METHOD OF PRODUCING HIGHLY PURE TEICOPLANIN Technical Field [1] The present invention pertains to a method of cultivating a microorganism, which is capable of producing teicoplanin, and of producing highly pure teicoplanin using a culture broth. More particularly, the present invention relates to a method of eco¬ nomically producing highly pure teicoplanin, in which teicoplanin is produced at a stable, neutral pH region. [2] Background Art [3] Recently, it is regarded as a serious problem that an antibiotic-resistant mi¬ croorganism is spread due to abuse of an antibiotic. With respect to this, teicoplanin acts against gram-positive bacteria, which is a glycopeptide antibiotic. Particularly, te¬ icoplanin, a glycopeptide antibiotic, which acts against gram positive bacteria, such as methicillin-resistant Staphylococcus aureus (MRSA), coagulase-negative Staphylococcus, Clostridium and Enterococcus, is called as a last defense line to infectious diseases. Teicoplanin is a complex of five kinds of A2 components, having different fatty acid branched chains, and A3, having an aglycone structure in which a sugar moiety of N-acyl-β-D-glucosamine, including the fatty acid branched chain, is removed from a basic structure of A2. In this specification, teicoplanin is designated by the teicoplanin A2 complex acting as an effective component. [4] Generally, a chemical synthetic process or a bio-synthetic process using the culture of the microorganism is adopted to produce antibiotics in commercial quantities. The glycopeptide antibiotics have a complicated chemical structure, in which sugar is bonded to a peptide skeleton. Hence, teicoplanin and the glycopeptide antibiotics com¬ mercialized as pharmaceuticals are produced according to the bio-synthetic process, which is a so-called fermentation process. In the bio-synthetic process, various impurities, such as medium components and metabolic products, are produced con¬ comitantly with the antibiotic. Accordingly, a number of separation and purification processes are required to purify the antibiotics, which are critical factors in eco¬ nomically producing the highly pure antibiotic. [5] Teicoplanin, a glycopeptide antibiotic produced from Actinoplanes tei- chomyceticus, was first reported in "The Journal of Antibiotics (Vol. 31;170-177, 1978)". A number of efforts have been made to separate teicoplanin from a culture broth of the microorganism and purify teicoplanin using various processes so as to produce teicoplanin of pharmaceutical grade. According to the above journal and US Pat. No. 4,239,751, a culture broth is divided into a mycelial cake and a filtrate. The mycelial cake is extracted with acetone and the extract is extracted again with butanol at acidic pH. The filtrate, made free from the mycelial mass by filtration, is extracted with butanol at acidic pH. Subsequently, the butanol layers are concentrated by vacuum distillation to form precipitates. The precipitates are mixed with each other, and the mixture is purified with Sephadex LH20 column. The eluate from Sephadex LH20 is further purified with an acidic ion exchange resin, such as IR- 120 and Dowex 50, and then, the teicoplanin is precipitated at 4°C. However, US Pat. No. 4,239,751 has disadvantages in that the purification is very complicated. Furthermore, it is difficult that Sephadex LH 20 is too expensive to apply in a large scale production. Another disadvantage is that the recovery and purity of teicoplanin are poor. [6] Korean Pat. No. 36780 recites a process of directly extracting teicoplanin from a culture broth, in which a water-miscible organic solvent, such as acetone, n-propanol, and acetonitrile, is added without separating mycelia. Furthermore, Korean Pat. No. 118034 discloses a process of producing teicoplanin by directly adding a strongly acidic cation exchange resin, such as Dow XFS-43278.00 and Diaion SK- 102, to a culture broth. However, Korean Pat. Nos. 367890 and 118034 are disadvantageous in that even though a process of directly extracting teicoplanin from the culture broth is more simplified than in the case of US Pat. No. 4,239,751, it is difficult to employ in the production process because a great amount of organic solvent that is inevitably used to extract teicoplanin may bring about a environmental pollution. In addition, it is difficult to produce highly pure teicoplanin by only modifying the extraction process. [7] Many studies have been carried out to purify teicoplanin by column chro¬ matographic processes using synthetic resins, as suggested by Heydorn et al., "J. of Biochem. Vol. 275; 6201-6206, 2000", and as disclosed in European Pat. No. 241,758, Korean Pat. No. 321304, Korean Pat. Laid-Open Publication No. 2003-0017067, and Korean Pat. Laid-Open Publication No. 2003-0034949. Additionally, European Pat. No. 241,758 recites a process of purifying teicoplanin using a polyamide resin. Further, Korean Pat. No. 184644 discloses an extraction process of teicoplanin from mycelium at alkaline pH, thereby simplifying a complicated extraction process of US Pat. No. 4,239,751. In Korean Pat. No. 184644, after the extraction of teicoplanin, the basic culture broth is neutralized, and then purified using the polyamide resin according to a procedure of European Pat. 241,758. However, when the purified teicoplanin was analyzed by HPLC (high performance liquid chromatography), the purity of te¬ icoplanin was nothing but 85 % and the decolorization was poor. Therefore, it can be seen that it is required to perform a further purifying process so as to produce highly pure teicoplanin. In order to study a biosynthetic pathway of teicoplanin, Heydorn et al. had separated and purified teicoplanin according to a chromatography process using an ion-exchange resin (Amberlite IRA958) and a hydrophobic adsorption resin (Diaion HP2MGL). However, this method suggested by Heydorn et al. is disadvantageous in that it is inconvenient because acetic acid has to continuously add to the basic solution passing through the resin to neutralize it and prevent an epimerization. Additionally, when the purity of teicoplanin is analyzed by HPLC after the purified solution is desalted, concentrated, and lyophilized to produce teicoplanin powder, the purity is a mere 50 to 60 %(w/w). Accordingly, it is undesirable to use the teicoplanin powder thusly produced as pharmaceutical ingredient. [8] Meanwhile, porous adsorption resins have been frequently used to purify gly- copeptide antibiotics, including teicoplanin. In detail, Korean Pat. No. 321304 discloses a process of purifying teicoplanin, which includes a hydrophobic