CN103710470B - A kind of technique of two step method sugaring and device - Google Patents
A kind of technique of two step method sugaring and device Download PDFInfo
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Abstract
The invention discloses technique and the device of the sugaring of a kind of two step method, step comprises: obtain raw sugar slurry after being dissolved in water by raw sugar, raw sugar slurry is sent into coarse filter successively, microfiltration membrane is filtered, and obtains filtrate; Filtrate is sent into the first exchange resin tower, obtain the first penetrating fluid, the first described ion exchange resin refers to macroporous strong basic anionite-exchange resin; First penetrating fluid is sent into the second exchange resin tower, obtains the second penetrating fluid, the second described ion exchange resin refers to the mixed bed of storng-acid cation exchange resin, weakly acidic cation-exchange resin or anion-cation exchange resin; Second penetrating fluid is sent into vaporizer concentrate, obtain sucrose concentrated solution, then through crystallization, centrifugal, dry, obtain sucrose finished product.Above-mentioned technique can the highly purified refined sucrose of Mass production, and pigment removal reaches 99.9%, and salinity clearance reaches 98%, and the Sucrose of product reaches 99.9%, reaches the standard of national top grade sugar.
Description
Technical field
The present invention relates to technique and the device of the sugaring of a kind of two step method, belong to sugar refining field.
Background technology
The sugaring of most of developed countries is the Closed Circulation in Sugar Production method adopting " two step method " in the world.Most sugar refinery produces raw sugar, then supplies refinery and produces refined sugar.Namely " two step method " sugaring is that sugar material first uses comparatively simple technique (lime method) to produce raw sugar (i.e. raw sugar), back dissolving again, after purifying, white sugar is produced in crystallization again, as refined sugar (namely purity is higher, colour is lower, impurity is less a kind of high target require white sugar) will be produced, need process again in ion-exchange etc. in decolouring, desalination.The major advantage of " two step method " is, through post-defecation impurity elimination, secondary crystal is purified, and quality product is high, can meet the demand of top-grade consumption.Purified sugar can production and sales throughout the year, and produce flexibly according to market situation, there is not the impact of Metamorphic Factors, the good price of quality is high.Method due to lime legal system raw sugar in " two step method " is easy, the process flow of sugarcane production raw sugar is the shortest, raw sugar can be produced within the shortest time, and during owing to producing raw sugar, methose and biose mixing, all as the product of raw sugar, reduce steam consumption in a large number, reduce non-physical loss, therefore, under same system refining appointed condition, throughput can improve 20-30%.
But the production of existing refined sugar is the technique adopting original lime method precipitation to add sulphur drift.The method has following shortcoming: first, employ filter press, belong to more traditional, level of automation is lower, labor-intensive equipment, the work under bad environment of this equipment, production efficiency is low, and filtering accuracy is inadequate, effectively can not remove the impurity such as colloid, tannin in syrup, carry out larger production load can to operation length of tape below; The second, employ lime method precipitation technology, can produce a large amount of residues, environmental pollution is comparatively serious, and introduces new impurity aborning---and ash content, causes quality product lower; 3rd, the decolouring of this technique uses stove drying method, has sulphur remnants in product, to human health, and the sugar that sulfurous gas is bleached, color development phenomenon can be there is after being long placed in.Along with country is to the further raising of food safety requirements, the method will be limited to use; 4th, do not use ion-exchange desalination, salinity remaining in liquid glucose cannot be removed, cause product ash content higher, quality is lower or defective, and the 4th, employ traditional triple-effect evaporator, waste a large amount of energy, the modern techniquies such as MVR of comparing, energy consumption is higher.5th, relevant processing parameter does not reach optimization, causes the waste of the energy.In view of this, the production technique that " two step method " that still await proposing a kind of optimization refines sugar.
