Method for producing lysine

Abstract

The present application relates to a method for producing lysine, the method comprising the steps of: culturing microorganisms to prepare a fermentation broth containing lysine; and removing carbon dioxide from the fermentation broth containing lysine by using a carbon dioxide degassing tower.

Description

Method for producing lysine

[0001] This application relates to a method for producing lysine.

[0002] Cross-citation with related application(s)

[0003] This application claims the benefit of priority from Republic of Korea Patent Application No. 10-2024-0116275, dated August 28, 2024, the entire contents of which are incorporated herein by reference.

[0004]

[0005] L-lysine is an amino acid primarily used in animal feed. Numerous methods for producing L-lysine from fermented broths containing L-lysine have been described. However, these methods are either low in L-lysine content or utilize an ion exchange process, which increases costs due to the use of chemicals in the process and generates large amounts of wastewater, making them uneconomical and environmentally unfriendly. Therefore, the development of a more economical and environmentally friendly method for producing L-lysine is urgently needed.

[0006]

[0007] (Patent Document 1) United States Patent Publication No. 2003-0152633 A1

[0008]

[0009] The purpose of this application is to provide a method for producing lysine.

[0010] Another object of the present application is to provide a method for removing carbon dioxide from a lysine fermentation broth.

[0011]

[0012] The way things work is,

[0013] (a) a step of culturing microorganisms to prepare a fermentation solution containing lysine; and

[0014] (b) A method for producing lysine is provided, comprising a step of removing carbon dioxide from a fermentation solution containing lysine using a carbon dioxide degassing tower.

[0015]

[0016] This is specifically explained as follows. Meanwhile, each description and embodiment disclosed in this application can also be applied to each other description and embodiment. That is, all combinations of the various elements disclosed in this application fall within the scope of this application. Furthermore, the scope of this application is not limited by the specific descriptions described below. Furthermore, those skilled in the art will recognize or ascertain numerous equivalents to the specific embodiments of this application described in this application using only routine experimentation. Furthermore, such equivalents are intended to be encompassed by this application.

[0017]

[0018] Glossary of terms

[0019] In this application, the term "fermented product" may refer to the result of enzymatic or metabolic decomposition of an organic substance using a microorganism. For example, the fermented product may include the culture itself obtained by culturing a microorganism in a culture medium, a culture from which the cells (the microorganism or a part of the microorganism) have been removed, or a concentrate, dried product, or lyophilized product of the culture from which the cells have been removed. Furthermore, in this case, the term "fermented liquid" may include the entire fermented product containing lysine produced from the microorganism, or a fermented product from which impurities have been removed.

[0020] In this application, the term "process liquid" may collectively refer to the liquid introduced into each process for manufacturing lysine and / or the liquid obtained after each process is performed. In one example, the process liquid may refer to a fermentation liquid, concentrate, filtrate, etc. containing lysine.

[0021] In the present application, the term “mother liquid” may mean a liquid remaining after performing a separation process and / or a concentration crystallization process, etc., on a process liquid containing lysine to separate lysine.

[0022] The above lysine may be lysine granules, lysine liquid, lysine crystals or lysine powder.

[0023] The above lysine may be L-lysine.

[0024]

[0025] (a) Step: A step of culturing microorganisms to prepare a fermentation solution containing lysine.

[0026] The fermented solution containing the above lysine can be obtained by culturing a microorganism that produces lysine. The lysine-producing microorganism includes both wild-type microorganisms and microorganisms that have undergone natural or artificial genetic modification. It may be a microorganism in which a specific mechanism has been weakened or strengthened due to reasons such as the insertion of an external gene or the enhanced or inactivated activity of an endogenous gene, and may be a microorganism that contains a genetic modification of the target protein for lysine production.

[0027] The lysine-producing microorganism of the present application may be, but is not limited to, a microorganism that naturally has lysine production ability, or a microorganism that has been granted lysine production ability to a microorganism that does not have lysine production ability. Specifically, the lysine-producing microorganism of the present application, or the microorganism having lysine production ability, may be a microorganism in which some of the genes in the lysine biosynthesis pathway are strengthened or weakened, or some of the genes in the lysine degradation pathway are strengthened or weakened. The phrase “strengthening” or “increasing” the lysine production ability of the microorganism of the present application means that the lysine production ability of the microorganism of the present application is improved compared to other microorganisms other than the microorganism of the present application, a parent strain, or an unmodified microorganism. For example, the microorganism of the present application may have an improved lysine productivity of about 1% or more, 2% or more, 5% or more, 10% or more, 100% or more, 200% or more, 500% or more, 1000% or more, 1100% or more, 1200% or more, or 1300% or more compared to the lysine productivity of other microorganisms, but is not limited thereto. The term “about” includes all of ±0.5, ±0.4, ±0.3, ±0.2, ±0.1, etc., and includes all of the values ​​in the range equivalent to or similar to the value following the term “about,” but is not limited thereto.

[0028] In one example, the microorganism producing the lysine may be Corynebacterium sp.

[0029] The above-mentioned Corynebacterium genus microorganisms are Corynebacterium glutamicum, Corynebacterium erythrogenes, Corynebacterium crudilactis, Corynebacterium deserti, Corynebacterium efficiens, Corynebacterium callunae, Corynebacterium stationis, Corynebacterium singulare, Corynebacterium halotolerans, Corynebacterium striatum, and Corynebacterium ammoniagenes. It may be at least one selected from the group consisting of, but is not limited to, Corynebacterium ammoniagenes, Corynebacterium pollutisoli, Corynebacterium imitans, Corynebacterium testudinoris, Corynebacterium crenatum, and Corynebacterium flavescens.

[0030] In one example, the microorganism of the genus Corynebacterium may be Corynebacterium glutamicum.

[0031] Cultivation of the above lysine-producing microorganism can be performed using suitable media and culture conditions known in the art. These cultivation processes can be easily adjusted and used by those skilled in the art depending on the selected strain.

[0032] In this application, "cultivation" may refer to growing a lysine-producing microorganism under appropriately controlled environmental conditions. The cultivation process of this application may be performed using appropriate media and culture conditions known in the art. Such a cultivation process can be easily adjusted and used by those skilled in the art depending on the selected strain. Specifically, the cultivation may be batch, continuous, and / or fed-batch, but is not limited thereto.

[0033] In this application, the term "medium" refers to a material containing nutrients as main components necessary for culturing the microorganism, and can supply nutrients and growth factors, including water, which is essential for survival and growth. Specifically, the medium and other culture conditions used for culturing the microorganism of this application may be any medium used for culturing general microorganisms without particular limitation, but the microorganism of this application may be cultured under aerobic conditions in a general medium containing an appropriate carbon source, nitrogen source, phosphorus source, inorganic compound, amino acid, and / or vitamin, while controlling the concentration of lysine, temperature, pH, etc. In one example, a culture medium for a Corynebacterium spp. strain can be found in the literature ["Manual of Methods for General Bacteriology" by the American Society for Bacteriology (Washington DC, USA, 1981)].

[0034] The carbon source may include carbohydrates such as glucose, saccharose, lactose, fructose, sucrose, maltose, etc.; sugar alcohols such as mannitol, sorbitol, etc.; organic acids such as pyruvic acid, lactic acid, citric acid, etc.; amino acids such as glutamic acid, methionine, lysine, etc. In addition, natural organic nutrients such as starch hydrolysate, molasses, blackstrap molasses, rice bran, cassava, sugarcane bagasse, and corn steep liquor may be used, and specifically, carbohydrates such as glucose and sterilized pretreated molasses (i.e., molasses converted to reducing sugar) may be used, and other appropriate amounts of carbon sources may be used in various ways without limitation. These carbon sources may be used alone or in combination of two or more, but are not limited thereto.

[0035] The nitrogen source may include inorganic nitrogen sources such as ammonia, ammonium sulfate, ammonium chloride, ammonium acetate, ammonium phosphate, ammonium carbonate, ammonium nitrate, etc.; organic nitrogen sources such as amino acids such as glutamic acid, methionine, glutamine, etc.; peptone, NZ-amine, meat extract, yeast extract, malt extract, corn steep liquor, casein hydrolysate, fish or its decomposition product, defatted soybean cake or its decomposition product, etc. These nitrogen sources may be used alone or in combination of two or more, but are not limited thereto.

