CN102617683B - Method for separating adenosine cyclophosphate - Google Patents

Method for separating adenosine cyclophosphate Download PDF

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CN102617683B
CN102617683B CN201210068263.7A CN201210068263A CN102617683B CN 102617683 B CN102617683 B CN 102617683B CN 201210068263 A CN201210068263 A CN 201210068263A CN 102617683 B CN102617683 B CN 102617683B
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camp
solution
sorbent material
zeo
resin
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CN102617683A (en
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应汉杰
杨丽
钱文斌
吴菁岚
柏建新
陈勇
陈晓春
谢婧婧
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Nanjing Tech University
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Abstract

The invention discloses a method for separating adenosine cyclophosphate. The method comprises the following steps of: adsorbing adenosine cyclophosphate in a solution by taking a novel chelation adsorption medium as an adsorbent; eluting the adsorbent by taking an alkaline liquor as an eluent; collecting an eluent; and regenerating the adsorbent by taking an acid liquor as a regenerating agent. In the method provided by the invention, the novel chelation adsorption medium is used for separating adenosine cyclophosphate. Compared with the conventional method for separating adenosine cyclophosphate with resin, the method has the advantages that: the adsorption medium can be suitable for an adenosine cyclophosphate system under any condition that the pH is 1-7, the adsorption amount can be 80-160 mg/g that of resin, and the concentration of adenosine cyclophosphate can be increased by 4-5 times. Moreover, in eluting and regenerating processes in which the novel medium is used, the using amounts of acid and alkali can be saved by over 50 percent, and the using amount of water can be saved by 20-30 percent. The adsorbent is a clean, environmentally-friendly, low-price and readily-available adsorbent.

Description

A kind of method of separated cAMP
Technical field
The invention belongs to bioseparation field, be specifically related to utilize the method for the separated cAMP of a kind of new adsorbent.
Background technology
CAMP, has another name called 3',5'-cyclic adenosine monophosphate, is called for short cAMP, is a kind of important physiologically active substance in organism, has the function that regulates plurality of enzymes catalyzed reaction in organism, is intracellular second messenger.Its main physiological function has: promote myocardial contraction, diastole unstriated muscle, coronary artery dilator blood vessel, improve liver function, promote neurotization, suppress the division of skin outer layer epithelial cell and transform paracytic function, the promotion oxidasic activity of respiratory chain and improve myocardial anoxia etc., the eubolism of human body is played an important role.
CAMP mainly contains three kinds of production methods, i.e. chemosynthesis, natural product extraction and microorganism fermentation.Separating step in its production process has mainly been applied macroporous resin, Zeo-karb and three kinds of sorbent materials of anionite-exchange resin.
Patent (TW200922612) discloses a kind of to prepare the method for medicine or protective foods containing the raw material of Cyclic adenosine-3',5'-monophosphate.Wherein in date, cAMP is mainly by macroporous resin OU-2 and the separated acquisition of ME-2 two post continuous adsorption, and the content that is finally extracted cAMP in thing is 1%, illustrates that macroporous resin is extremely low as the separated cAMP efficiency of sorbent material.And the up-to-date biochemical drug technology of preparing of the < < > > report of publishing in 2000: at the cAMP crystallization processes of chemosynthesis, what segregation section was used is cationite, adsorptive power is lower, separation and purification poor effect.Patent (201010191525.X) provides a kind of method of separated cAMP, and the sorbent material that its sepn process adopts is anionite-exchange resin, and every gram of wet ion exchange resin adsorptive capacity can reach 0.08-0.15g cAMP.The method has improved the adsorptive capacity of sorbent material to cAMP greatly, has improved separation efficiency, but this method needs to regulate the pH of cAMP solution for alkaline.Because cAMP belongs to organic monoacid, in the aqueous solution with cAMP and cAMP -form jointly exist, need regulator solution pH could all dissociate and become cAMP in the scope of 6.5-11 -.CAMP -could carry out the exchange of maximum with anionite-exchange resin, reach maximal absorptive capacity.And when not regulating pH value of solution, the cAMP that part is molecularity can not be switched on negative resin, will cause the adsorptive capacity of negative resin to reduce.
