CN201801525U - Complete set of equipment for producing crystalline fructose by adopting raw material of starch - Google Patents
Complete set of equipment for producing crystalline fructose by adopting raw material of starch Download PDFInfo
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- CN201801525U CN201801525U CN2010201928645U CN201020192864U CN201801525U CN 201801525 U CN201801525 U CN 201801525U CN 2010201928645 U CN2010201928645 U CN 2010201928645U CN 201020192864 U CN201020192864 U CN 201020192864U CN 201801525 U CN201801525 U CN 201801525U
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Abstract
The utility model relates to a complete set of equipment for producing crystalline fructose by adopting the raw material of starch, which comprises a biological reaction kettle, a circulating fluid bed bioreactor, a circulating membrane separation chemical reaction kettle and a circulating vacuum concentration crystallizer; the biological reaction kettle comprises a universal biological reaction kettle (44), a steam injection liquefier (45) and a high-pressure plunger pump (1) which are connected through a pipeline; the circulating fluid bed bioreactor takes a liquid storage pot (38) with two outlets (5 and 6) formed on both sides of the bottom as the center, and the two outlets are respectively connected with corresponding devices through a pipeline to form a vacuum concentration system and a fluid bed reaction system; the circulating membrane separation chemical reaction kettle comprises a chemical reaction kettle (33), an ultrafiltration membrane component (31), an ion-exchange duplex column (29), a liquid storage pot (27), a reverse osmosis membrane component (25) and high-pressure plunger pumps (11and 13) which are connected through pipelines, so as to form a circulating ultrafiltration system used for chemical reaction of solid-liquid separation; a circulating reverse osmosis system for heavy syrup is also formed; and a sandwich crystallizing rank (19), a high-pressure plunger pump (14) and a tubular heat exchanger (23) are connected through a pipeline to form a circulating vacuum concentration system.
Description
Technical field
The utility model relates to the suite of equipment that a kind of starch material is produced crystal diabetin.
Background technology
Existing starch material is produced the crystal diabetin technology and is mainly come from food engineering Dian Fentang Technology and processing unit: starch milk (size mixing jar)-steam ejection liquefaction (vapo(u)r blasting liquefier)-retort liquefaction (retort)-second spraying liquefaction-(vapo(u)r blasting liquefier)-flash cooling (water cooler)-advection liquefaction (laminar flow bed)-cooling (the water cooler)-PH adjusting of sizing mixing, saccharification (saccharification cylinder)-vacuum drum filters (drum filter)-heating, decolorizing with activated carbon (bleacher)-filtering under pressure (plate filter)-cooling (interchanger)-ion-exchange (ion exchange column)-concentrate (lifting/lowering film evaporator)-PH to regulate, isomery (isomery post fluidized-bed)-ion-exchange (ion exchange column)-chromatographic separation (simulation moving-bed)-vacuum-evaporation, decolorizing with activated carbon (bleacher)-filtering under pressure (plate filter)-ion-exchange (ion exchange column)-one time vacuum-evaporation (plate-type evaporator), secondary vacuum evaporation (scraper evaporator)-decrease temperature crystalline, centrifugation, dissolving, recrystallization (crystallizer, tripod pendulum type batch centrifugal)-dry (Vacuumdrier)-and packing technological processs such as (packaging production lines), it is long to show as technical process, the engineering structure complexity, problems such as technological equipment investment is big.General ten thousand tons of/grade production-line technique equipment manufacturing cost are about 4500-5000 is ten thousand yuan, and the investment of incompatibility medium-sized and small enterprises influences the popularization of crystal diabetin production technology.
Summary of the invention
The purpose of this utility model just provides the suite of equipment that a kind of starch material is produced crystal diabetin, be the industrial bio-transformation equipment that a kind of starch material based on biotechnology (the immobilization engineering of enzyme) and medication chemistry technology is produced crystal diabetin, to solve existing long, the problems such as engineering structure is complicated, processing unit cost height of crystal diabetin technical process.