[0036] The above-mentioned components may include potassium phosphate monobasic, potassium phosphate dibasic, or their corresponding sodium-containing salts. Inorganic compounds may include sodium chloride, calcium chloride, iron chloride, magnesium sulfate, iron sulfate, manganese sulfate, calcium carbonate, etc. In addition, amino acids, vitamins, and / or suitable precursors may be included. These components or precursors may be added to the medium in batch or continuous manner, but are not limited thereto.

[0037] During the cultivation of microorganisms, compounds such as ammonium hydroxide, potassium hydroxide, ammonia, phosphoric acid, sulfuric acid, etc. can be added to the medium in an appropriate manner to adjust the pH of the medium. In addition, during the cultivation, an antifoaming agent such as fatty acid polyglycol ester can be used to suppress bubble formation. In addition, in order to maintain the aerobic state of the medium, oxygen or an oxygen-containing gas can be injected into the medium, or in order to maintain anaerobic and microaerobic states, no gas can be injected or nitrogen, hydrogen, or carbon dioxide gas can be injected, but is not limited thereto. In the cultivation of the present application, the culture temperature can be maintained at 20 to 45°C, specifically 25 to 40°C, and can be cultured for about 10 to 160 hours, but is not limited thereto. The lysine produced by the cultivation of the present application can be secreted into the medium or remain within the cells.

[0038] The fermentation solution containing the above lysine may be a fermentation product obtained by culturing a lysine-producing microorganism in a medium, or may be a fermentation product from which cells (e.g., a lysine-producing microorganism, or a part of the microorganism, etc.) have been removed. Removing cells from the fermentation solution may be accomplished by a conventional method such as separation (e.g., centrifugation, etc.) or filtration (e.g., use of a cell separation facility, a ceramic membrane filter, etc.).

[0039] The fermentation solution containing lysine obtained by culturing the above lysine-producing microorganism may have a lysine concentration of 1 g / l or more, 2 g / l or more, 3 g / l or more, 4 g / l or more, 5 g / l or more, 6 g / l or more, 7 g / l or more, 8 g / l or more, 9 g / l or more, 10 g / l or more, 20 g / l or more, 30 g / l or more, 40 g / l or more, 50 g / l or more, 60 g / l or more, 70 g / l or more, 80 g / l or more, 90 g / l or more, 100 g / l or more (the upper limit is not particularly limited, and may be, for example, about 100 g / l or less, 200 g / l or less, 500 g / l or less, or 1000 g / l or less.) (unit: weight of lysine / volume of fermentation solution) or more.

[0040] The method for producing lysine of the present application may additionally include a step of preparing a microorganism producing lysine, a step of preparing a medium for culturing the microorganism, or a combination thereof (in any order), for example, before the culturing step.

[0041]

[0042] (b) Step: Step of removing carbon dioxide from a fermentation solution containing lysine using a carbon dioxide degassing tower.

[0043] The above step (b) may be a step of removing carbon dioxide from the fermentation liquid containing the lysine using a carbon dioxide degassing tower.

[0044] The above carbon dioxide degassing tower is,

[0045] (1) An input portion into which a fermentation solution containing the above lysine is input;

[0046] (2) A heat source that generates a heat transfer medium;

[0047] (3) a body part that comes into contact with the fermentation liquid and the heat transfer medium or through which the heat energy of the heat transfer medium is transferred to the fermentation liquid; and

[0048] (4) It may include a discharge unit through which the above fermented liquid is discharged.

[0049] The fermentation liquid containing the above lysine can be introduced into a carbon dioxide degassing tower through the inlet of the carbon dioxide degassing tower and discharged through the outlet.

[0050] As the retention time of the fermentation liquid containing the above lysine within the carbon dioxide degassing column increases, the carbon dioxide within the fermentation liquid can be efficiently removed. In one example, the retention time may refer to the difference between the time the fermentation liquid is introduced into the inlet and the time the fermentation liquid is discharged from the outlet.

[0051] In one example, the fermentation solution containing the lysine is kept in a carbon dioxide degassing tower for 30 minutes or more, 1 hour or more, 2 hours or more, 3 hours or more, 4 hours or more, 5 hours or more, 6 hours or more, 7 hours or more, 8 hours or more, 9 hours or more, 10 hours or more, 11 hours or more, 12 hours or more, 14 hours or more, 16 hours or more, 18 hours or more, 20 hours or more, 22 hours or more, 24 hours or more, 0.5 to 48 hours, 0.5 to 42 hours, 0.5 to 36 hours, 0.5 to 30 hours, 0.5 to 24 hours, 0.5 to 18 hours, 0.5 to 12 hours, 0.5 to 10 hours, 0.5 to 8 hours, 0.5 to 6 hours, 0.5 to 5 hours, 0.5 to 4 hours, 0.5 to 3 hours, 0.5 to 2 hours, 1 to 48 hours, 1 to 42 hours, 1 to 36 hours, 1 to 30 hours, 1 to 24 hours, 1 to 18 hours, 1 to 12 hours, 1 to 10 hours, 1 to 8 hours, 1 to 6 hours, 1 to 5 hours, 1 to 4 hours, 1 to 3 hours, 1 to 2 hours, 2 to 48 hours, 2 to 42 hours, 2 to 36 hours, 2 to 30 hours, 2 to 24 hours, 2 to 18 hours, 2 to 12 hours, 2 to 10 hours, 2 to 8 hours, 2 to 6 hours, 2 to 5 hours, 2 to 4 hours, 2 to 3 hours, 3 to 48 hours, 3 to 42 hours, 3 to 36 hours, 3 to 30 hours, 3 to 24 hours, 3 to 18 hours, 3 to 12 hours, 3 to 10 hours, 3 to 8 hours, 3 to 6 hours, 3 to 5 hours, 3 to 4 hours, 4 to 48 hours, 4 to 42 hours, 4 to 36 hours, 4 to 30 hours, 4 to 24 hours, 4 to 18 hours, 4 to 12 hours, 4 to 10 hours, 4 to 8 hours, 4 to 6 hours, 4 to 5 hours, 5 to 48 hours, 5 to 42 hours, 5 to 36 hours, 5 to 30 hours, 5 to 24 hours, 5 to 18 hours, 5 to 12 hours, 5 to 10 hours, 5 to 8 hours, 5 to 6 hours, 6 to 48 hours, 6 to 42 hours, 6 The stay may be, but is not limited to, 36 hours, 6 to 30 hours, 6 to 24 hours, 6 to 18 hours, 6 to 12 hours, 6 to 10 hours, or 6 to 8 hours.

[0052] Since the fermentation liquid containing the above lysine can efficiently remove carbon dioxide from the fermentation liquid as the residence time in the carbon dioxide degassing tower increases, the flow rate of the fermentation liquid introduced into the inlet can be appropriately set so as to increase the residence time.

[0053] In one example, the fermentation liquid containing the lysine is fed into the input unit at 1 to 150 ml / min, 1 to 125 ml / min, 1 to 100 ml / min, 1 to 90 ml / min, 1 to 80 ml / min, 1 to 70 ml / min, 1 to 60 ml / min, 1 to 50 ml / min, 5 to 150 ml / min, 5 to 125 ml / min, 5 to 100 ml / min, 5 to 90 ml / min, 5 to 80 ml / min, 5 to 70 ml / min, 5 to 60 ml / min, 5 to 50 ml / min, 10 to 150 ml / min, 10 to 125 ml / min, 10 to 100 ml / min, 10 to 90 ml / min, 10 to 80 ml / min, 10 to 70 ml / min, 10 to 60 ml / min, 10 to 50 ml / min, 15 to 150 ml / min, 15 to 125 ml / min, 15 to 100 ml / min, 15 to 90 ml / min, 15 to 80 ml / min, 15 to 70 ml / min, 15 to 60 ml / min, 15 to 50 ml / min, 20 to 150 ml / min, 20 to 125 ml / min, 20 to 100 ml / min, 20 to 90 ml / min, 20 to 80 ml / min, 20 to 70 ml / min, 20 to 60 ml / min, 20 to 50 ml / min, 30 to 150 ml / min, 30 to 125 ml / min, 30 to 100 ml / min, 30 to 90 ml / min, 30 to 80 ml / min, 30 to 70 ml / min, 30 to 60 ml / min, 30 to 50 ml / min, 40 to 150 ml / min, 40 to 125 ml / min, 40 to 100 ml / min, 40 to 90 ml / min, 40 to 80 ml / min, 40 to 70 ml / min, 40 to 60 ml / min, 40 to 50 ml / min,It can be injected at a flow rate of 50 to 150 ml / min, 50 to 125 ml / min, 50 to 100 ml / min, 50 to 90 ml / min, 50 to 80 ml / min, 50 to 70 ml / min, or 50 to 60 ml / min, but is not limited thereto.

