WO2006013918A1 - 酸素ガスおよび窒素ガスの併行分離方法および併行分離システム - Google Patents
酸素ガスおよび窒素ガスの併行分離方法および併行分離システム Download PDFInfo
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- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
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- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B21/00—Nitrogen; Compounds thereof
- C01B21/04—Purification or separation of nitrogen
- C01B21/0405—Purification or separation processes
- C01B21/0433—Physical processing only
- C01B21/0438—Physical processing only by making use of membranes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
- B01D53/229—Integrated processes (Diffusion and at least one other process, e.g. adsorption, absorption)
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- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
- C01B13/02—Preparation of oxygen
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- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
- C01B13/02—Preparation of oxygen
- C01B13/0229—Purification or separation processes
- C01B13/0248—Physical processing only
- C01B13/0251—Physical processing only by making use of membranes
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- C—CHEMISTRY; METALLURGY
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- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
- C01B13/02—Preparation of oxygen
- C01B13/0229—Purification or separation processes
- C01B13/0248—Physical processing only
- C01B13/0259—Physical processing only by adsorption on solids
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B21/00—Nitrogen; Compounds thereof
- C01B21/04—Purification or separation of nitrogen
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B21/00—Nitrogen; Compounds thereof
- C01B21/04—Purification or separation of nitrogen
- C01B21/0405—Purification or separation processes
- C01B21/0433—Physical processing only
- C01B21/045—Physical processing only by adsorption in solids
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/10—Nitrogen
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/12—Oxygen
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/10—Single element gases other than halogens
- B01D2257/102—Nitrogen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40001—Methods relating to additional, e.g. intermediate, treatment of process gas
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2210/00—Purification or separation of specific gases
- C01B2210/0043—Impurity removed
- C01B2210/0046—Nitrogen
Definitions
- the present invention relates to a method and system for separating oxygen gas and nitrogen gas in parallel from a mixed gas containing oxygen and nitrogen (for example, air).
- Oxygen gas and nitrogen gas obtained by aerodynamic separation are used in various applications.
- Oxygen gas is used, for example, for raising the temperature of refuse melting furnaces, ash melting furnaces, glass melting furnaces, improving the combustion efficiency of steelmaking electric furnaces, acid-rich reactions in chemical plants, and oxygen aeration in wastewater treatment equipment.
- nitrogen gas is used, for example, for gas sealing and purging in a garbage melting furnace chemistry plant, for adjusting the atmosphere gas in a heat treatment furnace, and for gas packaging for food packaging.
- Aerodynamic pressure As one of the practical methods for separating oxygen gas and nitrogen gas, the pressure fluctuation adsorption method (PSA method) is known.
- PSA gas separation device including an adsorption tower filled with an adsorbent for preferentially adsorbing a predetermined component is used, and at least an adsorption process and a desorption process are performed in the adsorption tower.
- the In the adsorption process a mixed gas is introduced into the adsorption tower, the easily adsorbed components in the mixed gas are adsorbed on the adsorbent under high pressure conditions, and the gas having the difficultly adsorbed component force is derived.
- the pressure in the tower is lowered to desorb the easily adsorbed component from the adsorbent, and the gas mainly containing the easily adsorbed component is led out from the adsorbing tower.
- the gas mainly containing the easily adsorbed component is led out from the adsorbing tower.
- an adsorbent capable of preferentially adsorbing nitrogen over oxygen and introducing air as a mixed gas into the adsorption tower
- oxygen is led out of the tower as a difficult adsorption component in the adsorption process.
- Nitrogen is adsorbed by the adsorbent as an easily adsorbing component in the adsorption process and led out of the tower in the desorption process.
- the gas concentration and gas of the hard-to-adsorb component gas that passes through the adsorption tower in the adsorption step is larger than the easily-adsorbed component gas that is desorbed in the desorption step and led out of the tower. Stable with respect to quantity. For this reason, in the PSA method, it is easier to acquire the target gas more efficiently by using the difficult-to-adsorb component gas than the easily-adsorbed component gas. Shi Therefore, when oxygen is separated from air by the PSA method, the adsorption tower of the PSA gas separator used is generally filled with a nitrogen adsorbent, and the adsorption tower power is also derived in the adsorption process.
- the oxygen enriched gas is recovered as product gas.
- nitrogen is separated and acquired by the PSA method, generally, an oxygen-adsorbing adsorbent is packed in the adsorption tower, and the nitrogen-enriched gas derived from the adsorption tower force in the adsorption process is the product. It is recovered as gas.
- FIG. 8 shows an oxygen / nitrogen parallel separation system X5, which is an example of a conventional system for separating oxygen and nitrogen in air in parallel.
- the oxygen / nitrogen parallel separation system X5 is equipped with a PSA gas separation device 81, a membrane gas separator 82, a storage tank 83, compressors 84 and 85, and a vacuum pump 86, which are connected via piping. It is connected.
- a plurality of automatic valves (not shown) are provided at predetermined locations in the piping, and when the system is in operation, the flow state of the gas in the system is switched by appropriately selecting the open / close state of each automatic valve.
- the PSA gas separation device 81 includes an adsorption tower (not shown) filled with an adsorbent that preferentially adsorbs nitrogen over oxygen.
- the membrane gas separator 82 has a gas separation membrane 82a for preferentially permeating oxygen.