Conventional ion exchange resin when regeneration adopt 6-8BV concentration be the acid, alkaline solution of 3%-5% as regenerator, also need in addition the water of 4-5BV to rinse resin column, the regeneration that just can reach resin column is complete.Acid, alkali and water that this traditional method consumption is a large amount of, easily cause environmental pollution and the wasting of resources.
Summary of the invention
Technical problem to be solved by this invention is to provide a kind of method that adopts the separated cAMP of chelating adsorption medium, the problem that efficiently solve that the sorbent material adsorptive capacity existing in existing isolation technique is low, wash-out and regenerative process consumes a large amount of acid, alkali, water.
For solving the problems of the technologies described above, the thinking that the present invention adopts is: cAMP is a kind of organic monoacid, and molecular formula is C 10h 12n 5o 6, there is a large amount of N, O, P atom in P, the lone-pair electron on atom can combine with the unoccupied orbital of metal ion in molecule, form coordinate bond, thereby make to set up between cAMP and metal ion stable chelate structure.Utilize this mechanism, the invention provides a kind of Novel adsorption medium, be about to Zeo-karb and process metal ion on portability through transition, become the Novel adsorption medium with chelating function, thereby can adsorb cAMP.The coordination chelating process of new type resin and cAMP as shown in Figure 1.While presenting different dissociated state due to cAMP in solution, its N, O, P atom provide the ability of lone-pair electron can not change, and therefore, sorbent material does not change with pH value of solution to the adsorptive power of cAMP.But consider OH in basic solution -can form ionic linkage with metal ion on resin, so the pH of cAMP system is chosen as 1-7.In addition, during alkaline solution wash-out, OH -can with strong ionic linkage, be combined by the metal on resin, therefore with a small amount of low concentration alkali solution, coordinate bond can be destroyed, thereby cAMP is departed from from resin.Wash-out is completely rear extremely neutral with pure water drip washing resin column, continues to use pure water drip washing to neutral after employing 4-5BV lower concentration acid upper prop, can complete the regeneration of sorbent material.
Concrete technical scheme is as follows:
A kind of method of separated cAMP, take the cAMP of novel chelating adsorption medium (i.e. transition after Zeo-karb) in sorbent material adsorbent solution, recycling alkali lye carries out wash-out as eluent to sorbent material, collect elutriant, use acid solution as regenerator, sorbent material to be regenerated.
Wherein, the precursor of described novel chelating adsorption medium is Zeo-karb, and it is skeleton that described Zeo-karb be take polystyrene or acrylic acid series, take sulfonic group, phosphate or carboxyl as functional group; Preferably take polystyrene as skeleton, take sulfonic acid group as functional group.The representational example of these Zeo-karbs has Amberlite IR-124, and (skeleton is vinylbenzene, functional group is sulfonic group), (skeleton is vinylbenzene to Amberlite IR-116, functional group is sulfonic group) or Amberlite IRC-84 (skeleton is vinylformic acid, and functional group is carboxyl).
Wherein, the preparation method of described novel chelating adsorption medium, to take inorganic metal salt brine solution as Complex reagent, it is contacted with Zeo-karb, by metal ion with ionic linkage the acid functional group on Zeo-karb be combined, thereby immobilizedly to Zeo-karb, can not come off, the functional group of the Zeo-karb after transition is metal ion.Wherein, in described inorganic metal salt brine solution, metal ion is Fe 2+, Fe 3+, Cu 2+, Zn 2+or Co 2+, preferred Fe 3+, Cu 2+or Zn 2+; Inorganic metal salt concn is 1～50g/L, preferably 3-20g/L.Zeo-karb before transition is 10-40mg/g wet resin to the adsorptive capacity of cAMP, and the adsorptive capacity after transition can reach 80-160mg/g wet resin.
The Zeo-karb step that specifically makes the transition is as follows:
(1) take a certain amount of Zeo-karb dress post;
(2) Complex reagent is flow through to resin column with constant flow rate, until outlet strength of solution equals import strength of solution;
(3) deionized water is flow through to resin column with constant flow rate, to non-metallic ion in effluent liquid;
(4) with ethanol drip washing resin column;
(5) resin that vacuum drying step (4) obtains at 30-60 ℃, completes transition.
According to method transition provided by the invention, the amount of metal ion that completes the new adsorbent load of transition is 0.05-2.00mmol/g resin.
Wherein, the concentration of cAMP solution can be 1-8g/L, and upper column flow rate can be 0.5-4BV/h.
