CN203530187U - Glycosidation reactor for continuously synthesizing alkyl glycoside by one-step method - Google Patents
Glycosidation reactor for continuously synthesizing alkyl glycoside by one-step method Download PDFInfo
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- CN203530187U CN203530187U CN201320519895.0U CN201320519895U CN203530187U CN 203530187 U CN203530187 U CN 203530187U CN 201320519895 U CN201320519895 U CN 201320519895U CN 203530187 U CN203530187 U CN 203530187U
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Abstract
The utility model relates to a glycosidation reactor for continuously synthesizing alkyl glycoside by a one-step method. The reactor comprises N grades of independent reaction units which are sequentially connected, the mixed raw material inlet and the product material outlet of the glycosidation reactor are respectively connected with the material inlet of the first grade of independent reaction unit and the material outlet of the last grade of independent reaction unit, when in continuous synthesis of the alkyl glycoside by the one-step method, the reacted material of the N-1 grade of independent reaction unit is taken as the raw material of the N grade of independent reaction unit, and the feed rate of the mixed raw material inlet of the glycosidation reactor is determined by the content of residue sugar in the reacted material of the last grade of independent reaction unit, and the discharge rate of the product material outlet of the glycosidation reactor is passively changed along with the change of the feed rate of the mixed raw material inlet of the glycosidation reactor. The reactor can realize continuous synthesis of alkyl glycoside through the one-step method, can guarantee the product to be homogeneous and has stable quality, and is beneficial for post treatment.
Description
Technical field
The utility model belongs to alkyl glycoside preparation field, is specifically related to the device of single stage method synthesizing alkyl polyglycoside, especially a kind of reaction of guanosine device that adopts the continuous synthesizing alkyl polyglycoside of single stage method.
Background technology
Alkyl glycoside (Alkyl Polyglycoside, APG), being a kind of new non-ionic surfactants occurring from the nineties in 20th century, is by natural renewable resources fatty alcohol and saccharide compound (mostly being glucose), and under an acidic catalyst, dehydration forms.It, can be composite preferably with any tensio-active agent with many features of nonionogenic tenside and anion surfactant, have simultaneously efficient, nontoxic, non-stimulated to skin, can complete biodegradable, the feature such as synergistic effect is obvious.Thereby be widely used in the every field of people life.
At present, the method for industrial production alkyl glycoside mainly contains two kinds:
A kind of is that glucose reacts with low-carbon alcohol, and then carries out transketalation reaction with higher alcohols, obtains high-carbon glucosides, finally by techniques such as distillation, bleachings, makes the alkyl glycoside aqueous solution.For example, United States Patent (USP) (US5374716), Chinese patent (CN92102625.0, CN95116215.2, CN95116217.9, CN92102625.0) have all adopted this method.Although this method production process is easily controlled, the APG quality product of gained is poor, exists color darker, and residual alcohol content is high, and product mostly is mixed glycosides, is unfavorable for the preparation of postorder workshop section derivative, affects quality product.
Another kind be glucose directly and higher alcohols reaction, then through neutralization, distillation, obtain alkyl glycoside after bleaching.In the method production process, because the solubleness of glucose in higher alcohols is very low, be solid-liquid two-phase substantially, cause speed of reaction lower, and sugar also easily caking, make reaction not thorough.United States Patent (USP) (US5576425) has been described glucose and higher alcohols has been made to suspension, then divides some batches to join in reaction, alleviates the caking of glucose, and it is fully reacted.Chinese patent (200510096464.8) has been described anhydrous or dextrose hydrate is carried out reacting with higher alcohols after ultra micro efflorescence processing again.Chinese patent (200410064505.0) is strengthened abundant mixing and the mass transfer of two parts of materials by material outside circulation.Although these measures have had significant improvement aspect speed of reaction, but because building-up process is carried out in reactor, periodical operation in batches, the quality of sintetics is unstable, at the polymerization degree, color and luster, residual sugar content, there is very big difference between batches, cause follow-up workshop section difficult treatment, be difficult to guarantee stable product quality.
Summary of the invention
In order to overcome the above-mentioned defect of prior art, the utility model object is to provide a kind of reaction of guanosine device that adopts the continuous synthesizing alkyl polyglycoside of single stage method, can realize and adopt carrying out continuously of One-step production alkyl glycoside, and can guarantee the stable, even of quality product, be conducive to the carrying out of subsequent disposal.
