Patent Grant
8864960
The present invention relates to a fluorine gas generating apparatus.
As a prior-art fluorine gas generating apparatus, an apparatus which generates fluorine gas by electrolysis using an electrolytic cell is known.
JP2004-43885A discloses a fluorine gas generating apparatus provided with an electrolytic cell for electrolyzing hydrogen fluoride in molten salt containing hydrogen fluoride, generating a product gas mainly containing a fluorine gas in a first gas phase section on an anode side, and generating a byproduct gas mainly containing a hydrogen gas in a second gas phase section on a cathode side.
In this type of fluorine gas generating apparatus, a hydrogen fluoride gas evaporated from the molten salt is mixed in the fluorine gas generated from the anode of the electrolytic cell. Thus, it is necessary to refine the fluorine gas by separating hydrogen fluoride from the gas generated from the anode.
JP2004-39740A discloses a device which separates a fluorine gas component from a component other than the fluorine gas component through cooling using liquid nitrogen or the like by using a difference in boiling points of the both.
Moreover, JP 2004-107761A discloses an apparatus which removes hydrogen fluoride from a fluorine gas generated from an anode by using a hydrogen fluoride adsorption tower filled with a filler of sodium fluoride (NaF) or the like.
In the apparatuses for refining a fluorine gas as described in JP2004-39740A and JP2004-107761A, the components other than the fluorine gas removed as a result of refining have not been used but discharged.
The present invention has been made in view of the above problems and has an object to provide a fluorine gas generating apparatus which can effectively use a component other than a fluorine gas trapped in a process of refining the fluorine gas.
The present invention is a fluorine gas generating apparatus which generates a fluorine gas by electrolyzing hydrogen fluoride in molten salt, including: an electrolytic cell including, above a liquid level of molten salt, a first gas chamber into which a product gas mainly containing the fluorine gas generated at an anode immersed in the molten salt and a second gas chamber which is separated from the first gas chamber and into which a byproduct gas mainly containing a hydrogen gas generated at a cathode immersed in the molten salt; a hydrogen fluoride supply source which retains hydrogen fluoride to be replenished in the electrolytic cell; a refining device which traps a hydrogen fluoride gas evaporated from the molten salt in the electrolytic cell and mixed in the product gas generated from the anode to refine the fluorine gas; and a recovery facility which conveys and recovers the hydrogen fluoride trapped in the refining device in the electrolytic cell or the hydrogen fluoride supply source.
According to the present invention, since hydrogen fluoride trapped in the refining device is recovered in the electrolytic cell or the hydrogen fluoride supply source and reused in order to generate the fluorine gas, hydrogen fluoride which is a component other than the fluorine gas trapped in a process of refining the fluorine gas can be effectively used.
Embodiments of the present invention will be described below by referring to the attached drawings.
A fluorine gas generating apparatus 100 according to a first embodiment of the present invention will be described by referring to
The fluorine gas generating apparatus 100 generates a fluorine gas by electrolysis and supplies the generated fluorine gas to an external device 4. The external device 4 is a semiconductor manufacturing device, for example, and in that case, the fluorine gas is used as a cleaning gas in a manufacturing process of a semiconductor, for example.
The fluorine gas generating apparatus 100 includes an electrolytic cell 1 which generates a fluorine gas by electrolysis, a fluorine gas supply system 2 which supplies the fluorine gas generated from the electrolytic cell 1 to the external device 4, and a byproduct gas treatment system 3 which treats a byproduct gas generated with the generation of the fluorine gas.
First, the electrolytic cell 1 will be described.
The electrolytic cell 1 retains molten salt containing hydrogen fluoride (HF). In this embodiment, a mixture (KF·2HF) of hydrogen fluoride and potassium fluoride (KF) is used as the molten salt.
The inside of the electrolytic cell 1 is divided by a partition wall 6 immersed in the molten salt into an anode chamber 11 and a cathode chamber 12. An anode 7 and a cathode 8 are immersed in the anode chamber 11 and the cathode chamber 12, respectively, and by means of supply of an electric current from a power supply 9 between the anode 7 and the cathode 8, a product gas mainly containing a fluorine gas (F2) is generated at the anode 7, while a byproduct gas mainly containing a hydrogen gas (H2) is generated at the cathode 8. A carbon electrode is used for the anode 7, while soft iron, monel or nickel is used for the cathode 8.
On the liquid level of the molten salt in the electrolytic cell 1, a first gas chamber 11a into which the fluorine gas generated at the anode 7 is introduced and a second gas chamber 12a into which the hydrogen gas generated at the cathode 8 is introduced are divided from each other by a partition wall 6 so that the gases cannot go back and forth between the chambers. As described above, the first gas chamber 11a and the second gas chamber 12a are fully separated by the partition wall 6 in order to prevent reaction by contact between the fluorine gas and the hydrogen gas. On the other hand, the molten salt of the anode chamber 11 and the cathode chamber 12 is not separated by the partition wall 6 but communicates with each other below the partition wall 6.
The melting point of KF·2HF is 71.7° C., and thus, the temperature of the molten salt is adjusted to 90 to 100° C. Hydrogen fluoride evaporated from the molten salt only by a proportion of a vapor pressure is mixed in each of the fluorine gas and the hydrogen gas generated from the anode 7 and the cathode 8 of the electrolytic cell 1. As described above, a hydrogen fluoride gas is contained in each of the fluorine gas generated at the anode 7 and introduced into the first gas chamber 11a and the hydrogen gas generated at the cathode 8 and introduced into the second gas chamber 12a.
In the electrolytic cell 1, a first pressure meter 13 which detects a pressure of the first gas chamber 11a and a second pressure meter 14 which detects a pressure of the second gas chamber 12a are provided. Detection results of the first pressure meter 13 and the second pressure meter 14 are outputted to controllers 10a and 10b.
Subsequently, the fluorine gas supply system 2 will be described.
A first main passage 15 for supplying the fluorine gas to the external device 4 is connected to the first gas chamber 11a.
A first pump 17 which leads the fluorine gas out of the first gas chamber 11a and conveys it is provided in the first main passage 15. A positive-displacement pump such as a bellows pump, a diaphragm pump or the like is used for the first pump 17. A first reflux passage 18 which connects a discharge side and a suction side of the first pump 17 is connected to the first main passage 15. A first pressure regulating valve 19 for returning the fluorine gas discharged from the first pump 17 to the suction side of the first pump 17 is provided in the first reflux passage 18.
The first pressure regulating valve 19 has its opening degree controlled by a signal outputted from the controller 10a. Specifically, the controller 10a controls the opening degree of the first pressure regulating valve 19 on the basis of the detection result of the first pressure meter 13 so that the pressure of the first gas chamber 11a becomes a set value determined in advance.
In
A refining device 16 which traps the hydrogen fluoride gas mixed in the product gas and refines the fluorine gas is provided on the upstream of the first pump 17 in the first main passage 15. The refining device 16 is a device which separates the hydrogen fluoride gas from the fluorine gas and traps it by using a difference in a boiling point between fluorine and hydrogen fluoride. The refining device 16 will be described later in detail.
A first buffer tank 21 which retains the fluorine gas conveyed by the first pump 17 is provided on the downstream of the first pump 17 in the first main passage 15. The fluorine gas retained in the first buffer tank 21 is supplied to the external device 4. A flow meter 26 which detects a flow rate of the fluorine gas supplied to the external device 4 is provided on the downstream of the first buffer tank 21. A detection result of the flow meter 26 is outputted to a controller 10c. The controller 10c controls a current value supplied from the power supply 9 between the anode 7 and the cathode 8 on the basis of the detection result of the flow meter 26. Specifically, a generation amount of the fluorine gas at the anode 7 is controlled so as to replenish the fluorine gas supplied from the first buffer tank 21 to the external device 4.
As described above, since the fluorine gas supplied to the external device 4 is controlled to be replenished, the internal pressure of the first buffer tank 21 is maintained at a pressure higher than the atmospheric pressure. On the other hand, since the external device 4 side where the fluorine gas is used has an atmospheric pressure, the fluorine gas is supplied from the first buffer tank 21 to the external device 4 by a pressure difference between the first buffer tank 21 and the external device 4 by opening the valve provided on the external device 4.
A branch passage 22 is connected to the first buffer tank 21, and a pressure regulating valve 23 which controls the internal pressure of the first buffer tank 21 is provided in the branch passage 22. Moreover, a pressure meter 24 which detects the internal pressure is provided on the first buffer tank 21. A detection result of the pressure meter 24 is outputted to a controller 10d. The controller 10d opens the pressure regulating valve 23 when the internal pressure of the first buffer tank 21 exceeds a set value determined in advance or specifically, 1.0 MPa and discharges the fluorine gas in the first buffer tank 21. As described above, the pressure regulating valve 23 executes control so that the internal pressure of the first buffer tank 21 does not exceed the predetermined pressure.
