CN102839201B - Production method of oral-level fructose sodium diphosphate - Google Patents
Production method of oral-level fructose sodium diphosphate Download PDFInfo
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Abstract
The invention relates to a production method of an oral-level fructose sodium diphosphate, which is performed according to the flows of enzyme reaction, filtering, cation exchange, anion exchange, impurity removal, eluting, concentrating, decolorizing, crystallizing, solid-liquid separation, washing, drying, screening and packaging, in particular, wherein solid-liquid separation, washing and drying are performed in the same vacuum rotary dryer, the vacuum rotary dryer comprises a frame, a tank body, a motor, a drying device and a vacuumizing device, the tank body can be rotatably arranged on the frame, the vacuumizing device comprises a vacuumizing pipe and a vacuum pump, and the vacuum dryer also comprises a filter gauze arranged in the tank body and used for carrying out solid-liquid separation, a filtrate container located below the filter gauze, a filtrate discharge pipe communicated with the filtrate container and used for discharging filtrate in the filtrate container and a vacuum filter arranged at the filtrate outlet of the filtrate container. By adopting the method, the labor intensity of the production personnel is reduced, the production efficiency is improved, the production cost is lowered and the product quality is good.
Description
Technical field
The present invention relates to a kind of production method of oral level Fructose Diphosphate.
Background technology
Fructose Diphosphate (FDP), molecular formula: C
6h
11o
12p
2na
38H
2o, chemical structural formula is as follows:
Fructose Diphosphate is white or off-white color crystalline powder, and micro-have a special smell, distinguishes the flavor of micro-salty, easily molten in water, almost insoluble in ether, ethanol or acetone.
Fructose Diphosphate is the cell metabolite be present in human body, can regulate the activity of plurality of enzymes system in glucose metabolism.It is reported, ectogenic Fructose Diphosphate, can be by the activity of activating phosphatase fructokinase and pyruvate kinase, the concentration of the interior Triphosaden of cell and phosphocreatine is increased, promote stream in potassium ion, be of value to the energy metabolism of cell under ischemic, anoxic condition and the utilization of glucose, thereby make ischemic myocardium alleviate damage.Therefore, Fructose Diphosphate can be used for the assisting therapy of myocardial ischemia, stenocardia, cerebral infarction.
At present, the production of oral preparation Fructose Diphosphate is undertaken by the flow process of enzyme reaction → filtration → cationic exchange → anionresin → impurity elimination → wash-out → concentrated → decolouring → crystallization → solid-liquid separation → washing → drying → sieve → pack.Be subject to the restriction (only possessing functions/drying) of existing drying machine, described solid-liquid separation step, washing step and drying step can only substep subset operations, have that labor strength is large, production efficiency is low, equipment cost is high, energy consumption is large and product easily because of ingress of air with extraneous degradation deficiency under the qualities such as rotten or introducing impurity occurs.
Summary of the invention
Technical problem to be solved by this invention is to overcome the deficiencies in the prior art, and a kind of production method of improved oral level Fructose Diphosphate is provided.
For solving above technical problem, the present invention adopts following technical scheme:
A kind of production method of oral level Fructose Diphosphate, its flow process by enzyme reaction → filtration → cationic exchange → anionresin → impurity elimination → wash-out → concentrated → decolouring → crystallization → solid-liquid separation → washing → drying → sieve → pack is carried out, particularly, described solid-liquid separation, washing and drying step carry out in same vacuum rotary shelf drier, described vacuum rotary shelf drier comprises frame, have into, the tank body of discharge port, for the motor that drives tank body to rotate, drying installation, the vacuum extractor be connected with tank body, described tank body can be arranged on frame rotationally, and the rotational axis line of tank body is consistent with horizontal direction, described vacuum extractor comprises that an end stretches into the vacuum-pumping tube in tank body, vacuum pump, described Vacuumdrier also comprises and being arranged in tank body for carrying out the filter screen of solid-liquid separation, be positioned at the filtrate container of filter screen below, be communicated with the filtrate discharge pipe for the filtrate in it is discharged with filtrate container, be arranged on the vacuum filter at the filtrate outlet place of filtrate container.