- Such an oxygen / nitrogen parallel separation system is described in Patent Document 1 below, for example.
- Patent Document 1 Japanese Patent Laid-Open No. 5-253438
- one cycle including the adsorption step and the desorption step is repeated in the adsorption tower of the PS A gas separation device 81 to separate and acquire the oxygen-enriched gas from the air.
- the compressor 84 is operated and air is supplied to the adsorption tower of the PSA gas separation device 81, and in the state where the inside of the tower rises to a predetermined pressure, the easily adsorbed component in the air (mainly (Containing nitrogen) is adsorbed by the adsorbent, and the oxygen-enriched gas is derived from the adsorption tower or the PSA gas separation device 81.
- This oxygen-enriched gas is continuously used for a predetermined application, for example.
- the vacuum pump 86 is activated to In the state where the inside is lowered to a predetermined pressure, the easily adsorbed components (mainly containing nitrogen) are desorbed from the adsorbent in the adsorption tower, and the easily adsorbed components are desorbed together with the oxygen remaining in the tower.
- the gas is discharged outside the tower or outside the PSA gas separator 81.
- the oxygen concentration in the desorption gas tends to gradually decrease with the passage of a relatively high time.
- the oxygen concentration of the desorbed gas from the PSA gas separation device 81 is constantly detected by an oxygen monitor, and the desorbed gas having a relatively high oxygen concentration at the beginning of the desorption process is indicated by the arrow G '. Discarded outside. Then, when the oxygen concentration of the desorption gas has decreased to a predetermined value, the discarding is stopped, the desorption gas is switched to the recovery of the storage tank 83, and the recovery of the desorption gas is started. Such disposal and subsequent recovery of the desorption gas is executed every time the desorption gas is discharged from the PSA gas separation device 81.
- the desorption gas collected in the storage tank 83 is supplied to the membrane gas separator 82 at a predetermined pressure by the operation of the compressor 85, and passes through the gas separation membrane 82a of the membrane gas separator 82. And non-permeate gas that does not permeate. Oxygen in the desorption gas is preferentially permeated through the gas separation membrane 82a, so that nitrogen-enriched gas whose oxygen concentration is reduced and nitrogen purity is increased is passed through the membrane gas separator 82 as a non-permeate gas. Discharged. This non-permeating gas is continuously used for a predetermined application, for example. According to the oxygen / nitrogen combined separation system X5, aerodynamic oxygen-enriched gas and nitrogen-enriched gas are separated and acquired as described above.
- the fluctuation of the driving force results in fluctuation of oxygen permeation amount or non-permeation amount of oxygen with respect to the gas separation membrane 82a. Therefore, the non-permeation gas (nitrogen-enriched gas) discharged from the membrane gas separator 82 is changed. The amount will change. Therefore, in the oxygen / nitrogen parallel separation system X5, all the desorbed gas from the PSA gas separation device 81 is stored in the storage tank 83. If it is not recovered once and is continuously supplied to the membrane gas separator 82, the nitrogen-enriched gas obtained as a non-permeate gas will be appropriately used as an inert gas because the supply amount is unstable. There are cases where it cannot be used.
- the disposal and recovery of the desorbed gas from the PSA gas separation device 81 are switched at a predetermined timing.
- the desorption gas in a predetermined oxygen concentration region ie, nitrogen concentration region
- the desorption gas having a substantially constant oxygen concentration ie, substantially constant nitrogen purity
- the fluctuation of the oxygen partial pressure (reduced oxygen concentration) of the desorption gas supplied to the membrane gas separator 82 is small, the fluctuation of the oxygen permeation amount with respect to the gas separation membrane 82a is small.
- a non-permeate gas (nitrogen-enriched gas) force S is discharged at a substantially constant flow rate.
- the switching line configuration and the storage tank 83 for separating the flow of desorbed gas from the PSA gas separator 81 to the membrane gas separator 82 prevent the operation of separation and acquisition of nitrogen-enriched gas. This is not preferable because it causes continuous system complexity. In addition, such a switching line configuration and storage tank 83 are not preferable because they lead to an increase in the size of the system. Further, the longer the period during which the flow of the desorbed gas from the PSA gas separation device 81 to the membrane gas separator 82 is divided, the larger the storage tank 83 needs a larger capacity.
- the desorption gas discharged in the initial and middle periods of 20 seconds from the start of the desorption process (the oxygen concentration is relatively high and the nitrogen purity is (Relatively low) is discarded outside the system as indicated by arrow G 'and desorbed gas (oxygen concentration is relatively low and nitrogen purity is relatively low) discharged at the end of desorption for 20 to 30 seconds from the start of the desorption process.
- the desorption gas is not stored in the storage tank 83 for 20 seconds in the initial and middle stages of the desorption, so that gas is supplied from the storage tank 83 to the membrane gas separator 82 during this period.
- the present invention has been conceived under such circumstances.
- the PSA gas separation device separates and obtains high-purity oxygen gas from the oxygen / nitrogen mixed gas force, and the PSA gas separation device.
- Power It is an object to provide a method and system capable of continuously and efficiently separating and obtaining high-purity nitrogen gas from continuously supplied desorption gas.
- a mixed gas power containing oxygen and nitrogen and a method for separating oxygen gas and nitrogen gas in parallel.
- This parallel separation method includes a pressure fluctuation adsorption gas separation step and a membrane gas separation step.