interaction chromatography step using a neutral adsorption resin and a lectin-immobilized affinity chromatography step. At this time, the neutral adsorption resin is selected from the group consisting of XAD 16, HP 20, silica gel, and activated carbon. In this patent, a filtered culture broth is directly purified by the hydrophobic adsorption chr omatography using HP-20 and the like, and thus, it is convenient to conduct the process. However, in case that the filtered culture broth extracted from a basic solution is adsorbed into a resin, such as HP 20, according to the process of Korean Pat. No. 321304, a great amount of teicoplanin is lost in an adsorption step, and the purity of te¬ icoplanin eluted by a methanol concentration gradient is very low. Moreover, it is necessary to remove methanol in order to apply the solution to a lectin-immobilized resin. Furthermore, it is not desirable to apply in the large scale production because of the cost of lectin-immobilized resins. [9] According to Korean Pat. Laid-Open Publication No. 2003-0017067, after te¬ icoplanin of a culture broth is adsorbed into a porous adsorption resin, the porous adsorption resin is washed with diluted hydrochloric acid, and teicoplanin is desorbed from the adsorption resin using a mixed solution of water and acetone. The eluting solution containing teicoplanin is concentrated by vacuum distillation, treated with an activated carbon, and subjected to a precipitation process, and thereby teicoplanin is purified. However, Korean Pat. Laid-Open Publication No. 2003-0017067 is disad¬ vantageous in that the stability and activity of teicoplanin are decreased because the pH of a process liquid is continuously changed to acid or basic. Other disadvantages are that a life-time and an exchange cycle of the resin are shortened, and recovery yield and purity of teicoplanin are poor because of moieties irreversibly adsorbed into the resin. Meanwhile, Korean Pat. Laid-Open Publication No. 2003-0034949 discloses a method of producing teicoplanin, which includes roughly purifying teicoplanin from a culture broth through a two-stage process using porous adsorption resins, and pre¬ cipitating teicoplanin at low temperatures and slightly acidic pH. However, this method has disadvantages in that the use of a large amount of organic solvent, such as n-propanol, isopropanol, and methanol, may bring about pollution, and that pre¬ cipitation at low temperature and slightly acidic pH reduces the solubility and activity of teicoplanin. [10] Furthermore, it is difficult to purify teicoplanin of 95 % or higher through only a purifying process using porous adsorption resins. Accordingly, many studies have been carried out with reverse phase resins to separate and purify teicoplanin from the culture broth. For example, references may be made to a process suggested by Riva et al. (Chromatographia Vol. 24; 295-301, 1987), and to the patents, Korean Pat. No. 40453, and Korean Pat. Laid-Open Publication Nos. 2003-0092504 and 10-2004-0008745. Riva et al. proposed a process of purifying teicoplanin using a Lichrosorb RP- 18 column. Korean Pat. No. 40453 discloses a process of separating each single component of teicoplanin A2 complex using a silanized silica gel column. At this time, in the case of using the reverse phase resin, it is possible to produce more pure te¬ icoplanin than in the case of a separation process using a combination of an extraction, an ion-exchange resin, and a porous adsorption resin. However, Korean Pat. No. 40453 is problematic in the economic efficiency because the reverse phase resin and high pressure chromatography system are both costly. Particularly, acetonitrile, toxic for nervous systems of human, is used in eluting teicoplanin from the reverse phase resin in Korean Pat. No. 40453. Furthermore, Korean Pat. Laid-Open Publication No. 2003-0092504 proposes a method of purifying teicoplanin, in which a mycelium- free culture broth directly passes through a reverse phase resin, such as YMC-gel ODS-A, or in which a roughly purified liquid, pre-treated with a cation-exchange resin, an anion-exchange resin, or a adsorption resin, passes through YMC-gel ODS-A. However, this method is disadvantageous in that acetonitrile is used for the elution, and thus, the residual amount of acetonitrile should be controlled. Another disadvant age is that production costs are inevitably increased because the reverse phase resin is frequently replaced with a new one. As well, Korean Pat. Laid-Open Publication No. 10-2004-0008745 recites a process of purifying teicoplanin from a culture broth of a microorganism capable of producing teicoplanin, which includes a primary purifying step using a synthetic adsorbent, a secondary purifying using a cation-exchange resin, a catalytic resin, or a chelate resin, a tertiary purifying step using a reverse phase resin, and a final lyophilization step. However, Korean Pat. Laid-Open Publication No. 10-2004-0008745 is disadvantageous in that even though highly pure teicoplanin is produced, the process is very complicated because the process includes a number of steps, and recovery yield of teicoplanin is very low. Moreover, Korean Pat. Laid-Open Publication No. 10-2004-0008745 has the same disadvantages, regarding the use of the reverse phase resin, as Korean Pat. Laid-Open Publication No. 2003-0092504. Disclosure of Invention Technical Problem [11] Accordingly, conventional technologies of purifying teicoplanin from the culture broth are problematic in that highly purified teicoplanin, containing no impurities and colored moieties, is not produced, stability of teicoplanin is not maintained, the organic solvents toxic to humans are used during the purification, recovery yield is relatively low, and production costs are relatively high. Hence, there remains a need to develop an improved technology of purifying teicoplanin. [12] Technical Solution [13] Therefore, the present invention has been made keeping in mind the above dis¬ advantages occurring in the prior arts, and an object of the present invention is to provide a method of inexpensive and safe producing highly pure teicoplanin. At this time, the production of teicoplanin is carried out at a stable, neutral pH. [14] The above object can be accomplished by providing a method of producing te¬ icoplanin according to a first aspect of the present invention. With the term "culture broth" as used hereafter it is denoted the filtered culture broth made free from the mycelium. The method includes (a) eluting a culture broth of Actinoplanes tei- chomyceticus strain capable of