CN101392009A - Novel production technique of xylose - Google Patents
Novel production technique of xylose Download PDFInfo
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- CN101392009A CN101392009A CNA2007101129753A CN200710112975A CN101392009A CN 101392009 A CN101392009 A CN 101392009A CN A2007101129753 A CNA2007101129753 A CN A2007101129753A CN 200710112975 A CN200710112975 A CN 200710112975A CN 101392009 A CN101392009 A CN 101392009A
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- temperature
- xylose
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- ion
- acid
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Links
- 238000000034 method Methods 0.000 title claims abstract description 32
- SRBFZHDQGSBBOR-IOVATXLUSA-N D-xylopyranose Chemical compound O[C@@H]1COC(O)[C@H](O)[C@H]1O SRBFZHDQGSBBOR-IOVATXLUSA-N 0.000 title claims abstract description 30
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 16
- PYMYPHUHKUWMLA-UHFFFAOYSA-N arabinose Natural products OCC(O)C(O)C(O)C=O PYMYPHUHKUWMLA-UHFFFAOYSA-N 0.000 title claims abstract description 15
- SRBFZHDQGSBBOR-UHFFFAOYSA-N beta-D-Pyranose-Lyxose Natural products OC1COC(O)C(O)C1O SRBFZHDQGSBBOR-UHFFFAOYSA-N 0.000 title claims abstract description 15
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 20
- 238000005342 ion exchange Methods 0.000 claims abstract description 20
- 239000007788 liquid Substances 0.000 claims abstract description 19
- 239000002253 acid Substances 0.000 claims abstract description 13
- 238000001728 nano-filtration Methods 0.000 claims abstract description 13
- 238000000909 electrodialysis Methods 0.000 claims abstract description 10
- 238000000926 separation method Methods 0.000 claims abstract description 10
- 238000002425 crystallisation Methods 0.000 claims abstract description 8
- 230000008025 crystallization Effects 0.000 claims abstract description 8
- 239000012535 impurity Substances 0.000 claims abstract description 8
- 239000002699 waste material Substances 0.000 claims abstract description 8
- 239000012141 concentrate Substances 0.000 claims abstract description 7
- 238000005516 engineering process Methods 0.000 claims abstract description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 7
- 235000011149 sulphuric acid Nutrition 0.000 claims abstract description 6
- 239000001117 sulphuric acid Substances 0.000 claims abstract description 6
- 238000001035 drying Methods 0.000 claims abstract description 4
- 239000000463 material Substances 0.000 claims description 29
- 229960003487 xylose Drugs 0.000 claims description 22
- 239000000243 solution Substances 0.000 claims description 17
- 230000007062 hydrolysis Effects 0.000 claims description 14
- 238000006460 hydrolysis reaction Methods 0.000 claims description 14
- SRBFZHDQGSBBOR-LECHCGJUSA-N alpha-D-xylose Chemical compound O[C@@H]1CO[C@H](O)[C@H](O)[C@H]1O SRBFZHDQGSBBOR-LECHCGJUSA-N 0.000 claims description 13
- 239000000047 product Substances 0.000 claims description 13
- 238000001704 evaporation Methods 0.000 claims description 12
- 230000008020 evaporation Effects 0.000 claims description 12
- 238000009413 insulation Methods 0.000 claims description 12
- 238000003756 stirring Methods 0.000 claims description 12
- 240000008042 Zea mays Species 0.000 claims description 11
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 claims description 11
- 235000002017 Zea mays subsp mays Nutrition 0.000 claims description 11
- 235000005822 corn Nutrition 0.000 claims description 11
- 239000002994 raw material Substances 0.000 claims description 10
- 239000013078 crystal Substances 0.000 claims description 9
- 230000000694 effects Effects 0.000 claims description 9
- 150000002500 ions Chemical class 0.000 claims description 9
- 238000011282 treatment Methods 0.000 claims description 8
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 claims description 7
- 239000000049 pigment Substances 0.000 claims description 7
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 6
- 238000004042 decolorization Methods 0.000 claims description 6
- 239000000428 dust Substances 0.000 claims description 6
- 238000000855 fermentation Methods 0.000 claims description 6
- 230000004151 fermentation Effects 0.000 claims description 6
- 239000008103 glucose Substances 0.000 claims description 6
- 239000003456 ion exchange resin Substances 0.000 claims description 6
- 229920003303 ion-exchange polymer Polymers 0.000 claims description 6
