CN1156392C - Process for recovering carbon dioxide in glutamic acid fermentation - Google Patents
Process for recovering carbon dioxide in glutamic acid fermentation Download PDFInfo
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- CN1156392C CN1156392C CNB991030591A CN99103059A CN1156392C CN 1156392 C CN1156392 C CN 1156392C CN B991030591 A CNB991030591 A CN B991030591A CN 99103059 A CN99103059 A CN 99103059A CN 1156392 C CN1156392 C CN 1156392C
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- glutamic acid
- carbon dioxide
- sodium bicarbonate
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- sodium
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/59—Biological synthesis; Biological purification
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- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Treating Waste Gases (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
A waste gas in the L-glutamic acid fermentation is blowed into an aqueous solution of caustic soda or sodium hydroxide, low-concentration CO2 in the waste gas is captured in the form of alkal carbonate, then links to the L-glutamic acid which needs alkali as neutralization agent. Thereby, the monosodium L-glutamate is produced to simultaneously recover high-concentration CO2 formed as a by-product, which is a source of liquid CO2.
Description
The present invention relates to a process in which carbon dioxide (hereinafter referred to as "CO") contained in an exhaust gas discharged from the fermentation of L-glutamic acid2") is effectively captured and effectively utilized in the process for producing L-glutamic acid, and finally recovered in a highly pure form.
The actual situation up to now is that CO contained in the exhaust gas from L-glutamic acid fermentation, an aerobic fermentation process2Is discharged to the atmosphere without any utilization.
In contrast, it is known that alcohol fermentation, a process in which the CO in the exhaust gas is discharged by anaerobic fermentation, is carried out2Is directly used for liquid CO2In the preparation method of (1). This is based on CO in the exhaust gas from the anaerobic fermentation process2To 95% or higher, making the above process relatively cost effective.
Generally, in L-glutamic acid fermentation, CO in exhaust gas2Is in the range of a few percent to about 10%, which is too low compared to the case in alcoholic fermentation. Therefore, the CO in the exhaust gas is to be removed2Using liquid CO2Additional CO is required in the preparation2And (5) concentrating. This would raise the cost without getting a profit at all. In addition, CO is added from the viewpoint of global environment protection (prevention of global warming)2Venting to the atmosphere is disadvantageous.
The invention aims to provide a method for recovering low-concentration CO2The process of (1), the CO2Is discharged from the fermentation process of L-glutamic acid, and is used in the preparation method of L-glutamic acid to highly concentrate or highly purify CO2Is recovered without any concentration of CO2The step (2).
Another object of the present invention is to provide a process for producing monosodium L-glutamic acid, which comprises separating L-glutamic acid from a fermentation medium of L-glutamic acid using not only basic carbonate as a neutralizing agent but also L-glutamic acidRecovery of high purity CO as by-product formed during acid neutralization2The method of (1).
The present invention achieves the above objects. According to the present invention, CO discharged from the fermentation of L-glutamic acid2Is blown into soda ash water solution or sodium hydroxide water solution, in which CO is2Is selectively captured in the form of sodium bicarbonate or sodium carbonate, and then these alkaline carbonates are used to neutralize L-glutamic acid separated from the L-glutamic acid fermentation medium, so that monosodium L-glutamic acid can be produced while CO is formed as a by-product2Can be recovered in high concentration.
That is, the present invention relates to:
1) a method for recovering carbon dioxide from L-glutamic acid fermentation, comprising the steps of:
(a) CO-containing discharged from L-glutamic acid fermentation process2The waste gas is blown into soda ash water solution or sodium hydroxide water solution to prepare sodium bicarbonate or sodium carbonate,
(b) allowing the obtained sodium bicarbonate or sodium carbonate to act on L-glutamic acid separated from the L-glutamic acid fermentation medium in an aqueous medium, and
(c) recovery of high purity CO formed as a by-product2And preparing monosodium L-glutamate.
2) The method for recovering carbon dioxide according to 1) above, wherein the sodium bicarbonate is prepared by blowing carbon dioxide discharged during the fermentation of L-glutamic acid into 5-30 wt% soda ash aqueous solution at a temperature of room temperature to 70 ℃.