A second buffer tank 50 which retains the fluorine gas discharged from the first buffer tank 21 is provided on the downstream of the pressure regulating valve 23 in the branch passage 22. That is, if the internal pressure of the first buffer tank 21 exceeds the predetermined pressure, the fluorine gas in the first buffer tank 21 is discharged through the pressure regulating valve 23, and the discharged fluorine gas is led to the second buffer tank 50. The second buffer tank 50 has a capacity smaller than the first buffer tank 21. A pressure regulating valve 51 which controls the internal pressure of the second buffer tank 50 is provided on the downstream of the second buffer tank 50 in the branch passage 22. Moreover, a pressure meter 52 which detects the internal pressure is provided on the second buffer tank 50. A detection result of the pressure meter 52 is outputted to a controller 10f. The controller 10f controls an opening degree of the pressure regulating valve 51 so that the internal pressure of the second buffer tank 50 becomes a set value determined in advance. The set value is set at a pressure higher than the atmospheric pressure. The fluorine gas discharged through the pressure regulating valve 51 from the second buffer tank 50 is rendered harmless at an abatement unit 53 and emitted. As described above, the pressure regulating valve 51 executes control so that the internal pressure of the second buffer tank 50 becomes a set value. A fluorine gas supply passage 54 which supplies the fluorine gas to the refining device 16 is connected to the second buffer tank 50.
Subsequently, the byproduct gas treatment system 3 will be described.
A second main passage 30 for discharging the hydrogen gas to the outside is connected to the second gas chamber 12a.
A second pump 31 which leads the hydrogen gas out of the second gas chamber 12a and conveys it is provided in the second main passage 30. Moreover, a second reflux passage 32 which connects a discharge side and a suction side of the second pump 31 is connected to the second main passage 30. A second pressure regulating valve 33 for returning the hydrogen gas discharged from the second pump 31 to the suction side of the second pump 31 is provided in the second reflux passage 32.
The second pressure regulating valve 33 has its opening degree controlled by a signal outputted from the controller 10b. Specifically, the controller 10b controls the opening degree of the second pressure regulating valve 33 on the basis of the detection result of the second pressure meter 14 so that the pressure of the second gas chamber 12a becomes a set value determined in advance.
As described above, the pressures of the first gas chamber 11a and the second gas chamber 12a are controlled by the first pressure regulating valve 19 and the second pressure regulating valve 33 so as to be the set values determined in advance, respectively. The set pressures of the first gas chamber 11a and the second gas chamber 12a are preferably controlled to equal pressures so that there is no difference between the liquid level of the molten salt of the first gas chamber 11a and the liquid level of the molten salt of the second gas chamber 12a.
An abatement unit 34 is provided on the downstream of the second pump 31 in the second main passage 30, and the hydrogen gas conveyed by the second pump 31 is rendered harmless at the abatement unit 34 and emitted.
The fluorine gas generating apparatus 100 is also provided with a raw material supply system 5 which supplies and replenishes hydrogen fluoride which is the raw material of the fluorine gas into the molten salt in the electrolytic cell 1. The raw material supply system 5 will be described below.
The raw material supply system 5 is provided with a hydrogen fluoride supply source 40 in which hydrogen fluoride to be replenished in the electrolytic cell 1 is retained. The hydrogen fluoride supply source 40 and the electrolytic cell 1 are connected through a raw material supply passage 41. The hydrogen fluoride retained in the hydrogen fluoride supply source 40 is supplied into the molten salt in the electrolytic cell 1 through the raw material supply passage 41. A flow rate control valve 42 for controlling a supply flow rate of hydrogen fluoride is provided in the raw material supply passage 41.
A current integrator 43 which integrates current supplied between the anode 7 and the cathode 8 is mounted on the power supply 9. The current integrated in the current integrator 43 is outputted to a controller 10e. The controller 10e controls a supply flow rate of the hydrogen fluoride to be led into the molten salt by opening/closing the flow rate control valve 42 on the basis of a signal inputted from the current integrator 43. Specifically, the supply flow rate of hydrogen fluoride is controlled so as to replenish the hydrogen fluoride electrolyzed in the molten salt. More specifically, the supply flow rate of the hydrogen fluoride is controlled so that the concentration of the hydrogen fluoride in the molten salt becomes within a predetermined range.
Moreover, a carrier-gas supply passage 46 which leads a carrier gas supplied from a carrier-gas supply source 45 into the raw material supply passage 41 is connected to the raw material supply passage 41. A shut-off valve 47 which switches between supply and shut-off of the carrier gas is provided in the carrier-gas supply passage 46. The carrier gas is a gas for leading the hydrogen fluoride retained in the hydrogen fluoride supply source 40 into the molten salt in the electrolytic cell 1 and in this embodiment, a nitrogen gas which is an inactive gas is used. During operation of the fluorine gas generating apparatus 100, the shut-off valve 47 is open in principle, and the nitrogen gas is supplied to the cathode chamber 12 of the electrolytic cell 1 together with the hydrogen fluoride. The nitrogen gas is hardly dissolved in the molten salt and is discharged from the second gas chamber 12a through the byproduct gas treatment system 3.
As described above, since the nitrogen gas is supplied into the molten salt of the electrolytic cell 1, there is a concern that the liquid level of the molten salt in the electrolytic cell 1 is pushed up by the nitrogen gas. Thus, it may be so configured that a liquid level meter which detects the liquid level is provided in the electrolytic cell 1, a fluctuation margin is set for the liquid level of the molten salt of the electrolytic cell 1 and the shut-off valve 47 is on/off controlled so that the liquid level of the molten salt is contained in the fluctuation margin. That is, it may be configured that the shut-off valve 47 is closed if the liquid level of the molten salt in the electrolytic cell 1 reaches the upper limit of the fluctuation margin.
A flow rate control valve capable of controlling a flow rate of the nitrogen gas may be provided instead of the shut-off valve 47.
Subsequently, overall control of the fluorine gas generating apparatus 100 configured as above will be described.
The flow rate of the fluorine gas used in the external device 4 is detected by the flow meter 26 provided between the first buffer tank 21 and the external device 4. A voltage to be applied between the anode 7 and the cathode 8 is controlled on the detection result of the flow meter 26, and a generation amount of the fluorine gas in the anode 7 is controlled. The hydrogen fluoride in the molten salt decreased by the electrolysis is replenished from the hydrogen fluoride supply source 40.
As described above, since control is executed so that the hydrogen fluoride in the molten salt is replenished in accordance with the fluorine gas amount used in the external device 4, the liquid level of the molten salt does not usually change greatly. However, if a use amount of the fluorine gas in the external device 4 is rapidly changed or if the pressure of the hydrogen gas in the byproduct gas treatment system 3 is rapidly changed, the pressures of the first gas chamber 11a and the second gas chamber 12a are significantly changed and the liquid levels of the anode chamber 11 and the cathode chamber 12 are significantly fluctuated. If the liquid levels of the anode chamber 11 and the cathode chamber 12 are significantly fluctuated, and if the liquid level falls below the partition wall 6, the first gas chamber 11a and the second gas chamber 12a communicate with each other. In that case, the fluorine gas and the hydrogen gas are mixed and reacted.
Thus, in order to suppress fluctuation of the liquid levels of the anode chamber 11 and the cathode chamber 12, the pressures of the first gas chamber 11a and the second gas chamber 12a are controlled so as to become the set values determined in advance on the basis of the detection results of the first pressure meter 13 and the second pressure meter 14, respectively. As described above, the liquid levels of the anode chamber 11 and the cathode chamber 12 are controlled by maintaining the pressures of the first gas chamber 11a and the second gas chamber 12a constant.
Subsequently, the refining device 16 will be described by referring to
The refining device 16 is composed of two systems, that is, a first refining device 16a and a second refining device 16b provided in parallel, and can be switched so that the fluorine gas passes through only one of the systems. That is, when one of the first refining device 16a and the second refining device 16b is in an operating state, the other is stopped or in a standby state. In this embodiment, two units of the refining devices 16 are arranged in parallel, but three or more refining devices 16 may be arranged in parallel.
Since the first refining device 16a and the second refining device 16b have the same configuration, the first refining device 16a will be mainly described below, and the same reference numeral are given to the same configurations in the second refining device 16b as those in the first refining device 16a, and the description will be omitted. The configurations of the first refining device 16a are suffixed by “a” and the configurations of the second refining device 16b are suffixed by “b” for discrimination.