producing the teicoplanin, adsorbed in a porous adsorption resin, from the porous adsorption resin to produce a roughly purified liquid, containing teicoplanin, and (b) treating the roughly purified liquid using an activated carbon to recover the highly pure teicoplanin. [15] At this time, the method also includes ultrafiltration of the liquid treated with the activated carbon after the step of (b). [16] The above object can be accomplished by providing a method of producing te¬ icoplanin according to a second aspect of the present invention. The method includes (a) eluting a culture broth of Actinoplanes teichomyceticus strain capable of producing the teicoplanin, adsorbed in a porous adsorption resin, from the porous adsorption resin to produce a roughly purified liquid, containing teicoplanin, and (b) ultrafiltration of the roughly purified liquid to recover the highly pure teicoplanin. [17] In this regard, the method also includes treating the permeate of ultrafiltration using an activated carbon after the step of (b). [18] The above object can be accomplished by providing a method of producing te¬ icoplanin according to a third aspect of the present invention. The method includes (a) ultrafiltration of a culture broth of Actinoplanes teichomyceticus strain capable of producing the teicoplanin, (b) eluting the permeate of ultrafiltration, adsorbed in a porous adsorption resin, from the porous adsorption resin to produce a roughly purified liquid, containing teicoplanin, and (c) treating the roughly purified liquid using an activated carbon to recover the highly pure teicoplanin. [19] In this regard, the method also includes ultrafiltration of the liquid treated with the activated carbon after the step of (c). [20] The above object can be accomplished by providing a method of producing te¬ icoplanin according to a fourth aspect of the present invention. The method includes (a) ultrafiltration of a culture broth of Actinoplanes teichomyceticus strain capable of producing the teicoplanin, (b) eluting the permeate of ultrafiltration, adsorbed in a porous adsorption resin, from the porous adsorption resin to produce a roughly purified liquid, containing teicoplanin, and (c) ultrafiltration of the roughly purified liquid to recover the highly pure teicoplanin. [21] In this respect, the method also includes treating permeate of ultrafiltration using an activated carbon after the step of c). [22] Additionally, the Actinoplanes teichomyceticus strain includes Actinoplanes tei¬ chomyceticus DKB 53. [23] Further, an eluting agent to elute teicoplanin from the porous adsorption resin includes 40 to 90 %(v/v) of Cl to C4 water-miscible alcohol with pH of 6.0 to 8.0, or 40 to 90 %(v/v) of C3 to C6 water-miscible ketone with pH of 6.0 to 8.0. [24] Alternatively, an eluting agent to elute teicoplanin from the porous adsorption resin may include a neutral salt. [25] Furthermore, a neutral salt includes 0.05 to 0.5 M of sodium salt or potassium salt. [26] As well, the porous adsorption resin has a pore radius of 20 to 300 A, and is at least one selected from the group consisting of DOWEX OPTIPORE L493, DOWEX OPTIPORE L323, DOWEX OPTIPORE SD-2, DIAION HP20, DIAION HP2MG, DIAION HP20SS, SEPABEADS SP825, SEPABEADS SP 850, SEPABEADS SP 700, SEPABEADS SP207, SEPABEADS SP20SS, AMBERLITE XAD4, AMBERLITE XAD7, AMBERLITE XAD16, and AMBERLITE XAD1600T. [27] The activated carbon is added into the roughly purified liquid at 0.2 to 5 times more weight than teicoplanin at 10 to 400C within 12 hours. [28] In addition, the activated carbon is added into the roughly purified liquid at 0.5 to 3 times more weight than teicoplanin at 18 to 36°C within 0.5 to 3 hours. [29] Furthermore, the treating of the roughly purified liquid using the activated carbon comprises directly adding the activated carbon into a process liquid with a pH of 6 to 8 passing through the porous adsorption resin, or adding the activated carbon into the process liquid diluted with water. [30] Additionally, the activated carbon is at least one selected from the group consisting of AQUA NUCHAR, NUCHAR SA, NUCHAR SA-20, NUCHAR SA-30, NUCHAR SN, NUCHAR SN-20, NORIT A SUPRA EUR, NORIT B SUPRA EUR, NORIT C EXTRA USP, NORIT CN 1, NORIT CN 3, DARCO G 60, DARCO KB, DARCO KB-B, NORIT E SUPRA USA, NORIT GBG, NORIT PN2, NORIT ROX 0.8, NORIT SX 1, NORIT SX IG, NORIT SX 2, NORIT SX PLUS, NORIT SX SUPRA E 153, NORIT SX ULTRA, CAL 12X40, and GW 12X40. [31] The activated carbon is removed by filtering. As well, the roughly purified liquid is further purified by method of adsorbing the filtered liquid into the porous adsorption resin, washing the porous adsorption resin using water, and eluting teicoplanin using 40 to 90 %(v/v) of Cl to C4 water-miscible organic solvent. [32] Furthermore, the porous adsorption resin, which is used after the activated carbon is removed, has a pore radius of 20 to 300 A, and is at least one selected from the group consisting of DOWEX OPTIPORE L493, DOWEX OPTIPORE L323, DOWEX OPTIPORE SD-2, DIAION HP20, DIAION HP2MG, DIAION HP20SS, SEPABEADS SP825, SEPABEADS SP 850, SEPABEADS SP 700, SEPABEADS SP207, SEPABEADS SP20SS, AMBERLITE XAD4, AMBERLITE XAD7, AMBERLITE XAD 16, and AMBERLITE XAD 1600T. [33] A membrane, used in the ultrafiltration of the culture broth or roughly purified liquid, has a molecular weight cut-off of 3000 to 100000 Da. [34] Further, the ultrafiltration is carried out at a temperature of 8 to 300C, an input pressure of 0 to 4 bar and a retentate pressure of 0 to 3.5 bar. [35] Alternatively, the ultrafiltration may be carried out at a temperature of 12 to 18°C, an input pressure of 0 to 4 bar and a retentate pressure of 0 to 3.5 bar. [36] As well, the ultrafiltration membrane is made of polyether sulfone or regenerated cellulose, and is at least one selected from the group consisting of Biomax, Ultracel, PT and PL of Prostak module, Helicon, Sartocon, Ultrasart, OMEGA, ALPHA, REGEN, SUPOR, Filmtec, and Kvick. [37] Advantageous Effects [38] As described above, the present invention is advantageous in that the production of teicoplanin is carried out within a neutral pH region, thereby ensuring the high stability and improving the purity of teicoplanin. Other advantages are that impurities, such as colored components, are clearly removed, and it is possible to apply in large scale production of teicoplanin. [39] The present invention has been described in an illustrative manner, and it is to be understood that the terminology used is intended to be in the nature of description rather than of limitation. Many modifications and variations of the present