WO2014104196A1 - ガス精製装置 - Google Patents
ガス精製装置 Download PDFInfo
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- WO2014104196A1 WO2014104196A1 PCT/JP2013/084893 JP2013084893W WO2014104196A1 WO 2014104196 A1 WO2014104196 A1 WO 2014104196A1 JP 2013084893 W JP2013084893 W JP 2013084893W WO 2014104196 A1 WO2014104196 A1 WO 2014104196A1
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
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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
- B01D53/229—Integrated processes (Diffusion and at least one other process, e.g. adsorption, absorption)
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/106—Silica or silicates
- B01D2253/108—Zeolites
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/116—Molecular sieves other than zeolites
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/30—Physical properties of adsorbents
- B01D2253/302—Dimensions
- B01D2253/308—Pore size
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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
- B01D2256/24—Hydrocarbons
- B01D2256/245—Methane
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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
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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
- B01D2257/104—Oxygen
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/06—Polluted air
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- 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
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40058—Number of sequence steps, including sub-steps, per cycle
- B01D2259/40075—More than ten
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- 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
- B01D2259/403—Further details for adsorption processes and devices using three beds
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- 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
- B01D2259/404—Further details for adsorption processes and devices using four beds
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
- C10L2290/542—Adsorption of impurities during preparation or upgrading of a fuel
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
- C10L2290/548—Membrane- or permeation-treatment for separating fractions, components or impurities during preparation or upgrading of a fuel
Definitions
- An adsorption tower filled with an adsorbent that adsorbs miscellaneous gases other than the gas to be purified from the source gas is provided.
- a source gas supply path for supplying source gas to the adsorption tower is provided,
- a product gas recovery path for discharging the gas to be purified that has not been adsorbed on the adsorbent as product gas is provided,
- the adsorption tower, the raw material gas supply path, the product gas recovery path, and the exhaust gas An adsorption step of receiving a raw material gas from the raw material gas supply path, adsorbing a miscellaneous gas to the adsorbent, and collecting a product gas;
- the present invention relates to
- coal mine gas is introduced into the adsorption tower filled with the adsorbent by a compressor or the like until a predetermined pressure is reached.
- oxygen, nitrogen, and carbon dioxide contained in the coal mine gas are first adsorbed to the front part (lower part) of the adsorption tower, and methane having a slow adsorption rate is adsorbed to the rear part (upper part) of the adsorption tower.
- an adsorbing step of adsorbing the miscellaneous gas in the raw material gas to the adsorbent in the adsorption tower can be performed.
- the gas to be purified in the raw material gas that has not been adsorbed by the adsorbent is recovered from the product gas recovery path, and the adsorption tower that has adsorbed and saturated the miscellaneous gas desorbs the miscellaneous gas adsorbed by the adsorbent under reduced pressure. It can be regenerated by performing a desorption process.
- the exhaust gas generated at this time is mainly composed of miscellaneous gas and is exhausted from the miscellaneous gas discharge passage.
- a pressure swing operation in which the adsorption process and the desorption process are repeated can be performed.
- the exhaust gas to be exhausted is further purified, and a configuration in which a membrane separation device is provided in the miscellaneous gas discharge path in order to improve the recovery rate of the gas to be purified (see Patent Document 1),
- Patent Document 2 The structure (refer patent document 2) which provides a membrane separation apparatus in the upstream is considered.
- an object of the present invention is to improve the recovery rate of the gas to be purified from the gas purifier using the PSA device, and to achieve both the purity and the recovery rate with high power efficiency.
- a source gas supply path for supplying source gas to the adsorption tower is provided,
- a product gas recovery path for discharging the gas to be purified that has not been adsorbed on the adsorbent as product gas is provided,
- the adsorption tower, the source gas supply path, the product gas recovery path, and the miscellaneous gas discharge path An adsorption step of receiving a raw material gas from the raw material gas supply path, adsorbing a miscellaneous gas to the adsorbent, and collecting a product gas;
- the miscellaneous gas discharge passage has a separation membrane that does not transmit the gas to be purified but permeates the mis
- a membrane separation device that has a separation membrane that does not allow the gas to be purified to permeate through the miscellaneous gas discharge path of the PSA device but permeates the gas to be purified, and that separates the gas to be purified and the gas by the exhaust pressure of the adsorption tower
- the membrane separation device does not participate in the purification of the gas to be purified.
- the gas purity can be set high by the PSA apparatus.
- the recovery rate can be improved efficiently without reducing the purity of the gas to be purified.
- the miscellaneous gas discharge path has a separation membrane that does not transmit the gas to be purified but permeates the miscellaneous gas, and a membrane separation device that separates the gas to be purified and the miscellaneous gas by the exhaust pressure of the adsorption tower.
- a regeneration gas return path is provided for returning the regeneration gas whose concentration of the gas to be purified is increased by the separation membrane to the source gas supply path
- a bypass path may be provided that guides the exhaust gas flowing through the miscellaneous gas discharge path to the regeneration gas return path by bypassing the membrane separation device.
- an exhaust gas with a high product gas concentration may be generated from the gas purifier. If such an exhaust gas is supplied to a membrane separation device in the same manner as a miscellaneous gas having a low product gas purity, there is a risk that the loss of product gas in the membrane separation device may increase. Rather, it may be reused as a raw material gas as it is. It may be preferable.
- a buffer tank may be provided upstream of the membrane separation device in the miscellaneous gas discharge path.
- the buffer tank can temporarily store the miscellaneous gas discharged in the desorption process before being supplied to the membrane separation device. At this time, high-pressure miscellaneous gas containing the gas to be purified having a relatively high concentration can be accumulated in the buffer tank by pressure equalization operation by the pressure difference between the adsorption tower and the buffer tank.
- the miscellaneous gas in the buffer tank can be supplied to the membrane separation device, and the high-pressure miscellaneous gas discharged from the adsorption tower at an early stage can be relaxed and supplied to the membrane separation device.
- the gas to be purified can be purified from the miscellaneous gas with high accuracy.
- the flow rate of high-pressure miscellaneous gas discharged from the adsorption tower at an early stage is too high, and the permeation of the miscellaneous gas through the separation membrane is not sufficiently performed, and a part of the miscellaneous gas is mixed into the regeneration gas side, thereby reducing the purification accuracy. You can avoid that.
- Configuration 4 Moreover, you may provide a pressure reduction pump in the miscellaneous gas permeation
- the membrane of the membrane separation device can be adjusted by adjusting the output of the decompression pump. It is easy to set and maintain the separation conditions suitably.
- the gas after removing the miscellaneous gas from the exhaust gas from the PSA apparatus by the membrane separator has a higher concentration of the gas to be purified, and becomes a regeneration gas that can be used as a raw material gas.
- the concentration of the purification target gas in the regeneration gas varies during each process of the PSA apparatus.
- the concentration fluctuation of the regeneration gas over time can be reduced, which contributes to the stable supply of the regeneration gas to the raw material gas.
- the pressure applied to the regeneration gas tank and the separation membrane of the membrane separation device can be changed by the regeneration pressure control valve. This makes it possible to stably remove the miscellaneous gas from the exhaust gas in the membrane separation apparatus and balance the source gas supply pressure on the source gas supply path side, which makes the supply of the source gas unstable. It can be suppressed.
- a regeneration control device that controls the membrane separation pressure of the separation membrane by the regeneration pressure control valve is provided, even if the regeneration gas pressure fluctuates during each process of the PSA device, This contributes to supplying the regeneration gas into the raw material gas.
- a product gas tank may be provided in the product gas recovery path.
- the membrane separation device can be operated continuously, so that it does not interfere with the operation of the membrane separation device. Stable operation is possible.
- the source gas may be a methane-containing gas
- the purification target gas may be methane
- the miscellaneous gas may be a gas mainly composed of carbon dioxide.
- a typical biogas composition is about 40 to 60% methane and about 60 to 40% carbon dioxide.
- the recovery rate cannot be increased so much, and the methane contained in the exhaust gas cannot be increased.
- the concentration tends to be high.
- methane in biogas can be used effectively and the atmosphere It can contribute to environmental conservation by reducing methane as a global warming gas emitted into the environment.
- the adsorbent may be mainly composed of at least one material selected from activated carbon, molecular sieve carbon, zeolite, and a porous metal complex.
- Adsorbents mainly composed of at least one material selected from activated carbon, molecular sieve carbon, zeolite, and porous metal complexes are widely used as adsorbents for PSA equipment, and those with high gas adsorption separation efficiency are known.
- activated carbon and molecular sieve carbon have excellent separation characteristics between methane gas and carbon dioxide, and can efficiently adsorb and separate carbon dioxide when concentrating biogas and coal mine gas.
- Molecular sieve carbon, zeolite, and a porous metal complex are suitable for separating a gas having a small molecular diameter, and are also suitably used for concentrating methane from a gas containing hydrogen, helium, or the like.
- Such molecular sieve carbon has extremely high methane and air separation performance, and can be in a form suitable for concentrating methane as a gas to be purified from a raw material gas such as biogas.
- the separation membrane is at least selected from cellulose acetate, polyamide, polyimide, polysulfone, polytetrafluoroethylene, polyethersulfone, carbon membrane, microporous glass composite membrane, DDR type zeolite, multi-branched polyimide silica, and polydimethylsiloxane.
- One kind of material can be the main component.
- the source gas supply path may be provided with a booster pump, and the supply pressure of the source gas to the adsorption tower by the booster pump may be 0.5 MPaG to 2 MPaG.
- “PaG” used in the present application represents the gauge pressure in terms of Pa, and indicates a relative pressure with respect to the atmospheric pressure.
- Such a pressure is preferable because the raw material gas supplied at normal pressure can be supplied to the adsorption tower of the PSA apparatus with relatively little power, and the PSA apparatus can easily exhibit sufficient adsorption separation performance. In addition, if the pressure is increased too much, there is a problem that the recovery rate of methane decreases. Therefore, by setting the pressure to 0.5 MPaG or more, the gas separation capability in the PSA apparatus is maintained high, and by setting the pressure to 2 MPaG or less, the apparatus as a whole can be set to energy-efficient power, and the methane recovery rate can also be maintained high.
- the exhaust pressure of the PSA apparatus varies according to the gas desorption pressure in the desorption process and the gas cleaning pressure when cleaning the adsorbent.
- the maximum membrane separation pressure is a differential pressure from the normal pressure (or the degree of pressure reduction when a decompression pump is provided on the miscellaneous gas permeation side of the membrane separation device). Therefore, the exhaust pressure varies to some extent depending on the progress of the process in the PSA apparatus, and the membrane separation pressure also varies accordingly. Further, if a decompression pump is provided on the miscellaneous gas permeation side of the membrane separation apparatus, the driving power of the decompression pump can be maintained and set within a range where efficient membrane separation is possible.
- the gas purification apparatus includes adsorption towers A1 to A4 packed with adsorbents A11 to A14.
- a raw material gas supply path L1 for supplying biogas as a raw material from a raw material gas tank T1
- a product gas recovery path for recovering methane as a purification target gas not adsorbed by the adsorbents A11 to A14 as a product gas L2 and product gas tank T2 and miscellaneous gas discharge path L3 for desorbing and exhausting carbon dioxide as miscellaneous gas adsorbed on adsorbents A11 to A41
- the four adsorption towers A1 to A4 are provided.
