct It is soluble in water, the certain density APG aqueous solution is formed, because the color of product is deeper, can not meet the needs of user, Need that it is carried out to float color processing.The drift color currently mainly taken is the drift color technique of intervalization.Its flow mainly passes through alkane The intermittent feeding of the pure material of base glucosides, by the way that bleaching agent is added portionwise so that the colourity of product constantly reduces to realize.Due to The time and addition that bleaching agent adds are often related to the state of material, and this adds increased the uncertainty of operation, this is with regard to pole The big stability that have impact on product, while the raising to production capacity also has a great impact.
The domestic technical study to APG is started late, and it is less particularly to float color technical study.External The companies such as Corporation are just comprehensively studied the preparation technology of APG product early in last century the nineties, U.S.Pat.No.2320507 and U.S.Pat.No.22335787 is referred to be carried out continuously using peroxide to APG The idea of color processing is floated, but does not illustrate that U.S.Pat.No.5432275 illustrates to bleach specifically for the mode of realization Agent continuous feed, to the idea of product continuous stripping processing, and implementing procedure is described, but it is not specifically described alkyl Glucosides material, liquid caustic soda, the feed postition of bleaching agent, do not refer to rational solving to do for foam caused by drift color process initial stage Method.The technology of continuous bleaching is used at present, but what is used is only that the kettle with Homogenizing pump and circulating pump comes continuous bleaching, nothing Method solves the well mixed relation with the residence time, as well known to those skilled in the art, after the tank reactor with stirring is full of It is that can not can guarantee that the time needed for bleaching action, therefore, the program is infeasible, can not realize that industrialization is long-term substantial amounts of raw Production.
The content of the invention
It is an object of the invention to can not solve the well mixed and residence time for existing APG preparation technology Relations problems, particularly when with stirring tank reactor be full of after it cannot be guaranteed that bleaching action needed for time the defects of, A kind of method that light APG product is prepared using loop reactor is proposed, this method is realized by loop reactor and made For light APG and especially suitable for industrializing long-term substantial amounts of production.
The purpose of the present invention is achieved in the following ways：
The method that one kind prepares light APG (APG) product using loop reactor, this method comprise the following steps:
Bed material material is passed through into loop reactor, and the bed material material is entered in the Bleaching reactor of loop reactor Row circulation；The Bleaching reactor of loop reactor is warming up to 40 DEG C~95 DEG C；Continuously added simultaneously not by entry mixers The APG aqueous solution, liquid caustic soda and the bleaching agent of color are floated, the pressure of control loop reactor is 0.05MPa~0.5MPa, in ring The Bleaching reactor of road reactor carries out successive reaction, while product is continuously removed.
Described continuous continuous reaction time is 0.5-3.0h.
Described bed material material is to have been subjected to the APG aqueous solution of drift color processing or the APG without drift color The aqueous solution, preferably C12~14The solid content of carbochain is the 50% APG aqueous solution bleached.
It is preferred that the Bleaching reactor of above-mentioned loop reactor is warming up to 60 DEG C~70 DEG C.
It is preferred that the pressure of control loop reactor is 0.15MPa~0.3MPa.
The aqueous solution of the described APG for not floating color, after referring to dealcoholation treatment, residual alcohol is between 0.6%~1.0% APG material add weight than 20~50% deionized waters gained.
Described liquid caustic soda is the aqueous solution of the sodium hydroxide that concentration is 32wt% or oxygen potassium oxide, and liquid is added in the unit interval The quality of alkali is the 1%~18% of APG material solid content.
Described bleaching agent is the industrial hydrogen peroxide solution that concentration is 30wt% or 48%, and bleaching agent is added in the unit interval Quality be APG material solid content 1%~16.5%.
To aqueous products colourity≤20 of APG, during residual oxygen≤100ppm, the APG aqueous solution is continuously moved Go out loop reactor.
Wherein, to aqueous products colourity≤20 of APG, during residual oxygen≤100ppm, the APG aqueous solution is connected It is continuous to remove reaction system.