[0054] The fermentation liquid introduced into the above-mentioned input section can come into contact with a heat transfer medium generated from a heat source in the body section. As the fermentation liquid comes into contact with the heat transfer medium, the heat energy of the heat transfer medium can be transferred to the fermentation liquid.

[0055] The above body portion may include one or more stages with which the fermentation liquid can come into contact. The stages are not limited to a specific form as long as the fermentation liquid containing lysine can efficiently come into contact with a heat transfer medium generated from a heat source, and may include 1 or more, 2 or more, 3 or more, 4 or more, 5 or more, 6 or more, 7 or more, 8 or more, 9 or more, 10 or more, 11 or more, 12 or more, 13 or more, 14 or more, 15 or more, 16 or more, 17 or more, 18 or more, 19 or more, 20 or more, 21 or more, 22 or more, 23 or more, 24 or more, 25 or more, 26 or more, 27 or more, 28 or more, 29 or more, 30 or more (the upper limit is not particularly limited and may be, for example, about 100 or less). In one embodiment, the body portion may comprise 15 to 25, or 20, sections.

[0056] The above-mentioned unit may refer to a structure that promotes contact between a fermentation liquid containing the lysine and a heat transfer medium, thereby enabling efficient transfer of heat energy.

[0057] In one example, the unit may be of tray type or packing type.

[0058] The above tray-type stage may refer to a structure in which one or more trays are horizontally arranged and stacked in layers within a carbon dioxide degassing tower, and in one example, a heat transfer medium may rise from the bottom to the top and contact the fermentation liquid on the tray to transfer heat energy to the fermentation liquid. The fermentation liquid may flow down from the top and be recovered through a discharge port.

[0059] The above tray-type stage may include an internal receiving portion where the fermentation liquid and the heat transfer medium can come into contact, a dam formed on one side or the outer surface of the internal receiving portion to receive the fermentation liquid, and a downcomer that moves the fermentation liquid to the next stage when the fermentation liquid is filled above the dam, and specifically, may be a bubble-cap tray, a sieve tray, a valve tray, a disk and doughnut tray, etc., but is not limited thereto.

[0060] The above bubble cap tray may have small caps installed on the tray, and holes may be formed under the caps. While the fermentation liquid flows over the top of the tray, the heat transfer medium may be structured to rise through the holes in the caps and come into contact with the fermentation liquid.

[0061] The above-mentioned body-shaped tray may have a structure in which one or more or more holes (sieves) are formed on the surface of the tray, so that a heat transfer medium passes through the holes and comes into contact with the fermentation liquid.

[0062] The above valve tray may be structured such that one or more bands (or valves) are installed on the tray so that the heat transfer medium passes through the bands and comes into contact with the fermentation liquid. The bands may open and close depending on the flow rate of the heat transfer medium.

[0063] The above-mentioned curved tray may have a structure in which two units, one in the shape of a disk and one in the shape of a doughnut, are arranged in an alternating manner. The heat transfer medium flows between the doughnuts, and the fermentation liquid containing the lysine flows over the disks and contacts them to transfer heat energy to the fermentation liquid.

[0064] The above-mentioned packing type may refer to a structure in which packing is filled inside a carbon dioxide degassing tower, and may be classified into structured packing or random packing. The fermentation liquid containing the lysine may pass between the packing and contact the heat transfer medium to receive heat energy. The packing mainly used in the structured packing may be, but is not limited to, a corrugated metal sheet, a graphic sheet, a plastic net, a ceramic honeycomb, etc. The packing mainly used in the oval packing may be, but is not limited to, a Raschig ring, a Pall ring, a Becktil saddle, an interlocking saddle, etc.

[0065] The terms “above,” “below,” “leading,” “rear,” “upper,” “lower,” “front,” “rear,” “top,” and “bottom” used in the above description are intended to exemplify various types of stages, and the shape and location of the stages are not limited by the above terms.

[0066]

[0067] The above heat source can generate a heat transfer medium capable of transferring heat energy to the fermentation liquid. The heat transfer medium can be a gas heated by the heat source.

[0068] In one example, the heat transfer medium may include water vapor, carbon dioxide, and / or ammonia.

[0069] The above heat transfer medium may have an appropriate temperature to transfer heat energy to the fermentation liquid to degas carbon dioxide in the fermentation liquid.

[0070] In one example, the temperature of the heat transfer medium is 75 to 150°C, 75 to 145°C, 75 to 140°C, 75 to 135°C, 75 to 130°C, 75 to 125°C, 75 to 120°C, 75 to 115°C, 75 to 110°C, 75 to 105°C, 75 to 100°C, 75 to 95°C, 75 to 90°C, 80 to 150°C, 80 to 145°C, 80 to 140°C, 80 to 135°C, 80 to 130°C, 80 to 125°C, 80 to 120°C, 80 to 115°C, 80 to 110 ℃, 80 to 105 ℃, 80 to 100 ℃, 80 to 95 ℃, 80 to 90 ℃, 85 to 150 ℃, 85 to 145 ℃, 85 to 140 ℃, 85 to 135 ℃, 85 to 130 ℃, 85 to 125 ℃, 85 to 120 ℃, 85 to 115 ℃, 85 to 110 ℃, 85 to 105 ℃, 85 to 100 ℃, 85 to 95 ℃, 85 to 90 ℃, 90 to 150 ℃, 90 to 145 ℃, 90 to 140 ℃, 90 to 135 ℃, 90 to 130 ℃, It may be, but is not limited to, 90 to 125 ℃, 90 to 120 ℃, 90 to 115 ℃, 90 to 110 ℃, 90 to 105 ℃, 90 to 100 ℃, 90 to 95 ℃, 95 to 150 ℃, 95 to 145 ℃, 95 to 140 ℃, 95 to 135 ℃, 95 to 130 ℃, 95 to 125 ℃, 95 to 120 ℃, 95 to 115 ℃, 95 to 110 ℃, 95 to 105 ℃, or 95 to 100 ℃.

[0071] Since the fermentation liquid containing lysine in the above carbon dioxide degassing tower comes into contact with the heat transfer medium generated from the heat source as it rises in the body, when this is used, the fermentation liquid with a large surface area can come into contact with the high-temperature heat transfer medium, so carbon dioxide can be efficiently removed from the fermentation liquid.

[0072] In one example, the step of removing the carbon dioxide may be performed by contacting a fermentation liquid containing lysine with an increased surface area introduced into the upper portion of a carbon dioxide degassing tower with a heat transfer medium generated by heating at the lower portion of the carbon dioxide degassing tower.

[0073] The above carbon dioxide degassing tower may further include a recovery unit for recovering carbon dioxide degassed while the fermentation liquid containing lysine is heated by a heat transfer medium. The recovered carbon dioxide may then be reused for a carbon dioxide absorption process that injects carbon dioxide into the fermentation liquid containing lysine.

[0074] The above step (b) may be a step of removing carbon dioxide from a fermentation liquid containing lysine by 85% or more, 86% or more, 87% or more, 88% or more, 89% or more, 90% or more, 91% or more, 92% or more, 93% or more, 94% or more, 95% or more, 96% or more, 97% or more, 98% or more, or 99% or more.

[0075] In one example, the removal rate of the carbon dioxide can be calculated as "amount of carbon dioxide removed / amount of carbon dioxide in the fermentation broth containing lysine." The amount of carbon dioxide can be by weight or mole, and the removal rate can be by weight ratio or mole ratio.