invention are possible in light of the above teachings. Therefore, it is to be understood that within the scope of the appended claims, the invention may be practiced otherwise than as specifically described. [40] Brief Description of the Drawings [41] The above and other objects, features and other advantages of the present invention will be more clearly understood from the following detailed description taken in conjunction with the accompanying drawings, in which: [42] FIG. 1 illustrates results regarding an HPLC analysis of teicoplanin. [43] Best Mode for Carrying Out the Invention [44] Hereinafter, a detailed description will be given of the present invention. [45] In the present invention, any strain may be used as a microorganism to produce highly pure teicoplanin as long as the strain is capable of producing teicoplanin. With respect to this, examples of the microorganism include Actinoplanes teichomyceticus, such as Actinoplanes teichomyceticus DKB53 (KCTC 10587BP) and Actinoplanes tei¬ chomyceticus ATCC31121 suggested by U.S. Pat. No. 4,239,751. Preferably, Actinoplanes teichomyceticus DKB53 (KCTC 10587BP) is used to produce te¬ icoplanin. Additionally, the microorganism may be optimally cultured under the following conditions. [46] In other words, a carbon source used in a culture medium for fermentation is ex¬ emplified by glucose, maltose, sucrose, and galactose. In consideration of the costs of raw materials, it is more preferable that starch is used in the medium for seed culture and maltose is used in a culture medium for production culture. [47] In the case of using maltose as a carbon source, it is preferable that the culture medium for teicoplanin production includes 40 to 100 gll of maltose, 3 to 5 gll of yeast extract, 5 to 10 gll of soybean flour, 5 to 10 gl£ of cottonseed meal, 3 to 5 UIl of corn steep liquor (CSL), 0.1 to 5 gll of sodium chloride, and 0.1 to 10 mgll of trace metal elements. [48] When Actinoplanes teichomyceticus DKB53 is cultivated, range of an optimum pH is preferably 6.8 ? 0.2. At this time, it is preferable that a culture temperature is 28 to 34°C. [49] Optimum culture conditions of Actinoplanes teichomyceticus DKB53 used to produce teicoplanin with high yield are as follows. [50] In an early step of the fermentation, it is preferable that the culture is carried out at an air flow rate is 1.0 to 1.5 vvm, pressure in a fermentation device is maintained to 0.2 to 0.3 bar, the fermentation temperature is 28 to 34°C, and the agitation is carried out at an agitation speed of 140 to 200 rpm. [51] In a middle step of the fermentation, it is preferable that the agitation speed is gradually increased to a speed range of 200 to 400 rpm within 48 to 90 hours since the fermentation start. The reason for this is that a gradual increase of the agitation speed is preferable in view of an oxygen utilization rate (OUR). More preferably, after the agitation speed is gradually increased, the air flow rate is controlled to 0.4 to 0.8 vvm while the pressure in the fermentation device being maintained to 0.1 to 0.2 bar, leading to the proper control of partial oxygen pressure. [52] According to the present invention, a method of producing teicoplanin includes a roughly purification step using a porous adsorption resin under a selective elution condition and a step of recovering highly pure teicoplanin using an activated carbon or/and an ultrafiltration. In this regard, the method may further include an ultra¬ filtration step as a pre-treating step before the culture broth is adsorbed into the porous adsorption resin so as to increase the purity of teicoplanin. [53] After the fermentation, the pH of the culture broth, in which the microorganism capable of yielding teicoplanin is cultured, and from which a mycelium is removed, is controlled to a neutral region of 6 to 8. In this respect, sodium hydroxide or hy¬ drochloric acid may be used to control the pH of the culture broth to the neutral region. After the pH of the clarified culture broth is controlled as described above, it is not necessary to conduct a further pH control process. More preferably, the pH of the clarified culture broth as a starting material in the roughly purification step using the porous adsorption resin is 6.5 to 7.5. At this time, it should be understood that the term "porous adsorption resin" as used herein is intended to include a synthetic adsorbent with a pore radius of 20 to 300 A, which is comprised of a polymer having no ion- exchange groups, such as a polymer of styrene and divinyl benzene, a cross-linked aromatic or aliphatic polymer, and a methacryl adsorbent. In detail, examples of the porous adsorption resin include DOWEX OPTIPORE L493, DOWEX OPTIPORE L323, and DOWEX OPTIPORE SD-2, manufactured by Dow Chemical Co., DIAION HP20, DIAION HP2MG, DIAION HP20SS, SEPABEADS SP825, SEPABEADS SP850, SEPABEADS SP700, SEPABEADS SP207, and SEPABEADS SP20SS, man¬ ufactured by Mitsubishi Chemical Co., and AMBERLITE XAD4, AMBERLITE XAD7, AMBERLITE XAD16, and AMBERLITE XAD1600T, manufactured by Rohm & Haas Co.. [54] After the porous adsorption resin is packed in a column, the culture broth is applied onto the column, or the porous adsorption resin is added into the culture broth in a vessel and a mixture is agitated to adsorb teicoplanin into the porous adsorption resin. In this regard, Cl to C4 water- miscible alcohol may be added to the neutral culture broth preferably in an amount less than 40 % (v/v), and more preferably, in an amount of 5 to 20 % (v/v) to prevent adsorption of impurities into the porous adsorption resin and to prevent the denaturing of teicoplanin due to an enzyme contained in the culture broth. The porous adsorption resin, including teicoplanin adsorbed thereinto, is washed with a mixed liquid of 10 to 40 % (v/v) of Cl to C4 alcohols or C3 to C6 ketones and water to sufficiently remove impurities or colored components therefrom. [55] Teicoplanin may be selectively eluted from the porous adsorption resin by controlling a salt concentration in an eluting agent. The eluting agent, used to elute te¬ icoplanin adsorbed into the porous adsorption resin, includes 0.05 to 0.5 M of neutral salt, and the mixed liquid of Cl to C4 alcohol or C3 to C6 ketone, and water. The neutral salt is exemplified by a sodium salt, such as sodium chloride and sodium phosphate, and a potassium salt, such as potassium chloride. Preferably, a con¬ centration of the salt added to the eluting agent is 0.1 to 0.3 M. In the case of using the eluting agent containing the salt, teicoplanin is produced at a relatively high purity in