CN103183744B - Using alkali proteinase method extracts the technique of high-purity heparin sodium from intestinal mucosa - Google Patents
Using alkali proteinase method extracts the technique of high-purity heparin sodium from intestinal mucosa Download PDFInfo
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Abstract
The present invention relates to technical field of heparin sodium production, provide a kind of using alkali proteinase method extracts high-purity heparin sodium technique from intestinal mucosa.Key step of the present invention is enzymolysis, absorption, washing, wash-out, precipitation, heavy molten redeposition and drying.The present invention is with short production cycle, and product yield is high, produces 100,000,000 international unit heparin sodium crudes and only needs about 1600 chitterlings; Decrease the discharge of intestines slag and waste water, be beneficial to environmental protection; Add heavy molten redeposition step, effectively can solve the alcohol of high density and elutriant and easily form salt-pepper noise and be mixed in heparin sodium product the problem causing product purity lower, product purity is high, the > 130U/mg that tires of heparin sodium.
Description
Technical field
The present invention relates to technical field of heparin sodium production, particularly a kind of using alkali proteinase method extracts the technique of high-purity heparin sodium from intestinal mucosa.
Background technology
Heparin sodium, also known as heparin, is a kind of natural anticoagulative substance of acid mucopolysaccharides containing sulfate.Heparin sodium is white or off-white powder, and odorless, tasteless has and draws moist, soluble in water, is insoluble to the organic solvents such as ethanol, acetone, dioxane.
Heparin sodium is extensively present in Mammals liver, lung, intestinal mucosa, how to become complex body to exist with protein bound.The separable heparin sodium of enzymolysis protein, heparin sodium is the mucopolysaccharide of sulfur acid, amino, glyconic acid.When pH8-9, electronegative, ion-exchange can be carried out with anionite, carry out roughing out, polysaccharide liquid precipitate in high concentration ethanol carry out consummate.Heparin sodium is antithrombotics best during blood chemistry measures.Heparin sodium is a kind of mucopolysaccharide of sulfur acid group, molecular weight is 1.5 ten thousand, and its anticoagulant mechanism is together with anti-freezing enzyme II, in lower concentration energy supressor Ⅸ a, effect between VIII and PF3, and antithrombin Ⅲ deactivation serine protease can be strengthened, thus zymoplasm is stoped to be formed; Also have the self-catalysis of Trombin inhibiting and the effect of supressor X.
The defect of the enzymolysis production method of traditional heparin sodium is: the production cycle is long, and energy consumption is large, and yield is low, produce 100,000,000 international unit heparin sodium crudes and need 2800-3000 root chitterlings, product purity is low, and tiring of heparin sodium is at most 80U/mg, and produce a large amount of intestines slags and waste water, contaminate environment.A kind of method utilizing bio-fermentation process to produce heparin sodium of the disclosure of the invention of CN1308088A.The method adopts 2709 proteolytic enzyme as catalyzer, and D204 strongly basic anion exchange resin as ion exchange resin, and adopts 150-180 order multilayer cloth screen to filter.The defect that the method exists is: product yield, purity are also lower, and produce a large amount of intestines slags and waste water, contaminate environment.
Summary of the invention
The object of the invention is to the above-mentioned defect overcoming prior art existence, provide a kind of using alkali proteinase method to extract the technique of high-purity heparin sodium from intestinal mucosa, with short production cycle, product yield, purity are high, decrease the discharge of intestines slag and waste water, are beneficial to environmental protection.
The technical solution adopted for the present invention to solve the technical problems is:
Using alkali proteinase method extracts a technique for high-purity heparin sodium from intestinal mucosa, and described processing step is as follows:
(1)
enzymolysis:pig intestinal mucosa slurries are added enzymatic vessel, pig intestinal mucosa slurries are pig intestinal mucosa: the mixture of the weight ratio of water=1:2.5-4, the sodium chloride solution adding salinity 21 °-24 ° in enzymatic vessel regulates salinity to 5 ± 0.5 ° of feed liquid in enzymatic vessel, controls the pH of feed liquid 8.5 ± 0.5; Then the enzyme amount adding 1.2 ± 0.4kg by every 1000L feed liquid adds 2709 Sumizyme MPs in enzymatic vessel, and control feed temperature at 53 ± 3 DEG C, salinity 4.2 ± 0.2 °, pH 7.0 ± 0.5 keeps 3 ± 0.5 hours; Finally be warming up to 85-88 DEG C, keep 20-25min to obtain enzymolysis solution, cross elimination residue.When the last enzymolysis solution of this step crosses elimination residue, often adopt Bag filter to remove residue, such efficiency is often lower, contriver, by practical exploration, has invented and has adopted vibratory screening apparatus to cross the mode of elimination residue, substantially increased filtration velocity, improve production efficiency, is the good method replacing Bag filter.
(2)
absorption:enzymolysis solution is inputted adsorption tanks, is cooled to 57 ± 3 DEG C, add water and regulate salinity to 3.0 ± 0.5 °, control pH 7.0-7.5, adds the amount of resin of 3-8kg by every 1000L enzymolysis solution, add ROHM AND HAAS FPA98CL type resin in adsorption tanks, after whip attachment 6-8 hour, collect resin.