[0076] The pH of the fermentation solution (or L-lysine process solution) from which carbon dioxide has been removed in the above step (b) is 8.5 to 11, 8.5 to 10.8, 8.5 to 10.75, 8.5 to 10.5, 8.5 to 10.25, 8.5 to 10, 8.5 to 9.75, 8.5 to 9.5, 8.75 to 11, 8.75 to 10.8, 8.75 to 10.75, 8.75 to 10.5, 8.75 to 10.25, 8.75 to 10, 8.75 to 9.75, 8.75 to 9.5, 9 to 11, 9 to 10.8, 9 to 10.75, 9 to 10.5, 9 to It may be, but is not limited to, 10.25, 9 to 10, 9 to 9.75, 9 to 9.5, 9.25 to 11, 9.25 to 10.8, 9.25 to 10.75, 9.25 to 10.5, 9.25 to 10.25, 9.25 to 10, 9.25 to 9.75, 9.25 to 9.5, 9.5 to 11, 9.5 to 10.8, 9.5 to 10.75, 9.5 to 10.5, 9.5 to 10.25, 9.5 to 10, or 9.5 to 9.75.

[0077] By removing carbon dioxide from the fermentation liquid containing the above lysine using the above carbon dioxide degassing tower, a high carbon dioxide removal rate can be achieved in a short period of time while obtaining a lysine product containing a high lysine content.

[0078] In the case of removing carbon dioxide from a fermentation liquid containing lysine using the above carbon dioxide degassing tower, compared to the case of removing carbon dioxide from a fermentation liquid containing lysine by performing a method of concentrating the fermentation liquid and / or a method of directly heating the fermentation liquid, the time required to remove carbon dioxide from the same amount of fermentation liquid can be reduced by 10% or more, 15% or more, 20% or more, 25% or more, 30% or more, 35% or more, 40% or more, 45% or more, 50% or more, 55% or more, 60% or more, 65% or more, 70% or more, 75% or more, 80% or more, or 85% or more, thereby removing carbon dioxide more efficiently.

[0079]

[0080] Below, a carbon dioxide degassing tower according to one embodiment is described in detail with reference to FIG. 1.

[0081] The configurations depicted in the drawings of this specification are merely preferred examples of the disclosed invention, and there may be various modified examples that can replace the embodiments and drawings of this specification at the time of filing of this application.

[0082] Additionally, the same reference numbers or symbols presented in each drawing of this specification represent parts or components that perform substantially the same function.

[0083] In addition, the terminology used in this specification is used to describe embodiments and is not intended to limit and / or restrict the disclosed invention. The singular expression includes the plural expression unless the context clearly indicates otherwise. In this specification, the terms “comprise” or “have” and the like are intended to specify the presence of a feature, number, step, operation, component, part or combination thereof described in the specification, but do not exclude in advance the possibility of the presence or addition of one or more other features, numbers, steps, operations, components, parts or combinations thereof.

[0084] Meanwhile, the terms “leading end,” “rear end,” “upper end,” “lower end,” “front end,” “rear end,” “top end,” and “bottom end” used in the description below are defined based on the drawings, and the shape and position of each component are not limited by these terms.

[0085] In this specification, the expression 'identical' means not only a complete match, but also a difference to a degree that takes into account the range of processing error.

[0086] Figure 1 is a drawing showing a carbon dioxide degassing tower according to one embodiment.

[0087] Referring to FIG. 1, the carbon dioxide degassing tower may include an inlet (10) into which a fermentation liquid containing lysine is introduced; a heat source (20) that generates a heat transfer medium (21); a body (30) that contacts the fermentation liquid and the heat transfer medium or through which the heat energy of the heat transfer medium is transferred to the fermentation liquid; and a discharge portion (40) through which the fermentation liquid is discharged.

[0088] The above-mentioned input section (10) is a section where a fermentation liquid containing lysine is input into the body section (30), and may be directly or indirectly connected to the body section. The body section (30) may be connected to one or more, two or more, three or more, four or more, or five or more input sections (10).

[0089] The above input portion (10) can be connected to the top, middle and / or bottom of the body portion (30). In one example, the input portion (10) can be connected to the top of the body portion (30).

[0090] The fermentation liquid (11) containing lysine, which is introduced into the body part (30) through the above-mentioned introduction part (10), comes into contact with the body part and receives heat energy from a heat transfer medium, so that carbon dioxide in the fermentation liquid can be degassed.

[0091] The above heat source (20) may generate a heat transfer medium (21) having thermal energy. The heat source (20) may be supplied with thermal energy through steam (201), but is not limited thereto. In one example, the steam (201) supplied to the heat source (20) may be recovered in the form of condensate (202).

[0092] The above body portion (30) may be directly or indirectly connected to a heat source (20). The above body portion (30) may be connected to one or more, two or more, three or more, four or more, or five or more heat sources (20).

[0093] The heat source (20) may be connected to the top, middle and / or bottom of the body portion (30). In one example, the heat source (20) may be connected to the bottom of the body portion (30).

[0094] The above body portion (30) may include one or more stages (31) with which the fermentation liquid containing the lysine can come into contact. As described above, the stage (31) is not limited to a specific form as long as the fermentation liquid containing the lysine can efficiently come into contact with the heat transfer medium (21) generated from the heat source (20).

[0095] When the fermentation liquid containing the above lysine receives heat energy from a heat transfer medium (21), carbon dioxide in the fermentation liquid can be degassed.

[0096] The above discharge section (40) is a section from which a fermentation liquid (41) containing lysine, from which carbon dioxide has been removed, is discharged, and may be directly or indirectly connected to the body section. The body section (30) may be connected to one or more, two or more, three or more, four or more, or five or more recovery sections (40).

[0097] The above recovery part (40) can be connected to the upper, middle and / or lower portion of the body part (30). In one example, the recovery part (40) can be connected to the lower portion of the body part (30).

[0098] The above carbon dioxide degassing tower may further include a recovery unit (50) for recovering carbon dioxide degassed while the fermentation liquid containing lysine is heated by a heat transfer medium.

[0099] The above recovery unit (50) is a unit for recovering degassed carbon dioxide and may be directly or indirectly connected to the body unit. The body unit (30) may be connected to one or more, two or more, three or more, four or more, or five or more recovery units (50).

[0100] The above recovery part (50) can be connected to the top, middle and / or bottom of the body part (30). In one example, the recovery part (50) can be connected to the top of the body part (30).

[0101] The above recovery section (50) may be a section into which gas (32) containing carbon dioxide generated in the body section enters.

[0102] The above recovery unit (50) may include a carbon dioxide separation unit (51) and a carbon dioxide recovery device (52).

[0103] The internal temperature of the above carbon dioxide separation unit (51) is reduced by the cooling water (511), and at this time, carbon dioxide (513) can be separated from the gas (32) containing carbon dioxide inside the carbon dioxide separation unit. The condensate (514) from which carbon dioxide is separated can be removed from the carbon dioxide separation unit (51).

[0104] The separated carbon dioxide (513) is recovered by a carbon dioxide recovery device (52), and the recovered carbon dioxide can be reused for a carbonic acid absorption process that subsequently injects carbon dioxide into a fermentation liquid containing lysine.

[0105]

[0106] (c) Step: A step of concentrating the lysine process solution from which carbon dioxide has been removed obtained in step (b).

[0107] The above step (c) may be a step of concentrating the lysine process solution from which carbon dioxide has been removed obtained in the above step (b).

