CN1125230A - Process for extracting macrolide antibiotics - Google Patents
Process for extracting macrolide antibiotics Download PDFInfo
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- CN1125230A CN1125230A CN 95105997 CN95105997A CN1125230A CN 1125230 A CN1125230 A CN 1125230A CN 95105997 CN95105997 CN 95105997 CN 95105997 A CN95105997 A CN 95105997A CN 1125230 A CN1125230 A CN 1125230A
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- 238000000034 method Methods 0.000 title claims abstract description 19
- 239000003120 macrolide antibiotic agent Substances 0.000 title claims abstract description 13
- 238000000605 extraction Methods 0.000 claims abstract description 98
- ULGZDMOVFRHVEP-RWJQBGPGSA-N Erythromycin Chemical compound O([C@@H]1[C@@H](C)C(=O)O[C@@H]([C@@]([C@H](O)[C@@H](C)C(=O)[C@H](C)C[C@@](C)(O)[C@H](O[C@H]2[C@@H]([C@H](C[C@@H](C)O2)N(C)C)O)[C@H]1C)(C)O)CC)[C@H]1C[C@@](C)(OC)[C@@H](O)[C@H](C)O1 ULGZDMOVFRHVEP-RWJQBGPGSA-N 0.000 claims abstract description 30
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 20
- ACTOXUHEUCPTEW-BWHGAVFKSA-N 2-[(4r,5s,6s,7r,9r,10r,11e,13e,16r)-6-[(2s,3r,4r,5s,6r)-5-[(2s,4r,5s,6s)-4,5-dihydroxy-4,6-dimethyloxan-2-yl]oxy-4-(dimethylamino)-3-hydroxy-6-methyloxan-2-yl]oxy-10-[(2s,5s,6r)-5-(dimethylamino)-6-methyloxan-2-yl]oxy-4-hydroxy-5-methoxy-9,16-dimethyl-2-o Chemical compound O([C@H]1/C=C/C=C/C[C@@H](C)OC(=O)C[C@@H](O)[C@@H]([C@H]([C@@H](CC=O)C[C@H]1C)O[C@H]1[C@@H]([C@H]([C@H](O[C@@H]2O[C@@H](C)[C@H](O)[C@](C)(O)C2)[C@@H](C)O1)N(C)C)O)OC)[C@@H]1CC[C@H](N(C)C)[C@@H](C)O1 ACTOXUHEUCPTEW-BWHGAVFKSA-N 0.000 claims abstract description 15
- 239000004187 Spiramycin Substances 0.000 claims abstract description 15
- 229960001294 spiramycin Drugs 0.000 claims abstract description 15
- 229930191512 spiramycin Natural products 0.000 claims abstract description 15
- 235000019372 spiramycin Nutrition 0.000 claims abstract description 15
- 229960003276 erythromycin Drugs 0.000 claims abstract description 13
- 239000002904 solvent Substances 0.000 claims abstract description 10
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 56
- KBPLFHHGFOOTCA-UHFFFAOYSA-N caprylic alcohol Natural products CCCCCCCCO KBPLFHHGFOOTCA-UHFFFAOYSA-N 0.000 claims description 38
- 239000000706 filtrate Substances 0.000 claims description 20
- 239000007788 liquid Substances 0.000 claims description 20
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 claims description 17
- 239000003350 kerosene Substances 0.000 claims description 15
- 239000012074 organic phase Substances 0.000 claims description 14
- 229950007634 kitasamycin Drugs 0.000 claims description 13
- XYJOGTQLTFNMQG-KJHBSLKPSA-N leucomycin V Chemical compound CO[C@H]1[C@H](O)CC(=O)O[C@H](C)C\C=C\C=C\[C@H](O)[C@H](C)C[C@H](CC=O)[C@@H]1O[C@H]1[C@H](O)[C@@H](N(C)C)[C@H](O[C@@H]2O[C@@H](C)[C@H](O)[C@](C)(O)C2)[C@@H](C)O1 XYJOGTQLTFNMQG-KJHBSLKPSA-N 0.000 claims description 13
- 239000002585 base Substances 0.000 claims description 12
- 238000002425 crystallisation Methods 0.000 claims description 12
- BWDBEAQIHAEVLV-UHFFFAOYSA-N 6-methylheptan-1-ol Chemical compound CC(C)CCCCCO BWDBEAQIHAEVLV-UHFFFAOYSA-N 0.000 claims description 11
- 230000008025 crystallization Effects 0.000 claims description 11
- 239000000047 product Substances 0.000 claims description 11
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 claims description 9
- TVMXDCGIABBOFY-UHFFFAOYSA-N n-Octanol Natural products CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 claims description 9
- 238000005984 hydrogenation reaction Methods 0.000 claims description 8