The loop reactor that the present invention uses is mainly by entry mixers, mixing pump, circulating pump, Bleaching reactor, regulation Valve and one or more post-reactors composition.The input connection APG solution inlet ports of entry mixers, bleaching agent import, and Liquid caustic soda import, three inlet parallel modes connect；The input of the output end connection Bleaching reactor of entry mixers, bleaching are anti- The output end of device is answered to connect the input of one or more post-reactors, the output end of the post-reactor connects final product Outlet.Until products export end, whole loop reactor must be arranged by high request step by step, without gas by entry mixers Bag.
The device of this loop reaction and follow-up further bleaching action, is Bubukao's arrangement, overcome due to airbag and Make the unsafe hidden danger of device；Its pH value real-time quantitative supplement alkali number can be detected in the inlet and outlet of follow-up device simultaneously, protected Hold the pH value of its bleaching.
First circulated in course of reaction of the present invention full of bed material material, raise temperature, the bar of question response temperature and pressure After part reaches, it is continuously added to not float the APG aqueous solution of color processing, is continuously added to bleaching agent and liquid caustic soda so that system is quick Reach continuous drift vitta part, because this reaction unit is continuous feeding and discharging device, no intermittent reaction is stopped because required to react The time only fed.
The inventive method contrasts compared with technology, is back to it is advantageous that the present invention is the material systemic circulation that will have been bleached Top is fed, and after the mixing of blended pump so that material reaches optimal reaction temperature and optimum response pressure at a touch, and greatly The big contact area improved between reaction mass, the problem of the thermograde and concentration gradient of the bleaching kettle of no normal tape stirring. In addition, the tank reactor of existing band stirring due to be not loop reaction system but in kettle by stirring and outer circulation come Strengthen and ensure mass transfer and the heat transfer of reaction, so that the reaction time needed for bleaching action can not ensure, therefore, actually It can not realize in industrial processes.This technique by loop reactor by the large-tonnage product bleached (product) (with not Reactant presses 1~20：1 ratio) systemic circulation reacting optimal temperature and pressure to charging aperture, then with the reactant of raw feed Under fully contacted due to the effect of mixing pump, material (bleaching agent, liquid caustic soda and the APG for not floating color of bleaching action can be made The aqueous solution) between it is quick realize mixing, shorten the drift color time, the pressure for maintaining drift color by the regulating valve that discharges can be at the beginning of color be floated Phase may refrain from the generation of foam, improve utilization rate of equipment and installations.It is additionally, since bleaching loop reaction system and is entirely full of material, without Fill N2Protection, save resource and simplify operability；With conventional process ration, it is advantageous that the material of continuous feed is at a touch Reach the optimum temperature and optimum pressure needed for reaction, the problem of in the absence of concentration gradient and thermograde, and can guarantee that one The fixed residence time, therefore the color time greatly shortens, bleaching effect is improved for drift, Bleaching Quality is guaranteed.
The present invention is made up of using loop reactor entry mixers, circulating pump etc., than traditional Homogenizing pump and circulating pump Tank reactor has obvious efficient mass transfer and heat transfer advantages, and micron order or nanometer can be made the liquid atomization into via entry mixers The droplet of level, increase and the contact area of liquid-liquid, thus can greatly increase mass transfer compared with interval Homogenizing pump and circulating pump kettle And heat transfer efficiency.
This method directly solves APG production technologies Central Plains hydrogen peroxide bleaching and prepares light APG process due to using There is thermograde in intermittent reaction and concentration gradient causes conversion ratio not high and the problem of drift color fluctuation of service；Overcome APG Generate equipment number of units and operate the excessive deficiency of number；Save a large amount of energy consumptions；Can be stably most importantly in production technology Light APG is safely synthesized.
The present invention uses continuous production, therefore the product quality that present invention production obtains is sufficiently stable, is producing 3000 per year Safe operation half a year is more on the APG devices of ton, quality of production remaining oxygen<While 100ppm, content 50% ± 0.2%, color and luster ＜ 20, remaining index entirely reach national standard and the high-quality product standard of export requirement.
Brief description of the drawings
Fig. 1 is the loop reactor that the present invention uses.
In figure, 1.APG solution inlet ports, 2. bleaching agent imports, 3. liquid caustic soda imports, 4. entry mixers, 5. mixing pumps, 6. follow Ring pump, 7. Bleaching reactors, 8, steam condensate (SC) outlet and cooling water inlet, 9. steam inlets and coolant outlet, 10. regulations Valve, 11. one or more post-reactors, 12. products exports.