The main technical schemes that the utility model adopts is:
A reaction of guanosine device that adopts the continuous synthesizing alkyl polyglycoside of single stage method, it mainly comprises:
N level independent reaction unit, there is N described independent reaction unit to connect successively (material inlet of N level independent reaction unit connects the material outlet of N-1 level independent reaction unit), the mixing raw material entrance of described reaction of guanosine device connects the material inlet of first step independent reaction unit, the product material outlet of described reaction of guanosine device connects the material outlet of last step independent reaction unit, wherein, N >=2.
While adopting the continuous synthesizing alkyl polyglycoside of single stage method, using from the reacting rear material in N-1 level independent reaction unit as raw material in N level independent reaction unit, and, alkyl glycoside content in the reacting rear material of N level independent reaction unit output is higher than the alkyl glycoside content in the reacting rear material of N-1 level independent reaction unit output, simultaneously, residual sugar content in the reacting rear material of the pan feeding speed of the mixing raw material entrance of described reaction of guanosine device in last step independent reaction unit is determined, the corresponding passive variation with the change of the pan feeding speed of the mixing raw material entrance of described reaction of guanosine device of the discharging speed of the product material outlet of described reaction of guanosine device.
Wherein, N≤50.Be preferably 3≤N≤10.
Be preferably N >=4.
Be preferably N >=5.
Wherein, described at least one, independent reaction unit is provided with the dividing plate of cutting apart that independent reaction unit that it is adjacent separates, and between adjacent independent reaction unit, be provided with from described in cut apart the overflow ducts of the material stream passed for liquid of the top of dividing plate extending to bottom.
Described reaction of guanosine device can comprise that an above inside is provided with the tubular reaction of guanosine device body of vacuum chamber.
When being provided with a described tubular reactor body, the set-up mode of described N level independent reaction unit in a described tubular reactor body is:
Mode (1), by cutting apart dividing plate described in N-1, in the vacuum chamber of tubular reaction of guanosine device body, be directly separated, between adjacent independent reaction unit, be equipped with from described in cut apart the overflow ducts of the material stream passed for liquid of the top of dividing plate extending to bottom; Or,
Mode (2), a plurality of described independent reaction unit connect and compose a reaction component successively, described in being equipped with certainly between adjacent independent reaction unit in this reaction component, cut apart the top of dividing plate to the overflow ducts of the material stream passed for liquid of bottom extension, m group comprises the described reaction component described N level independent reaction in series unit of equal amts or different quantities independent reaction unit, and is assembled in the vacuum chamber of described tubular reactor body.
When being provided with a plurality of described tubular reactor body, in at least one independent reaction unit in described N level independent reaction unit tubular reactor body located therein, while being provided with a plurality of independent reactions unit in a tubular reactor body, (1) or mode (2) arrange in a manner described.
Wherein, the set-up mode of described overflow ducts can be:
The described downstream position of cutting apart dividing plate is provided with over-pass, and the height of described over-pass is a little more than the described height of cutting apart dividing plate, described in cut apart the passage that the inwall of dividing plate and over-pass and tubular reaction of guanosine device body surrounds and form described overflow ducts; Or,
Described overflow ducts comprises the pipeline of material stream passed for liquid, and the entrance of described pipeline is located at the top of cutting apart dividing plate, and described pipeline extends to the bottom of cutting apart dividing plate, and the position of pipe outlet is lower than the position of entrance.
Wherein, described N level independent reaction can be equipped with stirring rake in unit, and described stirring rake is slurry formula, belt or frame, is preferably spiral belt.
Wherein, the set-up mode of described stirring rake is:
In aforesaid way (1), described stirring rake in described N level independent reaction unit is all located on same stir shaft, described stir shaft is through the dividing plates of cutting apart at different levels, and tubular reaction of guanosine device body is extended at two ends, and the two ends of stir shaft and tubular reaction of guanosine device body are tightly connected.Wherein, the two ends of stir shaft can be tightly connected by liquid sealing device and tubular reaction of guanosine device body.