- 239000010413 mother solution Substances 0.000 claims description 8
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 claims description 7
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims description 6
- 229910052799 carbon Inorganic materials 0.000 claims description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 5
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 5
- 239000003513 alkali Substances 0.000 claims description 5
- 235000006408 oxalic acid Nutrition 0.000 claims description 5
- 239000013557 residual solvent Substances 0.000 claims description 5
- 238000005406 washing Methods 0.000 claims description 5
- 238000013016 damping Methods 0.000 claims description 3
- 238000001035 drying Methods 0.000 claims description 3
- 239000012530 fluid Substances 0.000 claims description 3
- NJYFRQQXXXRJHK-UHFFFAOYSA-N (4-aminophenyl) thiocyanate Chemical compound NC1=CC=C(SC#N)C=C1 NJYFRQQXXXRJHK-UHFFFAOYSA-N 0.000 claims description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims description 2
- 238000000855 fermentation Methods 0.000 claims description 2
- 230000004151 fermentation Effects 0.000 claims description 2
- 239000011734 sodium Substances 0.000 claims description 2
- 229910052708 sodium Inorganic materials 0.000 claims description 2
- 239000007974 sodium acetate buffer Substances 0.000 claims description 2
- 238000010792 warming Methods 0.000 claims description 2
- 239000000243 solution Substances 0.000 claims 9
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims 4
- PGNYNCTUBKSHHL-UHFFFAOYSA-N 2,3-diaminobutanedioic acid Chemical compound OC(=O)C(N)C(N)C(O)=O PGNYNCTUBKSHHL-UHFFFAOYSA-N 0.000 claims 1
- XEEVLJKYYUVTRC-UHFFFAOYSA-N oxomalonic acid Chemical compound OC(=O)C(=O)C(O)=O XEEVLJKYYUVTRC-UHFFFAOYSA-N 0.000 claims 1
- 239000008057 potassium phosphate buffer Substances 0.000 claims 1
- ZNNZYHKDIALBAK-UHFFFAOYSA-M potassium thiocyanate Chemical compound [K+].[S-]C#N ZNNZYHKDIALBAK-UHFFFAOYSA-M 0.000 claims 1
- 229940116357 potassium thiocyanate Drugs 0.000 claims 1
- DKPFZGUDAPQIHT-UHFFFAOYSA-N Butyl acetate Natural products CCCCOC(C)=O DKPFZGUDAPQIHT-UHFFFAOYSA-N 0.000 abstract description 9
- DMUAPQTXSSNEDD-QALJCMCCSA-N Midecamycin Chemical compound C1[C@](O)(C)[C@@H](OC(=O)CC)[C@H](C)O[C@H]1O[C@H]1[C@H](N(C)C)[C@@H](O)[C@H](O[C@@H]2[C@H]([C@H](OC(=O)CC)CC(=O)O[C@H](C)C/C=C/C=C/[C@H](O)[C@H](C)C[C@@H]2CC=O)OC)O[C@@H]1C DMUAPQTXSSNEDD-QALJCMCCSA-N 0.000 abstract description 3
- 229960002757 midecamycin Drugs 0.000 abstract description 3
- 239000000654 additive Substances 0.000 abstract description 2
- 230000000996 additive effect Effects 0.000 abstract description 2
- 238000005516 engineering process Methods 0.000 abstract description 2
- 238000002360 preparation method Methods 0.000 abstract description 2
- 238000011027 product recovery Methods 0.000 abstract description 2
- FUZZWVXGSFPDMH-UHFFFAOYSA-N hexanoic acid Chemical compound CCCCCC(O)=O FUZZWVXGSFPDMH-UHFFFAOYSA-N 0.000 abstract 1
- -1 jitamycin Chemical compound 0.000 abstract 1
- 241000894006 Bacteria Species 0.000 description 2
- ZMZDMBWJUHKJPS-UHFFFAOYSA-N thiocyanic acid Chemical compound SC#N ZMZDMBWJUHKJPS-UHFFFAOYSA-N 0.000 description 2
- 206010013786 Dry skin Diseases 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- ZMZDMBWJUHKJPS-UHFFFAOYSA-M Thiocyanate anion Chemical compound [S-]C#N ZMZDMBWJUHKJPS-UHFFFAOYSA-M 0.000 description 1
- 241000209140 Triticum Species 0.000 description 1
- 235000021307 Triticum Nutrition 0.000 description 1