According to a concrete and preferred aspect of the present invention, described drying installation comprises that to be arranged on tank body outer for the chuck of logical heating medium, for pass into HAI Heated Air Intake pipe and the warm air feeding mechanism that adds warm air in tank body.
Preferably, described vacuum rotary shelf drier also includes temperature monitor and the pressure detecting instrument for detecting respectively temperature and pressure in tank body.
According to further embodiment of the present invention: in weight part, the composition of raw materials of described enzyme reaction comprises: 1800～2200 parts of purified water; 45～55 parts, sodium hydroxide; 35～145 parts of 85wt% phosphatase 11s; 20～25 parts, sodium carbonate; 380～420 parts of glucose; 6～12 parts, magnesium chloride; 3～6 parts of ammonium chlorides; 3～5 parts, Repone K; 950～1100 parts of fresh yeast; 40～60 parts of toluene.
Preferably, in weight part, the composition of raw materials of described enzyme reaction comprises: 1900～2100 parts, water; 48～52 parts, sodium hydroxide; 38～142 parts of 85wt% phosphatase 11s; 22～24 parts, sodium carbonate; 390～410 parts of glucose; 8～10 parts, magnesium chloride; 4～6 parts of ammonium chlorides; 3～5 parts, Repone K; 950～1050 parts of fresh yeast; 45～55 parts of toluene.
According to a concrete aspect, described enzyme reaction specifically is implemented as follows: add purified water in retort, open and stir, add sodium hydroxide, until completely dissolved, add phosphatase reaction, treat that temperature is down to below 50 ℃, add successively sodium carbonate, glucose, magnesium chloride, ammonium chloride, Repone K, be stirred to dissolve, add again fresh yeast, toluene, finally with sodium carbonate, regulate the pH value of mixed solution between 6.00～6.15, heat up, temperature is controlled at 35 ℃～36 ℃, react 3～4 hours, after the survey content of inorganic phosphorus is less than 0.6wt%, add excessive hydrochloric acid, react after 15～25 minutes, add sodium hydroxide to regulate pH to 5.6～5.8.Enzyme reaction adds super-cell after stopping, and filter press, after stoste is filtered, filters the washing precipitation material by purified water.
Described according to a further preferred aspect of the invention, cationic exchange adopts 732 resin cation (R.C.)s, and anionresin adopts 717 anionite-exchange resin.
Preferably, described drying temperature is 38 ℃～42 ℃.While carrying out drying, described vacuum rotary type drying
Vacuum tightness in the tank body of machine preferably is controlled at-below 0.09MPa.
Owing to adopting above technical scheme, the present invention compared with prior art has following advantage:
The vacuum rotary shelf drier that the present invention adopts, can make solid-liquid separation, washing and the drying of minute multistep operation of existing needs complete in an equipment, not only reduced producers' labour intensity, improved production efficiency, reduced production cost, more can reduce the chance that Fructose Diphosphate contacts with external environment, guarantee product quality.
The accompanying drawing explanation
Below in conjunction with accompanying drawing and specific embodiment, invention is further described in detail:
The main cross-sectional schematic of the vacuum rotary shelf drier that Fig. 1 is the inventive method employing;
The structure enlarged diagram that Fig. 2 is hot water entrance place in Fig. 1;
The structure enlarged diagram that Fig. 3 is the vacuum extractor in the tank body outside in Fig. 1;
The structure enlarged diagram that Fig. 4 is the vacuum filter in the tank body inboard in Fig. 1;
Wherein: 1, frame; 2, tank body; 20, opening for feed, discharge port; 21, Butterworth Hatch; 3, motor; 4, vacuum extractor; 40, vacuum-pumping tube; 400, dry vacuum interface; 41, liquid-inlet pipe; 5, filter screen; 6, filtrate container; 7, delivery pipe; 8, vacuum filter; 9, chuck; 90, import; 91, outlet; 10, inlet pipe; 11, capping; 110, service ports; 12, temperature monitor; 13, pressure detecting instrument; 14, retaining cover.