comparison with the case of using the mixed liquid of water-miscible organic solvent and water, containing no salt, as the eluting agent. In addition, because the pH of a process liquid added to the porous adsorption resin is maintained to be neutral, an epimerization of teicoplanin, occurring when the process liquid is basic, and the reduction of activity of teicoplanin, occurring when the process liquid is acidic, are prevented. [56] Roughly purified teicoplanin passing through the porous adsorption resin may be highly purified according to an activated carbon treating process, an ultrafiltration process, or a combined process of the activated carbon treating and ultrafiltration processes. [57] The activated carbon has been used to remove various impurities, such as colored components and substances with offensive odors, during the production of chemicals, foodstuffs and pharmaceuticals for a long time. Examples of the commercial activated carbon useful in the present invention include AQUA NUCHAR, NUCHAR SA, NUCHAR SA-20, NUCHAR SA-30, NUCHAR SN, and NUCHAR SN-20, man¬ ufactured by MeadWestvaco Co., NORIT A SUPRA EUR, NORIT B SUPRA EUR, NORIT C EXTRA USP, NORIT CN 1, NORIT CN 3, DARCO G 60, DARCO KB, DARCO KB-B, NORIT E SUPRA USA, NORIT GBG, NORIT PN 2, NORIT ROX 0.8, NORIT SX 1, NORIT SX IG, NORIT SX 2, NORIT SX PLUS, NORIT SX SUPRA E 153, and NORIT SX ULTRA, manufactured by NORIT Nederland B.V., and CAL 12X40 and GW 12X40, manufactured by Calgon Carbon Co.. Additionally, the activated carbon may be added directly to the roughly purified liquid passing through the porous adsorption resin or added to it after dilution with water. In other words, the method of the present invention is advantageous in that the activated carbon may be directly added to roughly purified liquid passing through the porous adsorption resin, or added to roughly purified liquid after a concentration of the water-miscible organic solvent or salt is reduced by addition of water, and thus, organic solvent removal, desalting, and concentration processes may be omitted. [58] After teicoplanin content in the process liquid passing through the porous adsorption resin is measured using HPLC (high performance liquid chromatography) according to a method as described in Japanese Pharmacopoeia, the activated carbon is preferably added to the process liquid by a 0.2 to 5 times more amount than a measured teicoplanin. More preferably, the activated carbon is added to the process liquid by a 0.5 to 3 times more amount than the teicoplanin. After the activated carbon is added to the process liquid, it is checked whether the pH of the process liquid is 6 to 8, or not. The process liquid is then agitated at 10 to 400C within 12 hours. More preferably, the process liquid is treated with the activated carbon at 18 to 36°C for 0.5 to 3 hours, thereby preventing teicoplanin from being irreversibly adsorbed into the activated carbon and promoting the adsorption of the impurities, such as colored components, into the activated carbon. [59] After the process liquid is treated with the activated carbon, the process liquid is filtered using a KS 80 filter (manufactured by Pall Co.) or Whatman filter paper 4 (manufactured by Whatman Int'l Ltd.) to remove the activated carbon from the process liquid, and then is passed through the column, in which the porous adsorption resin is packed, or is adsorbed into the porous adsorption resin in a vessel. Subsequently, the porous adsorption resin is washed with water, and teicoplanin is eluted from the porous adsorption resin using the eluting agent in which any one of Cl to C4 water- miscible alcohols is mixed with water in an amount of 40 to 90 % (v/v). With respect to this, the porous adsorption resin is selected from the group consisting of DOWEX OPTIPORE L493, DOWEX OPTIPORE L323, DOWEX OPTIPORE SD-2, DIAION HP20, DIAION HP2MG, DIAION HP20SS, SEPABEADS SP825, SEPABEADS SP850, SEPABEADS SP700, SEPABEADS SP207, SEPABEADS SP20SS, AMBERLITE XAD4, AMBERLITE XAD7, AMBERLITE XAD16, and AMBERLITE XAD1600T. [60] The ultrafiltration process is applied to separate substances with different molecular weights from each other according to a molecular weight cut-off of a filtration membrane. Batch type or continuous type of ultrafiltration processes are carried out according to structures of the filtration membrane and a filtering device. In the present invention, the term "ultrafiltration" preferably means a continuous cross-flow type of ultrafiltration. According to the present invention, the impurities in the process liquid, which contains teicoplanin purified using the porous adsorption resin and activated carbon, mostly consist of macromolecules, such as lipid, protein, and polysaccharide, or the colored components combined with the macromolecules or included in the macromolecules. Hence, the impurities have a larger molecular weight than te¬ icoplanin. The reason why the impurities mostly consist of macromolecules is that metabolic products with low molecular weights and components resulting from the culture medium are mostly removed by the porous adsorption resin and activated carbon. The ultrafiltration process is not limited to a process of treating the process liquid purified using the porous adsorption resin and activated carbon. In other words, the ultrafiltration process may be carried out as the pre-treatment process before the process liquid is treated with the porous adsorption resin, and the process liquid purified through the ultrafiltration process may be then treated with the porous adsorption resin and activated carbon, thereby highly pure teicoplanin can be produced. In case that the roughly purified process liquid treated with the porous adsorption resin is subjected to the ultrafiltration process without being treated with the activated carbon, the purity of teicoplanin is 90 % (w/v) or more. [61] The ultrafiltration membrane useful in the ultrafiltration process of the present invention may be made of polyether sulfone or regenerated cellulose, and has a molecular weight cut-off of 3,000 to 100,000 Da. More preferably, the molecular weight cut-off of the ultrafiltration membrane is 5,000 to 50,000 Da. The ultrafiltration membrane is at least one selected from the group consisting of Biomax and Ultracel ul¬ trafiltration membrane of Pellicon module, PT and PL ultrafiltration membranes of Prostak module, PT, PL, and Helicon ultrafiltration membrane of Spiral Wound Ultra¬ filtration module, manufactured by Millipore Co., Sartocon®, and Ultrasart® ultra¬ filtration membrane, manufactured by Sartorius