- a pressure fluctuation adsorption gas separation process a pressure fluctuation adsorption gas separation method using an adsorption tower filled with an adsorbent for preferentially adsorbing nitrogen is used.
- a mixed gas is introduced into the adsorption tower, nitrogen in the mixed gas is adsorbed by the adsorbent, the adsorption tower force oxygen-enriched gas is derived, and the inside of the adsorption tower is at a relatively low pressure.
- nitrogen is desorbed from the adsorbent, and oxygen-containing desorption gas containing oxygen remaining in the adsorption tower and the nitrogen is led out from the adsorption tower.
- the permeation side of the gas separation membrane for preferentially permeating oxygen is reduced to a pressure lower than atmospheric pressure, and the gas separation membrane allows oxygen-containing desorbed gas to pass through the gas separation membrane. Separate into permeate gas and permeate non-permeate nitrogen enriched gas.
- the parallel separation method further includes a compression step for compressing the oxygen-containing desorption gas before the oxygen-containing desorption gas is subjected to the membrane gas separation step.
- a compression step for compressing the oxygen-containing desorption gas before the oxygen-containing desorption gas is subjected to the membrane gas separation step.
- the adsorption tower force in the pressure fluctuation adsorption gas separation step and the pressure reduction in the adsorption tower when deriving the oxygen-containing desorption gas and the pressure reduction on the permeate side in the membrane gas separation step are a single This is realized by the decompression means.
- a part of the oxygen-containing desorption gas is introduced to the permeation side of the gas separation membrane without passing through the gas separation membrane.
- a mixed gas power containing oxygen and nitrogen is provided.
- This parallel separation system includes a pressure fluctuation adsorption gas separation device, a membrane gas separator, and a decompression means.
- the pressure fluctuation adsorption gas separation device has an adsorption tower filled with an adsorbent for preferentially adsorbing nitrogen, and the inside of the adsorption tower is obtained by a pressure fluctuation adsorption gas separation method performed using the adsorption tower.
- a mixed gas is introduced into the adsorption tower, nitrogen in the mixed gas is adsorbed by the adsorbent, the adsorption tower force oxygen-enriched gas is derived, and the inside of the adsorption tower is relatively In this state, nitrogen is desorbed from the adsorbent at a low pressure, and oxygen-containing desorbed gas containing oxygen remaining in the adsorption tower and the nitrogen is led out from the adsorption tower.
- the membrane gas separator has a gas separation membrane for preferentially permeating oxygen, and separates the oxygen-containing desorption gas into a permeate gas that permeates the gas separation membrane and a non-permeate nitrogen-enriched gas that does not permeate. It is for deriving.
- the depressurizing means is for depressurizing the permeation side of the gas separation membrane of the membrane gas separator to a pressure lower than atmospheric pressure. According to the parallel separation system, the method of the first aspect of the present invention can be appropriately performed.
- the parallel separation system further includes compression means for compressing the oxygen-containing desorption gas before the oxygen-containing desorption gas is supplied to the membrane gas separator.
- the depressurization means also functions as a means for depressurizing the inside of the adsorption tower when the oxygen-containing desorption gas is derived from the adsorption tower of the pressure fluctuation adsorption gas separation apparatus.
- the parallel separation system further includes a bypass unit for bypassing a part of the oxygen-containing desorption gas and introducing it into the permeation side of the gas separation membrane without passing through the gas separation membrane.
- FIG. 1 shows a schematic configuration of an oxygen / nitrogen parallel separation system according to a first embodiment of the present invention.
- FIG. 2 An example of the pressure change with time for the oxygen-containing desorption gas discharged from the pressure fluctuation adsorption gas separation device shown in FIG.
- FIG. 3 Oxygen of the present invention carried out using the oxygen-nitrogen parallel separation system shown in Fig. 1 Regarding the membrane gas separation process in the nitrogen parallel separation method, as shown in Fig. 2, when the oxygen-containing desorption gas is discharged from the PSA gas separation device, the desorption initial stage (at the start of the desorption process) and the desorption middle period (10 seconds have elapsed) ), And a table summarizing examples of changes in physical quantities over the end of desorption (when 30 seconds have passed).
- FIG. 4 shows the membrane gas separation process performed without depressurizing the permeation side of the gas separation membrane in the membrane gas separator of the oxygen / nitrogen parallel separation system shown in Fig. 1.
- FIG. 5 shows a schematic configuration of an oxygen / nitrogen parallel separation system according to a second embodiment of the present invention.
- FIG. 6 shows a schematic configuration of an oxygen / nitrogen parallel separation system according to a third embodiment of the present invention.
- FIG. 7 shows a schematic configuration of an oxygen / nitrogen parallel separation system according to a fourth embodiment of the present invention.
- FIG. 8 A schematic configuration of a conventional oxygen / nitrogen separation system is shown.
- FIG. 1 shows an oxygen / nitrogen parallel separation system XI according to a first embodiment of the present invention.
- Oxygen / nitrogen parallel separation system XI consists of pressure fluctuation adsorption (PSA) gas separation device 1, membrane gas separator 2, raw material gas supply device 3, pumps 4, 5, silencer 6, and compressor 7 And a gas-liquid separator 8, an oxygen concentration control mechanism 9, and a pipe connecting them, separating oxygen-enriched gas and nitrogen-enriched gas from air (oxygen-nitrogen-containing source gas) in parallel. It may be configured to implement an oxygen-nitrogen parallel separation method including a pressure fluctuation adsorption gas separation process, a compression process, and a membrane gas separation process.
