JP5839855B2 - Process for producing polyhydroxyalkanoate - Google Patents

Description

  The present invention relates to a polyhydroxyalkanoate copolymer (hereinafter referred to as “polyhydroxyalkanoate copolymer”) obtained by polymerizing 3-hydroxybutyric acid (hereinafter also referred to as “3HB”) and 3-hydroxyhexanoic acid (hereinafter also referred to as “3HH”) produced using a microorganism. , Also referred to as PHA) and its manufacturing method. More specifically, the present invention relates to a method for controlling the copolymerization ratio of 3-hydroxybutyric acid units, 3-hydroxyhexanoic acid units and / or other monomer units.

  PHA is a polyester-type organic molecular polymer produced by a wide range of microorganisms. PHA is a biodegradable thermoplastic polymer. PHA can also be produced from renewable resources. For these reasons, attempts have been made to industrially produce PHA as an environmentally conscious material or a biocompatible material and use it in various industries.

  To date, many microorganisms are known to accumulate PHA as an energy storage substance in the cells. A typical example of PHA is poly-3-hydroxybutyric acid (hereinafter also referred to as P (3HB)), which is a homopolymer of 3-hydroxybutyric acid (hereinafter also referred to as 3HB). P (3HB) was first discovered in 1925 in Bacillus megaterium. P (3HB) is a thermoplastic polymer and is biologically decomposed in the natural environment, and thus has attracted attention as an environmentally friendly plastic. However, P (3HB) has a hard and brittle nature because of its high crystallinity, so its practical application range is limited. In order to expand the application range, it was necessary to give flexibility to P (3HB).

  Among them, 3HB and other hydroxy acids such as 3-hydroxyvaleric acid (hereinafter also referred to as 3HV), 3-hydroxypropionic acid (hereinafter also referred to as 3HP), 3-hydroxypentanoic acid (hereinafter also referred to as 3HC). 3-hydroxyhexanoic acid (hereinafter also referred to as 3HH), 3-hydroxyoctanoic acid (hereinafter also referred to as 3HO), 3-hydroxynonanoic acid (hereinafter also referred to as 3HN), 3-hydroxydecanoic acid (hereinafter referred to as Copolyesters obtained by polymerizing 3-hydroxydodecanoic acid (hereinafter also referred to as 3HDD) and the like have been energetically studied (Non-Patent Document 1).

  Among them, as a remarkable one, research on a copolymerized polyester obtained by polymerizing 3HB and 3HH, particularly a copolymer of 3HB and 3HH (hereinafter also referred to as P (3HB-co-3HH)) and a production method thereof. (Patent Documents 1 and 2). The production methods of P (3HB-co-3HH) described therein use Aeromonas caviae and Aeromonas hydrophila isolated from soil, and use fatty acids such as lauric acid, oleic acid, palmitic acid, and glucose as carbon sources. It was the method that was. Studies on the properties of P (3HB-co-3HH) have also been made (Non-Patent Document 2). In this report, A. caviae is cultured using a fatty acid having 12 or more carbon atoms as a sole carbon source, and P (3HB-co-3HH) having a 3HH composition of 11 to 19 mol% is produced by fermentation. This P (3HB-co-3HH) gradually becomes more flexible from the hard and brittle nature of P (3HB) as the 3HH composition increases. From the 3HB and 3HV reported so far, It was clarified that it exhibits a higher flexibility than the copolymer (hereinafter also referred to as P (3HB-co-3HV)).