Embodiment
Below in conjunction with specific embodiment, technical scheme of the present invention is further described, but the present invention should not only limit to these embodiment.
Embodiment 1
The vacuum rotary shelf drier that the present embodiment provides a kind of the inventive method to use.As shown in Figures 1 to 4, the vacuum rotary shelf drier comprises frame 1; Tank body 2 with charging and discharging mouth 20, tank body 2 can be arranged on frame 1 rotationally, and its rotational axis line is consistent with horizontal direction; For the variable-frequency motor 3 that drives tank body 2 to rotate; The vacuum extractor 4 be connected with tank body 2; Drying installation for dry tank body 2 interior materials; Wherein vacuum extractor 4 comprises that an end stretches into vacuum-pumping tube 40, the vacuum pump in tank body 2; Be arranged in tank body 2 for the filter screen 5 that carries out solid-liquid separation, the filtrate container 6 that is positioned at filter screen 5 belows, be communicated with filtrate discharge pipe 7 for the discharge of the filtrate by it with filtrate container 6, be arranged on the vacuum filter 8 at the filtrate outlet place of filtrate container 6.
Drying machine in the present embodiment, drying installation comprises that to be arranged on tank body 2 outer for the chuck 9 of logical heating medium, for pass into HAI Heated Air Intake pipe 10 and the warm air feeding mechanism that adds warm air in tank body 2, on the one hand heating medium is passed in chuck 9, heat transmission is carried out in tank body 2 surfaces, and then by heat with separate after solid substances contact, thereby realize the drying of material; On the other hand, will add warm air by the warm air feeding mechanism and pass in tank body 2 from inlet pipe 10, contact and heat exchange with solid substances, steam is extracted out from vacuum-pumping tube, therefore, two aspects carry out the material in tank body 2 is carried out to drying simultaneously, improve the drying efficiency of drying machine.Vacuum extractor 4 in the present embodiment also has the scavenging solution liquid-inlet pipe 41 be communicated with vacuum-pumping tube 40, prevent the filtrate of vacuum filter 8, fail all from filtrate discharge pipe 7, to discharge, residual in the interior formation of vacuum-pumping tube 40, the work-ing life of reducing vacuum extractor 4.Vacuum rotary shelf drier in the present embodiment also is included in capping 11, temperature monitor 12 and the pressure detecting instrument 13 for detecting respectively tank body 2 interior temperature and pressures of charging and discharging mouth 20 tops, wherein capping 11 is provided with service ports 110, for accident, the serviceman is entered in tank body 2 by service ports 110, keep in repair very convenient, simultaneous temperature detector 12 and pressure detecting instrument 13 detect the dry environment in tank body 2 interior materials, thereby the roughly degree of drying of judgement tank body 2 interior materials that can be preliminary, provide reference to the sampling of material.