- PSA pressure fluctuation adsorption
- the PSA gas separation device 1 is provided with at least one adsorption tower (not shown) filled with an adsorbent mainly for preferentially adsorbing nitrogen, and a pressure fluctuation adsorption method performed using the adsorption tower.
- An oxygen-enriched gas can be extracted from an oxygen / nitrogen-containing source gas (air in this embodiment) by a gas separation method.
- As the adsorbent packed in the adsorption tower Li-X type Olite molecular sieve, Ca-X type zeolite molecular sieve, Ca-A type zeolite molecular sieve, and the like can be employed.
- a single adsorption tower can be filled with one type of adsorbent or with multiple types of adsorbents.
- the pressure fluctuation adsorption gas separation method executed by the PSA gas separation apparatus 1 one cycle including an adsorption step, a desorption step, and a regeneration step is repeated for a single adsorption tower.
- air is introduced into an adsorption tower having a predetermined high pressure in the tower to adsorb nitrogen and other components (carbon dioxide, moisture, etc.) in the raw material gas to the adsorbent, and the adsorption Column power is also a process for deriving oxygen-enriched gas.
- the desorption step is a step for depressurizing the inside of the adsorption tower to desorb nitrogen from the adsorbent and discharging the nitrogen out of the tower.
- the regeneration step is a step for recovering the adsorption performance of the adsorbent to nitrogen by passing a cleaning gas, for example, through which the adsorption tower is provided in the second adsorption step.
- a cleaning gas for example, through which the adsorption tower is provided in the second adsorption step.
- a PSA gas separation device 1 a known PSA oxygen separation device can be used.
- the membrane gas separator 2 has an inlet 2a and outlets 2b, 2c, and includes a gas separation membrane 2A that preferentially permeates oxygen.
- a predetermined gas passage (specifically not shown) is provided inside the membrane gas separator 2, and the inlet 2a and outlet 2b communicate with each other through a part of the gas passage.
- a gas separation membrane 2A is disposed at a predetermined location in the gas flow path from the inlet 2a to the outlet 2c.
- the gas separation membrane 2A is a porous resin membrane made of, for example, polyimide or polysulfone. As such a porous resin membrane, Upilex PT (manufactured by Ube Industries, Ltd.) can be used.
- the source gas supply device 3 is for supplying air, which is an oxygen / nitrogen-containing source gas, to the adsorption tower of the PSA gas separation device 1 and is, for example, an air blower.
- the pump 4 is for sucking and depressurizing the inside of the adsorption tower of the PSA gas separation apparatus 1, and is, for example, a vacuum pump.
- the pump 5 is for sucking and depressurizing the permeation side of the gas separation membrane 2A in the membrane gas separator 2 (the gas flow path to the gas separation membrane 2A force outlet 2c).
- the vacuum pump It is.
- the silencer 6 guides a part of the gas from the pump 4 to the compressor 7 and discharges the remaining gas from the pump 4 to the outside of the system.
- the silencer 6 compresses the gas from the pump 4.
- On machine 7 It has a gas flow path for guiding and a gas flow path for discharging the gas from the pump 4 to the outside of the system while silencing.
- the compressor 7 is for compressing the gas that has passed through the silencer 6 and supplying the compressed gas to the gas-liquid separator 8. Further, the gas-liquid separator 8 has a discharge port 8a, and is for separating the water contained in the gas sent from the compressor 7 from the gas force. The discharge port 8 a is for discharging the water collected in the gas-liquid separator 8 to the outside of the gas-liquid separator 8.
- the oxygen concentration control mechanism 9 is a gas that flows through the pipe L1 with the force of the oxygen sensor 9a and the automatic valve 9b installed in the pipe L1 connected to the outlet 2b of the membrane gas separator 2.
- the oxygen concentration of the gas is adjusted to a desired value by adjusting the flow rate of the gas (that is, the amount of gas that does not permeate the gas separation membrane 2A of the membrane gas separator 2) according to the oxygen concentration of the gas. It is for doing.
- the oxygen sensor 9a is for constantly detecting the oxygen concentration of the gas flowing through the pipe L1.
- the oxygen concentration control mechanism 9 is configured such that the opening degree of the automatic valve 9b is adjusted as desired according to the detection result of the oxygen sensor 9a.
- air is subjected to a pressure fluctuation adsorption gas separation process. Specifically, in the PSA gas separation apparatus 1, one cycle including an adsorption process, a desorption process, and a regeneration process is repeated for each adsorption tower by the pressure fluctuation adsorption gas separation method.
- the adsorption step air is introduced into the adsorption tower in which the inside of the tower is in a predetermined high pressure state.
- nitrogen and other components (carbon dioxide, moisture, etc.) contained in the air are adsorbed and removed by the adsorbent, and high-purity oxygen gas (oxygen-enriched gas) is led out of the tower. .
- This high-purity oxygen gas is taken out of the oxygen / nitrogen parallel separation system XI through a predetermined pipe.