3) The method for recovering carbon dioxide as described in 1) above, wherein the sodium hydrogencarbonate is allowed to act as a 24 to 42 wt% aqueous slurry at a temperature of from room temperature to 70 ℃ to L-glutamic acid.
4) The method for recovering carbon dioxide as described in 1) above, wherein the sodium carbonate is allowed to act on the L-glutamic acid in the form of a 15 to 32 wt% aqueous solution at a temperature of from room temperature to 70 ℃.
The present invention is described in detail below.
For containing CO discharged from the fermentation process of L-glutamic acid2The waste gas is blown into soda ash water solution or sodium hydroxide water solutionSodium bicarbonate or sodium carbonate is efficiently produced in solution using 5-30 wt%, preferably 18-22 wt% soda grey water solution or 4-30 wt% sodium hydroxide aqueous solution.
Usually the above-mentioned CO-containing2Contains smoke, ammonia and other impurities, and thus the smoke should be removed by a smoke separator and then CO containing substantially no smoke should be allowed to flow2The exhaust gas is contacted with a soda grey water solution or an aqueous sodium hydroxide solution.
Any of the packed column, plate column and bubble column types of absorption columns can be used as CO2The absorption apparatus of (4), however, a packed column is preferred. In addition, CO is absorbed2The operation of (2) may be batch or continuous, but a continuous mode is preferred. Removing CO from fume exhaust2The concentration is diluted to a few percent to about 10 percent by volume. To efficiently absorb CO by blowing off-gas into soda ash water solution or sodium hydroxide aqueous solution2To carry out CO2The temperature of the absorption operation is preferably as follows: the temperature is between normal temperature and 70 ℃ when soda ash water solution is used, and between normal temperature and 40 ℃ when sodium hydroxide water solution is used.
Soda ash with CO2The reaction produces sodium bicarbonate in the form of a crystalline precipitate which is separated by conventional solid/liquid separation methods such as filtration, centrifugation and the like after precipitation in a settling tank. To the obtained sodium hydrogencarbonate crystals were added an amount of water to prepare a 24 to 42% by weight slurry for neutralizing L-glutamic acid. Sodium hydroxide and CO, on the other hand2The sodium carbonate solution obtained by the reaction is mixed with a certain amount of water to prepare a 15-32 wt% aqueous sodium carbonate solution for neutralizing L-glutamic acid.
If the sodium bicarbonate slurry or the aqueous sodium carbonate solution reaches the above concentration, it is used to neutralize L-glutamic acid.
The L-glutamic acid to be neutralized with an alkaline carbonate is such that the microorganism contained therein is removed by centrifugation from the L-glutamic acid fermentation medium in accordance with a conventional method, then the pH is adjusted to 3.2 to 3.5 with hydrochloric acid, and the L-glutamic acid is crystallized and isolated for use inthe present invention.
Mixing the L-glutamic acid crystal with sodium bicarbonate water slurry and/or sodium carbonate water solution, and carrying out neutralization reaction to prepareObtaining L-monosodium glutamate and CO2A gas.
The temperature of the neutralization reaction is preferably from room temperature to 70 deg.C, more preferably from 50 to 70 deg.C.
The neutralization reaction of L-glutamic acid may be carried out as crystals or as a slurry in water. When a slurry is used, the slurry can be conveniently prepared by mixing L-glutamic acid crystals with an aqueous solution of monosodium L-glutamate, e.g., a saturated solution of monosodium L-glutamate in which precipitate of sodium L-glutamate crystals has been separated.
The neutralization reaction may be carried out batchwise or continuously, but a continuous operation is preferred.
The obtained monosodium L-glutamate solution is concentrated to crystallize monosodium L-glutamate, and the monosodium L-glutamate crystal is prepared by separating and drying according to a conventional method.
On the other hand, CO formed in the neutralization reaction of L-glutamic acid with an alkaline carbonate can be efficiently neutralized with a vapor/liquid separator2The gas is separated from the solution and the CO with a purity higher than 95% can be recovered2And directly using it for preparing liquid CO2In the operation of (1).