Embodiment
Embodiment provided by the invention is elaborated with reference to embodiment.
As shown in figure 1, being full of bed material material into the Bleaching reactor 7 of loop reactor, and make the bed material material in ring Circulated in the Bleaching reactor 7 of road reactor, Bleaching reactor 7 is warming up to 40 DEG C~95 DEG C.It is logical from bleaching agent import 2 Enter bleaching agent, the APG solution for not floating color is passed through from APG solution inlet ports 1, be passed through liquid caustic soda from liquid caustic soda import 3, three passes through mixing pump 5 entry mixers 4 driven are pre-mixed, and enter back into circulating pump 6, mixed material is pumped into Bleaching reactor 7 and carried out Successive reaction, the pressure of control loop reactor are 0.05MPa~0.5MPa, obtained reactant be largely recycled back into Material the circulation port of blender 4 with it is foregoing enter raw material premixed, a small amount of product pass through regulating valve 10 entrance 1~4 post-reactor After 11, then the product bleached released from products export 12.
Wherein, bed material material is C12~14Carbochain solid content is the 50% APG aqueous solution bleached, and colourity is 20, residual oxygen is 100ppm.
Color C is not floated12~14The APG aqueous solution that the solid content of carbochain is 60% comes from the thick glycosides after dealcoholysis, colourity For 200~300, residual oxygen is 100ppm.
Embodiment 1
In loop reactor, full of having bleached C12~14The solid content of carbochain is 50% APG aqueous solution conduct The bed material material of color is floated, and the bed material material is circulated in the Bleaching reactor 7 of loop reactor, by Bleaching reactor 7 are warming up to 95 DEG C, and the solid content for being continuously added to not float color respectively by three imports of connection entry mixers 4 is 60% C12~14The APG aqueous solution of carbochain, flow 4.8kg/hr are continuously added to the liquid caustic soda that concentration is 32%, and flow is 0.20kg/hr, the industrial hydrogen peroxide solution that concentration is 30wt% is continuously added to, flow 0.16kg/hr, three is in mixing pump 5 It is pre-mixed in the entry mixers 4 of drive, after entering back into circulating pump 6, mixed material is pumped into Bleaching reactor 7 and carried out Successive reaction, while pass through regulating valve 10 so that the Stress control of loop reactor reaches the water-soluble of APG in 0.2MPa Liquid product colourity≤20, during residual oxygen≤100ppm, material is released from products export 12 again by post-reactor 11, and not up to this refers to Target reaction mass is recycled back to entry mixers 4.The time of successive reaction is 3 hours.Obtain APG finished product.Its colourity is 12, residual oxygen is 56ppm.
Embodiment 2
In loop reactor, full of C12~14The solid content of carbochain is the 50% APG aqueous solution bleached As the bed material material of drift color, and the bed material material is set to be circulated in the Bleaching reactor 7 of loop reactor, bleaching is anti- Device 7 is answered to be warming up to 60 DEG C, the solid content for being continuously added to not float color respectively by three imports of connection entry mixers 4 is 60% C12~14The APG aqueous solution of carbochain, flow 4.8kg/hr, while the liquid caustic soda that concentration is 32% is continuously added to, flow is 0.20kg/hr, is continuously added to the industrial hydrogen peroxide solution that concentration is 30wt%, flow 0.16kg/hr, and three passes through mixing pump It is pre-mixed in 5 entry mixers 4 driven, after entering back into circulating pump 6, mixed material is pumped into Bleaching reactor 7 and entered Row successive reaction, while pass through regulating valve 10 so that the Stress control of loop reactor reaches the water of APG in 0.3MPa Solution product colourity≤20, during residual oxygen≤100ppm, material is released from products export 12 again by post-reactor 11, not up to should The reaction mass of index is recycled back to entry mixers 4, and the time of successive reaction is 1.5 hours.Its colourity is 17, and residual oxygen is 86ppm。
Embodiment 3
In loop reactor, full of having bleached C12~14The solid content of carbochain is 50% APG aqueous solution conduct The bed material material of color is floated, and the bed material material is circulated in the Bleaching reactor 7 of loop reactor, by Bleaching reactor 7 are warming up to 70 DEG C, and the solid content for being continuously added to not float color respectively by three imports of connection entry mixers 4 is 60% C12~14The APG aqueous solution of carbochain, flow 4.8kg/hr, while the liquid caustic soda that concentration is 32% is continuously added to, flow is 0.20kg/hr, is continuously added to the industrial hydrogen peroxide solution that concentration is 30wt%, flow 0.16kg/hr, and three passes through mixing pump It is pre-mixed in 5 entry mixers 4 driven, after entering back into circulating pump 6, mixed material is pumped into Bleaching reactor 7 and entered Row successive reaction, while pass through regulating valve 10 so that the Stress control of loop reactor reaches APG in 0.15MPa Aqueous products colourity≤20, during residual oxygen≤100ppm, material is released from products export 12 again by post-reactor 11, not up to The reaction mass of the index is recycled back to entry mixers 4.The time of successive reaction is 2 hours.APG finished product is obtained, its color Spend for 20, residual oxygen is 58ppm.