The first refining device 16a includes an inner tube 61a as a gas inflow unit into which the fluorine gas containing the hydrogen fluoride gas flows and a cooling device 70a which cools the inner tube 61a at a temperature not lower than the boiling point of fluorine and not higher than the melting point of hydrogen fluoride so that the fluorine gas passes through the inner tube 61a while the hydrogen fluoride gas mixed in the fluorine gas is coagulated.
The inner tube 61a is a bottomed cylindrical member, and an upper opening thereof is sealed by a lid member 62a. An inlet passage 63a which leads the fluorine gas generated in the anode 7 into the inner tube 61a is connected to the lid member 62a of the inner tube 61a. The inlet passage 63a is one of two passages which are branched off the first main passage 15, and the other inlet passage 63b is connected to an inner tube 61b of the second refining device 16b. An inlet valve 64a which allows or shuts off inflow of the fluorine gas into the inner tube 61a is provided in the inlet passage 63a.
A conduit 67a provided by being suspended into the inner tube 61a is connected to the inner surface of the lid member 62a of the inner tube 61a. The conduit 67a is formed by having a length such that a lower end opening unit is located in the vicinity of the bottom part of the inner tube 61a. An upper end unit of the conduit 67a is connected to an outlet passage 65a connected to the lid member 62a and discharging the fluorine gas through the inner tube 61a. Therefore, the fluorine gas in the inner tube 61a flows out to the outside through the conduit 67a and the outlet passage 65a. An outlet valve 66a which allows or shuts off outflow of the fluorine gas from the inner tube 61a is provided in the outlet passage 65a. The outlet passage 65a merges with an outlet passage 65b of the second refining device 16b and is connected to the first pump 17.
As described above, the fluorine gas generated in the anode 7 flows into the inner tube 61a through the inlet passage 63a and flows out of the inner tube 61a through the conduit 67a and the outlet passage 65a.
When the first refining device 16a is in the operating state, the inlet valve 64a and the outlet valve 66a are open, while when the first refining device 16a is in the stop or standby state, the inlet valve 64a and the outlet valve 66a are closed.
A thermometer 68a which detects an internal temperature is provided in the inner tube 61a by being inserted through the lid member 62a. Moreover, a pressure meter 69a which detects the internal pressure of the inner tube 61a is provided in the inlet passage 63a.
The cooling device 70a includes a jacket tube 71a capable of partially containing the inner tube 61a and capable of retaining liquid nitrogen as a cooling medium therein, and a liquid nitrogen supply/discharge system 72a which supplies/discharges liquid nitrogen to/from the jacket tube 71a.
The jacket tube 71a is a bottomed cylindrical member, and an upper opening is sealed by a lid member 73a. The inner tube 61a is coaxially contained in the jacket tube 71a in a state having the upper part side protruding from the lid member 73a. Specifically, 80 to 90% of the inner tube 61a is contained in the jacket tube 71a.
Subsequently, the liquid nitrogen supply/discharge system 72a will be described.
A liquid nitrogen supply passage 77a which leads the liquid nitrogen supplied from a liquid nitrogen supply source 76 into the jacket tube 71a is connected to the lid member 73a of the jacket tube 71a. A conduit 82a provided by being suspended into the jacket tube 71a is connected to the inner surface of the lid member 73a of the jacket tube 71a, and an upper end unit of the conduit 82a is connected to the liquid nitrogen supply passage 77a. Therefore, the liquid nitrogen supplied from the liquid nitrogen supply source 76 is led into the jacket tube 71a through the liquid nitrogen supply passage 77a and the conduit 82a. The conduit 82a is formed having a length such that a lower end opening unit is located in the vicinity of the bottom part of the jacket tube 71a.
A flow rate control valve 78a which controls the supply flow rate of the liquid nitrogen is provided in the liquid nitrogen supply passage 77a. A pressure meter 80a which detects an internal pressure of the jacket tube 71a is provided on the downstream of the flow rate control valve 78a in the liquid nitrogen supply passage 77a.
The inside of the jacket tube 71a is formed of two layers, that is, the liquid nitrogen and evaporated nitrogen gas, and the liquid level of the liquid nitrogen is detected by a liquid level meter 74a provided by being inserted through the lid member 73a.
A nitrogen gas discharge passage 79a for discharging the nitrogen gas in the jacket tube 71a is connected to the lid member 73a of the jacket tube 71a. A pressure regulating valve 81a which controls the internal pressure of the jacket tube 71a is provided in the nitrogen gas discharge passage 79a. The pressure regulating valve 81a executes control such that the internal pressure of the jacket tube 71a becomes a predetermined pressure determined in advance on the basis of a detection result of the pressure meter 80a. This predetermined pressure is determined so that the temperature of the liquid nitrogen in the jacket tube 71a becomes not lower than the boiling point of fluorine (−188° C.) and not higher than the melting point of hydrogen fluoride (−84° C.). Specifically, the pressure is set to 0.4 MPa so that the temperature of the liquid nitrogen in the jacket tube 71a becomes approximately −180° C. As described above, the pressure regulating valve 81a controls the internal pressure of the jacket tube 71a to 0.4 MPa so that the temperature of the liquid nitrogen in the jacket tube 71a is maintained at approximately −180° C. The nitrogen gas discharged through the pressure regulating valve 81a is emitted to the outside.
When the liquid nitrogen in the jacket tube 71a is evaporated and emitted to the outside, the liquid nitrogen in the jacket tube 71a decreases. Thus, the flow rate control valve 78a controls the supply flow rate of the liquid nitrogen from the liquid nitrogen supply source 76 to the jacket tube 71a so that the liquid level of the liquid nitrogen in the jacket tube 71a is maintained constant.
An insulating material for heat-retention or a vacuum insulation layer may be provided outside the jacket tube 71a in order to suppress heat transfer between the jacket tube 71a and the outside.
Since the inner tube 61a is cooled by the jacket tube 71a to a temperature not lower than the boiling point of fluorine and not higher than the melting point of hydrogen fluoride, only hydrogen fluoride mixed in the fluorine gas is coagulated in the inner tube 61a, and the fluorine gas passes through the inner tube 61a. As described above, the hydrogen fluorine gas can be trapped in the inner tube 61a. Since the fluorine gas is continuously led from the electrolytic cell 1 into the inner tube 61a, the coagulated hydrogen fluoride accumulates in the inner tube 61a as time elapses. When the accumulated amount of the coagulated hydrogen fluoride reaches a predetermined amount, the operation of the first refining device 16a is stopped, the second refining device 16b in the standby state is started, and operation of the refining device 16 is switched. The operation switching will be described later in detail.
Whether or not the accumulated amount of the coagulated hydrogen fluoride has reached the predetermined amount is determined on the basis of a detection result of a differential pressure meter 86a provided over the inlet passage 63a and the outlet passage 65a of the inner tube 61a, that is, a differential pressure between the inlet and the outlet of the inner tube 61a. When the differential pressure between the inlet and the outlet of the inner tube 61a reaches the predetermined value, it is determined that the accumulated amount of the coagulated hydrogen fluoride in the inner tube 61a has reached the predetermined amount, and the first refining device 16a is stopped. The differential pressure meter 86a corresponds to an accumulated state detector which detects an accumulated state of the hydrogen fluoride in the inner tube 61a. The accumulated state of the hydrogen fluoride in the inner tube 61a may be detected by the pressure meter 69a instead of the differential pressure meter.
The first refining device 16a is stopped by closing the inlet valve 64a and the outlet valve 66a of the inner tube 61a. After the first refining device 16a is stopped, the hydrogen fluoride trapped in the inner tube 61a is conveyed and recovered in the electrolytic cell 1, and the first refining device 16a is regenerated and enters the standby state. As described above, the first refining device 16a is also provided with a recovery facility which conveys and recovers the hydrogen fluoride trapped in the inner tube 61a into the electrolytic cell 1 and a regeneration facility which recycles the first refining device 16a. The recovery facility and the regeneration facility will be described below.
A discharge valve 91a that can discharge liquid nitrogen in the jacket tube 71a into an external tank 90a is provided on the bottom part of the jacket tube 71a. Moreover, a nitrogen gas supply passage 93a which leads the nitrogen gas supplied from a nitrogen gas supply source 92 into the jacket tube 71a is connected to the downstream of the flow rate control valve 78a in the liquid nitrogen supply passage 77a. A shut-off valve 94a which switches between supply and shut-off of the nitrogen gas to the jacket tube 71a is provided in the nitrogen gas supply passage 93a. The supply of the nitrogen gas from the nitrogen gas supply source 92 to the jacket tube 71a is performed while the discharge valve 91a is fully open and the flow rate control valve 78a is fully closed. A gas at a normal temperature is used as the nitrogen gas.
