WO2021207903A1 - 一种移动式变压吸附氧气生产装置的方法 - Google Patents

一种移动式变压吸附氧气生产装置的方法 Download PDF

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Publication number
WO2021207903A1
WO2021207903A1 PCT/CN2020/084582 CN2020084582W WO2021207903A1 WO 2021207903 A1 WO2021207903 A1 WO 2021207903A1 CN 2020084582 W CN2020084582 W CN 2020084582W WO 2021207903 A1 WO2021207903 A1 WO 2021207903A1
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adsorption
oxygen
pressure swing
adsorption tower
section
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PCT/CN2020/084582
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English (en)
French (fr)
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宋宇文
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成都盈辰科技有限公司
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Priority to CN202080001896.9A priority Critical patent/CN112041264B/zh
Priority to PCT/CN2020/084582 priority patent/WO2021207903A1/zh
Publication of WO2021207903A1 publication Critical patent/WO2021207903A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
    • C01B13/02—Preparation of oxygen
    • C01B13/0229—Purification or separation processes
    • C01B13/0248—Physical processing only
    • C01B13/0259—Physical processing only by adsorption on solids
    • 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
    • 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
    • B01D53/26—Drying gases or vapours
    • B01D53/261—Drying gases or vapours by adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/12—Oxygen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/80—Water
    • 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
    • B01D2259/40062—Four

Definitions

  • the invention relates to the field of pressure swing adsorption technology oxygen production, in particular to a method for a mobile pressure swing adsorption oxygen production device.
  • the pure oxygen used in the gas cutting process is produced by a cryogenic device.
  • the pure oxygen is compressed to 12.5MPa or more with a compressor and loaded into a special 40-liter steel cylinder, and then transported to each user.
  • the operating pressure is lower than 0.95MPa, which consumes a lot of manpower and material resources, not only the cost of oxygen is high, but also the safety is poor.
  • the present invention aims to provide a method for a mobile PSA oxygen production device that is small in size, light in weight, open and stopped at any time, easy to use, and low in pressure, which greatly reduces the cost of oxygen and improves the safety of oxygen use. sex.
  • the purpose of the present invention is achieved through the following technical solutions:
  • a method for a mobile pressure swing adsorption oxygen production device adopts two stages of pressure swing adsorption in series operation.
  • the raw material air without gaseous water first enters the nitrogen balance selective adsorbent from the bottom of the adsorption tower of the first pressure swing adsorption section In the bed, most of the nitrogen in the raw air is adsorbed by the nitrogen balance selective adsorbent bed, and most of the oxygen and argon flow out of the adsorption tower outlet and enter the speed selective adsorbent bed from the bottom of the adsorption tower in the second pressure swing adsorption section
  • the oxygen-rich layer is adsorbed by the speed-selective adsorbent bed.
  • the adsorption tower of the first pressure swing adsorption section sequentially undergoes four pressure swing adsorption process steps in one cycle: adsorption A, equal pressure drop ED, reverse discharge BD or vacuum VC, and equal pressure rise ER; the second pressure swing adsorption section
  • the adsorption tower in a cycle sequentially undergoes the process steps of adsorption A, product oxygen replacement P, vacuum VC, and series adsorption A1 pressure swing adsorption.
  • the adsorption tower of the second pressure swing adsorption section adds a series replacement P1 step after the adsorption A step, and the replacement gas of this series replacement step comes from the mixed gas discharged from the outlet of another adsorption tower in the product oxygen replacement P step.
  • the adsorption tower of the first pressure swing adsorption stage adds a final pressure boosting FR step after the equalizing pressure raising ER step, and the boosted gas in this step comes from the oxygen-rich mixed gas at the outlet of the first stage adsorption tower adsorption A step.
  • the raw material air may contain gaseous water, in order to ensure the adsorption effect of the nitrogen balance selective adsorbent bed in the first pressure swing adsorption section, the raw material air needs to be dried.
  • the present invention provides two solutions :
  • Scheme 2 Add a pressure swing adsorption drying section before the first pressure swing adsorption section to remove gaseous water in the air to meet the moisture requirements of the adsorption tower entering the first pressure swing adsorption section.
  • the pressure swing adsorption drying section sequentially undergoes two pressure swing adsorption process steps of adsorption A and purge P in one cycle.
  • the gas of the purge P step comes from the outlet of the adsorption step A of the adsorption tower of the first pressure swing adsorption section.
  • the air and the adsorption tower of the second pressure swing adsorption section decompose the air.
  • the drying section is filled with activated alumina as a desiccant; the adsorption tower of the first pressure swing adsorption section is filled with 5A molecular sieves or X-type lithium molecular sieves as nitrogen balance selective adsorbents; the adsorption tower of the second pressure swing adsorption section is filled with carbon molecular sieves Speed selective adsorbent.
  • the pressure of the adsorption tower adsorption step A of the first pressure swing adsorption section and the second pressure swing adsorption section is 0.005-0.2 MPa (gauge pressure).
  • the concentration of oxygen in the outlet gas at the end of the adsorption step A of the adsorption tower of the first pressure swing adsorption section is 70-80% (V).
  • the adsorption tower of the first pressure swing adsorption section is filled with 5A molecular sieves or X-type lithium molecular sieves; the adsorption tower of the second pressure swing adsorption section is filled with carbon molecular sieves.
  • the mobile pressure swing adsorption pure oxygen production device provided by the method of the present invention greatly reduces the cost of oxygen, and the safety is greatly improved.
  • the mobile pressure swing adsorption pure oxygen production device is small in size, light in weight, and stops at any time. , Easy to use, the maximum pressure is only 1.2MPa.
  • Fig. 1 is a timing diagram of the operation steps of each stage of the adsorption tower and the switching of the programmable valve in the embodiment 1 of the present invention.
  • Figure 2 is a process flow diagram of Example 1 of the present invention.
  • Fig. 3 is a time sequence diagram of the operation steps of each stage of the adsorption tower and the switch of the programmable valve in the second embodiment of the present invention.
  • Figure 4 is a process flow diagram of Example 2 of the present invention.
  • Fig. 5 is a time sequence diagram of the operation steps of each stage of the adsorption tower and the switching of the programmable valve in the embodiment 3 of the present invention.
  • Fig. 6 is a process flow diagram of Example 3 of the present invention.
  • Fig. 7 is a time sequence diagram of the operation steps of each stage of the adsorption tower and the switching of the programmable valve in the embodiment 4 of the present invention.
  • Fig. 8 is a process flow diagram of Example 4 of the present invention.
  • Fig. 1 is a timing diagram of the operation steps of each stage of the adsorption tower and the switching of the programmable valve in the embodiment 1 of the present invention.
  • Figure 2 is a process flow diagram of Example 1 of the present invention.
  • vacuum pump P0101, vacuum buffer tank V0101, programmable valve, PLC control system, instrumentation, process piping and fittings, adsorption tower T0101A and T0101B constitute the first pressure swing adsorption section, and the adsorbent filled in the adsorption tower is 5A Molecular sieve or lithium molecular sieve, run single tower adsorption, pressure equalization and vacuuming procedures; pure oxygen vacuum pump P0201, pure oxygen compressor C0201, oxygen-enriched buffer tank V0201, compressor buffer tank V0202, product pure oxygen buffer tank V0203, programmable valve,
  • the PLC control system, instrumentation, process pipe fittings, adsorption towers T0201A, T0201B, T0201C and T0201D constitute the second pressure swing adsorption section.
  • the adsorbent filled in the adsorption tower is carbon molecular sieve, and the single-tower adsorption, replacement and vacuuming procedures are run.
  • the above-mentioned two pressure swing adsorption stages are operated in series.
  • the first pressure swing adsorption stage adsorbs nitrogen in the air
  • the second pressure swing adsorption stage is used to adsorb the enrichment obtained in step A by the adsorption tower of the first pressure swing adsorption stage.
  • the oxygen in the oxygen mixture is absorbed and the oxygen is increased to above 99.5% (V).
  • Dry air with a pressure greater than 5KPa enters the adsorption tower in the first pressure swing adsorption section in the adsorption step.
  • the adsorbent in the adsorption tower selectively adsorbs nitrogen and other components in the air, and oxygen and argon that are difficult to adsorb from the outlet end
  • the adsorbent in the adsorption tower selectively adsorbs oxygen and other components in the oxygen-rich mixed gas, and the components such as nitrogen and argon that are not easily adsorbed flow out from the outlet end and enter the second adsorption tower.
  • the pressure is increased and oxygen is adsorbed, the pressure is increased to the adsorption pressure and the oxygen is adsorbed, and then vented.
  • pressure equalization is performed and then vacuum is drawn. The nitrogen and a small amount of oxygen drawn by the vacuum pump are vented.
  • the product is replaced with oxygen. After the replacement, vacuum is performed, and part of the extracted high-concentration oxygen is used as the product after being compressed and enters the product pure oxygen buffer tank, and the other part is used to replace the adsorbent bed after the adsorption is completed.
  • the oxygen concentration in the outlet gas of the adsorption tower of the first pressure swing adsorption section is controlled to be above 70% (V) during the adsorption process, and the adsorption tower undergoes adsorption A, equalization pressure drop ED, vacuum VC, and equalization pressure in a cycle.