The technical scheme that realizes above-mentioned purpose is:
Starch material is produced the suite of equipment of crystal diabetin by air tight cycle biological respinse still, the circulating fluidized bed bio-reactor, and 4 unit of circulation membrane sepn chemical reaction kettle and circulating vacuum condensing crystal jar are formed, wherein:
A air tight cycle biological respinse still is formed by general biological reactor, vapo(u)r blasting liquefier and the connection of high-pressure plunger pump pipeline, connecting mode is: biological respinse still outlet at bottom connects with the ram pump import, the ram pump outlet connects with the Jet liquefier opening for feed, the Jet liquefier jet orifice connects with one import of biological respinse still top, the pre-portion of biological respinse still is provided with an outlet and connects with the vacuum pump of suction steam, and the bottom is provided with a discharge port and connects with the automatic sludge discharge disk centrifugal machine inlet capable pipeline of separating impurity; Be used for that starch milk downgrades, cyclic spray liquefaction, enzymatic hydrolysis, impurity flocculation separation.
B circulating fluidized bed bio-reactor is the center with the container for storing liquid that a two bottom sides is provided with two outlets, by pipeline two outlets is connected with corresponding device respectively, constitutes a circulating vacuum concentration systems, a circulating fluidized bed reactive system; Specifically be that a side outlet connects with a high-pressure plunger pump inlet, the high-pressure plunger pump discharge connects with the tubular heat exchange import, the tubular heat exchange outlet connects with one import of container for storing liquid top, and the container for storing liquid top is provided with an outlet and connects with the vacuum pump of suction steam, constitutes the circulating vacuum concentration systems; The opposite side outlet connects with another high-pressure plunger pump inlet, and the high-pressure plunger pump discharge connects with isomerase post inlet pipeline, and the isomerase column outlet connects with another inlet pipeline of container for storing liquid top, constitutes the circulating fluidized bed reactive system; Successively operate two recycle systems and finish vacuum concentration and isomerization reaction.
C circulation membrane sepn chemical reaction kettle is made up of by pipe connection chemical reaction kettle, hyperfiltration membrane assembly, ion-exchange duplex post, container for storing liquid, reverse osmosis membrane assembly and high pressure plunger pump; The chemical reaction kettle outlet at bottom connects with the high-pressure plunger pump inlet, the high-pressure plunger pump discharge connects with aperture 1000-10000MD hyperfiltration membrane assembly import, the hyperfiltration membrane assembly outlet connects with one import of chemical reaction kettle top, is configured for " solid-liquid separation " loop ultrafiltration system of chemical reaction; See through the liquid outlet and connect with the import of ion-exchange duplex post, ion-exchange duplex column outlet connects with the container for storing liquid top inlet; The container for storing liquid outlet at bottom connects with another high-pressure plunger pump inlet; The high-pressure plunger pump discharge is installed a T-valve, and one logically connects with aperture 100-1000MD reverse osmosis membrane assembly import, and reverse osmosis membrane assembly exports and connects with one import of container for storing liquid top, is configured for the circulation reverse osmosis system of heavy syrup; Seeing through mouthful with the pre-portion of chemical reaction kettle import of reverse osmosis membrane assembly connects, and constitutes a chemical reaction clean cycle mechanism; One logical connects with the crystallizer top inlet again.
D circulating vacuum condensing crystal jar is made up of a minute interlayer crystallizer, high pressure plunger pump, tubular heat exchange pipe connection; The outlet at bottom of crystallizer connects with the high-pressure plunger pump inlet, the high-pressure plunger pump discharge connects with the tubular heat exchange import, the tubular heat exchange outlet connects with one import of crystallizer top, the crystallizer top is provided with an outlet and connects with suction steam-to-vacuum pump, promptly constitutes a circulating vacuum and concentrates the crystallisation by cooling system.Finish syrup vacuum concentration and crystallisation by cooling technology.The crystallizer bottom is provided with a discharge port and tripod pendulum type batch centrifugal UNICOM, is used to collect crystal.