As described above, cooling of the inner tube 61a is cancelled by supplying the nitrogen gas at a normal temperature while the liquid nitrogen in the jacket tube 71a is discharged. With that, the hydrogen fluoride accumulated in the coagulated state in the inner tube 61a is dissolved.
A lower end of the fluorine gas supply passage 54 connected to the second buffer tank 50 (See
The internal pressure of the second buffer tank 50 is controlled to a pressure higher than the atmospheric pressure by the pressure regulating valve 51 (See
A conveying passage 95a which discharges and conveys dissolved hydrogen fluoride in the inner tube 61a is connected to the downstream of the inlet valve 64a in the inlet passage 63a. The conveying passage 95a merges with a conveying passage 95b of the second refining device 16b and become a merged conveying passage 95, and a downstream end of the merged conveying passage 95 is connected to the electrolytic cell 1. Discharge valves 97a and 97b opened when the hydrogen fluoride is discharged are provided in the conveying passages 95a and 95b, respectively. Moreover, a shut-off valve 83 which opens when the hydrogen fluoride is conveyed to the electrolytic cell 1 from the inner tube 61a is provided in the merged conveying passage 95.
A branch passage 99 is connected to the upstream of the shut-off valve 83 in the merged conveying passage 95, and a vacuum pump 96 which deaerates the inside of the jacket tube 71a is provided in the branch passage 99. A shut-off valve 84 which opens when the inside of the jacket tube 71a is deaerated is provided on the upstream of the vacuum pump 96 in the branch passage 99. Moreover, an abatement unit 98 is provided on the downstream end of the branch passage 99.
The hydrogen fluoride dissolved in the inner tube 61a is recovered in the electrolytic cell 1 by supplying the fluorine gas into the inner tube 61a through the fluorine gas supply passage 54 and by being conveyed through the conveying passage 95a and the merged conveying passage 95. As described above, the dissolved hydrogen fluoride in the inner tube 61a is accompanied by the fluorine gas by supplying the fluorine gas into the inner tube 61a as a carrier gas and is recovered in the electrolytic cell 1. Since the fluorine gas is used as a carrier gas, the hydrogen fluoride conveyed through the merged conveying passage 95 is recovered into the anode chamber 11 of the electrolytic cell 1.
After the hydrogen fluoride in the inner tube 61a is discharged, it is necessary to fill the fluorine gas into the inner tube 61a and to regenerate the first refining device 16a. This is because, when the accumulated amount of the coagulated hydrogen fluoride in the inner tube 61b reaches the predetermined amount while the second refining device 16b is operating, an operation can be quickly switched to the first refining device 16a.
Here, if the fluorine gas is used as a carrier gas, filling of the fluorine gas into the inner tube 61a, that is, regeneration of the first refining device 16a is completed at the same time as when discharge of the dissolved hydrogen fluoride in the inner tube 61a is completed.
As described above, the fluorine gas retained in the second buffer tank 50 is used for discharge of the dissolved hydrogen fluoride in the inner tube 61a, conveying it to the electrolytic cell 1, and filling of the fluorine gas into the inner tube 61a. The fluorine gas retained in the first buffer tank 21 may be used instead of the fluorine gas retained in the second buffer tank 50. In that case, the fluorine gas supply passage 54 is connected to the first buffer tank 21. However, in this case, the pressure of the first buffer tank 21 can fluctuate easily, and the pressure of the fluorine gas to be supplied to the external device 4 may fluctuate. Therefore, as in this embodiment, use of the fluorine gas retained in the second buffer tank 50 is more preferable.
Subsequently, the operation of the refining device 16 configured as above will be described. The operation of the refining device 16 is controlled by a controller 20 (See
The case in which the first refining device 16a is in the operating state and the second refining device 16b is in the standby state will be described. In the first refining device 16a, the inlet valve 64a and the outlet valve 66a of the inner tube 61a is in the open state, and the fluorine gas is continuously led from the electrolytic cell 1 into the inner tube 61a. On the other hand, in the second refining device 16b, the inlet valve 64b and the outlet valve 66b of the inner tube 61b are in the closed state, and the fluorine gas is filled in the inner tube 61b. As described above, the fluorine gas generated in the electrolytic cell 1 passes only through the first refining device 16a.
In the following, the first refining device 16a in the operating state will be described.
The liquid nitrogen lead through the liquid nitrogen supply passage 77a is retained in the jacket tube 71a of the first refining device 16a so that the inner tube 61a is cooled by the liquid nitrogen. The internal pressure of the jacket tube 71a is controlled by the pressure regulating valve 81a to 0.4 MPa. As a result, since the temperature of the liquid nitrogen in the jacket tube 71a is maintained at approximately −180° C. which is the temperature not lower than the boiling point of fluorine and not higher than the melting point of hydrogen fluoride, only the hydrogen fluoride is coagulated in the inner tube 61a, while the fluorine gas passes through the inner tube 61a and is conveyed by the first pump 17 to the first buffer tank 21.
Here, the fluorine gas generated in the electrolytic cells 1 flows into the inner tube 61a through the inlet passage 63a and flows out of the inner tube 61a through the conduit 67a and the outlet passage 65a. A lower end opening unit of the conduit 67a is located in the vicinity of the bottom part of the inner tube 61a, and thus, the fluorine gas flows from the upper part of the inner tube 61a and flows out of the lower part of the inner tube 61a. Therefore, the fluorine gas is sufficiently cooled while passing through the inner tube 61a, and hydrogen fluoride in the fluorine gas can be reliably coagulated and trapped.
Since the fluorine gas is continuously led from the electrolytic cell 1 into the inner tube 61a, the liquid nitrogen in the jacket tube 71a for cooling the fluorine gas is also continuously evaporated. The evaporated nitrogen gas is emitted to the outside through the pressure regulating valve 81a.
When the accumulated amount of the coagulated hydrogen fluoride in the inner tube 61a increases and the differential pressure between the inlet and the outlet of the inner tube 61a detected by the differential pressure meter 86a reaches the predetermined value, the operation of the first refining device 16a is stopped, and the second refining device 16b in the standby state is started so that operation of the refining device 16 is switched. In the first refining device 16a, the recovery process of the trapped hydrogen fluoride and the regeneration process are performed in the first refining device 16a.
The operation switching process from the first refining device 16a to the second refining device 16b, the recovery process of the hydrogen fluoride trapped in the first refining device 16a, and the regeneration process of the first refining device 16a will be described below by referring to
As illustrated in
In the stopped first refining device 16a, the recovery process of the trapped hydrogen fluoride is performed in compliance with the following procedure:
First, the discharge valve 97a of the conveying passage 95a and the shut-off valve 84 of the branch passage 99 are opened, and the fluorine gas in the inner tube 61a is suctioned by the vacuum pump 96, rendered harmless in the abatement unit 98 and emitted. At the time when the internal pressure of the inner tube 61a lowers to a predetermined pressure P1 (not more than 100 Pa) not more than the atmospheric pressure (time t2), the shut-off valve 84 is closed, and deaeration inside the inner tube 61a is completed. Since the hydrogen fluoride in the inner tube 61a is in the coagulated state, it is not suctioned by the vacuum pump 96.
When the deaeration of the inside of the inner tube 61a is completed, the flow rate control valve 78a of the liquid nitrogen supply passage 77a is fully closed, supply of the liquid nitrogen to the jacket tube 71a is stopped, and then, the discharge valve 91a is fully opened to discharge the liquid nitrogen. After that, the shut-off valve 94a of the nitrogen gas supply passage 93a is opened, and the nitrogen gas at a normal temperature is supplied to the jacket tube 71a. As a result, as illustrated in
Moreover, at the same time as the discharge of the liquid nitrogen in the jacket tube 71a, the shut-off valve 88a of the fluorine gas supply passage 54 is opened so that the fluorine gas is supplied into the inner tube 61a as a carrier gas. As a result, the internal pressure of the inner tube 61a rises.
At the time when the internal pressure of the inner tube 61a reaches the atmospheric pressure which is the same pressure as in the electrolytic cell 1 (time t3), the shut-off valve 83 of the merged conveying passage 95 is opened, and the dissolved hydrogen fluoride in the inner tube 61a is accompanied by the fluorine gas and conveyed to the anode chamber 11 of the electrolytic cell 1. As a result, the dissolved hydrogen fluoride in the inner tube 61a is recovered in the electrolytic cell 1.