- the operation of the pump 4 depressurizes the adsorption tower to desorb the adsorbent power nitrogen and other components, and the oxygen-containing desorption gas containing oxygen remaining in the tower and the desorption component is converted into the tower. It is discharged outside or outside the PSA gas separator 1.
- Adsorption tower force in the desorption process A graph showing an example of time change of pressure in the oxygen-containing desorption gas discharged, Figure 2 shows. In the graph of FIG. 2, the horizontal axis represents the desorption time in the adsorption tower (elapsed time from the start of the desorption process), and the vertical axis represents the desorption pressure (pressure of the oxygen-containing desorption gas).
- the pressure at the start of the desorption process is atmospheric pressure
- the pressure after 10 seconds is 0.0611 MPa
- the pressure after 30 seconds is 0.0332 MPa.
- FIG. 2 also shows the oxygen concentration (oxygen volume ratio) of the oxygen-containing desorption gas at the start of the desorption process, at the time of 10 seconds, and at the time of 30 seconds.
- the adsorption performance of the adsorbent mainly to nitrogen is recovered by flowing a cleaning gas into the tower.
- the adsorption described above is performed again in the adsorption tower after the regeneration process.
- the PSA gas separation apparatus 1 by performing the pressure fluctuation adsorption gas separation process as described above, high-purity oxygen gas is taken out and oxygen-containing desorption gas is taken out.
- the high-purity oxygen gas is stored in a predetermined tank or a predetermined tank, for example, for continuous use in a predetermined application.
- the adsorption tower force in the desorption process is also sent to the silencer 6 through a predetermined pipe and the pump 4 after the oxygen-containing desorption gas discharged out of the PSA gas separation device 1.
- a part of the oxygen-containing desorption gas passes through the silencer 6 and reaches the compressor 7.
- the remainder of the oxygen-containing desorption gas is exhausted out of the system by the silencer 6.
- the oxygen-containing desorption gas that has passed through the silencer 6 is compressed by the compressor 7 (compression process), and is supplied to the membrane gas separator 2 via the gas-liquid separator 8.
- the oxygen-containing desorption gas is compressed by the compressor 7 to a pressure of 0.6 MPa or more.
- moisture is separated from the oxygen-containing desorption gas. This moisture is discharged from the gas-liquid separator 8 to the outside through the discharge port 8a.
- the oxygen-containing desorption gas is subjected to a membrane gas separation step. Specifically, the oxygen-containing desorption gas G 1 introduced into the membrane gas separator 2 from the inlet 2a is caused by the gas separation membrane 2A disposed in the gas flow path of the membrane gas separator 2. The gas is separated into a permeate gas G2 that permeates the gas separation membrane 2A and a non-permeate gas G3 that does not permeate.
- the permeate gas G2 is an oxygen-enriched gas whose oxygen concentration is increased based on the permeation characteristics of the gas separation membrane 2A, and the non-permeate gas G3 has a high nitrogen concentration based on the permeation characteristics of the gas separation membrane 2A. High purity nitrogen gas (nitrogen-enriched gas) produced.
- the permeation side of the gas separation membrane 2A is depressurized to a pressure lower than the atmospheric pressure by the operation of the pump 5.
- the reduced pressure by the pump 5 is, for example, 0.02 to 0.05 MPa.
- the permeated gas G2 is led out of the membrane gas separator 2 from the outlet 2c, and then discharged out of the system through the pump 5.
- the oxygen concentration control mechanism 9 operates to directly adjust the amount of non-permeate gas, and the oxygen concentration of the non-permeate gas G3 is kept constant.
- the oxygen sensor 9a of the oxygen concentration control mechanism 9 constantly detects the oxygen concentration of the non-permeate gas G3 that is led out of the membrane gas separator 2 through the outlet 2b and passes through the pipe L1.
- the opening degree of the automatic valve 9b is reduced, the flow rate of the non-permeate gas G3 passing through the pipe L1, and hence the membrane gas separation in the membrane gas separator 2
- the amount of non-permeate gas G3 generated in the process (the amount generated per unit time) is reduced.
- the opening degree of the automatic valve 9b is increased, the flow rate of the non-permeate gas G3 passing through the pipe L1, and thus the membrane gas in the membrane gas separator 2 is increased.
- the amount of non-permeate gas G3 generated in the separation process is increased. Since the purity and oxygen concentration of the non-permeate gas G3 in the membrane gas separation process can vary depending on the amount of the non-permeate gas G3 generated, the non-permeate gas G3 can be adjusted by adjusting the flow rate of the non-permeate gas G3.
- the oxygen concentration of the gas G3 can be controlled.
- the membrane gas separator 2 by performing the membrane gas separation process as described above, high-purity nitrogen gas is taken out while the oxygen concentration is controlled.
- This high-purity nitrogen gas is continuously used for a predetermined application, for example, or stored in a predetermined tank.
- high-purity oxygen gas and high-purity nitrogen gas can be separated from air in parallel as described above.
- Oxygen / nitrogen combined separation system The oxygen / nitrogen combined separation method using XI! In the first place, the adsorption tower power of the PSA gas separation device 1 in which the pressure fluctuation adsorption gas separation process is performed is discharged and subjected to the membrane gas separation process in the membrane gas separator 2. Partial pressure (or oxygen concentration expressed as the amount of substance per volume) and the oxygen-containing desorption gas G1 Is separated by the gas separation membrane 2A, and the permeation side of the gas separation membrane 2A is less than atmospheric pressure with respect to the oxygen partial pressure of the permeation gas G2 (3 ⁇ 4V, and the oxygen concentration expressed by the amount of substance per volume). By reducing the pressure to a desired pressure, a sufficient difference can be provided.