Comparative example 1
Carry temperature inductor at one, in the 25L of gate stirrer tank reactor, open stirring and be warming up to 95 DEG C, while kettle top adds N2 so that for the Stress control of loop reactor in 0.2MPa, entry mixers, which disposably add, does not float color C12~C14 carbochains solid content be 60% the APG aqueous solution, quality 12.5kg, at the same add 32% liquid caustic soda 0.52kg, the concentration of addition are 30% industrial hydrogen peroxide solution 0.42kg.The aqueous solution for obtaining APG production after 9.5hr Product, stop stirring.The pH and total solid content of product are adjusted, obtains APG finished product.Its colourity is 52, and residual oxygen is 67ppm.
Comparative example 2
Carry temperature inductor at one, in the 25L of gate stirrer tank reactor, open stirring and be warming up to 85 DEG C, while kettle top adds N2 so that for the Stress control of loop reactor in 0.5MPa, entry mixers, which disposably add, does not float color C12~C14 carbochains solid content be 60% the APG aqueous solution, quality 12.5kg, at the same add 32% liquid caustic soda 0.52kg, add the hydrogen peroxide solution 0.42kg that concentration is 48%.The aqueous products of APG are obtained after 4hr, are stopped Stirring.The pH and total solid content of product are adjusted, obtains APG finished product.Its colourity is 156, and residual oxygen is 320ppm.
Comparative example 3
Carry temperature inductor at one, in the 25L of gate stirrer tank reactor, open stirring and be warming up to 70 DEG C, while kettle top adds N2 so that in 0.05MPa, entry mixers disposably add does not float the Stress control of loop reactor The solid content of C12~C14 carbochains of color is the 60% APG aqueous solution, quality 12.5kg, while the liquid of addition 32% Alkali 0.52kg, add the hydrogen peroxide solution 0.42kg that concentration is 30%.The aqueous products of APG are obtained after 9hr, are stopped Only stir.The pH and total solid content of product are adjusted, obtains APG finished product.Its colourity is 218, and residual oxygen is 350ppm.
Comparative example 4
Carry temperature inductor at one, in the 25L of gate stirrer reactor, add 3.5kgC12-14 carbochains Bed material material of the APG aqueous solution that solid content is 50% as drift color, opens stirring and is warming up to 85 DEG C, while kettle top adds Enter N2So that the Stress control of reactor is continuously added to not float the C12-14 of color in 0.5MPa by gear wheel metering pump by bottom The solid content of carbochain is the 60% APG aqueous solution, flow 4.8kg/h, while be continuously added to 32% liquid caustic soda, flow For 0.20kg/h, the hydrogen peroxide solution that concentration is 30%, flow 0.16kg/h are continuously added to.After continuous feed 4.0h, product Gone out by the overflow of reactor upper end, adjust the pH value and total solid content of product, obtain APG finished product.Its colourity is 77, residual oxygen For 96ppm.
Embodiment 1 is compared with comparative example 1
Embodiment 1 Comparative example 1
Bleaching form Continuously Intermittently
Residual oxygen 56ppm 67ppm
Color and luster 12 52
Product stability It is good It is good
Embodiment 2 is compared with comparative example 2
Embodiment 2 Comparative example 2
Bleaching form Continuously Intermittently
Residual oxygen 86ppm 320ppm
Color and luster 17 156
Product stability It is good Difference
Embodiment 3 is compared with comparative example 3
Embodiment 3 Comparative example 3
Bleaching form Continuously Intermittently
Residual oxygen 58ppm 350ppm
Color and luster 20 218
Product stability It is good Difference
Embodiment 1 is compared with comparative example 4
Embodiment 3 Comparative example 4
Bleaching form Continuously Continuously
Residual oxygen 56ppm 96ppm
Color and luster 12 77
Product stability It is good Difference
Remaining oxygen is determined according to potassium permanganate colorimetry.
Color and luster is determined according to GB/T19464-2004 methods.
Product stability preferably refers to：Product chromatic value<50, remaining oxygen≤100ppm.In product chromatic value and remaining oxygen Have that an index is below standard, it is as poor.
Colourity and residual oxygen value in table are to weigh the important indicator of product quality, and bleaching form is the direct indicator of production capacity.
Therefore, the present invention realizes bleaching process using loop reactor, and largely completely reacted Matter Transfer is returned and added Shots, and optimal reaction condition, whole reaction system are reached by mixing pump and circulating pump reaction mass at a touch Mass transfer and heat transfer efficiency are greatly improved.In conventional tank reactor, homogeneous and can was both reached and has retained certain reaction Time can not be realized.