- 239000012528 membrane Substances 0.000 claims description 6
- 238000002156 mixing Methods 0.000 claims description 6
- 239000012047 saturated solution Substances 0.000 claims description 6
- 239000000084 colloidal system Substances 0.000 claims description 5
- 239000004744 fabric Substances 0.000 claims description 5
- 238000002203 pretreatment Methods 0.000 claims description 5
- 240000004808 Saccharomyces cerevisiae Species 0.000 claims description 3
- 239000003610 charcoal Substances 0.000 claims description 3
- 239000003795 chemical substances by application Substances 0.000 claims description 3
- 230000005684 electric field Effects 0.000 claims description 3
- 230000005518 electrochemistry Effects 0.000 claims description 3
- 239000012530 fluid Substances 0.000 claims description 3
- 239000003014 ion exchange membrane Substances 0.000 claims description 3
- 238000011068 loading method Methods 0.000 claims description 3
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims description 3
- 230000008929 regeneration Effects 0.000 claims description 3
- 238000011069 regeneration method Methods 0.000 claims description 3
- 239000002689 soil Substances 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- 239000000126 substance Substances 0.000 claims description 3
- 238000005406 washing Methods 0.000 claims description 3
- 230000008719 thickening Effects 0.000 claims description 2
- 239000003513 alkali Substances 0.000 abstract description 4
- 230000003472 neutralizing effect Effects 0.000 abstract description 2
- 229920002125 Sokalan® Polymers 0.000 abstract 2
- 230000015572 biosynthetic process Effects 0.000 abstract 1
- 239000003518 caustics Substances 0.000 abstract 1
- 238000005119 centrifugation Methods 0.000 abstract 1
- 230000003247 decreasing effect Effects 0.000 abstract 1
- 230000002708 enhancing effect Effects 0.000 abstract 1
- 238000004064 recycling Methods 0.000 abstract 1
- 230000008439 repair process Effects 0.000 abstract 1
- 238000006386 neutralization reaction Methods 0.000 description 4
- 230000003245 working effect Effects 0.000 description 3
- 241000196324 Embryophyta Species 0.000 description 2
- 229910052602 gypsum Inorganic materials 0.000 description 2
- 239000010440 gypsum Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- 125000002091 cationic group Chemical group 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 238000010297 mechanical methods and process Methods 0.000 description 1
- 230000005226 mechanical processes and functions Effects 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 235000010987 pectin Nutrition 0.000 description 1
- 229920001277 pectin Polymers 0.000 description 1
- 239000001814 pectin Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 239000006200 vaporizer Substances 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention discloses a new manufacturing technique of a xylose and relates to a technique for manufacturing the xylose. The technique adopts the technology of electrodialysis recycling sulphuric acid, a bag adopted by a nanofiltration concentration device and a special nanofiltration separation system concentrates the liquid in the technique for manufacturing the xylose at normal temperature, therefore water and other impurities can be removed from the product; the manufacturing technique comprises: 1. pretreatment, 2. hydrolyzation, 3. decoloration, 4. electrodialysis, 5. ion exchange, 6. nanofiltration, 7. concentration, 8. ferment, 9. crystallization, 10. centrifugation, and 11. drying, then the high purity xylose is obtained. The new manufacturing technique of the xylose can not only recycle 50 percent sulphuric acid in the hydrolyze liquid, but also can recycle waste acid and spent caustic produced in the regenerative process of duolite, therefore the dosage of sulphuric acid can be saved and the environment pollution is avoided. The technique solves the problems of scale formation in device in the neutralizing deacidification technique, large usage of duolite in deacidification technique, large usage of devices, large investment, large consumption of acid and alkali, high costs and the like; thus improving the device utilization rate and the service life, decreasing the ash and the acid contents in the hydrolyze liquid, improving the quality of the hydrolyze liquid and enhancing the product quality and separating efficiency.