- XXPWHJXOXOLNGF-UHFFFAOYSA-N [C-]#N.[C-]#N.[C-]#N.[SH4+2].[K+] Chemical compound [C-]#N.[C-]#N.[C-]#N.[SH4+2].[K+] XXPWHJXOXOLNGF-UHFFFAOYSA-N 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000003115 biocidal effect Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hcl hcl Chemical compound Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- JVTAAEKCZFNVCJ-UHFFFAOYSA-N lactic acid Chemical class CC(O)C(O)=O JVTAAEKCZFNVCJ-UHFFFAOYSA-N 0.000 description 1
- 239000010985 leather Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 239000000825 pharmaceutical preparation Substances 0.000 description 1
- 229940127557 pharmaceutical product Drugs 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- DCKVNWZUADLDEH-UHFFFAOYSA-N sec-butyl acetate Chemical compound CCC(C)OC(C)=O DCKVNWZUADLDEH-UHFFFAOYSA-N 0.000 description 1
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Abstract
The present invention relates to a new extraction technology of macrolide antibiotics mainly including such preparation processes of erythromycin, jitamycin, spiramycin and medemycin. Said new technology uses a new extraction system consisting of extracting agent and dilutent instead of butyl acetate extraction solvent in the traditional technological process. If necessary, a certain proportion of additive can be added. ADVANTAGE-. Reduces solvent consumption and product cost, and raises its product recovery ratio.
Description
The present invention relates to a kind of extracting macrolide antibiotics novel process, belong to the pharmaceutical products technical field.
Macrolide antibiotics mainly is to resist the blue formula positive bacteria of leather and some to remove from office a class microbiotic of blue formula negative bacterium, and its constructional feature is that intramolecularly contains big lactonic ring (14-16 ring), is for having amino alkaline antibiotic.Wherein commonly used has: erythromycin (Erythromycin), Kitasamycin (Kitasamycin), Spiramycin Base (Spiramycin) and mydecamycin (Midecamycin, difference is referred to as Meleumycinum to home products owing to forming slightly, and latin name is Meleumycinum) etc.The extracting method of macrolide antibiotics mainly is a solvent extration at present, used extraction solvent is a N-BUTYL ACETATE, promptly be to extract with N-BUTYL ACETATE from ferment filtrate under alkaline condition, get final crystalline product through other processing again, its concrete treatment scheme as shown in Figure 1.
Fig. 1 is a principle process, and different microbiotic are slightly different, as erythromycin can butyl ester mutually in direct crystallization get lactic acid salt or thiocyanate-; Kitasamycin, Meleumycinum and Spiramycin Base then all are adjust pHs after back extraction, crystallization under alkaline condition.The main drawback of above-mentioned flow process is: N-BUTYL ACETATE when extraction solvent consumption is big, though its consumption of different microbiotic is slightly different, it is estimated that its expense accounts for the nearly 1/3 of this product cost, simultaneously in order to reclaim extraction solvent from extraction raffinate, needs additional energy consumption again.
The objective of the invention is to study a kind of extraction process of new macrolide antibiotics, change traditional technical process, particularly change the extraction system in the former technical process, replace N-BUTYL ACETATE with a new extraction system of forming by extraction agent and thinner, so that on the basis of existing product yield and quality, reduce solvent consumption, thereby reduce production costs.
