CN214469628U - High-purity liquid oxygen preparation facilities - Google Patents

High-purity liquid oxygen preparation facilities Download PDF

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Publication number
CN214469628U
CN214469628U CN202120367682.5U CN202120367682U CN214469628U CN 214469628 U CN214469628 U CN 214469628U CN 202120367682 U CN202120367682 U CN 202120367682U CN 214469628 U CN214469628 U CN 214469628U
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oxygen
nitrogen
condenser
outlet
evaporator
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Chinese (zh)
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林序飞
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Shanghai Chinllenge Gases Co ltd
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Shanghai Chinllenge Gases Co ltd
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/56—Ultra high purity oxygen, i.e. generally more than 99,9% O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/50—Separating low boiling, i.e. more volatile components from oxygen, e.g. N2, Ar
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/52—Separating high boiling, i.e. less volatile components from oxygen, e.g. Kr, Xe, Hydrocarbons, Nitrous oxides, O3
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/50—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The utility model relates to the technical field of high-purity oxygen production, in particular to a high-purity liquid oxygen preparation device, which comprises a first rectifying tower, a first condenser, a first evaporator, a second rectifying tower, a second condenser, a second evaporator and a third condenser, wherein the first rectifying tower is internally provided with a first condensation cavity at the top of the tower and a first evaporation cavity at the bottom of the tower, the middle part of the first rectifying tower is provided with a raw material oxygen inlet, the upper part of the first rectifying tower is arranged below the first condensation cavity and is provided with a poor hydrocarbon oxygen outlet, the first condenser is arranged in the first condensation cavity, the first evaporator is arranged in the first evaporation cavity, the second rectifying tower is internally provided with a second condensation cavity at the top of the tower and a second evaporation cavity at the bottom of the tower, the middle lower part of the second rectifying tower is provided with an evaporator discharging inlet, the lower part of the first rectifying tower is arranged above the second evaporation cavity and is provided with a high-purity oxygen outlet, the second condenser is arranged in the second condensation cavity, the second evaporator is arranged in the second evaporation cavity, and the third condenser is arranged at the downstream of the second rectifying tower.

Description

High-purity liquid oxygen preparation facilities
Technical Field
The utility model relates to a technical field of high pure oxygen production especially relates to a high-purity liquid oxygen preparation facilities.
Background
When the low-temperature rectification method is used for producing the high-purity oxygen, the raw material generally adopts industrial oxygen or fraction oxygen, the impurities in the raw material oxygen mainly comprise nitrogen, argon and methane, and trace carbon dioxide, carbon monoxide, hydrocarbons, krypton, xenon, moisture and the like, and the impurities are removed in the low-temperature rectification process to obtain the high-purity oxygen product with the oxygen content of more than 99.999 percent.
The method for preparing high-purity oxygen mainly adopts a single-tower process gas oxygen feeding mode, and has the obvious defects that impurities with high and low boiling points are required to be removed in a single auxiliary tower, part of the impurities are difficult to remove, especially methane, so that the position for extracting raw material oxygen from a main tower is required to be proper. The quality of the high-purity oxygen product prepared by adopting the single-tower process flow is not high, and the high-purity oxygen product prepared by adopting the single-tower process flow has certain limitation, and the purity of the high-purity oxygen product prepared by adopting the single-tower process flow can only reach 99.995%. Therefore, a high purity liquid oxygen preparation apparatus is needed to produce high purity oxygen product with oxygen content of 99.999%.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a high-purity liquid oxygen preparation facilities can prepare the high pure oxygen product that the oxygen content reaches more than 99.999%.
To achieve the purpose, the utility model adopts the following technical proposal:
a high purity liquid oxygen production apparatus comprising:
the first rectifying tower is internally provided with a first condensation cavity at the top of the tower and a first evaporation cavity at the bottom of the tower, the middle part of the first rectifying tower is provided with a raw material oxygen inlet, and the upper part of the first rectifying tower, which is positioned below the first condensation cavity, is provided with a lean hydrocarbon oxygen outlet;
the first condenser is arranged in the first condensation cavity;
a first evaporator disposed within the first evaporation chamber;
the second rectifying tower is internally provided with a second condensation cavity at the top of the tower and a second evaporation cavity at the bottom of the tower, the middle lower part of the second rectifying tower is provided with an evaporator discharging inlet, and the lower part of the first rectifying tower, which is positioned above the second evaporation cavity, is provided with a high-purity oxygen outlet;
the second condenser is arranged in the second condensation cavity;
a second evaporator disposed within the second evaporation chamber;
a third condenser disposed downstream of the second rectification column;
raw material oxygen enters the first rectifying tower from the raw material oxygen inlet, after cold is absorbed in the first condensation cavity and heat is absorbed in the first evaporation cavity to remove part of heavy components, lean hydrocarbon oxygen is output from the lean hydrocarbon oxygen outlet and enters the second evaporator to absorb cold, after being output from the second evaporator, the lean hydrocarbon oxygen enters the second rectifying tower from the evaporator discharge inlet, high-purity oxygen is obtained after cold is absorbed in the second condensation cavity and heat is absorbed in the second evaporation cavity to remove light components and residual heavy components, and the high-purity oxygen is output from the high-purity oxygen outlet and enters the third condenser to be condensed to obtain high-purity liquid oxygen.