In aforesaid way (2), the described stirring rake in each independent reaction unit in described reaction component is all located on same stir shaft.Wherein, the described stirring rake that m organizes in each independent reaction unit in described reaction component can be all located on same stir shaft.
Wherein, described tubular reaction of guanosine device body can be provided with chuck, is provided with heating agent path in described chuck, and the two ends of described heating agent path are provided with high temperature heating agent entrance and the outlet of low temperature heating agent, utilize heating agent to heat the material in tubular reaction of guanosine device body, and maintain suitable temperature.For example, temperature range can be 20 ℃-150 ℃, is preferably 60 ℃-120 ℃.
Wherein, a part for the vacuum chamber of described tubular reaction of guanosine device body can be the gas space, and this gas space is provided with vacuum orifice.
Wherein, the cross section of described tubular reaction of guanosine device body can and be that the oval middle part of part is any shape in rectangle up and down for circle, rectangle, ellipse, pyriform, lower-circle-square-shape.
Wherein, described tubular reaction of guanosine device body can also be provided with thief hatch as required.
Be preferably, described thief hatch place is provided with a detector that automatically detects residual sugar amount in sample, this detector connects a controller, described mixing raw material ingress is provided with a raw material flow controller, raw material flow controller also connects this controller, the residual sugar amount concentration that this controller measures according to residual sugar amount detector, controls raw material flow controller work, enters into the speed of tubular reactor body to control mixing raw material.
Wherein, described tubular reaction of guanosine device body can also be provided with as required in temperature-measuring port, visor, vacuum orifice and manhole any or appoint several.
Wherein, the below of described tubular reaction of guanosine device body can be provided with the bracing or strutting arrangement that supports described tubular reaction of guanosine device body.
Above-mentioned reaction of guanosine device described in any, is preferably, described in cut apart dividing plate and be vertically located in tubular reaction of guanosine device body, and each overflow height of cutting apart dividing plate top is in same level.
Described tubular reaction of guanosine device body can be a horizontal reacting tank.
Be preferably, arranging of described mixing raw material entrance and product material outlet is highly identical and a little less than described horizontal plane, the inner side of described mixing raw material entrance is also provided with over-pass, described product material outlet inner side is provided with buffering overflow port, and the overflow height of described buffering overflow port is identical with the overflow height of described overflow ducts.
The beneficial effects of the utility model are:
Owing to reactor being divided into N independent reaction unit, and connect according to this, make reaction of guanosine can be divided into multistage carrying out, residual sugar content in next stage independent reaction unit is lower than upper level, i.e. reaction is progressively carried out, there will not be back-mixing, the long reaction time of having avoided back-mixing to cause, react inhomogeneous defect, and make the reaction of guanosine process in reactor easily control, and be convenient to control the discharging of product after reaction, avoided the inhomogeneous defect of discharging, and, by the N level independent reaction unit connecting is successively set, and by the residual sugar content in the reacting rear material in last step independent reaction unit, determine the pan feeding speed of the mixing raw material entrance of described reaction of guanosine device, simultaneously, by controlling the pan feeding speed of the mixing raw material entrance of described reaction of guanosine device, adjust the discharging speed of the product material outlet of described reaction of guanosine device simultaneously, what make that reaction of guanosine device of the present utility model both can realize raw material adds the continuous output with product continuously, can guarantee again quality product stable of institute's output, evenly.
Accompanying drawing explanation
Fig. 1 is the one-piece construction schematic diagram of the utility model the first embodiment.
Fig. 2 is the one-piece construction schematic diagram (arrow is flow direction, and distribution and the liquid trend of independent reaction unit is only shown) of the utility model the second embodiment.
Fig. 3 is the one-piece construction schematic diagram (arrow is flow direction, and distribution and the liquid trend of independent reaction unit is only shown) of the utility model the 3rd embodiment.
Fig. 4 is the vertical view (arrow is flow direction, and distribution and the liquid trend of independent reaction unit is only shown, and overflow ducts is at medium position) of the superiors in Fig. 3.
Fig. 5 is the vertical view (arrow is flow direction, and distribution and the liquid trend of independent reaction unit is only shown, and overflow ducts is in circumferential position) of the upper several second layers in Fig. 3.