Process for extracting macrolide antibiotics of the present invention mainly is that Spiramycin Base, erythromycin, Kitasamycin and the wheat extraction process from mycin is made improvements.Wherein used extraction system is made up of extraction agent and thinner, adds a certain proportion of other additive in case of necessity.Extraction agent is eight carbon alcohol, comprises n-Octanol, isooctyl alcohol or secondary octanol (second octanol), and thinner is normal hexane, hexanaphthene, normal heptane, sulfonated kerosene or hydrogenation kerosene.The volume ratio of extraction agent and thinner is V
Collection: V
Rare=0.5-1: 0-0.5.
Two closed cycles of organic solvent after employing product crystalline mother solution and the back extraction in this novel process simultaneously, thus can further improve product recovery rate, and its principle process is as shown in Figure 2.
1. 2. erythromycin of Spiramycin Base, Kitasamycin and Meleumycinum among Fig. 2
In the process for extracting macrolide antibiotics of the present invention:
1. the preparation technology of Spiramycin Base is:
Get factory's ferment of spiramycin filtrate, add NaOH liquor adjust pH to 9.0-10.0, the back is carried out multi-stage counter current extraction with the new extraction solvent of the present invention by a constant current than on the annulus type centrifugal extractor stand, extract stream is A than the ratio between water A and the organic phase O: O=5-8: 1 come together organic phase, use oxalic acid (H again
2C
2O
4)+potassium primary phosphate (KH
2PO
4) damping fluid (pH ≈ 2) is by constant current ratio strip (adverse current or multistage cross flow), back extraction stream was than O: A=4-6.5: 1, extraction and reextraction service temperature are: 10 ℃-40 ℃, back extraction gets and adds NaOH liquid adjust pH to 11.0 after liquid removes residual solvent through blowing, and is heated to 50-60 ℃, is incubated 5-30 minutes, and the Spiramycin Base crystallization, crystalline mother solution returns fermented liquid (or ferment filtrate) and applies mechanically, and crystallization is through washing, and drying then can get the Spiramycin Base product.Following table (table 1) has been listed the process implementing example of the extraction of part Spiramycin Base, back extraction:
Down together.</entry></row></tbody></tgroup></table></tables>
2. erythromycin extraction
Get factory's abomacetin fermentation filtrate, add NaOH liquid adjust pH to 10.0 ± 0.5, press a constant current than A: O=4-8: 1 with the new extraction system of the present invention, on the annulus type centrifugal extractor stand, carry out multistage (2-3 grades) counter-current extraction, use acetic acid+sodium-acetate buffer (pH=4.0-4.8) to carry out multi-stage countercurrent (2-3 grades) or cross-flow (2-3 cross-flows) back extraction by a constant current than (O: A=1-5: 1) more then, 10-40 ℃ of extraction and back extraction temperature, add NaOH liquid and transfer back extraction to get liquid pH value, add excess of sulfur potassium cyanide (KCNS) or sodium sulfocynanate (NaCNS) then to nearly neutral (6.0-7.0), rhodan ammonium (NH
4CNS), thiocyanide and erythromycin molecular ratio are 2-20mol/mol, the thiocyanate-crystallization that under 15 ℃ of-35 ℃ of conditions, got erythromycin through 20 minutes to 3 hours, and filtrated stock partly or entirely returns fermented liquid (or ferment filtrate) and applies mechanically.The erythromycin salt crystal after washing, oven dry promptly gets the thiocyanate-finished product of erythromycin.Its part of test results is listed in table 2.