[0108] The step of concentrating the lysine process solution from which carbon dioxide has been removed obtained in the step (b) above is performed so that the lysine process solution has a solid content of 30 to 65 wt%, 30 to 62.5 wt%, 30 to 60 wt%, 30 to 57.5 wt%, 30 to 55 wt%, 30 to 52.5 wt%, 30 to 50 wt%, 30 to 47.5 wt%, 30 to 45 wt%, 30 to 42.5 wt%, 30 to 40 wt%, 32.5 to 65 wt%, 32.5 to 62.5 wt%, 32.5 to 60 wt%, 32.5 to 57.5 wt%, 32.5 to 55 wt%, 32.5 to 52.5 wt%, 32.5 to 50 wt%, 32.5 47.5 wt%, 32.5 to 45 wt%, 32.5 to 42.5 wt%, 32.5 to 40 wt%, 35 to 65 wt%, 35 to 62.5 wt%, 35 to 60 wt%, 35 to 57.5 wt%, 35 to 55 wt%, 35 to 52.5 wt%, 35 to 50 wt%, 35 to 47.5 wt%, 35 to 45 wt%, 35 to 42.5 wt%, 35 to 40 wt%, 37.5 to 65 wt%, 37.5 to 62.5 wt%, 37.5 to 60 wt%, 37.5 to 57.5 wt%, 37.5 to 55 wt%, 37.5 to 52.5 wt%, 37.5 to 50 wt%, 37.5 to 47.5 wt%, 37.5 to 45 wt%, 37.5 to 42.5 wt%, 37.5 to 40 wt%, 40 to 65 wt%, 40 to 62.5 wt%, 40 to 60 wt%, 40 to 57.5 wt%, 40 to 55 wt%, 40 to 52.5 wt%, 40 to 50 wt%, 40 to 47.5 wt%, 40 to 45 wt%, 40 to 42.5 wt%, 42.5 to 65 wt%, 42.5 to 62.5 wt%, 42.5 to 60 wt%, 42.5 to 57.5 wt%, 42.5 to 55 wt%, 42.5 to 52.5 wt%, 42.5 to 50 wt%, 42.5 to 47.5 wt%, 42.5 to 45 wt%, 45 to 65 wt%, 45 to 62.5 wt%, 45 to 60 wt%, 45 to 57.5 wt%, 45 to 55 wt%, 45 to 52.5 wt%, 45 to 50 wt%, 45 to 47.5 wt%, 47.5 to 65 wt%, 47.5 to 62.5 wt%, 47.5 to 60 wt%, 47.5 to 57.5 wt%, 47.5 to 55 wt%, 47.5 to 52.5 wt%, 47.5 to 50 wt%, 50 to 65 wt%, 50 to 62.5 wt%, 50 to 60 wt%, 50 to 57.5 wt%, 50 to 55 wt%, It may be a step of concentrating until the weight ratio becomes 50 to 52.5 wt%, 52.5 to 65 wt%, 52.5 to 62.5 wt%, 52.5 to 60 wt%, 52.5 to 57.5 wt%, 52.5 to 55 wt%, 55 to 65 wt%, 55 to 62.5 wt%, 55 to 60 wt%, 55 to 57.5 wt%, 57.5 to 65 wt%, 57.5 to 62.5 wt%, 57.5 to 60 wt%, 60 to 65 wt%, or 60 to 62.5 wt%, but is not limited thereto.

[0109] In one example, if the solid content of the lysine process solution exceeds the above range, fluidity may decrease, making it difficult to proceed with the process.

[0110] The step of concentrating the fermentation liquid containing the lysine comprises concentrating the fermentation liquid containing the lysine at a pressure of 10 to 1000 torr, 10 to 900 torr, 10 to 800 torr, 10 to 700 torr, 10 to 600 torr, 10 to 500 torr, 10 to 400 torr, 10 to 300 torr, 10 to 200 torr, 10 to 100 torr, 20 to 1000 torr, 20 to 900 torr, 20 to 800 torr, 20 to 700 torr, 20 to 600 torr, 20 to 500 torr, 20 to 400 torr, 20 to 300 torr, 20 to 200 torr, 20 to 100 torr, 30 to 1000 torr, 30 to 900 torr, 30 to 800 torr, 30 to 700 torr, 30 to 600 torr, 30 to 500 torr, 30 to 400 torr, 30 to 300 torr, 30 to 200 torr, 30 to 100 torr, 40 to 1000 torr, 40 to 900 torr, 40 to 800 torr, 40 to 700 torr, 40 to 600 torr, 40 to 500 torr, 40 to 400 torr, 40 to 300 torr, 40 to 200 torr, 40 to 100 torr, 50 to 1000 torr, 50 to 900 torr, 50 to at a pressure of 800 torr, 50 to 700 torr, 50 to 600 torr, 50 to 500 torr, 50 to 400 torr, 50 to 300 torr, 50 to 200 torr, or 50 to 100 torr; and / or

[0111] The step may be a step of concentrating at a temperature of 50 to 90°C, 50 to 85°C, 50 to 80°C, 50 to 75°C, 50 to 70°C, 55 to 90°C, 55 to 85°C, 55 to 80°C, 55 to 75°C, 55 to 70°C, 60 to 90°C, 60 to 85°C, 60 to 80°C, 60 to 75°C, 60 to 70°C, 65 to 90°C, 65 to 85°C, 65 to 80°C, 65 to 75°C, or 65 to 70°C, but is not limited thereto.

[0112]

[0113] The step (c) above may further include a step of injecting carbon dioxide into the lysine concentrate from which the carbon dioxide has been removed.

[0114] The carbon dioxide injected in the above step (c) may be recycled from the carbon dioxide removed in the above step (b).

[0115] The above method for manufacturing lysine has the advantage of being environmentally friendly, as it does not require a separate carbon source by recycling the carbon dioxide removed in step (b), thereby reducing manufacturing costs.

[0116] When the step of reinjecting the carbon dioxide is performed, the step (c) may be a step of concentrating the lysine process solution from which the carbon dioxide has been removed obtained in the step (b) until the solid content becomes 30 to 65 wt%, 30 to 60 wt%, 30 to 55 wt%, 30 to 50 wt%, 30 to 45 wt%, 35 to 65 wt%, 35 to 60 wt%, 35 to 55 wt%, 35 to 50 wt%, 35 to 45 wt%, 40 to 65 wt%, 40 to 60 wt%, 40 to 55 wt%, 40 to 50 wt%, 40 to 45 wt%, 45 to 65 wt%, 45 to 60 wt%, 45 to 55 wt%, or 45 to 50 wt%, but is not limited thereto.

[0117] By injecting carbon dioxide into the above concentrate, the beneficial effect of improving the hygroscopicity of lysine can be achieved. As used herein, the term "hygroscopicity" can refer to a tendency to absorb or retain moisture. Lysine has high hygroscopicity, which can lead to clumping. Therefore, improving hygroscopicity can prevent clumping.

[0118] In one example, the carbon dioxide-infused concentrate is an anion for lysine (in this paragraph, the anion is bicarbonate ion (HCO3 - ), carbonate ion (CO3 2-), or a combination thereof.) may mean a molar ratio of 0.1 to 52%, 0.1 to 50%, 0.1 to 45%, 0.1 to 41%, 0.1 to 40%, 0.5 to 52%, 0.5 to 50%, 0.5 to 45%, 0.5 to 41%, 0.5 to 40%, 1 to 52%, 1 to 50%, 1 to 45%, 1 to 41%, 1 to 40%, 5 to 52%, 5 to 50%, 5 to 45%, 5 to 41%, 5 to 40%, 10 to 52%, 10 to 50%, 10 to 45%, 10 to 41%, 10 to 40%, 15 to 52%, 15 to 50%, 15 to 45%, 15 to 41%, 15 to 40%, 20 to 52%, 20 to 50%, 20 to 45%, 20 to 41%, 20 to 40%, 25 to 65%, 25 to 52%, 25 to 50%, 25 to 45%, 25 to 41%, 25 to 40%, 30 to 65%, 30 to 52%, 30 to 50%, 30 to 45%, 30 to 41%, 30 to 40%, 35 to 52%, 35 to 50%, 35 to 45%, 35 to 41%, 35 to 40%, 40 It may be, but is not limited to, 52%, 40% to 50%, 40% to 45%, or 40% to 41%.

[0119] In one example, the carbon dioxide-infused concentrate may have a pH of, but is not limited to, 8.5 to 10, 8.5 to 9.8, 8.5 to 9.75, 8.5 to 9.5, 8.5 to 9.25, 8.5 to 9, 8.5 to 8.75, 8.75 to 10, 8.75 to 9.8, 8.75 to 9.75, 8.75 to 9.5, 8.75 to 9.25, 8.75 to 9, 9 to 10, 9 to 9.8, 9 to 9.75, 9 to 9.5, 9 to 9.25, 9.25 to 10, 9.25 to 9.8, 9.25 to 9.75, or 9.25 to 9.5.

[0120]

[0121] The step of injecting carbon dioxide may be a step of injecting carbon dioxide using a carbon dioxide absorption tower.