Summary of the invention
The object of the invention is to overcome the deficiencies in the prior art, provide " two step method " sugar production process of a kind of comparatively energy-conserving and environment-protective, less investment, it has pollution-free, and quality product is high, and technical process is short, and energy consumption is low, invests little, the features such as floor space is little.Technical scheme is as follows:
A technique for two step method sugaring, comprises the steps:
1st step, raw sugar is dissolved in water after obtain raw sugar slurry, by raw sugar slurry send into coarse filter successively, microfiltration membrane is filtered, and obtains filtrate;
2nd step, filtrate is sent into the first exchange resin tower, obtain the first penetrating fluid, the first described ion exchange resin refers to macroporous strong basic anionite-exchange resin;
3rd step, the first penetrating fluid is sent into the second exchange resin tower, obtain the second penetrating fluid, the second described ion exchange resin refers to the mixed bed of storng-acid cation exchange resin, weakly acidic cation-exchange resin or anion-cation exchange resin;
4th step, the second penetrating fluid is sent into vaporizer concentrate, obtain sucrose concentrated solution, then through crystallization, centrifugal, dry, obtain sucrose finished product.
In the 1st step, the mass concentration of raw sugar slurry is preferably 40% ~ 80%, can ensure that raw sugar syrup has suitable viscosity, also can ensure production efficiency, if the viscosity of syrup can be made when concentration is excessive too high, in coarse filter and microfiltration membrane, flux is not suitable for needed for engineering, if concentration is too low, then feed liquid can be caused rarer, follow-up evaporative process energy consumption is bigger than normal, and crystallization yields is low.Preferred, mass concentration is 60%, under this concentration range, can ensure that the solubleness of the macromole in raw sugar, colloidal impurity is low, can be retained by microfiltration membrane, ensure the quality product of follow-up sucrose finished product, also can ensure that the viscosity of syrup is less simultaneously, the flux of later stage membrane filtration is comparatively large, and the steam output of postorder is also less, can ensure higher production efficiency.Coarse filter in this step includes but are not limited to: deep bed filter or screen cloth (aperture of screen cloth is preferably 0.1 μm-5 μm) etc., fully to remove oarse-grained impurity.Microfiltration membrane preferably adopts ceramic microfiltration membrane, physical strength is high, acid-alkali-corrosive-resisting, filtering accuracy are high advantage that it has.Some granule foreign, the colloids etc. in raw sugar syrup are removed in the effect of microfiltration membrane, can improve purity and the quality of product.In order to make filter effect more excellent, the size of the mean pore size to microfiltration membrane is needed to select.If mean pore size is too little, then filtration flux can be caused too little, then filtration flux can be caused too low, and the sucrose of a part of larger particles can be trapped, and has influence on yield, if mean pore size is too large, a part of impurity can be caused to enter to per-meate side through rete, have influence on the quality of product.The mean pore size scope of preferred microfiltration membrane is 50 ~ 500nm.The solubleness of the temperature of microfiltration process and sucrose and impurity, colloid and the viscosity of system relevant, if temperature is too high, impurity, colloid can be caused also to be dissolved in material, cannot obtain being separated and remove, if temperature is too low, a part of sucrose then can be caused not dissolve, and separated film retains, and overall yield is reduced, preferable temperature is 50 ~ 90 DEG C, at this temperature, can also ensure that flux is comparatively large and suppression ratio is comparatively slow preferably, energy consumption is relatively low simultaneously.If when filter pressure is less than normal, flux can be caused low, do not conform to and be suitable for engineering actual demand, if when pressure is excessive, a part of most of impurity can be caused to be pressed, through rete, cause product quality bad, and more serious Pore Blocking can be produced, make it not easily be cleaned, preferred filter pressure is 0.1 ~ 0.5MPa.
In 2nd step, macroporous strong basic anionite-exchange resin has the effect of desalination and decolouring, and can remove some negatively charged ion in sucrose liquid, and has the effect of decolouring.Preferred, the blade diameter length ratio of the first exchange resin tower is 1/3 ~ 1/10, and flow velocity is 2 ~ 10BV/h, and temperature is 40 ~ 80 DEG C.Contriver finds, be 1/8 at adsorption tower blade diameter length ratio, flow velocity is 4BV/h, when temperature is 60 DEG C, the viscosity of liquid glucose is less, the best results of absorption, can ensure decolorizing effect, can ensure higher production efficiency again, energy consumption is relatively low simultaneously, and the yield of sucrose is higher.