AG, OMEGATM, ALPHATM, REGENTM, SUPOR® ultrafiltration membranes, manufactured by Pall Co., FilmtecTM ultrafiltration membrane, manufactured by Dow Chemical Co., and KvickTM ultrafiltration membrane, manufactured by Amersham Pharmacia Biotech Inc.. [62] After water is added into the process liquid, treated with the porous adsorption resin, or treated with the activated carbon and porous adsorption resin, to reduce an alcohol content in the process liquid to 20 % (v/v) or less, the ultrafiltration process is carried out at 8 to 300C, more preferably 12 to 18°C, and at an input pressure (Pin) of 0 to 4 bar and a retentate pressure (Pret) of 0 to 3.5 bar. More preferably, the input pressure is 0 to 2.5 bar, and the retentate pressure is 0 to 2 bar. In case that the process liquid is concentrated until a volume of the retentate is 1/10 or less of the volume of the process liquid before it is subjected to the ultrafiltration process, a diafiltration process may be utilized, in which the purified water is continuously fed into retentate keeping up a constant volume. At this time, a volume of the purified water is 0.5 to 5 times larger than that of the process liquid before it is subjected to the ultrafiltration process, and more preferably, the volume of the purified water is 1 to 2 times larger than that of the process liquid before it is subjected to the ultrafiltration process. [63] The process liquid, from which polymer impurities and colored components are removed by the ultrafiltration membrane, and which contains teicoplanin, is con- centrated using a thin film evaporation system, a reverse osmosis system, or a vacuum distillation system. After acetone is added to the concentrate by a 3 to 10 times larger volume than a concentrate to precipitate teicoplanin for one hour or more, a precipitate is filtered and then dried to produce teicoplanin powder. [64] Having generally described this invention, a further understanding can be obtained by reference to examples and comparative examples which are provided herein for the purposes of illustration only and are not intended to be limiting unless otherwise specified. [65] [66] EXAMPLE 1 [67] [68] 160 £ of culture broth of Actinoplanes teichomyceticus DKB 53 was filtered using a drum filter to remove a mycelium therefrom, and 120 £ of filtrate was obtained. The filtrate was analyzed by an OPTIMAPAK® Cl 8 (4.6 X 250 mm, RStech Co.) HPLC column. Teicoplanin 1st International Standard (National Institute for Biological Standards and Control, Hertfordshire UK) was used as a reference standard for quan¬ tification. With respect to this, a content and a total amount of teicoplanin in the filtrate were 4.2 g/£ and 504 g, respectively. Additionally, the pH of the filtrate was 6.8. 4 £ of methanol was added to 20 £ of filtrate (teicoplanin 84 g), and the resulting mixture was applied onto a column (15 X 50 cm) packed with 4 £ of DOWEX OPTIPORE SD-2 at a flow rate of 2 BV (bed volume)/hr without controlling the pH of the resulting mixture. Subsequently, 4 BV (16 £) of 30 %(v/v) methanol was loaded at the flow rate of 4 BV/hr into the column to wash the resin packed in the column. Further, 8 BV (32 £) of 60 %(v/v) methanol, containing 0.15 M sodium chloride, was loaded into the column at the flow rate of 4 BV/hr to elute teicoplanin. It was confirmed by an analysis of an eluate using HPLC that a peak area of teicoplanin A2 was 84.8 % of a total peak area, and a roughly purified substance was produced at relatively high purity. Furthermore, an amount of teicoplanin was 72.2 g, which meant that recovery of te¬ icoplanin was 85.9 % (refer to Table 1). [69] [70] EXAMPLE 2 [71] [72] 2 £ of isopropanol was added to 20 £ of filtered culture broth (teicoplanin 84 g) according to example 1, and the resulting mixture was applied on a column (15 X 50 cm) packed with 4 £ of DOWEX OPTIPORE SD-2 at a flow rate of 2 BV/hr. Sub¬ sequently, 4 BV (16 £) of 15 %(v/v) isopropanol was loaded at the flow rate of 4 BV/hr into the column to wash the resin packed in the column. Further, 8 BV (32 £) of 40 %(v/v) isopropanol, containing 0.15 M sodium chloride, was loaded into the column at the flow rate of 4 BV/hr to elute teicoplanin. It was confirmed by an analysis of an eluate using HPLC that a peak area of teicoplanin A2 was 81.7 % of a total peak area. Furthermore, an amount of teicoplanin was 73.6 g, which meant that recovery of te¬ icoplanin was 87.6 % (refer to Table 1). [73] [74] EXAMPLE 3 [75] [76] 4 I of methanol was added to 20 I of filtered culture broth according to example 1, and the resulting mixture was applied on a column (15 X 50 cm) packed with 4 £ of Diaion HP 20 at a flow rate of 2 BV/hr. Subsequently, 4 BV (16 €) of 30 %(v/v) methanol solution was loaded at the flow rate of 4 BV/hr into the column to wash the resin packed in the column. Further, 8 BV (32 £) of 60 %(v/v) methanol solution, containing 0.15 M sodium chloride, was loaded into the column at the flow rate of 4 BV/hr to elute teicoplanin. It was confirmed by an analysis of an eluate using HPLC that a peak area of teicoplanin A2 was 83.4 % of a total peak area. Furthermore, an amount of teicoplanin was 70.7 g, which meant that recovery of teicoplanin was 84.2 % (refer to Table 1). [77] [78] COMPARATIVE EXAMPLE 1 [79] [80] After the pH of the filtered culture broth of example 1 was adjusted to 11 using IN NaOH, 20 I of filtrate was applied on a column (15 X 50 cm) packed with 4 I of Diaion HP 20 at a flow rate of 2 BV/hr according to a process as disclosed in Korean Pat. No. 321304. Subsequently, 30 %(v/v), 50 %(v/v), and 80 %(v/v) methanol were loaded at the flow rate of 2 BV/hr into the column. At this time, an amount of each methanol solution loaded into the column was 4 BV (16 €). Eluates passed from the column by 50 %(v/v) and 80 %(v/v) methanol containing teicoplanin were pooled with each other. With respect to this, it was confirmed by an analysis of the mixed eluate using HPLC that a peak area of teicoplanin A2 was 67.4 % of a total peak area. Furthermore, an amount of teicoplanin was 53.74 g, which meant that recovery of te¬ icoplanin was a relatively low 63.9 % (refer to Table 1). Teicoplanin contents in a portion of the solution passing through the column without being adsorbed into Diaion HP 20 when the filtrate with a pH of 11 was applied on the column, and in 30 % (v/v) methanol eluate were 11.8 % and 21.7 % of the teicoplanin content in the filtrated culture broth, respectively. Therefore, it can be seen that a yield of teicoplanin was reduced due to the basic pH of the filtered culture broth during an adsorption process using