[main element nomenclature]
1, tubular reaction of guanosine device body; 2, stir shaft; 3, stirring rake; 4, over-pass; 5, cut apart dividing plate; 6, chuck; 7, liquid sealing device; 8, bracing or strutting arrangement; 9, mixing raw material entrance; 10, product material outlet.
Embodiment
In order being more convenient for, to understand the utility model, below in conjunction with accompanying drawing, by embodiment, the utility model to be further described.
Referring to Fig. 1, the reaction of guanosine device (referred to as reaction of guanosine device) of the continuous synthesizing alkyl polyglycoside of employing single stage method of the utility model the first embodiment, it mainly comprises a tubular reaction of guanosine device body 1.
Described tubular reaction of guanosine device body can be a horizontal reacting tank.
The inside of described tubular reaction of guanosine device body 1 is provided with vacuum chamber, in described vacuum chamber, be provided with multi-stage division dividing plate 5, described multi-stage division dividing plate 5 distributes vertically in reaction of guanosine device, in vacuum chamber, be separated out a plurality of relatively independent reaction compartments, each reaction compartment is equivalent to an independently reaction member.
In described reaction of guanosine device, be provided with N level independent reaction unit (N >=2), independent reaction unit described in N level connects (material inlet of n level independent reaction unit connects the material outlet of n-1 level independent reaction unit) successively, the mixing raw material entrance 9 of described reaction of guanosine device connects the material inlet of first step independent reaction unit, and the product material outlet 10 of described reaction of guanosine device connects the material outlet of last step independent reaction unit.
Described N level independent reaction unit can for 2 grades, 3 grades, 4 grades or 5 grades (shown in Fig. 1, be that 5 grades of independent reaction unit transverses are linked in sequence, be located in the vacuum chamber of tubular reaction of guanosine device body 1), described N level independent reaction unit can be also more multistage, can arrange as required.
Described in being provided with certainly between adjacent independent reaction unit, cut apart the top of dividing plate 5 to the overflow ducts of the material stream passed for liquid of bottom extension.
Make reaction of guanosine device of the present utility model, while adopting the continuous synthesizing alkyl polyglycoside of single stage method, using from the reacting rear material in N-1 level independent reaction unit as raw material in N level independent reaction unit, and the alkyl glycoside content in the reacting rear material of N level independent reaction unit output is higher than the alkyl glycoside content in the reacting rear material of N-1 level independent reaction unit output.
Simultaneously, residual sugar content in the reacting rear material of the pan feeding speed of the mixing raw material entrance 9 of described reaction of guanosine device in last step independent reaction unit is determined, the corresponding passive variation with the change of the pan feeding speed of the mixing raw material entrance 9 of described reaction of guanosine device of the discharging speed of the product material outlet 10 of described reaction of guanosine device.While measuring residual sugar content, can be undertaken by described product material outlet 10, also can on tubular reaction of guanosine device body 1, thief hatch be set as required, so that at any time residual sugar content is measured in operational process.
Wherein, the set-up mode of described overflow ducts is: described in cut apart dividing plate 5 downstream position be provided with over-pass 4, the height of described over-pass 4 is a little more than the described height of cutting apart dividing plate 5, described in the passage cut apart between dividing plate 5 and the inwall of over-pass 4 and tubular reaction of guanosine device body 1 form described overflow ducts.
In another embodiment of the present utility model, described overflow ducts comprises the pipeline of the independent setting of material stream passed for liquid, the entrance of described pipeline is located at the top of cutting apart dividing plate 5, and described pipeline extends to the bottom of cutting apart dividing plate 5, and the position of outlet is lower than the position of entrance.Described pipeline can be round tube or rectangular pipe.
In the first embodiment of the present utility model shown in Fig. 1, described in cut apart dividing plate 5 and be vertically located in the vacuum chamber of tubular reaction of guanosine device body 1, and each overflow height of cutting apart dividing plate 5 tops is in same level.
Be preferably, arranging of described mixing raw material entrance 9 and product material outlet 10 is highly identical and a little less than described horizontal plane, the inner side of described mixing raw material entrance 9 is provided with described over-pass 4, described product material outlet 10 inner sides are provided with buffering overflow port, and the overflow height of described buffering overflow port is identical with the overflow height of described overflow ducts.