In 3rd step, ion exchange resin is strongly-acid or weakly acidic cation-exchange resin, and also can be the mixed bed of anion-cation exchange resin, it can play and remove cationic effect, also can play the effect of decolouring.Described second exchange resin tower blade diameter length ratio is 1/3 ~ 1/10, and flow velocity is 2 ~ 10BV/h, and temperature is 30 ~ 70 DEG C.In addition, contriver finds, be 1/5 at adsorption tower blade diameter length ratio, flow velocity is 4BV/h, and when temperature is 50 DEG C, the best results of desalination, can slough the salinity of 95%, and the yield of sucrose is higher simultaneously.
In 4th step, vaporizer preferably adopts MVR vaporizer (MechanicalVaporRecompression), and thickening temperature is 30 ~ 80 DEG C, and treating that liquid glucose is concentrated to supersaturation degree is about 1.05, decrease temperature crystalline; Wherein rearing crystal time is 1.5h, and cooling rate is 0.2 ~ 1 DEG C/min, is preferably 0.4 DEG C/min, cools the temperature to 5 DEG C.During centrifugation, centrifugal rotational speed is 5000 ~ 8000rpm; Preferably forced air drying, drying temperature is 90 ~ 100 DEG C.
In an optimum embodiment of the present invention, the mean pore size of microfiltration membrane is 200nm, the filtration temperature of micro-filtration is 70 DEG C, the transmembrane pressure of micro-filtration is 0.4MPa, under this parameter area, the microfiltration membrane of 200nm retains some fat, protein of getting rid of in sucrose, and this can ensure the life of ion exchange resin, and resin can be prevented by macromole impurity absorption, have influence on the decreasing ratio for salt and pigment.
Based on above-mentioned method, another object of the present invention there is provided the device of a kind of two step method sugaring, includes the coarse filter, microfiltration membrane, the first ion exchange resin column, the second ion exchange resin column, vaporizer, crystallizer, whizzer, the moisture eliminator that connect successively.
Further, the mean pore size of described microfiltration membrane is 50 ~ 500nm.
Further, what fill in the first described ion exchange resin column is macroporous strong basic anionite-exchange resin.
Further, what fill in the second described ion exchange resin column is storng-acid cation exchange resin or weakly acidic cation-exchange resin.
Beneficial effect
Technique tool of the present invention has the following advantages:
1, above-mentioned technique is adopted, can the highly purified refined sucrose of Mass production, in preferably embodiment, the pigment removal of product reaches 99.9%, the clearance of salinity reaches 98%, the Sucrose of product reaches 99.9%, and Conductivity ash is lower than 0.01%, and content of sulfur dioxide does not detect, reach the standard of national top grade sugar, simultaneously the rate of recovery of sucrose is more than 99%, and this sucrose finished product, after placement half a year, has no and returns look phenomenon in traditional technology.
2, the parameter of this technique to new installation and traditional technology has done a large amount of Optimization Works, obtains optimum processing parameter, ensure that the energy-efficient operation of production, and the quality of product is higher simultaneously.This production technique relative energy-saving, traditional processing technology of comparing, level of automation is high, can save the labour cost of 70%, reduces the production cost of more than 25%, remarkable in economical benefits.
3, instead of traditional filter press and lime precipitation with ceramic membrane, eliminate filter press and lime method settling step, substantially reduce technical process, reduce human input on the one hand, improve production efficiency; Ceramic membrane is compared traditional polymeric amide or polyether sulfone material organic membrane, can withstand high temperatures, high pressure, chemical corrosion, and work-ing life is longer; It also avoid the pollution of solid waste to environment on the other hand.
4, instead of traditional stove drying technique with ion exchange method decoloration process, solve the problem of sulphur remnants in finished product sucrose on the one hand; Also eliminate the operation section of stove drying on the other hand, reduce production cost;
5, ion exchange method desalination is used, more effective except the ash content in sugarcane juice, improve the quality of products.
6, concentrate with MVR equipment, significantly reduce energy consumption, and vaporization temperature is lower, sugared coking can not be made because temperature is high, produce new pigment.
7, production technique is comparatively simple, and flow process is shorter, and control process is simple, and personnel labor intensity and usage quantity greatly reduce, and production quality control is stablized.
8, adopt membrane separation plant and ion-exchange unit, reduce the floor space of equipment, reduce capital construction cost.