(3)
washing:the resin of collection is washed with water to pH for neutral, then resin is put into the sodium chloride solution of salinity 4 ± 1 °, temperature 55-60 DEG C, stir and wash at least 1 hour, wherein, resin: sodium chloride solution=1:1.3-1.7(w/v); Control sodium chloride solution temperature at 55-60 DEG C, be convenient to the dirt settling of resin surface lipid to clean up, be convenient to wash-out.
(4)
wash-out:resin after step (3) being washed is poured in wash-out tank and is carried out twice wash-out, wherein, first time, wash-out was: resin joined salinity is 21 ± 1 °, stir at least 3 hours, resin in the sodium chloride solution of temperature 55-60 DEG C: sodium chloride solution=1:1-1.4(w/v); Second time wash-out is: the resin after first time wash-out joined salinity is 21 ± 1 °, stir at least 3 hours, resin in the sodium chloride solution of temperature 55-60 DEG C: sodium chloride solution=1:0.8-1.2(w/v); Merge the elutriant of twice collection; Sodium chloride solution temperature when controlling twice wash-out wash-out, at 55-60 DEG C, is convenient to sebaceous heparin sodium to elute from resin, increases yield.
(5)
precipitation:the elutriant that step (4) is collected is poured in setting tank, in setting tank, the alcohol of alcoholic strength 85 ± 5 ° is added under agitation condition, alcohol consumption is as the criterion to 45 °-60 ° with the alcoholic strength of surveying mixed solution in setting tank, staticly settles more than 15 hours, collecting precipitation thing.
(6)
heavy molten redeposition:by throw out: the weight ratio mixing of water=1:8-10, fully dissolve and form throw out solution, in throw out solution, add casing special-purpose salt, stir, the consumption of casing special-purpose salt is the 1-3% of throw out solution quality; The alcohol adding alcoholic strength 85 ± 5 ° again precipitates again, and alcohol consumption is as the criterion to 45 °-60 ° with the alcoholic strength of surveying mixed solution in setting tank, staticly settles more than 15 hours, collecting precipitation thing.
(7)
dry:the alcohol that the throw out that step (6) is collected adds alcoholic strength more than 85 ° carries out dehydration 1-3 hour, does drying and processing and namely obtain heparin sodium product after being filtered dry.
W/v in the present invention is that mass volume ratio is specially: kg:L.
The present invention is raw material with pig intestinal mucosa, and by Optimization Technology, prepare heparin sodium, yield is high, produces 100,000,000 international unit heparin sodium crudes and only needs about 1600 chitterlings.
During the heavy i.e. settling step of the wine of existing heparin sodium production process, the alcohol of high density and elutriant easily form salt-pepper noise and are mixed in heparin sodium product, alcohol and the elutriant of high density easily form salt-pepper noise and are not easy found from heparin sodium product and be separated, and greatly reduce the purity of heparin sodium product like this.The present invention, by adding heavy molten redeposition step, effectively can solve the alcohol of high density and elutriant and easily form salt-pepper noise and be mixed in heparin sodium product the problem causing product purity lower.Heparin sodium product purity after process of the present invention is significantly improved, the > 130U/mg that tires of heparin sodium.
As preferably, step (1) processes the enzymolysis solution that obtains under the rotating speed of 6000-8000 rev/min, after centrifugal treating 20-40min, then enters next step absorption.
Milkiness shape liquid is obtained after enzymolysis; whizzer is entered after elimination residue; start whizzer; enzymolysis solution is under centrifugal action, and after making milkiness shape enzymolysis solution enter centrifuge drum, solid particulate or the larger liquid (containing albumen) of density are to rotatory drum wall sedimentation; form sediment; the heparin sodium decomposed solution that density is less is assembled to rotary drum center position, flow to overflow port and discharges, become parting liquid.Sediment is squeezed out sediment by worm drive from slag-drip opening, parting liquid is discharged from discharge port by whizzer, is transported in adsorption tanks and carries out next step resin absorption operation.
In decomposition workshop section, directly remove partial impurities after increasing this step, make the resin energy fully adsorbing liquaemin in absorption process, improve resin absorption validity.In decomposition process, directly carry out the separation of impurity, improve the purity of the finished product.Control centrifugal speed and time, ensure the effect of centrifugation.
As preferably, after step (2) is collected resin, remaining feed liquid is delivered to adsorption tanks again, control temperature is at 57 ± 3 DEG C, pH 7.0-7.5, the amount of resin adding 2-3kg by every 1000L feed liquid adds after ROHM AND HAAS FPA98CL type resin adsorbs 6-8 hour again in adsorption tanks, collect resin, after the resin then collected with step (2) merges, enter next step washing step.
Feed liquid after resin absorption is re-started absorption by this step, can improve the yield of heparin sodium, cut the waste, and can reduce the content of albumen in waste liquid simultaneously, be beneficial to wastewater treatment.