  In addition, a PHA synthase gene of A. caviae was cloned, and a transformant introduced into a Cupriavidus necator (former classification: Ralstonia eutropha or Alcaligenes eutrophus) having a high PHB accumulation capacity of 90% or more per dry cell was used. There have been reports of producing P (3HB-co-3HH) using fatty acid as a carbon source (Non-patent Document 3, Patent Document 3). Among these, it is reported that P (3HB-co-3HH) having a 3HH composition of 10 to 20 mol% can be produced by using sodium octoate as a carbon source. Furthermore, when producing polyester using the transformant, a method using a plurality of carbon sources is disclosed, and the number of carbons of fats and fatty acids used as the carbon source is 3HH of P (3HB-co-3HH). It was revealed that the composition was affected (Patent Document 4). According to this, by using at least two types of fats and oils and / or fatty acids having different carbon numbers as a carbon source, it becomes possible to produce a polyester having a 3HH composition of 1 to 40 mol%, and P ( 3HB-co-3HH) can be produced. However, in this production method, it is necessary to add expensive fatty acids such as hexanoic acid and octanoic acid or corresponding fatty acid salts for controlling the composition of 3HH, and since high concentrations of hexanoic acid are cytotoxic, As a result, productivity is lowered, and it is not suitable for practical use because it is expensive to apply to industrial production.

  On the other hand, a culture method has been proposed in which the efficiency of conversion to a valerate repeat unit in P (3HB-co-3HV) is increased by feeding phosphorus during culture (Patent Document 5). According to this culture method, the efficiency of propionic acid uptake can be increased by adding phosphoric acid using rapeseed oil or crude corn oil and propionic acid as a carbon source. Specifically, after cell growth is stopped or markedly slowed, the weight ratio of phosphoric acid and carbon source to the total amount of phosphorus (P) of the total amount of carbon (C) (hereinafter referred to as C / P ratio) is 300 to 600. By adding while maintaining within the range up to, the 3HV composition of the obtained P (3HB-co-3HV) is increased to 8.7 mol% compared to the case without adding phosphoric acid (7.4 mol%). It was possible. This phosphate and carbon source addition rate is sufficient to increase cell dry weight to the desired level, but is insufficient to cause substantial growth with suppression of PHA accumulation. . However, since expensive fatty acids are used as described above, production at low cost is difficult.

  Other examples have been reported in which phosphorus fed-batch was performed during the culture of PHB and P (3HB-co-3HV), but both have been carried out for the purpose of increasing polymer productivity (Non-Patent Document 4, 5). In Non-Patent Document 5, in the cultivation of P (3HB-co-3HV), the carbon source was fed so as to be kept at 10 to 30 g / L, and after cell growth stopped, the cell production rate was set to a constant value (0. It is reported that the polymer content is maximized by adding the phosphate aqueous solution necessary for maintaining the pressure to 02 g / L · h) at a constant rate (0.2 mg-P / L · h). However, data on 3HV composition is not shown.

  In addition, the culture period is divided into two phases, a cell growth phase and a polyester accumulation phase, and in each phase, the culture is performed by controlling the specific substrate supply rate of fats and oils used as a carbon source at a constant level. A controlled culture method has been proposed (Patent Document 6). According to this culture method, it is reported that the 3HH composition can be arbitrarily controlled by controlling the flow acceleration of the carbon source without using expensive fatty acids. However, according to the present culture method, in order to increase the 3HH composition, it is necessary to reduce the flow acceleration of the carbon source, so that the polymer productivity is lowered, and a copolymer polymer having a high 3HH composition rich in flexibility is obtained. There was a problem in high production.

  In the future, if a copolymer can be produced by controlling the composition ratio of monomer units of a copolyester such as P (3HB-co-3HH), in particular, the 3HH composition within an arbitrary wide range, it will be soft from a hard copolymer. Copolymers can be fermented and can be applied in a wide range of fields, from those that require hardness, such as television casings, to those that require flexibility, such as yarn and film. It is considered.