In order to promote that in independent reactions at different levels unit, mixing of materials is even, can in described N level independent reaction unit, be equipped with stirring rake 3.
Wherein, described stirring rake 3 is located on same stir shaft 2, and described stir shaft 2 is through the dividing plates 5 of cutting apart at different levels, and tubular reaction of guanosine device body 1 is extended at two ends, and is tightly connected by liquid sealing device 7 and tubular reaction of guanosine device body 1.Described stir shaft 2 extends wherein one end of tubular reaction of guanosine device body 1, is connected with drive-motor.
Be preferably, described stirring rake 3 is propeller.
In order guaranteeing to react under stable, suitable temperature condition, to carry out, in described reaction of guanosine device, to be provided with heating or attemperator, utilize heating agent to heat the material in tubular reaction of guanosine device body, and maintain suitable temperature.Be preferably, described tubular reaction of guanosine device body 1 can be provided with chuck, is provided with heating agent path in described chuck, and the two ends of described heating agent path are provided with high temperature heating agent entrance and the outlet of low temperature heating agent, and high temperature heating agent entrance is typically provided with heating medium valve.For example, temperature range can be 20 ℃-150 ℃, is preferably 60 ℃-120 ℃.For the ease of carrying out temperature actuated, described tubular reaction of guanosine device body can also be provided with temperature-measuring port as required.
Wherein, a part for the vacuum chamber of described tubular reaction of guanosine device body can be the gas space, and this gas space is provided with vacuum orifice.Vacuum orifice can be for connecting vacuum extractor.Vacuum tightness in described vacuum chamber is generally 0-0.1Mpa.
Wherein, the cross section of described tubular reaction of guanosine device body 1 can and be that the oval middle part of part is any shape in rectangle up and down for circle, rectangle, ellipse, pyriform, lower-circle-square-shape.
Described tubular reaction of guanosine device body 1 can also be provided with visor as required, so that the situation of carrying out of observing response.
For the ease of installation, maintenance, described tubular reaction of guanosine device body 1 can also be provided with manhole as required.
Wherein, the below of described tubular reaction of guanosine device body 1 can be provided with the bracing or strutting arrangement that supports described tubular reaction of guanosine device body.
Above-mentioned reaction of guanosine device described in any, can work according to the following procedure:
By higher alcohols, glucose mixes by a certain percentage, make mixture, the mixture of making is added to reaction of guanosine device from mixing raw material entrance 9 with given pace, can add entrance by catalyzer and add proper catalyst, and enter successively independently reaction compartment of each section by overflow ducts, after making each section of independent reaction unit all be full of mixture, stop feeding in raw material, under the stirring action of stirring rake, mixture further mixes, open chuck heating medium valve, control reaction operates under certain temperature and vacuum tightness, the clarification that becomes of reaction solution in back segment independent reaction space, the mensuration of residual sugar content is carried out in sampling, when residual sugar content is less than 0.05%, start from mixing raw material entrance 9, to add continuously mixture by setting speed, simultaneously with same speed from product material outlet 10 extraction materials, realize continuously and producing.And constantly detect the residual sugar content of extraction material, and according to the residual sugar content in extraction material, regulating reaction conditions and feeding rate, Optimizing operation index, makes constant product quality, evenly.
The service temperature of alkyl glycoside building-up process is generally 20 ℃-150 ℃, and optimal temperature is 60 ℃-120 ℃.
The operation vacuum tightness of alkyl glycoside building-up process is generally 0-0.1MPa.
Several Application Example of the present utility model (wherein, Application Example 1-3 is based on the first embodiment, and Application Example 4 is based on another embodiment) is also provided below:
Application Example 1: octanol, glucose in mass ratio 5:1 ratio mixes, with add the catalyzer of raw material total mass 0.5% in reaction of guanosine device, control 110 ℃ of temperature of reaction, vacuum tightness 0.095MPa, stir lower reaction reaction solution clarification that becomes after 2 hours, the residual sugar content of measuring in the reacting rear material in last step independent reaction unit is 0.03%, beginning adds material from mixing raw material entrance 9 continuously with the speed of 400Kg/h, from product material outlet 10, automatically flow out product material simultaneously, constantly detect the residual sugar content of extraction material, residual sugar content remains unchanged substantially, flow out material color and luster light, micro-yellow, gas Chromatographic Determination is the mixture of APG, its polymerization degree is 1.243, the parameter of product material is as shown in table 1 with the relation of continuous production time.