As preferably, re-use after the resin activated process of described ROHM AND HAAS FPA98CL type, activation treatment is: resin 50-60 DEG C warm water soaking is rinsed well with clear water after more than 20 hours and drained, add again mass concentration be 10% sodium hydroxide solution stir more than 1 hour, it is neutral for finally rinsing to washing lotion pH with clear water, and the add-on of described sodium hydroxide solution is the gauge that every kilogram resin adds 1L sodium hydroxide solution; Resin after activation is under the rotating speed of 4000-5000 rev/min, and centrifugal treating 10-30min, is used further to absorption.
Resin to be used after activation treatment is entered whizzer by whizzer opening for feed.Start whizzer, resin is under the rotating speed effect of 4000-5000 rev/min, and after resin enters centrifuge drum, solid particulate resin, to rotatory drum wall sedimentation, sticks in bulging wall.The liquid that centrifugation throws away or the less material of density are assembled to rotary drum center position, flow to overflow port and discharge, become refuse.Collect the resin staying bulging wall, prepare to be used for absorption process.In this step resin hole, moisture is fully dried, and to increase the adsorption space of resin, improves the adsorptive power of resin.
As preferably, enter step (5) precipitation after the elutriant that step (4) is collected enters ultrafilter ultrafiltration again, the ultra-filtration membrane aperture of ultrafilter is at 0.45 μm-0.6 μm.
Through ultrafiltration, the waste water in elutriant and impurity can be got rid of, effectively improve the purity of product, and the alcohol usage quantity that next step wine sinks in technique can be reduced, cost-saving.
As preferably, the elutriant that step (4) is collected, under the rotating speed of 8000-10000 rev/min, after centrifugal treating 10-20min, then enters step (5) precipitation.
Elutriant is entered whizzer by whizzer opening for feed; start whizzer; elutriant decomposed solution centrifugal force (8000-10000 rev/min) effect under; after making milkiness shape elutriant enter centrifuge drum; solid particulate or the larger liquid (containing albumen) of density are to rotatory drum wall sedimentation, and form sediment, the heparin sodium elutriant that density is less is assembled to rotary drum center position; flow to overflow port to discharge, become parting liquid.Sediment is squeezed out sediment by worm drive from slag-drip opening, parting liquid is discharged from discharge port by whizzer, is transported in setting tank and carries out next step alcohol precipitation operation.This step increases the operation centrifugal to elutriant, thus directly removes partial impurities and albumen in elution procedure, thus the purity of raising the finished product, and can reduce the alcohol usage quantity that next step wine sinks in technique, cost-saving.
As preferably, after step (5) collecting precipitation thing, remaining supernatant liquor inputs in another sky setting tank, in another sky setting tank, add saturated nacl aqueous solution stir, and regulate pH to be 9-10, the volume ratio of supernatant liquor and saturated nacl aqueous solution is 1:0.5-0.7, after staticly settling 8-12 hour, collecting precipitation, enters next step the molten redeposition of weight after the throw out then collected with step (5) merges.
This step first time wine is sunk after supernatant liquor again carry out wine and sink, effectively can improve the yield of heparin sodium, cut the waste, be beneficial to wastewater treatment.
As preferably, the temperature of step (7) drying and processing is 60-80 DEG C.
As preferably, collect step (1) enzymolysis solution and filter the residue obtained, the sodium chloride solution of salinity 5 ± 0.5 ° is added in enzymatic vessel, then residue is rejoined in enzymatic vessel, the weight ratio of the sodium chloride solution of residue and salinity 5 ± 0.5 ° is 1:5-6, controls the pH of feed liquid 8.5 ± 0.5, and the enzyme amount then adding 1.0-1.2kg by every 1000L feed liquid adds 2709 Sumizyme MPs in enzymatic vessel, control feed temperature at 55 ± 1 DEG C, insulation 6-7 hour; Finally be warming up to 88-90 DEG C, keep 20-25min, then obtain enzymolysis solution after leaving standstill 20-30min, enzymolysis solution, under the rotating speed of 6000-8000 rev/min, after centrifugal treating 20-40min, enters next step absorption.
In existing technique, the remaining residue of enzymolysis and intestines slag are often given it up, so comparatively waste and add the burden of environment.And the present inventor is through practical exploration for many years, invent the processing step that effectively recycles residue, by the enzymolysis processing again to residue, can further residue decomposition, extract heparin sodium, add the yield of heparin sodium, decrease waste discharge, be beneficial to environmental protection.
The invention has the beneficial effects as follows:
1, prepare heparin sodium by Optimization Technology, yield is high, produces 100,000,000 international unit heparin sodium crudes and only needs about 1600 chitterlings.
2, add heavy molten redeposition step, effectively can solve the alcohol of high density and elutriant and easily form salt-pepper noise and be mixed in heparin sodium product the problem causing product purity lower, product purity is high, the > 130U/mg that tires of heparin sodium.