At the time when the temperature in the inner tube 61a reaches a normal temperature (RT) (time t4), the shut-off valve 83 and the shut-off valve 88a are closed, and the conveying of the hydrogen fluoride to the electrolytic cell 1 and the supply of the fluorine gas as a carrier gas into the inner tube 61a are stopped.
As above, the recovery process of the trapped hydrogen fluoride is completed. In the above-described recovery process, since the carrier gas is the fluorine gas, the deaeration inside the inner tube 61a by the vacuum pump 96 performed at the beginning of the recovery process does not necessarily have to be done. That is, the dissolved hydrogen fluoride may be conveyed to the electrolytic cell 1 by supplying the fluorine gas as a carrier gas into the inner tube 61a at the same time as the discharge of the liquid nitrogen in the jacket tube 71a without performing the deaeration in the inner tube 61a. However, if the deaeration in the inner tube 61a is not performed at the beginning of the recovery process, the other micro components in the fluorine gas in the inner tube 61a are also recovered into the electrolytic cell 1, and the other micro components might be concentrated. Therefore, in order to avoid such a situation, the inner tube 61a is preferably deaerated.
Subsequently, the regeneration process of the first refining device 16a is performed in compliance with the following procedure:
First, while the discharge valve 91a and the shut-off valve 94a of the nitrogen gas supply passage 93a are fully closed, the flow rate control valve 78a of the liquid nitrogen supply passage 77a is opened to supply the liquid nitrogen into the jacket tube 71a (time t5). As a result, the internal temperature of the inner tube 61a lowers. The internal pressure of the jacket tube 71a is controlled by the pressure regulating valve 81a to 0.4 MPa, and thus, the internal temperature of the inner tube 61a is lowered to approximately −180° C. and is maintained at the temperature.
At the time when the recovery process is completed, the fluorine gas supplied as a carrier gas has been already filled in the inner tube 61a, but the volume of the fluorine gas in the inner tube 61a is reduced by the supply of the liquid nitrogen to the jacket tube 71a. Thus, the internal pressure of the inner tube 61a may fall below the atmospheric pressure. In that case, the shut-off valve 88a of the fluorine gas supply passage 54 is opened, and the fluorine gas is filled in the inner tube 61a. At the time when the recovery process is finished (time t4), it may be so configured that the shut-off valve 88a is not closed, but the shut-off valve 88a is open all the time during the regeneration process and closed when the internal temperature of the inner tube 61a reaches −180° C.
In this way, the regeneration process of the first refining device 16a is completed, and the first refining device 16a enters the standby state.
As described above, while the first refining device 16a is stopped, the inner tube 61a is cooled to −180° C. and enters the standby state in which the fluorine gas is filled in the inner tube 61a. Therefore, if the differential pressure between the inlet and the outlet of the inner tube 61b in the second refining device 16b during operation reaches the predetermined value, the operation of the second refining device 16b is stopped, and the first refining device 16a is quickly started so that the operation of the refining device 16 can be switched.
According to the above-described embodiment, the following working effects are exerted.
The hydrogen fluoride trapped in the refining device 16 is recovered in the electrolytic cell 1 and reused for regeneration of a fluorine gas, and thus, the hydrogen fluoride which is a component other than the fluorine gas trapped in the process of refining the fluorine gas can be effectively used.
Moreover, the fluorine gas generated in the electrolytic cell 1 is used as the carrier gas for conveying the hydrogen fluoride trapped in the refining device 16 to the electrolytic cell 1. Therefore, a dedicated carrier gas is no longer necessary, and a gas facility for that is not needed, either, so the fluorine gas generating apparatus 100 can be formed in a compact manner and a cost can be reduced. Moreover, the fluorine gas retained in the second buffer tank 50 is used for the fluorine used as the carrier gas. The second buffer tank 50 is a tank for retaining the fluorine gas discharged with control of the internal pressure of the first buffer tank 21. That is, the fluorine gas having been emitted from the first buffer tank to the outside in the prior-art technology is retained in the second buffer tank 50, and the retained fluorine gas is used as the carrier gas. Therefore, the fluorine gas can be effectively used, and also, the emission of the fluorine gas to the outside and the fluorine gas amount treated in the abatement unit 53 are reduced, thereby reducing a load of the abatement unit 53.
Moreover, the refining device 16 is composed of at least two systems, and the refining device 16 of the system stopped by the operation switching is regenerated after the hydrogen fluoride is discharged from the inner tubes 61a and 61b and then, enters the standby state. Thus, the refining device 16 can be operated any time. Therefore, when the accumulated amount of the hydrogen fluoride coagulated in the refining device 16 of the operating system becomes large, the refining device 16 of the system in the standby state can be started quickly. Therefore, there is no need to stop the fluorine gas generating apparatus 100, and the fluorine gas can be supplied stably to the external device 4.
Another mode of the first embodiment will be described below.
In the above-described first embodiment, a mode in which the fluorine gas is used as a carrier gas in the recovery facility for conveying and recovering the hydrogen fluoride trapped in the inner tubes 61a and 61b into the electrolytic cell 1 has been described.
As another configuration of the recovery facility, as illustrated in
As a procedure of the recovery process, the conveying pump 60 is driven with the opening of the shut-off valve 83 at the same time as the discharge of the liquid nitrogen in the jacket tube 71a, whereby the dissolved hydrogen fluoride in the inner tube 61a is conveyed to the electrolytic cell 1. This point is different from the procedure illustrated in the above-described first embodiment. That is, the trapped hydrogen fluoride is conveyed to the electrolytic cell 1 by suctioning the insides of the inner tubes 61a and 61b by the conveying pump 60 while the cooling of the inner tubes 61a and 61b is cancelled.
In the case of this configuration, the supply of the fluorine gas through the fluorine gas supply passage 54 is performed only when the fluorine gas is filled in the inner tubes 61a and 61b in the recovery process.
If the hydrogen fluoride is recovered by using the conveying pump 60 without using a carrier gas, by deaerating the fluorine gas in the inner tube 61a by the vacuum pump 96 before the cooling of the inner tubes 61a and 61b is canceled, only the hydrogen fluoride is recovered. Therefore, the destination of recovery of the hydrogen fluoride may be the hydrogen fluoride supply source 40 instead of the electrolytic cell 1. That is, the hydrogen fluoride trapped in the inner tubes 61a and 61b may be conveyed and recovered in the hydrogen fluoride supply source 40.
A fluorine gas generating apparatus 200 according to a second embodiment of the present invention will be described by referring to
Differences from the above-described first embodiment will be mainly described below, and the same reference numerals are given to the same configuration as those in the first embodiment, and the description will be omitted.
In the fluorine gas generating apparatus 200, the configuration of the byproduct gas treatment system 3 is partially different from that of the first embodiment. That point will be described below by referring to
As illustrated in
Moreover, in the fluorine gas generating apparatus 200, the configuration of the refining device 16 is partially different from that of the first embodiment. The apparatus will be described by referring to
A lower end of the hydrogen gas supply passage 58 connected to the buffer tank 55 is connected to the upstream of the outlet valve 66a in the outlet passage 65a. A shut-off valve 59a which switches between supply and shut-off of the hydrogen gas to the inner tube 61a is provided in the hydrogen gas supply passage 58.
The internal pressure of the buffer tank 55 is controlled by the pressure regulating valve 56 to a pressure higher than the atmospheric pressure. Therefore, by opening the shut-off valve 59a, the hydrogen gas retained in the buffer tank 55 is supplied to the inner tube 61a by the differential pressure between the buffer tank 55 and the inner tube 61a.
As described above, in the fluorine gas generating apparatus 200, the hydrogen gas generated in the cathode chamber 12 of the electrolytic cell 1 and retained in the buffer tank 55 is used as a carrier gas used for discharge of dissolved hydrogen fluoride in the inner tube 61a and for conveying thereof to the electrolytic cell 1. Since the hydrogen gas is used as a carrier gas, the hydrogen fluoride conveyed through the merged conveying passage 95 is recovered into the cathode chamber 12 of the electrolytic cell 1.
A lower end of the fluorine gas supply passage 54 connected to the second buffer tank 50 (See
The internal pressure of the second buffer tank 50 is controlled by the pressure regulating valve 51 (See
Subsequently, an operation of the refining device 16 will be described by referring to
If the accumulated amount of hydrogen fluoride coagulated in the inner tube 61a increases, the internal pressure of the inner tube 61a rises. When the differential pressure between the inlet and the outlet of the inner tube 61a reaches a predetermined value, the inlet valve 64b and the outlet valve 66b of the inner tube 61b of the second refining device 16b are opened, and then, the inlet valve 64a and the outlet valve 66a of the inner tube 61a of the first refining device 16a are closed so that the operation is switched from the first refining device 16a to the second refining device 16b (time t1).