Considering that the production of liquid CO is now industrially obtained by burning heavy oil2The present invention is characterized in that the CO-containing raw material discharged into the atmosphere can be effectively utilized2And therefore, the present invention can be said to have significant effects in terms of protecting the atmospheric environment and saving petroleum resources.
According to the present invention, L-glutamic acid ('Glu') is mixed with a sodium bicarbonate/water slurry or an aqueous sodium carbonate solution to perform a neutralization reaction, thereby producing monosodium L-glutamate ('MSG') and CO2A gas. CO recovery from the monosodium L-glutamate (MSG) obtained per unit2From the viewpoint of gas amount, the use of sodium bicarbonate as a neutralizing agent for L-glutamic acid is more preferable. Sodium bicarbonate can recover 2 times more CO than sodium carbonate as shown in the following reaction scheme2A gas. In the preferred embodiment of the present invention shown in FIGS. 1 and 2, CO is contained in the discharge from the fermentation of L-glutamic acid2Is blown into the soda ash water solution to produce sodium bicarbonate/waterSlurry which is then reacted with L-glutamic acid to produce CO2Is recovered to prepare the L-monosodium glutamate.
2C5H9NO4(Glu)+2NaHCO2
2C5H8NO4·Na(MSG)+2CO2+2H2O
2C5H9NO4(Glu)+Na2CO3
2C5H8NO4·Na(MSG)+CO2+H2O
The flow chart of the apparatus used in the example of the present invention is shown in fig. 1 and 2.
FIG. 1 is a schematic flow chart showing the absorption of CO contained in the exhaust gas discharged from the fermentation of L-glutamic acid2In which the CO is contained starting from the discharge at the top of the fermenter 1 (sodium bicarbonate/water slurry preparation method)2The exhaust gas supply line a is connected to a mist separator 2 for removing mist, and its outlet side is connected to the lower end of a cleaning tower 3 for removing other impurities present in the exhaust gas.
The outlet side of the cleaning tower 3 is connected to a heat exchanger 5 connected to a steam supply line for heating the exhaust gas by a blower 4. Outlet side of heat exchanger 5 and CO2The lower ends of the absorption towers 6 are connected, and two CO are arranged2The absorption columns 6 and 7 are connected in series with each other.
On the other hand, the circulating supply line B for soda ash water solution is connected to CO via a feed pump 112The top end of the absorption column 7 has a branch extending to the point of CO2Above the sodium bicarbonate settler 8 below the absorption column 6 to feed the settler 8. CO 22The outlet side of the absorption column 7 is located above the sodium bicarbonate replenishment tank 10.
The recycle line from the sodium bicarbonate settler 8 was connected to the CO2The top of the absorption column 6, the outlet side of which is located above the sodium bicarbonate settler 8. The outlet side of the sodium bicarbonate settler 8 is connected to a separator 13 by a feed pump 12, and sodium bicarbonate is discharged from the bottom at the outlet side of the settler 8 for controlling the slurryAnd (4) concentration.
A sodium bicarbonate slurry tank 14 is provided below the separator 13 to store sodium bicarbonate crystals separated from the separator 13, and a mother liquor tank 15 is provided below the separator 13 to store mother liquor separated from the separator 13. A mother liquor supply line from the outlet side of the mother liquor tank 15 is connected to the upper side of the sodium hydrogencarbonate settling tank 8 through a feed pump 16 so that the mother liquor is introduced thereinto.
A water supply line is connected to the upper side of the sodium hydrogencarbonate slurry tank 14, sodium hydrogencarbonate is crystallized to prepare a slurry, and the resulting slurry is supplied from the outlet of the sodium hydrogencarbonate slurry tank 14 to an L-glutamic acid neutralization column 19 (see FIG. 2) through a feed pump 17.
FIG. 2 is a flow chart illustrating CO incorporated in a process for the preparation of monosodium L-glutamate2A recovery process wherein a supply line of an L-glutamic acid solution from an L-glutamic acid supply tank 18 is connected to the bottom end of an L-glutamic acid neutralization column 19.