Can manufacture the suite of equipment that starch material is produced crystal diabetin according to such scheme, produce the production line of crystal diabetin with its conduct with starch material.Positively effect is with immobilized enzyme and air tight cycle biological respinse still " one kettle way " biological respinse that combines; Simplified food engineering from the starch milk cooled starch sugar technical process of sizing mixing, changed one step of Dian Fentang technology, the one purified course of processing, biological respinse still and disk centrifugal separator have promptly substituted equipment such as the jar of sizing mixing, liquefied pot, advection jar, saccharification cylinder, bleacher, rotary drum filtration, filtering under pressure and multistage ion exchange column, have reduced investment.In circulating fluidized bed bio-reactor and circulating vacuum condensing crystal jar, be connected into high speed cycle heat exchange system with tubular heat exchange and high pressure plunger pump, the frame mode of the container for storing liquid that connects vacuum pump as evaporating vaporization chamber, main equipments such as alternative multistage lifting/lowering film evaporator, multistage plate-type evaporator and luwa evaporator, and heat-up time is short, can prevent the burnt fusion look of syrup.The traditional chemical separating technology is used for substituting expensive simulation moving-bed chiral separation technology with new and old combination of circulation membrane sepn chemical reaction kettle, also can reduce facility investment.Whole industrial bio-transformation complexes are used for starch material and produce crystal diabetin, have reduced investment of production equipment significantly, adapt to the medium-sized and small enterprises investment more.
Description of drawings
Fig. 1 is the suite of equipment formation synoptic diagram that starch material is produced crystal diabetin.
Embodiment
Below in conjunction with accompanying drawing, technical scheme is specified as embodiment.
Example one, equipment structure example: with reference to Fig. 1, the equipment formation is the bio-conversion process requirement according to the Starch Production crystal diabetin, is made up of four parts.
First part relates to the liquefaction of sizing mixing, hydrolysis reaction, flocculation reaction, centrifugation four procedures.By general biological reactor 44, vapo(u)r blasting liquefier 45 and high pressure plunger pump 1 usefulness pipeline and conduit coupling connection commonly used form, connecting mode is: biological respinse still outlet at bottom 47 connects with the ram pump import, the ram pump outlet connects by pipeline 46 with the Jet liquefier opening for feed, Jet liquefier 45 jet orifices connect with 44 tops, one import of biological respinse still, biological respinse still top is provided with an outlet and connects with the vacuum pump 43 of suction steam, the bottom is provided with a discharge port and connects with the automatic sludge discharge disk centrifugal separator 2 opening for feed pipelines 42 of separating impurity, produces purity greater than the refining glucose syrup of 90% light color.
Second section relates to vacuum concentration and isomerization reaction two big operations.The container for storing liquid 38 that two outlets are set with a two bottom sides is the center, by pipeline two outlets is connected with corresponding device respectively, constitutes a circulating vacuum concentration systems, a circulating fluidized bed reactive system.Specifically be that a side outlet 5 connects with high pressure plunger pump 3 imports, the high-pressure plunger pump discharge connects with tubular heat exchange 40 inlet pipelines 4, tubular heat exchange 40 outlets connect with container for storing liquid top one inlet pipeline 39, container for storing liquid 38 tops are provided with an outlet and connect with the vacuum pump 37 of suction steam, constitute the circulating vacuum concentration systems; Opposite side outlet 6 connects with another high pressure plunger pump 8 imports, and high pressure plunger pump 8 exports and connects with 7 imports of isomerase post, and another inlet pipeline 36 of isomerase column outlet and container for storing liquid top connects, formation circulating fluidized bed reactive system; The import of the crown center of container for storing liquid 38 connects with the outlet of disk centrifugal separator 2 by pipeline 41.Successively operate the circulating fluidized bed bio-reactor that two recycle systems are formed, finish vacuum concentration and isomerization reaction, obtain the F42-F45 high fructose syrup.
Third part is to constitute circulation membrane sepn chemical reaction kettle, makes the F94-F96 high fructose syrup.Form by pipe connection by chemical reaction kettle 33, hyperfiltration membrane assembly 31, ion-exchange duplex post 29, container for storing liquid 27, reverse osmosis membrane assembly 25 and two high pressure plunger pumps 11 and 13; Chemical reaction kettle outlet at bottom 9 connects with high pressure plunger pump 11 imports, high pressure plunger pump 11 outlets connect with aperture 1000-10000MD hyperfiltration membrane assembly 31 imports, hyperfiltration membrane assembly 31 outlets connect with one import 32 of chemical reaction kettle top, are configured for " solid-liquid separation " loop ultrafiltration system of chemical reaction; See through liquid and connected by pipeline 10 with ion-exchange duplex post 29 imports that are used for from handing over reaction, ion-exchange duplex column outlet connects with container for storing liquid top inlet 28 pipelines; Container for storing liquid outlet at bottom 12 connects with another high pressure plunger pump 13 imports; A T-valve is installed in these high pressure plunger pump 13 outlets, one logical connects with aperture 100-1000MD reverse osmosis membrane assembly 25 imports, reverse osmosis membrane assembly 25 outlets connect by pipeline 26 with one import of container for storing liquid top, are configured for the circulation reverse osmosis system of heavy syrup; Seeing through of reverse osmosis membrane assembly 25 mouthfuls 24 connects by pipeline 30 with one import of chemical reaction kettle top, constitutes a chemical reaction clean cycle mechanism; One logical is connected by pipeline 22 with the crystallizer top inlet again.