Optionally, the first condensation chamber is provided with a first liquid nitrogen inlet and a first nitrogen outlet, high-pressure nitrogen enters the first evaporator to absorb cold energy to generate liquid nitrogen, the liquid nitrogen enters the first condensation chamber from the first liquid nitrogen inlet to release cold energy and generate nitrogen, and the nitrogen is discharged from the first nitrogen outlet to the first condensation chamber and is pressurized by the first pressurization device to obtain the high-pressure nitrogen.
Optionally, a second liquid nitrogen inlet and a second nitrogen outlet are arranged on the second condensation cavity, part of the liquid nitrogen enters the second condensation cavity from the second liquid nitrogen inlet to release cold energy and generate nitrogen, and the nitrogen is discharged from the second nitrogen outlet out of the second condensation cavity and is pressurized by the first pressurization device to obtain the high-pressure nitrogen.
Optionally, part of the liquid nitrogen enters the third condenser to release cold energy and generate nitrogen, and the nitrogen is pressurized by the first pressurizing device to obtain the high-pressure nitrogen.
Optionally, the system further comprises a heat exchanger, and the cold energy is absorbed in the heat exchanger after the lean hydrocarbon oxygen is output from the lean hydrocarbon oxygen outlet and before the lean hydrocarbon oxygen enters the second evaporator.
Optionally, a second pressurizing device is included for pressurizing the lean hydrocarbon prior to introduction into the heat exchanger.
Optionally, part of the nitrogen discharged from the first condensation chamber is introduced into the heat exchanger to absorb heat before being pressurized;
and/or introducing part of the nitrogen discharged from the second condensation chamber into the heat exchanger to absorb heat before pressurization;
and/or introducing part of the nitrogen evaporated from the third condenser into the heat exchanger to absorb heat before pressurizing.
Optionally, the system further comprises supplementary liquid nitrogen, and the supplementary liquid nitrogen is mixed with the part of the liquid nitrogen which enters the second condensation cavity and releases cold energy;
and/or the supplementary liquid nitrogen is mixed with the part of the liquid nitrogen which enters the third condenser and releases cold energy.
Optionally, a light component outlet is arranged at the upper part of the second rectifying tower and below the second condensing cavity, and the light component is output from the light component outlet and enters the heat exchanger to absorb heat.
Optionally, the bottom of the first evaporation chamber is provided with a first heavy fraction discharge outlet from which the partially heavy fraction is discharged;
and a second heavy component discharge port is formed in the bottom of the second evaporation cavity, and the residual heavy component is discharged from the second heavy component discharge port.
The utility model has the advantages that:
the utility model provides a high-purity liquid oxygen preparation device, which comprises a first rectifying tower, a first condenser, a first evaporator, a second rectifying tower, a second condenser, a second evaporator and a third condenser, wherein, a first condensation cavity at the top of the tower and a first evaporation cavity at the bottom of the tower are arranged in the first rectifying tower, a raw material oxygen inlet is arranged at the middle part of the first rectifying tower, a poor hydrocarbon oxygen outlet is arranged at the lower part of the first condensation cavity at the upper part of the first rectifying tower, the first condenser is arranged in the first condensation cavity, the first evaporator is arranged in the first evaporation cavity, a second condensation cavity at the top of the tower and a second evaporation cavity at the bottom of the tower are arranged in the second rectifying tower, an evaporator discharging inlet is arranged at the middle lower part of the second rectifying tower, a high-purity oxygen outlet is arranged at the upper part of the second evaporation cavity at the lower part of the first rectifying tower, the second condenser is arranged in the second condensation cavity, the second evaporator is arranged in the second evaporation cavity, and the third condenser is arranged at the downstream of the second rectifying tower. Raw material oxygen enters the first rectifying tower from a raw material oxygen inlet, after cold is absorbed in the first condensation cavity and heat is absorbed in the first evaporation cavity to remove part of heavy components, lean hydrocarbon oxygen is output from a lean hydrocarbon oxygen outlet and enters the second evaporator to absorb cold, after being output from the second evaporator, the lean hydrocarbon oxygen enters the second rectifying tower from an evaporator discharge inlet, after cold is absorbed in the second condensation cavity and heat is absorbed in the second evaporation cavity to remove light components and residual heavy components, high-purity oxygen is obtained, and the high-purity oxygen is output from a high-purity oxygen outlet and enters the third condenser to be condensed to obtain high-purity liquid oxygen. The high-purity liquid oxygen preparation device can prepare a high-purity oxygen product with the oxygen content of more than 99.999%.