- the compression process in the compressor 7 also provides a sufficient difference between the oxygen partial pressure of the oxygen-containing desorption gas G1 from the adsorption tower and the oxygen partial pressure of the permeated gas G2 separated by the gas separation membrane 2A. Donate to Even when the oxygen partial pressure (3 ⁇ 4V, oxygen concentration) of the oxygen-containing desorption gas G1 fluctuates, by providing a sufficient difference between the oxygen partial pressures, oxygen permeation through the gas separation membrane 2A can be achieved. Sufficient driving force can be ensured, and the fluctuation ratio of the driving force can be suppressed, so that a sufficient amount of oxygen permeating the gas separation membrane 2A can be obtained and the permeating amount can be reduced. Fluctuations can be suppressed.
- the nitrogen permeation amount in the gas separation membrane 2A increases, the nitrogen permeation amount in the gas separation membrane 2A tends to be smaller. Therefore, the non-permeate gas (higher in the membrane gas separation step in the membrane gas separator 2) Purity nitrogen gas) G3 generation tends to be large.
- the smaller the fluctuation ratio of the oxygen permeation amount in the gas separation membrane 2A the smaller the fluctuation ratio of the generation amount of the non-permeating gas (high purity nitrogen gas) G3 in the membrane gas separation process.
- the PSA gas separation device 1 separates and acquires aerodynamic high-purity oxygen gas and continuously supplies oxygen-containing desorption gas power high-purity nitrogen gas supplied from the PSA gas separation device 1. It is possible to separate and acquire efficiently. Therefore, according to this parallel separation method, there is no need to use a tank or the like for temporarily storing oxygen-containing desorbed gas from the PSA gas separation device 1!
- the pressure is P (MPa)
- the oxygen concentration volume ratio of oxygen
- the gas Let the amount be Q (Nm 3 / hour)
- the pressure (that is, the pressure on the permeate side of the gas separation membrane 2A) is P (MPa)
- the oxygen concentration is X
- the gas amount is Q (Nm 3 / hour) and membrane type
- Equation (1) represents the gas amount balance
- Equation (2) represents the oxygen amount balance
- Equation (3) represents the oxygen permeation characteristic of the gas separation membrane 2A.
- Q2xX2 Kx-x (PixXi-P 2 xX 2 )
- Upilex PT (Ube Industries, Ltd.), which is a polyimide porous membrane, is used as the gas separation membrane 2A.
- the K (SZL) value in equation (3) is set to 186, and the desorption process is started from the PSA gas separator 1 as shown in Figure 2. At that time (initial desorption), oxygen-containing desorption gas with an oxygen concentration (X) of 20.6% was compressed to 0.79 MPa (P) by the compressor 7
- the pressure on the permeate side is reduced to 0.0332 MPa (P), and the non-permeate gas with a residual oxygen concentration (X) of 1%
- the oxygen concentration (X) of the oxygen-containing desorption gas is 10.0% in the middle of desorption
- the PSA gas separation device 1 as shown in FIG. X, Q and Q at the beginning, middle and end of desorption when gas is discharged
- the amount of change (or fluctuation ratio) in 3 is also small. From the above, it can be understood that a large amount of high-purity nitrogen gas can be supplied at a stable flow rate by the membrane gas separation process in the oxygen / nitrogen parallel separation system XI.
- FIG. 5 shows an oxygen / nitrogen parallel separation system X2 according to a second embodiment of the present invention.
- the oxygen / nitrogen parallel separation system X2 is not equipped with a pump 5, and is provided with a pipe L2 that joins the outlet 2c of the membrane gas separator 2 and the suction side of the pump 4. Different from parallel separation system XI.
- the pump 4 in the oxygen / nitrogen concurrent separation system X2 functions as a decompression means for decompressing the inside of the adsorption tower of the PSA gas separator 1, and in the membrane gas separator 2 It also functions as a decompression means for decompressing the permeation side of the gas separation membrane 2A.
- Such a configuration is suitable for building a compact system.
- the PSA gas separation device 1 When the oxygen / nitrogen parallel separation system X2 is in operation, the PSA gas separation device 1 performs the pressure fluctuation adsorption gas separation process in the same manner as described above for the oxygen / nitrogen parallel separation system XI. As a result, high-purity oxygen gas and oxygen-containing desorption gas are taken out. Further, in the membrane gas separator 2, except for the depressurization method on the permeate side of the gas separation membrane 2A, the membrane gas separation process is performed in the same manner as described above for the oxygen / nitrogen parallel separation system XI. Purity nitrogen gas is removed. In the membrane gas separation step in the present embodiment, the permeation side of the gas separation membrane 2A is depressurized to a pressure lower than atmospheric pressure by the operation of the pump 4. For example, by operating the pump 4, the inside of the adsorption tower in the adsorption process is sucked and depressurized, and at the same time, the permeation side of the gas separation membrane 2A is depressurized.
- the oxygen / nitrogen parallel separation method using the oxygen / nitrogen parallel separation system X2 it is possible to supply high-purity oxygen gas in substantially the same manner as with the oxygen / nitrogen parallel separation system XI. In other words, a large amount of high-purity nitrogen gas can be supplied at a stable flow rate.