3, the enzymolysis and extraction again of residue, can further residue decomposition, extracts heparin sodium, adds the yield of heparin sodium, decrease waste discharge, be beneficial to environmental protection.
Embodiment
Below by specific embodiment, technical scheme of the present invention is described in further detail.
In the present invention, if not refer in particular to, the raw material adopted and equipment etc. all can be buied from market or this area is conventional.Method in following embodiment, if no special instructions, is the ordinary method of this area.
Resin activated process:
By new ROHM AND HAAS FPA98CL type resin (commercially available import resin, dealer Beijing Bosaisi Biotech. Co., Ltd.) to rinse well with clear water after 20 hours with 50 DEG C of warm water soaking and to drain, add again mass concentration be 10% sodium hydroxide solution stir more than 1 hour, it is neutral for finally rinsing to washing lotion pH with clear water, and the add-on of described sodium hydroxide solution is the gauge that every kilogram resin adds 1L sodium hydroxide solution.Research shows, the warm water temperature adopted in resin activated process is between 50-60 DEG C, and soak time, between 16-24 hour, is equivalent to the activation treatment effect of resin, does not do repeating one by one at this.Resin after activation is under the rotating speed of 4000-5000 rev/min, and centrifugal treating 10-30min, is used further to absorption.
Embodiment 1:
(1)
enzymolysis:2000L pig intestinal mucosa slurries (being obtained through archenteron-scrapping machine process by chitterlings) are added enzymatic vessel, pig intestinal mucosa slurries are pig intestinal mucosa: the mixture of the weight ratio of water=1:2.5, the sodium chloride solution adding salinity 21 ° in enzymatic vessel regulates salinity to 5 ± 0.5 ° of feed liquid in enzymatic vessel, controls the pH of feed liquid about 8; Then the enzyme amount adding 0.8kg by every 1000L feed liquid adds 2709 Sumizyme MPs in enzymatic vessel, and control feed temperature at 56 DEG C, salinity 4.2 ± 0.2 °, pH 6.5 keeps 2.5 hours; Finally be warming up to 85 DEG C, keep 25min to obtain enzymolysis solution, cross elimination residue; Then enzymolysis solution is under the rotating speed of 6000 revs/min, after centrifugal treating 40min, then enters next step absorption.
Collect enzymolysis solution and filter the residue obtained, the sodium chloride solution of salinity 5 ± 0.5 ° is added in enzymatic vessel, then residue is rejoined in enzymatic vessel, the weight ratio of the sodium chloride solution of residue and salinity 5 ± 0.5 ° is 1:5, control the pH of feed liquid about 8, then the enzyme amount adding 1.0kg by every 1000L feed liquid adds 2709 Sumizyme MPs in enzymatic vessel, controls feed temperature at 56 DEG C, is incubated 6 hours; Finally be warming up to 88 DEG C, keep 25min, then obtain enzymolysis solution after leaving standstill 30min, enzymolysis solution, under the rotating speed of 6000 revs/min, after centrifugal treating 40min, enters next step absorption.
(2)
absorption:enzymolysis solution is inputted adsorption tanks, is cooled to 54 DEG C, add water and regulate salinity to 3.0 ± 0.5 °, control pH 7.0, adds the amount of resin of 3kg by every 1000L enzymolysis solution, add ROHM AND HAAS FPA98CL type resin in adsorption tanks, and whip attachment, after 8 hours, collects resin; Feed liquid remaining after collection resin is delivered to adsorption tanks again, control temperature is at 54 DEG C, pH 7.0, the amount of resin adding 2kg by every 1000L feed liquid adds after ROHM AND HAAS FPA98CL type resin adsorbs 8 hours again in adsorption tanks, collect resin, then, after the resin collected with absorption enzymolysis solution merges, next step washing step is entered.
(3)
washing:the resin of collection is washed with water to pH for neutral, then resin is put into the sodium chloride solution of salinity 4 ± 1 °, temperature 55 DEG C, stir and wash for 3 hours, wherein, resin: sodium chloride solution=1:1.3(w/v);
(4)
wash-out:resin after step (3) being washed is poured in wash-out tank and is carried out twice wash-out, wherein, first time wash-out be: resin joined salinity is 21 ± 1 °, stir 5 hours in the sodium chloride solution of temperature 55 DEG C, resin: sodium chloride solution=1:1(w/v); Second time wash-out is: the resin after first time wash-out joined salinity is 21 ± 1 °, stir 5 hours in the sodium chloride solution of temperature 55 DEG C, resin: sodium chloride solution=1:0.8(w/v); Merge the elutriant of twice collection;
Enter next step precipitation after the elutriant collected enters ultrafilter ultrafiltration again, the ultra-filtration membrane aperture of ultrafilter is at 0.45 μm-0.6 μm.