Wherein, described alkali lye is sodium hydroxide or potassium hydroxide aqueous solution, and concentration is 0.01～0.6mol/L, preferably 0.1-0.4mol/L; Alkali lye consumption is 2～5BV, preferably 3-4BV; Elution flow rate is 0.5-3BV/h.
Wherein, described acid solution is hydrochloric acid or sulfuric acid, and concentration is 0.01-0.6mol/L, preferably 0.1-0.4mol/L; Acid solution consumption is 2-5BV, preferably 3-4BV.
Wherein, before regeneration, first use deionized water drip washing sorbent material to neutral, after regeneration, then to neutrality, reuse sorbent material with deionized water drip washing sorbent material.
Beneficial effect: method provided by the invention adopts the separated cAMP of novel chelating adsorption medium, cAMP separated with conventional resins compared, advantage of the present invention is: this adsorption medium is applicable to the cAMP system under any pH1-7 condition, adsorptive capacity can reach 80-160mg/g resin, and cAMP concentration can improve 4-5 doubly.And the acid of this novel medium wash-out, regenerative process, alkali consumption all can be saved more than 50%, and water consumption can be saved 20%-30%, be a kind of clean environment firendly, cheap, the sorbent material that is easy to get.
Accompanying drawing explanation
Fig. 1 is the Coordination Adsorption procedure chart of new adsorbent (vinylbenzene skeleton, sulfonic acid group) to cAMP after transition.
Fig. 2 is the adsorptive capacity of novel chelating adsorption medium to cAMP under different pH cAMP systems.
Fig. 3 is the new adsorbent loading capacity of embodiment 5 mensuration and the changing conditions figure of wash-out yield.
Embodiment
According to following embodiment, the present invention may be better understood.Yet, those skilled in the art will readily understand, the described content of embodiment is only for the present invention is described, and should also can not limit the present invention described in detail in claims.
The preparation of cAMP solution
Following examples cAMP solution used prepares as follows:
Fermentation culture based component is: glucose 5% (g/100mL, below identical), K 2hPO 41%, KH 2pO 41%, MgSO 41%, urea 0.5%, peptone 0.5% adds 0.1g NaF, 0.1g VB1 and 5g xanthoglobulin in every liter of substratum simultaneously.
Seed culture based component is: glucose 1%, and peptone 1%, yeast extract paste 0.5%, extractum carnis 1%, NaCl 0.3%.
Cultural method: by Arthrobacter A302 (CGMCC No.3584) access seed culture medium, cultivate 18 hours under 30 ℃, 240rpm.In inoculum size access fermention medium with 10% (v/v), it is 7.0 that the NaOH of take controls pH again, and it is 30%, 400rpm, 30 ℃ of bottom fermentations 72 hours that dissolved oxygen is controlled.While putting tank, cAMP output is 3-8g/L.Then by fermented liquid by the centrifugal thalline of removing of whizzer, the more centrifugal supernatant liquor obtaining seen through to ultra-filtration membrane remove most of protein, can obtain concentration range at the cAMP solution of 3-8g/L.
Embodiment 1:
Take 50g Zeo-karb Amberlite IR-124 dress post, the ferric chloride Solution that is 3g/L by concentration flows through resin column with 1BV/h, when outflow concentration is also 3g/L, stops transition.With identical flow velocity, continue to pass into deionized water, to effluent liquid, do not contain iron ion.Finally use ethanol drip washing resin column, after drip washing completes, by resin as for vacuum-drying in 30 ℃ of vacuum drying ovens, the transition that completes sorbent material.Get the sorbent material potting resin post of 20g after transition, the cAMP solution upper prop that is 4.5g/L by concentration after balance, flows through resin column with 3.5BV/h, and adsorbing saturated rear mensuration adsorptive capacity is 126mg/g wet resin.With 0.4mol/L sodium hydroxide, carry out wash-out, elution flow rate 1BV/h, eluent consumption is 3BV, collects elutriant, and the concentration of cAMP is 16.50g/L, and purity is 95.12%, yield 98.48%.