- FIG. 6 shows an oxygen / nitrogen parallel separation system X3 according to a third embodiment of the present invention.
- the oxygen / nitrogen parallel separation system X3 is composed of an inlet 2d provided on the permeate side of the gas separation membrane 2A in the membrane gas separator 2, an upstream side of the compressor 7, and an inlet 2d of the membrane gas separator 2. This is different from the oxygen / nitrogen combined separation system X2 in that it further includes a pipe L3 for connecting and a flow rate adjusting valve 10 provided in the pipe L3.
- Pipe L3 in the oxygen / nitrogen parallel separation system X3 is one of the oxygen-containing desorption gas discharged from the adsorption tower of the PSA gas separation apparatus 1 in the desorption process and flowing toward the membrane gas separator 2. This is a part that functions as a bypass means for bypassing the gas separation membrane 2A without passing through it and introducing it to the permeate side of the gas separation membrane 2A.
- the PSA gas separation device 1 performs the pressure fluctuation adsorption gas separation process in the same manner as described above for the oxygen / nitrogen combined separation system XI. As a result, high-purity oxygen gas and oxygen-containing desorption gas are taken out.
- the adsorption tower force of the PSA gas separator 1 is discharged and the membrane gas separation is performed.
- a part of the oxygen-containing desorption gas directed to the vessel 2 is introduced to the permeate side of the gas separation membrane 2A through the pipe L3 and the inlet 2d. That is, a part of the oxygen-containing desorption gas (hereinafter referred to as oxygen partial pressure reducing gas G4) bypasses the gas separation membrane 2A and is supplied to the permeate side of the gas separation membrane 2A.
- oxygen partial pressure reducing gas G4 a part of the oxygen-containing desorption gas
- the supply of the oxygen partial pressure reducing gas G4 to the permeation side of the gas separation membrane 2A via the pipe L3 is performed continuously and stably. Is called. Further, the supply amount of the oxygen partial pressure reducing gas G4 to the permeation side of the gas separation membrane 2A is adjusted by the flow rate adjusting valve 10 as desired.
- a relatively high oxygen concentration permeate gas G2 that permeates the gas separation membrane 2A and a relatively low oxygen concentration that bypasses the gas separation membrane 2A without passing through it. and oxygen partial pressure reduction gas G4 are merged (hereinafter, the merged gas that combined gas G 5.) 0
- the oxygen concentration of the combined gas G5 is lower Kunar than the oxygen concentration of the permeate gas G2.
- the oxygen partial pressure of the combined gas G5 is lower than the oxygen partial pressure of the permeated gas G2.
- the permeation side of the gas separation membrane 2A is reduced to a predetermined pressure lower than atmospheric pressure, and the oxygen partial pressure reducing gas G4 is used as the gas.
- the oxygen partial pressure of the oxygen-containing desorption gas G1 from the adsorption tower and the oxygen-containing desorption gas G1 are separated from each other by the gas separation membrane 2A.
- the oxygen partial pressure of the existing gas (the combined gas G5 composed of the permeating gas G2 and the oxygen partial pressure reducing gas G4) can be made larger. This also contributes to increasing the driving force for oxygen permeation in the gas separation membrane 2A and increasing the amount of non-permeating gas (high purity nitrogen gas) G3.
- FIG. 7 shows an oxygen / nitrogen parallel separation system X4 according to a fourth embodiment of the present invention.
- the oxygen / nitrogen parallel separation system X4 is different from the oxygen / nitrogen parallel separation system X3 in that a pipe L4 is provided instead of the pipe L3 and a pressure control valve 11 is further provided.
- the pipe L4 is configured to connect the downstream side of the compressor 7 and the inlet 2d of the membrane gas separator 2 together.
- Pipe L4 is the same as the pipe L3 in the oxygen / nitrogen parallel separation system X3, and the adsorption tower power of the PSA gas separation device 1 in the desorption process is discharged and flows to the membrane gas separator 2 in an oxygen-containing desorption gas. Part of the gas (oxygen partial pressure reducing gas G4) is bypassed without passing through the gas separation membrane 2A and introduced into the permeation side of the gas separation membrane 2A.
- the pipe L4 is provided with a flow regulating valve 10 as in the oxygen / nitrogen parallel separation system X3.
- the pressure control valve 11 is provided between the compressor 7 and the membrane gas separator 2, and is for adjusting the pressure of the oxygen-containing desorption gas G1 introduced into the membrane gas separator 2 as desired. It is.
- the downstream side of the compressor 7 and the inlet 2d of the membrane gas separator 2 are connected by the pipe L4.
- the oxygen partial pressure reducing gas G4 is supplied to the permeate side of the gas separation membrane 2A through the pipe L4.
- the permeated gas G2 having a relatively high oxygen concentration that has permeated through the gas separation membrane 2A and the oxygen component having a relatively low oxygen concentration that has bypassed without passing through the gas separation membrane 2A.
- the pressure reducing gas G4 is merged, the oxygen concentration of the merged gas G5 is lower than the oxygen concentration of the permeate gas G2.
- the permeation side of the gas separation membrane 2A is reduced to a predetermined pressure lower than the atmospheric pressure, the oxygen partial pressure of the combined gas G5 is lower than the oxygen partial pressure of the permeated gas G2.