Claims (9)

  1. A kind of 1. method that light APG product is prepared using loop reactor, it is characterised in that this method includes following Step:
    Bed material material is passed through into loop reactor, and the bed material material is followed in the Bleaching reactor of loop reactor Ring；The Bleaching reactor of loop reactor is warming up to 40 DEG C~95 DEG C；Continuously added simultaneously by entry mixers and do not float color The APG aqueous solution, liquid caustic soda and bleaching agent, the pressure of control loop reactor is 0.05MPa~0.5MPa, anti-in bleaching Answer and successive reaction is carried out in device, while product is continuously removed.
  2. 2. the method according to claim 1 that light APG product is prepared using loop reactor, it is characterised in that Described continuous reaction time is 0.5-3.0h.
  3. 3. the method according to claim 1 that light APG product is prepared using loop reactor, it is characterised in that Described bed material material is to have been subjected to the APG aqueous solution of drift color processing or the APG aqueous solution without drift color.
  4. 4. the method that light APG product is prepared using loop reactor according to claim, it is characterised in that The Bleaching reactor of described loop reactor is warming up to 60 DEG C~70 DEG C.
  5. 5. the method that light APG product is prepared using loop reactor according to claim, it is characterised in that The pressure of described loop reactor is 0.15MPa~0.3MPa.
  6. 6. the method according to claim 1 that light APG product is prepared using loop reactor, it is characterised in that The aqueous solution of the described APG for not floating color, after referring to dealcoholation treatment, alkyl sugar of the residual alcohol between 0.6%~1.0% Glycosides material adds weight than obtained by 20~50% deionized waters.
  7. 7. the method according to claim 1 that light APG product is prepared using loop reactor, it is characterised in that Described liquid caustic soda is the aqueous solution of the sodium hydroxide that concentration is 32wt% or oxygen potassium oxide.
  8. 8. the method according to claim 1 that light APG product is prepared using loop reactor, it is characterised in that Described bleaching agent is the industrial hydrogen peroxide solution that concentration is 30wt% or 48%.
  9. 9. the method according to claim 1 that light APG product is prepared using loop reactor, it is characterised in that To aqueous products colourity≤20 of APG, during residual oxygen≤100ppm, it is anti-that the APG aqueous solution is continuously removed loop Answer device.
CN201710835247.9A 2017-09-15 2017-09-15 A kind of method that light APG is prepared using loop reactor Pending CN107522755A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201710835247.9A CN107522755A (en) 2017-09-15 2017-09-15 A kind of method that light APG is prepared using loop reactor