The extraction of table 2 erythromycin, the salt experimental result of stripping, sink
| Sequence number | Ferment filtrate u/ml | Extraction agent+thinner | Extract stream compares A/O | Percentage extraction % | Back extraction stream compares O/A | Stripping rate % | KCNS adds molmol erythromycin | Salt yield % |
| ???1# | ??2624 | 60% isooctyl alcohol+40% normal heptane | ?????6∶1 | ???96.8 | ????3∶2 | ??94.35 | ????10 | ?79.34 |
| ???2# | ??3296 | 70% isooctyl alcohol+30% normal heptane | ???8.1∶1 | ???97.56 | ????3∶2 | ??93.310 | ????11 | ?77.87 |
| ???3# | ??2344 | 70% n-Octanol+30% hydrogenation kerosene | ???6.8∶1 | ???96.03 | ???1.3∶1 | ??95.66 | ????12 | ?78.0 |
| ???4# | ??2500 | 70% secondary octanol+30% sulfonated kerosene | ?????6∶1 | ???97.01 | ????2∶1 | ??92.5 | ????10 | ?78.2 |
| ???5# | ??3100 | 70% n-Octanol+30% hexanaphthene | ???5.8∶1 | ???95.8 | ????3∶2 | ??95.4 | ????10 | ?77.9 |
| ???6# | ??3200 | 60% isooctyl alcohol+40% normal hexane | ???6.2∶1 | ???94.9 | ???1.8∶1 | ??92.6 | ????12 | ?79.3 |
3. Kitasamycin extraction
Get factory's Kitasamycin ferment filtrate (3000u/ml), add NaOH liquid to pH value 8.8-9.0, the back on centrifugal extractor stand carry out multistage (2-3) counter-current extraction by a constant current than (A: O=4-8: 1) with the new extraction solvent of the present invention, come together organic phase, use saturated oxalic acid (H again
2C
2O
4) liquid, pH=2.5-3.0 strips, and back extraction can be undertaken by multi-stage countercurrent (2-3 grades) or multistage cross flow mode, and back extraction is flowed than O: A=3-6: 1, extraction and reextraction temperature: 10 ℃-40 ℃.Back extraction gets liquid and add NaOH liquid adjust pH to 6.5 after blow removing residual solvent, and is heated to 40 ℃, adds alkali to pH=8.5-9.0, is incubated 5-10 minutes after being warming up to 50 ℃, the Kitasamycin crystallization.Filter, and in 60 ℃ of oven dry down.Crystalline mother solution returns fermented liquid (or ferment filtrate) and applies mechanically.Following table (having 3) has been listed the extraction of part Kitasamycin, reextraction example.
The extraction of table 3 Kitasamycin, back extraction experimental result
| Sequence number | Ferment filtrate u/ml | Extraction agent+thinner | Extract stream compares A/O | Percentage extraction % | Back extraction stream compares O/A | Stripping rate % | Extraction, back extraction temperature ℃ |
| ??1# | ???3000 | 80% isooctyl alcohol+20% hydrogenation kerosene | ??6∶1 | ???95.0 | ????5∶1 | ???96.0 | ????18—20℃ |
| ??2# | ???3050 | 80% secondary octanol+20% normal hexane | ??6∶1 | ???96.9 | ????5∶1 | ???95.4 | ????18—20℃ |
| ??3# | ???2000 | 80% n-Octanol+20 sulfonated kerosenes | ??6∶1 | ???96.2 | ????5.1∶1 | ???95.6 | ????18—20℃ |
| ??4# | ???2150 | 70% isooctyl alcohol+30% normal heptane | ??6∶1 | ???94.1 | ????5∶1 | ???95.4 | ??????25℃ |
4. Meleumycinum extraction
Get factory's Meleumycinum ferment filtrate, add NaOH liquid adjust pH to 8.5-9.0.The back is carried out multistage (2-3) counter-current extraction by a constant current than (A: O=4-6: 1) with new extraction system of the present invention, back oxalic acid (H
2C
2O
4) or hydrochloric acid (HCl) pH=2.0-2.5 strip, blow to remove back extraction and get residual solvent in the liquid, add NaOH liquid adjust pH to 8.5-9.0 again, and be heated to 40 ℃, stirred 20 minutes and must the Meleumycinum crystallization.With the salt-free water washing of hot pH=8.5, get finished product 60-70 ℃ of following dryings, crystalline mother solution returns fermented liquid (or ferment filtrate) and applies mechanically, and the example is listed in table 4.