- the number of towers is not limited as long as it is plural, and three towers, five towers, and the like can be selected as necessary. Is possible.
- Gas supply from the raw material gas tank T1 to the raw material gas supply passage L1 is performed using the supply pump P1, and when the pressure control valve Vc1 is provided in the bypass passage L10 that bypasses the supply pump P1, the adsorption towers A1 to A4 are pressurized.
- the pressure can be controlled stably.
- the source gas supplied to the source gas supply path L1 is supplied to the adsorption towers A1 to A4 through supply paths L11 to L41 having switching valves V11 to V41.
- the product gas discharged from the adsorption towers A1 to A4 flows into the product gas recovery path L2 through the recovery paths L12 to L42 provided with switching valves V12 to V42.
- a pressure control valve Vc2 is provided in the product gas recovery path L2.
- the miscellaneous gas adsorbed in the adsorption towers A1 to A4 is desorbed from the adsorbents A11 to A14 by being depressurized, and is discharged from the miscellaneous gas discharge path L3 through the exhaust gas paths L13 to L43 having switching valves V13 to V43. Is done.
- the miscellaneous gas discharge path L3 has a separation membrane M1 that does not transmit methane as the gas to be purified but transmits carbon dioxide as the miscellaneous gas.
- a membrane separation device M for separating the purification target gas and the miscellaneous gas by the exhaust pressure of the adsorption towers A1 to A4 is provided, and the regeneration gas whose concentration of the purification target gas is increased by the separation membrane M1 is supplied to the raw material gas supply path L1.
- a regeneration gas return path L5 for return is provided, and an exhaust path L6 is provided on the miscellaneous gas permeation side of the membrane separation apparatus M in the miscellaneous gas discharge path L3.
- the product gas recovery path L2 has a product gas cleaning path L4 through which product gas as a cleaning gas flows from the product gas tank T2 into the adsorption towers A1 to A4 on the upstream side of the pressure control valve Vc2 (adsorption tower). (A1 to A4 side). That is, the cleaning gas flows from the product gas tank T2 to the product gas cleaning path L4, and is supplied to each adsorption tower through the cleaning paths L14 to L44 having switching valves V14 to V44, and the gas in the adsorption towers A1 to A4. Is replaced with product gas and discharged as miscellaneous gas from the miscellaneous gas discharge path L3 through exhaust gas paths L13 to L43 provided with switching valves V13 to V43.
- a pressure reducing valve Vr4, an on-off valve Vo, and a needle valve Vn4 are provided between the product gas recovery path L2 and the adsorption towers A1 to A4 in the product gas cleaning path L4.
- the product gas from the product gas tank T2 is flowed into the adsorption towers A1 to A4 through the washing paths L14 to L44 having the switching valves V14 to V44 from the product gas washing path L4 as the cleaning gas.
- A1 to A4 can be cleaned.
- the washing pressures of the adsorption towers A1 to A4 are controlled by the pressure reducing valve Vr4, adjusted so as not to cause a rapid pressure change by the needle valve Vn4, and the operation switching is facilitated by the on-off valve Vo4.
- the regeneration gas return path L5 is provided with a regeneration gas tank T5 and a pressure control valve Vc5. That is, the miscellaneous gas that has not permeated through the separation membrane M1 in the membrane separation device M is collected and stored in T5 through L5, and is re-supplied from the regeneration gas tank T5 to L1.
- the membrane separation pressure of the membrane separation apparatus M is controlled based on the exhaust pressure of each of the adsorption towers A1 to A4, and the regeneration gas stored in the regeneration gas tank T5 and returned to the regeneration gas return path L5 is kept at a constant pressure. It is returned to the raw material gas supply path L1 and reused.
- bypass passage L30 that bypasses the miscellaneous gas from the miscellaneous gas discharge passage L3 to the downstream side (regeneration gas tank T5 side) from the pressure control valve Vc5 of the regeneration gas return passage L5 without passing through the membrane separation device M.
- On-off valves Vo3 and Vo5 are provided on the bypass passage L30 and the miscellaneous gas discharge passage L3 on the side of the membrane separator M from the bypass passage L30, so that miscellaneous gases having high methane purity can be directly regenerated without passing through the membrane separator M. Recoverable at T5.
- a decompression pump P6 is provided in the exhaust passage L6 on the miscellaneous gas permeation side of the membrane separation device M.
- the decompression pump P6 is operated in a steady state and plays a role of maintaining the membrane separation pressure at a predetermined pressure or higher based on the miscellaneous gas discharge path L3 side pressure of the adsorption towers A1 to A4.
- Each adsorption tower A1 to A4 is provided with an inter-column pressure equalization path L7, and the gas discharged from the upper part of the adsorption towers A1 to A4 in each pressure equalization (pressure reduction) step is supplied to each pressure equalization (pressure increase) via L4. ) It can be transferred to the upper part of the adsorption towers A1 to A4 where the process is performed. That is, the gas discharged from the upper part of the adsorption towers A1 to A4 in the pressure equalization (pressure reduction) step flows into the inter-column pressure equalization path L7 via the pressure equalization paths L17 to L47 provided with the switching valves V17 to V47.
- the pressure equalizing path is configured to connect the upper parts of the adsorption towers to equalize the pressure, but the present invention is not limited to this.
- the upper and lower parts of the adsorption towers The connecting structure, the structure connecting the lower part and the lower part, the structure connecting the intermediate part, and the like can be changed as appropriate.
- each of the adsorption towers A1 to A4 is provided with a product gas boosting path L8 for supplying a product gas as a boosting gas inside the adsorption towers A1 to A4. That is, in the boosting process, the product gas supplied from T2 flows into the respective adsorption towers from the product gas boosting path L8 via the boosting paths L18 to L48 including the switching valves V18 to V48.
- the product gas pressurization path L8 is provided with an on-off valve Vo8 and a pressure control valve Vc8 so that the product gas can be circulated into the adsorption towers A1 to A4 based on the pressure held in the product gas tank T2 to increase the pressure. It is configured.
- the gas purification device is provided with a control device C.
- the control device C includes the adsorption towers A1 to A4, the raw material gas supply path L1, the product gas recovery path L2, the miscellaneous gas discharge path L3, the product gas cleaning path L4, the L5, the L6, and the L7.
- the switching valves V11 to V48 and the like provided in the pipes of L8 are controlled to open and close.
- the regeneration control device functions as an adsorption / desorption control device that performs each adsorption step in each adsorption tower A1 to A4 using P1 and P6, and controls the membrane separation pressure of the separation membrane M1 by the pressure control valve Vc5.
- it also functions as a cleaning control device for cleaning the adsorption towers A1 to A4 by flowing product gas from the product gas tank T2 into the adsorption towers A1 to A4.
- adsorbents A11 to A41 adsorbents A11 to A14 capable of selectively adsorbing miscellaneous gases mainly composed of carbon dioxide in biogas are preferably used.
- adsorbents A11 to A41 those mainly composed of at least one material selected from activated carbon, molecular sieve carbon, zeolite, and porous metal complex are used.
- the MP method The pore volume (V 0.40 ) at the pore diameter does not exceed 0.01 cm 3 / g and the pore volume (V 0.34 ) at the pore diameter of 0.34 nm is measured.
- a molecular sieve carbon having an A of 0.20 cm 3 / g or more is used.
- a material that transmits a miscellaneous gas mainly composed of carbon dioxide in the exhaust gas and does not transmit methane as a purification target gas is preferably used.
- a separation membrane is selected from cellulose acetate, polyamide, polyimide, polysulfone, polytetrafluoroethylene, polyethersulfone, carbon membrane, microporous glass composite membrane, DDR type zeolite, multi-branched polyimide silica, and polydimethylsiloxane.
- the main component is at least one kind of material.
- the biogas as the raw material gas used here is mainly for methane and carbon dioxide with a methane content rate of about 60%, to obtain a product gas containing 98% or more of methane. Perform gas purification.
- the adsorption towers A1 to A4 are filled with adsorbents A11 to A14, respectively.
- supply paths L11 to L41 for supplying biogas from the source gas tank T1 by the supply pump P1 are provided to constitute the source gas supply path L1.
- recovery paths L12 to L42 for recovering methane as a purification target gas that has not been adsorbed by the adsorbents A11 to A41 out of the biogas supplied to the adsorption towers A1 to A4 are provided above the adsorption towers A1 to A4.
- a product gas recovery path L2 is provided.
- the biogas is supplied from the raw material gas supply path L1 to the adsorption towers A1 to A4, and methane that has not been adsorbed by the adsorbents A11 to A14 is discharged from the product gas recovery path L2, thereby allowing the adsorbents A11 to A14. It can be separated from methane by adsorbing miscellaneous gas.
- exhaust gas passages L13 to L43 for discharging miscellaneous gases adsorbed by the adsorbents A11 to A14 are provided below the adsorption towers A1 to A4 to constitute the miscellaneous gas discharge passage L3.
- the biogas supplied from the raw material gas supply path L1 is adsorbed by the adsorbents A11 to A41 so that the concentrated high-concentration carbon dioxide can be taken out.
- the gas passages L11 to L48 are provided with switching valves V11 to V48, and the operation of the pumps P1 and P6 controls the switching of gas supply, discharge and stop to the adsorption towers A1 to A4.
- the apparatus C can be controlled collectively.
- the membrane separation apparatus M includes a separation membrane M1 as a module, and is configured to be capable of recovering a purification target gas contained in the miscellaneous gas by performing membrane separation on the miscellaneous gas supplied via the miscellaneous gas discharge path L3.
- a separation membrane M1 as a module
- the miscellaneous gas supplied to the membrane separator M comes into contact with the separation membrane M1 in the membrane separator M, and carbon dioxide permeates and is removed through the separation membrane M1 due to the membrane separation characteristics of the separation membrane M1.
- a regenerated gas in which methane is more concentrated than the supplied miscellaneous gas is obtained.
- the regeneration gas is discharged to the regeneration gas return path L5 and returned to the raw material gas supply path L1, while the gas mainly composed of carbon dioxide that has permeated through the membrane is discharged to the outside through the exhaust path L6.
- the regeneration gas return path L5 is provided with a regeneration gas tank T5, and the regeneration gas separated from the membrane is stored in the regeneration gas tank T5 and then returned to the raw material gas supply path L1 at a predetermined pressure.
- the control device C controls the switching valves V11 to V47 and the pumps P1 and P6, and in accordance with FIG.
- a pressure fluctuation operation is performed in which a desorption step of desorbing the miscellaneous gas mainly composed of carbon dioxide adsorbed on the adsorbents A11 to A14 and exhausting it from the miscellaneous gas discharge path L3 is performed.
- the biogas near atmospheric pressure is supplied from the lower part of the adsorption towers A1 to A4 and supplied to the adsorbents A11 to A41 by the supply pump P1 to adsorb the miscellaneous gas mainly composed of carbon dioxide and as a gas to be purified.