Accompanying drawing explanation
Fig. 1 is sugar refining technology schema provided by the invention;
Fig. 2 is sugaring device schematic diagram provided by the invention.
Embodiment
Embodiment 1
A novel process for sugar industry, it comprises the following steps:
A, change sugar: heated by adding water by raw sugar to 80 DEG C of dissolvings, make syrup, sucrose content is about 40%, 50%, 60%, 70%, about 80% respectively;
B, pre-treatment: syrup is carried out pre-treatment by sheet frame, remove colloid or larger particulate contamination; The precision of sheet frame filter cloth used is 0.1 μm;
C, ceramic membrane filter: by the pretreated syrup collected, by microfiltration of ceramic membrane, mean pore size is 50nm, the temperature of filtration is 50 DEG C, and filter pressure is 0.5Mpa, obtains syrup clear liquid;
D, primary ion exchange desalination: syrup clear liquid macroporous strong basic anionite-exchange resin is carried out ion-exchange desalination, also can play the effect of decolouring, the flow velocity in resin column is 2BV/h, and temperature is 70 DEG C simultaneously, blade diameter length ratio is 1/3, and the brix of the sucrose syrup obtained is 55;
E, secondary ion exchange desalination: the syrup anionite-exchange resin obtained in step D is carried out desalination, also can play the effect of decolouring, the flow velocity in resin column is 10BV/h, and temperature is 30 DEG C simultaneously, blade diameter length ratio is 1/10, and the brix of the sucrose syrup obtained is 55;
F, concentrated: the syrup obtained in step e is sent into MVR vaporizer, and thickening temperature is 65 DEG C, and liquid glucose being concentrated to degree of supersaturation is 1.05, obtains sucrose concentrated solution;
G, crystallization: add crystal seed, growing the grain 1.5h, then be slow cooling to 60 DEG C with the speed of 0.2 DEG C/min, separate out crystallization of sucrose;
H, centrifugation: by crystallization of sucrose centrifuge, rotating speed 8000rpm, time 25min;
I, drying: dry 4 hours at 90 DEG C, obtain finished product, measure the indexs such as colour, percent of decolourization, ratio of desalinization, Sucrose and the rate of recovery.
。
As can be seen from the table, with the increase of sucrose content, there is downward trend in the rate of recovery of sucrose, and this is mainly because syrup concentration becomes greatly, cause having more sucrose to be trapped, and certain cycles of concentration cannot be reached, but, sucrose concentration is controlled 60% time, macromole in raw sugar can be reduced solubleness, these impurity are more easily trapped, thus prevent these impurity effects such as colloid, albumen to ion exchange resin, make it keep higher desalination and percent of decolourization.This sucrose finished product, after placement half a year, has no and returns look phenomenon in traditional technology.
Embodiment 2
A novel process for sugar industry, it comprises the following steps:
A, change sugar: heated by adding water by raw sugar to 80 DEG C of dissolvings, make syrup, sucrose content is respectively about 60%;
B, pre-treatment: syrup is carried out pre-treatment by sheet frame, remove colloid or larger particulate contamination; The precision of sheet frame filter cloth used is 5 μm;
C, ceramic membrane filter: by the pretreated syrup collected, by microfiltration of ceramic membrane, mean pore size is 50nm, 200nm and 500nm respectively, and the temperature of filtration is 90 DEG C, and filter pressure is 0.1Mpa, obtains syrup clear liquid;
D, primary ion exchange desalination: syrup clear liquid macroporous strong basic anionite-exchange resin is carried out ion-exchange desalination and decolouring, and the flow velocity in resin column is 10BV/h, and temperature is 40 DEG C, and blade diameter length ratio is 1/10, and the brix of the sucrose syrup obtained is 55;
E, secondary ion exchange desalination: the syrup anionite-exchange resin obtained in step D is carried out desalination and decolouring, and the flow velocity in resin column is 2BV/h, and temperature is 70 DEG C, and blade diameter length ratio is 1/3, and the brix of the sucrose syrup obtained is 55;
F, concentrated: the syrup obtained in step e is sent into MVR vaporizer, and thickening temperature is 65 DEG C, and liquid glucose being concentrated to degree of supersaturation is 1.05, obtains sucrose concentrated solution;
G, crystallization: add crystal seed, growing the grain 1.5h, then be slow cooling to 60 DEG C with the speed of 0.2 DEG C/min, separate out crystallization of sucrose;
H, centrifugation: by crystallization of sucrose centrifuge, rotating speed 8000rpm, time 25min;
I, drying: dry 4 hours at 90 DEG C, obtain finished product, measure the indexs such as colour, percent of decolourization, ratio of desalinization, Sucrose and the rate of recovery.