Description
Technical field
The present invention relates to a kind of processing method of producing wood sugar.
Background technology
At present, the preparation method of wood sugar mainly contains neutralisation deacidifying process and ion-exchange deacidifying process.
The neutralisation depickling prepares the operational path that wood sugar technology neutralisation prepares wood sugar: raw material (being the agricultural fibre waste material), successively pass through raw materials pretreatment, and hydrolysis, neutralization, decolouring, ion-exchange concentrates, and crystallization separates obtaining the wood sugar crystal at last.Because in and the gypsum (CaSO that forms in the operation
4) finally understand on the tube wall that some gypsum is deposited on vaporizer, form thermofin, reduce evaporation and render a service, waste steam reduces plant factor.Because this layer fouling be difficult to remove, particularly be difficult to remove with chemical process, to have to remove fouling with mechanical process, trouble not only, and labour intensity is very big also has in various degree damage, the work-ing life of reducing equipment to equipment.Because wood sugar is a stable in properties under a kind of acidic conditions, extremely unsettled reducing sugar under the alkaline condition.When with lime neutralizing hydrolysis liquid, partial pH value is too high will inevitably to be made some wood sugar sex change and influences final product quality.Simultaneously, both got rid of part SO with operation in
4 2-, also brought number of C a into
2+, increased the burden of cationic exchange coloum.
The operational path of ion-exchange depickling is: raw material is through pre-treatment, and hydrolysis is decoloured, the ion-exchange removal of impurities, and condensing crystal separates obtaining the wood sugar crystal at last.The shortcoming of equipment scaling in having solved and in the deacidifying process has improved usage ratio of equipment and work-ing life, has reduced the content of ash in the hydrolyzed solution and acid, has improved the quality of hydrolyzed solution, has improved quality product accordingly.Though the ion-exchange deacidifying process has above advantage, its technology more complicated, the ion exchange resin consumption is more, and equipment is more, and investment is big, has increased acid and alkali consumption, has strengthened cost, and is seriously polluted.
Summary of the invention
In order to overcome the deficiencies in the prior art, the invention provides a kind of novel production technique of xylose, easily form thermofin to solve prior art, reducing evaporation renders a service, waste steam reduces plant factor, the technology more complicated, the ion exchange resin consumption is more, equipment is more, and investment is big, has increased acid and alkali consumption, strengthened cost, problem such as seriously polluted.
The present invention solves its technical problem and adopts to such an extent that technical scheme is to use electrodialysis reclaim(ed) sulfuric acid technology, the cloth bag that the nanofiltration thickening equipment adopts, special nanofiltration membrane separation system concentrate the liquid in the xylose production process at normal temperatures, water and other impurity in the product can be removed, and spent acid, the salkali waste that produces in the ion exchange resin regeneration process can be reclaimed.Its producing and manufacturing technique:
One, pre-treatment
Utilize screen scarifier dust removal soil, foreign material in small, broken bits, adopt the rotary drum washer washing, dust, foreign material, pigment on the raw material corn cob are washed, make it to see true qualities, no-sundries.Each air-dry corn cob raw material 3.2-3.5T, adding 12m of throwing
3The 0.05-0.15% dilute sulphuric acid is handled, and is pressurized to 0.04-0.06Mpa, behind the pressurize 40-80min, and the treatment solution of draining.Add 12m then
3De-mineralized water is handled, and is pressurized to 0.04-0.06Mpa, behind the pressurize 10-30min, and the treatment solution of draining.