A sodium hydrogencarbonate slurry supply line from the sodium hydrogencarbonate slurry tank 14 was connected to an L-glutamic acid solution supply line at a position below the L-glutamic acid neutralization column 19 to mix sodium hydrogencarbonate with the L-glutamic acid solution and perform a neutralization reaction between L-glutamic acid and sodium hydrogencarbonate. A supply line of the monosodium L-glutamate solution from the outlet side of the L-glutamic acid neutralization column 19 is connected to a gas/liquid separator 20 in which the monosodium L-glutamate solution and CO are supplied2The gases are separated from each other.
Below the gas/liquid separator 20 is a monosodium L-glutamate solution tank 22 for storing the monosodium L-glutamate solution separated by the gas/liquid separator 20, and then supplied from the outlet side of the monosodium L-glutamate solution tank 22 to the monosodium L-glutamate crystal production operation by a feed pump 23. In order to prepare an L-glutamic acid solution by adding a monosodium L-glutamate solution to crystals of L-glutamic acid, a monosodium L-glutamate solution supply line from the outlet side of the monosodium L-glutamate solution tank 22 is connected to the upper side of the L-glutamic acid supply tank 18 via a feed pump 24 so as to store a monosodium L-glutamate solution therein.
High purity CO recovered from gas/liquid separator 202Is connected to liquid CO by a blower 212In the preparation operation.
Example 1: (1) absorbing CO in waste gas discharged in the fermentation process of L-glutamic acid2Method (2)
3.6kg of soda ash crystals were dissolved in 16.4kg of water to obtain 20kg of a 18 wt% soda ash water solution, which was used as CO2Absorbing the liquid. Then the glutamic acid is fermented to produce CO-containing2The exhaust gas was passed continuously through a packed column (packing: Tellerette, trade name, available from Nitttetsu chemical engineering Co., Ltd.) having a diameter of 100mm and a length of 1000mm, which contained a soda ash aqueous solution circulating under the following conditions, CO in the exhaust gas2Where the batch is absorbed.
CO2Temperature of the absorption liquid: 25 deg.C
CO2Circulating flow rate of the absorption liquid: 0.7m3/h
Temperature of exhaust gas: 25 deg.C
Exhaust gas flow rate: 6Nm3/h
CO in exhaust gas2The concentration of (a): 5-10% (volume)
As a result, CO2In the column at a molar ratio of 0.27 to 0.54mol-CO2Velocity absorption per hour. And CO at the beginning2After 9 hours of absorption sodium bicarbonate crystals were observed.
Example 2: (2) absorbing CO in waste gas discharged in the fermentation process ofL-glutamic acid2Method (2)
An operating procedure similar to example 1 was carried out batchwise with the same soda grey water solution as in example 1, except that the CO was changed2The temperature of the absorption liquid and the exhaust gas.
CO2Temperature of the absorption liquid: 60 deg.C
CO2Circulating flow rate of the absorption liquid: 0.7m3/h
Temperature of exhaust gas: 60 deg.C
Exhaust gas flow rate: 6Nm3/h
CO in exhaust gas2The concentration of (a): 5-10% (volume)
As a result, CO was noted2The absorption rate of (A) is increased to 0.65-0.93mol-CO2H and the higher the operating temperature, CO2Absorption ofThe greater the speed. As a result, sodium bicarbonate crystals were formed in a large amount.
Example 3: (3) absorbing CO in waste gas discharged in the fermentation process of L-glutamic acid2Method (2)
An operation analogous to example 2 was carried out intermittently for 24 hours with the same soda grey water solution as in example 1.
CO2Temperature of the absorption liquid: 60 deg.C
CO2Circulating flow rate of the absorption liquid: 0.7m3/h
Temperature of exhaust gas: 60 deg.C
Exhaust gas flow rate: 6Nm3/h
CO in exhaust gas2The concentration of (a): 5-10% (volume)
The following reaction took place in the solution, and 20.7kg of sodium bicarbonate slurry containing 3.4kg of sodium bicarbonate was finally obtained.