Drying machine in use, directly the solid-liquid crystalline mixture is advanced from material, outlet 20 is pressed in tank body 2, by filter screen 5 by solid-liquid separation, solid-state material after separation has been stayed in tank body 2, liquid material flows in filtrate container 6, now, under the effect of vacuum filter 8, filtrate in filtrate container 6 is discharged from the filtrate discharge pipe, after separating end, can be pressed into alcohol the crystal in tank body is carried out to drip washing, wash material complete, open variable-frequency motor 3 and drive tank body 2 slow circumvolves, and heated by 9 pairs of materials of chuck, material is constantly mixed, uniform drying, further accelerate the rate of drying of material, to add warm air by the warm air feeding mechanism passes in tank body 2 from inlet pipe 10 simultaneously, with solid substances, contact and heat exchange, the interior steam of tank body 2 is discharged from the dry vacuum interface 400 of vacuum-pumping tube 40, therefore, adopt the time of the present embodiment drying machine dried material to shorten dramatically, the residence time of material in tank body 2 also shortens dramatically, with the rake type drier that there is multi-disc rake wing in tank body 2, compare, also significantly minimizing of the chance of collision mutually between granular material, thereby original shape of material substantially can be not destroyed, meanwhile, filter screen 5 and filtrate container 6 have been set up in tank body 2, filtrate discharge pipe 7 and the vacuum filter 8 that is arranged on the filtrate outlet place of filtrate container 6, by filter screen 5 by the material solid-liquid separation, and under vacuum filter 8 effects, filtrate self-discharging pipe 7 is discharged, utilize the drying installation of drying machine simultaneously, solid substances after separating is carried out to drying, and the separation of material and drying are all to carry out in tank body 2, prevented that material from contacting with air, Working environment and the quality that has improved material have been protected, reduced producers' labour intensity simultaneously, reduce production costs.
Embodiment 2
The present embodiment provides a kind of production method of oral level Fructose Diphosphate, specific as follows:
(1) enzyme reaction:
1. enzyme reaction composition of raw materials:
2000 kilograms, water; 23 kilograms, sodium carbonate; (85%) 140 kilogram of phosphoric acid; 50 kilograms, sodium hydroxide; 400 kilograms of glucose; 9 kilograms, magnesium chloride; 5 kilograms of ammonium chlorides; 4 kilograms, Repone K; 1000 kilograms of fresh yeasts; 50 kilograms of toluene.
2. operating process
Get the raw materials ready: get required supplementary material on duty from the supplementary material storehouse by batch production ordering, check the supplementary material outer packaging tight, without damaged, by the supplementary material block pattern row pattern in reaction workshop section.
Reaction: according to batch production ordering, add purified water 2000Kg in retort, open and stir, add phosphoric acid (85%) reaction after adding sodium hydroxide that it is dissolved fully, when temperature is down to 50 ℃ of left and right, add successively soda ash, glucose, magnesium chloride, ammonium chloride, Repone K to be stirred to dissolve, then add fresh yeast, toluene.(finally with soda ash, regulate the pH value of mixed solution, make the pH value between 6.00～6.15.) heat up, temperature is controlled at 35～36 ℃, after reaction 3.5hr, surveys after inorganic phosphorus is less than 0.6% and gets final product termination reaction.
Termination reaction: add hydrochloric acid 53L in reaction solution, react 20 minutes back end hydrogenation sodium oxide 20kg, survey pH between 5.6～5.8.
(2) filter: enzyme reaction adds super-cell 80kg after stopping, filter press, and stoste was filtered after 40 minutes, with purified water 4T, filtered, and washed sedimentable matter.
(3) cationic exchange and anionresin
1. resin model: 732 resin cation (R.C.)s and 717 resin anion(R.A)s;
Wash assorted liquid formula: every liter containing analytical pure ammonium chloride 1.5g, strong aqua 2.5ml.
Pickle solution formula: the hydrochloric acid of 0.015N (analytical pure)
The elutriant formula: every liter containing refined salt 88g, analytical pure hydrochloric acid 9.6ml.
2. operating process
Resin regeneration: first, with the pressurized air resin that recoils, make it loose.Open again hydrochloric acid pump and bottom acid inlet valve, by the hydrochloric acid of the 1.5N of resin volume doubling dose in the displacement pile of column bottom, to the amount of process stipulation.Close the bottom acid inlet valve, the open top part acid inlet valve stops into acid when acid adds to the upper visor of post, the regeneration activating resin, and during regeneration, the flow rate control of hydrochloric acid completed in 2～3 hours.After advancing the acid end, open residue hydrochloric acid in the compressed air valve goalkeeper post of top and discharge outside post.Carry out the resin recoil by purified water again.Close the bottom water intaking valve after breaking up, simultaneously, open top water intaking valve and bottom blow-down valve and just wash, when extremely neutral with pH detection paper discharge water from the sewage draining exit sampling, stand-by.