the porous adsorption resin and a washing process of the porous adsorption resin. [81] [82] COMPARATIVE EXAMPLE 2 [83] [84] 20 I of filtered culture broth according to example 1 was mixed with 4 I of methanol, and the resulting mixture was applied on a column (15 X 50 cm) packed with 4 € of Diaion HP 20 at a flow rate of 1.2 BV/hr. Subsequently, 4 BV (16 €) of distilled water was loaded at the flow rate of 2 BV/hr into the column, and 5 BV of 20 %(v/v) isopropanol was then loaded into the column to wash the resin packed in the column according to a process as disclosed in Korean Pat. Laid-Open Publication No. 2003-0034949. After the completion of the washing, 4.5 BV of 40 %(v/v) isopropanol was loaded into the column to elute teicoplanin from the column. It was confirmed by an analysis of an eluate using HPLC that a peak area of teicoplanin A2 was 63.3 % of a total peak area. Furthermore, an amount of teicoplanin was 71.2 g, which meant that the recovery of teicoplanin was 84.8 % (refer to Table 1). From the comparison of examples 1, 2, and 3 with comparative example 2, it can be seen that a roughly purified liquid containing a relatively high content of teicoplanin was yielded from the porous adsorption resin in the case of using the eluent containing a salt. [85] TABLE 1 [86] Recovery and purity of teicoplanin according to elution conditions when teicoplanin is eluted from the porous adsorption resin [87] Table 1

[88] [89] EXAMPLE 4 [90] [91] A portion of 32 £ of roughly purified liquid, containing teicoplanin, that is to say, 8 £ of roughly purified liquid (teicoplanin 18 g), according to example 1 was mixed with 8 £ of distilled water in a vessel with a volume of 20 £. The pH of the mixture was adjusted to 7.0 using 0.1 N NaOH. Subsequently, 18 g of Darco KB-B as an activated carbon was added to the mixture, and the resulting mixture was agitated using a mechanical agitator. At this time, an amount of the activated carbon was the same as that of teicoplanin in the roughly purified liquid. Additionally, the resulting mixture was agitated at 28°C for 2 hours, and then filtered by a KS 80 filter to remove the activated carbon from the resulting mixture. The filtered liquid was applied on a column (15 X 50 cm) packed with 4 £ of DOWEX OPTIPORE SD-2 at a flow rate of 2 BV/hr. Subsequently, 4 BV (16 £) of distilled water was loaded at the flow rate of 4 BV/hr into the column to wash the resin packed in the column. After the completion of the washing, 2 BV (8 £) of 70 %(v/v) methanol was loaded into the column to elute te¬ icoplanin from the column. It was confirmed by an analysis of an eluate using HPLC that the purity of teicoplanin was 94.7 %, and an amount of teicoplanin was 13.1 g. [92] 20 £ of distilled water was added to the eluate to dilute it so that a concentration of methanol was reduced to 20 %(v/v) or less. The diluted eluate was filtered by a Biomax 2 ultrafiltration membrane with a molecular weight cut-off of 50,000 Da and a filtering area of 0.1 m2 at Pin of 1 bar and Pret of 0.5 bar. When a volume of the retentate was 2 £ or less, the distilled water was fed continuously into the retentate with same flux rate of the ultrafiltration. Thereby, a volume of the retentate was maintained to 1.8 to 2 £ during the diafiltration process. A total volume of the filtrate, including the diafiltration step, was 42 £. The filtrate was concentrated by a reverse osmosis filtering membrane (Nanomax-50, Millipore Co.) at Pin of 1.5 bar and Pret of 0 bar, and the volume of a concentrate was 500 D. The concentration was continued while 2 £ of distilled water being fed to the concentrate keeping up the volume and recovered 420 D of concentrate. With respect to this, it was confirmed by an analysis of the concentrate using HPLC that the amount of teicoplanin in the concentrate was 11.8 g. As well, 3.36 £ of acetone was slowly added to the concentrate while the concentrate being agitated to precipitate teicoplanin for 12 hours, and the resulting concentrate was filtered by Whatman filter paper 4 to recover a precipitate. The precipitate was dried in a vacuum drier at 400C for 6 hours to recover 10.2 g of teicoplanin powder. [93] The teicoplanin powder was dissolved in the distilled water in such a way that a concentration of the teicoplanin in the distilled water was 50 mg/D, and a teicoplanin suspension was compared with Targocid® (Aventis) containing teicoplanin in the same concentration as the teicoplanin suspension to evaluate the removal of colored components. In detail, the teicoplanin suspension and Targocid® were dispensed in wells of a 96 well plate, and absorbencies of them were measured at a wavelength of 405 nm using a THERMOmax Microplate reader (Molecular Devices Corp.). In consequence, the teicoplanin powder of the present invention had a lower absorbance than Targocid®. Therefore, it can be seen that teicoplanin with excellent decolorization was produced according to the present invention (refer to Table 2). With reference to FIG. 1, there is illustrated the results regarding the analysis of teicoplanin, produced according to example 4, using an OPTIMAPAK® Cl 8 column. At this time, the purity of teicoplanin was 97.8 %(w/w). [94] [95] EXAMPLE 5 [96] [97] A portion of 32 I of roughly purified liquid, containing teicoplanin, that is to say, 8 £ of roughly purified liquid (teicoplanin 18.4 g), according to example 2 was mixed with 8 I of distilled water in a vessel with a volume of 20 I. The pH of the mixture was adjusted to 7.0 using 0.1 N NaOH. Subsequently, 18.4 g of NUCHAR SN-20 as an activated carbon was added to the mixture. At this time, an amount of the activated carbon was the same as that of teicoplanin in the roughly purified liquid. Additionally, the resulting mixture was agitated using a mechanical agitator at 28°C for 2 hours, and then filtered by a KS 80 filter to remove the activated carbon from the resulting mixture. The filtered liquid was applied on a column (15 X 50 cm) packed with 4 I of a DOWEX OPTIPORE SD-2 at a flow rate of 2 BV/hr. Subsequently, 4 BV (16 ζ) of distilled water was loaded at the flow rate of 4 BV/hr into the column to wash the resin packed in the column. After the completion of the washing, 2 BV (8 €) of 40 %(v/v) isopropanol was loaded into the column to elute teicoplanin from the column. It was confirmed by an analysis of an eluate using HPLC that the purity of teicoplanin was 93.6 %, and an amount of teicoplanin was 13.4 g. [98] 24 1 of distilled water was added to the eluate to dilute it so that a concentration of isopropanol was reduced to 10 %(v/v) or less. The