The sodium bicarbonate crystals formed were separated from the slurry using a buchner funnel and dried to give 2.7kg of sodium bicarbonate crystals.
Example 4: (1) CO recovery in monosodium L-glutamate production operations2Method (2)
6.3kg of L-glutamic acid crystals containing 25% by weight of crystal water were separated from the fermentation medium by a conventional method. 2.7kg of sodium bicarbonate crystals were mixed with 5kg of water to make 7.7kg of a 35 wt% sodium bicarbonate slurry. The L-glutamic acid crystals were placed in a closed vessel equipped with a stirring device, and then a sodium hydrogencarbonate slurry was added thereto at a flow rate of 0.1kg/min while maintaining the liquid temperature at 30 ℃ to conduct the following reaction.
Collecting CO generated by the reaction by a gas collecting pipe2. As a result, 12.5kg of a solution containing 5.4kg of monosodium L-glutamate was obtained, while 32mol (0.78 m at 25 ℃ C., 1 atm) was recovered3)CO2A gas.
Example 5: (2) CO recovery in monosodium L-glutamate production operations2Method (2)
6.3kg of L-glutamic acid crystals containing 25% by weight of crystal water were separated from the fermentation medium by a conventional method. 1.7kg of soda ash crystals were mixed with 6.8kg of water to make 8.5kg of a 20 wt% soda ash water solution. The L-glutamic acid crystals were placed in a closed vessel equipped with a stirring device, and then a soda ash aqueous solution was added thereto at a flow rate of 0.1kg/min while maintaining the liquid temperature at 30 ℃to conduct the following reaction.
Collecting CO generated by the reaction by a gas collecting pipe2. As a result, 14.0kg of a solution containing 5.4kg of monosodium L-glutamate was obtained, while 16mol (0.39 m at 25 ℃ C., 1 atm) was recovered3)CO2A gas.
As described above, according to the present invention, CO contained in a low concentration in an exhaust gas discharged from a fermentation process of L-glutamic acid which has been hitherto discharged into the atmosphere2Selectively trapped in the form of an alkaline carbonate and then incorporated into a process for producing L-glutamic acid which requires an alkali as a neutralizing agent, not only can produce a monobasic salt of L-glutamic acid but also can form CO which can be recovered at a high concentration2By-products for use as liquid CO2And (4) source.
Brief description of the drawings
FIG. 1 is a flow diagram illustrating one embodiment of the present invention.
FIG. 2 is a flow diagram illustrating one embodiment of the present invention.
The corresponding symbols in fig. 1 and 2 are as follows:
a: containing CO2Exhaust gas supply line of
B: soda ash water solution supply line
1: l-glutamic acid fermentation tank
2: smoke separator
3: cleaning tower
4: blower fan
5: heat exchanger
6：CO2Absorption tower
7：CO2Absorption tower
8: sodium bicarbonate settling tank
9: circulating pump
10: sodium bicarbonate supply tank
11: feed pump
12: feed pump
13: separator
14: sodium bicarbonate slurry tank
15: sodium bicarbonate mother liquor tank
16: feed pump
17: feed pump
18: l-glutamic acid supply tank
19: l-glutamic acid neutralizing tower
20: gas/liquid separator
21: blower fan
22: l-monosodium glutamate solution tank
23: feed pump
24: feed pump
Claims (4)
1. A method for recovering carbon dioxide from L-glutamic acid fermentation, comprising the steps of:
(a) CO-containing discharged from L-glutamic acid fermentation process2The waste gas is blown into soda ash water solution or sodium hydroxide water solution to prepare sodium bicarbonate or sodium carbonate,
(b) allowing the obtained sodium bicarbonate or sodium carbonate to act on L-glutamic acid separated from the L-glutamic acid fermentation medium in an aqueous medium, and
(c) recovery of high purity CO formed as a by-product2And preparing monosodium L-glutamate.