The 4th part is to obtain crystal diabetin by condensing crystal, finishes in circulating vacuum condensing crystal jar.By a minute interlayer crystallizer 19, vacuum pump 20, high pressure plunger pump 14, tubular heat exchange 23, pipe connection is formed circulating vacuum condensing crystal jar; The outlet at bottom 18 of crystallizer 19 connects with high pressure plunger pump 14 imports, high pressure plunger pump 14 outlets are connected by pipeline 15 with tubular heat exchange 23 imports, tubular heat exchange 23 outlets connect with crystallizer top one inlet pipeline 21, the crystallizer top is provided with an outlet and connects with the vacuum pump 20 of suction steam, promptly constitutes a circulating vacuum concentration systems.Finish syrup vacuum concentration and crystallisation by cooling technology.The crystallizer bottom is provided with a discharge port 17 and tripod pendulum type batch centrifugal 16 UNICOMs, is used to collect crystal.
Example two, production process embodiment: with reference to Fig. 1, producing crystal diabetin with the smart starch material of 200Kg potato is example.1, in 1000L biological respinse still 44, inject pure water 600L, turn on agitator, rotating speed is chosen in the 100-150 rev/min of scope.Claimed potato smart starch 200kg, dropped in the biological respinse still, continued to stir from manhole.1 circulation of opening plunger pump, flow 20L/min.Open steam liquefaction injector 45, air pressure 1kg, cyclic spray 1h opens vacuum pump 43, can be observed the starch milk of even gelatinization.Stop plunger pump, injector work, lasting stirring is cooled to 60C.Close vacuum pump, open manhole and drop into liquid particulate immobilization diastase, saccharifying enzyme 300ml, constant temperature stirs 16h.Stop to stir, 4h is left standstill in insulation.Can be observed light-transmissive fluid and flocculent substance.Open disk centrifugal separator 2, speed-raising 5min imports reaction solution, gets light glucose syrup clear liquor 500L, purity 92%, concentration 35%, calculation of starch transformation efficiency 80%.
2, in 1000L container for storing liquid 38, inject glucose syrup clear liquor 500L, tubular heat exchange 40 logical steam heating, steam flow rate 300L/min, container for storing liquid vacuumizes, vacuum is pressed 0.5kg, starts ram pump 3 pulling glucose syrups cycle heat exchange between interchanger and container for storing liquid, flow 20L/min.Sampling in per 10 minutes is observed, and concentration determination stopped ram pump by 50% o'clock, stops steam.When reducing to 60c, temperature stops vacuum pump.Drip saturated solution of magnesium sulfate 10ml, start another ram pump 8 pulling glucose syrups and between isomery post 7 and container for storing liquid 38, circulate.Sampling in per 30 minutes is observed, and gets 50% concentration F42 high fructose syrup 350L.
3, F42 high fructose syrup 350L is moved into chemical reaction kettle 33, the logical steam procedures of interlayer is warming up to 70c, starts agitator 34, and rotating speed is adjusted to 100 commentaries on classics/min, drips 20% inorganic calcium A solution to PH8-9, time 1h.Can be observed syrup by the variation of muddiness, stop to stir to suspendible.Start ram pump 11 loop ultrafiltrations; suspension concentration reaches at 70% o'clock and starts the reverse osmosis system moisturizing; dual system is all kept the circular flow of 10L/min, and the inspection by sampling glucose content was shut down less than 1% o'clock from chemical reaction kettle 33, emitted the glucose syrup in the reverse osmosis container for storing liquid.Restart chemical reaction kettle, temperature programming is to 70c, and mixing speed is adjusted to 100 commentaries on classics/min, drips 15% inorganic sodium solution to PH8-9, time 1h.Can be observed inorganic calcium B white particles suspension, stop to stir.Start ram pump 11 loop ultrafiltrations; suspension concentration reaches at 70% o'clock and starts the reverse osmosis system moisturizing; dual system is all kept the circular flow of 10L/min; inspection by sampling fructose sodium content was shut down less than 1% o'clock from chemical reaction kettle; from the reverse osmosis storage tank sampling detect the fructose sodium solution of 96% purity, solid yield 92%.Fructose sodium solution is imported ion exchange column 29, get the 2BV purified rinse water, get translucent F96 high fructose syrup 835L.