Two, hydrolysis
With the pentosan in the corn cob at pressure 0.11-0.15Mpa, 12m
3Concentration is heat-insulation pressure keeping hydrolysis 90-150min under the sulfuric acid condition of 1.4-2.0%, is hydrolyzed into the xylose hydrolysis fluid of individual molecule, and is standby.
Three, decolouring
Utilize the discoloring agent gac to remove pigment colloid and the nitrogenous thing of part in the hydrolyzed solution.
When 1, once decolouring, add the about 100kg/ still of the old charcoal of secondary decolourization, temperature 70-80 ℃, stir insulation 20-40min;
2, during secondary decolourization, add new gac 80-120kg/ still, temperature 70-80 ℃, stir insulation 20-40min;
When 3, decolouring for three times, add new gac 60-100kg/ still, temperature 70-80 ℃, stir insulation 20-40min.
Four, electrodialysis
Electrodialysis is under the effect of DC electric field, and ion sees through selective ion exchange membrane and moves, and makes charged H
+And SO
4 2-Ion a kind of electrochemistry sepn process that part is separated from hydrolyzed solution.
Feeding temperature requires smaller or equal to 40 ℃, and flow velocity is 1.0-1.6m
3/ h.
Five, ion-exchange
Temperature is less than and equals 40 ℃ during material ion-exchange, and flow velocity is more than or equal to 15m
3/ h.The primary ions exchange: the order that feed liquid enters ion exchange column is positive post, cloudy post, cloudy post, positive post.The secondary ions exchange: the order that feed liquid enters ion exchange column is positive post, cloudy post, cloudy post.
Six, nanofiltration
The nanofiltration membrane separation feeding temperature is less than and equals 40 ℃, and flow rate control is at 35m
3/ h cover, pressure is 2.5-3.0Mpa.
Seven, concentrate
Triple effect evaporation and single-effect evaporation:
Processing parameter:
1, vacuum tightness: 0.01-0.09Mpa
2, flow: 16-22m
3/ h
3, temperature: 50-95 ℃
Eight, fermentation
Owing to contain a small amount of glucose in the saccharification liquid, influence the crystallization and the quality product of wood sugar, can remove glucose by yeast fermentation.
Processing parameter:
1, leavening temperature: 37 ± 1 ℃
2, pH value=4-7
Nine, crystallization
Material becomes saturated solution through evaporation concentration, with the way of cooling, obtains crystal and saturated solution then.The supplied materials greenhouse cooling adds 1 ‰ crystal seed amounts to 63-64 ℃, and mixing speed is 3-8rpm, and the back control that stirs is per hour lowered the temperature 1-2 ℃.
Ten, centrifugal
Utilize the revolution rapidly of rotary drum to produce centrifugal force, material passes through the filter cloth of lining in rotary drum, with solid substance and liquid separation, thus the product after obtaining to separate.
Processing parameter:
Centrifuging temperature≤42 ℃, centrifugal rotational speed 1000-1200rpm
11, oven dry
Product after adopting vibra fluidized bed drying centrifugal.
Processing parameter:
1, air intake mixing temperature :≤90 ℃
2, material loading speed: about 1.0T/h
The positively effect that adopts this novel production technique of xylose is to reclaim in the hydrolyzed solution 50% sulfuric acid, and can reclaim spent acid, the salkali waste that produces in the ion exchange resin regeneration process, has not only saved the sulfuric acid consumption but also avoided environmental pollution.The shortcoming of equipment scaling in having solved and in the deacidifying process, improved usage ratio of equipment and work-ing life, reduced the content of ash in the hydrolyzed solution and acid, it is more to have solved ion-exchange deacidifying process intermediate ion exchange resin consumption simultaneously, equipment is more, investment is big, has increased acid and alkali consumption, has strengthened problems such as cost, save energy, cut down the consumption of energy, improved the quality of hydrolyzed solution simultaneously, and improved quality product accordingly.But maximum amplitude ground reduces operator's quantity and labour intensity, separation efficiency height, stable and reliable operation.