JP-A-5-93049 JP 7-265065 A Japanese Patent Laid-Open No. 10-108682 JP 2001-340078 A Japanese National Patent Publication No. 11-500008 International Publication Number WO2004 / 033670

BIO / TECHNOLOGY 13, 142-150 (1995) Macromolecules 28, 4822-3 (1995) J. Bacteriol. 179 (15), 4821-30 (1997) Process Biochemistry (Oxford) 34 (2), 109-14 (1999) Applied Microbiology and Biotechnology 61 (3), 257-60 (2003)

  An object of the present invention is to provide an inexpensive method for producing PHA that can realize high polymer productivity and can arbitrarily control the composition of the copolyester. In addition, an inexpensive PHA production method that can arbitrarily control the 3HH composition of a copolyester obtained by polymerizing at least 3HB and 3HH without using an expensive fatty acid as a carbon source and realizes high polymer productivity. The issue is to provide. It is another object of the present invention to provide a method for arbitrarily controlling the 3HH composition of the copolyester without changing the carbon source during the culture period.

  As a result of intensive studies to solve the above-mentioned problems, the present inventors have produced a microorganism that produces a copolyester composed of two or more components containing at least 3-hydroxybutyric acid and 3-hydroxyhexanoic acid as monomer units. Culturing in a medium containing at least one oil selected from the group consisting of natural oils, fractionated oils, synthetic oils, and mixed oils as a carbon source, and adding a phosphorus compound to the medium during the culture By using the method for producing PHA, a copolymer polyester that not only increases polymer productivity but also has a well-controlled 3HH composition within an arbitrary range without using a particularly expensive fatty acid as a carbon source. The production was found and the present invention was completed.

  That is, one of the features of the present invention is that a microorganism producing a copolyester composed of two or more components including at least 3-hydroxybutyric acid and 3-hydroxyhexanoic acid as a monomer unit is used for natural oils, fractionated fats and oils. A method for producing PHA, comprising culturing a medium containing at least one type of oil selected from the group consisting of oils and fats and mixed oils and fats as a carbon source, and adding a phosphorus compound to the medium during the culture.

  Another feature of the present invention is that the total amount of phosphorus in the phosphorus compound added per unit time of the total amount of carbon (C) in the carbon source added per unit time of the period in which the phosphorus compound is added to the medium ( A method for producing PHA, wherein the weight ratio (C / P ratio) to P) is 150 to 20000.

  Another feature of the present invention is a method for producing a PHA, wherein the C / P ratio is 300 to 12000.

  Another feature of the present invention is a method for producing PHA, wherein the C / P ratio is more than 600 to 1600.

  Another feature of the present invention is a method for producing PHA, wherein the phosphorus compound contains phosphoric acid and / or phosphate.

  Another feature of the present invention is a method for producing PHA in which the copolyester is P (3HB-co-3HH).

  Another feature of the present invention is that the microorganism is any of the genus Cupriavidus, Pseudomonas, Aeromonas, Alcaligenes, or Escherichia. This is a method for producing PHA which is a microorganism belonging to the above.

  Another feature of the present invention is a method for producing PHA, wherein the microorganism is a transformed microorganism into which a polyester polymerizing enzyme gene is incorporated.

  By using the method for producing PHA of the present invention, it is possible to provide an inexpensive method for producing PHA capable of realizing high polymer productivity and arbitrarily controlling the composition of the copolyester. In addition, an inexpensive PHA production method that can arbitrarily control the 3HH composition of a copolyester obtained by polymerizing at least 3HB and 3HH without using an expensive fatty acid as a carbon source and realizes high polymer productivity. Can be provided. Furthermore, it is possible to provide a method for arbitrarily controlling the 3HH composition of the copolyester without changing the carbon source during the culture period.

  The present invention relates to a microorganism that produces a copolyester composed of two or more kinds of constituents containing at least 3-hydroxybutyric acid and 3-hydroxyhexanoic acid as a monomer unit. Natural microorganisms, fractionated fats and oils, synthetic fats and oils, and mixed fats and oils It is related with the manufacturing method of PHA characterized by culturing with the culture medium which contains at least 1 type of fats and oils selected from the group which consists of as a carbon source, and adding a phosphorus compound to a culture medium during culture | cultivation.