Upper prop: reaction filtrate is diluted (being diluted to pol 1.0-3.0) by purified water, then upper prop absorption, the advanced positive post of filtrate, laggard cloudy post.Coutroi velocity during upper prop (effluent liquid ethanol detection method), the whole upper prop time was controlled at about 22～26 hours.After finishing, upper prop rinses cloudy post by 2000L left and right purified water quick (by-pass valve control is opened to maximum).
Impurity elimination: (every liter containing analytical pure ammonium chloride 1.5g, strong aqua 2.5ml to prepare the assorted liquid of washing of some amount (about 18000L) by purified water.), will wash the assorted liquid cloudy post of at the uniform velocity flowing through, flow velocity is 1000L/ hour, until the pH of last effluent liquid is neutrality.
Pickling: hydrochloric acid (analytical pure) the solution 4000L of preparation 0.015N makes it to pass through fast cloudy post.
Wash-out: (every liter containing refined salt 88g to prepare the elutriant of some amount (about 4500L) by purified water, analytical pure hydrochloric acid 9.6ml), eluent stream is through cloudy post, and coutroi velocity 500L/ hour, start when effluent liquid has FDP to collect until detect effluent liquid without FDP.
(4) concentrated
Adopt scraper plate film vacuum vaporizer, elutriant is concentrated by scraper-type film vacuum vaporizer.Concentrated vacuum tightness requires :-0.098Mpa.The concentrate feed liquid temp is no more than 45 ℃.Concentrated solution concentration 40%.
(5) decolouring
Adopt filtering machine with horizontal blade, concentrated solution is regulated to pH value to 5.2 left and right, add 10 kilograms of activated carbon for 767 pins in concentrated solution, stir 1 hour, then 320 order press filtrations (pressure≤0.5MPa).Adding again 10 kilogram of 767 pin activated carbon in destainer for the first time, to stir 1 hour, 320 order press filtrations, obtain destainer (as still coloured amount that increases activated carbon or decolouring number of times).
(6) crystallization
Wash hetero-ion: destainer is pumped into and washes in the hetero-ion tank, open and stir, slowly add 95% ethanol (in mixed solution, final ethanol content is 67%) of 2.5 times of amounts of about destainer, add rear continuation and stir 30 minutes, make FDP become syrup to separate out.Then close stirring, within standing 1 hour, make the syrup layering, emit syrup to the syrup storage tank, bleed off waste alcohol; To the purified water that adds 1 times of amount of syrup volume in the syrup storage tank, it is 5.0 left and right that 6mol/L hydrochloric acid is adjusted pH, and this syrup solution blowback is washed in the hetero-ion tank again.Repeat twice of aforesaid operations.
Crystallization: get syrup 150L, after the filter element filtering of 0.45 μ m, 0.22 μ m, pump in crystallizer respectively.Slowly add 95% ethanol, make in tank final alcohol concn in 72% left and right.Add crystal seed 500g, stir the 4hr post crystallization and separate out, continue to stir 30 minutes.In crystallisation process, mixing speed is controlled at 25Hz, and temperature is controlled at 28～29 ℃.
(7) solid-liquid separation, washing and drying
Solidliquid mixture after crystallization is put into to the described vacuum rotary shelf drier of embodiment 1, separated, washed and drying, after wherein separating, the ethanol drip washing with 75% two times, chlorine detection ion qualified (≤0.03%) after getting wet-milling after drip washing and drying, enter the vacuum-drying state.Vacuum degree control-below 0.090Mpa, the moisture eliminator operating frequency is controlled at 21Hz, drying temperature is controlled at 40 ± 2 ℃, sampling stops after detecting moisture content qualified (moisture content should be 24.0%～27.0%).