diluted eluate was filtered by a Sartocon ultrafiltration membrane with a molecular weight cut-off of 30,000 Da and a filtering area of 0.1 m2 at Pin of 1 bar and Pret of 0.5 bar. When a volume of the retentate was 2 I or less, the distilled water was fed continuously into the retentate with same flux rate of the ultrafiltration. Thereby, a volume of the retentate was maintained to 1.8 to 2 I during the diafiltration. A total volume of the permeate, including the distilled water used in the diafiltration, was 48 £. The filtrate was concentrated by a reverse osmosis filtering membrane (Nanomax-50, Millipore Co.) at Pin of 1.5 bar and Pret of 0 bar, and the volume of a concentrate was 480 D. The concentration was continued while 2 £ of distilled water being fed to the concentrate keeping up the volume and recovered 460 D of concentrate. With respect to this, it was confirmed by an analysis of the concentrate using HPLC that the amount of teicoplanin in the concentrate was 11.9 g. As well, 3.68 £ of acetone was slowly added to the concentrate while the concentrate being agitated to precipitate teicoplanin for 12 hours, and the resulting concentrate was filtered by Whatman filter paper 4 to recover a precipitate. The precipitate was dried in a vacuum drier at 400C for 6 hours to recover teicoplanin powder. The teicoplanin powder was analyzed using HPLC, and the purity and amount of the teicoplanin powder were 97.1 %(v/v) and 10.7 g, respectively. Like in the case of example 4, the teicoplanin powder was dissolved in the distilled water in such a way that a concentration the teicoplanin in the distilled water was 50 mg/D, and the absorbance of a teicoplanin suspension was measured at a wavelength of 405 nm (refer to Table 2). [99] TABLE 2 [100] Absorbance of the teicoplanin suspension [101] Table 2

[102] [103] EXAMPLE 6 [104] [105] 20 £ of filtered culture broth according to example 1 was subjected to an ultra¬ filtration process before it was adsorbed into a porous adsorption resin. In detail, 20 £ of filtered culture broth according to example 1 was subjected to a ultrafiltration by a Biomax 2 ultrafiltration membrane equipped in ETU-II MF/UF system (Millipore Co.), having a molecular weight cut-off of 50,000 Da and a filtering area of 0.5 m2, at Pin of 2.0 bar and Pret of 1.0 bar without controlling the pH of the culture broth. At this time, when a volume of the retentate was 2 £ or less, the distilled water was fed into the retentate with the same flux rate of the ultrafiltration. A total volume of the permeate, i ncluding the diafiltration, was 50 £. The permeate was analyzed by HPLC with the use of an OPTIMAPAK® C18 column (4.6 X 250 mm, RStech Co.). With respect to this, a content and a total amount of teicoplanin in the permeate were 1.58 g/£ and 79 g, re¬ spectively. Hence, recovery yield of teicoplanin was 94 %. The permeate was applied on a column (15 X 50 cm) packed with 4 £ of DOWEX OPTIPORE SD-2 at a flow rate of 2 BV (bed volume)/hr. Subsequently, 4 BV (16 £) of 30 %(v/v) methanol was loaded at the flow rate of 4 BV/hr into the column to wash the resin packed in the column. Further, 8 BV (32 £) of 60 %(v/v) methanol, containing 0.15 M sodium chloride, was loaded into the column at the flow rate of 4 BV/hr to elute teicoplanin. It was confirmed by an analysis of an eluate using HPLC that a peak area of teicoplanin A2 was 87.4 % of a total peak area. As well, an amount of teicoplanin was 70 g, which meant that recovery of teicoplanin was 88.6 %. [106] 17.5 g of Darco KB-B as an activated carbon was added into a portion of 32 £ of eluate passing through the porous adsorption resin, that is to say, 8 £ of eluate (containing 17.5 g of teicoplanin), and the resulting mixture was agitated using a mechanical agitator at 28°C for 2 hours. The agitated mixture was filtered by a KS 80 filter to remove the activated carbon from the mixture. The filtered liquid was applied on a column (5 X 30 cm) packed with 0.4 £ of DOWEX OPTIPORE SD-2 at a flow rate of 4 BV/hr. Subsequently, 4 BV (1.6 ^) of distilled water was loaded at the flow rate of 4 BV/hr into the column to wash the resin packed in the column. After the completion of the washing, 2 BV (800 D) of 70 %(v/v) methanol was loaded into the column to elute teicoplanin from the column. 70 %(v/v) methanol, which was eluted from the resin and contained teicoplanin, was concentrated by vacuum distillation until its volume was 200 D. 1.6 £ of acetone was slowly added to the concentrate while it being agitated to precipitate teicoplanin for 8 hours, and the resulting mixture was filtered by Whatman filter paper 4 to recover a precipitate. The precipitate was dried in a vacuum drier at 400C for 6 hours to recover 10.9 g of teicoplanin powder. The te¬ icoplanin powder was then suspended in distilled water such that a concentration of the teicoplanin was 1 mg/D. It was confirmed by an analysis using HPLC that the purity of teicoplanin was 95.8 %(w/w). [107] [108] EXAMPLE 7 [109] [110] A portion of 32 I of roughly purified liquid, containing teicoplanin and passing through a porous adsorption resin, that is to say, 8 £ of roughly purified liquid (teicoplanin 18 g), according to example 1 was mixed with 16 £ of distilled water. A mixture was subjected to a ultrafiltration with a Biomax 2 ultrafiltration membrane equipped in ETU-II MF/UF system (Millipore Co.), having a molecular weight cut-off of 50,000 Da and a filtering area of 0.5 m2, at Pin of 2.0 bar and Pret of 1.0 bar. At this time, when a volume of the retentate was 2 £ or less, the distilled water was fed into the retentate with the same flux rate of the ultrafiltration. A total volume of the permeate, including the diafiltration, was 36 £. The permeate was concentrated by a reverse osmosis membrane (Nanomax-50, Millipore Co.) at Pin of 1.5 bar and Pret of 0 bar, and the volume of a concentrate was 500 D. Subsequently, the concentration process was continued while 4 £ of distilled water being fed to the concentrate with the same flux rate of the reverse osmosis and recovered 380 D of concentrate. 3 I of acetone was slowly added to the concentrate while the concentrate being agitated to precipitate te- icoplanin for 12 hours, and the resulting mixture was filtered by Whatman filter paper 4 to recover a precipitate. The precipitate was dried in a vacuum drier at 400C for 6 hours to recover 12.9 g of teicoplanin powder. The teicoplanin powder was then dissolved in distilled water such that a concentration of teicoplanin was 1 mg/D. It was confirmed by an analysis using HPLC that the purity of teicoplanin was 90.2 %(w/w).