Drawings
Fig. 1 is a schematic structural diagram of a high-purity liquid oxygen production apparatus provided in an embodiment of the present invention.
In the figure:
1. a first rectification column; 2. a first condensation chamber; 3. a first evaporation chamber; 4. a first condenser; 5. a first evaporator; 6. a second rectification column; 7. a second condensation chamber; 8. a second evaporation chamber; 9. a second condenser; 10. a second evaporator; 11. a third condenser; 12. a raw material oxygen feed line; 13. a lean hydrocarbon oxidation line; 14. an evaporator discharge line; 15. a high purity oxygen line; 16. a high purity liquid oxygen pipeline; 17. a high pressure nitrogen input line; 18. a liquid nitrogen output pipeline; 19. a first nitrogen output line; 20. a first pressurizing device; 21. a heat exchanger; 22. a light component output pipeline; 23. a first heavies output line; 24. a second heavy component output line; 25. a second pressurizing device; 26. a second nitrogen output pipeline; 27. a first liquid nitrogen input pipeline; 28. a second liquid nitrogen input pipeline; 29. a third liquid nitrogen input pipeline; 30. a third nitrogen output pipeline; 31. and a fourth liquid nitrogen input pipeline.
Detailed Description
The technical solution of the present invention will be further explained with reference to the accompanying drawings and embodiments. It is to be understood that the specific embodiments described herein are merely illustrative of the invention and are not limiting of the invention. It should be further noted that, for the convenience of description, only some but not all of the elements related to the present invention are shown in the drawings.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection or a removable connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.
In the present disclosure, unless expressly stated or limited otherwise, the first feature "on" or "under" the second feature may comprise direct contact between the first and second features, or may comprise contact between the first and second features not directly. Also, the first feature being "on," "above" and "over" the second feature includes the first feature being directly on and obliquely above the second feature, or merely indicating that the first feature is at a higher level than the second feature. A first feature being "under," "below," and "beneath" a second feature includes the first feature being directly under and obliquely below the second feature, or simply meaning that the first feature is at a lesser elevation than the second feature.
As shown in fig. 1, this embodiment provides a high purity liquid oxygen preparation apparatus, which is suitable for using about 99.5% of liquid oxygen or oxygen as a raw material, and the raw material oxygen is finally purified by a double-tower rectification process to obtain 99.999% of high purity liquid oxygen. Specifically, the high purity liquid oxygen preparation apparatus provided by this embodiment includes: the system comprises a first rectifying tower 1, a first condenser 4, a first evaporator 5, a second rectifying tower 6, a second condenser 9, a second evaporator 10 and a third condenser 11. Wherein, be provided with the first condensation chamber 2 of top of the tower department and the first evaporation chamber 3 of bottom of the tower department in the first rectifying column 1, first condenser 4 sets up in first condensation chamber 2, and first evaporimeter 5 sets up in first evaporation chamber 3. The middle part of first rectifying column 1 is provided with raw materials oxygen import, and raw materials oxygen import department intercommunication has raw materials oxygen feed line 12, and raw materials oxygen feed line 12's the other end and raw materials oxygen store the device intercommunication, and raw materials oxygen can store the device from raw materials oxygen and get into raw materials oxygen feed line 12 to get into first rectifying column 1 through the import of raw materials oxygen. When liquid oxygen is selected as raw material oxygen, the liquid oxygen flows downwards after entering the first rectifying tower 1, and transfers heat and mass with a medium which is evaporated in the first evaporator 5 and flows upwards, finally, part of heavy components with higher evaporation temperature is remained in the first evaporation cavity 3 in a liquid phase, and a gas-phase mixture of part of heavy components with lower evaporation temperature, light components and oxygen forms poor hydrocarbon oxygen. When oxygen is selected as the raw material oxygen, the oxygen flows upward in the first rectifying column 1. On the upper portion of first rectifying column 1, be located the below of first condensation chamber 2, be provided with first condensation export and first condensation entry on the wall of first rectifying column 1, the first pipeline intercommunication first condensation export and the entry of first condenser 4, the export of second pipeline intercommunication first condensation entry