  The method for producing PHA for controlling the composition of the copolymerized polyester of the present invention is applied when producing a biodegradable copolymerized polyester using microorganisms.

  The copolyester to which the method for producing PHA of the present invention can be applied is not particularly limited, and any copolyester obtained by polymerizing at least two kinds of monomer units can be used. Specifically, copolymer polyester P (3HB-co-3HH) obtained by polymerizing 3HB and 3HH, a copolymer obtained by polymerizing three components of 3HB, 3HH and 3HV, and other Pseudomonas bacteria Copolymers obtained by polymerizing 3HB, 3HH, 3HO, 3HD, 3HDD, etc. that can be produced can be mentioned as typical examples (Appl. Microbiol. Biotechnol. 47, 207-11 (1997), Appl. Microbiol. Biotechnol. 49, 431-7 (1998)). Among these, P (3HB-co-3HH) is particularly preferable.

  The microorganism used in the present invention was isolated from nature without any particular limitation as long as it produces a copolyester composed of two or more components containing at least 3-hydroxybutyric acid and 3-hydroxyhexanoic acid as monomer units. Microorganisms, microorganisms into which mutations have been introduced, microorganisms that have been genetically manipulated, and microorganisms that have been deposited with a depository organization (for example, IFO, ATCC, etc.) can be used. Specifically, any of the genus Capriavidus (old classification: Ralstonia or Alcaligenes), Aeromonas, Pseudomonas, or Escherichia Can be preferably used.

  In addition, when the microorganism cannot produce the desired copolymer in the wild type state or the production amount is low, the microorganism can be obtained by introducing a polymerization enzyme gene of the desired copolymer polyester into the microorganism. Transformants can be used. When preparing a transformant, a general method such as using a recombinant vector containing a polyester polymerizing enzyme gene can be used, and a plasmid vector capable of autonomously growing in the microbial cell is used as the vector. Can be used. The polyester polymerase gene may be directly integrated into the host chromosome.

  The polyester polymerase enzyme gene used in the production of the copolyester of the present invention is not particularly limited, but a gene isolated from A. caviae is preferable. For example, a gene fragment described in Patent Document 3 is used. Can do. Introduction of a recombinant vector into a microorganism can be performed by a known method. For example, a bonding method, a calcium method, an electroporation method, or the like can be used. As an example of the microorganism used in the present invention, Cupriavidus necator PHB-4 / pJRDEE32d13 strain (Appl. Microbiol. Biotechnol. 49, 333-6 (1998)) in which a polyester polymerase gene derived from A. caviae was introduced into Cupriavidus necator. Can be preferably used.

  In the cultivation method of the present invention, in the production of the copolyester, inexpensive fats and oils are used as the main carbon source in terms of price, supply stability, quality stability, fungus body or polyester yield, etc. as fermentation raw materials. Use as As a nutrient source other than the carbon source, a medium containing a nitrogen source, a phosphorus compound, inorganic salts, and other general organic nutrient sources can be used. From the viewpoint of reducing the production cost, it is preferable to use an expensive organic nitrogen source such as polypeptone, yeast extract, meat extract, etc. in a minimum amount. Although culture | cultivation temperature should just be the temperature which can grow the microbe, 20-40 degreeC is preferable. The culture time is not particularly limited, but may be about 1 to 7 days. Moreover, when using a transformant, you may add antibiotics, such as kanamycin, ampicillin, and tetracycline corresponding to the resistance gene which exists in a vector during culture | cultivation.

  Oils and fats used as a carbon source in the present invention are classified into relatively stable natural oils such as soybean oil, corn oil, cottonseed oil, palm oil, palm kernel oil, coconut oil, and peanut oil, and these oils and fats. Fractionation of each fraction obtained, for example, palm W olein oil (low melting point fraction obtained by fractionating palm oil twice), palm kernel oil olein (low melting point fraction obtained by fractionating palm kernel oil once) Oils and fats, synthetic oils obtained by chemically or biochemically treating these natural fats and their fractions, and mixed oils obtained by mixing them can be used. Among these, it is preferable to use natural fats and oils from the viewpoint of cost.