- a parallel adsorption process is performed in which the adsorption process proceeds simultaneously to the two adsorption towers A1 to A4.
- Adsorption process, adsorption process, and post-parallel adsorption process are performed in order)
- the gas having a relatively low concentration in the high-pressure adsorption towers A1 to A4 is transferred to the other adsorption towers A1 to A4 in an intermediate pressure state lower than the adsorption towers A1 to A4.
- a final pressure equalization (pressure reduction) step for setting the pressure in the adsorption towers A1 to A4 to an intermediate pressure state on the low pressure side
- the adsorbents A11 to A41 are further depressurized to a low pressure state, and the miscellaneous gases adsorbed on the adsorbents A11 to A41 are desorbed to adsorb the towers A1 to A1.
- Desorption process to recover from the bottom of A4 A cleaning process in which the miscellaneous gas remaining in the adsorption towers A1 to A4 where the adsorbents A11 to A14 are regenerated by the desorption process is replaced with a product gas.
- the intermediate pressure state on the high pressure side Receiving the gas in the adsorption towers A1 to A4 and setting the pressure in the adsorption towers A1 to A4 to an intermediate pressure state on the low pressure side; A waiting process; The gas in the other adsorption towers A1 to A4 in the high pressure state is received in the adsorption towers A1 to A4 in the intermediate pressure state on the low pressure side, and the pressure in the adsorption towers A1 to A4 is changed to the intermediate pressure state on the high pressure side.
- Pressure equalization (pressure increase) process After increasing the pressure in the tower by the pressure equalization (pressure increase) step, further pressurization air is supplied into the adsorption towers A1 to A4 from the upper part of the adsorption towers A1 to A4, and methane is selected as the adsorbents A11 to A41.
- Boosting process to restore the high-pressure state that can be adsorbed automatically, The operation is controlled in such a way as to perform in order.
- each adsorption tower A1 to A4 changes as shown in FIG. That is, by sequentially reducing the pressure in the tower through each pressure equalization process, the desorption process can be performed from a state where the pressure in the tower is greatly reduced, and adsorption is performed by desorbing the miscellaneous gas adsorbed on the adsorbent with less power. The material can be easily regenerated.
- the adsorption tower A1 is controlled according to the following steps.
- the other adsorption towers A2 to A4 perform the same operation by shifting the phase, but since the description is duplicated, the detailed description is omitted with the description of FIGS.
- the adsorption towers A1 to A4 are referred to as first to fourth adsorption towers A1 to A4 in this order.
- 2 and 3 show the operating state of the on-off valve and the like in each step. Further, ⁇ number> in the following description indicates a step number in FIGS.
- the operating conditions specifically shown below are examples, and the present invention is not limited to the following specific examples.
- the internal pressure of the fourth adsorption tower A4 is gradually decreased at the end of the adsorption process of the fourth adsorption tower A4.
- the adsorption process of the first adsorption tower A1 is started. That is, prior to the start of the adsorption process of the first adsorption tower A1, the pre-parallel adsorption process is performed together with the post-parallel adsorption process of the fourth adsorption tower A4.
- the second adsorption tower A2 is a standby process, and the third adsorption tower A3 is started with a desorption process.
- This pre-parallel adsorption step is performed for about 5 seconds, and adsorption separation of methane and carbon dioxide in the raw material gas is started in the first adsorption tower A1.
- the ⁇ 1> final pressure equalization (pressure increase) step is performed and the process proceeds to the ⁇ 2-3> pressure increase step.
- a ⁇ 2> cleaning step and a ⁇ 3> first-stage pressure equalization (pressure increase) step are performed.
- the ⁇ 1> first-stage pressure equalization (step-down) process is performed, and the ⁇ 2> standby step is interposed, and the process proceeds to the ⁇ 3> final pressure-equalization (step-down) process.
- the methane purity in the product gas at this time can be set by setting the time of the adsorption process, and can be 90% or more.
- a cylindrical type (inner diameter 54 mm, volume 4.597 L) adsorption tower A1 is used,
- the adsorbent A11 when the pore size distribution is measured by the MP method and the pore size is 0.38 nm or more, the pore volume (V 0.40 ) at the pore size is 0.05 cm 3 / g.
- molecular sieve carbon having a pore volume (V 0.34 ) of 0.20 to 0.23 cm 3 / g at a pore diameter of 0.34 nm
- V 0.34 pore volume of 0.20 to 0.23 cm 3 / g at a pore diameter of 0.34 nm
- a post-parallel adsorption process is performed in which the adsorption process is performed in parallel with the second adsorption tower A2 at the beginning of the adsorption process. That is, since the biogas supply amount in the adsorption step and the sum of the biogas supply amounts to the first and second adsorption towers A1 and A2 in this step are the same, in this step, the first and second adsorption towers A1 are used. , A2 is set to be smaller than the biogas supply amount in the adsorption process. Therefore, as shown in FIGS.
- a standby process is performed in the third adsorption tower A3, and a desorption process is performed in the fourth adsorption tower A4.
- the parallel adsorption process is performed for 5 seconds immediately after the adsorption process.
- the first-stage pressure equalization (pressure reduction) process is performed with the third adsorption tower A3 that performs the final pressure equalization (pressure increase) process. That is, as shown in FIGS. 2 and 3, the non-adsorbed gas in the tower is discharged via the switching valve V17 of the pressure equalizing path L17 and transferred to the third adsorption tower A3 via the switching valve V34 of the cleaning path L34. It is the composition to do. As a result, as shown in FIG. 3, the first adsorption tower A1 is pressure balanced with the third adsorption tower A3 in the intermediate pressure state on the low pressure side.
- the adsorption process is performed in the second adsorption tower A2, and the desorption process is performed in the fourth adsorption tower A4.
- this first-stage pressure equalization (step-down) process is performed for 5 seconds, and shifts to an intermediate pressure state on the high pressure side of about 0.5 MPaG.
- the second adsorption tower A2 is performing the adsorption process
- the third adsorption tower A3 is shifted to the pressure increasing process
- the fourth adsorption tower A4 is shifted to the washing process.
- this standby process is performed for 90 seconds, and the intermediate pressure state on the high pressure side is maintained.
- the first adsorption tower A ⁇ b> 1 finishes the desorption process and performs the first-stage pressure equalization (pressure increase) process with the fourth adsorption tower A ⁇ b> 4.
- the final pressure equalization (pressure reduction) process is performed in between. That is, the non-adsorbed gas in the tower and the miscellaneous gas that starts to be desorbed from the adsorbent A11 are discharged through the switching valve V17 in the pressure equalizing path L17, and the fourth adsorbing tower through the switching valve V44 in the cleaning path L44. It is configured to transfer to A4.
- the first adsorption tower A1 finishes the desorption process, and the pressure is balanced with the fourth adsorption tower A4 in the low pressure state.
- the second adsorption tower A2 is performing an adsorption process
- the third adsorption tower A3 is performing a pressure increasing process.
- this final pressure equalization (pressure reduction) step is performed for 5 seconds, and shifts to an intermediate pressure state on the low pressure side of about 0.25 MPaG.
- the first adsorption tower A1 that has reached the intermediate pressure state on the low pressure side is adsorbing a high-concentration miscellaneous gas to the adsorbent A11 in the tower.
- the high concentration miscellaneous gas adsorbed by the adsorbent A11 is recovered by performing a desorption process in which the inside of the tower is depressurized from an intermediate pressure state on the low pressure side to a low pressure state. That is, the miscellaneous gas concentrated through the switching valve V13 of the exhaust gas passage L13 is supplied to the membrane separation device M by the internal pressure of the first adsorption tower A1.
- the operation state of the membrane separation apparatus M at this time will be described later.
- the second adsorption tower A2 performs the ⁇ 8> post-parallel adsorption process in parallel with the third adsorption tower A3, and then the ⁇ 9> first-stage pressure equalization (pressure reduction) process with the fourth adsorption tower A4. Is done.
- the ⁇ 9> pre-adsorption process is performed in parallel with the second adsorption tower A2, and then the ⁇ 9> adsorption process is performed.
- a ⁇ 9> final pressure equalization (pressure increase) process is sequentially performed with the second adsorption tower A2.
- this desorption step is performed for 365 seconds, and the first adsorption tower A1 shifts from the intermediate pressure state on the low pressure side to the low pressure state of almost atmospheric pressure as shown in FIG.
- the first adsorption tower A1 that has shifted to a low pressure state replaces the gas in the tower with a gas mainly composed of methane by flowing the product gas into the tower. Wash. That is, the on-off valve Vo4 of the product gas cleaning path L4 is opened, the needle valve Vn4 is adjusted, and the product gas is allowed to flow from the product gas tank T2 to the first adsorption tower A1 through the switching valve V14 of the cleaning path L14.
- the atmosphere in the first adsorption tower A1 is replaced with methane, and the gas exhaust gas remaining in the first adsorption tower A1 is passed through the switching valve V13 of the exhaust gas passage L13. It supplies to discharge to the miscellaneous gas discharge path L3.
- the on-off valve Vo5 is opened, the on-off valve Vo3 is closed, and the cleaning gas containing the product gas as a main component is transferred to the regeneration gas return path L5, bypassing the membrane separation device M, and directly into the regeneration gas tank. It is set as the structure collect
- the second adsorption tower A2 is a standby process, and the third adsorption tower A3 is continuing the adsorption process.
- the fourth adsorption tower A4 a pressure increasing process is performed.
- This cleaning step is performed for about 90 seconds, and the inside of the first adsorption tower A1 is shifted to a low pressure state of almost atmospheric pressure.
- First-stage pressure equalization (pressure increase) step As shown in FIGS. 2 and 3, in the first adsorption tower A1 in which the adsorbent A11 is regenerated by releasing the adsorbed methane by releasing the adsorbed methane, the second adsorption tower By performing the first-stage pressure equalization (pressure increase) step with A2, the pressure in the tower is recovered, and the initial pressure from the adsorbent A11 discharged in the final pressure equalization (pressure decrease) step in the second adsorption tower A2 The desorbed gas receives exhaust gas containing a relatively high concentration of methane.
- the gas in the column discharged from the second adsorption tower A2 in the intermediate pressure state on the high pressure side via the switching valve V27 in the pressure equalizing path L27 is transferred from the switching valve V14 in the cleaning path L14. accept.
- the first adsorption tower A1 recovers the pressure from the low pressure state to the intermediate pressure state on the low pressure side, as shown in FIG.
- the third adsorption tower A3 continues the adsorption process, and the fourth adsorption tower A4 performs the pressure increasing process.
- This first-stage pressure equalization (pressure increase) step is performed for about 10 seconds, and the first adsorption tower A1 recovers the pressure to about 0.25 MPaG.
- the second adsorption tower A2 is performing the desorption process, and the third adsorption tower A3 and the fourth adsorption tower A4 are shifted to the post-parallel adsorption process and the pre-parallel adsorption process.
- This standby step is performed for about 5 seconds, and the first adsorption tower A1 is maintained at about 0.25 MPaG.
- the desorption process is performed in the second adsorption tower A2, and the adsorption process is performed in the fourth adsorption tower A4.