and first condenser 4. After the raw material oxygen enters the first rectifying tower 1 and flows upwards, and transfers heat and mass with a medium which is condensed in the first condenser 4 and flows downwards, a formed gas-phase mixture rises to a first condensation outlet, is output from the first condensation outlet, reaches an inlet of the first condenser 4 through a first pipeline, and enters the first condenser 4 to absorb cold, wherein heavy components with higher evaporation temperature are firstly condensed, the gas-liquid mixture is output from an outlet of the first condenser 4 and returns to the first rectifying tower 1 from the first condensation inlet through a second pipeline, finally, part of the gas-phase mixture of the heavy components, the light components and the oxygen with lower evaporation temperature forms lean hydrocarbon oxygen, and part of the heavy components with higher evaporation temperature flows to the first evaporation cavity 3 in a liquid phase. The upper part of the first rectifying tower 1 is provided with a lean hydrocarbon outlet below the first condensing cavity 2, and the lean hydrocarbon outlet is communicated with a lean hydrocarbon pipeline 13.
A second condensation cavity 7 at the top of the tower and a second evaporation cavity 8 at the bottom of the tower are arranged in the second rectifying tower 6, a second condenser 9 is arranged in the second condensation cavity 7, and a second evaporator 10 is arranged in the second evaporation cavity 8. One end of the lean hydrocarbon oxygen pipeline 13 is communicated with the lean hydrocarbon oxygen outlet of the first rectifying tower 1, and the other end of the lean hydrocarbon oxygen pipeline 13 is communicated with the inlet of the second evaporator 10 in the second rectifying tower 6. The middle lower part of the second rectifying tower 6 is provided with an evaporator discharging inlet, and two ends of an evaporator discharging pipeline 14 are respectively communicated with an outlet of the second evaporator 10 and the evaporator discharging inlet on the second rectifying tower 6. The lean hydrocarbon oxygen flows into the second evaporator 10 through the lean hydrocarbon oxygen pipeline 13 to absorb cold energy, and the cold energy is output from the outlet of the second evaporator 10 and then reaches the evaporator discharging inlet through the evaporator discharging pipeline 14 and enters the second rectifying tower 6. A second condensation outlet and a second condensation inlet are arranged below the second condensation cavity 7 above the second rectifying tower 6, a third pipeline is communicated with the second condensation outlet and the inlet of the second condenser 9, and a fourth pipeline is communicated with the second condensation inlet and the outlet of the second condenser 9. In the second rectifying tower 6, the gas-phase mixture of the light components and the oxygen reaching the second condensation outlet flows out from the second condensation outlet, passes through the third pipeline, reaches the second condenser 9, absorbs cold energy, flows out from the outlet of the second condenser 9, and flows into the second rectifying tower 6 through the fourth pipeline and the second condensation inlet. The second rectifying tower 6 is also provided with a light component outlet below the second condensation outlet, and a high-purity oxygen outlet is also arranged below the second rectifying tower 6 and above the second evaporation cavity 8. In the second rectifying tower 6, the gas phase medium rises, the liquid phase medium falls, and after continuous heat and mass transfer and final stabilization, the residual heavy component with higher evaporation temperature flows to the second evaporation cavity 8 at the bottom of the second rectifying tower 6 in a liquid phase manner, the light component with lower evaporation temperature is discharged from the light component outlet on the second rectifying tower 6, and the high-purity oxygen is output from the high-purity oxygen outlet on the second rectifying tower 6.
A third condenser 11 is arranged at the downstream of the second rectifying tower 6, a high purity oxygen pipeline 15 is arranged between the second rectifying tower 6 and the third condenser 11, and two ends of the high purity oxygen pipeline 15 are respectively communicated with a high purity oxygen outlet and an inlet of the third condenser 11. A high-purity liquid oxygen pipeline 16 is arranged between the third condenser 11 and the liquid oxygen storage device, and two ends of the high-purity liquid oxygen pipeline 16 are respectively communicated with an outlet of the third condenser 11 and an inlet of the liquid oxygen storage device. The high-purity oxygen enters the third condenser 11 through the high-purity oxygen pipeline 15 to absorb cold energy and is condensed into high-purity liquid oxygen, and the high-purity liquid oxygen is output from the third condenser 11 and enters the liquid oxygen storage device through the high-purity liquid oxygen pipeline 16.