。
As can be seen from the table, when using the microfiltration membrane of 500nm, there is more impurity can enter into per-meate side through rete, these impurity not only can have influence on the purity of product, also the operating performance of ion exchange resin can be had influence on, cause the decrease in efficiency of desalination and decolouring, if when adopting the less microfiltration membrane in aperture, make the yield of product be affected.
Embodiment 3
A novel process for sugar industry, it comprises the following steps:
A, change sugar: heated by adding water by raw sugar to 80 DEG C of dissolvings, make syrup, sucrose content is respectively about 60%;
B, pre-treatment: syrup is carried out pre-treatment by sheet frame, remove colloid or larger particulate contamination; The precision of sheet frame filter cloth used is 4 μm;
C, ceramic membrane filter: by the pretreated syrup collected, by microfiltration of ceramic membrane, mean pore size is 200nm, the temperature of filtration is respectively 50 DEG C, 70 DEG C, 90 DEG C, and filter pressure is 0.4Mpa, obtains syrup clear liquid;
D, primary ion exchange desalination: syrup clear liquid macroporous strong basic anionite-exchange resin is carried out ion-exchange desalination and decolouring, and the flow velocity in resin column is 4BV/h, and temperature is 60 DEG C, and blade diameter length ratio is 1/8, and the brix of the sucrose syrup obtained is 55;
E, secondary ion exchange desalination: the syrup anionite-exchange resin obtained in step D is carried out desalination and decolouring, and the flow velocity in resin column is 4BV/h, and temperature is 50 DEG C, and blade diameter length ratio is 1/5, and the brix of the sucrose syrup obtained is 55;
F, concentrated: the syrup obtained in step e is sent into MVR vaporizer, and thickening temperature is 65 DEG C, and liquid glucose being concentrated to degree of supersaturation is 1.05, obtains sucrose concentrated solution;
G, crystallization: add crystal seed, growing the grain 1.5h, then be slow cooling to 60 DEG C with the speed of 0.2 DEG C/min, separate out crystallization of sucrose;
H, centrifugation: by crystallization of sucrose centrifuge, rotating speed 8000rpm, time 25min;
I, drying: dry 4 hours at 90 DEG C, obtain finished product, measure the indexs such as colour, percent of decolourization, ratio of desalinization, Sucrose and the rate of recovery.
。
As can be seen from the table, when higher micro-filtration temperature, the solubleness of a part of impurity in material can be caused to raise, in the process of filtering, enter to per-meate side through rete, these impurity can have influence on life-span of resin and percent of decolourization and ratio of desalinization, if filtration temperature is low, cycles of concentration then can be caused to promote, the rate of recovery that result in sucrose is on the low side, under the preferred conditions, can reach the rate of recovery of 99% and the Sucrose of 99%.
Claims (1)
1. a technique for two step method sugaring, is characterized in that, comprise the steps:
A, change sugar: being heated by adding water by raw sugar to 80 DEG C of dissolvings, making syrup, sucrose content is 60%;
B, pre-treatment: syrup is carried out pre-treatment by sheet frame, remove colloid or larger particulate contamination; The precision of sheet frame filter cloth used is 4 μm;
C, ceramic membrane filter: by the pretreated syrup collected, by microfiltration of ceramic membrane, mean pore size is 200nm, the temperature of filtration is 70 DEG C, and filter pressure is 0.4Mpa, obtains syrup clear liquid;
D, primary ion exchange desalination: syrup clear liquid macroporous strong basic anionite-exchange resin is carried out ion-exchange desalination and decolouring, and the flow velocity in resin column is 4BV/h, and temperature is 60 DEG C, and blade diameter length ratio is 1/8, and the brix of the sucrose syrup obtained is 55;
E, secondary ion exchange desalination: the syrup anionite-exchange resin obtained in step D is carried out desalination and decolouring, and the flow velocity in resin column is 4BV/h, and temperature is 50 DEG C, and blade diameter length ratio is 1/5, and the brix of the sucrose syrup obtained is 55;
F, concentrated: the syrup obtained in step e is sent into MVR vaporizer, and thickening temperature is 65 DEG C, and liquid glucose being concentrated to degree of supersaturation is 1.05, obtains sucrose concentrated solution;
G, crystallization: add crystal seed, growing the grain 1.5h, then be slow cooling to 60 DEG C with the speed of 0.2 DEG C/min, separate out crystallization of sucrose;
H, centrifugation: by crystallization of sucrose centrifuge, rotating speed 8000rpm, time 25min;
I, drying: drying 4 hours at 90 DEG C, obtains finished product.