  • V 70%
  • the oxygen concentration in the outlet gas is controlled above 60-70% (V)
  • Product oxygen replacement P, vacuum VC and series adsorption A1 four pressure swing adsorption process steps.
  • the total oxygen recovery rate is about 60%
  • the two-stage circulation time is generally 20-80 seconds
  • the first stage vacuum is -0.07MPa
  • the air volume of the blower the empty tower speed of the two-stage adsorption tower
  • the suction volume of the vacuum pump the amount of adsorbent
  • the diameter of the adsorption tower and other design parameters are designed according to the usual conditions in the field of pressure swing adsorption technology.
  • Each adsorption tower in each stage of the present invention sequentially undergoes the following steps in a cycle.
  • each adsorption tower of the first stage sequentially undergoes the following steps in a cycle:
  • the dry air boosted to 5KPa enters the adsorption tower T0101A to increase the pressure
  • the adsorption pressure is increased
  • the adsorbent in the adsorption tower selectively adsorbs nitrogen in the air sequentially
  • the components such as oxygen and argon that are not easily adsorbed open the program-controlled valve KV2A-1 and are discharged from the outlet end into the oxygen-enriched buffer tank V0201.
  • the oxygen-enriched concentration is controlled above 70%.
  • the adsorbent adsorbs nitrogen The total amount continues to increase. When the adsorbent is saturated with nitrogen, the gas flow is stopped, and the adsorption is over.
  • the adsorption tower T0101A completes a cycle and enters the raw gas adsorption again.
  • the steps and sequence of the other adsorption tower are exactly the same as the adsorption tower T0101A, except that they are staggered in time.
  • the adsorbent in T0201A is selectively enriched with oxygen and other components in the oxygen mixture, and the unadsorbed part of oxygen and the difficult-to-adsorb nitrogen and argon tail gas flow out from the outlet end into the bottom of the adsorption tower T0201B to increase the pressure, and when it rises to the adsorption pressure
  • the programmable valve KV2B-2 is opened, the unadsorbed nitrogen and argon are vented from the outlet of the adsorption tower T0201B. With the passage of time, the total amount of oxygen adsorbed by the adsorbent continues to increase.
  • the oxygen concentration in the outlet gas is controlled at 60-70% (V).
  • the adsorption step A After the adsorption step A is completed, close the program-controlled valves KV1A-2, KV4A-2 and KV2B-2, and open the program-controlled valves KV3A-2 and KV6A-2.
  • the product oxygen enters the top of the adsorbent bed from the bottom of the adsorption tower T0201A and flows out from the top.
  • the mixed gas returns to the inlet of the first pressure swing adsorption section and is mixed with the oxygen-rich mixed gas obtained in the adsorption tower adsorption step A of the first pressure swing adsorption section, and then enters the adsorption tower of the second pressure swing adsorption section as raw material for adsorption.
  • the oxygen concentration in the outlet gas is controlled to be above 98% (V).
  • the adsorption tower T0201A completes a cycle and enters the oxygen-rich feed gas adsorption again.
  • the steps and sequence of the other three adsorption towers are exactly the same as the adsorption tower T0201A, but they are staggered in time.
  • Fig. 3 is a time sequence diagram of the operation steps of each stage of the adsorption tower and the switch of the programmable valve in the second embodiment of the present invention.
  • Figure 4 is a process flow diagram of Example 2 of the present invention.
  • the adsorbent in the adsorption tower is carbon molecular sieve, and a single tower is operated in series adsorption, series replacement and Vacuum procedure.
  • the above-mentioned two pressure swing adsorption stages are operated in series.
  • the first pressure swing adsorption stage adsorbs nitrogen in the air, and the second pressure swing adsorption stage is used to adsorb the enrichment obtained in step A by the adsorption tower of the first pressure swing adsorption stage.
  • the oxygen in the oxygen mixture is absorbed and the oxygen is increased to above 99.5% (V).
  • Dry air with a pressure greater than 5KPa enters the adsorption tower in the first pressure swing adsorption section in the adsorption step.
  • the adsorbent in the adsorption tower selectively adsorbs nitrogen and other components in the air, and oxygen and argon that are difficult to adsorb from the outlet end
  • the adsorbent in the adsorption tower selectively adsorbs oxygen and other components in the oxygen-rich mixed gas, and the components such as nitrogen and argon that are not easily adsorbed flow out from the outlet end and enter the second adsorption tower.
  • the pressure is increased and oxygen is adsorbed, the pressure is increased to the adsorption pressure and the oxygen is adsorbed, and then vented.
  • the pressure is equalized and then vacuumed. The nitrogen and a small amount of oxygen drawn by the vacuum pump are vented.
  • the oxygen concentration in the outlet gas is controlled to be above 70%(V).
  • Its adsorption tower undergoes four pressure swing adsorption process steps in sequence: adsorption A, equalized pressure drop ED, vacuum VC, and equalized pressure rise in a cycle; the second pressure swing adsorption section is in the adsorption step, the concentration of oxygen in the outlet gas of the adsorption tower Controlled to be close to the oxygen concentration of the raw gas, the adsorption tower undergoes five pressure swing adsorption process steps in a cycle: adsorption A, series replacement P1, product oxygen replacement P, vacuum VC, and series adsorption A1.
  • the total oxygen recovery rate is about 60%
  • the two-stage circulation time is generally 20-80 seconds
  • the first stage vacuum is -0.07MPa
  • the air volume of the blower the empty tower speed of the two-stage adsorption tower
  • the suction volume of the vacuum pump the amount of adsorbent
  • the diameter of the adsorption tower and other design parameters are designed according to the usual conditions in the field of pressure swing adsorption technology.
  • Each adsorption tower in each stage of the present invention sequentially undergoes the following steps in a cycle.
  • each adsorption tower of the first stage sequentially undergoes the following steps in a cycle:
  • the dry air boosted to 5KPa enters the adsorption tower T0101A to increase the pressure
  • the adsorption pressure is increased
  • the adsorbent in the adsorption tower selectively adsorbs nitrogen in the air sequentially
  • the components such as oxygen and argon that are not easily adsorbed open the program-controlled valve KV2A-1 and are discharged from the outlet end into the oxygen-enriched buffer tank V0201.
  • the oxygen-enriched concentration is controlled above 70%.
  • the adsorbent adsorbs nitrogen The total amount continues to increase. When the adsorbent is saturated with nitrogen, the gas flow is stopped, and the adsorption ends.
  • the adsorption tower T0101A completes a cycle and enters the raw gas adsorption again.
  • the steps and sequence of the other adsorption tower are exactly the same as the adsorption tower T0101A, except that they are staggered in time.
  • the adsorbent in T0201A is selectively enriched with oxygen and other components in the oxygen mixture, and the unadsorbed part of oxygen and the difficult-to-adsorb nitrogen and argon tail gas flow out from the outlet end into the bottom of the adsorption tower T0201B to increase the pressure, and when it rises to the adsorption pressure
  • the programmable valve KV2B-2 is opened, the unadsorbed nitrogen and argon are vented from the outlet of the adsorption tower T0201B.
  • the total amount of adsorbed oxygen by the adsorbent increases continuously.
  • the adsorption tower T0201A When the adsorption tower T0201A is saturated with oxygen, it stops Air intake, the adsorption is over at this time. After the adsorption step of the adsorption tower is completed, the oxygen concentration in the outlet gas is controlled at 60-70% (V).
  • the product oxygen enters the adsorbent bed from the bottom of the adsorption tower T0201E to replace the nitrogen And argon, and then flow out from the top, the replacement tail gas from the top enters from the bottom of the adsorption tower T0201A, after passing through the adsorption tower T0201A adsorbent bed to adsorb oxygen, it returns to the second stage inlet and the first variable pressure through the programmable valve KV2A-2
  • the oxygen-rich gas obtained in the adsorption step of the adsorption tower of the adsorption section is mixed.
  • the oxygen concentration in the outlet gas is controlled at 60-80% (V).
  • the serial replacement step P1 After the serial replacement step P1 is completed, close the program-controlled valves KV6E-2, KV3E-2, and KV2A-2, and open the program-controlled valves KV3A-2 and KV6A-2.
  • the product oxygen enters the adsorbent bed from the bottom of the adsorption tower T0201A to replace nitrogen and argon. , And then flow out from the top, the replacement tail gas from the top enters from the bottom of the adsorption tower T0201B, passes through the adsorption tower T0201B adsorbent bed to adsorb oxygen, and then vents through the programmable valve KV2B-2.
  • the oxygen concentration in the outlet gas is controlled to be above 98% (V).
  • the adsorption tower T0201A completes a cycle and enters the oxygen-rich feed gas adsorption again.
  • the steps and sequence of the other four adsorption towers are exactly the same as the adsorption tower T0201A, but they are staggered in time.
  • Fig. 5 is a time sequence diagram of the operation steps of each stage of the adsorption tower and the switch of the programmable valve in the embodiment 3 of the present invention.
  • Fig. 6 is a process flow diagram of Example 3 of the present invention.