- This final pressure equalization (pressure increase) step is performed for about 10 seconds, and the pressure in the first adsorption tower A1 is increased to about 0.5 MPaG.
- the first adsorption tower A1 that has recovered the pressure to the intermediate pressure state on the high pressure side is restored to the high pressure state by injecting the product gas. That is, the product gas is caused to flow into the first adsorption tower A1 via the switching valve V14 of the product gas cleaning path L4. Thereby, the inside of the first adsorption tower A1 is restored to a high pressure state, and is regenerated to a high pressure state capable of adsorbing carbon dioxide in the biogas by supplying the biogas.
- a ⁇ 15> first-stage pressure equalization (pressure increase) process is performed with the third adsorption tower A3.
- a ⁇ 15> final pressure equalization (pressure reduction) process is performed with the second adsorption tower A2.
- an adsorption step is performed in the fourth adsorption tower A4.
- This pressurization step is performed for about 50 seconds, and the pressure in the first adsorption tower A1 is increased to 0.8 MPaG that can separate methane and carbon dioxide in the biogas.
- the miscellaneous gas discharge path L3 is provided with a membrane separation device M having a separation membrane M1, and separates methane by permeating carbon dioxide from miscellaneous gas mainly composed of carbon dioxide discharged from the miscellaneous gas discharge path L3. Connected as possible.
- a gas that does not permeate the separation membrane M1 and has an increased methane concentration is discharged as a regeneration gas to the regeneration gas return path L5, and a gas mainly containing carbon dioxide that permeates the separation membrane M1 and passes through the separation membrane M1. Thus, it can be discharged into the exhaust path L6.
- the primary pressure of the separation membrane M1 by the membrane separator M becomes the exhaust pressure of the adsorption towers A1 to A4, and therefore fluctuates to about 0.25 MPaG to 0 MPaG. -0.1 MPaG (equivalent to vacuum), the membrane separation pressure of 0.35 MPaG to 0.1 MPaG is maintained, and a continuous membrane separation operation can be performed.
- the primary pressure of the membrane separation by the membrane separation apparatus M becomes the cleaning pressure of the adsorption towers A1 to A4 and is constant at about 0 MPaG, so the membrane separation pressure of 0.1 MPaG is maintained.
- continuous membrane separation operation can be performed, basically, when product gas is used as a cleaning gas, the gas supplied to the membrane separator M does not contain much carbon dioxide gas. Sufficient gas separation is continued.
- the exhaust gas discharged from the exhaust path L6 can be an exhaust gas of about 2 to 6% methane and 94 to 98% carbon dioxide.
- the gas composition returned to the regeneration gas return path L5 is a methane-containing gas of about 60% methane and about 40% carbon dioxide.
- the regeneration gas return path L5 is provided with a pressure control valve Vc5, and a regeneration gas tank T5 is provided between the membrane separation device M and the pressure control valve Vc5. Since it is connected to the upstream side of the supply pump P1 in the path L1, the regeneration gas can be mixed with the raw material gas and separated and purified again.
- the exhaust gas was 15-20% methane, and the methane recovery rate was 83%. That is, according to the methane concentration method of the present invention, it was experimentally clarified that both high concentration efficiency and high recovery rate can be achieved.
- the gas purification apparatus can be appropriately provided with a pressure sensor, a temperature sensor, and the like. Specifically, a pressure sensor or a gas sensor for monitoring the supply pressure of the raw material gas or the methane concentration of the product gas is usually provided, but detailed description is omitted in the above-described embodiment. .
- the supply pump P1 and the decompression pump P6 for allowing the gas to flow through each pipe are not limited to the above arrangement, and can be variously modified as long as the gas can flow.
- the supply pump P1 is provided upstream (source gas tank T1 side) from the connection portion with the regeneration gas return path L5 in the source gas supply path L1.
- the supply pump P1 may be omitted, and the regeneration gas return path L5 may be provided with a compression pump P5 that applies the source gas supply pressure to the source gas supply path L1.
- the supply pressure to the raw material gas supply path L1 is appropriately maintained by the pressure control valve Vc51 configured as shown in FIG. 5 and provided in the bypass path bypassed to the compression pump P5.
- the exhaust passage L6 can be operated without providing the pressure reducing pump P6, and the pressure reducing pump P6 is omitted from the viewpoint of simplifying the equipment. It is preferable to provide a decompression pump P6 from the viewpoint of stabilizing the membrane separation pressure. In the case of providing the decompression pump P6, it is desirable to operate the decompression pump P6 in a steady manner from the viewpoint of stable operation. However, Steps 3, 7, 11, 15 in which the cleaning process in FIG. In steps 4, 8, 12, and 16 until the desorption process is started, the decompression pump P6 can be operated at a low load or stopped. In such a case, the pressure control valve Vc5 can be fixed in a state where the opening degree is reduced or in a closed state.
- the gas in the miscellaneous gas discharge path L3 needs to be membrane-separated to obtain a regenerated gas. Therefore, it is necessary to sufficiently apply the membrane separation pressure.
- a product gas is used at the time of a process that does not flow out or at the time of a cleaning process, it is less necessary to perform membrane separation.
- the gas supply pressure to the membrane separation apparatus M is low in the cleaning process. Therefore, the output of the decompression pump P6 can be lowered during a time period when the membrane separation pressure is not required.
- the pressure reducing pump P6 can be inverter-controlled.
- the product gas is the main component of the gas flowing through the miscellaneous gas discharge passage L3 during the cleaning process, it may be recovered directly as the product gas after the membrane separation process. It can be purity. Moreover, even if it is the regeneration gas in a normal desorption process, it may have sufficient purity similarly.
- the regeneration gas return path L5 is provided with a regeneration gas recovery path L9 for recovering the regeneration gas as product gas, and the product gas recovery path L2 is connected via the press-fit pump P9. It can also be bypassed.
- the regeneration gas distribution destination is the regeneration gas return path L5 ⁇ the raw material gas supply path L1, or the regeneration gas recovery path L9 ⁇ the product gas tank T2.
- branch control That is, when the product gas purity of the regeneration gas is high, the regeneration gas is recovered to the product gas tank T2 via the regeneration gas recovery path L9, and when the product gas purity of the regeneration gas is low, the raw material is returned via the regeneration gas return path L5. It can be set as the form which returns to the gas supply path L1.
- the regeneration gas can always be maintained at a product gas purity that can be recovered as a product gas, or (2) the regeneration gas is higher in purity than the source gas, or ( 3)
- the regeneration gas return path L5 is omitted and the regeneration gas recovery path L9 is omitted.
- the gas purification apparatus is provided with four adsorption towers A1 to A4.
- the gas purification apparatus is not limited to this, and may be a system in which two or three towers are alternately treated. Any configuration that can perform typical PSA is acceptable.
- three towers can be configured as shown in FIG.
- the PSA cycle is not limited to the above-described configuration as long as each adsorption tower can be effectively used continuously, and various modifications can be made.
- the gas purification apparatus has the configuration shown in FIG. 7, the operation method according to FIG. 8 is possible.
- the product gas was supplied at a static pressure (no pressure applied) to the adsorption tower during the cleaning step, but the cleaning step can be performed in a pressurized state. In this case, the cleaning efficiency can be improved.
- the gas purification apparatus of the present invention has shown an example used for biogas purification, but in addition to biogas, for example, coal mine gas, etc. It can be used for the purpose of purification by adsorbing miscellaneous gases other than the gas to be purified from the raw material gas. Can be changed.
- a buffer tank T3 can be provided in the upstream portion of the membrane separation device M in the miscellaneous gas discharge path L3.
- Vc52 is a pressure control valve for maintaining the pressure in the buffer tank T3 appropriately below the internal pressure of the adsorption towers A1 to A4.
- L9 in FIG. 9 is similar to the regeneration gas recovery path L9 in FIG. 6 and is denoted by the same reference numeral as being a conduit for recovering the regeneration gas to the product gas recovery path L2 via the press-in pump P9. It is shown.
- the buffer tank can temporarily store the miscellaneous gas discharged in the desorption process before being supplied to the membrane separation device.
- high-pressure miscellaneous gas containing the gas to be purified having a relatively high concentration can be accumulated in the buffer tank by pressure equalization operation by the pressure difference between the adsorption tower and the buffer tank.
- miscellaneous gases miscellaneous gases having a relatively low pressure can be supplied to the regeneration gas tank via Vo5, and the miscellaneous gases in the buffer tank and the regeneration gas tank are not subjected to the desorption process in the adsorption tower. Even if it exists, it can supply to a membrane separator as needed.
- the miscellaneous gas in the buffer tank is supplied to the membrane separation device, the high-pressure miscellaneous gas discharged from the adsorption tower in the initial stage can be relaxed and supplied to the membrane separation device. While performing a membrane separation operation with a high recovery rate using the pressure of the miscellaneous gas, the gas to be purified can be purified from the miscellaneous gas with high accuracy.
- the regeneration gas distribution destination is changed from the regeneration gas return path L5 to the source gas supply path L1 in accordance with the composition of the gas flowing in the miscellaneous gas discharge path L3.
- branch control can be performed such that the regeneration gas recovery path L9 is changed to the product gas tank T2, or the regeneration gas recovery path L9 is directly used as the product gas. That is, when the product gas purity of the regeneration gas is high, the regeneration gas is recovered in the product gas tank T2 via the regeneration gas recovery path L9, or the product gas in the product gas tank T2 without being recovered in the product gas tank T2.
- the product gas can be used as another product gas for other purposes, and when the product gas purity of the regeneration gas is low, it can be returned to the raw material gas supply path L1 via the regeneration gas return path L5.
- the regeneration gas return path L5 can be abbreviate
- the operation method according to FIGS. 10 to 12 can be performed by simplifying the piping and valve configuration in the gas purification apparatus having the configuration of FIGS. 2 to 4 in the previous embodiment. That is, according to the configuration of FIGS. 10 to 12, the pressure of the adsorption tower by the product gas is omitted, and the pressure by the raw material gas eliminates the need for the product gas boosting path L8 and eliminates the cleaning process. The gas cleaning path L4 is unnecessary. At this time, loss of product gas due to pressure increase can be saved, so that the product gas recovery rate can be improved. Further, by providing a standby process after the post-parallel adsorption process, the pressure fluctuation is temporarily interrupted, so that the pressure changes in three stages from the maximum pressure to the minimum pressure in FIG. 4, but becomes slower in four stages in FIG. As a result, there is no sudden pressure fluctuation in the adsorption tower, which contributes to a more stable operation of the gas purification apparatus.
- the gas purification apparatus of the present invention can recover higher-purity methane, and can be used as a gas purification apparatus that can effectively utilize biogas and the like that have been difficult to reuse in the past with a high methane recovery rate. be able to.