  In the method of the present invention, the phosphorus source is fed continuously or intermittently throughout the entire period of culture or within a phase period of culture. In this specification, the whole culture period means the whole period from the start of culture to the end of culture in the main culture, and feeding through the whole culture period means that both the cell growth phase and the polyester accumulation phase. It is to feed in the period. In addition, the cell growth phase and polyester accumulation phase of culture here means that when the culture period is roughly divided into two phases, there is a sufficient amount of phosphorus in the medium, and cell growth is active. The first half of the phase where the polyester accumulation rate is relatively low (cell growth phase) and the second half phase (polyester) where the phosphorus concentration in the medium is reduced, the cell growth is restricted, and the polyester accumulation rate is increased. Accumulation period). Substantially, the period in which the residual phosphorus concentration in the medium is 50 ppm or more can be defined as the cell growth period, and the period after the concentration becomes less than 50 ppm as the polyester accumulation period.

  As the phosphorus compound used in the present invention, a phosphorus compound containing phosphoric acid and / or a phosphate can be suitably used.

  One of the features of the present invention is that the total amount of phosphorus (P) in the phosphorus compound added per unit time of the total amount of carbon (C) in the carbon source added per unit time during the period of adding the phosphorus compound to the medium. It is the manufacturing method of PHA which controls the weight ratio (C / P ratio) with respect to.

  Although preferable C / P ratio is based also on the kind of phosphorus compound and carbon source to be used, it is about 150-20000, Preferably it is 300-12000, More preferably, it is more than 600-1600.

In the present invention, it has been found for the first time that the 3HH composition of a copolyester produced, for example, P (3HB-co-3HH), is increased by feeding a phosphorus source during culture. Furthermore, by appropriately changing the feeding period and / or flow acceleration, it is possible to control the rising period and / or rate of the 3HH composition, and as a result, obtain a copolyester having the desired 3HH composition. Is possible. Here, the rate of increase of the 3HH composition is expressed by the following equation.
3HH composition increase rate (mol% / g / L) = (3HH (t2) -3HH (t1)) / (DCW (t2) -DCW (t1))
3HH (t1): 3HH composition at time t1 (mol%)
3HH (t2): 3HH composition (mol%) at time t2
DCW (t1): Weight of dry cells at time t1 (g / L)
DCW (t2): Weight of dry cells at time t2 (g / L)
Examples of the nitrogen source used in the method of the present invention include inorganic nitrogen sources that are ammonium salts such as ammonia, ammonium chloride, ammonium sulfate, and ammonium phosphate, and organic nitrogen sources such as peptone, meat extract, and yeast extract. Examples of the phosphorus source include phosphorus compounds such as potassium monohydrogen phosphate, potassium dihydrogen phosphate, sodium phosphate, sodium monohydrogen phosphate, sodium dihydrogen phosphate, magnesium phosphate, and phosphoric acid. As other inorganic salts, for example, magnesium sulfate, sodium chloride and the like can be used. As other organic nutrient sources, amino acids such as glycine, alanine, serine, threonine, and proline, and vitamins such as vitamin B1, vitamin B12, and vitamin C can be used. However, from the viewpoint of reducing production costs, organic nutrient sources such as peptone, meat extract, yeast extract and amino acids such as glycine, alanine, serine, threonine and proline, and vitamins such as vitamin B1, vitamin B12 and vitamin C are the most used. A small amount is preferable.