Embodiment 2:
Take 50g Zeo-karb Amberlite IR-116 dress post, the Cupric Chloride Solution that is 10g/L by concentration flows through resin column with 1BV/h, when outflow concentration is also 10g/L, stops transition.With identical flow velocity, continue to pass into deionized water, to copper ions not in effluent liquid.Finally use ethanol drip washing resin column, after drip washing completes, by resin as for vacuum-drying in 40 ℃ of vacuum drying ovens, the transition that completes sorbent material.Get the sorbent material potting resin post of 10g after transition, the cAMP solution upper prop that is 4g/L by concentration after balance, flows through resin column with 2BV/h, and adsorbing saturated rear mensuration adsorptive capacity is 85mg/g wet resin.With 0.3mol/L sodium hydroxide, carry out wash-out again, elution flow rate 2BV/h, eluent consumption is 4BV.Collect elutriant, cAMP concentration is 11.06g/L, and purity is 94.75%, yield 97.67%.
Embodiment 3:
Take 50g Zeo-karb Amberlite IR-116 dress post, the solution of ferrous chloride that is 15g/L by concentration flows through resin column with 1BV/h, when outflow concentration is also 15g/L, stops transition.With identical flow velocity, continue to pass into deionized water, to effluent liquid, do not contain ferrous ion.Finally use ethanol drip washing resin column, after drip washing completes, by resin as for vacuum-drying in 50 ℃ of vacuum drying ovens, the transition that completes sorbent material.Get the sorbent material potting resin post of 30g after transition, the cAMP solution upper prop that is 3g/L by concentration after balance, flows through resin column with 3.5BV/h, and adsorbing saturated rear mensuration adsorptive capacity is 109mg/g wet resin.With 0.2mol/L sodium hydroxide, carry out wash-out, elution flow rate 2.5BV/h, eluent consumption is 5BV.Collect elutriant, cAMP concentration is 14.1g/L, and purity is 94.87%, yield 97.10%.
Embodiment 4:
Take 100g Zeo-karb Amberlite IRC-84 dress post, the ferric chloride Solution that is 8g/L by concentration flows through resin column with 1BV/h, when outflow concentration is also 8g/L, stops transition.With identical flow velocity, continue to pass into deionized water, to effluent liquid, do not contain iron ion.Finally use ethanol drip washing resin column, after drip washing completes, by resin as for vacuum-drying in 40 ℃ of vacuum drying ovens, the transition that completes sorbent material.
Take rear Amberlite IRC-84 dress post 10g transition, upper prop cAMP strength of solution is that 3g/L regulator solution pH are 1, the saturated rear calculating adsorptive capacity of upper prop absorption.
Take rear Amberlite IRC-84 dress post 10g transition, upper prop cAMP strength of solution is that 3g/L regulator solution pH are 2, the saturated rear calculating adsorptive capacity of upper prop absorption.
Take rear Amberlite IRC-84 dress post 10g transition, upper prop cAMP strength of solution is that 3g/L regulator solution pH are 3, the saturated rear calculating adsorptive capacity of upper prop absorption.
Take rear Amberlite IRC-84 dress post 10g transition, upper prop cAMP strength of solution is that 3g/L regulator solution pH are 4, the saturated rear calculating adsorptive capacity of upper prop absorption.
Take rear Amberlite IRC-84 dress post 10g transition, upper prop cAMP strength of solution is that 3g/L regulator solution pH are 5, the saturated rear calculating adsorptive capacity of upper prop absorption.
Take rear Amberlite IRC-84 dress post 10g transition, upper prop cAMP strength of solution is that 3g/L regulator solution pH are 6, the saturated rear calculating adsorptive capacity of upper prop absorption.
Take rear Amberlite IRC-84 dress post 10g transition, upper prop cAMP strength of solution is that 3g/L regulator solution pH are 7, the saturated rear calculating adsorptive capacity of upper prop absorption.
As shown in Figure 2, under different pH cAMP solution systems, the Amberlite IRC-84 after processing transition is substantially constant to the saturated extent of adsorption of cAMP.Illustrate, this chelating adsorption medium is applicable to the cAMP system under pH1-7 condition.
Embodiment 5:
Take 30g Zeo-karb Amberlite IR-124 dress post, the ferric chloride Solution that is 2g/L by concentration flows through resin column with 1BV/h, when outflow concentration is also 2g/L, stops transition.With identical flow velocity, continue to pass into deionized water, to effluent liquid, do not contain iron ion.Finally use ethanol drip washing resin column, after drip washing completes, by resin as for vacuum-drying in 30 ℃ of vacuum drying ovens, the transition that completes sorbent material.