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201710835247.9A CN107522755A (en) 2017-09-15 2017-09-15 A kind of method that light APG is prepared using loop reactor

Publications (1)

Publication Number Publication Date
CN107522755A true CN107522755A (en) 2017-12-29

Family

ID=60736750

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201710835247.9A Pending CN107522755A (en) 2017-09-15 2017-09-15 A kind of method that light APG is prepared using loop reactor

Country Status (1)

Country Link
CN (1) CN107522755A (en)

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5432275A (en) * 1994-02-25 1995-07-11 Henkel Corporation Continuous bleaching of alkylpolyglycosides
CN102503866A (en) * 2011-09-29 2012-06-20 无锡青苹果工程勘察设计院 Method for preparing sodium fatty acid methyl ester sulfonate with low content of disodium salt
CN105732731A (en) * 2016-01-28 2016-07-06 上海发凯化工有限公司 Method for preparing light-colored alkyl glycoside product

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5432275A (en) * 1994-02-25 1995-07-11 Henkel Corporation Continuous bleaching of alkylpolyglycosides
CN102503866A (en) * 2011-09-29 2012-06-20 无锡青苹果工程勘察设计院 Method for preparing sodium fatty acid methyl ester sulfonate with low content of disodium salt
CN105732731A (en) * 2016-01-28 2016-07-06 上海发凯化工有限公司 Method for preparing light-colored alkyl glycoside product

Similar Documents

Publication Publication Date Title
CN103992443A (en) Method for preparing polycarboxylate water reducing agent by normal-temperature mixing process
CN103484264B (en) High concentrated paste-shaped detergent
CN102020578B (en) Method and device for continuously producing fatty acid alkanolamide
CN110449103A (en) A kind of integration system of band premix for diazonium salt method and apparatus
CN102585199B (en) Method for preparing polyether polyol
CN105967161A (en) Method for continuously preparing low-cost battery grade ferric phosphate by utilizing iron filings
CN208213187U (en) A kind of nitrification installation preparing H acid
CN101693678A (en) Process for preparing alpha-sulfo fatty acid methyl ester sodium salt
CN110395770A (en) A method of iron oxide red is produced using sludge material
CN107522755A (en) A kind of method that light APG is prepared using loop reactor
CN114105735A (en) Preparation method and production device of Guerbet alcohol ether
CN208275392U (en) A kind of continuous neutralization device
CN108299177B (en) Full continuous flow synthesis process of 2-methyl-1, 4-naphthoquinone
CN102786557B (en) Preparation method of tetradecyl glucopyranoside
CN106010845B (en) A kind of energy-saving soapmaking system
CN205556513U (en) Continuous hydrogenation ware of organic intermediate
CN101723991B (en) Method for preparing alkyl polyglycoside
CN101239864A (en) Method and device for synthesizing six-membered cyclic compound by continuous method
US2838575A (en) Production of glycerine by hydroxylation of allyl alcohol
CN107382123A (en) A kind of efficient cement liquid grinding aid
CN105732731A (en) Method for preparing light-colored alkyl glycoside product
CN108129327A (en) Parachloroanilinum is produced using solvent-free continuous catalytic hydrogenation
CN218422779U (en) Methyl-terminated polyether production device
CN206438057U (en) The system that isobutene is prepared for tert-butyl alcohol dehydration
CN109851654A (en) The method of pipeline reactor saponification extracting cholesterin from lanolin

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
RJ01 Rejection of invention patent application after publication
RJ01 Rejection of invention patent application after publication

Application publication date: 20171229