[0122] The above carbon dioxide absorption tower,

[0123] (1) An input section into which a process solution containing lysine (which may be, in one example, a process solution from which carbon dioxide has been removed and / or a concentrated solution from which the process solution has been concentrated, obtained in step (b) above) is input;

[0124] (2) A carbon dioxide supply device that generates carbon dioxide;

[0125] (3) a body part in which the process liquid comes into contact with the carbon dioxide or the carbon dioxide is transferred to the process liquid; and

[0126] (4) It may include a discharge unit through which the above process liquid is discharged.

[0127] The above (1) input section; (3) body section and (4) discharge section are the same as the carbon dioxide degassing tower described above.

[0128] In one example, the body portion may include one or more stages with which the process liquid can come into contact. The stages are not limited to a specific form as long as the process liquid can efficiently come into contact with the carbon dioxide generated from the carbon dioxide supply device, and may include 1 or more, 2 or more, 3 or more, 4 or more, 5 or more, 6 or more, 7 or more, 8 or more, 9 or more, 10 or more, 11 or more, 12 or more, 13 or more, 14 or more, 15 or more, 16 or more, 17 or more, 18 or more, 19 or more, 20 or more, 21 or more, 22 or more, 23 or more, 24 or more, 25 or more, 26 or more, 27 or more, 28 or more, 29 or more, 30 or more (the upper limit is not particularly limited and may be, for example, about 100 or less). In one embodiment, the body portion may comprise 15 to 25 or 20 sections.

[0129] In one example, the carbon dioxide supply device may supply carbon dioxide recovered through a recovery unit of a carbon dioxide degassing tower after carbon dioxide is removed in step (b).

[0130]

[0131] (d) Step: A step of granulating the concentrate obtained in step (c).

[0132] The above step (d) may be a step of granulating the concentrate obtained in the above step (c).

[0133] In one example, lysine granules can be obtained by performing the above granulating step.

[0134] The above granulating step can be performed using granulating equipment commonly known in the art, such as a dry granulator, a wet granulator (low shear granulator (ribbon / paddle mixer, planetary mixer, orbital spiral mixer, sigma blade mixer, etc.), a high shear granulator, a roller compactor, a spray dryer, a fluidized bed granulator, etc.).

[0135] The lysine granules obtained by performing the above granulating step have a lysine solid content of 75 wt% or more, 76 wt% or more, 77 wt% or more, 78 wt% or more, 79 wt% or more, 80 wt% or more, 80.3 wt% or more, 80.4 wt% or more, 81 wt% or more, 82 wt% or more, 83 wt% or more, 84 wt% or more, 85 wt% or more, 86 wt% or more, 87 wt% or more, 88 wt% or more, 88.1 wt% or more, 88.2 wt% or more, 88.3 wt% or more; Or 75 to 95 wt%, 75 to 92.5 wt%, 75 to 90 wt%, 75 to 89 wt%, 75 to 88 wt%, 75 to 87.5 wt%, 75 to 87 wt%, 75 to 85 wt%, 75 to 82.5 wt%, 75 to 80 wt%, 77.5 to 95 wt%, 77.5 to 92.5 wt%, 77.5 to 90 wt%, 77.5 to 89 wt%, 77.5 to 88 wt%, 77.5 to 87.5 wt%, 77.5 to 85 wt%, 77.5 to 82.5 wt%, 77.5 to 80 wt%, 80 to 95 wt%, 80 to 92.5 wt%, 80 to 90 wt%, 80 to 89 wt%, 80 to 88 wt%, 80 to 87.5 wt%, 80 to 87 wt%, 80 to 85 wt%, 80 to 82.5 wt%, 82.5 to 95 wt%, 82.5 to 92.5 wt%, 82.5 to 90 wt%, 82.5 to 89 wt%, 82.5 to 88 wt%, 82.5 to 87.5 wt%, 82.5 to 87 wt%, 82.5 to 85 wt%, 85 to 95 wt%, 85 to 92.5 wt%, 85 to 90 wt%, 85 to 89 wt%, 85 to 88 wt%, 85 to 87.5 wt%, 85 to 87 wt%, 88 to 95 wt%, 88 to 92.5 wt%, 88 to 90 wt%, 88 to 89 wt%, 88.1 to 95 wt%, 88.1 to 92.5 wt%, 88.1 to 90 wt%, 88.1 to 89 wt%, 88.It may be 3 to 95 wt%, 88.3 to 92.5 wt%, 88.3 to 90 wt% or 88.3 to 89 wt%, but is not limited thereto.

[0136]

[0137] The method for producing lysine of the present application may not involve performing an ion exchange process.

[0138] The above ion exchange process may not be performed in the step of removing carbon dioxide from the fermentation liquid containing lysine using a carbon dioxide degassing tower (b), and may not be performed after the step of preparing the fermentation liquid containing lysine by culturing microorganisms (a) and / or before the step of concentrating the lysine process liquid from which carbon dioxide has been removed obtained in the step (b) (c).

[0139] In this specification, the ion exchange process may refer to both a cation exchange process and an anion exchange process. The cation exchange process may refer to a step of removing cationic impurities using a cation exchange resin, and the cation exchange resin may refer to a commonly known cation exchange resin, such as a strongly acidic cation exchange resin (SAC) or a weakly acidic cation exchange resin (WAC).

[0140] The lysine manufacturing method of the present application does not perform the ion exchange process as described above, so there is no need for the use of ion exchange resin, pH regulator, eluent, or waste liquid treatment, thereby reducing manufacturing costs and providing the advantage of being environmentally friendly.

[0141] The lysine manufacturing method of the present application has the advantage of being able to manufacture a lysine product containing a high lysine content without performing an ion exchange process.

[0142]

[0143] Another aspect is a step of (a) culturing microorganisms to prepare a fermentation solution containing lysine; and

[0144] (b) A method for removing carbon dioxide from a lysine fermentation solution is provided, comprising a step of removing carbon dioxide from a fermentation solution containing lysine using a carbon dioxide degassing tower.

[0145] Steps (a), (b), etc. above are as described above.

[0146]

[0147] The present application relates to a method for producing lysine, comprising the steps of: culturing a microorganism to prepare a fermentation solution containing lysine; and removing carbon dioxide from the fermentation solution containing lysine using a carbon dioxide degassing tower. By removing carbon dioxide using the carbon dioxide degassing tower, a lysine product containing a high lysine content can be obtained while achieving a high carbon dioxide removal rate in a short period of time.

[0148]

[0149] Figure 1 is a drawing showing the structure of a carbon dioxide degassing tower according to one embodiment.

[0150]

[0151] The present invention will be described in more detail below with reference to the following examples. However, these examples are provided solely to illustrate the present invention, and the scope of the present invention is not limited by these examples.

[0152]

[0153] Example 1. Preparation of fermentation solution containing L-lysine

[0154] Corynebacterium glutamicum CJ3P (US 9556463 ​​B2), which can produce L-lysine, was cultured in 25 ml of seed medium at 30°C and 200 rpm for 20 hours. The microorganism obtained through the seed culture was inoculated at a ratio of 3.0% (v / v) into a 5 L fermentation tank (pH 7.0) containing a medium supplemented with 0.46% ammonium sulfate and 0.03% phosphate based on the molar ratio of glucose. The medium was sufficiently aerated and stirred at 30°C, and cultured until all the introduced glucose was consumed to obtain the final fermentation solution. The microorganism obtained through the 5 L seed culture was inoculated at a ratio of 20.0% (v / v) into a production medium (30 L fermentation tank) containing a medium supplemented with 0.42% ammonium salt (such as ammonium sulfate) based on the molar ratio of glucose. The fermented solution was cultured at 30°C with sufficient aeration and stirring until all the added glucose was consumed, thereby obtaining the final fermented solution. After the culture was completed, the L-lysine concentration in the fermented solution was analyzed using HPLC (Water, 2478). Microorganisms in the fermented solution were removed using a 0.1 μm membrane.

[0155] The L-lysine concentration in the fermentation solution was measured and found to be approximately 30 g / l.