- A1 to A4 (first to fourth) adsorption towers A11 to A41: adsorbent C: control device L1: raw material gas supply path L2: product gas recovery path L3: miscellaneous gas discharge path L4: product gas cleaning path L5: regeneration Gas return path L6: Exhaust path L7: Inter-column pressure equalization path L8: Product gas pressure increase path L9: Regeneration gas recovery path L10, L30: Bypass paths L11-L41: Supply path L12-L42: Recovery path L13-L43: Exhaust gas path L14 to L44: Washing paths L17 to L47: Pressure equalizing paths L18 to L48: Boosting path M: Membrane separation device M1: Separation membrane P1: Supply pump P5: Compression pump P6: Pressure reducing pump P9: Pressurizing pump T1: Feed gas tank T2: Product gas tank T5: Regeneration gas tanks V11 to V44: Switching valves Vc1 to Vc8: Pressure control valves Vn4,
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Abstract
Description
前記吸着塔に原料ガスを供給する原料ガス供給路を設け、
前記吸着材に吸着しなかった精製対象ガスを製品ガスとして排出する製品ガス回収路を設け、
前記吸着材に吸着した雑ガスを脱着させて排気する雑ガス排出路を設け、
前記吸着塔と、前記原料ガス供給路と、前記製品ガス回収路と、前記排ガスとを、
前記原料ガス供給路から原料ガスを受け入れて、雑ガスを前記吸着材に吸着するとともに、製品ガスを回収する吸着工程と、
吸着材に吸着した雑ガスを脱着して前記雑ガス排出路より排気する脱着工程と、
を交互に行う圧力揺動運転可能に接続したガス精製装置に関する。
これにより、原料ガスとしての炭鉱ガスから、吸着材を用いて空気を分離し、メタンを濃縮して、当該濃縮されたメタンを燃料等として利用することができるものとされている。
前記吸着塔に原料ガスを供給する原料ガス供給路を設け、
前記吸着材に吸着しなかった精製対象ガスを製品ガスとして排出する製品ガス回収路を設け、
前記吸着材に吸着した雑ガスを減圧脱着させて排気する雑ガス排出路を設け、
前記吸着塔と、前記原料ガス供給路と、前記製品ガス回収路と、前記雑ガス排出路とを、
前記原料ガス供給路から原料ガスを受け入れて、雑ガスを前記吸着材に吸着するとともに、製品ガスを回収する吸着工程と、
吸着材に吸着した雑ガスを脱着して前記雑ガス排出路より排気する脱着工程と、
を交互に行う圧力揺動運転可能に接続した構成(以下PSA装置と称する)が想定される。
上記目的を達成するための本発明のガス精製装置の特徴構成は、
原料ガスから精製対象ガス以外の雑ガスを吸着する吸着材を充填してある吸着塔を設け、
前記吸着塔に原料ガスを供給する原料ガス供給路を設け、
前記吸着材に吸着しなかった精製対象ガスを製品ガスとして排出する製品ガス回収路を設け、
前記吸着材に吸着した雑ガスを脱着させて排気する雑ガス排出路を設け、
前記吸着塔と、前記原料ガス供給路と、前記製品ガス回収路と、前記雑ガス排出路とを、
前記原料ガス供給路から原料ガスを受け入れて、雑ガスを前記吸着材に吸着するとともに、製品ガスを回収する吸着工程と、
吸着材に吸着した雑ガスを脱着して前記雑ガス排出路より排気する脱着工程と、
を交互に行う圧力揺動運転可能に接続したガス精製装置であって、
前記雑ガス排出路に、精製対象ガスを透過せず、前記雑ガスを透過する分離膜を有するとともに、前記吸着塔の排気圧で精製対象ガスと雑ガスとを分離する膜分離装置を設け、
分離膜で精製対象ガス濃度の高められた再生ガスを原料ガス供給路に返送する再生ガス返送路及び/又は製品ガスとして回収する再生ガス回収路を設けた点にある。
すなわち、PSA装置の雑ガス排出路に精製対象ガスを透過せず、前記雑ガスを透過する分離膜を有するとともに、前記吸着塔の排気圧で精製対象ガスと雑ガスとを分離する膜分離装置を設けると、原料ガスから製品ガスを取り出すガス路では、PSA装置が精製対象ガスの精製に寄与するものの、前記膜分離装置は精製対象ガスの精製に関与しないために、製品ガス中の精製対象ガス純度はPSA装置によって高く設定することができる。このとき、PSA装置からの精製対象ガス回収率は低下しがちになるが、排ガスを回収して原料ガス供給路に返送するから、精製対象ガスの回収率を高くすることができる。排ガスを全量回収しても、吸着塔に供給されるガス中の雑ガス濃度が上昇することになるから、製品ガス中の精製対象ガス純度が低下するおそれがある。そこで、膜分離装置により、返送される排ガス中から精製対象ガスを含まない真の排ガスを除去すれば、吸着塔に供給されるガス中の雑ガス濃度上昇を抑制することができるようになる。すると、製品ガス中の精製対象ガス純度が低下するのを抑制してPSA装置での精製対象ガス純度を低下させることなく回収率を向上させることができるようになる。
また、前記雑ガス排出路に、精製対象ガスを透過せず、雑ガスを透過する分離膜を有するとともに、前記吸着塔の排気圧で精製対象ガスと雑ガスとを分離する膜分離装置を設け、
分離膜で精製対象ガス濃度の高められた再生ガスを前記原料ガス供給路に返送する再生ガス返送路を設け、
前記雑ガス排出路に流通する排ガスを、前記膜分離装置をバイパスして前記再生ガス返送路に導くバイパス路を設けてあってもよい。
PSAの工程によっては、ガス精製装置から、製品ガス濃度の高い排ガスが発生する場合がある。このような排ガスを、製品ガス純度の低い雑ガスと同様に膜分離装置に供給すると、膜分離装置における製品ガスのロスが大きくなるおそれがあって、むしろ、そのまま原料ガスとして再利用するのが好ましい場合もある。
前記雑ガス排出路における前記膜分離装置の上流部に、バッファタンクを設けてあってもよい。
前記バッファタンクは、脱着工程により排出される雑ガスを、前記膜分離装置に供給される前に一旦貯留することができる。このとき、前記吸着塔とバッファタンクとの圧力差により均圧操作により、比較的高濃度に精製対象ガスを含む高圧の雑ガスをそのバッファタンク内に蓄積することができる。
〔構成4〕
また、前記雑ガス排出路における前記膜分離装置の雑ガス透過側に減圧ポンプを設けてもよい。
減圧ポンプを設けてあれば、膜分離装置の膜分離圧が不足する場合に、精製対象ガスの膜分離を継続するために必要最小限の動力を供給することができ、より安定に膜分離動作を継続することができるようになる。
また、前記再生ガス返送路に再生ガスタンクを設けてあってもよい。
膜分離装置でPSA装置からの排ガス中から雑ガスを除去した後のガスは、精製対象ガスの濃度が高められており、原料ガスとして用いることができる再生ガスとなる。しかし、この再生ガス中の精製対象ガス濃度は、PSA装置の各工程中に変動する。そこで、再生ガスを再生ガスタンクに一時貯留することによって、再生ガスの経時的な濃度変動を緩和することができ、原料ガスに対する再生ガスの安定供給に寄与する。
また、前記再生ガス返送路に再生圧力制御弁を設け、前記再生圧力制御弁により前記分離膜の膜分離圧を制御する再生制御装置を備えてもよい。
上記構成によると、再生ガスタンクおよび膜分離装置の分離膜にかかる圧力を再生圧力制御弁により設定変更することができるようになる。これにより、膜分離装置における排ガス中から雑ガスの除去が安定的に行えるようになるとともに、原料ガス供給路側の原料ガス供給圧とのバランスをとることができ、原料ガスの供給が不安定になるのを抑制することができる。
また、前記製品ガス回収路に製品ガスタンクを設けてもよい。
製品ガス回収路においても製品ガスタンクを設けてあれば製品ガス中の精製対象ガス濃度を安定化することができる。また、このような構成において製品ガスタンクを設けると、製品ガスタンク内は有圧になるので、吸着塔内の吸着材から雑ガスを脱着させて再吸着可能に再生する際の洗浄用ガスとして製品ガスを流入させて用いることもできる。
さらに、上記構成において、前記製品ガスタンクから前記吸着塔に製品ガスを流入する製品ガス洗浄路を設け、製品ガス洗浄路における製品ガスタンクと吸着塔との間に製品圧力制御弁を設け、前記製品ガスタンクから製品ガスを吸着塔に流入させて前記吸着塔を洗浄する洗浄制御装置を備えてもよい。
製品ガスタンクに加えて製品ガスタンクから前記吸着塔に製品ガスを流入する洗浄路を設け、洗浄路における製品ガスタンクと吸着塔との間に製品圧力制御弁を設けてあれば、製品ガスタンクから洗浄路を介してPSA装置へ製品ガスを供給することができる。これにより、吸着塔内の吸着材から雑ガスを脱着させて再吸着可能に再生する際の洗浄用ガスとしてそのまま製品ガスを用いることができる。また、この際の圧力は洗浄排ガスが雑ガス排出路に排出される際にも排ガスに負荷される。そのため、洗浄排ガスに含まれる精製対象ガスも、膜分離装置により回収可能に運転される。また、負荷される圧力を別途供給する必要も無いので、膜分離装置に対する動力供給を低減することができる。
また、前記原料ガスがメタン含有ガスであり、精製対象ガスがメタンであり、雑ガスが二酸化炭素を主成分とするガスとすることができる。
たとえば、バイオガス等の、燃料ガスとしてそのまま用いるにはメタン含有率が低いガス源から、燃料ガスとしてそのまま利用可能な純度のメタンを供給可能にでき、未利用燃料ガスの有効利用を図ることができる。また、このような原料ガスは、雑ガスとして二酸化炭素を主に含んでいる場合、メタンと二酸化炭素との化学的性質の違いにより、膜分離装置による分離が適している場合が多く、特に好適に利用できる。
さらに、前記原料ガスが、精製対象ガスとしてメタンを40%以上含有するメタン含有ガスであり、メタンを90%以上含有する製品ガスを得るものとすることができる。
典型的なバイオガスの組成は、メタン40~60%、二酸化炭素60~40%程度である。このようなバイオガスに対して、従来のガス精製装置を用いてメタンを90%以上含有する製品ガスを得る場合には、回収率をあまり高くすることができず、排ガス中に含まれるメタンの濃度が高くなりやすいという実情があった。
しかし、膜分離装置を備えて、回収率を高めたガス精製装置として、メタンを90%以上含有する製品ガスを得ることができると、バイオガス中のメタンを有効利用することができるとともに、大気中に放散される地球温暖化ガスとしてのメタンを減少させ、環境保全に寄与することができる。
前記吸着材が活性炭、モレキュラーシーブカーボン、ゼオライト、多孔性の金属錯体から選ばれる少なくとも一種の材料を主成分とするものであってもよい。