Take rear Amberlite IR-124 dress post 20g transition, upper prop cAMP strength of solution is 4.5g/L, adsorbs saturated rear calculating adsorptive capacity.Regenerate afterwards, first with 5BV 0.4mol/LNaOH, carry out wash-out, the completely rear elution amount of calculating of wash-out.With 3BV deionized water rinsing resin column, be neutral, then use 4BV 0.4mol/L salt acid soak 6h, then be neutral with 3BV deionized water rinsing resin column, it is rear standby that resin completes regeneration.With the make the transition absorption of resin of above-mentioned the same terms, adsorb saturated rear regeneration, so circulate four times, the changing conditions of loading capacity relatively, as shown in Figure 3, transition, the regeneration effect of resin was fine for result, and loading capacity is substantially constant.
Embodiment 6:
Identical with the method for embodiment 2, difference is that Complex reagent substitutes iron(ic) chloride with zinc chloride.
Embodiment 7:
Identical with the method for embodiment 2, difference is that Complex reagent substitutes iron(ic) chloride with cobalt chloride.
Embodiment 8:
Method with embodiment 2 is identical, and difference is that ferric chloride concn is 1g/L.
Embodiment 9:
Identical with the method for embodiment 2, difference is that ferric chloride concn is 50g/L.
Embodiment 10:
Identical with the method for embodiment 2, difference is, the concentration of cAMP solution is 1g/L, and upper column flow rate is that 0.5BV/h is saturated to adsorbing.
Embodiment 11:
Identical with the method for embodiment 2, difference is, the concentration of cAMP solution is 8g/L, and upper column flow rate is that 4BV/h is saturated to adsorbing.
Embodiment 12:
Identical with the method for embodiment 2, difference is, take 0.01mol/L potassium hydroxide aqueous solution as eluent, and eluent consumption is 5BV, and elution flow rate is 0.5BV/h.
Embodiment 13:
Identical with the method for embodiment 2, difference is, take 0.6mol/L potassium hydroxide aqueous solution as eluent, and eluent consumption is 2BV, and elution flow rate is 3BV/h.
Embodiment 14:
Identical with the method for embodiment 5, difference is, regenerator is sulfuric acid, and concentration is 0.01mol/L, and regenerant consumption is 5BV.
Embodiment 15:
Identical with the method for embodiment 5, difference is, regenerator is sulfuric acid, and concentration is 0.6mol/L, and regenerant consumption is 2BV.

Claims (4)

1. the method for a separated cAMP, it is characterized in that, take the cAMP of chelating adsorption medium in sorbent material adsorbent solution, recycling alkali lye carries out wash-out as eluent to sorbent material, collect elutriant, use acid solution as regenerator, sorbent material to be regenerated;
Wherein, the precursor resin of described chelating adsorption medium is Zeo-karb, take polystyrene or acrylic acid series as skeleton, take sulfonic group, phosphate or carboxyl as functional group;
Wherein, the preparation of described chelating adsorption medium, refers to and take inorganic metal salt brine solution as Complex reagent, and it is contacted with Zeo-karb, metal ion is immobilized to Zeo-karb, and the functional group of the Zeo-karb after transition is metal ion;
Wherein, in described inorganic metal salt brine solution, metal ion is Fe 2+, Fe 3+, Cu 2+, Zn 2+or Co 2+, inorganic metal salt concn is 1～50g/L.
2. the method for separated cAMP according to claim 1, is characterized in that, described alkali lye is sodium hydroxide or potassium hydroxide aqueous solution, and concentration is 0.01～0.6mol/L, and alkali lye consumption is 2～5BV.
3. the method for separated cAMP according to claim 1, is characterized in that, described acid solution is hydrochloric acid or sulfuric acid, and concentration is 0.01-0.6mol/L, and acid solution consumption is 2-5BV.
4. the method for separated cAMP according to claim 1, is characterized in that, before regeneration, first uses deionized water drip washing sorbent material to neutral, after regeneration, then to neutrality, reuses sorbent material with deionized water drip washing sorbent material.
CN201210068263.7A 2012-02-29 2012-03-15 Method for separating adenosine cyclophosphate Active CN102617683B (en)

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