4, F96 high fructose syrup 835L is moved into crystallizer 19.Tubular heat exchange 23 logical steam heating, steam flow rate 300L/min, crystallizer vacuumizes, and vacuum is pressed 0.5kg, and startup ram pump 14 pulling glucose syrups circulate between tubular heat exchange 23 and crystallizer 19 and concentrate flow 20L/min.Every 10min sampling detects syrup concentration and degree of supersaturation, syrup concentration 80%, and degree of supersaturation is 1 o'clock, stops tubulation heating and syrup circulation.Following interlayer feeds steam, and vacuum pump 20 continues to vacuumize, and adds bio-surfactant 1352mg, starts agitator 60-80 commentaries on classics/min and continues to stir.Every 10min sampling detects syrup concentration, syrup concentration 90%, or stop the interlayer heating when manifesting caramel colour, stop vacuum pump 20 work.Last interlayer feeds the circulating water cooling, and continue to stir Dropwise 5 0% dehydrated alcohol down: the crystal seed suspension is to 10% of the heavy syrup total amount.Stop to stir growing the grain, adjusting interlayer circulating condensing water flow velocity control cooling rate is 2c/h, leaves standstill the 16h crystallization.Crystal and mother liquor are emitted in unlatching crystallizer bottom valve outlet 17, start tripod pendulum type batch centrifugal 16 and dry, and wash crystal with raw spirit, clean surperficial caramel colorant, get translucent granulated sugar sample crystallization 135kg, and calculated yield is 67.5%.
Claims (1)
1. starch material is produced the suite of equipment of crystal diabetin, by air tight cycle biological respinse still, and the circulating fluidized bed bio-reactor, 4 unit of circulation membrane sepn chemical reaction kettle and circulating vacuum condensing crystal jar are formed, and it is characterized in that:
A air tight cycle biological respinse still is by general biological reactor (44), vapo(u)r blasting liquefier (45) and high pressure plunger pump (1) form with the pipeline connection, connecting mode is: biological respinse still outlet at bottom (47) connects with ram pump (1) import, ram pump (1) outlet connects with Jet liquefier (45) opening for feed, the Jet liquefier jet orifice connects with one import of biological respinse still top, biological respinse still (44) top is provided with an outlet and connects with the vacuum pump (43) of suction steam, and the bottom is provided with a discharge port and connects with automatic sludge discharge disk centrifugal separator (2) the opening for feed pipeline (42) of separating impurity;
B circulating fluidized bed bio-reactor is the center with the container for storing liquid (38) that a two bottom sides is provided with two outlets (5,6), by pipeline two outlets is connected with corresponding device respectively, constitutes a circulating vacuum concentration systems, a circulating fluidized bed reactive system; Specifically be that a side outlet (5) connects with a high pressure plunger pump (3) import, high pressure plunger pump (3) outlet connects with tubular heat exchange (40) import, tubular heat exchange (40) outlet connects with container for storing liquid (38) top one import, container for storing liquid (38) top is provided with an outlet and connects with the vacuum pump (37) of suction steam, constitutes the circulating vacuum concentration systems; Opposite side outlet (6) connects with another high pressure plunger pump (8) import, high pressure plunger pump (8) outlet connects with isomerase post (7) inlet pipeline, isomerase post (7) outlet connects with container for storing liquid (38) another inlet pipeline of top (36), constitutes the circulating fluidized bed reactive system;