  • the vacuum pump P0101, vacuum buffer tank V0101, programmable valve, PLC control system, instrumentation, process pipe fittings, adsorption towers T0101A, T0101B and T0101C constitute the first pressure swing adsorption section, and the adsorbent filled in the adsorption tower It is 5A molecular sieve or lithium molecular sieve, running single tower adsorption, pressure equalization and vacuuming procedures; pure oxygen vacuum pump P0201, pure oxygen compressor C0201, compressor buffer tank V0202, product pure oxygen buffer tank V0203, programmable valve, PLC control system, Instrumentation, process piping and fittings, adsorption towers T0201A, T0201B, T0201C and T0201D constitute the second pressure swing adsorption section.
  • the adsorbent filled in the adsorption tower is carbon molecular sieve, and the single-tower adsorption, displacement and vacuuming procedures are run.
  • the above-mentioned two stages of pressure swing adsorption are operated in series.
  • the first pressure swing adsorption stage adsorbs nitrogen in the air
  • the second pressure swing adsorption stage is used to adsorb the enrichment obtained in step A by the adsorption tower of the first pressure swing adsorption stage.
  • the oxygen in the oxygen mixture is absorbed and the oxygen is increased to above 99.5% (V).
  • Dry air with a pressure greater than 5KPa enters the adsorption tower in the first pressure swing adsorption section in the adsorption step.
  • the adsorbent in the adsorption tower selectively adsorbs nitrogen and other components in the air, and oxygen and argon that are difficult to adsorb from the outlet end
  • the adsorbent in the adsorption tower selectively adsorbs oxygen and other components in the oxygen-rich mixed gas, and the components such as nitrogen and argon that are not easily adsorbed flow out from the outlet end and enter the second adsorption tower.
  • the pressure is increased and oxygen is adsorbed, the pressure is increased to the adsorption pressure and the oxygen is adsorbed, and then vented.
  • pressure equalization is performed and then vacuum is drawn. The nitrogen and a small amount of oxygen drawn by the vacuum pump are vented.
  • the product is replaced with oxygen. After the replacement, vacuum is performed, and part of the extracted high-concentration oxygen is used as the product after being compressed and enters the product pure oxygen buffer tank, and the other part is used to replace the adsorbent bed after the adsorption is completed.
  • the oxygen concentration in the outlet gas is controlled above 70% (V).
  • the adsorption tower undergoes adsorption A, equalization pressure drop ED, vacuum VC, equalization pressure in a cycle.
  • the cycle undergoes four pressure swing adsorption process steps, namely adsorption A, product oxygen replacement P, vacuum VC, and series adsorption A1.
  • the total oxygen recovery rate is about 60%
  • the two-stage circulation time is generally 20-80 seconds
  • the first stage vacuum is -0.07MPa
  • the air volume of the blower the empty tower speed of the two-stage adsorption tower
  • the suction volume of the vacuum pump the amount of adsorbent
  • the diameter of the adsorption tower and other design parameters are designed according to the usual conditions in the field of pressure swing adsorption technology.
  • Each adsorption tower in each stage of the present invention sequentially undergoes the following steps in a cycle.
  • each adsorption tower of the first stage sequentially undergoes the following steps in a cycle:
  • the adsorbent in the adsorption tower T0101A is selectively nitrogen and other components, and the unadsorbed part Nitrogen and components such as oxygen and argon that are not easily adsorbed flow out from the outlet end into the adsorption tower in the second pressure swing adsorption section in the adsorption step. As time goes by, the total amount of nitrogen and other components adsorbed by the adsorbent continues to increase. When the adsorption tower T0101A is saturated with nitrogen, stop the gas supply and the adsorption is over. During the adsorption step A of the adsorption tower, the oxygen concentration in the outlet gas is controlled above 70% (V).
  • the dead space gas in the adsorption tower T0101A is discharged from the adsorption tower outlet into the adsorption tower T0101C that has completed the vacuum VC step in this section to increase the pressure, try to make the pressure of the two towers equal.
  • the programmable valve KV4A-1 is opened, the nitrogen adsorbed in the adsorption tower T0101A is pumped out and vented, and the adsorbent is regenerated.
  • the adsorption tower T0101A completes a cycle and enters the raw gas adsorption again.
  • the steps and sequence of the other adsorption tower are exactly the same as the adsorption tower T0101A, except that they are staggered in time.
  • the adsorbent in T0201A is selectively enriched with oxygen and other components in the oxygen mixture, and the unadsorbed part of oxygen and the difficult-to-adsorb nitrogen and argon tail gas flow out from the outlet end into the bottom of the adsorption tower T0201B to increase the pressure, and when it rises to the adsorption pressure
  • the programmable valve KV2B-2 is opened, the unadsorbed nitrogen and argon are vented from the outlet of the adsorption tower T0201B. With the passage of time, the total amount of oxygen adsorbed by the adsorbent continues to increase.
  • the oxygen concentration in the outlet gas is controlled at 60-70% (V).
  • the adsorption step A After the adsorption step A is completed, close the program-controlled valves KV1A-2, KV4A-2 and KV2B-2, and open the program-controlled valves KV3A-2 and KV6A-2.
  • the product oxygen enters the top of the adsorbent bed from the bottom of the adsorption tower T0201A and flows out from the top.
  • the mixed gas returns to the inlet of the first pressure swing adsorption section and is mixed with the oxygen-rich mixed gas obtained in the adsorption tower adsorption step A of the first pressure swing adsorption section, and then enters the adsorption tower of the second pressure swing adsorption section as raw material for adsorption.
  • the oxygen concentration in the outlet gas is controlled to be above 98% (V).
  • the program-controlled valves KV1D-2, KV4D-2 and KV2A-2 are closed.
  • the oxygen concentration in the outlet gas is controlled at 20-40% (V).
  • the adsorption tower T0201A completes a cycle and enters the oxygen-rich feed gas adsorption again.
  • the steps and sequence of the other three adsorption towers are exactly the same as the adsorption tower T0201A, but they are staggered in time.
  • Fig. 7 is a time sequence diagram of the operation steps of each stage of the adsorption tower and the switching of the programmable valve in the embodiment 4 of the present invention.
  • Fig. 8 is a process flow diagram of Example 4 of the present invention.
  • blower C0100, programmable valve, PLC control system, instrumentation, process pipe fittings, adsorption tower T0100A and T0100B constitute pressure swing adsorption in the drying section.
  • the adsorbent in the adsorption tower is activated alumina desiccant.
  • the adsorbent in the adsorption tower is carbon molecular sieve, and a single tower is operated for adsorption, replacement and pumping. Vacuum program.
  • the pressure swing adsorption in the drying section is used to adsorb gaseous water in the air to meet the water requirements of the pressure swing adsorption oxygen generation adsorbent.
  • the first pressure swing adsorption section removes air
  • the second pressure swing adsorption section is used to adsorb the oxygen in the oxygen-enriched gas mixture obtained in step A by the adsorption tower of the first pressure swing adsorption section, and increase the oxygen to more than 99.5% (V).
  • the air After the air is boosted to 5KPa by the blower C0100, it enters the pressure swing adsorption in the drying section.
  • the adsorbent in the adsorption tower selectively adsorbs the gaseous water and other components in the humid air, and the components such as oxygen, nitrogen and argon that are not easily adsorbed are from the outlet end.
  • the adsorbent in the adsorption tower selectively adsorbs nitrogen and other components in the air, and the components such as oxygen and argon that are not easily adsorbed are discharged from the outlet end into the second pressure swing
  • the adsorption tower is adsorbing in the adsorption section.
  • the adsorbent in the adsorption tower selectively adsorbs oxygen and other components in the oxygen-rich mixed gas.
  • the components such as nitrogen and argon that are not easy to adsorb flow out from the outlet end and enter the second section to complete the vacuum
  • the adsorption tower performs pressure increase and adsorption of oxygen, and is vented after the pressure is increased to the adsorption pressure and the oxygen is adsorbed.
  • pressure equalization is performed and then vacuum is drawn.
  • the nitrogen and a small amount of oxygen drawn by the vacuum pump are vented.
  • the product is replaced with oxygen.
  • the pressure swing adsorption in the drying section is used to control the dew point of the humid air above -50°C.
  • the adsorption tower undergoes two pressure swing adsorption process steps of adsorption A and purge P in one cycle; the first pressure swing adsorption section During the adsorption process of the adsorption tower, the oxygen concentration in the outlet gas is controlled above 70% (V).
  • the adsorption tower undergoes four pressure swing adsorption processes, namely adsorption A, equal pressure drop ED, vacuum VC, and equal pressure rise in a cycle.
  • Step: After the adsorption of the adsorption tower in the second pressure swing adsorption section is completed, the oxygen concentration in the outlet gas is controlled above 60-70% (V), and the adsorption tower undergoes adsorption A, product oxygen replacement P, and pumping in a cycle.
  • the total oxygen recovery rate is about 60%
  • the three-stage cycle time is generally 20-80 seconds
  • the first stage vacuum is -0.07MPa
  • the air volume of the blower is -0.07MPa
  • the empty tower speed of the three-stage adsorption tower is adsorption tower and other design parameters are designed according to the usual conditions in the field of pressure swing adsorption technology.