(8) sieve, pack
Dried product is crossed 30 mesh sieves.Product after sieving is packed in the medicinal plastics bag of double-layer polyethylene, 25 kilograms of every bag of net weight.Put between transfer to be testedly, the Fructose Diphosphate work in-process that are up to the standards are packed in fiber can, cover lid, the label that will be printed on lot identification mark, date manufactured, validity period and net weight is affixed on fiber can, and custody for account of customers is to be checked.Warehousing after passing.
Above-described embodiment is only explanation technical conceive of the present invention and characteristics; its purpose is to allow the person skilled in the art can understand content of the present invention and implement according to this; can not limit the scope of the invention with this; all equivalences that spirit is done according to the present invention change or modify, within all should being encompassed in protection scope of the present invention.
Claims (8)
1. the production method of an oral level Fructose Diphosphate, its flow process by enzyme reaction → filtration → cationic exchange → anionresin → impurity elimination → wash-out → concentrated → decolouring → crystallization → solid-liquid separation → washing → drying → sieve → pack is carried out, it is characterized in that: described solid-liquid separation, washing and drying step carry out in same vacuum rotary shelf drier, described vacuum rotary shelf drier comprises frame, have into, the tank body of discharge port, for the motor that drives tank body to rotate, drying installation, the vacuum extractor be connected with tank body, described tank body can be arranged on frame rotationally, and the rotational axis line of tank body is consistent with horizontal direction, described vacuum extractor comprises that an end stretches into the vacuum-pumping tube in tank body, vacuum pump, the scavenging solution liquid-inlet pipe be communicated with described vacuum-pumping tube, described drying installation comprises and is arranged on the outer chuck for logical heating medium of described tank body, for in tank body, passing into HAI Heated Air Intake pipe and the warm air feeding mechanism that adds warm air, described Vacuumdrier also comprises and being arranged in tank body for carrying out the filter screen of solid-liquid separation, be positioned at the filtrate container of filter screen below, be communicated with the filtrate discharge pipe for the filtrate in it is discharged with filtrate container, be arranged on the vacuum filter at the filtrate outlet place of filtrate container, for detecting respectively temperature monitor and the pressure detecting instrument of temperature and pressure in tank body,
Drying machine in use, directly by the solid-liquid crystalline mixture from advancing, discharge port is pressed in tank body, by filter screen by solid-liquid separation, solid-state material after separation has been stayed in tank body, liquid material flows in filtrate container, now, under the effect of vacuum filter, filtrate in filtrate container is discharged from the filtrate discharge pipe, after separating end, be pressed into alcohol the crystal in tank body is carried out to drip washing, wash material complete, open motor and drive the tank body slow circumvolve, and by chuck, material is heated, material is constantly mixed, uniform drying, further accelerate the rate of drying of material, to add warm air by the warm air feeding mechanism passes in tank body from inlet pipe simultaneously, with solid substances, contact and heat exchange, steam in tank body is discharged from the dry vacuum interface of vacuum-pumping tube.
2. the production method of oral level Fructose Diphosphate according to claim 1, it is characterized in that: in weight part, the composition of raw materials of described enzyme reaction comprises: 1800 ~ 2200 parts of purified water; 45 ~ 55 parts, sodium hydroxide; 35 ~ 145 parts of 85wt% phosphatase 11s; 20 ~ 25 parts, sodium carbonate; 380 ~ 420 parts of glucose; 6 ~ 12 parts, magnesium chloride; 3 ~ 6 parts of ammonium chlorides; 3 ~ 5 parts, Repone K; 950 ~ 1100 parts of fresh yeast; 40 ~ 60 parts of toluene.