In the stopped first refining device 16a, the recovery process of trapped hydrogen fluoride is executed in compliance with the following procedure:
First, the discharge valve 97a of the conveying passage 95a and the shut-off valve 84 of the branch passage 99 are opened, and the fluorine gas in the inner tube 61a is suctioned by the vacuum pump 96, rendered harmless in the abatement unit 98 and emitted. At the time when the internal pressure of the inner tube 61a lowers to the predetermined pressure P1 (not more than 10 Pa) not more than the atmospheric pressure (time t2), the shut-off valve 84 is closed, and deaeration in the inner tube 61a is completed. Since the hydrogen fluoride in the inner tube 61a is in the coagulated state, it is not suctioned by the vacuum pump 96. Moreover, in the above-described first embodiment, it was described that the inside of the inner tube 61a does not necessarily have to be deaerated. However, in the fluorine gas generating apparatus 200 using the hydrogen gas as a carrier gas, deaeration of the inside of the inner tube 61a is indispensable in order to prevent contact between the fluorine gas and the hydrogen gas in the inner tube 61a.
When the deaeration of the inside of the inner tube 61a is completed, the flow rate control valve 78a of the liquid nitrogen supply passage 77a is fully closed, supply of the liquid nitrogen to the jacket tube 71a is stopped, and then, the discharge valve 91a is fully opened to discharge the liquid nitrogen. After that, the shut-off valve 94a of the nitrogen gas supply passage 93a is opened, and the nitrogen gas at a normal temperature is supplied to the jacket tube 71a. As a result, as illustrated in
Moreover, at the same time as the discharge of the liquid nitrogen in the jacket tube 71a, the shut-off valve 59a of the hydrogen gas supply passage 58 is opened, so that the hydrogen gas is supplied into the inner tube 61a as a carrier gas. As a result, the internal pressure of the inner tube 61a rises.
At the time when the internal pressure of the inner tube 61a reaches the atmospheric pressure which is the same pressure as in the electrolytic cell 1 (time t3), the shut-off valve 83 of the merged conveying passage 95 is opened, and the dissolved hydrogen fluoride in the inner tube 61a is accompanied by the hydrogen gas and conveyed to the cathode chamber 12 of the electrolytic cell 1. As a result, the dissolved hydrogen fluoride in the inner tube 61a is recovered in the electrolytic cell 1.
At the time when the temperature in the inner tube 61a reaches a normal temperature (RT) (time t4), the shut-off valve 83 and the shut-off valve 59a are closed, and the conveying of the hydrogen fluoride to the electrolytic cell 1 and the supply of the hydrogen gas as a carrier gas into the inner tube 61a are stopped. The recovery process of the trapped hydrogen fluoride is completed as above.
Subsequently, the regeneration process of the first refining device 16a is performed in compliance with the following procedure:
First, while the shut-off valve 84 of the branch passage 99 is fully opened (time t5), the hydrogen gas in the inner tube 61a is suctioned by the vacuum pump 96, rendered harmless in the abatement unit 98 and emitted. At the time when the internal pressure of the inner tube 61a lowers to the predetermined pressure P1 (not more than 10 Pa) not more than the atmospheric pressure (time t6), the shut-off valve 84 is closed, and deaeration of the inside of the inner tube 61a is completed.
Subsequently, while the discharge valve 91a and the shut-off valve 94a of the nitrogen gas supply passage 93a are fully closed, the flow rate control valve 78a of the liquid nitrogen supply passage 77a is opened, so that the liquid nitrogen is supplied into the jacket tube 71a. As a result, the internal temperature of the inner tube 61a lowers. The internal pressure of the jacket tube 71a is controlled by the pressure regulating valve 81a to 0.4 MPa, and thus, the internal temperature of the inner tube 61a is lowered to approximately −180° C. and is maintained at that temperature.
Subsequently, the shut-off valve 88a of the fluorine gas supply passage 54 is opened, and the fluorine gas is supplied into the inner tube 61a (time t7). As a result, the internal pressure of the inner tube 61a rises, and at the time when the internal pressure of the inner tube 61a becomes not less than the atmospheric pressure, the shut-off valve 88a is closed. The filling of the fluorine gas is completed as above (time t8).
Accordingly, the regeneration process of the first refining device 16a is completed. In the first refining device 16a during stop, the inner tube 61a is cooled to −180° C. and enters the standby state in which the fluorine gas is filled in the inner tube 61a. Therefore, when the differential pressure between the inlet and the outlet of the inner tube 61b in the second refining device 16b during operation reaches a predetermined value, the operation of the second refining device 16b is stopped, and the first refining device 16a is quickly started so that the operation of the refining device 16 can be switched.
As described above, in the fluorine gas generating apparatus 200, the hydrogen gas retained in the buffer tank 55 is used for the discharge of the dissolved hydrogen fluoride in the inner tube 61a and the conveying thereof to the electrolytic cell 1, and the fluorine gas retained in the second buffer tank 50 is used for the filling of the fluorine gas into the inner tube 61a.
According to the above-described embodiment, the following working effects are exerted.
The hydrogen gas generated in the electrolytic cell 1 is used as the carrier gas for conveying the hydrogen fluoride trapped in the refining device 16 to the electrolytic cell 1. Therefore, a dedicated carrier gas is no longer necessary, and a gas facility for that is not needed, either, so the fluorine gas generating apparatus 200 can be formed in a compact manner and a cost can be reduced.
Moreover, the hydrogen gas used as a carrier gas is the hydrogen gas generated at the cathode 8 of the electrolytic cell 1 and retained in the buffer tank 55 and is a byproduct gas which has conventionally been emitted to the outside. Since the hydrogen gas which has been emitted to the outside is used as a carrier gas in this way, the hydrogen gas can be effectively used, and also, the emission amount of the hydrogen gas to the outside and the hydrogen gas amount treated in the abatement unit 34 are reduced, thereby reducing a load to the abatement unit 34.
Another mode of the second embodiment will be described below.
In this second embodiment, the hydrogen gas is used as a carrier gas for conveying the hydrogen fluoride in the inner tubes 61a and 61b to the electrolytic cell 1.
Instead, an inactive gas such as a nitrogen gas, an argon gas and the like may be used as a carrier gas. In that case, in
The procedures of the recovery process and the regeneration process when an inactive gas is used as a carrier gas are the same as the above-described procedure when the hydrogen gas is used.
If an inactive gas is used as a carrier gas, the buffer tank 55 which retains the hydrogen gas is no longer needed in the byproduct gas treatment system 3. Moreover, if a nitrogen gas is used as a carrier gas, the facility can be simplified by using the nitrogen gas in the nitrogen gas supply source 92 which is a supply source of the nitrogen gas led into the jacket tube 71a.
A fluorine gas generating apparatus 300 according to a third embodiment of the present invention will be described by referring to
Differences from the above-described first embodiment will be mainly described below and the same reference numerals are given to the same configuration as those in the first embodiment, and the description will be omitted.
In a fluorine gas generating apparatus 300, only the configuration of the refining device which traps the hydrogen fluoride gas mixed in the fluorine gas and refines the fluorine gas is different from the first embodiment. A refining device 301 in the fluorine gas generating apparatus 300 will be described below by referring to
The refining device 301 is a device which has the hydrogen fluoride gas in the fluorine gas adsorbed by an adsorbent so as to separate and to trap the hydrogen fluoride gas from the fluorine gas. The refining device 301 is composed of two systems, that is, a first refining device 301a and a second refining device 301b provided in parallel, and is switched so that the fluorine gas passes through only one of the systems. That is, when one of the first refining device 301a and the second refining device 301b is in the operating state, the other is stopped or in the standby state. In this embodiment, two units of the refining devices 301 are arranged in parallel, but three or more refining devices 301 may be arranged in parallel.
Since the first refining device 301a and the second refining device 301b have the same configuration, the first refining device 301a will be mainly described below, and the same reference numeral are given to the same configurations in the second refining device 301b as those in the first refining device 301a, and the description will be omitted. The configurations of the first refining device 301a are suffixed by “a” and the configurations of the second refining device 301b are suffixed by “b” for discrimination.
The first refining device 301a has an upstream refining tower 302a which roughly traps hydrogen fluoride mixed in the fluorine gas generated in the electrolytic cell 1 and a downstream refining tower 303a which removes hydrogen fluoride that cannot be fully recovered by the upstream refining tower 302a arranged in series.
First, the upstream refining tower 302a will be described.