The extraction of table 4 Meleumycinum, back extraction experimental result
| Sequence number | Ferment filtrate u/ml | Extraction agent+thinner | Extract stream compares A/O | Percentage extraction % | Back extraction stream compares O/A | Stripping rate % | Extraction, back extraction temperature ℃ |
| ?1# | ???1750 | 80% isooctyl alcohol+20% hydrogenation kerosene | ???4∶1 | ???95.0 | ????5∶1 | ????96.2 | ????18—20℃ |
| ?2# | ???1800 | 80% secondary octanol+20% normal heptane | ?4.5∶1 | ???94.8 | ????4∶1 | ????97.0 | ????18—20℃ |
| ?3# | ???2200 | 80% n-Octanol+20% hexanaphthene | ?4.5∶1 | ???95.5 | ????6∶1 | ????94.5 | ????18—20℃ |
| ?4# | ???2450 | 80% secondary octanol+20% sulfonated kerosene | ???4∶1 | ???95.1 | ????5∶1 | ????97.2 | ??????25℃ |
Claims (4)
1, a kind of process for extracting macrolide antibiotics is characterized in that this microbiotic is a Spiramycin Base, and its extraction process is made up of following each step:
(1) gets factory's ferment of spiramycin filtrate, add sodium hydroxide solution adjust pH to 9.0-10.0;
(2) use the extraction system of forming by extraction agent and thinner that above-mentioned solution is extracted, wherein extraction agent is eight carbon alcohol, comprise n-Octanol, isooctyl alcohol or secondary octanol, thinner is any in normal hexane, hexanaphthene, normal heptane, sulfonated kerosene or the hydrogenation kerosene, and the joint of extraction agent and thinner is long-pending than being V
Collection: V
Rare=0.5-1: 0-0.5, the extracting operation temperature is 10 ℃-40 ℃, and the extract stream ratio is: water A is O with the ratio of organic phase O: A=5-8: 1;
(3) with above-mentioned come together organic phase strip with oxalic acid and potassium phosphate buffer, wherein the pH value of damping fluid is 2-3, back extraction stream is than being O: A=4-6.5: 1, the back extraction service temperature is 10 ℃-40 ℃;
(4) above-mentioned the 3rd step back extraction is got liquid and removes remaining solvent with air blast after, add sodium hydroxide adjust pH to 11.0, and be heated to 50 ℃-60 ℃, be incubated 5-30 minutes, promptly get the Spiramycin Base crystallization, its crystallization gets the Spiramycin Base product after washing drying, crystalline mother solution returns ferment filtrate and applies mechanically.
(5) organic phase after the back extraction is multiplexing after alkali lye is handled.
2, a kind of process for extracting macrolide antibiotics is characterized in that this microbiotic is an erythromycin, and its extraction process is made up of following each step:
(1) gets factory's abomacetin fermentation filtrate, add sodium hydroxide solution adjust pH to 10.0 ± 0.5;
(2) use the extraction system of forming by extraction agent and thinner that above-mentioned solution is extracted, wherein extraction agent is eight carbon alcohol, comprise n-Octanol, isooctyl alcohol or secondary octanol, thinner is any in normal hexane, hexanaphthene, normal heptane, sulfonated kerosene or the hydrogenation kerosene, and the volume ratio of extraction agent and thinner is V
Collection: V
Rare=0.5-1: 0-0.5, the extracting operation temperature is 10 ℃-40 ℃, and the extract stream ratio is: water A is O with the ratio of organic phase O: A=4-8: 1;
(3) with above-mentioned come together organic liquor strip with acetic acid and sodium-acetate buffer, wherein the pH value of damping fluid is 4.0-4.8, back extraction stream is than being O: A=1-5: 1; The back extraction service temperature is 10 ℃-40 ℃;
(4) get and add sodium hydroxide in the liquid in above-mentioned the 3rd step back extraction, adjust pH is 6.0-7.0, adds any in potassium thiocyanate or sodium sulfocynanate or the rhodan ammonium again, and the mole ratio of itself and erythromycin is 2-20mol: 1mol;
(5) go on foot product under 15 ℃-35 ℃ with the above-mentioned the 4th, be incubated 20 minutes to 3 hours, get the Erythromycin Thiocyanate crystallization.
(6) crystalline mother solution returns ferment filtrate and applies mechanically;
(7) organic phase is multiplexing after alkali lye is handled after the back extraction.