In order to effectively utilize the cold in the first evaporation cavity 3, the cold in the first evaporation cavity 3 is brought into the first condenser 4, and optionally, the cold in the first evaporation cavity 3 is absorbed and brought into the first condenser 4 by taking high-pressure nitrogen as a heat transfer medium. Specifically, a high-pressure nitrogen input pipeline 17 is arranged between the storage device for high-pressure nitrogen and the inlet of the first evaporator 5, a first liquid nitrogen inlet and a first nitrogen outlet which are respectively communicated with the first condensation cavity 2 are arranged on the wall surface of the first condensation cavity 2, the first liquid nitrogen inlet is communicated with the liquid phase cavity of the first condensation cavity 2, and the first nitrogen outlet is communicated with the gas phase cavity of the first condensation cavity 2. A liquid nitrogen output pipeline 18 and a first liquid nitrogen input pipeline 27 are arranged between the outlet of the first evaporator 5 and the first liquid nitrogen inlet, one end of the liquid nitrogen output pipeline 18 is communicated with the outlet of the first evaporator 5, the other end of the liquid nitrogen output pipeline 18 is communicated with one end of the first liquid nitrogen input pipeline 27, and the other end of the first liquid nitrogen input pipeline 27 is communicated with the first liquid nitrogen inlet. High-pressure nitrogen enters the first evaporator 5 from a high-pressure nitrogen storage device through a high-pressure nitrogen input pipeline 17, the high-pressure nitrogen absorbs cold in the first evaporation cavity 3 in the first evaporator 5 and is condensed to generate liquid nitrogen, the liquid nitrogen is output from an outlet of the first evaporator 5 and sequentially reaches a first liquid nitrogen inlet through a liquid nitrogen output pipeline 18 and a first liquid nitrogen input pipeline 27, and the liquid nitrogen enters the first condensation cavity 2 from the first liquid nitrogen inlet to release the cold and is evaporated to generate the nitrogen. Optionally, a first nitrogen outlet is arranged at the top of the first condensation chamber 2, and the first nitrogen outlet is communicated with the gas phase chamber in the first condensation chamber 2. Both ends of the first nitrogen output pipeline 19 are respectively communicated with the first nitrogen outlet and the high-pressure nitrogen input pipeline 17, and a first pressurizing device 20 is further arranged on the first nitrogen output pipeline 19. The nitrogen is discharged from the first nitrogen outlet, passes through the first nitrogen output pipeline 19, is pressurized by the first pressurizing device 20 to obtain high-pressure nitrogen, and enters the first evaporator 5 again through the high-pressure nitrogen input pipeline 17 to serve as a heat transfer medium, so that the cyclic utilization of the nitrogen is realized.
In order to further improve the energy efficiency, the cold energy in the first evaporation cavity 3 is utilized to a greater extent, and optionally, the liquid nitrogen obtained by condensation in the first evaporation cavity 3 partially enters the first condensation cavity 2 to release the cold energy and partially enters the second condensation cavity 7 to release the cold energy. Specifically, a second liquid nitrogen inlet and a second nitrogen outlet are arranged on the second condensation chamber 7, wherein the second liquid nitrogen inlet is communicated with the liquid phase chamber of the second condensation chamber 7, and the second nitrogen outlet is communicated with the gas phase chamber of the second condensation chamber 7. A second liquid nitrogen input pipeline 28 is further arranged between the first rectifying tower 1 and the second rectifying tower 6, one end of the second liquid nitrogen input pipeline 28 is communicated with the downstream end of the liquid nitrogen output pipeline 18, and the other end of the second liquid nitrogen input pipeline 28 is communicated with a second liquid nitrogen inlet of the second condensation cavity 7. A second nitrogen output pipeline 26 is further arranged between the first rectifying tower 1 and the second rectifying tower 6, one end of the second nitrogen output pipeline 26 is communicated with a second nitrogen outlet, the second nitrogen outlet is communicated with a gas phase chamber above the second condensation cavity 7, the other end of the second nitrogen output pipeline 26 is converged with the first nitrogen output pipeline 19 into one path, and the converged position is located at the upstream of the first pressurizing device 20. Part of the liquid nitrogen flows into the second liquid nitrogen input pipeline 28 from the liquid nitrogen output pipeline 18, enters the second condensation cavity 7 from the second liquid nitrogen inlet, releases cold energy and is evaporated to generate nitrogen gas, the nitrogen gas is discharged out of the second condensation cavity 7 from the second nitrogen outlet, enters the first nitrogen gas output pipeline 19 through the second nitrogen gas output pipeline 26, and is converged with the nitrogen gas generated in the first condensation cavity 2 in the first nitrogen gas output pipeline 19, and the converged nitrogen gas is pressurized by the first pressurizing device 20 to obtain high-pressure nitrogen gas. Similarly, the high-pressure nitrogen enters the first evaporator 5 again through the high-pressure nitrogen input pipeline 17 to serve as a heat transfer medium, so that the nitrogen is recycled.