(5)
precipitation:poured into by elutriant in setting tank, add the alcohol of alcoholic strength 80 ° under agitation condition in setting tank, alcohol consumption is as the criterion to 45 ° with the alcoholic strength of surveying mixed solution in setting tank, staticly settles 20 hours, collecting precipitation thing; After collecting precipitation thing, remaining supernatant liquor inputs in another sky setting tank, in another sky setting tank, add saturated nacl aqueous solution stir, and regulate pH to be 9, the volume ratio of supernatant liquor and saturated nacl aqueous solution is 1:0.5, after staticly settling 12 hours, collecting precipitation, then precipitates the molten redeposition of weight entering next step after the throw out obtained merges with elutriant.
(6)
heavy molten redeposition:by throw out: the weight ratio mixing of water=1:8, fully dissolve and form throw out solution, in throw out solution, add casing special-purpose salt, stir, the consumption of casing special-purpose salt is 1% of throw out solution quality; The alcohol adding alcoholic strength 80 ° again precipitates again, and alcohol consumption is as the criterion to 45 ° with the alcoholic strength of surveying mixed solution in setting tank, staticly settles 20 hours, collecting precipitation thing.
(7)
dry:the alcohol adding alcoholic strength 85 ° to throw out carries out dehydration 3 hours, is filtered dry latter 60 DEG C and dries and obtain heparin sodium product.
After testing, produce 100,000,000 international unit heparin sodium crudes and only need about 1600 chitterlings, the > 130U/mg that tires of heparin sodium.
Embodiment 2:
(1)
enzymolysis:1000L pig intestinal mucosa slurries (being obtained through archenteron-scrapping machine process by chitterlings) are added enzymatic vessel, pig intestinal mucosa slurries are pig intestinal mucosa: the mixture of the weight ratio of water=1:4, the sodium chloride solution adding salinity 24 ° in enzymatic vessel regulates salinity to 5 ± 0.5 ° of feed liquid in enzymatic vessel, controls the pH of feed liquid about 9; Then the enzyme amount adding 1.6kg by every 1000L feed liquid adds 2709 Sumizyme MPs in enzymatic vessel, and control feed temperature at 50 DEG C, salinity 4.2 ± 0.2 °, pH 7. 5 keeps 3.5 hours; Finally be warming up to 88 DEG C, keep 20min to obtain enzymolysis solution, cross elimination residue; Then enzymolysis solution is under the rotating speed of 8000 revs/min, after centrifugal treating 20min, then enters next step absorption.
Collect enzymolysis solution and filter the residue obtained, the sodium chloride solution of salinity 5 ± 0.5 ° is added in enzymatic vessel, then residue is rejoined in enzymatic vessel, the weight ratio of the sodium chloride solution of residue and salinity 5 ± 0.5 ° is 1:6, control the pH of feed liquid about 9, then the enzyme amount adding 1.2kg by every 1000L feed liquid adds 2709 Sumizyme MPs in enzymatic vessel, controls feed temperature at 54 DEG C, is incubated 7 hours; Finally be warming up to 90 DEG C, keep 20min, then obtain enzymolysis solution after leaving standstill 20min, enzymolysis solution, under the rotating speed of 8000 revs/min, after centrifugal treating 20min, enters next step absorption.
(2)
absorption:enzymolysis solution is inputted adsorption tanks, is cooled to 60 DEG C, add water and regulate salinity to 3.0 ± 0.5 °, control pH7.5, adds the amount of resin of 8kg by every 1000L enzymolysis solution, add ROHM AND HAAS FPA98CL type resin in adsorption tanks, and whip attachment, after 6 hours, collects resin; Feed liquid remaining after collection resin is delivered to adsorption tanks again, control temperature is at 60 DEG C, pH 7.5, the amount of resin adding 3kg by every 1000L feed liquid adds after ROHM AND HAAS FPA98CL type resin adsorbs 6 hours again in adsorption tanks, collect resin, then, after the resin collected with absorption enzymolysis solution merges, next step washing step is entered.
(3)
washing:the resin of collection is washed with water to pH for neutral, then resin is put into the sodium chloride solution of salinity 4 ± 1 °, temperature 60 C, stir and wash for 1 hour, wherein, resin: sodium chloride solution=1:1.7(w/v);
(4)
wash-out:resin after step (3) being washed is poured in wash-out tank and is carried out twice wash-out, wherein, first time wash-out be: resin joined salinity is 21 ± 1 °, stir 3 hours in the sodium chloride solution of temperature 60 C, resin: sodium chloride solution=1:1.4(w/v); Second time wash-out is: the resin after first time wash-out joined salinity is 21 ± 1 °, stir 3 hours in the sodium chloride solution of temperature 60 C, resin: sodium chloride solution=1:1.2(w/v); Merge the elutriant of twice collection;
The elutriant collected, under the rotating speed of 8000 revs/min, after centrifugal treating 20min, then enters next step precipitation.
(5)
precipitation:poured into by elutriant in setting tank, add the alcohol of alcoholic strength 90 ° under agitation condition in setting tank, alcohol consumption is as the criterion to 60 ° with the alcoholic strength of surveying mixed solution in setting tank, staticly settles 15 hours, collecting precipitation thing; After collecting precipitation thing, remaining supernatant liquor inputs in another sky setting tank, in another sky setting tank, add saturated nacl aqueous solution stir, and regulate pH to be 10, the volume ratio of supernatant liquor and saturated nacl aqueous solution is 1:0.7, after staticly settling 8 hours, collecting precipitation, then precipitates the molten redeposition of weight entering next step after the throw out obtained merges with elutriant.