2. Themethod for recovering carbon dioxide as claimed in claim 1, wherein the sodium bicarbonate is prepared by blowing carbon dioxide discharged during the fermentation of L-glutamic acid into 5-30 wt% soda grey water solution at a temperature of room temperature to 70 ℃.
3. The method for recovering carbon dioxide as claimed in claim 1, wherein the sodium hydrogencarbonate is allowed to act as a 24 to 42 wt% aqueous slurry at a temperature of from room temperature to 70 ℃ to L-glutamic acid.
4. The method for recovering carbon dioxide as claimed in claim 1, wherein the sodium carbonate acts on the L-glutamic acid in the form of a 15-32 wt% aqueous solution at a temperature of room temperature to 70 ℃.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP10047291A JPH11243985A (en) | 1998-02-27 | 1998-02-27 | Recovery of carbon dioxide in fermentation of l-glutamic acid |
| JP47291/1998 | 1998-02-27 | ||
| JP47291/98 | 1998-02-27 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1235931A CN1235931A (en) | 1999-11-24 |
| CN1156392C true CN1156392C (en) | 2004-07-07 |
Family
ID=12771189
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB991030591A Expired - Lifetime CN1156392C (en) | 1998-02-27 | 1999-02-27 | Process for recovering carbon dioxide in glutamic acid fermentation |
Country Status (5)
| Country | Link |
|---|---|
| JP (1) | JPH11243985A (en) |
| CN (1) | CN1156392C (en) |
| BR (1) | BR9900794A (en) |
| ID (1) | ID23629A (en) |
| MY (1) | MY118894A (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BR0100483B1 (en) * | 2000-02-10 | 2009-01-13 | process for the production of carbon dioxide. | |
| JP2005000827A (en) * | 2003-06-12 | 2005-01-06 | Toshiba Corp | Apparatus and method for recovering carbon dioxide |
| US7727374B2 (en) * | 2004-09-23 | 2010-06-01 | Skyonic Corporation | Removing carbon dioxide from waste streams through co-generation of carbonate and/or bicarbonate minerals |
| FR2885900B1 (en) * | 2005-05-20 | 2009-02-13 | Omya Development Ag | MINERAL MATERIALS CONTAINING CARBONATE WITH REDUCED FOSSIL FUEL CELL CARBONIC GAS EMISSION AT THE TIME OF THEIR DECOMPOSITIONS AND THEIR SYNTHESIS PROCESS AND USES THEREOF. |
| CA2564590C (en) | 2006-10-19 | 2010-05-11 | Bitmin Resources Inc. | Method for treating a process water to obtain carbon dioxide therefrom |
| JP5934928B2 (en) * | 2012-09-27 | 2016-06-15 | パナソニックＩｐマネジメント株式会社 | Carbon dioxide production equipment |
| CN103071380B (en) * | 2013-01-30 | 2015-09-09 | 杭州森井大气环境科技有限公司 | A kind of method of collecting carbonic anhydride and pyrolysis |
| CN107055734A (en) * | 2017-05-31 | 2017-08-18 | 燕京啤酒(桂林漓泉)股份有限公司 | The method and device of sewage disposal system pH value is adjusted using beer waste gas |
| CN115212710A (en) * | 2022-07-22 | 2022-10-21 | 碳索(杭州)能源环境科技有限公司 | Is suitable for ultralow-concentration CO 2 Carbon capture system of flue gas |
-
1998
- 1998-02-27 JP JP10047291A patent/JPH11243985A/en active Pending
-
1999
- 1999-02-24 BR BR9900794-0A patent/BR9900794A/en not_active Application Discontinuation
- 1999-02-25 MY MYPI99000697A patent/MY118894A/en unknown
- 1999-02-27 CN CNB991030591A patent/CN1156392C/en not_active Expired - Lifetime
- 1999-03-01 ID IDP990169A patent/ID23629A/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| JPH11243985A (en) | 1999-09-14 |
| BR9900794A (en) | 2000-03-28 |
| MY118894A (en) | 2005-02-28 |
| CN1235931A (en) | 1999-11-24 |
| ID23629A (en) | 2000-05-04 |
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