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| CN104004860A (en) * | 2014-05-29 | 2014-08-27 | 江苏久吾高科技股份有限公司 | Production process and device of golden sugar |
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| CN104805222B (en) * | 2015-04-02 | 2018-02-27 | 广西大学 | A kind of refined sugar clarifier |
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| CN104831002B (en) * | 2015-04-27 | 2018-05-04 | 广西大学 | A kind of sugar clarification production line |
| CN105671214A (en) * | 2016-02-26 | 2016-06-15 | 广西大学 | Method for producing crystallized fructose by taking raw sugar as raw material |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5554227A (en) * | 1993-11-12 | 1996-09-10 | Societe Nouvelle De Recherches Et D'applications Industrielles D'echangeurs D'ions Applexion | Process of manufacturing crystal sugar from an aqueous sugar juice such as cane juice or sugar beet juice |
| US20030230301A1 (en) * | 2002-04-17 | 2003-12-18 | Applexion | Method and plant for the production of refined sugar from a sugared juice |
| CN1740341A (en) * | 2005-09-15 | 2006-03-01 | 陈秀恋 | Decolour and refining apparatus for ion exchange method of sugar cane juice |
| CN1962878A (en) * | 2006-11-21 | 2007-05-16 | 华南理工大学 | Method for producing natural coloured sugar |
| JP4303867B2 (en) * | 2000-04-27 | 2009-07-29 | オルガノ株式会社 | Method and apparatus for producing purified sucrose liquid containing mineral components |
| CN103468832A (en) * | 2013-10-12 | 2013-12-25 | 云南省轻工业科学研究院 | Process for producing high-safety white granulated sugar |
-
2013
- 2013-12-26 CN CN201310729069.3A patent/CN103710470B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5554227A (en) * | 1993-11-12 | 1996-09-10 | Societe Nouvelle De Recherches Et D'applications Industrielles D'echangeurs D'ions Applexion | Process of manufacturing crystal sugar from an aqueous sugar juice such as cane juice or sugar beet juice |
| JP4303867B2 (en) * | 2000-04-27 | 2009-07-29 | オルガノ株式会社 | Method and apparatus for producing purified sucrose liquid containing mineral components |
| US20030230301A1 (en) * | 2002-04-17 | 2003-12-18 | Applexion | Method and plant for the production of refined sugar from a sugared juice |
| CN1740341A (en) * | 2005-09-15 | 2006-03-01 | 陈秀恋 | Decolour and refining apparatus for ion exchange method of sugar cane juice |
| CN1962878A (en) * | 2006-11-21 | 2007-05-16 | 华南理工大学 | Method for producing natural coloured sugar |
| CN103468832A (en) * | 2013-10-12 | 2013-12-25 | 云南省轻工业科学研究院 | Process for producing high-safety white granulated sugar |
Non-Patent Citations (1)
| Title |
|---|
| 二步法制糖在中国应用的探讨;蓝贤州，等;《广西轻工业》;20021231(第6期);第23-26页 * |
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Address after: 211806 No. 195 Buyue Road, Pukou Economic Development Zone, Nanjing City, Jiangsu Province Patentee after: Jiangsu Jiuwu High-Tech Co., Ltd. Address before: 211808, No. 9 Hu Dong Road, Pukou Economic Development Zone, Jiangsu, Nanjing Patentee before: Jiangsu Jiuwu High-Tech Co., Ltd. |
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| CP02 | Change in the address of a patent holder |