C circulation membrane sepn chemical reaction kettle is made up of by pipe connection chemical reaction kettle (33), hyperfiltration membrane assembly (31), ion-exchange duplex post (29), container for storing liquid (27), reverse osmosis membrane assembly (25) and high pressure plunger pump (11,13); Chemical reaction kettle (33) outlet at bottom (9) connects with high pressure plunger pump (11) import, high pressure plunger pump (11) outlet connects with aperture 1000-10000MD hyperfiltration membrane assembly (31) import, hyperfiltration membrane assembly (31) outlet connects with chemical reaction kettle (33) top one import (32), is configured for " solid-liquid separation " loop ultrafiltration system of chemical reaction; See through the liquid outlet and connect with ion-exchange duplex post (29) import, ion-exchange duplex post (29) outlet connects with container for storing liquid (27) top inlet; Container for storing liquid (27) outlet at bottom (12) connects with another high pressure plunger pump (13) import; A T-valve is installed in high pressure plunger pump (13) outlet, one logical connects with aperture 100-1000MD reverse osmosis membrane assembly (25) import, reverse osmosis membrane assembly (25) outlet connects with container for storing liquid (27) top one import, is configured for the circulation reverse osmosis system of heavy syrup; See through mouthful (24) of reverse osmosis membrane assembly (25) connect with chemical reaction kettle (33) top inlet, constitute a chemical reaction clean cycle mechanism; One logical connects with crystallizer (19) top inlet again;
D circulating vacuum condensing crystal jar is made up of a minute interlayer crystallizer (19), high pressure plunger pump (14), tubular heat exchange (23) pipe connection; The outlet at bottom of crystallizer (18) connects with high pressure plunger pump (14) import, high pressure plunger pump (14) outlet connects with tubular heat exchange (23) import, tubular heat exchange (23) outlet connects with crystallizer (19) top one import, crystallizer (19) top is provided with an outlet and connects with suction steam-to-vacuum pump (20), promptly constitutes a circulating vacuum and concentrates the crystallisation by cooling system.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2010201928645U CN201801525U (en) | 2010-05-14 | 2010-05-14 | Complete set of equipment for producing crystalline fructose by adopting raw material of starch |
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| Application Number | Priority Date | Filing Date | Title |
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| CN2010201928645U CN201801525U (en) | 2010-05-14 | 2010-05-14 | Complete set of equipment for producing crystalline fructose by adopting raw material of starch |
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| CN201801525U true CN201801525U (en) | 2011-04-20 |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102337316A (en) * | 2011-09-30 | 2012-02-01 | 广州双桥股份有限公司 | Process for producing starch sugar |
| CN110387391A (en) * | 2018-04-23 | 2019-10-29 | 诺瓦塞普工艺公司 | By the method for glucose production fructose |
| CN112210493A (en) * | 2020-09-17 | 2021-01-12 | 北京劢克机械工程有限公司 | Ultrahigh maltose syrup production system and preparation method thereof |
| US11661635B2 (en) | 2018-04-23 | 2023-05-30 | Novasep Process Solutions | Fructose purification method |
| US11987853B2 (en) | 2018-04-23 | 2024-05-21 | Novasep Process Solutions | Method for chromatographic purification of viscous loads |
-
2010
- 2010-05-14 CN CN2010201928645U patent/CN201801525U/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102337316A (en) * | 2011-09-30 | 2012-02-01 | 广州双桥股份有限公司 | Process for producing starch sugar |
| CN102337316B (en) * | 2011-09-30 | 2013-07-31 | 广州双桥股份有限公司 | Process for producing starch sugar |
| CN110387391A (en) * | 2018-04-23 | 2019-10-29 | 诺瓦塞普工艺公司 | By the method for glucose production fructose |
| US11661635B2 (en) | 2018-04-23 | 2023-05-30 | Novasep Process Solutions | Fructose purification method |
| CN110387391B (en) * | 2018-04-23 | 2023-08-04 | 诺瓦塞普工艺处理公司 | Method for producing fructose from glucose |
| US11987853B2 (en) | 2018-04-23 | 2024-05-21 | Novasep Process Solutions | Method for chromatographic purification of viscous loads |
| CN112210493A (en) * | 2020-09-17 | 2021-01-12 | 北京劢克机械工程有限公司 | Ultrahigh maltose syrup production system and preparation method thereof |
| CN112210493B (en) * | 2020-09-17 | 2022-10-18 | 北京劢克机械工程有限公司 | Ultrahigh maltose syrup production system and preparation method thereof |
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Granted publication date: 20110420 Termination date: 20120514 |