  In the present invention, the method for recovering the copolyester from the microbial cells is not particularly limited, and a known solvent extraction method, physical disruption method, chemical treatment method, etc. can be employed. For example, the following method is used. it can. After completion of the culture, the cells are separated from the culture solution using a centrifuge, and the cells are washed with distilled water and methanol, and then dried. Polyester is extracted from the dried cells using an organic solvent such as chloroform. Cellular components are removed from the organic solvent solution containing the polyester by filtration or the like, and a poor solvent such as methanol or hexane is added to the filtrate to precipitate the polyester. The supernatant is removed by filtration or centrifugation, and dried to recover the polyester.

  Examples of the method for analyzing the monomer unit of the obtained polyester include a nuclear magnetic resonance method or a method in which the monomer is methylesterified and then analyzed by gas chromatography or high performance liquid chromatography.

  Hereinafter, the present invention will be described more specifically with reference to examples. In the following examples, P (3HB-co-3HH) was produced as a copolyester. Of course, the scope of the present invention is not limited to these examples, and is not limited to P (3HB-co-3HH).

  For example, it is possible to produce other copolymers other than P (3HB-co-3HH) by changing the type of microorganism, polyester polymerase enzyme gene, or carbon source used.

(Example 1)
Using Pac-bktB / AS + pCUP-631 strain described in Table 1 of International Publication No. WO2009-145164, the culture was performed as follows.

The composition of Tanehaha medium 1w / v% Meat-extract, 1w / v% Bacto-Trypton, 0.2w / v% Yeast-extract, 0.9w / v% Na 2 HPO 4 · 12H 2 O, 0.15w / V% KH ₂ PO ₄ (pH 6.8).

The composition of the preculture medium is 1.1 w / v% Na ₂ HPO ₄ · 12H ₂ O, 0.19 w / v% KH ₂ PO ₄ , 1.29 w / v% (NH ₄ ) ₂ SO ₄ , 0.1 w _{/ v% MgSO 4 · 7H 2} O, 2.5w / v% palm kernel oil olein, 0.5 v / v% trace metal salt solution (in 0.1N hydrochloric acid _{1.6w / v% FeCl 3 · 6H} 2 O, 1 w / v% CaCl ₂ .2H ₂ O, 0.02 w / v% CoCl ₂ .6H ₂ O, 0.016 w / v% CuSO ₄ .5H ₂ O, 0.012 w / v% NiCl ₂ .6H ₂ O Melted).

The composition of the polyester production medium is 0.385 w / v% Na ₂ HPO ₄ · 12H ₂ O, 0.067 w / v% KH ₂ PO ₄ , 0.291 w / v% (NH ₄ ) ₂ SO ₄ , 0.1 w / v% MgSO ₄ .7H ₂ O, 0.5 v / v% trace metal salt solution (1.6 W / v% FeCl ₃ .6H ₂ O in 0.1N hydrochloric acid, 1 w / v% CaCl ₂ .2H ₂ O, 0 0.02 w / v% CoCl ₂ · 6H ₂ O, 0.016 w / v% CuSO ₄ · 5H ₂ O, 0.012 w / v% NiCl ₂ · 6H ₂ O)), 0.05 w / v% BIOSPUMEX 200K (antifoaming agent: manufactured by Cognis Japan) was used. As the carbon source, palm kernel oil olein, which is a low melting point fraction obtained by fractionating palm kernel oil, was used. As the aqueous solution of phosphate for feeding, one prepared to be 4.00 w / v% Na ₂ HPO ₄ · 12H ₂ O, 0.69 w / v% KH ₂ PO ₄ was used.

  A glycerol stock (50 μl) of the KNK-631 strain was inoculated into a seed mother medium (10 ml), cultured for 24 hours, and a 3 L jar fermenter (MDL-300 model manufactured by Marubishi Bioengineering) containing 1.8 L of a preculture medium ) Was inoculated with 1.0 v / v%. The operating conditions were a culture temperature of 33 ° C., a stirring speed of 500 rpm, and an aeration rate of 1.8 L / min. And culturing for 28 hours while controlling the pH between 6.7 and 6.8. A 7% aqueous ammonium hydroxide solution was used for pH control.