[0156] The composition of the above-mentioned seed medium (25 ml), seed medium (5 L), and production medium is as shown below:

[0157] Seed medium (25ml)

[0158] Per 1L of distilled water: 10 g of glucose, 5.0 g of bacto tryptone, 5.0 g of bacto yeast extract, 10.0 g of ammonium sulfate, 2.0 g of urea, 5.0 g of KH2PO4, 10.0 g of K2HPO4, 0.5 g of MgSO47H2O

[0159] Seedling tray (5L)

[0160] 1 mL of antifoaming agent, 10.0 g of corn steep liquor, 1.0 mg of biotin, 10.0 mg of thiamine, 10.0 mg of pantothenic acid, 10.0 mg of niacinamide per 1 L of distilled water

[0161] production medium

[0162] 1 mL of antifoaming agent, 10.0 g of corn steep liquor, 1.0 mg of biotin, 10.0 mg of thiamine, 10.0 mg of pantothenic acid, 10.0 mg of niacinamide per 1 L of distilled water

[0163]

[0164] Example 2. Preparation of lysine granules (carbon dioxide degassing tower process)

[0165] Example 2-1. Preparation of lysine granules (1)

[0166] A carbon dioxide degassing tower was used to remove carbon dioxide from a fermentation solution containing L-lysine. The carbon dioxide degassing tower is a structure comprising an upper inlet into which a fermentation solution containing L-lysine is introduced, one or more stages with which the fermentation solution comes into contact as it descends, a lower heat source that generates a heat transfer medium toward the upper end, and a lower discharge portion through which the fermentation solution is discharged.

[0167] In this example, carbon dioxide present in the fermentation solution containing L-lysine prepared in Example 1 was removed using a carbon dioxide stripping tower (QBR Tech). The carbon dioxide stripping tower has 20 stages inside, and the L-lysine process solution descending from the upper portion of the carbon dioxide stripping tower is heated by a heat source at the lower portion of the carbon dioxide stripping tower, and as the heat transfer medium generated rises, gas-liquid contact occurs at each of the 20 stages. Therefore, when this is used, the L-lysine process solution with a large surface area can come into contact with the hot heat transfer medium, so that carbon dioxide can be efficiently removed from the L-lysine process solution.

[0168] 30 kg of the fermentation solution containing L-lysine manufactured in Example 1 (solid content 16 wt%) was placed in a carbon dioxide degassing tower for about 4 hours to remove carbon dioxide, and as a result, an L-lysine process solution (about 27.7 kg, pH 10.0, concentration ration 1.08) with about 98% of carbon dioxide removed was obtained.

[0169] The above carbon dioxide removal rate was calculated as “amount of carbon dioxide removed / amount of carbon dioxide in the fermentation liquid containing lysine,” and the removed carbon dioxide was recovered for reuse in the subsequent process through the recovery unit in the carbon dioxide stripping tower. The above concentrated effluent reflects the increase in the concentration of lysine due to the evaporation of some of the water during the carbon dioxide removal process, and was calculated as “content of lysine in the process liquid discharged after carbon dioxide removal / content of lysine in the fermentation liquid introduced.”

[0170] Table 1 below shows the carbon dioxide degassing results according to the operation of the carbon dioxide degassing tower in the manufacturing method of Example 2-1.

[0171] Carbon dioxide stripping results using a carbon dioxide stripping tower Time Lower temperature Upper temperature Bicarbonate concentration CO2 removal rate Concentration multiple -℃℃ g / L% -1:00103.30 97.000.72 98.21 02 2:00103.30 95.30 0.76 98.11 08 3:00103.00 95.30 0.59 98.51 04 4:00103.00 95.50 0.47 98.81 14

[0172] 27 kg of the L-lysine process solution manufactured by removing the above carbon dioxide was placed in a 20 L rotary concentrator (N-21NS, EYELA) and concentrated until the solid content became 65 wt% (internal pressure 100 torr, 70 ℃), thereby obtaining 7.2 kg of L-lysine concentrate (solid content 65 wt%, pH 10.3, 25 ℃). Using a fluidized bed granulator (Daesung), the manufactured L-lysine concentrate was used to obtain 4.6 kg of L-lysine granules having an L-lysine content of approximately 88.3%.

[0173]

[0174] Example 2-2. Manufacturing of lysine granules (2) (including carbonic acid absorption process)

[0175] In Example 2-1, 27 kg of the lysine process solution manufactured by removing carbon dioxide was introduced into a 20 L rotary concentrator (N-21NS, EYELA) and concentrated until the solid content became 45 wt% (internal pressure 100 torr, 70°C), thereby obtaining 10.4 kg of L-lysine concentrate (solid content 45 wt%, pH 10.0, 25°C).

[0176] In order to improve the hygroscopicity of the L-lysine concentrate manufactured above, carbon dioxide was injected into the L-lysine concentrate using a carbon dioxide absorption tower (QBR Tech). The carbon dioxide absorption tower includes 20 stages inside, and the L-lysine process solution (L-lysine concentrate) descending from the upper part of the carbon dioxide absorption tower makes gas-liquid contact in each of the 20 stages as the carbon dioxide generated from the carbon dioxide generator at the lower part of the carbon dioxide absorption tower rises. Therefore, when this is used, the L-lysine process solution with a large surface area can come into contact with the carbon dioxide, so that carbon dioxide can be efficiently injected into the L-lysine process solution.

[0177] As a result of injecting carbon dioxide by injecting the above L-lysine concentrate into the upper part of the carbon dioxide absorption tower at a flow rate of 44.8 ml / min, approximately 58.4% of the supplied carbon dioxide was absorbed, and the pH was 9.0, and the molar ratio of bicarbonate ion / lysine was approximately 40.3%.

[0178] The above carbon dioxide-injected L-lysine concentrate was granulated using a fluidized bed granulator (Daesung) to obtain 4.7 kg of L-lysine granules having an L-lysine content of approximately 80.6%. The detailed operating conditions of the fluidized bed granulator are as shown in Example 2-1 and Table 1.

[0179]

[0180] Comparative Examples 1 and 2 below are examples in which a concentration process (Comparative Example 1) or a heating process (Comparative Example 2) is performed to remove carbon dioxide from a fermentation solution containing L-lysine manufactured in Example 1. The L-lysine manufacturing method provided in the present application can obtain a lysine product containing a high lysine content while achieving a high carbon dioxide removal rate in a short period of time compared to the manufacturing methods of Comparative Examples 1 and 2.

[0181]

[0182] Comparative Example 1. Manufacturing of lysine granules (1) (concentration process)

[0183] Comparative Example 1-1. Preparation of lysine granules (1)

[0184] The fermentation liquid containing L-lysine prepared in Example 1 was concentrated, and carbon dioxide present in the fermentation liquid was removed.

[0185] 30 kg of fermentation broth containing L-lysine (solid content 16 wt%) was charged into a 20 L rotary concentrator (N-21NS, EYELA) and concentrated for 7 hours (internal pressure 100 torr, 70 ℃) to remove carbon dioxide. Since carbon dioxide was emitted from the fermentation broth, the vacuum inside the concentrator was dynamically controlled. As a result of carbonic acid degassing through the concentration process, carbon dioxide was removed as the fermentation broth containing L-lysine was concentrated. When the fermentation broth was concentrated 1.22 times the amount of concentration input (solid content in the fermentation broth was approximately 19.52 wt%), approximately 52% of carbon dioxide was removed, and when the fermentation broth was concentrated 2 times the amount of concentration input (solid content in the fermentation broth was 32 wt%), approximately 60% of carbon dioxide was removed.

[0186] Since the above concentration process alone cannot sufficiently remove carbon dioxide, the process liquid was heated with a heating mantle (Daihan science, DH-WHM12073-EA) to further remove carbon dioxide. The process liquid was heated at 105°C for 2 hours three times while stirring at 150 rpm using a magnetic stirrer, and a circulator (Julabo, Dyneo DD) was installed at the top to recondense the evaporated water vapor. As a result, 15 kg of L-lysine process liquid with approximately 98% of carbon dioxide removed was obtained.

[0187]

[0188] 20 kg of the L-lysine process solution manufactured above was placed in a 20 L rotary concentrator (N-21NS, EYELA) and concentrated until the solid content became 65 wt% (internal pressure 100 torr, 70 ℃), thereby obtaining 7.38 kg of L-lysine concentrate (solid content 65 wt%, pH 10.2, 25 ℃).

[0189] The L-lysine concentrate prepared above was used to produce 4.72 kg of L-lysine granules having an L-lysine content of 87.9% using a fluidized bed granulator (Daesung).