(6)
heavy molten redeposition:by throw out: the weight ratio mixing of water=1:10, fully dissolve and form throw out solution, in throw out solution, add casing special-purpose salt, stir, the consumption of casing special-purpose salt is 3% of throw out solution quality; The alcohol adding alcoholic strength 90 ° again precipitates again, and alcohol consumption is as the criterion to 60 ° with the alcoholic strength of surveying mixed solution in setting tank, staticly settles 15 hours, collecting precipitation thing.
(7)
dry:the alcohol adding alcoholic strength 90 ° to throw out carries out dehydration 1 hour, is filtered dry latter 80 DEG C and dries and obtain heparin sodium product.
After testing, produce 100,000,000 international unit heparin sodium crudes and only need about 1600 chitterlings, the > 130U/mg that tires of heparin sodium.
Embodiment 3:
(1)
enzymolysis:1500L pig intestinal mucosa slurries (being obtained through archenteron-scrapping machine process by chitterlings) are added enzymatic vessel, pig intestinal mucosa slurries are pig intestinal mucosa: the mixture of the weight ratio of water=1:3, the sodium chloride solution adding salinity 22 ° in enzymatic vessel regulates salinity to 5 ± 0.5 ° of feed liquid in enzymatic vessel, controls the pH of feed liquid about 8.5; Then the enzyme amount adding 1.2kg by every 1000L feed liquid adds 2709 Sumizyme MPs in enzymatic vessel, and control feed temperature at 53 DEG C, salinity 4.2 ± 0.2 °, pH about 7.0 keeps 3 hours; Finally be warming up to 86 DEG C, keep 22min to obtain enzymolysis solution, cross elimination residue; Then enzymolysis solution is under the rotating speed of 7000 revs/min, after centrifugal treating 30min, then enters next step absorption.
Collect enzymolysis solution and filter the residue obtained, the sodium chloride solution of salinity 5 ± 0.5 ° is added in enzymatic vessel, then residue is rejoined in enzymatic vessel, the weight ratio of the sodium chloride solution of residue and salinity 5 ± 0.5 ° is 1:5.5, control the pH of feed liquid 8.5, then the enzyme amount adding 1.1kg by every 1000L feed liquid adds 2709 Sumizyme MPs in enzymatic vessel, controls feed temperature at 55 DEG C, is incubated 6.5 hours; Finally be warming up to 89 DEG C, keep 22min, then obtain enzymolysis solution after leaving standstill 25min, enzymolysis solution, under the rotating speed of 7000 revs/min, after centrifugal treating 30min, enters next step absorption.
(2)
absorption:enzymolysis solution is inputted adsorption tanks, is cooled to 57 DEG C, add water and regulate salinity to 3.0 ± 0.5 °, control pH about 7.0, adds the amount of resin of 5kg by every 1000L enzymolysis solution, add ROHM AND HAAS FPA98CL type resin in adsorption tanks, whip attachment, after 7 hours, collects resin; Feed liquid remaining after collection resin is delivered to adsorption tanks again, control temperature is at 57 DEG C, pH about 7.0, the amount of resin adding 2.5kg by every 1000L feed liquid adds after ROHM AND HAAS FPA98CL type resin adsorbs 7 hours again in adsorption tanks, collect resin, then, after the resin collected with absorption enzymolysis solution merges, next step washing step is entered.
(3)
washing:the resin of collection is washed with water to pH for neutral, then resin is put into the sodium chloride solution of salinity 4 ± 1 °, temperature 58 DEG C, stir and wash for 2 hours, wherein, resin: sodium chloride solution=1:1.5(w/v);
(4)
wash-out:resin after step (3) being washed is poured in wash-out tank and is carried out twice wash-out, wherein, first time wash-out be: resin joined salinity is 21 ± 1 °, stir 4 hours in the sodium chloride solution of temperature 58 DEG C, resin: sodium chloride solution=1:1.2(w/v); Second time wash-out is: the resin after first time wash-out joined salinity is 21 ± 1 °, stir 4 hours in the sodium chloride solution of temperature 58 DEG C, resin: sodium chloride solution=1:1(w/v); Merge the elutriant of twice collection;
The elutriant collected, under the rotating speed of 10000 revs/min, after centrifugal treating 10min, then enters next step precipitation.
(5)
precipitation:poured into by elutriant in setting tank, add the alcohol of alcoholic strength 85 ° under agitation condition in setting tank, alcohol consumption is as the criterion to 50 ° with the alcoholic strength of surveying mixed solution in setting tank, staticly settles 18 hours, collecting precipitation thing; After collecting precipitation thing, remaining supernatant liquor inputs in another sky setting tank, in another sky setting tank, add saturated nacl aqueous solution stir, and regulate pH to be 9, the volume ratio of supernatant liquor and saturated nacl aqueous solution is 1:0.6, after staticly settling 10 hours, collecting precipitation, then precipitates the molten redeposition of weight entering next step after the throw out obtained merges with elutriant.