  • Each adsorption tower in each stage of the present invention sequentially undergoes the following steps in a cycle.
  • step A2 enters the adsorption tower from the outlet end of the adsorption tower T0100A through the programmable valve KV3A-0, and then is discharged from the bottom of the adsorption tower T0100A through the process control valve KV4A-0.
  • the purge P is completed, close the programmable valves KV3A-0 and KV4A -0.
  • the adsorption tower T0100A completes a cycle and enters the dry air adsorption again.
  • the steps and sequence of the other adsorption tower are exactly the same as the adsorption tower T0100A, except that they are staggered in time.
  • each adsorption tower of the first stage sequentially undergoes the following steps in a cycle:
  • the dry air boosted to 5KPa enters the adsorption tower T0101A to increase the pressure
  • the adsorption pressure is increased
  • the adsorbent in the adsorption tower selectively adsorbs nitrogen in the air sequentially
  • the components such as oxygen and argon that are not easily adsorbed open the program-controlled valve KV2A-1 and are discharged from the outlet end into the oxygen-enriched buffer tank V0201.
  • the oxygen-enriched concentration is controlled above 70%.
  • the adsorbent adsorbs nitrogen The total amount continues to increase. When the adsorbent is saturated with nitrogen, the gas flow is stopped, and the adsorption ends.
  • the adsorption tower T0101A completes a cycle and enters the raw gas adsorption again.
  • the steps and sequence of the other adsorption tower are exactly the same as the adsorption tower T0101A, except that they are staggered in time.
  • the adsorbent in T0201A is selectively enriched with oxygen and other components in the oxygen mixture, and the unadsorbed part of oxygen and the difficult-to-adsorb nitrogen and argon tail gas flow out from the outlet end into the bottom of the adsorption tower T0201B to increase the pressure, and when it rises to the adsorption pressure
  • the programmable valve KV2B-2 is opened, the unadsorbed nitrogen and argon are vented from the outlet of the adsorption tower T0201B. With the passage of time, the total amount of oxygen adsorbed by the adsorbent continues to increase.
  • the oxygen concentration in the outlet gas is controlled at 60-70% (V).
  • the adsorption step A After the adsorption step A is completed, close the program-controlled valves KV1A-2, KV4A-2 and KV2B-2, and open the program-controlled valves KV3A-2 and KV6A-2.
  • the product oxygen enters the top of the adsorbent bed from the bottom of the adsorption tower T0201A and flows out from the top.
  • the mixed gas returns to the inlet of the first pressure swing adsorption section and is mixed with the oxygen-rich mixed gas obtained in the adsorption tower adsorption step A of the first pressure swing adsorption section, and then enters the adsorption tower of the second pressure swing adsorption section as raw material for adsorption.
  • the oxygen concentration in the outlet gas is controlled to be above 98% (V).
  • the program-controlled valves KV1D-2, KV4D-2 and KV2A-2 are closed.
  • the oxygen concentration in the outlet gas is controlled at 20-40% (V).
  • the adsorption tower T0201A completes a cycle and enters the oxygen-rich feed gas adsorption again.
  • the steps and sequence of the other three adsorption towers are exactly the same as the adsorption tower T0201A, but they are staggered in time.

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Abstract

本发明提供一种移动式变压吸附氧气生产装置的方法，其包括串联操作的第一变压吸附段和第二变压吸附段，干燥的原料空气中的大部分氮气被第一变压吸附段的氮平衡选择型吸附剂床层吸附，富氧混合气流入第二变压吸附段的速度选择型吸附剂床层，使氧气被速度选择型吸附剂床层吸附，第二变压吸附段解析出高浓度氧气；第一变压吸附段的吸附塔在一个循环周期中至少依次经历吸附A、均压降ED、逆放BD或抽真空VC、均压升ER四个步骤；第二变压吸附段的吸附塔在一个循环周期中至少依次经历吸附A、产品氧气置换P、抽真空VC和串联吸附A1步骤。采用本发明方法的变压吸附装置体积小、重量轻、使用方便、压力低，大大降低了用氧成本，显著提高了用氧安全性。