- the permeation side of the gas separation membrane 2A is reduced to a predetermined pressure lower than atmospheric pressure and the oxygen partial pressure reducing gas G4 is gasified.
- the oxygen partial pressure of the oxygen-containing desorption gas G1 from the adsorption tower and the oxygen-containing desorption gas G1 are separated from each other by the gas separation membrane 2A.
- the oxygen partial pressure of the existing gas (the combined gas G5 composed of the permeating gas G2 and the oxygen partial pressure reducing gas G4) can be made larger. This also contributes to increasing the driving force for oxygen permeation in the gas separation membrane 2A and increasing the amount of non-permeating gas (high purity nitrogen gas) G3.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Analytical Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Separation Of Gases By Adsorption (AREA)
- Oxygen, Ozone, And Oxides In General (AREA)
Abstract
Description
Claims
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KR1020077005076A KR101120992B1 (ko) | 2004-08-05 | 2005-08-04 | 산소 가스 및 질소 가스의 병행 분리방법 및 병행 분리시스템 |
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JP2004228966A JP4538275B2 (ja) | 2004-08-05 | 2004-08-05 | 酸素ガスおよび窒素ガスの併行分離方法および併行分離システム |
JP2004-228966 | 2004-08-05 |
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KR (1) | KR101120992B1 (ja) |
CN (1) | CN100536992C (ja) |
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Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
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WO2007023761A1 (ja) * | 2005-08-22 | 2007-03-01 | Sumitomo Seika Chemicals Co., Ltd. | 酸素ガスおよび窒素ガスの併行分離方法および併行分離システム |
EP4324547A1 (en) * | 2022-08-03 | 2024-02-21 | Hitachi, Ltd. | Gas separation apparatus |
Families Citing this family (9)
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KR100856912B1 (ko) * | 2007-11-13 | 2008-09-05 | 주식회사 와이 에치 씨 | 정제질소 공급장치 |
CN102071963A (zh) * | 2010-12-04 | 2011-05-25 | 北京科技大学 | 一种高原非煤矿井采掘工作面增氧方法及装置 |
CN103007674A (zh) * | 2011-09-27 | 2013-04-03 | 上海弘中实业有限公司 | 基于分子大小排列优先过滤技术和变压吸附制氧技术相结合的复合高浓度制氧机 |
KR102330572B1 (ko) * | 2012-09-28 | 2021-11-25 | 아사히 가세이 케미칼즈 가부시키가이샤 | 내연 기관의 운전 방법 및 공기 공급 장치 |
KR101722045B1 (ko) | 2016-08-26 | 2017-03-31 | 주식회사 엠에스엘 콤프레서 | 용기 상태 검지형 호흡용 공기 충전기 |
JP6851839B2 (ja) * | 2017-01-27 | 2021-03-31 | 大陽日酸株式会社 | 熱回収型酸素窒素供給システム |
JP6860197B2 (ja) * | 2017-02-06 | 2021-04-14 | Vigo Medical株式会社 | 酸素濃縮装置 |
CN108401605B (zh) * | 2018-02-05 | 2020-12-08 | 日照方源机械科技有限公司 | 一种低压种子处理装置 |
CN112021636A (zh) * | 2020-06-22 | 2020-12-04 | 武汉东昌仓贮技术有限公司 | 一种密闭仓的循环脱氧富氮防虫装置及方法 |
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JPH0293282A (ja) * | 1988-09-30 | 1990-04-04 | Hitachi Ltd | 液体窒素及び窒素ガスの製造方法及び装置 |
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JPS61127609A (ja) * | 1984-11-27 | 1986-06-14 | Kobe Steel Ltd | He精製装置 |
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- 2004-08-05 JP JP2004228966A patent/JP4538275B2/ja not_active Expired - Fee Related
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2005
- 2005-08-04 CN CNB2005800264526A patent/CN100536992C/zh active Active
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- 2005-08-04 WO PCT/JP2005/014285 patent/WO2006013918A1/ja active Application Filing
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JPS6391119A (ja) * | 1986-10-01 | 1988-04-21 | ザ・ビーオーシー・グループ・インコーポレーテッド | ガス拡散バリヤーを使用するpsa法および装置 |
JPH0293282A (ja) * | 1988-09-30 | 1990-04-04 | Hitachi Ltd | 液体窒素及び窒素ガスの製造方法及び装置 |
JPH0312307A (ja) * | 1989-06-08 | 1991-01-21 | Nippon Sanso Kk | 空気分離方法 |
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WO2007023761A1 (ja) * | 2005-08-22 | 2007-03-01 | Sumitomo Seika Chemicals Co., Ltd. | 酸素ガスおよび窒素ガスの併行分離方法および併行分離システム |
EP4324547A1 (en) * | 2022-08-03 | 2024-02-21 | Hitachi, Ltd. | Gas separation apparatus |
Also Published As
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CN100536992C (zh) | 2009-09-09 |
TW200618856A (en) | 2006-06-16 |
JP4538275B2 (ja) | 2010-09-08 |
TWI277438B (en) | 2007-04-01 |
KR101120992B1 (ko) | 2012-06-13 |
JP2006043599A (ja) | 2006-02-16 |
CN1993166A (zh) | 2007-07-04 |
KR20070053728A (ko) | 2007-05-25 |
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