活性炭、モレキュラーシーブカーボン、ゼオライト、多孔性の金属錯体から選ばれる少なくとも一種の材料を主成分とする吸着材は、PSA装置の吸着材として汎用されており、ガス吸着分離効率が高いものが知られている。特に、活性炭や、モレキュラーシーブカーボンは、メタンガスと二酸化炭素との分離特性に優れ、バイオガス、炭鉱ガスの濃縮の際二酸化炭素を効率よく吸着分離できる。モレキュラーシーブカーボン、ゼオライト、多孔性の金属錯体は、分子径の小さなガスを分離するのに適しており、水素、ヘリウム等を含有するガスからメタンを濃縮する用途でも好適に用いられる。
前記吸着材が、MP法で測定した細孔径0.38nm以上において、その細孔径における細孔容積(V0.40)が0.01cm3/gを超えず、細孔径0.34nmにおける細孔容積(V0.34)が0.20cm3/g以上であるモレキュラーシーブカーボンであってもよい。
このようなモレキュラーシーブカーボンは、きわめてメタン、空気分離性能が高く、バイオガス等の原料ガスから精製対象ガスとしてメタンを濃縮するのに好適な形態とすることができる。
また、前記分離膜が酢酸セルロース、ポリアミド、ポリイミド、ポリスルホン、ポリテトラフルオロエチレン、ポリエーテルスルホン、カーボン膜、微多孔質ガラス複合膜、DDR型ゼオライト、多分岐ポリイミドシリカ、ポリジメチルシロキサンから選ばれる少なくとも一種の材料を主成分とするものとすることができる。
膜分離装置が、これらの分離膜を備えると、効率よく膜分離を行え、しかも、耐久性が高いことが知られており有用である。また、これらの材料は、特にメタンと二酸化炭素の分離係数が高く、バイオガスからメタンを濃縮する際に有効である。
また、前記原料ガス供給路に昇圧ポンプを備え、前記昇圧ポンプによる原料ガスの吸着塔に対する供給圧が0.5MPaG~2MPaGとすることができる。
なお、本願で用いる「PaG」とは、ゲージ圧をPaであらわしたものであって、大気圧との相対圧を示すものである。
このような圧力であれば、常圧で供給される原料ガスを比較的少ない動力でPSA装置の吸着塔に供給でき、PSA装置でも十分な吸着分離性能を発揮しやすいため好適である。また、圧力を上げすぎると、メタンの回収率が低下する問題がある。
そこで、0.5MPaG以上としておくことによって、PSA装置におけるガス分離能力を高く維持しつつ、2MPaG以下としておくことによって、装置全体としてエネルギー効率の高い動力に設定でき、メタン回収率も高く維持できる。
ガス精製装置は、図1に示すように、吸着材A11~A14を充填した吸着塔A1~A4を備える。各吸着塔には、原料ガスタンクT1からたとえばバイオガスを原料として供給する原料ガス供給路L1、吸着材A11~A14に吸着されなかった精製対象ガスとしてのメタンを製品ガスとして回収する製品ガス回収路L2および製品ガスタンクT2、吸着材A11~A41に吸着した雑ガスとしての二酸化炭素を脱着させて排気する雑ガス排出路L3が設けられる。本実施の形態では、吸着塔A1~A4の4塔を備える構成としたが、塔数は複数であれば限定されるものではなく、3塔、5塔その他、適宜必要に応じ選択することが可能である。
吸着塔A1~A4は、それぞれ、吸着材A11~A14を充填してなる。各吸着塔A1~A4の下部には、原料ガスタンクT1から供給ポンプP1によりバイオガスを供給する供給路L11~L41を設けて原料ガス供給路L1を構成する。また、各吸着塔A1~A4の上部に、吸着塔A1~A4に供給されたバイオガスのうち吸着材A11~A41に吸着されなかった精製対象ガスとしてのメタンを回収する回収路L12~L42を設けて製品ガス回収路L2を構成してある。これにより、原料ガス供給路L1から吸着塔A1~A4にバイオガスを供給するとともに、吸着材A11~A14に吸着されなかったメタンを製品ガス回収路L2から排出することによって、吸着材A11~A14に雑ガスを吸着してメタンと分離可能に構成してある。また、前記吸着塔A1~A4には、吸着材A11~A14に吸着された雑ガスを排出する排ガス路L13~L43を各吸着塔A1~A4の下部に設けて前記雑ガス排出路L3を構成してあり、原料ガス供給路L1から供給されたバイオガスのうち吸着材A11~A41に吸着され、濃縮後の高濃度の二酸化炭素を取出し可能に構成する。
前記膜分離装置Mは、分離膜M1をモジュールとして備え、雑ガス排出路L3を介して供給される雑ガスを膜分離して雑ガスに含まれる精製対象ガスを回収可能に構成してある。具体的には、原料ガスとしてバイオガスを用いて精製対象ガスとしてメタンを精製する場合、雑ガスとして二酸化炭素を主成分とし、メタンを含有するガスが膜分離装置Mに供給される。膜分離装置Mに供給された雑ガスは膜分離装置M内で分離膜M1と接触し、分離膜M1の膜分離特性により、二酸化炭素が分離膜M1を透過して除去されるとともに、不透過のガスとして、供給された雑ガスよりもメタンの濃縮された再生ガスが得られる。この再生ガスを再生ガス返送路L5に排出し、原料ガス供給路L1に返送供給する一方、膜を透過した二酸化炭素を主成分とするガスを、排気路L6より外部に排出する。
前記制御装置Cは、図3に示すように、前記各切換弁V11~V47および各ポンプP1,P6を制御して、図2にしたがって、各吸着塔A1~A4で、
前記原料ガス供給路L1から原料ガスを受け入れて、雑ガスを前記吸着材A11~A14に吸着するとともに、製品ガスを回収する吸着工程と、
吸着材A11~A14に吸着した二酸化炭素を主成分とする雑ガスを減圧脱着して前記雑ガス排出路L3より排気する脱着工程と、を交互に行う圧力揺動運転を行う。
吸着塔A1~A4下部から大気圧近傍のバイオガスの供給を受けて供給ポンプP1により前記吸着材A11~A41に供給し、二酸化炭素を主成分とする雑ガスを吸着するとともに、精製対象ガスとしてのメタンを主成分とする製品ガスを吸着塔A1~A4上部から放出する前記吸着工程の前後で、2塔の吸着塔A1~A4に同時に吸着工程を進行する並行吸着工程を行い、(前並行吸着工程、吸着工程、後並行吸着工程を順に行い、)
後並行吸着工程の後、高圧状態の吸着塔A1~A4内の、比較的雑ガス濃度の低いガスを、当該吸着塔A1~A4より低圧の中間圧状態の他の吸着塔A1~A4に移送して、吸着塔A1~A4内の圧力を高圧側の中間圧状態とする初段均圧(降圧)工程、
吸着塔A1~A4の動作を行わない待機工程、
低圧状態より高圧の中間圧状態の吸着塔A1~A4内の、初段均圧(降圧)工程に比べてメタン濃度のやや高められたガスを、低圧状態の他の吸着塔A1~A4に移送して、吸着塔A1~A4内の圧力を低圧側の中間圧状態とする最終均圧(降圧)工程と、
均圧(降圧)工程により塔内圧力が低下した後、さらに前記吸着材A11~A41を低圧状態まで減圧して、前記吸着材A11~A41に吸着された雑ガスを脱着させて吸着塔A1~A4下部から回収する脱着工程、
脱着工程により吸着材A11~A14の再生された吸着塔A1~A4内に残留する雑ガスを製品ガスで置換洗浄する洗浄工程
低圧状態の吸着塔A1~A4内に、前記高圧側の中間圧状態の吸着塔A1~A4内のガスを受け入れて、吸着塔A1~A4内の圧力を低圧側の中間圧状態とする初段均圧(昇圧)工程と、
待機工程と、
低圧側の中間圧状態の吸着塔A1~A4内に、高圧状態の他の吸着塔A1~A4内のガスを受け入れて、吸着塔A1~A4内の圧力を高圧側の中間圧状態とする最終均圧(昇圧)工程と、
均圧(昇圧)工程により塔内圧力を上昇した後、さらに、前記吸着塔A1~A4内に吸着塔A1~A4上部から昇圧用空気を供給して、前記吸着材A11~A41をメタンを選択的に吸着可能な高圧状態に復元する昇圧工程、
を順に行うように運転制御する。
図2、3に示すように第一吸着塔A1に、原料ガスタンクT1より原料ガスとしてのバイオガスを導入する。このとき第一吸着塔A1内の圧力は、原料ガスの供給圧により昇圧される。また、供給路L11の切換弁V11を介して原料ガスタンクT1から供給されるバイオガス中の雑ガスとしての二酸化炭素を前記吸着材A11に吸着させつつ、吸着しなかった製品ガスとしてのメタンを回収路L12の切換弁V12を介して製品ガスタンクT2に回収する。
ここで、吸着工程初期には、徐々に第一吸着塔A1内圧を上昇させるために、第四吸着塔A4の吸着工程の終了時期に徐々に第四吸着塔A4内圧を低下するのと合わせて、第一吸着塔A1の吸着工程を開始する。すなわち、第一吸着塔A1の吸着工程の開始に先立って、第四吸着塔A4の後並行吸着工程ととともに前並行吸着工程を行う。
図2、3に示すように、前記前並行吸着工程に続き、第一吸着塔A1に、原料ガスタンクT1よりバイオガスを導入する。このとき第一吸着塔A1内の圧力は、原料ガスの供給圧によりさらに昇圧される。また、供給路L11の切換弁V11を介して二酸化炭素を前記吸着材A11に吸着させつつ、メタンを製品ガスタンクT2に回収する。
また、第三吸着塔A3では、<1>脱着工程の後、<2>洗浄工程、<3>初段均圧(昇圧)工程を行っている。
さらに、第四吸着塔A4では、<1>初段均圧(降圧)工程を行うとともに、<2>待機工程を挟んで、<3>最終均圧(降圧)工程に移行している。
たとえば、円筒型(内径54mm、容積4.597L)の吸着塔A1を用い、
前記吸着材A11として、MP法によって細孔分布を測定した場合の細孔径分布が、細孔径0.38nm以上において、その細孔径における細孔容積(V0.40)が0.05cm3/g程度、細孔径0.34nmにおける細孔容積(V0.34)が0.20~0.23cm3/gであるモレキュラーシーブカーボンを用い、
10L/分でメタン約60%、二酸化炭素約40%のバイオガスを処理したところ、
吸着工程を、供給ポンプP1による供給圧を0.8MPaG程度として90秒間行った場合、メタン濃度96~98%、二酸化炭素濃度2%、圧力0.7~0.75MPaG程度の製品ガスを製品ガスタンクT2に回収することができた。
第一吸着塔A1の吸着工程の終期に、吸着工程始期の第二吸着塔A2と並行して吸着工程を行う後並行吸着工程を行う。すなわち、吸着工程におけるバイオガスの供給量と、本工程における第一、第二吸着塔A1,A2に対するバイオガス供給量の和が同量となるので、本工程では第一、第二吸着塔A1,A2に対するバイオガス供給量それぞれが、吸着工程におけるバイオガス供給量よりも少なく設定されることになる。したがって、図2、3に示すように、この工程では、吸着工程の終期に吸着流量を低下させることによって、吸着塔内の環境変化が穏やかに進行するように抑制することができ、吸着塔A1内のバイオガス流を安定させ、吸着塔A1内に乱流が生じるのを抑制し、吸着材A11を安定的に作用させることができる。
吸着工程を終えた第一吸着塔A1では、最終均圧(昇圧)工程を行う第三吸着塔A3との間で初段均圧(降圧)工程を行う。すなわち、図2、3に示すように、均圧路L17の切換弁V17を介して、塔内の非吸着ガスを排出し、洗浄路L34の切換弁V34を介して第三吸着塔A3に移送する構成となっている。これにより第一吸着塔A1は、図3に示すように、低圧側の中間圧状態の第三吸着塔A3と圧力平衡が行われる。
次に、第一吸着塔A1は待機状態となり、高圧側の中間圧状態が維持される。
次に、図2、3に示すように、第一吸着塔A1は、脱着工程を終え、初段均圧(昇圧)工程を行う第四吸着塔A4との間で最終均圧(降圧)工程を行う。すなわち、均圧路L17の切換弁V17を介して、塔内の非吸着ガスおよび吸着材A11から初期に脱着し始める雑ガスを排出し、洗浄路L44の切換弁V44を介して第四吸着塔A4に移送する構成となっている。これにより、第一吸着塔A1は、脱着工程を終えて低圧状態の第四吸着塔A4と圧力平衡が行われる。
図2、3に示すように、低圧側の中間圧状態に達した第一吸着塔A1は、塔内の吸着材A11に高濃度の雑ガスを吸着している状態になっており、塔内を低圧側の中間圧状態から低圧状態にまで減圧する脱着工程を行うことにより、吸着材A11に吸着された高濃度の雑ガスを回収する。すなわち、排ガス路L13の切換弁V13を介して濃縮された雑ガスを第一吸着塔A1の内圧により膜分離装置Mに供給する。