In order to further improve the energy efficiency, the cold energy in the first evaporation cavity 3 is utilized to a greater extent, optionally, the liquid nitrogen obtained by condensation in the first evaporation cavity 3 is divided into three parts, the first part of liquid nitrogen enters the first condensation cavity 2 to release the cold energy, the second part of liquid nitrogen enters the second condensation cavity 7 to release the cold energy, and the third part of liquid nitrogen enters the third condenser 11 to release the cold energy. Specifically, a third liquid nitrogen input line 29 and a third nitrogen output line 30 are provided between the first rectifying column 1 and the third condenser 11. One end of a third liquid nitrogen input pipe 29 is communicated with the downstream end of the liquid nitrogen output pipe 18, and the other end of the third liquid nitrogen input pipe 29 is communicated with the inlet of the third condenser 11. One end of the third nitrogen output pipeline 30 is communicated with the outlet of the third condenser 11, and the other end of the third nitrogen output pipeline 30 is merged with the first nitrogen output pipeline 19 into a whole, and the merged part is positioned at the upstream of the first pressurizing device 20. Alternatively, in this embodiment, the other end of the third nitrogen output pipeline 30 is merged with the second nitrogen output pipeline 26 and then merged with the first nitrogen output pipeline 19, and the pipeline arrangement can be adjusted according to the actual orientation relationship between the devices. Part of the liquid nitrogen flows into the third liquid nitrogen input pipeline 29 from the liquid nitrogen output pipeline 18, enters the third condenser 11 from the inlet of the third condenser 11, releases cold energy and is evaporated to generate nitrogen gas, the nitrogen gas is discharged from the outlet of the third condenser 11, enters the second nitrogen gas output pipeline 26 through the third nitrogen gas output pipeline 30, is merged with the nitrogen gas generated in the second condensation chamber 7 in the second nitrogen gas output pipeline 26, the merged nitrogen gas enters the first nitrogen gas output pipeline 19 and is merged with the nitrogen gas generated in the first condensation chamber 2 in the first nitrogen gas output pipeline 19, and the three merged nitrogen gases are pressurized through the first pressurizing device 20 to obtain high-pressure nitrogen gas. Similarly, the high-pressure nitrogen enters the first evaporator 5 again through the high-pressure nitrogen input pipeline 17 to be used as a heat transfer medium, so that the nitrogen can be recycled.
In order to further improve the purification efficiency, the high-purity oxygen preparation device is optionally further provided with a heat exchanger 21, and the lean hydrocarbon oxygen enters the heat exchanger 21 to absorb cold after being output from the lean hydrocarbon oxygen outlet and before entering the second evaporator 10. Optionally, a second pressurizing device 25 is further disposed upstream of the heat exchanger 21, and the lean hydrocarbon is pressurized in the second pressurizing device 25 after being output from the lean hydrocarbon outlet and before entering the heat exchanger 21, so as to provide the power required for the subsequent heat exchange of the lean hydrocarbon in the heat exchanger 21 and the heat and mass transfer in the second rectifying tower 6.
In order to utilize the cold energy in the nitrogen gas efficiently, optionally, the part of the nitrogen gas discharged from the first condensation chamber 2 is introduced into the heat exchanger 21 to absorb heat energy (not shown in the figure) before entering the first pressurizing device 20 for pressurizing, so as to further release the cold energy absorbed by the part of the nitrogen gas from the first evaporation chamber 3, thereby improving the utilization rate of the cold energy. That is, the first nitrogen output line 19 is arranged at the upstream part of the first pressurizing device 20, and the first nitrogen output line 19 is firstly communicated with the pipeline of the heat exchanger 21, that is, the first nitrogen output line 19 is cut off, the upstream port of the cut-off is communicated with one inlet of the heat exchanger 21, and the downstream port of the cut-off is communicated with one outlet of the heat exchanger 21, so that the part of nitrogen is introduced into the heat exchanger 21 before being pressurized. It can be known that the lean hydrocarbon oxygen can absorb the part of cold released by the part of nitrogen in the heat exchanger 21 so as to improve the subsequent purification efficiency.