3, a kind of process for extracting macrolide antibiotics is characterized in that this microbiotic is a Kitasamycin, and its extraction process is made up of following each step:
(1) gets factory's Kitasamycin ferment filtrate, add sodium hydroxide solution adjust pH to 8.8-9.0;
(2) use the extraction system of forming by extraction agent and thinner that above-mentioned solution is extracted, wherein extraction agent is eight carbon alcohol, comprise n-Octanol, isooctyl alcohol and secondary octanol, thinner is any in normal hexane, hexanaphthene, normal heptane, sulfonated kerosene or the hydrogenation kerosene, and the volume ratio of extraction agent and thinner is V
Collection: V
Rare=0.5-1: 0-0.5, the extracting operation temperature is 10 ℃-40 ℃, and the extract stream ratio is: water A is O with the ratio of organic phase O: A=4-8: 1;
(3) with above-mentioned come together organic phase strip with saturated oxalic acid, the pH value of oxalic acid is 2.5-3.0, back extraction stream is than being O: A=3-6: 1, the back extraction service temperature is 10 ℃-40 ℃;
(4) above-mentioned the 3rd step back extraction is got liquid and removes residual solvent with air blast after, add sodium hydroxide solution adjust pH to 6.5, reheat to 40 ℃, and add adjusting PH with base value to 8.5-9.0;
(5) above-mentioned solution is warming up to 50 ℃, is incubated 5-10 minutes, promptly get the Kitasamycin crystallization.
(6) crystalline mother solution returns ferment filtrate and applies mechanically;
(7) organic phase is multiplexing after alkali lye is handled after the back extraction.
4, a kind of process for extracting macrolide antibiotics is characterized in that this microbiotic is a Meleumycinum, and its extraction process is made up of following each step:
(1) gets factory's Meleumycinum ferment filtrate, add sodium hydroxide adjust pH to 8.5-9.0;
(2) use the extraction system of forming by extraction agent and thinner that above-mentioned solution is extracted, wherein extraction agent is eight carbon alcohol, comprise n-Octanol, isooctyl alcohol and secondary octanol, thinner is any in normal hexane, hexanaphthene, normal heptane, sulfonated kerosene or the hydrogenation kerosene, and the volume ratio of extraction agent and thinner is V
Collection: V
Rare=0.5-1: 0-0.5, the extracting operation temperature is 10 ℃-40 ℃, and the extract stream ratio is: water A is O with the ratio of organic phase O: A=4-6: 1;
(3) with above-mentioned come together organic phase strip with oxalic acid or hydrochloric acid, the pH value of its mesoxalic acid or hydrochloric acid is 2.0-2.5, back extraction is flowed than O: A=4-8: 1, the back extraction service temperature is 10-40 ℃;
(4) above-mentioned the 3rd step back extraction is got liquid and remove wherein residual solvent, add sodium hydroxide adjust pH to 8.5-9.0 with air blast;
(5) above-mentioned work in-process are heated to 40 ℃, stirred 20 minutes, the pH value of reusable heat is 8.5 salt-free water washing, gets the Meleumycinum finished product 60 ℃ of-70 ℃ of following crystallizations.
(6) crystalline mother solution returns ferment filtrate and applies mechanically;
(7) organic phase is multiplexing after alkali lye is handled after the back extraction.
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| CN95105997A CN1035674C (en) | 1995-06-09 | 1995-06-09 | Process for extracting macrolide antibiotics |
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| Application Number | Priority Date | Filing Date | Title |
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| CN95105997A CN1035674C (en) | 1995-06-09 | 1995-06-09 | Process for extracting macrolide antibiotics |
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| CN1125230A true CN1125230A (en) | 1996-06-26 |
| CN1035674C CN1035674C (en) | 1997-08-20 |
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| CN1054131C (en) * | 1998-04-08 | 2000-07-05 | 浙江大学 | Process for extracting ilotycin by two aqueous phase extracting process |
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| CN103665073A (en) * | 2012-09-03 | 2014-03-26 | 北大方正集团有限公司 | Method for preparing midecamycin |
| CN104109181A (en) * | 2014-06-30 | 2014-10-22 | 北大医药重庆大新药业股份有限公司 | Membrane filtration process method of meleumycin |
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| CN1025198C (en) * | 1989-10-06 | 1994-06-29 | 中国科学院化工冶金研究所 | Extraction of lincomycin from fermented liquid |
| CN1021443C (en) * | 1990-03-21 | 1993-06-30 | 核工业北京化工冶金研究院 | Method for extracting lincomycin by solvent |
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