このときの膜分離装置Mの動作状態については後述する。
また第三吸着塔A3では、第二吸着塔A2と並行して<8>前並行吸着工程が行われた後、<9>吸着工程が行われる。
第四吸着塔A4では、<8>待機工程の後、第二吸着塔A2との間で<9>最終均圧(昇圧)工程が順に行われる。
図2、3に示すように、低圧状態に移行した第一吸着塔A1は、塔内に製品ガスを流入させることにより、塔内ガスをメタンを主成分とするガスに置換洗浄する。すなわち、製品ガス洗浄路L4の開閉弁Vo4を開成し、ニードル弁Vn4を調節して、洗浄路L14の切換弁V14を通じて製品ガスタンクT2から第一吸着塔A1に製品ガスを流入させて製品ガスタンクT2の内圧を吸着塔A1内に静かに作用させて、第一吸着塔A1内雰囲気をメタンに置換するとともに、第一吸着塔A1内に残留するガス排ガスとして排ガス路L13の切換弁V13を介して雑ガス排出路L3に放出するに供給する。
このとき、開閉弁Vo5を開成するとともに、開閉弁Vo3を閉成し、製品ガスを主成分とする洗浄ガスを、膜分離装置Mをバイパスして再生ガス返送路L5に移行させ、直接再生ガスタンクT5に回収する構成とする。
図2、3に示すように、低圧状態となって、吸着したメタンを放出し、吸着材A11を再生された第一吸着塔A1では、第二吸着塔A2との間で初段均圧(昇圧)工程を行うことにより、塔内の圧力を回復するとともに、第二吸着塔A2における最終均圧(降圧)工程で排出された、吸着材A11からの初期脱離ガスにより比較的メタンを高濃度に含有する排ガスを受け入れる。すなわち、塔間均圧路L7において、均圧路L27における切換弁V27を介して高圧側の中間圧状態の第二吸着塔A2から排出される塔内ガスを、洗浄路L14における切換弁V14より受け入れる。これにより第一吸着塔A1は、図3に示すように、低圧状態から低圧側の中間圧状態にまで圧力を回復する。
次に、図2、3に示すように、第一吸着塔A1は待機状態となり、高圧側の中間圧状態が維持される。
図2、3に示すように、低圧側の中間圧状態にまで圧力を回復した第一吸着塔A1は、次に吸着工程を終えた直後で初段均圧(降圧)工程を行う第三吸着塔A3との間で最終均圧(昇圧)工程を行うことにより、さらに塔内の圧力の回復を図る。すなわち、塔間均圧路L7の均圧路L17~L37において、切換弁V17、V37を介して、高圧状態の第三吸着塔A3から排出される塔内ガスを受け入れる。これにより第一吸着塔A1は、図3に示すように、低圧側の中間圧状態から高圧側の中間圧状態にまで圧力を回復する。
図3に示すように、高圧側の中間圧状態にまで圧力を回復した第一吸着塔A1は、製品ガスを圧入することにより高圧状態にまで圧力を復元される。すなわち、製品ガス洗浄路L4の切換弁V14を介して第一吸着塔A1に製品ガスを流入させる。これにより、第一吸着塔A1内部は高圧状態まで復元され、バイオガスを供給することによりバイオガス中の二酸化炭素を吸着可能な高圧状態に再生される。
雑ガス排出路L3には、分離膜M1を備えた膜分離装置Mが設けられ、雑ガス排出路L3から排出される二酸化炭素を主成分とする雑ガスから二酸化炭素を透過してメタンを分離可能に接続されている。分離膜M1を透過せず、メタン濃度の高められたガスは、再生ガスとして再生ガス返送路L5に排出され、分離膜M1を透過して、二酸化炭素を主成分とするガスは、減圧ポンプP6により排気路L6に放出可能に構成してある。
これに対して、上記膜分離装置を用いることなく、前記吸着塔を圧力揺動運転して、メタン濃縮を行ったところ、10L/分でメタン60%のバイオガスを処理した場合に、メタン96~98%の製品ガスを得ると、排ガスはメタン15~20%となり、メタンの回収率は83%であった。
すなわち、本発明のメタン濃縮方法によると、高い濃縮効率と高い回収率とを両立できることが実験的に明らかになった。
(1)
上記ガス精製装置には、圧力センサ、温度センサ等は適宜設けることができる。具体的には、通常、原料ガスの供給圧や、製品ガスのメタン濃度などをモニタする圧力センサやガスセンサを設けるのであるが、上述の実施形態においては詳細な説明を省略してあるものとする。
また、各配管にガスを流通させるための供給ポンプP1や減圧ポンプP6は、上記配置に限らず、ガス流通可能に構成されるのであれば種々変形することができる。具体的には、上述のガス精製装置では、必要最小限度の構成としてあるが、原料ガス供給路L1における再生ガス返送路L5との接続部分より上流側(原料ガスタンクT1側)に供給ポンプP1を設ける構成が採用できるほか、たとえば、供給ポンプP1を省略して、再生ガス返送路L5に原料ガス供給路L1に対して原料ガスの供給圧を与える圧縮ポンプP5を設けることとしてもよい。このような場合、たとえば、図5のように構成し、圧縮ポンプP5にバイパスするバイパス路に設けた圧力制御弁Vc51により、原料ガス供給路L1に対する供給圧を適正に維持する。
また、上述の実施形態の説明によると、排気路L6には、減圧ポンプP6を設けなくても動作可能であることが明らかであり、設備の簡素化の観点からは減圧ポンプP6を省略することが好ましく、膜分離圧の安定化の観点からは、減圧ポンプP6を設けることが好ましい。また、減圧ポンプP6を設ける場合、安定運転の観点からは、減圧ポンプP6を定常運転することが望ましいが、図2における洗浄工程が進行しているステップ3,7,11,15および、その後、脱着工程が開始されるまでのステップ4,8,12,16においては、減圧ポンプP6を低負荷運転、または、停止することができる。またこのような場合に、圧力制御弁Vc5は、開度を絞った状態あるいは閉止状態に固定しておくことができる。
上記実施形態において再生ガス返送路L5においては、ガス組成のバランスを図る上で、膜分離装置Mから回収するガス量が原料ガス供給路L1に再供給されるガス量を上回る状況も想定される。このような場合、再生ガスタンクT5に貯留されるガスは、増加し続けることになるので、前記再生ガスタンクT5に余剰再生ガスを廃棄するための廃棄路を設けておくこともできる。
先にも述べたように、洗浄工程の際に雑ガス排出路L3に流通するガスは、製品ガスが主成分であるから、膜分離工程後、直接製品ガスとして回収してもかまわない程度の純度である場合もある。また、通常の脱着工程における再生ガスであっても、同様に十分な純度である場合がある。このような場合、図6に示すように、再生ガス返送路L5に、再生ガスを製品ガスとして回収するための再生ガス回収路L9を設けて、圧入ポンプP9を介して製品ガス回収路L2にバイパスさせることもできる。このような場合、雑ガス排出路L3に流通するガスの組成等に応じて、再生ガスの流通先を再生ガス返送路L5→原料ガス供給路L1にするか再生ガス回収路L9→製品ガスタンクT2にするか分岐制御すればよい。すなわち、再生ガスの製品ガス純度が高い場合には、再生ガスを再生ガス回収路L9を介して製品ガスタンクT2に回収し、再生ガスの製品ガス純度が低いときには再生ガス返送路L5を介して原料ガス供給路L1に返送する形態とすることができる。
なお、たとえば、(1)常に、再生ガスを製品ガスとして回収してよい製品ガス純度に維持できるような場合、または、(2)再生ガスが、原料ガスより高純度である場合、もしくは、(3)再生ガスに原料ガスを適量添加することで発電用燃料として十分に使用可能になる程度の純度を有している場合などは、再生ガス返送路L5を省略して、再生ガス回収路L9のみ設けることもできる(図13参照)。
上記実施形態では4塔の吸着塔A1~A4を備えたガス精製装置としたが、これに限らず2塔、3塔で交互に処理する方式のものであっても良く、複数塔備えて連続的なPSAが行える構成であればよい。たとえば、3塔であれば、図7のように構成することができる。
PSAサイクルとしては、各吸着塔を連続的に有効に利用できる形態であれば上述の構成に限るものではなく、種々変形を行うことができる。たとえば、上記図7の構成のガス精製装置であれば、図8に従った運転方法が可能である。
前の実施形態では、洗浄工程の際に前記吸着塔に対して静圧(圧力をかけない)で製品ガスを供給したが、加圧状態で洗浄工程を行うこともできる。この場合、洗浄効率を向上できる。
本発明のガス精製装置は、バイオガスの精製に用いる例を示したが、バイオガス以外にもたとえば炭鉱ガスなど、バイオガス同様に含有するメタンを高濃度に濃縮する場合や、他にも、原料ガスから精製対象ガス以外の雑ガスを吸着することにより精製する用途で用いることができ、この際、精製対象ガス、雑ガスの種類、濃度に応じて、吸着剤、分離膜の材料を適宜変更することができる。
先の実施形態の構成に加えて、図9に示すように、前記雑ガス排出路L3における前記膜分離装置Mの上流部に、バッファタンクT3を設けて構成することができる。なお、Vc52は、バッファタンクT3内の圧力を適宜吸着塔A1~A4の内圧よりも低く維持するための圧力制御弁である。また、図9中L9は、図6における再生ガス回収路L9と同様に、圧入ポンプP9を介して製品ガス回収路L2に再生ガスを回収する管路であることを同様の符号を付して示すものである。
なお、常に、再生ガスを製品ガスとして回収してよい製品ガス純度に維持できるような場合、再生ガス返送路L5を省略して、再生ガス回収路L9のみ設けることもできる。
前の実施形態における図2~4の構成のガス精製装置における配管、弁構成を簡略化することによって、図10~12に従った運転方法を行うことができる。
すなわち、図10~12の構成によると、製品ガスによる吸着塔の昇圧を省略し、原料ガスにより昇圧することにより、製品ガス昇圧路L8を不要とするとともに、洗浄工程を不要にできることから、製品ガス洗浄路L4を不要としている。このとき、昇圧による製品ガスのロスを節約できるので、製品ガス回収率を向上することができる。また、後並行吸着工程ののち待機工程を設けることで、圧力変動を一旦中断させることにより、図4において最大圧力から最少圧力まで3段階で変動していたところ、図12において4段階でより緩慢に変動することになり、吸着塔内に急激な圧力変動を生じないのでより安定したガス精製装置の運転に寄与する。
A11~A41:吸着材
C :制御装置
L1 :原料ガス供給路
L2 :製品ガス回収路
L3 :雑ガス排出路
L4 :製品ガス洗浄路
L5 :再生ガス返送路
L6 :排気路
L7 :塔間均圧路
L8 :製品ガス昇圧路
L9 :再生ガス回収路
L10、L30:バイパス路
L11~L41:供給路
L12~L42:回収路
L13~L43:排ガス路
L14~L44:洗浄路
L17~L47:均圧路
L18~L48:昇圧路
M :膜分離装置
M1 :分離膜
P1 :供給ポンプ
P5 :圧縮ポンプ
P6 :減圧ポンプ
P9 :圧入ポンプ
T1 :原料ガスタンク
T2 :製品ガスタンク
T5 :再生ガスタンク
V11~V44:切換弁
Vc1~Vc8:圧力制御弁
Vn4、Vn7:ニードル弁
Vo3~Vo8:開閉弁
Vr4 :減圧弁
Claims (14)
- 原料ガスから精製対象ガス以外の雑ガスを吸着する吸着材を充填してある吸着塔を設け、
前記吸着塔に原料ガスを供給する原料ガス供給路を設け、
前記吸着材に吸着しなかった精製対象ガスを製品ガスとして排出する製品ガス回収路を設け、
前記吸着材に吸着した雑ガスを脱着させて排気する雑ガス排出路を設け、
前記吸着塔と、前記原料ガス供給路と、前記製品ガス回収路と、前記雑ガス排出路とを、
前記原料ガス供給路から原料ガスを受け入れて、雑ガスを前記吸着材に吸着するとともに、製品ガスを回収する吸着工程と、
前記吸着材に吸着した雑ガスを減圧脱着して前記雑ガス排出路より排気する脱着工程と、