The upstream refining tower 302a includes a cartridge 305a as a gas inflow unit into which the fluorine gas containing the hydrogen fluoride gas flows, an adsorbent 307 contained in the cartridge 305a and by which the hydrogen fluoride gas mixed in the fluorine gas is adsorbed, and a heater 306a as a temperature adjuster which adjusts the temperature of the cartridge 305a.
The cartridge 305a is a container which contains a large number of adsorbents 307, and a material of the cartridge preferably has resistance against fluorine gas and hydrogen fluoride gas such as metal including stainless steel, monel, nickel and the like, for example.
The adsorbent 307 is a porous bead made of sodium fluoride (NaF). Sodium fluoride has its adsorption capability changed depending on the temperature, and thus, the heater 306a is provided in the periphery of the cartridge 305a, and the temperature in the cartridge 305a is adjusted by the heater 306a. As a chemical used in the adsorbent 307, alkali metal fluorides such as KF, RbF, CsF and the like can be used other than sodium fluoride, but sodium fluoride is particularly preferable.
Any temperature adjuster can be used as long as it can adjust the temperature in the cartridge 305a, but a heating/cooling device using steam heating, a heating medium or a cooling medium, for example, may be used in addition to the heater 306a.
An inlet passage 310a which leads the fluorine gas generated at the anode 7 therein is connected to the cartridge 305a. The inlet passage 310a is one of two branches from the first main passage 15, and the other inlet passage 310b is connected to a cartridge 305b of the second refining device 301b. An inlet valve 311a which allows or shuts off inflow of the fluorine gas into the cartridge 305a is provided in the inlet passage 310a.
Moreover, an outlet passage 312a which discharges the fluorine gas is connected to the cartridge 305a. An outlet valve 313a which allows or shuts off outflow of the fluorine gas from the cartridge 305a is provided in the outlet passage 312a.
As described above, the fluorine gas generated at the anode 7 flows into the cartridge 305a through the inlet passage 310a and flows out of the cartridge 305a through the outlet passage 312a. When the first refining device 301a is in the operating state, the inlet valve 311a and the outlet valve 313a are in the open state, and the fluorine gas passes through the cartridge 305a, while when the first refining device 301a is stopped or in the standby state, the inlet valve 311a and the outlet valve 313a are in the closed state.
A concentration detector 315a which optically analyzes and detects hydrogen fluoride concentration in the fluorine gas passing through the cartridge 305a is provided on the upstream of the outlet valve 313a in the outlet passage 312a. Concentration detectors are not particularly limited as long as it can analyze the hydrogen fluoride concentration, but Fourier transform infrared spectrometer (FT-IR) can be cited, for example.
The upstream refining tower 302a also includes a recovery facility which conveys and recovers the hydrogen fluoride trapped in the cartridge 305a into the electrolytic cell 1 and a regeneration facility which regenerates the upstream refining tower 302a. The recovery facility and the regeneration facility will be described below.
A lower end of the fluorine gas supply passage 54 connected to the second buffer tank 50 (See
The internal pressure of the second buffer tank 50 is controlled by the pressure regulating valve 51 (See
Moreover, the conveying passage 95a which discharges and conveys the hydrogen fluoride adsorbed by the adsorbent 307 in the cartridge 305a is connected to the cartridge 305a. The conveying passage 95a and the conveying passage 95b of the second refining device 301b are merged and becomes the merged conveying passage 95, and a lower end of the merged conveying passage 95 is connected to the electrolytic cell 1. The discharge valves 97a and 97b opened in discharge of the hydrogen fluoride are provided in the conveying passages 95a and 95b, respectively.
The hydrogen fluoride trapped by the adsorbent 307 in the cartridge 305a is conveyed through the conveying passage 95a and the merged conveying passage 95 and recovered in the electrolytic cell 1 by supplying the fluorine gas into the cartridge 305a through the fluorine gas supply passage 54. As described above, the hydrogen fluoride in the cartridge 305a is accompanied by the fluorine gas and recovered in the electrolytic cell 1 by supplying the fluorine gas as a carrier gas into the cartridge 305a. Since the fluorine gas is used as a carrier gas, the hydrogen fluoride conveyed through the merged conveying passage 95 is recovered in the anode chamber 11 of the electrolytic cell 1.
After the hydrogen fluoride in the cartridge 305a is discharged, it is necessary to fill the fluorine gas in the cartridge 305a and to regenerate the first refining device 301a. That is because while the second refining device 301b is operating, when the hydrogen fluoride concentration in the fluorine gas having passed through the cartridge 305b reaches the predetermined concentration, it can be quickly switched to the first refining device 301a.
Here, if the fluorine gas is used as a carrier gas, at the same time as the discharge of the hydrogen fluoride in the cartridge 305a is completed, the filling of the fluorine gas into the cartridge 305a, that is, the regeneration of the first refining device 301a is completed.
As described above, the fluorine gas retained in the second buffer tank 50 is used for the discharge of the hydrogen fluoride in the cartridge 305a, the conveying to the electrolytic cell 1, and the filling of the fluorine gas in the cartridge 305a.
Since the downstream refining tower 303a has the configuration similar to that of the upstream refining tower 302a, the same reference numerals are given to the similar configuration as in the upstream refining tower 302a, and the description will be omitted.
The outlet passage 312a connected to the cartridge 305a of the downstream refining tower 303a merges with an outlet passage 312b connected to the cartridge 305b of the downstream refining tower 303b and is connected to the first pump 17.
The upstream of the inlet valve 311a of the downstream refining tower 303a in the first refining device 301a and the upstream of an inlet valve 311b of the downstream refining tower 303b in the second refining device 301b communicate with each other through a bypass passage 320. A switching valve 321 which selectively leads the fluorine gas to the downstream refining tower 303a or the downstream refining tower 303b is provided in the bypass passage 320. Since the first refining device 301a and the second refining device 301b communicate with each other in the bypass passage 320 as above, the fluorine gas having passed through the upstream refining tower 302a or the upstream refining tower 302b can be selectively led to the downstream refining tower 303a or the downstream refining tower 303b by opening/closing the switching valve 321.
The temperatures of the cartridges 305a of the upstream refining tower 302a and the downstream refining tower 303a are controlled by the heaters 306a, respectively. Since sodium fluoride has high adsorption capability of hydrogen fluoride in a range of an approximately room temperature, its adsorption amount becomes large and it can easily deteriorate. Thus, the temperature of the cartridge 305a of the upstream refining tower 302a is preferably set to a temperature such that most of the hydrogen fluoride is adsorbed by the adsorbent 307, while a large load is not applied to the adsorbent 307. As described above, the upstream refining tower 302a functions as a rough trapping process which removes most of the hydrogen fluoride in the fluorine gas.
The temperature of the cartridge 305a of the upstream refining tower 302a is preferably adjusted in a range of 70 to 120° C., considering the required concentration of the, hydrogen fluoride in the fluorine gas and a load of the adsorbent 307. Moreover, it is particularly preferable to be adjusted in a range of 70 to 100° C. so that deterioration of sodium fluoride filled in the cartridge 305a is reduced, and the concentration of the hydrogen fluoride in the fluorine gas at the outlet of the upstream refining tower 302a becomes less than 1000 ppm.
Most of the hydrogen fluoride in the fluorine gas passing through the upstream refining tower 302a has been removed. Thus, the temperature of the cartridge 305a of the downstream refining tower 303a is preferably set approximately to a room temperature at which the adsorption capability of sodium fluoride increases so that the hydrogen fluoride that could not be fully removed in the upstream refining tower 302a is adsorbed by the adsorbent 307. As described above, the downstream refining tower 303a functions as a finishing trapping process which removes the hydrogen fluoride that could not be fully removed in the upstream refining tower 302a.
The temperature of the cartridge 305a of the downstream refining tower 303a is preferably adjusted to a range of 0 to 50° C. so that the concentration of the hydrogen fluoride in the fluorine gas at the outlet of the downstream refining tower 303a becomes less than 100 ppm.
As described above, by setting the temperature of the cartridge 305a of the upstream refining tower 302a higher than the temperature of the cartridge 305a of the downstream refining tower 303a, the hydrogen fluoride can be trapped in two stages, that is, rough trapping in the upstream refining tower 302a and finishing trapping in the downstream refining tower 303a, and thus, deterioration of the adsorbents 307 in the upstream refining tower 302a and the downstream refining tower 303a can be prevented.