(6)
heavy molten redeposition:by throw out: the weight ratio mixing of water=1:9, fully dissolve and form throw out solution, in throw out solution, add casing special-purpose salt, stir, the consumption of casing special-purpose salt is 2% of throw out solution quality; The alcohol adding alcoholic strength 85 ° again precipitates again, and alcohol consumption is as the criterion to 50 ° with the alcoholic strength of surveying mixed solution in setting tank, staticly settles 18 hours, collecting precipitation thing.
(7)
dry:the alcohol adding alcoholic strength 85 ° to throw out carries out dehydration 2 hours, is filtered dry latter 70 DEG C and dries and obtain heparin sodium product.
After testing, produce 100,000,000 international unit heparin sodium crudes and only need about 1600 chitterlings, the > 130U/mg that tires of heparin sodium.
Above-described embodiment is one of the present invention preferably scheme, not does any pro forma restriction to the present invention, also has other variant and remodeling under the prerequisite not exceeding the technical scheme described in claim.
Claims (5)
1. using alkali proteinase method extracts a technique for high-purity heparin sodium from intestinal mucosa, it is characterized in that: described processing step is as follows:
(1)
enzymolysis:pig intestinal mucosa slurries are added enzymatic vessel, pig intestinal mucosa slurries are pig intestinal mucosa: the mixture of the weight ratio of water=1:2.5-4, the sodium chloride solution adding salinity 21 °-24 ° in enzymatic vessel regulates salinity to 5 ± 0.5 ° of feed liquid in enzymatic vessel, controls the pH of feed liquid 8.5 ± 0.5; Then the enzyme amount adding 1.2 ± 0.4kg by every 1000L feed liquid adds 2709 Sumizyme MPs in enzymatic vessel, and control feed temperature at 53 ± 3 DEG C, salinity 4.2 ± 0.2 °, pH 7.0 ± 0.5 keeps 3 ± 0.5 hours; Finally be warming up to 85-88 DEG C, keep 20-25min to obtain enzymolysis solution, cross elimination residue;
(2)
absorption:enzymolysis solution is inputted adsorption tanks, is cooled to 57 ± 3 DEG C, add water and regulate salinity to 3.0 ± 0.5 °, control pH 7.0-7.5, adds the amount of resin of 3-8kg by every 1000L enzymolysis solution, add ROHM AND HAAS FPA98CL type resin in adsorption tanks, after whip attachment 6-8 hour, collect resin;
(3)
washing:the resin of collection is washed with water to pH for neutral, then resin is put into the sodium chloride solution of salinity 4 ± 1 °, temperature 55-60 DEG C, stir and wash at least 1 hour, wherein, resin: sodium chloride solution=1kg:1.3-1.7L;
(4)
wash-out:resin after step (3) being washed is poured in wash-out tank and is carried out twice wash-out, wherein, first time, wash-out was: resin joined salinity is 21 ± 1 °, stir at least 3 hours, resin in the sodium chloride solution of temperature 55-60 DEG C: sodium chloride solution=1kg:1-1.4L; Second time wash-out is: the resin after first time wash-out joined salinity is 21 ± 1 °, stir at least 3 hours, resin in the sodium chloride solution of temperature 55-60 DEG C: sodium chloride solution=1kg:0.8-1.2L; Merge the elutriant of twice collection;
(5)
precipitation:the elutriant that step (4) is collected is poured in setting tank, in setting tank, the alcohol of alcoholic strength 85 ± 5 ° is added under agitation condition, alcohol consumption is as the criterion to 45 °-60 ° with the alcoholic strength of surveying mixed solution in setting tank, staticly settles more than 15 hours, collecting precipitation thing;
(6)
heavy molten redeposition:by throw out: the weight ratio mixing of water=1:8-10, fully dissolve and form throw out solution, in throw out solution, add casing special-purpose salt, stir, the consumption of casing special-purpose salt is the 1-3% of throw out solution quality; The alcohol adding alcoholic strength 85 ± 5 ° again precipitates again, and alcohol consumption is as the criterion to 45 °-60 ° with the alcoholic strength of surveying mixed solution in setting tank, staticly settles more than 15 hours, collecting precipitation thing;
(7)
dry:the alcohol that the throw out that step (6) is collected adds alcoholic strength more than 85 ° carries out dehydration 1-3 hour, does drying and processing and namely obtain heparin sodium product after being filtered dry;
Step (1) processes the enzymolysis solution that obtains under the rotating speed of 6000-8000 rev/min, after centrifugal treating 20-40min, then enters next step absorption; After step (2) is collected resin, remaining feed liquid is delivered to adsorption tanks again, control temperature is at 57 ± 3 DEG C, pH 7.0-7.5, the amount of resin adding 2-3kg by every 1000L feed liquid adds after ROHM AND HAAS FPA98CL type resin adsorbs 6-8 hour again in adsorption tanks, collect resin, then, after the resin collected with step (2) merges, next step washing step is entered; After step (5) collecting precipitation thing, remaining supernatant liquor inputs in another sky setting tank, in another sky setting tank, add saturated nacl aqueous solution stir, and regulate pH to be 9-10, the volume ratio of supernatant liquor and saturated nacl aqueous solution is 1:0.5-0.7, after staticly settling 8-12 hour, collecting precipitation, enters next step the molten redeposition of weight after the throw out then collected with step (5) merges; Collect step (1) enzymolysis solution and filter the residue obtained, the sodium chloride solution of salinity 5 ± 0.5 ° is added in enzymatic vessel, then residue is rejoined in enzymatic vessel, the weight ratio of the sodium chloride solution of residue and salinity 5 ± 0.5 ° is 1:5-6, control the pH of feed liquid 8.5 ± 0.5, then the enzyme amount adding 1.0-1.2kg by every 1000L feed liquid adds 2709 Sumizyme MPs in enzymatic vessel, controls feed temperature at 55 ± 1 DEG C, insulation 6-7 hour; Finally be warming up to 88-90 DEG C, keep 20-25min, then obtain enzymolysis solution after leaving standstill 20-30min, enzymolysis solution, under the rotating speed of 6000-8000 rev/min, after centrifugal treating 20-40min, enters next step absorption.