Optionally, the part of nitrogen discharged from the second condensation chamber 7 is introduced into the heat exchanger 21 to absorb heat before entering the first pressurizing device 20 for pressurizing, so that the nitrogen can further release the cold absorbed from the first evaporation chamber 3, thereby improving the utilization rate of the cold. In order to introduce the nitrogen into the heat exchanger 21 before pressurization, the pipeline is provided in various ways, for example, the second nitrogen output pipeline 26 is communicated with the pipeline of the heat exchanger 21 before the second nitrogen output pipeline 26 is merged with the third nitrogen output pipeline 30, namely, the second nitrogen output pipeline 26 has a cut, the upstream port of the cut is communicated with one inlet of the heat exchanger 21, and the downstream port of the cut is communicated with one outlet of the heat exchanger 21, so that the nitrogen is introduced into the heat exchanger 21 before pressurization. It can be known that the lean hydrocarbon oxygen can absorb the part of cold energy released by the part of nitrogen in the heat exchanger 21 so as to improve the subsequent purification efficiency and further improve the energy utilization rate.
Optionally, the part of nitrogen evaporated from the third condenser 11 is introduced into the heat exchanger 21 to absorb heat before entering the first pressurizing device 20 for pressurizing, and the nitrogen can further release the cold absorbed from the first evaporation cavity 3, so as to improve the utilization rate of the cold. In order to introduce the nitrogen into the heat exchanger 21 before pressurization, the pipeline is arranged in various ways, for example, the third nitrogen output pipeline 30 is communicated with the pipeline of the heat exchanger 21 before the third nitrogen output pipeline 30 is merged with the second nitrogen output pipeline 26, namely, the third nitrogen output pipeline 30 is cut off, the upstream port of the cut-off is communicated with one inlet of the heat exchanger 21, and the downstream port of the cut-off is communicated with one outlet of the heat exchanger 21, so that the nitrogen is introduced into the heat exchanger 21 before pressurization. It can be known that the lean hydrocarbon oxygen can absorb the part of cold energy released by the part of nitrogen in the heat exchanger 21 so as to improve the subsequent purification efficiency and further improve the energy utilization rate.
Optionally, in order to supplement cold energy, the high purity oxygen preparation apparatus is further provided with a fourth liquid nitrogen input pipeline 31, and the fourth liquid nitrogen input pipeline 31 is communicated with the second liquid nitrogen input pipeline 28, that is, the supplemental liquid nitrogen enters the second liquid nitrogen input pipeline 28 from the fourth liquid nitrogen input pipeline 31, and is mixed with part of liquid nitrogen entering the second condensation chamber to release cold energy, so that the cold energy in the second condensation chamber is supplemented. Or the fourth liquid nitrogen input pipeline 31 is communicated with the third liquid nitrogen input pipeline 29, namely the supplementary liquid nitrogen enters the third liquid nitrogen input pipeline 29 from the fourth liquid nitrogen input pipeline 31 and is mixed with part of liquid nitrogen which enters the third condenser and releases cold energy, so that the cold energy in the third condenser is supplemented. Alternatively, the fourth liquid nitrogen inlet line 31 is in communication with the second liquid nitrogen inlet line 28 and the manifold line upstream of the third liquid nitrogen inlet line 29, such that a portion of the make-up liquid nitrogen enters the second liquid nitrogen inlet line 28 and a portion of the make-up liquid nitrogen enters the third liquid nitrogen inlet line 29.
Alternatively, at least one of the nitrogen gas discharged from the first condensation chamber 2, the nitrogen gas discharged from the second condensation chamber 7 and the nitrogen gas discharged from the third condenser 11 is introduced into the heat exchanger 21 before pressurization, but it may be one of the nitrogen gas, two of the nitrogen gas may be introduced into the heat exchanger 21 separately or after being combined, or three of the nitrogen gas may be introduced into the heat exchanger 21 separately or after being combined. The arrangement of the pipeline can be adjusted according to the specific equipment orientation relationship, which is not described herein.