Embodiment
Producing wood sugar with corn cob is example, and concrete production technique is as follows:
One, pre-treatment
Owing to contain impurity such as ash content, colloid, pectin in the corn cob raw material, need carry out pre-treatment before the hydrolysis and remove impurity, at first utilize screen scarifier dust removal soil, foreign material in small, broken bits, the washing of employing rotary drum washer, dust, foreign material, pigment on the raw material corn cob are washed, make it to see true qualities, no-sundries.Each corn cob raw material 3.2T that throws adds 12m
30.1% dilute sulphuric acid is handled, and is pressurized to 0.05Mpa, behind the pressurize 60min, and the treatment solution of draining.Add 12 side's water treatments then, be pressurized to 0.05Mpa, behind the pressurize 30min, the treatment solution of draining.
Two, hydrolysis
Utilize the hydrolysis principle, with the pentosan in the corn cob at pressure 0.13Mpa, 12m
3Concentration is heat-insulation pressure keeping hydrolysis 120min under the sulfuric acid condition of 1.7-1.8%, is hydrolyzed into the xylose hydrolysis fluid of individual molecule, to reach the purpose of further production requirement.
Three, decolouring
Utilize the discoloring agent gac to remove pigment colloid and the nitrogenous thing of part in the hydrolyzed solution.
When 1, once decolouring, add the about 100kg/ still of the old charcoal of secondary decolourization, 80 ℃ of temperature stir insulation 20min;
2, during secondary decolourization, add new gac 100kg/ still, 80 ℃ of temperature stir insulation 30min;
When 3, decolouring for three times, add new gac 80kg/ still, 80 ℃ of temperature stir insulation 30min.
Four, electrodialysis
Electrodialysis is under the effect of DC electric field, and ion sees through selective ion exchange membrane and moves, and makes charged H
+And SO
4 2-Ion a kind of electrochemistry sepn process that part is separated from hydrolyzed solution.
Feeding temperature requires smaller or equal to 40 ℃, and flow velocity is 1.2m
3/ h.
Five, ion-exchange
Remove impurity such as organic acid in the material, mineral acid, ash, pigment, colloid with yin, yang ion exchange phase bonded method, improving its purity, and make the purification liquid glucose after the exchange reach evaporation and crystalline requirement.
Temperature is less than and equals 40 ℃ during material ion-exchange, and flow velocity is more than or equal to 15m
3/ h.
The primary ions exchange: the order that feed liquid enters ion exchange column is positive post, cloudy post, cloudy post, positive post.
The secondary ions exchange: the order that feed liquid enters ion exchange column is positive post, cloudy post, cloudy post.
Six, nanofiltration
Nanofiltration membrane separation is the process that material was through or was retained in film, is similar to screening process, reaches impurity and the isolating purposes of wood sugar such as water according to the size of membrane pore size, realizes the recovery of spent acid, salkali waste simultaneously.
Feeding temperature is less than and equals 40 ℃, and flow rate control is at 35m
3/ h cover, pressure is 2.7Mpa.
Seven, concentrate
Triple effect evaporation: material is uniformly distributed in each generating tube through dividing equipped system, becomes membranaceous from top to down to flow under the effect of the gravity of material and secondary steam, and the while evaporates with the heating steam generation heat exchange of generating tube outer wall, and material is concentrated.
Single-effect evaporation: material enters the effect body through the punishment in advance mouth, rises along the heating tubulation, descends along central circulating tube, the density official post material circulation that relies on the material temperature difference to produce, and evaporate.