[0190] In this way, in order to concentrate the fermentation liquid containing L-lysine and remove more than 98% of the carbon dioxide in the fermentation liquid, a process time of more than 13 hours (7 hours of concentration + 2 hours of heating * 3 times) was required.

[0191]

[0192] Comparative Example 1-2. Manufacturing of lysine granules (2) (including carbonic acid absorption process)

[0193] 15 kg of the lysine process solution manufactured in Comparative Example 1-1 was placed in a 20 L rotary concentrator (N-21NS, EYELA) until the solid content became 45 wt% and concentrated for 7 hours (internal pressure 100 torr, 70 ℃), thereby obtaining 10.7 kg of L-lysine concentrate (solid content 45 wt%, pH 10.2, 25 ℃).

[0194] The L-lysine concentrate prepared above was injected with carbon dioxide using a carbon dioxide absorption tower (QBR Tech). As a result of injecting carbon dioxide into the upper portion of the carbon dioxide absorption tower of Example 2-2 at a flow rate of 44.8 ml / min, approximately 58.9% of the supplied carbon dioxide was absorbed, and the pH was 9.0, and the molar ratio of bicarbonate ions / lysine was approximately 40.7%.

[0195] The above carbon dioxide-injected L-lysine concentrate was granulated using a fluidized bed granulator (Daesung) to obtain 4.85 kg of L-lysine granules having an L-lysine content of approximately 80.3%.

[0196]

[0197] Comparative Example 2. Manufacturing of lysine granules (2) (heating process)

[0198] Comparative Example 2-1. Manufacturing of lysine granules (1)

[0199] The fermentation solution containing L-lysine prepared in Example 1 was heated using a heating mantle to remove carbon dioxide present in the fermentation solution.

[0200] 30 kg of fermentation solution containing L-lysine was divided into 5 kg portions in 10 L glass flasks and heated with a heating mantle (Daihan science, DH-WHM12073-EA). The solution was heated at 105 ℃ for 4 hours, repeated 6 times, while stirring at 150 rpm using a magnetic stirrer, and a circulator (Julabo, Dyneo DD) was installed at the top to recondense the evaporated water vapor. The carbon dioxide removal rate according to the heating time is shown in Table 2 below. As a result, 30 kg of L-lysine process solution with approximately 98% of carbon dioxide removed was obtained.

[0201]

[0202] In this way, when performing a heating process using a heating mantle on a fermentation liquid containing L-lysine, a heating time of 24 hours (4 hours of heating * 6 times) or more was required to remove more than 98% of the carbon dioxide in the fermentation liquid.

[0203]

[0204] 30 kg of the L-lysine process solution manufactured above was placed in a 20 L rotary concentrator (N-21NS, EYELA) and concentrated until the solid content became 65 wt% (internal pressure 100 torr, 70°C), thereby obtaining 7.38 kg of L-lysine concentrate (solid content 65 wt%, pH 10.3, 25°C).

[0205] Using the L-lysine concentrate prepared above, a fluidized bed granulator (Daesung) was used to obtain 4.8 kg of L-lysine granules having an L-lysine content of approximately 88.1%.

[0206]

[0207] Comparative Example 2-2. Manufacturing of lysine granules (2) (including carbonic acid absorption process)

[0208] 25 kg of the lysine process solution manufactured in Comparative Example 2-1 was placed in a 20 L rotary concentrator (N-21NS, EYELA) and concentrated until the solid content became 45 wt% (internal pressure 100 torr, 70 ℃), thereby obtaining 10.6 kg of L-lysine concentrate (solid content 45 wt%, pH 10.3, 25 ℃).

[0209] The L-lysine concentrate prepared above was injected with carbon dioxide using the carbon dioxide absorption tower (QBR Tech) of Example 2-2. As a result of injecting carbon dioxide by introducing the L-lysine concentrate into the upper part of the carbon dioxide absorption tower at a flow rate of 44.8 ml / min, approximately 59.2% of the supplied carbon dioxide was absorbed, and the pH was 9.0, and the molar ratio of bicarbonate ions / lysine was approximately 40.8%.

[0210] The above carbon dioxide-injected L-lysine concentrate was granulated using a fluidized bed granulator (Daesung) to obtain 4.73 kg of L-lysine granules having an L-lysine content of approximately 80.4%.

[0211]

[0212]

[0213] From the above description, those skilled in the art will understand that the present invention can be implemented in other specific forms without altering its technical spirit or essential characteristics. In this regard, it should be understood that the embodiments described above are illustrative in all respects and not restrictive. The scope of the present invention should be interpreted as encompassing all changes or modifications derived from the meaning and scope of the following claims and their equivalent concepts, rather than the detailed description above.

[0214]

[0215] [Explanation of symbols]

[0216] 10: Input section

[0217] 11: Lysine fermentation solution

[0218] 20: Heat source

[0219] 201: Steam

[0220] 202: Condensate

[0221] 21: Heat transfer medium

[0222] 30: Body

[0223] 31: Single

[0224] 32: Gas containing carbon dioxide

[0225] 40: Exhaust

[0226] 41: Lysine fermentation solution with carbon dioxide removed

[0227] 50: Recovery Department

[0228] 51: Carbon dioxide separation unit

[0229] 511: Coolant in

[0230] 512: Coolant out

[0231] 513: Carbon dioxide

[0232] 514: vapor condensate

[0233] 52: Carbon dioxide recovery device

Claims

(a) a step of culturing microorganisms to prepare a fermentation solution containing lysine; and (b) A method for producing lysine, comprising a step of removing carbon dioxide from a fermentation solution containing the lysine using a carbon dioxide degassing tower, The above carbon dioxide degassing tower is, (1) An input portion into which a fermentation solution containing the above lysine is input; (2) A heat source that generates a heat transfer medium; (3) a body part that comes into contact with the fermentation liquid and the heat transfer medium or through which the heat energy of the heat transfer medium is transferred to the fermentation liquid; and (4) Including a discharge unit through which the above fermented liquid is discharged, Method for producing lysine. A method for producing lysine, wherein the fermentation solution containing lysine in step (a) is a fermentation product obtained by culturing a microorganism producing lysine in a medium, or a fermentation product obtained by removing the cell from the fermentation product. A method for producing lysine in claim 1, wherein the heat transfer medium is a gas. A method for producing lysine in claim 1, wherein the temperature of the heat transfer medium is 75 to 150°C. A method for producing lysine, wherein the body part comprises at least one stage with which the fermentation liquid can come into contact. A method for producing lysine, wherein in the first paragraph, step (b) is a step of removing 85% or more of carbon dioxide from a fermentation solution containing lysine. A method for producing lysine, wherein the pH of the fermentation solution containing lysine from which carbon dioxide has been removed obtained in step (b) in the first paragraph is 8.5 to 11. A method for producing lysine, wherein in the first paragraph, the carbon dioxide degassing tower further includes a recovery unit for recovering the degassed carbon dioxide. A method for producing lysine, further comprising the step of concentrating the lysine process solution from which carbon dioxide has been removed obtained in step (b) in paragraph 1. A method for producing lysine, wherein in claim 9, step (c) is a step of concentrating the lysine process solution from which carbon dioxide has been removed obtained in step (b) until the solid content becomes 30 to 65 wt%. A method for producing lysine, further comprising the step of granulating the concentrate obtained in step (c) in paragraph 9. A method for producing lysine, wherein the lysine content of the lysine granules obtained by granulation in step (d) is 75 to 90 wt%. A method for producing lysine, wherein in claim 9, step (c) further comprises a step of injecting carbon dioxide into the lysine concentrate from which carbon dioxide has been removed. A method for producing lysine, wherein in the 13th paragraph, the step of injecting carbon dioxide is to reuse and inject the carbon dioxide removed in the step (b). A method for producing lysine, wherein in the 13th paragraph, the step (c) is a step of concentrating the lysine process solution from which the carbon dioxide has been removed until the solid content becomes 30 to 60 wt%. In the 13th paragraph, the carbon dioxide-injected concentrate is a bicarbonate ion (HCO3) for lysine - ) A method for producing lysine, wherein the molar ratio of lysine is 10 to 65%. A method for producing lysine in claim 13, wherein the carbon dioxide-injected concentrate has a pH of 8.5 to 10.

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