Description

一种移动式变压吸附氧气生产装置的方法 技术领域
本发明涉及变压吸附技术制氧领域,具体涉及一种移动式变压吸附氧气生产装置的方法。
背景技术
目前，在气割过程中所用的纯氧均是采用深冷装置制出纯氧后，用压缩机将纯氧压缩到12.5MPa以上装入特制的40升钢瓶中，然后运输到各个用户，而用户使用压力低于0.95MPa，耗费大量的人力和物力，不仅用氧成本高，而且安全性差。
发明内容
针对上述问题，本发明旨在提供一种体积小、重量轻、随开随停、使用方便和压力低的移动式变压吸附氧气生产装置的方法，大大降低用氧成本和幅度提高用氧安全性。本发明的目的是通过以下技术方案实现的：
一种移动式变压吸附氧气生产装置的方法，该方法采用两段变压吸附串联操作，不含气态水的原料空气首先从第一变压吸附段的吸附塔底部进入氮平衡选择型吸附剂床层，原料空气中的大部分氮气被氮平衡选择型吸附剂床层吸附，大部分氧气和氩气从吸附塔出口流出从第二变压吸附段的吸附塔底部进入速度选择型吸附剂床层，富氧被速度选择型吸附剂床层吸附，氮气和氩气以及少量氧气从吸附塔出口流出，解析出来的混合气为高浓度氧气。第一变压吸附段的吸附塔在一个循环周期中依次经历吸附A、均压降ED、逆放BD或抽真空VC、均压升ER四个变压吸附工艺步骤；第二变压吸附段的吸附塔在一个循环周期中依次经历吸附A、产品氧气置换P、抽真空VC和串联吸附A1变压吸附工艺步骤。
进一步，第二变压吸附段的吸附塔在吸附A步骤之后增加串联置换P1步骤，该串联置换步骤的置换气来自另一个处于产品氧气置换P步骤的吸附塔出口排出的混合气。
进一步，第一变压吸附段的吸附塔在均压升ER步骤之后增加最终升压FR步骤，该步骤的升压气来自第一段吸附塔吸附A步骤的出口富氧混合气。
考虑到原料空气中可能含气态水的情况，为确保第一变压吸附段的氮平衡选择型吸附剂床层的吸附效果，需要对原料空气进行干燥，对此，本发明提供两种解决方案：
方案1：第一段吸附塔的底部装填干燥剂、上部装填氮平衡选择型吸附剂床层，原料空气中从第一段吸附塔底部通过时，其气态水绝大部分被干燥剂床层吸附，大部分氮气被氮平衡选择型吸附剂床层吸附，大部分氧气和氩气从吸附塔出口流出从第二变压吸附段的吸附塔底部进入速度选择型吸附剂床层，富氧被速度选择型吸附剂床层吸附，氮气和氩气以及少量氧气从吸附塔出口流出，解析出来的混合气为高浓度氧气。
方案2：在第一变压吸附段之前增设变压吸附干燥段，用于除去空气中的气态水， 达到进入第一变压吸附段的吸附塔对水分的要求。该变压吸附干燥段在一个循环周期中依次经历吸附A和吹扫P两个变压吸附工艺步骤，吹扫P步骤的气体来源于第一变压吸附段的吸附塔吸附A步骤出口的放空气和第二变压吸附段的吸附塔解析放空气。干燥段装填活性氧化铝作为干燥剂；第一变压吸附段的吸附塔内部装填5A型分子筛或X型锂分子筛作为氮平衡选择型吸附剂；第二变压吸附段的吸附塔装填碳分子筛作为速度选择型吸附剂。
进一步，第一变压吸附段和第二变压吸附段的吸附塔吸附A步骤的压力为0.005-0.2MPa(表压)。
进一步，第一变压吸附段的吸附塔吸附A步骤结束时出口气中氧气的浓度为70-80％(V)。
进一步，第一变压吸附段的吸附塔装填5A型分子筛或X型锂分子筛；第二变压吸附段的吸附塔装填碳分子筛。
本发明的方法所提供的移动式变压吸附纯氧生产装置，大大降低用氧成本，而且安全性大幅度提高，本移动式变压吸附纯氧生产装置体积小、重量轻、随开随停、使用方便，最高压力只有1.2MPa。
附图说明
图1是本发明实施例1各段吸附塔运行步骤及程控阀开关时序图。
图2是本发明实施例1的工艺流程图。
图3是本发明实施例2各段吸附塔运行步骤及程控阀开关时序图。
图4是本发明实施例2的工艺流程图。
图5是本发明实施例3各段吸附塔运行步骤及程控阀开关时序图。
图6是本发明实施例3的工艺流程图。
图7是本发明实施例4各段吸附塔运行步骤及程控阀开关时序图。
图8是本发明实施例4的工艺流程图。
实现本发明的最佳方式
下面结合附图对本发明的优选实施例加以说明，以下实施例只是为方便理解本发明的技术方案而给出的优选实施例，不作为对本发明权利要求保护范围的限定。
实施例1：
图1是本发明实施例1各段吸附塔运行步骤及程控阀开关时序图。
图2是本发明实施例1的工艺流程图。
本实施例的原料空气组成如下：
组份 O 2 N 2 Ar CO 2 其它 ∑
浓度(％)(V) 20.93 78.03 0.932 0.03 0.078 100
温度：≤40℃
压力：0.05MPa(G)
如图2所示，真空泵P0101、真空缓冲罐V0101、程控阀、PLC控制系统、仪器仪表、工艺管道管件、吸附塔T0101A和T0101B组成第一变压吸附段，吸附塔内装填的吸附剂为5A分子筛或锂分子筛，运行单塔吸附、均压和抽真空程序；纯氧真空泵P0201、纯氧压缩机C0201、富氧缓冲罐V0201、压缩机缓冲罐V0202、产品纯氧缓冲罐V0203、程控阀、PLC控制系统、仪器仪表、工艺管道管件、吸附塔T0201A、T0201B、T0201C和T0201D组成第二变压吸附段，吸附塔内装填的吸附剂为碳分子筛，运行单塔吸附、置换和抽真空程序。本实施例将上述两段变压吸附串联操作，第一变压吸附段将空气中的氮气吸附下来，第二变压吸附段用于将第一变压吸附段吸附塔吸附A步骤获得的富氧混合气中的氧吸附下来，并把氧提高到99.5％(V)以上。
压力大于5KPa的干燥空气进入第一变压吸附段处于吸附步骤的吸附塔，吸附塔中的吸附剂选择性地吸附空气中的氮气等组分，不易吸附的氧和氩等组分从出口端排出进入第二变压吸附段正在吸附的吸附塔，吸附塔中的吸附剂选择性地吸附富氧混合气中的氧等组分，不易吸附的氮和氩等组分从出口端流出进入第二段抽完真空的吸附塔进行升压和吸附氧气，升压到吸附压力并吸附氧气后放空。第一变压吸附段的吸附塔吸附结束后，先进行均压再抽真空，真空泵抽出来的氮气和少量氧气放空，第二变压吸附段的吸附塔吸附结束后，先用产品氧气置换，置换结束后，进行抽真空，抽出来的高浓度氧气，一部分作为产品经过压缩后进入产品纯氧缓冲罐，另一部分去置换吸附结束后的吸附剂床层。第一变压吸附段的吸附塔吸附过程中出口气中氧气浓度控制在70％(V)以上，其吸附塔在一个循环周期中依次经历吸附A、均压降ED、抽真空VC和均压升四个变压吸附工艺步骤；第二变压吸附段的吸附塔吸附结束后，出口气中氧气浓度控制在60-70％(V)以上，其吸附塔在一个循环周期中依次经历吸附A、产品氧气置换P、抽真空VC和串联吸附A1四个变压吸附工艺步骤。氧气总回收率在60％左右，两段循环时间一般为20-80秒，第一段真空度为-0.07MPa,鼓风机气量、两段吸附塔的空塔速度、真空泵的抽气量、吸附剂用量和吸附塔直径以及其他设计参数按变压吸附技术领域通常的情况进行设计。
本发明各段的每个吸附塔在一个循环中依次经历如下步骤。
第一变压吸附段的吸附塔：第一段的每个吸附塔在一个循环中依次经历如下步骤：
⑴吸附A
打开程控阀KV1A-1，升压到5KPa的干燥空气进入吸附塔T0101A升压，当升到吸附压力时，打开程控阀KV2A-1，吸附塔中的吸附剂选择性地依次吸附空气中的氮气等组分，不易吸附的氧和氩等组分打开程控阀KV2A-1从出口端排出进入富氧缓冲罐V0201，富氧浓度控制在70％以上，随着时间的推移，吸附剂吸附的氮气总量不断增加，当吸附剂吸附氮气饱和时，停止进气，此时吸附结束。
⑵均压降ED
吸附A步骤结束后，打开程控阀KV3A-1，吸附塔T0101A内死空间气体从吸附塔出口排出进入本段已完成抽真空VC步骤的吸附塔T0101B升压，尽量让两塔压力相等。
⑶抽真空VC
吸附塔T0101A均压降ED步骤结束后，打开程控阀KV4A-1，将吸附塔T0101A内吸附的氮气抽出来放空。
⑷均压升ER
吸附塔T0101A抽真空VC步骤结束后，打开程控阀KV3A-1，利用吸附塔T0101B均压降ED步骤排出的气体，从吸附塔T0101A出口端进入吸附塔T0101A，使吸附塔T0101A升高压力，尽量让吸附塔T0101A和T0101B压力相等。
经过上述步骤后，吸附塔T0101A完成了一个循环，再次进入原料气吸附，另外一个吸附塔的步骤和次序与吸附塔T0101A完全一样，只是在时间上相互错开。
第二变压吸附段
⑴吸附A
同时打开第二变压吸附段的程控阀KV1A-2和KV4A-2，第一变压吸附段的吸附塔吸附A步骤获得的富氧混合气从底部进入吸附塔T0201A吸附剂床层，吸附塔T0201A中的吸附剂选择性地富氧混合气中的氧气等组分，未吸附的部分氧气和不易吸附的氮和氩等尾气从出口端流出进入吸附塔T0201B底部升压，当升到吸附压力时，打开程控阀KV2B-2，未吸附的氮气和氩气从吸附塔T0201B的出口放空，随着时间的推移，吸附剂吸附的氧气的总量不断增加，当吸附塔T0201A吸附氧气饱和时，停止进气，此时吸附结束。吸附塔吸附A步骤结束后，出口气中氧气浓度控制在60-70％(V)。