Processing parameter:
1, vacuum tightness: 0.01-0.09Mpa
2, flow: 18-20m
3/ h
3, temperature: 65-90 ℃
Eight, fermentation
Owing to contain a small amount of glucose in the saccharification liquid, influence the crystallization and the quality product of wood sugar, can remove glucose by yeast fermentation.
Processing parameter:
1, leavening temperature: 37 ± 1 ℃
2, pH value=5-6
Nine, crystallization
Material becomes saturated solution through evaporation concentration, with the way of cooling, obtains crystal and saturated solution then.The supplied materials greenhouse cooling adds 1 ‰ crystal seed amounts to 63-64 ℃, and mixing speed is 3-6rpm, and the back control that stirs is per hour lowered the temperature 1 ℃.
Ten, centrifugal
Utilize the revolution rapidly of rotary drum to produce centrifugal force, material passes through the filter cloth of lining in rotary drum, with solid substance and liquid separation, thus the product after obtaining to separate.
Processing parameter:
Centrifuging temperature≤42 ℃, centrifugal rotational speed 1100-1200rpm
11, oven dry
Product after adopting vibra fluidized bed drying centrifugal.
Processing parameter:
1, air intake mixing temperature :≤90 ℃
2, material loading speed: about 1.0T/h.
Claims (1)
1, a kind of novel production technique of xylose, it is characterized in that using electrodialysis reclaim(ed) sulfuric acid technology, the cloth bag that the nanofiltration thickening equipment adopts, special nanofiltration membrane separation system concentrate the liquid in the xylose production process at normal temperatures, can remove water and other impurity in the product, and can reclaim spent acid, the salkali waste that produces in the ion exchange resin regeneration process, its producing and manufacturing technique:
(1) pre-treatment
Utilize screen scarifier dust removal soil, foreign material in small, broken bits, adopt the rotary drum washer washing, dust, foreign material, pigment on the raw material corn cob are washed, make it to see true qualities, no-sundries.Each corn cob raw material 3.2-3.5T that throws adds 12m
3The 0.05-0.15% dilute sulphuric acid is handled, and is pressurized to 0.04-0.06Mpa, behind the pressurize 40-80min, and the treatment solution of draining.Add 12m then
3Water treatment is pressurized to 0.04-0.06Mpa, behind the pressurize 10-30min, and the treatment solution of draining.
(2) hydrolysis
With the pentosan in the corn cob at pressure 0.11-0.15Mpa, 12m
3Concentration is heat-insulation pressure keeping hydrolysis 90-150min under the sulfuric acid condition of 1.4-2.0%, is hydrolyzed into the xylose hydrolysis fluid of individual molecule, and is standby;
(3) decolouring
Utilize the discoloring agent gac to remove pigment colloid and the nitrogenous thing of part in the hydrolyzed solution;
When once decolouring, add the about 100kg/ still of the old charcoal of secondary decolourization, temperature 70-80 ℃, stir insulation 20-40min;
During secondary decolourization, add new gac 80-120kg/ still, temperature 70-80 ℃, stir insulation 20-40min;
During three decolourings, add new gac 60-100kg/ still, temperature 70-80 ℃, stir insulation 20-40min;
(4) electrodialysis
Electrodialysis is under the effect of DC electric field, and ion sees through selective ion exchange membrane and moves, and makes charged H
+And SO
4 2-Ion a kind of electrochemistry sepn process that part is separated from hydrolyzed solution;
Feeding temperature requires smaller or equal to 40 ℃, and flow velocity is 1.0-1.6m
3/ h;
(5) ion-exchange
Temperature is less than and equals 40 ℃ during material ion-exchange, and flow velocity is more than or equal to 15m
3/ h; The primary ions exchange: the order that feed liquid enters ion exchange column is positive post, cloudy post, cloudy post, positive post.The secondary ions exchange: the order that feed liquid enters ion exchange column is positive post, cloudy post, cloudy post;