Table 1
Application Example 2: get decyl alcohol and glucose in mass ratio 5:1 ratio after mixing, put into reaction of guanosine device and react, at 110 ℃, vacuum tightness 0.095MPa, stir lower reaction question response liquid clarification that becomes after 2 hours, carry out the mensuration of the residual sugar content in the reacting rear material in last step independent reaction unit, residual sugar content equals 0.02% after testing, now start with the speed of 400Kg/h, to add continuously mixture from mixing raw material entrance 9, from product material outlet 10, flow out material simultaneously, constantly detect the residual sugar content of extraction material, residual sugar content will remain unchanged (substantially constant by regulating feeding rate to maintain residual sugar content: while detecting residual sugar content substantially, as bigger than normally in numerical value should reduce feeding rate, as residual sugar content reduces, can suitably increase feed rate).Flow out material color and luster light, micro-yellow, the mixture that gas Chromatographic Determination is APG, its polymerization degree is 1.3.The parameter of product material is as shown in table 2 with the relation of continuous production time.
Table 2
Application Example 3: the mixed alcohol (mol ratio 1:1) of getting C8-C10 and glucose in mass ratio 5:1 ratio are put into reaction of guanosine device after mixing, at 110 ℃, vacuum tightness 0.095MPa reacts, the clarification that becomes of question response liquid, carry out the mensuration of the residual sugar content in the reacting rear material in last step independent reaction unit, residual sugar content equals 0.03% after testing, now start with the speed of 385Kg/h, to add continuously material from mixing raw material entrance 9, from product material outlet 10, automatically flow out material simultaneously, constantly detect the residual sugar content of extraction material, when residual sugar content remains unchanged substantially, flow out material color and luster light, micro-yellow, gas Chromatographic Determination is the mixture of APG, its polymerization degree is 1.3.The parameter of product material is as shown in table 3 with the relation of continuous production time.
Table 3
Application Example 4(is by the above-mentioned reaction of guanosine device series connection of two N=2, form the Application Example of the reaction of guanosine device that is equivalent to N=4), the mixed alcohol (mol ratio 1:1) of getting C8-C10 and glucose in mass ratio 5:1 ratio are entered by first reaction of guanosine device import 9 after mixing, two reaction of guanosine devices are all at 110 ℃, vacuum tightness 0.095MPa reacts, until the second reactor outlet (being product material outlet 10) residual sugar content lower than 0.02% time, beginning adds material from mixing raw material entrance 9 continuously with the speed of 400Kg/h, from product material outlet 10, automatically flow out material simultaneously, constantly detect the residual sugar content of extraction material, when residual sugar content remains unchanged substantially, flow out material color and luster light, micro-yellow, gas Chromatographic Determination is the mixture of APG, its polymerization degree is 1.3.The parameter of product material is as shown in table 4 with the relation of continuous production time.
Table 4
From above-mentioned Application Example 1-4, the reaction of guanosine device of the continuous synthesizing alkyl polyglycoside of employing single stage method of the present invention, can realize the continuous production of alkyl glycoside, and, constant product quality.
The second embodiment of the present utility model as shown in Figure 2, the described dividing plate 5 of cutting apart longitudinally distributes, be horizontally set in tubular reaction of guanosine device body 1, and form the multilayer independent reaction unit distributing up and down, mixing raw material entrance 9 is located at one end of the superiors' independent reaction unit, overflow ducts is located at the other end of independent reaction unit, the flow direction of material in neighbouring two independent reaction unit is contrary, after material reaction in the independent reaction unit on upper strata, under flowing into, in the independent reaction unit of one deck, continue reaction, product material outlet 10 is located at one end away from its overflow ducts of undermost independent reaction unit.In embodiment shown in Fig. 2, in overflow ducts position, be provided with over-pass 4, in another embodiment of the present utility model, also over-pass 4 can be set, and play the effect identical with over-pass 4 with the inwall of tubular reaction of guanosine device body 1.