⑵产品氧气置换P
吸附A步骤结束后，关闭程控阀KV1A-2、KV4A-2和KV2B-2，打开程控阀KV3A-2和KV6A-2，产品氧气从吸附塔T0201A底部进入吸附剂床层顶部流出，顶部流出的混合气返回第一变压吸附段的入口与第一变压吸附段的吸附塔吸附A步骤获得的富氧混合气混合后作为原料气进入第二变压吸附段的吸附塔吸附。吸附塔产品氧气置换P步骤结束后，出口气中氧气浓度控制在98％(V)以上。
⑶抽真空VC
吸附塔T0201A产品氧气置换P结束后，关闭程控阀KV3A-2和KV6A-2，打开程控阀KV5A-2从吸附塔底部用真空泵将吸附剂吸附的氧气抽出来，一部分作为产品氧气送出，另一部分作为置换气返回去置换吸附剂床层。
⑷串联吸附A1
吸附塔T0201A抽真空VC结束后，关闭程控阀KV5A-2，打开程控阀KV1D-2、KV4D-2和KV2A-2，富氧原料气与吸附塔T0201C产品氧气置换后从顶部流出的尾气混合后先进入吸附塔T0201D吸附剂床层吸附氧气，其尾气再通过程控阀KV4D-2进入吸附塔T0201A升压和吸附氧气，不易吸附的氮和氩以及少量的氧通过程控阀KV2A-2放空，吸附塔T0201D 吸附和T0201A串联吸附结束后，关闭程控阀KV1D-2、KV4D-2和KV2A-2。吸附塔串联吸附A1步骤过程中，出口气中氧气浓度控制在20-40％(V)。
经过上述步骤后，吸附塔T0201A完成了一个循环，再次进入富氧原料气吸附，其他三个吸附塔的步骤和次序与吸附塔T0201A完全一样，只是在时间上相互错开。
实施例2：
图3是本发明实施例2各段吸附塔运行步骤及程控阀开关时序图。
图4是本发明实施例2的工艺流程图。
本实施例的原料空气组成如下：
组份 O 2 N 2 Ar CO 2 其它 ∑
浓度(％)(V) 20.93 78.03 0.932 0.03 0.078 100
温度：≤40℃
压力：0.05MPa(G)
如图4所示，真空泵P0101、真空缓冲罐V0101、程控阀、PLC控制系统、仪器仪表、工艺管道管件、吸附塔T0101A和T0101B组成第一变压吸附段，吸附塔内装填的吸附剂为5A分子筛或锂分子筛，运行单塔吸附、均压和抽真空程序；纯氧真空泵P0201、纯氧压缩机C0201、富氧缓冲罐V0201、压缩机缓冲罐V0202、产品纯氧缓冲罐V0203、程控阀、PLC控制系统、仪器仪表、工艺管道管件、吸附塔T0201A、T0201B、T0201C、T0201D和T0201E组成第二变压吸附段，吸附塔内装填的吸附剂为碳分子筛，运行单塔串联吸附、串联置换和抽真空程序。本实施例将上述两段变压吸附串联操作，第一变压吸附段将空气中的氮气吸附下来，第二变压吸附段用于将第一变压吸附段吸附塔吸附A步骤获得的富氧混合气中的氧吸附下来，并把氧提高到99.5％(V)以上。
压力大于5KPa的干燥空气进入第一变压吸附段处于吸附步骤的吸附塔，吸附塔中的吸附剂选择性地吸附空气中的氮气等组分，不易吸附的氧和氩等组分从出口端排出进入第二变压吸附段正在吸附的吸附塔，吸附塔中的吸附剂选择性地吸附富氧混合气中的氧等组分，不易吸附的氮和氩等组分从出口端流出进入第二段抽完真空的吸附塔进行升压和吸附氧气，升压到吸附压力并吸附氧气后放空。第一变压吸附段的吸附塔吸附结束后，先进行均压再抽真空，真空泵抽出来的氮气和少量氧气放空，吸附塔吸附过程中出口气中氧气浓度控制在70％(V)以上，其吸附塔在一个循环周期中依次经历吸附A、均压降ED、抽真空VC和均压升四个变压吸附工艺步骤；第二变压吸附段处于吸附步骤的吸附塔出口气中氧气浓度控制在接近原料气氧浓度，其吸附塔在一个循环周期中依次经历吸附A、串联置换P1、产品氧气置换P、抽真空VC和串联吸附A1五个变压吸附工艺步骤。氧气总回收率在60％左右，两段循环时间一般为20-80秒，第一段真空度为-0.07MPa,鼓风机气量、两段吸附塔的空塔速度、真空泵的抽气量、吸附剂用量和吸附塔直径以及其他设计参数按变压吸附技术领域通常的情况进行设计。
本发明各段的每个吸附塔在一个循环中依次经历如下步骤。
第一变压吸附段的吸附塔：第一段的每个吸附塔在一个循环中依次经历如下步骤：
⑴吸附A
打开程控阀KV1A-1，升压到5KPa的干燥空气进入吸附塔T0101A升压，当升到吸附压力时，打开程控阀KV2A-1，吸附塔中的吸附剂选择性地依次吸附空气中的氮气等组分，不易吸附的氧和氩等组分打开程控阀KV2A-1从出口端排出进入富氧缓冲罐V0201，富氧浓度控制在70％以上，随着时间的推移，吸附剂吸附的氮气总量不断增加，当吸附剂吸附氮气饱和时，停止进气，此时吸附结束。
⑵均压降ED
吸附A步骤结束后，打开程控阀KV3A-1，吸附塔T0101A内死空间气体从吸附塔出口排出进入本段已完成抽真空VC步骤的吸附塔T0101B升压，尽量让两塔压力相等。
⑶抽真空VC
吸附塔T0101A均压降ED步骤结束后，打开程控阀KV4A-1，将吸附塔T0101A内吸附的氮气抽出来放空。
⑷均压升ER
吸附塔T0101A抽真空VC步骤结束后，打开程控阀KV3A-1，利用吸附塔T0101B均压降ED步骤排出的气体，从吸附塔T0101A出口端进入吸附塔T0101A，使吸附塔T0101A升高压力，尽量让吸附塔T0101A和T0101B压力相等。
经过上述步骤后，吸附塔T0101A完成了一个循环，再次进入原料气吸附，另外一个吸附塔的步骤和次序与吸附塔T0101A完全一样，只是在时间上相互错开。
第二变压吸附段
⑴吸附A
同时打开第二变压吸附段的程控阀KV1A-2和KV4A-2，第一变压吸附段的吸附塔吸附A步骤获得的富氧混合气从底部进入吸附塔T0201A吸附剂床层，吸附塔T0201A中的吸附剂选择性地富氧混合气中的氧气等组分，未吸附的部分氧气和不易吸附的氮和氩等尾气从出口端流出进入吸附塔T0201B底部升压，当升到吸附压力时，打开程控阀KV2B-2，未吸附的氮气和氩气从吸附塔T0201B的出口放空，随着时间的推移，吸附剂吸附氧气的总量不断增加，当吸附塔T0201A吸附氧气饱和时，停止进气，此时吸附结束。吸附塔吸附A步骤结束后，出口气中氧气浓度控制在60-70％(V)。
⑵串联置换P1
吸附A步骤结束后，关闭程控阀KV1A-2、KV4A-2和KV2B-2，打开程控阀KV6E-2、KV3E-2和KV2A-2，产品氧气从吸附塔T0201E底部进入吸附剂床层置换氮气和氩气，然后从顶部流出，顶部流出的置换尾气从吸附塔T0201A的底部进入，经过吸附塔T0201A吸附剂床层吸附氧气后，通过程控阀KV2A-2返回第二段入口与第一变压吸附段的吸附塔吸附步骤获得的富氧气体混合。吸附塔串联置换P1步骤结束后，出口气中氧气浓度控制在60-80％(V)。
⑶产品氧气置换P
串联置换P1步骤结束后，关闭程控阀KV6E-2、KV3E-2和KV2A-2，打开程控阀KV3A-2和KV6A-2，产品氧气从吸附塔T0201A底部进入吸附剂床层置换氮气和氩气，然后从顶部流出，顶部流出的置换尾气从吸附塔T0201B的底部进入，经过吸附塔T0201B吸附剂床层吸附氧气后，通过程控阀KV2B-2放空。吸附塔产品氧气置换P步骤结束后，出口气中氧气浓度控制在98％(V)以上。
⑷抽真空VC
吸附塔T0201A产品氧气置换P结束后，关闭程控阀KV3A-2和KV6A-2，打开程控阀KV5A-2从吸附塔底部用真空泵将吸附剂吸附的氧气抽出来，一部分作为产品氧气送出，另一部分作为置换气返回去置换吸附剂床层。
⑸串联吸附A1
吸附塔T0201A抽真空VC结束后，关闭程控阀KV5A-2，打开程控阀KV1E-2、KV4E-2和KV7A-2，富氧原料气先进入吸附塔T0201E吸附剂床层吸附氧气，其尾气再通过程控阀KV4E-2进入吸附塔T0201A升压和吸附氧气，吸附塔T0201E富氧吸附和T0201A串联吸附结束后，关闭程控阀KV1E-2、KV4E-2和KV7A-2。
经过上述步骤后，吸附塔T0201A完成了一个循环，再次进入富氧原料气吸附，其他四个吸附塔的步骤和次序与吸附塔T0201A完全一样，只是在时间上相互错开。
实施例3：
图5是本发明实施例3各段吸附塔运行步骤及程控阀开关时序图。
图6是本发明实施例3的工艺流程图。
本实施例的原料空气组成如下：
组份 O 2 N 2 Ar CO 2 其它 ∑
浓度(％)(V) 20.93 78.03 0.932 0.03 0.078 100
温度：≤40℃
压力：0.05MPa(G)