In the production culture of PHA, a 10 L jar fermenter (MDL-1000 type, manufactured by Maruhishi Bioengine) containing 4.3 L of production medium was inoculated with 5.0 v / v% of the preculture seed. The operating conditions were a culture temperature of 28 ° C., a stirring speed of 600 rpm, and an aeration rate of 6 L / min. And the pH was controlled between 6.7 and 6.8. A 14% aqueous ammonium hydroxide solution was used for pH control. The carbon source is palm kernel oil olein throughout the culture so that the specific substrate feed rate is 0.1 to 0.12 (g fat) x (g net dry cell weight) ^-1 x (h) ^-1. Fed. Here, the specific substrate supply rate is a culture variable defined as the amount of oil supplied per unit time per net cell weight, that is, the oil flow acceleration per net dry cell weight. The net dry cell weight is the dry cell weight obtained by subtracting the polyester weight contained from the total dry cell weight. That is, the specific substrate supply rate is a value obtained from the following equation.
Specific substrate feed rate = Oil flow acceleration (g / h) / Net dry cell weight (g) = Oil feed per unit time (g / h) / (Total dry cell weight (g) -Polyester content Amount (g))
Moreover, the phosphate aqueous solution was continuously added after 20 hours of culture at a flow rate such that the C / P ratio was 600 to 800. Culturing was carried out for about 64 hours. After completion of the cultivation, the cells were collected by centrifugation, washed with methanol, lyophilized, and the weight of the dried cells was measured.

  100 ml of chloroform was added to about 1 g of the obtained dried microbial cells, and stirred overnight at room temperature to extract the polyester in the microbial cells. The bacterial cell residue was filtered off and concentrated with an evaporator until the total volume reached about 30 ml. Then, about 90 ml of hexane was gradually added, and the mixture was allowed to stand for 1 hour with slow stirring. The precipitated polyester was filtered off and then vacuum dried at 50 ° C. for 3 hours. The weight of the dried polyester was measured, and the polymer content in the cells was calculated.

  The 3HH composition of the copolyester was measured by gas chromatography as follows.

  To 20 mg of the dried polyester, 2 ml of a sulfuric acid-methanol mixture (15:85) and 2 ml of chloroform were added and sealed, and heated at 100 ° C. for 140 minutes to obtain a methyl ester of a polyester degradation product. After cooling, 1.5 g of sodium bicarbonate was added little by little to neutralize it, and the mixture was allowed to stand until the generation of carbon dioxide gas stopped. After adding 4 ml of diisopropyl ether and mixing well, the mixture was centrifuged and the monomer unit composition of the polyester degradation product in the supernatant was analyzed by capillary gas chromatography. The gas chromatograph used was Shimadzu Corporation GC-17A, and the capillary column used was GL Science's NEUTRA BOND-1 (column length 25 m, column inner diameter 0.25 mm, liquid film thickness 0.4 μm). He was used as the carrier gas, the column inlet pressure was 100 kPa, and 1 μl of the sample was injected. As temperature conditions, the temperature was raised from the initial temperature of 100 to 200 ° C. at a rate of 8 ° C./min, and further from 200 to 290 ° C. at the rate of 30 ° C./min.

  The content of the copolyester accumulated in the cells was determined from the cultured cells according to the method of Kato et al. (Appl. Microbiol. Biotechnol. 45, 363 (1996), Bull. Chem. Soc. 69, 515 (1996)). It extracted by using, and calculated | required by measuring the weight after drying.

(Example 2)
Cultivation was performed under the same conditions as in Example 1 except that the phosphate aqueous solution was added at a flow rate such that the C / P ratio was 300 to 400.

(Example 3)
Cultivation was carried out under the same conditions as in Example 1 except that the phosphate aqueous solution was added at a flow rate such that the C / P ratio was 200 to 300.