As Fig. 3, the 3rd embodiment of the present utility model shown in Fig. 4 and Fig. 5, described tubular reaction of guanosine device body 1 is vertical response tank, the described dividing plate 5 of cutting apart longitudinally distributes, be horizontally set in tubular reaction of guanosine device body 1, mixing raw material entrance 9 is located at the outside of the superiors' independent reaction unit, and form the multilayer independent reaction unit distributing up and down, the overflow ducts of the independent reaction unit of adjacent layers is alternately located at centre and outside left, and, a plurality of independent reaction subelements that distribute ringwise of inside and outside arranged concentric are set in every layer of independent reaction unit, the flow direction in the independent reaction subelement of the flow direction of material in each annular independent reaction subelement and adjacent annular is contrary.
For example, mixture enters in the outermost independent reaction subelement of the superiors' independent reaction unit from mixing raw material entrance 9, and along flowing to and flow clockwise, to the overflow port being connected with the independent reaction subelement of adjacent interior ring, overflow enters in the independent reaction subelement of adjacent interior ring, and flow in the counterclockwise direction, to the overflow port being connected with the independent reaction subelement of adjacent interior ring, overflow enters in the independent reaction subelement of adjacent interior ring, and flow along clockwise direction, the rest may be inferred, until arrive the overflow ducts position that this layer of independent reaction unit is connected with lower one deck independent reaction unit, overflow enters in lower one deck independent reaction unit, in ensuing one deck independent reaction unit, in the independent reaction subelement of material in this layer, by interior hoop outer shroud, flowed, until the independent reaction subelement of outer shroud, arrive the overflow ducts position being connected with lower one deck independent reaction unit, overflow enters in lower one deck independent reaction unit, the rest may be inferred, until arrive the product material outlet 10 of tubular reaction of guanosine device body 1.
The overflow ducts position of the independent reaction unit of adjacent layers can arrange over-pass 4, and wherein, over-pass 4 can arrange by the mode shown in Fig. 3, and its height is a little less than cutting apart arranging highly of dividing plate 5.
Each layer of independent reaction unit in the utility model the 3rd embodiment also can not be set to concentric some annular independent reaction subelement, and presses spiral of Archimedes setting.
Reaction of guanosine device of the present utility model is by arranging the N level independent reaction unit connecting successively, and by the residual sugar content in the reacting rear material in last step independent reaction unit, determine the pan feeding speed of the mixing raw material entrance of described reaction of guanosine device, simultaneously, by controlling the pan feeding speed of the mixing raw material entrance of described reaction of guanosine device, adjust the discharging speed of the product material outlet of described reaction of guanosine device simultaneously, what make that reaction of guanosine device of the present utility model both can realize raw material adds the continuous output with product continuously, can guarantee again quality product stable of institute's output, evenly.
Claims (13)
1. a reaction of guanosine device that adopts the continuous synthesizing alkyl polyglycoside of single stage method, is characterized in that, comprising:
N level independent reaction unit, there is N described independent reaction unit to connect successively, the mixing raw material entrance of described reaction of guanosine device connects the material inlet of first step independent reaction unit, the product material outlet of described reaction of guanosine device connects the material outlet of last step independent reaction unit, wherein, N >=2.
2. reaction of guanosine device as claimed in claim 1, is characterized in that: 3≤N≤50.
3. reaction of guanosine device as claimed in claim 2, is characterized in that: 3≤N≤10.
4. reaction of guanosine device as claimed in claim 1, it is characterized in that: described at least one, independent reaction unit is provided with the dividing plate of cutting apart that independent reaction unit that it is adjacent separates, and the overflow ducts of the material stream passed for liquid that extend to bottom at the top of cutting apart dividing plate described in being provided with certainly between adjacent independent reaction unit, described reaction of guanosine device comprises that one or more inside is provided with the tubular reactor body of vacuum chamber
When being provided with a described tubular reactor body, the set-up mode of described N level independent reaction unit in a described tubular reactor body is:
Mode 1, by cutting apart dividing plate described in N-1, in the vacuum chamber of tubular reactor body, be directly separated, between adjacent independent reaction unit, be equipped with from described in cut apart the overflow ducts of the material stream passed for liquid of the top of dividing plate extending to bottom; Or,
Mode 2, a plurality of described independent reaction unit connect and compose a reaction component successively, described in being equipped with certainly between adjacent independent reaction unit in this reaction component, cut apart the top of dividing plate to the overflow ducts of the material stream passed for liquid of bottom extension, m group comprises the described reaction component described N level independent reaction in series unit of equal amts or different quantities independent reaction unit, and be assembled in the vacuum chamber of described tubular reactor body
When being provided with a plurality of described tubular reactor body, in at least one independent reaction unit in described N level independent reaction unit tubular reactor body located therein, while being provided with a plurality of independent reactions unit in a tubular reactor body, in a manner described 1 or mode 2 arrange.