を交互に行う圧力揺動運転可能に接続したガス精製装置であって、
前記雑ガス排出路に、精製対象ガスを透過せず、雑ガスを透過する分離膜を有するとともに、前記吸着塔の排気圧で精製対象ガスと雑ガスとを分離する膜分離装置を設け、
分離膜で精製対象ガス濃度の高められた再生ガスを前記原料ガス供給路に返送する再生ガス返送路及び/又は製品ガスとして回収する再生ガス回収路を設けたガス精製装置。 - 前記雑ガス排出路に、精製対象ガスを透過せず、雑ガスを透過する分離膜を有するとともに、前記吸着塔の排気圧で精製対象ガスと雑ガスとを分離する膜分離装置を設け、
分離膜で精製対象ガス濃度の高められた再生ガスを前記原料ガス供給路に返送する再生ガス返送路を設け、
前記雑ガス排出路に流通する雑ガスを、前記膜分離装置をバイパスして前記再生ガス返送路に導くバイパス路を設けた請求項1に記載のガス精製装置。 - 前記雑ガス排出路における前記膜分離装置の上流部に、バッファタンクを設けてある請求項1または2に記載のガス精製装置。
- 前記雑ガス排出路における前記膜分離装置の雑ガス透過側に減圧ポンプを設けてある請求項1~3のいずれか一項に記載のガス精製装置。
- 前記再生ガス返送路に再生ガスタンクを設けてある請求項1~4のいずれか一項に記載のガス精製装置。
- 前記再生ガス返送路に再生圧力制御弁を設け、前記再生圧力制御弁により前記分離膜の膜分離圧を制御する再生制御装置を備えた請求項1~5のいずれか一項に記載のガス精製装置。
- 前記製品ガス回収路に製品ガスタンクを設けてある請求項1~6のいずれか一項に記載のガス精製装置。
- 前記製品ガスタンクから前記吸着塔に製品ガスを流入する製品ガス洗浄路を設け、製品ガス洗浄路における前記製品ガスタンクと前記吸着塔との間に製品圧力制御弁を設け、前記製品ガスタンクから製品ガスを前記吸着塔に流入させて前記吸着塔を洗浄する洗浄制御装置を備えた請求項7に記載のガス精製装置。
- 前記原料ガスがメタン含有ガスであり、精製対象ガスがメタンであり、雑ガスが二酸化炭素を主成分とするガスである請求項1~8のいずれか一項に記載のガス精製装置。
- 前記原料ガスが、精製対象ガスとしてメタンを40%以上含有するメタン含有ガスであり、メタンを90%以上含有する製品ガスを得る請求項1~9のいずれか一項に記載のガス精製装置。
- 前記吸着材が活性炭、モレキュラーシーブカーボン、ゼオライト、多孔性の金属錯体から選ばれる少なくとも一種の材料を主成分とするものである請求項1~10のいずれか一項に記載のガス精製装置。
- 前記吸着材が、MP法で測定した細孔径0.38nm以上において、その細孔径における細孔容積(V0.40)が0.01cm3/gを超えず、細孔径0.34nmにおける細孔容積(V0.34)が0.20cm3/g以上であるモレキュラーシーブカーボンである請求項11に記載のガス精製装置。
- 前記分離膜が酢酸セルロース、ポリアミド、ポリイミド、ポリスルホン、ポリテトラフルオロエチレン、ポリエーテルスルホン、カーボン膜、微多孔質ガラス複合膜、DDR型ゼオライト、多分岐ポリイミドシリカ、ポリジメチルシロキサンから選ばれる少なくとも一種の材料を主成分とするものである請求項1~12のいずれか一項に記載のガス精製装置。
- 前記原料ガス供給路に昇圧ポンプを備え、前記昇圧ポンプによる原料ガスの前記吸着塔に対する供給圧が0.5MPaG~2MPaGである請求項1~13のいずれか一項に記載のガス精製装置。
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SG11201504518SA SG11201504518SA (en) | 2012-12-28 | 2013-12-26 | Gas purification apparatus |
JP2014554548A JP6305938B2 (ja) | 2012-12-28 | 2013-12-26 | ガス精製装置 |
PH12015501485A PH12015501485A1 (en) | 2012-12-28 | 2015-06-26 | Gas purification apparatus |
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MY (1) | MY176621A (ja) |
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Cited By (7)
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KR20160113969A (ko) * | 2015-03-23 | 2016-10-04 | 스미또모 세이까 가부시키가이샤 | 헬륨 가스의 정제 방법 및 정제 시스템 |
JP6091681B1 (ja) * | 2016-03-31 | 2017-03-08 | 大阪瓦斯株式会社 | 圧力変動吸着式ガス製造装置 |
JP6091682B1 (ja) * | 2016-03-31 | 2017-03-08 | 大阪瓦斯株式会社 | 圧力変動吸着式ガス製造装置 |
JP6091683B1 (ja) * | 2016-03-31 | 2017-03-08 | 大阪瓦斯株式会社 | 圧力変動吸着式ガス製造装置 |
CN109260905A (zh) * | 2018-09-28 | 2019-01-25 | 合肥鸿叶紫新能源有限公司 | 一种新能源领域的可燃气湿式净化设备 |
TWI673100B (zh) * | 2018-03-22 | 2019-10-01 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | 吸附塔的切換裝置 |
FR3097450A1 (fr) * | 2019-06-20 | 2020-12-25 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Traitement d’un flux de méthane comprenant des COV et du dioxyde de carbone par combinaison d’une unité d’adsorption et d’une unité de séparation par membrane |
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Cited By (18)
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JP2016175815A (ja) * | 2015-03-23 | 2016-10-06 | 住友精化株式会社 | ヘリウムガスの精製方法および精製システム |
KR102446032B1 (ko) | 2015-03-23 | 2022-09-21 | 스미또모 세이까 가부시키가이샤 | 헬륨 가스의 정제 방법 및 정제 시스템 |
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WO2017169688A1 (ja) * | 2016-03-31 | 2017-10-05 | 大阪瓦斯株式会社 | 圧力変動吸着式ガス製造装置 |
JP2017177068A (ja) * | 2016-03-31 | 2017-10-05 | 大阪瓦斯株式会社 | 圧力変動吸着式ガス製造装置 |
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WO2017169690A1 (ja) * | 2016-03-31 | 2017-10-05 | 大阪瓦斯株式会社 | 圧力変動吸着式ガス製造装置 |
JP6091682B1 (ja) * | 2016-03-31 | 2017-03-08 | 大阪瓦斯株式会社 | 圧力変動吸着式ガス製造装置 |
WO2017169689A1 (ja) * | 2016-03-31 | 2017-10-05 | 大阪瓦斯株式会社 | 圧力変動吸着式ガス製造装置 |
JP6091683B1 (ja) * | 2016-03-31 | 2017-03-08 | 大阪瓦斯株式会社 | 圧力変動吸着式ガス製造装置 |
JP6091681B1 (ja) * | 2016-03-31 | 2017-03-08 | 大阪瓦斯株式会社 | 圧力変動吸着式ガス製造装置 |
US10710019B2 (en) | 2016-03-31 | 2020-07-14 | Osaka Gas Co., Ltd. | Pressure swing adsorption type of gas production device |
TWI673100B (zh) * | 2018-03-22 | 2019-10-01 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | 吸附塔的切換裝置 |
CN109260905A (zh) * | 2018-09-28 | 2019-01-25 | 合肥鸿叶紫新能源有限公司 | 一种新能源领域的可燃气湿式净化设备 |
FR3097450A1 (fr) * | 2019-06-20 | 2020-12-25 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Traitement d’un flux de méthane comprenant des COV et du dioxyde de carbone par combinaison d’une unité d’adsorption et d’une unité de séparation par membrane |
EP3756749A1 (fr) * | 2019-06-20 | 2020-12-30 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Traitement d'un flux de méthane comprenant des cov et du dioxyde de carbone par combinaison d'une unité d'adsorption et d'une unité de séparation par membrane |
US11351499B2 (en) | 2019-06-20 | 2022-06-07 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Treatment of a methane stream comprising VOCs and carbon dioxide by a combination of an adsorption unit and a membrane separation unit |
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JP6305938B2 (ja) | 2018-04-04 |
SG10201705168PA (en) | 2017-07-28 |
SG11201504518SA (en) | 2015-07-30 |
JPWO2014104196A1 (ja) | 2017-01-19 |
PH12015501485B1 (en) | 2015-09-21 |
PH12015501485A1 (en) | 2015-09-21 |
MY176621A (en) | 2020-08-18 |
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