Example 4
Cultivation was performed under the same conditions as in Example 1 except that the phosphate aqueous solution was added at a flow rate such that the C / P ratio was 1200 to 1600.

(Example 5)
The culture volume is 5.4 L, the stirring speed is 400 rpm, and the aeration rate is 3.6 L / min. The culture was carried out under the same conditions as in Example 1 except that.

(Example 6)
Cultivation was performed under the same conditions as in Example 5, except that the aqueous phosphate solution was added at a flow rate such that the C / P ratio was 100 to 200.

(Comparative Example 1)
The culture was carried out under the same conditions as in Example 1 except that the phosphate aqueous solution was not fed during the culture.

  Table 1 shows the effect of adding an aqueous phosphate solution on the 3HH composition.

  From this result, it was found that the 3HH composition in the copolyester was increased by feeding a phosphate aqueous solution during the cultivation. Moreover, it became clear that the 3HH composition in the copolyester further increased as the C / P ratio decreased, in other words, as the phosphorus flow acceleration relative to the carbon source flow acceleration was relatively increased. Moreover, although the polymer productivity is increased by feeding the phosphate aqueous solution, it has been clarified that the PHBH productivity is lowered when the C / P ratio is a certain value or less.

(Example 7)
Culturing was carried out under the same medium and conditions as in Example 1 except that palm W olein oil was used instead of palm kernel oil olein, and the results shown in Table 2 were obtained.

(Comparative Example 2)
Cultivation was performed under the same conditions as in Example 7 except that the phosphate aqueous solution was not fed during the culturing. Table 2 shows the effect of the carbon source used on the 3HH composition.

  As shown in Table 2, even when palm W olein oil was used as a carbon source, as in the case of using palm kernel oil olein, by adding a phosphate aqueous solution, It was found that the 3HH composition was improved. However, when the 3HH composition is compared between the palm W olein oil and the palm kernel oil olein of Example 1 under the same phosphate aqueous solution supply conditions, the palm W olein oil is clearly lower and the same phosphate aqueous solution supply conditions. However, it was found that there is a difference in the 3HH composition obtained depending on the fat and oil used as the substrate.

(Example 8)
Culturing was performed under the same conditions as in Example 1 except that the strain used for the culture was the KNK-005 strain described in International Publication No. WO2008 / 010296. The results are shown in Table 3.

(Comparative Example 3)
Cultivation was performed under the same conditions as in Example 8 except that the phosphate aqueous solution was not fed during the culturing. Table 3 shows the effect of different strains used on the 3HH composition.

  From the above results, it was found that 3HH composition improvement effect by feeding phosphate aqueous solution was recognized regardless of the strain used.

Claims (5)

A microorganism belonging to the genus Cupriavidus that produces a copolyester comprising two or more constituents containing at least 3-hydroxybutyric acid and 3-hydroxyhexanoic acid as a monomer unit, and a natural fat and / or a fractionated fat A method for producing PHA , comprising culturing in a medium containing a carbon source and adding a phosphorus compound to the medium during the culture , wherein carbon added per unit time of a period during which the phosphorus compound is added to the medium A method for producing PHA, wherein the weight ratio (C / P ratio) of the total amount of carbon (C) in the source to the total amount of phosphorus (P) in the phosphorus compound added per unit time is more than 600 to 1600. The method for producing a PHA according to claim 1, wherein the C / P ratio is more than 600 to 800. The phosphorus compound, according to claim 1 or 2 method for producing PHA according characterized in that it comprises a phosphoric acid and / or phosphate. The method for producing PHA according to any one of claims 1 to 3, wherein the copolyester is P (3HB-co-3HH). The method for producing PHA according to any one of claims 1 to 4 , wherein the microorganism is a transformed microorganism into which a polyester polymerizing enzyme gene is incorporated.