如图6所示，真空泵P0101、真空缓冲罐V0101、程控阀、PLC控制系统、仪器仪表、工艺管道管件、吸附塔T0101A、T0101B和T0101C组成第一变压吸附段，吸附塔内装填的吸附剂为5A分子筛或锂分子筛，运行单塔吸附、均压和抽真空程序；纯氧真空泵P0201、纯氧压缩机C0201、压缩机缓冲罐V0202、产品纯氧缓冲罐V0203、程控阀、PLC控制系统、仪器仪表、工艺管道管件、吸附塔T0201A、T0201B、T0201C和T0201D组成第二变压吸附段，吸附塔内装填的吸附剂为碳分子筛，运行单塔吸附、置换和抽真空程序。本实施例将上述两段变压吸附串联操作，第一变压吸附段将空气中的氮气吸附下来，第二变压吸附段用于将第一变压吸附段吸附塔吸附A步骤获得的富氧混合气中的氧吸附下来，并把氧提高到99.5％(V)以上。
压力大于5KPa的干燥空气进入第一变压吸附段处于吸附步骤的吸附塔，吸附塔中的 吸附剂选择性地吸附空气中的氮气等组分，不易吸附的氧和氩等组分从出口端排出进入第二变压吸附段正在吸附的吸附塔，吸附塔中的吸附剂选择性地吸附富氧混合气中的氧等组分，不易吸附的氮和氩等组分从出口端流出进入第二段抽完真空的吸附塔进行升压和吸附氧气，升压到吸附压力并吸附氧气后放空。第一变压吸附段的吸附塔吸附结束后，先进行均压再抽真空，真空泵抽出来的氮气和少量氧气放空，第二变压吸附段的吸附塔吸附结束后，先用产品氧气置换，置换结束后，进行抽真空，抽出来的高浓度氧气，一部分作为产品经过压缩后进入产品纯氧缓冲罐，另一部分去置换吸附结束后的吸附剂床层。第一变压吸附段的吸附塔吸附过程中出口气中氧气浓度控制在70％(V)以上，其吸附塔在一个循环周期中依次经历吸附A、均压降ED、抽真空VC、均压升ER和再加压FR五个变压吸附工艺步骤；第二变压吸附段的吸附塔吸附结束后，出口气中氧气浓度控制在60-70％(V)以上，其吸附塔在一个循环周期中依次经历吸附A、产品氧气置换P、抽真空VC和串联吸附A1四个变压吸附工艺步骤。氧气总回收率在60％左右，两段循环时间一般为20-80秒，第一段真空度为-0.07MPa,鼓风机气量、两段吸附塔的空塔速度、真空泵的抽气量、吸附剂用量和吸附塔直径以及其他设计参数按变压吸附技术领域通常的情况进行设计。
本发明各段的每个吸附塔在一个循环中依次经历如下步骤。
第一变压吸附段的吸附塔：第一段的每个吸附塔在一个循环中依次经历如下步骤：
⑴吸附A
打开第一变压吸附段的程控阀KV1A-1和KV2A-1，干燥空气从底部进入吸附塔T0101A吸附剂床层，吸附塔T0101A中的吸附剂选择性地氮气等组分，未吸附的部分氮气和不易吸附的氧和氩等组分从出口端流出进入第二变压吸附段处于吸附步骤的吸附塔，随着时间的推移，吸附剂吸附的氮气等组分的总量不断增加，当吸附塔T0101A吸附氮气饱和时，停止进气，此时吸附结束。吸附塔吸附A步骤进行中，出口气中氧气浓度控制在70％(V)以上。
⑵均压降ED
吸附A步骤结束后，打开程控阀KV3A-1和KV3C-1，吸附塔T0101A内死空间气体从吸附塔出口排出进入本段已完成抽真空VC步骤的吸附塔T0101C升压，尽量让两塔压力相等。
⑶抽真空VC
吸附塔T0101A均压降ED结束后，打开程控阀KV4A-1，将吸附塔T0101A内吸附的氮气抽出来放空，吸附剂得到再生。
⑷均压升ER
吸附塔T0101A抽真空VC步骤结束后，打开程控阀KV3A-1和KV3B-1，利用吸附塔T0101B均压降ED步骤排出的气体，从吸附塔T0101A出口端进入吸附塔，使吸附塔T0101A升高压力，尽量让吸附塔T0101A和T0101B压力相等。
⑸最终升压FR
均压升ER结束后，关闭程控阀KV3A-1，打开程控阀KV2A-1，用吸附过程中的出口气对吸附塔T0101A进行升压，直到接近第一变压吸附段的吸附压力。
经过上述步骤后，吸附塔T0101A完成了一个循环，再次进入原料气吸附，另外一个吸附塔的步骤和次序与吸附塔T0101A完全一样，只是在时间上相互错开。
第二变压吸附段
⑴吸附A
同时打开第二变压吸附段的程控阀KV1A-2和KV4A-2，第一变压吸附段的吸附塔吸附A步骤获得的富氧混合气从底部进入吸附塔T0201A吸附剂床层，吸附塔T0201A中的吸附剂选择性地富氧混合气中的氧气等组分，未吸附的部分氧气和不易吸附的氮和氩等尾气从出口端流出进入吸附塔T0201B底部升压，当升到吸附压力时，打开程控阀KV2B-2，未吸附的氮气和氩气从吸附塔T0201B的出口放空，随着时间的推移，吸附剂吸附的氧气的总量不断增加，当吸附塔T0201A吸附氧气饱和时，停止进气，此时吸附结束。吸附塔吸附A步骤结束后，出口气中氧气浓度控制在60-70％(V)。
⑵产品氧气置换P
吸附A步骤结束后，关闭程控阀KV1A-2、KV4A-2和KV2B-2，打开程控阀KV3A-2和KV6A-2，产品氧气从吸附塔T0201A底部进入吸附剂床层顶部流出，顶部流出的混合气返回第一变压吸附段的入口与第一变压吸附段的吸附塔吸附A步骤获得的富氧混合气混合后作为原料气进入第二变压吸附段的吸附塔吸附。吸附塔产品氧气置换P步骤结束后，出口气中氧气浓度控制在98％(V)以上。
⑶抽真空VC
吸附塔T0201A产品氧气置换P结束后，关闭程控阀KV3A-2和KV6A-2，打开程控阀KV5A-2从吸附塔底部用真空泵将吸附剂吸附的氧气抽出来，一部分作为产品氧气送出，另一部分作为置换气返回去置换吸附剂床层。
⑷串联吸附A1
吸附塔T0201A抽真空VC结束后，关闭程控阀KV5A-2，打开程控阀KV1D-2、KV4D-2和KV2A-2，富氧原料气与吸附塔T0201C产品氧气置换后从顶部流出的尾气混合后先进入吸附塔T0201D吸附剂床层吸附氧气，其尾气再通过程控阀KV4D-2进入吸附塔T0201A升压和吸附氧气，不易吸附的氮和氩以及少量的氧通过程控阀KV2A-2放空，吸附塔T0201D吸附和T0201A串联吸附结束后，关闭程控阀KV1D-2、KV4D-2和KV2A-2。吸附塔串联吸附A1步骤过程中，出口气中氧气浓度控制在20-40％(V)。
经过上述步骤后，吸附塔T0201A完成了一个循环，再次进入富氧原料气吸附，其他三个吸附塔的步骤和次序与吸附塔T0201A完全一样，只是在时间上相互错开。
实施例4：
图7是本发明实施例4各段吸附塔运行步骤及程控阀开关时序图。
图8是本发明实施例4的工艺流程图。
本实施例的原料空气组成如下：
组份 O 2 N 2 Ar CO 2 其它 ∑
浓度(％)(V) 20.93 78.03 0.932 0.03 0.078 100
温度：≤40℃
压力：0.05MPa(G)
如图8所示，鼓风机C0100、程控阀、PLC控制系统、仪器仪表、工艺管道管件、吸附塔T0100A和T0100B组成干燥段变压吸附，吸附塔内装填的吸附剂为活性氧化铝干燥剂，运行单塔吸附和吹扫再生程序；真空泵P0101、真空缓冲罐V0101、程控阀、PLC控制系统、仪器仪表、工艺管道管件、吸附塔T0101A和T0101B组成第一变压吸附段，吸附塔内装填的吸附剂为5A分子筛或锂分子筛，运行单塔吸附、均压和抽真空程序；纯氧真空泵P0201、纯氧压缩机C0201、富氧缓冲罐V0201、压缩机缓冲罐V0202、产品纯氧缓冲罐V0203、程控阀、PLC控制系统、仪器仪表、工艺管道管件、吸附塔T0201A、T0201B、T0201C和T0201D组成第二变压吸附段，吸附塔内装填的吸附剂为碳分子筛，运行单塔吸附、置换和抽真空程序。本实施例将上述三段变压吸附串联操作，干燥段变压吸附用于将空气中的气态水吸附下来，满足变压吸附制氧吸附剂对水的要求，第一变压吸附段将空气中的氮气吸附下来，第二变压吸附段用于将第一变压吸附段吸附塔吸附A步骤获得的富氧混合气中的氧吸附下来，并把氧提高到99.5％(V)以上。
空气经过鼓风机C0100升压到5KPa后进入干燥段变压吸附，吸附塔中的吸附剂选择性地吸附湿空气中的气态水等组分，不易吸附的氧、氮和氩等组分从出口端进入第一变压吸附段处于吸附步骤的吸附塔，吸附塔中的吸附剂选择性地吸附空气中的氮气等组分，不易吸附的氧和氩等组分从出口端排出进入第二变压吸附段正在吸附的吸附塔，吸附塔中的吸附剂选择性地吸附富氧混合气中的氧等组分，不易吸附的氮和氩等组分从出口端流出进入第二段抽完真空的吸附塔进行升压和吸附氧气，升压到吸附压力并吸附氧气后放空。第一变压吸附段的吸附塔吸附结束后，先进行均压再抽真空，真空泵抽出来的氮气和少量氧气放空，第二变压吸附段的吸附塔吸附结束后，先用产品氧气置换，置换结束后，进行抽真空，抽出来的高浓度氧气，一部分作为产品经过压缩后进入产品纯氧缓冲罐，另一部分去置换吸附结束后的吸附剂床层。干燥段变压吸附用于将湿空气的露点控制在-50℃以上，其吸附塔在一个循环周期中依次经历吸附A和吹扫P两个变压吸附工艺步骤；第一变压吸附段的吸附塔吸附过程中出口气中氧气浓度控制在70％(V)以上，其吸附塔在一个循环周期中依次经历吸附A、均压降ED、抽真空VC和均压升四个变压吸附工艺步骤；第二变压吸附段的吸附塔吸附结束后，出口气中氧气浓度控制在60-70％(V)以上，其吸附塔在一个循环周期中依次经历吸附A、产品氧气置换P、抽真空VC和串联吸附A1四个变压吸附工艺步骤。氧气总回收率在60％左右，三段循环时间一般为20-80秒，第一段真空度为-0.07MPa,鼓风机气量、三段吸附塔的空塔速度、真空泵的抽气量、 吸附剂用量和吸附塔直径以及其他设计参数按变压吸附技术领域通常的情况进行设计。