Subsequently, an operation of the refining device 301 configured as above will be described. The operation of the refining device 301 illustrated below is controlled by the controller 20 (See
The case in which the first refining device 301a is in the operating state and the second refining device 301b is in the standby state will be described. In the first refining device 301a, the inlet valve 311a and the outlet valve 313a of the upstream refining tower 302a are in the open state, and the inlet valve 311a and the outlet valve 313a of the downstream refining tower 303a are also in the open state, and the fluorine gas is continuously led out of the electrolytic cell 1 into the cartridges 305a of the upstream refining tower 302a and the downstream refining tower 303a, respectively. On the other hand, in the second refining device 301b, the inlet valve 311b and the outlet valve 313b of the upstream refining tower 302b are in the closed state, and the inlet valve 311b and the outlet valve 313b of the downstream refining tower 303b are also in the closed state, and the upstream refining tower 302b and the downstream refining tower 303b are in the standby state in which the fluorine gas is filled in the respective cartridges 305b. In this way, the fluorine gas generated in the electrolytic cell 1 passes only through the first refining device 301a.
The first refining device 301a in the operating state will be described below.
The fluorine gas generated in the electrolytic cell 1 passes through the cartridge 305a of the upstream refining tower 302a and then, passes through the cartridge 305a of the downstream refining tower 303a. In this process, the hydrogen fluoride in the fluorine gas is adsorbed by the adsorbent 307 in the upstream refining tower 302a and roughly trapped and then, adsorbed by the adsorbent 307 in the downstream refining tower 303a and finishingly trapped.
When the adsorption amount of the hydrogen fluoride adsorbed by the adsorbent 307 in the cartridge 305a of the upstream refining tower 302a increases and the concentration of the hydrogen fluoride detected by the concentration detector 315a provided in the outlet passage 312a reaches a predetermined value, the operation of the upstream refining tower 302a is stopped, and the upstream refining tower 302b in the standby state is started so that the operation of the upstream refining tower 302 is switched. Specifically, the inlet valve 311b and the outlet valve 313b of the upstream refining tower 302b are opened and the switching valve 321 is opened, and then, the inlet valve 311a and the outlet valve 313a of the upstream refining tower 302a are closed. As a result, the upstream refining tower 302b is started, while the upstream refining tower 302a is stopped, and the fluorine gas from the electrolytic cell 1 is led to the upstream refining tower 302b and led to the downstream refining tower 303a through the bypass passage 320.
Moreover, when the adsorption amount of the hydrogen fluoride adsorbed by the adsorbent 307 in the cartridge 305a increases and the concentration of the hydrogen fluoride detected by the concentration detector 315a provided in the outlet passage 312a reaches the predetermined value also in the downstream refining tower 303a, the operation of the downstream refining tower 303a is stopped, and the downstream refining tower 303b in the standby state is started so that the operation of the downstream refining tower 303 is switched. Specifically, the inlet valve 311b and the outlet valve 313b of the downstream refining tower 303b are opened and then, the inlet valve 311a and the outlet valve 313a of the downstream refining tower 303a are closed, and the switching valve 321 is closed. As a result, the downstream refining tower 303b is started, and the downstream refining tower 303a is stopped so that the fluorine gas from the electrolytic cell 1 is led from the upstream refining tower 302b to the downstream refining tower 303b.
In the stopped upstream refining tower 302a and downstream refining tower 303a, the recovery process and the regeneration process of the trapped hydrogen fluoride are performed in compliance with the following procedure. Since the procedures of the recovery process and the regeneration process of the upstream refining tower 302a and the downstream refining tower 303a are the same, only the upstream refining tower 302a will be described.
First, the shut-off valve 88a of the fluorine gas supply passage 54 is opened, the fluorine gas is supplied into the cartridge 305a as a carrier gas, and the discharge valve 97a of the conveying passage 95a is opened. As a result, the hydrogen fluoride adsorbed by the adsorbent 307 in the cartridge 305a and trapped is accompanied by the fluorine gas and conveyed to the anode chamber 11 of the electrolytic cell 1.
When the trapped hydrogen fluoride is conveyed to the electrolytic cell 1, the temperature of the cartridge 305a is adjusted by the heater 306a to a range of 150 to 300° C. As a result, the hydrogen fluoride adsorbed by the adsorbent 307 in the cartridge 305a is removed and can be easily accompanied by the fluorine gas and conveyed to the electrolytic cell 1.
By maintaining this state for a predetermined time, all the hydrogen fluoride in the cartridge 305a is recovered in the electrolytic cell 1, the shut-off valve 88a and the discharge valve 97a are closed, and the recovery process of the trapped hydrogen fluoride is completed.
Subsequently, in order to bring the upstream refining tower 302a into the standby state, the temperature setting of the cartridge 305a is changed from 150 to 300° C. to the normal temperature of 70 to 120° C. Here, since the cartridge 305a is already filled with the fluorine gas supplied as a carrier gas, the regeneration process is also completed by the change of the set temperature of the cartridge 305a, and the upstream refining tower 302a enters the standby state.
As described above, since the stopped upstream refining tower 302a is brought into the standby state, when the concentration of the hydrogen fluoride at the outlet of the operating upstream refining tower 302b reaches the predetermined value, the operation of the upstream refining tower 302b is stopped, and the upstream refining tower 302a is quickly started so that the operation of the upstream refining tower 302 is switched.
A controller may be provided in the concentration detectors 315a and 315b so that the operation of the refining device 301 is controlled by the controller.
According to the above-described embodiment, the following working effects are exerted.
Since the hydrogen fluoride trapped in the refining device 301 is recovered in the electrolytic cell 1 and reused in order to generate the fluorine gas, hydrogen fluoride which is a component other than the fluorine gas trapped in the process of refining the fluorine gas can be effectively used.
Moreover, the fluorine gas generated in the electrolytic cell 1 is used as a carrier gas which conveys the hydrogen fluoride trapped in the refining device 301 to the electrolytic cell 1. Therefore, a dedicated carrier gas is no longer necessary, and a gas facility for that is not needed, either, and the fluorine gas generating apparatus 300 can be formed in a compact manner and a cost can be reduced.
Moreover, the refining device 301 is composed of at least two systems, and it can be operated at any time since the refining device 301 of the system stopped by the operation switching is regenerated and enters the standby state after the hydrogen fluoride is discharged from the cartridges 305a and 305b. Thus, when the adsorption amount of hydrogen fluoride adsorbed by the adsorbents 307 in the cartridges 305a and 305b of the refining device 301 of the operating system becomes large, the refining device 301 of the standby system can be quickly started. Therefore, it is not necessary to stop the fluorine gas generating apparatus 300, and the fluorine gas can be stably supplied to the external device 4.
Another mode of the third embodiment will be described below.
(1) In the above-described third embodiment, the mode in which the fluorine gas is used as a carrier gas in the recovery facility which conveys and recovers the hydrogen fluoride trapped in the cartridges 305a and 305b into the electrolytic cell 1 has been described.
As another configuration of the recovery facility, as illustrated in
As a procedure of the recovery process, the conveying pump 60 is driven and the discharge valve 97a is opened instead of supplying the fluorine gas as a carrier gas in the cartridge 305a, whereby the hydrogen fluoride in the cartridge 305a is conveyed to the electrolytic cell 1, and this point is different from the procedure illustrated in the above-described third embodiment. That is, the trapped hydrogen fluoride is conveyed to the electrolytic cell 1 by suctioning the insides of the cartridges 305a and 305b by the conveying pump 60.
In the case of this configuration, the supply of the fluorine gas through the fluorine gas supply passage 54 is performed only when the fluorine gas is filled in the cartridges 305a and 305b in the regeneration process.
(2) If the hydrogen fluoride is recovered by using the conveying pump 60 without using a carrier gas, by deaerating the fluorine gas in the cartridges 305a and 305b before the conveying of the hydrogen fluoride by the conveying pump 60, only the hydrogen fluoride is recovered. Therefore, as illustrated in
As the facility which deaerates the fluorine gas in the cartridges 305a and 305b, as illustrated in
The embodiments of the present invention have been described but the above-described embodiments illustrate only a part of application examples of the present invention and are not intended to limit the technical scope of the present invention to the specific configurations of the above-described embodiments.
This application claims priority on the basis of Japanese Patent Application No. 2009-274676 filed with Japan Patent Office on Dec. 2, 2009 and all the contents of this application is incorporated in this description by reference.
| Number | Date | Country | Kind |
|---|---|---|---|
| 2009-274676 | Dec 2009 | JP | national |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/JP2010/071015 | 11/25/2010 | WO | 00 | 6/4/2012 |
| Publishing Document | Publishing Date | Country | Kind |
|---|---|---|---|
| WO2011/068071 | 6/9/2011 | WO | A |
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| 20120241313 A1 | Sep 2012 | US |