(6) nanofiltration
The nanofiltration membrane separation feeding temperature is less than and equals 40 ℃, and flow rate control is at 35m
3/ h cover, pressure is 2.5-3.0Mpa;
(7) concentrate
Triple effect evaporation and single-effect evaporation:
Processing parameter:
Vacuum tightness: 0.01-0.09Mpa
Flow: 16-22m
3/ h
Temperature: 50-95 ℃
(8) fermentation
Owing to contain a small amount of glucose in the saccharification liquid, influence the crystallization and the quality product of wood sugar, can remove glucose by yeast fermentation;
Processing parameter:
Leavening temperature: 37 ± 1 ℃
PH value=4-7
(9) crystallization
Material becomes saturated solution through evaporation concentration, with the way of cooling, obtains crystal and saturated solution then, and the supplied materials greenhouse cooling adds 1 ‰ crystal seed amounts to 63-64 ℃, and mixing speed is 3-8rpm, and the back control that stirs is per hour lowered the temperature 1-2 ℃;
(10) centrifugal
Utilize the revolution rapidly of rotary drum to produce centrifugal force, material passes through the filter cloth of lining in rotary drum, with solid substance and liquid separation, thus the product after obtaining to separate;
Processing parameter:
Centrifuging temperature≤42 ℃, centrifugal rotational speed 1000-1200rpm
(11) oven dry
Product after adopting vibra fluidized bed drying centrifugal;
Processing parameter:
Air intake mixing temperature :≤90 ℃
Material loading speed: about 1.0T/h.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200710112975 CN101392009B (en) | 2007-09-21 | 2007-09-21 | Novel production technique of xylose |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200710112975 CN101392009B (en) | 2007-09-21 | 2007-09-21 | Novel production technique of xylose |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101392009A true CN101392009A (en) | 2009-03-25 |
| CN101392009B CN101392009B (en) | 2011-05-11 |
Family
ID=40492541
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200710112975 Active CN101392009B (en) | 2007-09-21 | 2007-09-21 | Novel production technique of xylose |
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| Country | Link |
|---|---|
| CN (1) | CN101392009B (en) |
Cited By (22)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101824054B (en) * | 2009-06-30 | 2012-01-04 | 山东福田药业有限公司 | Xylose production and purification process |
| CN102534053A (en) * | 2011-12-23 | 2012-07-04 | 甘肃赫原生物制品有限公司 | Method for improving xylose crystallization yield |
| CN102559944A (en) * | 2012-01-30 | 2012-07-11 | 黑龙江浩源生物科技有限公司 | Method for producing xylose |
| CN102586496A (en) * | 2012-03-26 | 2012-07-18 | 山东福田药业有限公司 | Process for producing xylose |
| CN101705313B (en) * | 2009-10-21 | 2012-07-25 | 安徽丰原发酵技术工程研究有限公司 | Method for removing catalysts from polypentaose-containing plant acidolysis solution |
| CN102676707A (en) * | 2012-05-16 | 2012-09-19 | 成都连接流体分离科技有限公司 | Efficient and energy-saving xylose producing process |
| CN102703613A (en) * | 2012-06-26 | 2012-10-03 | 山东福田药业有限公司 | Xylose hydrolysate preparation pre-treatment method for papermaking wastewater |
| CN101643795B (en) * | 2009-08-28 | 2013-01-02 | 长宁县泰宁化工有限公司 | Method for preparing xylose and xylitol by using bamboo |
| WO2013113323A1 (en) | 2012-01-31 | 2013-08-08 | Syral Belgium Nv | Process for extraction of pentose from ligno-cellulosic substrate |
| CN103509884A (en) * | 2012-06-29 | 2014-01-15 | 中国科学院宁波材料技术与工程研究所 | Method for preparing monosaccharide by using red alga biomass as raw material |
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| CN1640881A (en) * | 2004-01-12 | 2005-07-20 | 邾立能 | Process for preparing xylose |
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