2. using alkali proteinase method according to claim 1 extracts the technique of high-purity heparin sodium from intestinal mucosa, it is characterized in that: re-use after the resin activated process of described ROHM AND HAAS FPA98CL type, activation treatment is: resin 50-60 DEG C warm water soaking is rinsed well with clear water after more than 20 hours and drained, add again mass concentration be 10% sodium hydroxide solution stir more than 1 hour, it is neutral for finally rinsing to washing lotion pH with clear water, and the add-on of described sodium hydroxide solution is the gauge that every kilogram resin adds 1L sodium hydroxide solution; Resin after activation is under the rotating speed of 4000-5000 rev/min, and centrifugal treating 10-30min, is used further to absorption.
3. using alkali proteinase method according to claim 1 extracts the technique of high-purity heparin sodium from intestinal mucosa, it is characterized in that: enter step (5) precipitation after the elutriant that step (4) is collected enters ultrafilter ultrafiltration again, the ultra-filtration membrane aperture of ultrafilter is at 0.45 μm-0.6 μm.
4. using alkali proteinase method according to claim 1 extracts the technique of high-purity heparin sodium from intestinal mucosa, it is characterized in that: the elutriant that step (4) is collected is under the rotating speed of 8000-10000 rev/min, after centrifugal treating 10-20min, then enter step (5) precipitation.
5. using alkali proteinase method according to claim 1 extracts the technique of high-purity heparin sodium from intestinal mucosa, it is characterized in that: the temperature of step (7) drying and processing is 60-80 DEG C.
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| CN103848929B (en) * | 2014-03-21 | 2016-08-17 | 广元市申达实业有限公司 | A kind of high efficiency extraction technique of heparin sodium |
| CN104086672A (en) * | 2014-06-10 | 2014-10-08 | 安徽申奥生物科技有限公司 | Preparation method of heparin sodium crude product |
| CN104119457A (en) * | 2014-07-07 | 2014-10-29 | 广元市海天实业有限责任公司 | Heparin sodium and dermatan sulfate combined production process |
| CN104910295A (en) * | 2015-07-06 | 2015-09-16 | 丰润生物科技有限公司 | Method for improving potency of heparin sodium |
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| EP0261088A3 (en) * | 1986-09-19 | 1989-02-01 | Farmaceutici Damor S.p.A. | Process for the production of heparanlysopeptide sulphate, the product thus obtained and its therapeutic use |
| CN101864002A (en) * | 2010-06-21 | 2010-10-20 | 广元市海天实业有限责任公司 | Method for extracting sodium heparin |
| CN101914170A (en) * | 2010-08-19 | 2010-12-15 | 郓城绅联生物科技有限公司 | Preparation method for producing sodium heparin by using small sheep intestines |
| CN102229681A (en) * | 2011-06-22 | 2011-11-02 | 郓城绅联生物科技有限公司 | Preparation method for producing heparin sodium by using porcine small intestines |
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| EP0261088A3 (en) * | 1986-09-19 | 1989-02-01 | Farmaceutici Damor S.p.A. | Process for the production of heparanlysopeptide sulphate, the product thus obtained and its therapeutic use |
| CN101864002A (en) * | 2010-06-21 | 2010-10-20 | 广元市海天实业有限责任公司 | Method for extracting sodium heparin |
| CN101914170A (en) * | 2010-08-19 | 2010-12-15 | 郓城绅联生物科技有限公司 | Preparation method for producing sodium heparin by using small sheep intestines |
| CN102229681A (en) * | 2011-06-22 | 2011-11-02 | 郓城绅联生物科技有限公司 | Preparation method for producing heparin sodium by using porcine small intestines |
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