3. the production method of oral level Fructose Diphosphate according to claim 2, it is characterized in that: in weight part, the composition of raw materials of described enzyme reaction comprises: 1900 ~ 2100 parts, water; 48 ~ 52 parts, sodium hydroxide; 38 ~ 142 parts of 85wt% phosphatase 11s; 22 ~ 24 parts, sodium carbonate; 390 ~ 410 parts of glucose; 8 ~ 10 parts, magnesium chloride; 4 ~ 6 parts of ammonium chlorides; 3 ~ 5 parts, Repone K; 950 ~ 1050 parts of fresh yeast; 45 ~ 55 parts of toluene.
4. according to the production method of the described oral level Fructose Diphosphate of claim 2 or 3, it is characterized in that: described enzyme reaction specifically is implemented as follows: add purified water in retort, open and stir, add sodium hydroxide, until completely dissolved, add phosphatase reaction, treat that temperature is down to below 50 ℃, add successively sodium carbonate, glucose, magnesium chloride, ammonium chloride, Repone K, be stirred to dissolve, add again fresh yeast, toluene, finally with sodium carbonate, regulate the pH value of mixed solution between 6.00 ~ 6.15, heat up, temperature is controlled at 35 ℃ ~ 36 ℃, react 3 ~ 4 hours, after the survey content of inorganic phosphorus is less than 0.6wt%, add excessive hydrochloric acid, react after 15 ~ 25 minutes, add sodium hydroxide to regulate pH to 5.6 ~ 5.8.
5. the production method of oral level Fructose Diphosphate according to claim 4, it is characterized in that: enzyme reaction adds super-cell after stopping, and filter press, after stoste is filtered, filters the washing precipitation material by purified water.
6. the production method of oral level Fructose Diphosphate according to claim 1, it is characterized in that: described cationic exchange adopts 732 resin cation (R.C.)s, and described anionresin adopts 717 anionite-exchange resin.
7. the production method of oral level Fructose Diphosphate according to claim 1, it is characterized in that: described drying temperature is 38 ℃ ~ 42 ℃.
8. according to the production method of the described oral level Fructose Diphosphate of claim 1 or 7, it is characterized in that: while carrying out drying, the vacuum degree control in the tank body of described vacuum rotary shelf drier-below 0.09MPa.
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| CN106276834A (en) * | 2016-08-05 | 2017-01-04 | 常熟市圆启晶体材料有限公司 | The stirring means of potassium dihydrogen phosphate crystallisation by cooling |
| CN106810583B (en) * | 2016-12-30 | 2019-04-02 | 珠海同源药业有限公司 | A kind of fructose sodium diphosphate compound and preparation method thereof |
| CN110487029B (en) * | 2019-08-23 | 2021-12-31 | 老肯医疗科技股份有限公司 | Drying method of medical instrument |
| CN112245442B (en) * | 2020-09-29 | 2022-04-29 | 北京华靳制药有限公司 | Fructose diphosphate sodium reverse osmosis concentrated solution and preparation method thereof |
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| CN2451985Y (en) * | 2000-10-12 | 2001-10-03 | 沈善明 | Non-sealing double-cone vacuum dryer |
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| CN102154399A (en) * | 2010-12-30 | 2011-08-17 | 张家港市华天药业有限公司 | Production process flow of fructose diphosphate sodium |
| CN201992958U (en) * | 2011-03-08 | 2011-09-28 | 常州先锋干燥设备有限公司 | Vacuum double-cone rotating drying unit |
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| CN2451985Y (en) * | 2000-10-12 | 2001-10-03 | 沈善明 | Non-sealing double-cone vacuum dryer |
| CN2482037Y (en) * | 2001-04-12 | 2002-03-13 | 沈善明 | Medicine refining filtering vacuum dryer |
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| CN102154399A (en) * | 2010-12-30 | 2011-08-17 | 张家港市华天药业有限公司 | Production process flow of fructose diphosphate sodium |
| CN201992958U (en) * | 2011-03-08 | 2011-09-28 | 常州先锋干燥设备有限公司 | Vacuum double-cone rotating drying unit |
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