5. reaction of guanosine device as claimed in claim 4, it is characterized in that: described in cut apart dividing plate downstream position be provided with over-pass, the height of described over-pass is a little more than the described height of cutting apart dividing plate, described in cut apart the passage that the inwall of dividing plate and over-pass and tubular reactor body surrounds and form described overflow ducts.
6. reaction of guanosine device as claimed in claim 4, it is characterized in that: described overflow ducts comprises the pipeline of material stream passed for liquid, the entrance of described pipeline is located at the top of cutting apart dividing plate, and described pipeline extends to the bottom of cutting apart dividing plate, and the position of pipe outlet is lower than the position of entrance.
7. reaction of guanosine device as claimed in claim 4, is characterized in that: described N level independent reaction is provided with stirring rake in unit, and described stirring rake is slurry formula, belt or frame,
Wherein, the set-up mode of described stirring rake is:
In aforesaid way 1, described stirring rake in described N level independent reaction unit is all located on same stir shaft, described stir shaft is through the dividing plates of cutting apart at different levels, and tubular reactor body is extended at two ends, and the two ends of stir shaft and tubular reactor body are tightly connected;
In aforesaid way 2, the described stirring rake in each independent reaction unit in described reaction component is all located on same stir shaft.
8. reaction of guanosine device as claimed in claim 7, is characterized in that: described stirring rake is spiral belt,
Wherein, the set-up mode of described stirring rake is:
In aforesaid way 1, described stirring rake in described N level independent reaction unit is all located on same stir shaft, described stir shaft is through the dividing plates of cutting apart at different levels, and tubular reactor body is extended at two ends, and the two ends of stir shaft and tubular reactor body are tightly connected;
In aforesaid way 2, the described stirring rake in each independent reaction unit in described reaction component is all located on same stir shaft.
9. reaction of guanosine device as claimed in claim 4, is characterized in that:
Described tubular reactor body is provided with chuck, is provided with heating agent path in described chuck, and the two ends of described heating agent path are provided with high temperature heating agent entrance and the outlet of low temperature heating agent.
10. reaction of guanosine device as claimed in claim 4, is characterized in that: a part for the vacuum chamber of described tubular reactor body is the gas space, and this gas space is provided with vacuum orifice.
11. reaction of guanosine devices as claimed in claim 4, is characterized in that: the cross section of described tubular reactor body is circle, rectangle, ellipse, lower-circle-square-shape and is that the oval middle part of part is any shape in rectangle up and down.
12. reaction of guanosine devices as claimed in claim 4, it is characterized in that: described tubular reactor body be provided with in thief hatch, temperature-measuring port, visor, vacuum orifice and manhole any or appoint severally, the below of described tubular reactor body is also provided with or is not provided with the bracing or strutting arrangement that supports described tubular reactor body.
13. reaction of guanosine devices as claimed in claim 12, it is characterized in that: when being provided with thief hatch, described thief hatch place is provided with a detector that automatically detects residual sugar amount in sample, this detector connects a controller, described mixing raw material ingress is provided with a raw material flow controller, raw material flow controller also connects this controller, the residual sugar amount concentration that this controller measures according to residual sugar amount detector, control raw material flow controller is worked, and enters into the speed of tubular reactor body to control mixing raw material.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110575804A (en) * | 2018-06-11 | 2019-12-17 | 中国石油化工股份有限公司 | Y-shaped molecular sieve heating type spiral reactor with stable structure |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110575804A (en) * | 2018-06-11 | 2019-12-17 | 中国石油化工股份有限公司 | Y-shaped molecular sieve heating type spiral reactor with stable structure |
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