本发明各段的每个吸附塔在一个循环中依次经历如下步骤。
变压吸附干燥段
⑴吸附A
打开程控阀KV1A-0和KV2A-0，原料空气经过鼓风机(C0101)升压到5KPa(G)后，从吸附塔T0100A底部进入活性氧化铝床层，将空气中的气态水吸附下来，不易吸附的氧气、氮气和氩气等组分从出口端排出进入第一变压吸附段的吸附塔底部，随着时间的推移，活性氧化铝吸附的气态水总量不断增加，当活性氧化铝吸附气态水饱和时，停止进气，此时吸附结束，控制变压吸附干燥段吸附A步骤的出口混合气露点再-50℃左右。
⑵吹扫
吸附塔T0100A吸附结束后，打开程控阀KV3A-0和KV4A-0，第一变压吸附段的吸附塔吸附A步骤和尾气吸附A1步骤的放空气和第二变压吸附段的吸附塔空气吸附A2步骤的放空气从吸附塔T0100A出口端经程控阀KV3A-0进入吸附塔，然后经过程控阀KV4A-0从吸附塔T0100A底部排出放空，吹扫P结束后，关闭程控阀KV3A-0和KV4A-0。
经过上述步骤后，吸附塔T0100A完成了一个循环，再次进入干燥空气吸附，另一个吸附塔的步骤和次序与吸附塔T0100A完全一样，只是在时间上相互错开。
第一变压吸附段的吸附塔：第一段的每个吸附塔在一个循环中依次经历如下步骤：
⑴吸附A
打开程控阀KV1A-1，升压到5KPa的干燥空气进入吸附塔T0101A升压，当升到吸附压力时，打开程控阀KV2A-1，吸附塔中的吸附剂选择性地依次吸附空气中的氮气等组分，不易吸附的氧和氩等组分打开程控阀KV2A-1从出口端排出进入富氧缓冲罐V0201，富氧浓度控制在70％以上，随着时间的推移，吸附剂吸附的氮气总量不断增加，当吸附剂吸附氮气饱和时，停止进气，此时吸附结束。
⑵均压降ED
吸附A步骤结束后，打开程控阀KV3A-1，吸附塔T0101A内死空间气体从吸附塔出口排出进入本段已完成抽真空VC步骤的吸附塔T0101B升压，尽量让两塔压力相等。
⑶抽真空VC
吸附塔T0101A均压降ED步骤结束后，打开程控阀KV4A-1，将吸附塔T0101A内吸附的氮气抽出来放空。
⑷均压升ER
吸附塔T0101A抽真空VC步骤结束后，打开程控阀KV3A-1，利用吸附塔T0101B均压降ED步骤排出的气体，从吸附塔T0101A出口端进入吸附塔T0101A，使吸附塔T0101A升高压力，尽量让吸附塔T0101A和T0101B压力相等。
经过上述步骤后，吸附塔T0101A完成了一个循环，再次进入原料气吸附，另外一个吸附塔的步骤和次序与吸附塔T0101A完全一样，只是在时间上相互错开。
第二变压吸附段
⑴吸附A
同时打开第二变压吸附段的程控阀KV1A-2和KV4A-2，第一变压吸附段的吸附塔吸附A步骤获得的富氧混合气从底部进入吸附塔T0201A吸附剂床层，吸附塔T0201A中的吸附剂选择性地富氧混合气中的氧气等组分，未吸附的部分氧气和不易吸附的氮和氩等尾气从出口端流出进入吸附塔T0201B底部升压，当升到吸附压力时，打开程控阀KV2B-2，未吸附的氮气和氩气从吸附塔T0201B的出口放空，随着时间的推移，吸附剂吸附的氧气的总量不断增加，当吸附塔T0201A吸附氧气饱和时，停止进气，此时吸附结束。吸附塔吸附A步骤结束后，出口气中氧气浓度控制在60-70％(V)。
⑵产品氧气置换P
吸附A步骤结束后，关闭程控阀KV1A-2、KV4A-2和KV2B-2，打开程控阀KV3A-2和KV6A-2，产品氧气从吸附塔T0201A底部进入吸附剂床层顶部流出，顶部流出的混合气返回第一变压吸附段的入口与第一变压吸附段的吸附塔吸附A步骤获得的富氧混合气混合后作为原料气进入第二变压吸附段的吸附塔吸附。吸附塔产品氧气置换P步骤结束后，出口气中氧气浓度控制在98％(V)以上。
⑶抽真空VC
吸附塔T0201A产品氧气置换P结束后，关闭程控阀KV3A-2和KV6A-2，打开程控阀KV5A-2从吸附塔底部用真空泵将吸附剂吸附的氧气抽出来，一部分作为产品氧气送出，另一部分作为置换气返回去置换吸附剂床层。
⑷串联吸附A1
吸附塔T0201A抽真空VC结束后，关闭程控阀KV5A-2，打开程控阀KV1D-2、KV4D-2和KV2A-2，富氧原料气与吸附塔T0201C产品氧气置换后从顶部流出的尾气混合后先进入吸附塔T0201D吸附剂床层吸附氧气，其尾气再通过程控阀KV4D-2进入吸附塔T0201A升压和吸附氧气，不易吸附的氮和氩以及少量的氧通过程控阀KV2A-2放空，吸附塔T0201D吸附和T0201A串联吸附结束后，关闭程控阀KV1D-2、KV4D-2和KV2A-2。吸附塔串联吸附A1步骤过程中，出口气中氧气浓度控制在20-40％(V)。
经过上述步骤后，吸附塔T0201A完成了一个循环，再次进入富氧原料气吸附，其他三个吸附塔的步骤和次序与吸附塔T0201A完全一样，只是在时间上相互错开。

Claims (9)

  1. 一种移动式变压吸附氧气生产装置的方法，其特征在于，此方法包括串联操作的第一变压吸附段和第二变压吸附段，干燥的原料空气首先在第一变压吸附段的吸附塔进入氮平衡选择型吸附剂床层，使大部分氮气被氮平衡选择型吸附剂床层吸附，大部分氧气和氩气从吸附塔出口流入第二变压吸附段的吸附塔，并经由第二变压吸附段的速度选择型吸附剂床层，富氧混合气中的氧气被第二变压吸附段的速度选择型吸附剂床层吸附，氮气和氩气以及少量氧气从吸附塔出口流出，第二变压吸附段解析出来的混合气为高浓度氧气；第一变压吸附段的吸附塔在一个循环周期中至少依次经历吸附A、均压降ED、逆放BD或抽真空VC、均压升ER四个变压吸附工艺步骤；第二变压吸附段的吸附塔在一个循环周期中至少依次经历吸附A、产品氧气置换P、抽真空VC和串联吸附A1变压吸附工艺步骤。
  2. 根据权利要求1所述的移动式变压吸附氧气生产装置的方法，其特征在于，第二变压吸附段的吸附塔在吸附A步骤之后增加串联置换P1步骤，该串联置换P1步骤的置换气来自另一个处于产品氧气置换P步骤的吸附塔出口排出的混合气。
  3. 根据权利要求1或2所述的移动式变压吸附氧气生产装置的方法，其特征在于，第一变压吸附段的吸附塔在均压升ER步骤之后增加最终升压FR步骤，该终升压FR步骤的升压气来自第一段吸附塔吸附A步骤的出口富氧混合气。
  4. 根据权利要求1至3任一所述的移动式变压吸附氧气生产装置的方法，其特征在于，第一变压吸附段的吸附塔底部装填干燥剂、上部装填氮平衡选择型吸附剂床层，含有气态水的原料空气从第一变压吸附段的吸附塔底部进入并依次经过干燥剂床层和氮平衡选择型吸附剂床层，原料空气中的气态水绝大部分被干燥剂床层吸附，大部分氮气被氮平衡选择型吸附剂床层吸附，大部分氧气和氩气从吸附塔出口流出并从第二变压吸附段的吸附塔底部进入第二变压吸附段的速度选择型吸附剂床层，富氧混合气中的氧气被速度选择型吸附剂床层吸附，氮气和氩气以及少量氧气从吸附塔出口流出，解析出来的混合气为高浓度氧气。
  5. 根据权利要求1至4任一所述的移动式变压吸附氧气生产装置的方法，其特征在于，第一变压吸附段和第二变压吸附段的吸附塔吸附A步骤的压力为0.005-0.2MPa(表压)。
  6. 根据权利要求1至5任一所述的移动式变压吸附氧气生产装置的方法，其特征在于，第一变压吸附段的吸附塔吸附A步骤结束时出口气中氧气的浓度为70-80％(V)。
  7. 根据权利要求1至3任一所述的移动式变压吸附氧气生产装置的方法，其特征在于，第一变压吸附段的吸附塔装填5A型分子筛或X型锂分子筛作为氮平衡选择型吸附剂；第二变压吸附段的吸附塔装填碳分子筛作为速度选择型吸附剂。
  8. 根据权利要求1至3和5至7任一所述的移动式变压吸附氧气生产装置的方法，其特 征在于，第一变压吸附段之前增设变压吸附干燥段，用于除去原料空气中的气态水，使其达到进入第一变压吸附段的吸附塔对水分的要求；该变压吸附干燥段在一个循环周期中至少依次经历吸附A和吹扫P两个变压吸附工艺步骤，吹扫P步骤的气体来源于第一变压吸附段的吸附塔吸附A步骤出口的放空气和第二变压吸附段的吸附塔解析放空气。
  9. 根据权利要求8所述的移动式变压吸附氧气生产装置的方法，其特征在于，干燥段装填活性氧化铝作为干燥剂；第一变压吸附段的吸附塔内部装填5A型分子筛或X型锂分子筛作为氮平衡选择型吸附剂；第二变压吸附段的吸附塔装填碳分子筛作为速度选择型吸附剂。
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