In order to realize the separation, discharge and collection of the light components and the recycling of the cold of the light components, a light component outlet is optionally arranged at the upper part of the second rectifying tower 6 below the second condensation chamber 7, and the light components are output from the light component outlet and enter the heat exchanger 21 to absorb heat. Specifically, a light component output pipeline 22 is arranged between the second rectifying tower 6 and the heat exchanger 21, one end of the light component output pipeline 22 is communicated with a light component outlet, the other end of the light component output pipeline is communicated with one inlet of the heat exchanger 21, and an outlet of the light component pipeline of the heat exchanger 21 can be communicated with a pipeline for discharging or communicated with a light component collecting device. It can be known that the lean hydrocarbon oxygen can absorb the cold energy released by the light component in the heat exchanger 21, so as to improve the subsequent purification efficiency and further improve the energy utilization rate.
In order to achieve separation, discharge and collection of the heavy fraction, the bottom of the first evaporation chamber 3 is optionally provided with a first heavy fraction discharge opening from which part of the heavy fraction is discharged, and the bottom of the second evaporation chamber 8 is provided with a second heavy fraction discharge opening from which the remaining heavy fraction is discharged. In particular, the first heavy fraction discharge opening communicates with the heavy fraction collecting device via a first heavy fraction outlet line 23, and the second heavy fraction discharge opening communicates with the heavy fraction collecting device via a second heavy fraction outlet line 24. Optionally, regulating valves are provided on the first heavy fraction output line 23 and the second heavy fraction output line 24 to control whether the heavy fraction is circulated and to control the amount of flow.
The operation principle of the high purity oxygen production apparatus is briefly described as follows:
raw material oxygen enters the first rectifying tower 1 from a raw material oxygen inlet, after cold is absorbed in the first condensation cavity 2 and heat is absorbed in the first evaporation cavity 3 to remove part of heavy components, lean hydrocarbon oxygen is output from a lean hydrocarbon oxygen outlet and enters the second evaporator 10 to absorb cold, after being output from the second evaporator 10, the lean hydrocarbon oxygen enters the second rectifying tower 6 from an evaporator discharge inlet, after cold is absorbed in the second condensation cavity 7 and heat is absorbed in the second evaporation cavity 8 to remove light components and residual heavy components, high-purity oxygen is obtained, and the high-purity oxygen is output from a high-purity oxygen outlet and enters the third condenser 11 to be condensed to obtain high-purity liquid oxygen. The high-purity liquid oxygen preparation device can prepare a high-purity oxygen product with the oxygen content of more than 99.999%, and through the circulating flow of the heat exchange medium and the arrangement of the heat exchanger 21, the energy utilization efficiency can be obviously improved, the energy is saved, the emission is reduced, and the economic cost is reduced.
It is obvious that the above embodiments of the present invention are only examples for clearly illustrating the present invention, and are not intended to limit the embodiments of the present invention. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. Any modification, equivalent replacement, and improvement made within the spirit and principle of the present invention should be included in the protection scope of the claims of the present invention.

Claims (10)

1. A high-purity liquid oxygen preparation device is characterized by comprising:
the device comprises a first rectifying tower (1), wherein a first condensation cavity (2) at the top of the tower and a first evaporation cavity (3) at the bottom of the tower are arranged in the first rectifying tower (1), a raw material oxygen inlet is formed in the middle of the first rectifying tower (1), and a lean hydrocarbon oxygen outlet is formed in the position, below the first condensation cavity (2), of the upper part of the first rectifying tower (1);
a first condenser (4), said first condenser (4) being arranged inside said first condensation chamber (2);
a first evaporator (5), said first evaporator (5) being arranged inside said first evaporation chamber (3);
a second rectifying tower (6), wherein a second condensation cavity (7) at the top of the tower and a second evaporation cavity (8) at the bottom of the tower are arranged in the second rectifying tower (6), an evaporator discharging inlet is arranged at the middle lower part of the second rectifying tower (6), and a high-purity oxygen outlet is arranged at the position, above the second evaporation cavity (8), of the lower part of the first rectifying tower (1);
a second condenser (9), said second condenser (9) being arranged inside said second condensation chamber (7);
a second evaporator (10), said second evaporator (10) being arranged inside said second evaporation chamber (8);
a third condenser (11), said third condenser (11) being arranged downstream of said second rectification column (6);
raw material oxygen enters the first rectifying tower (1) from the raw material oxygen inlet, lean hydrocarbon oxygen is output from the lean hydrocarbon oxygen outlet and enters the second evaporator (10) to absorb cold after absorbing cold in the first condensation cavity (2) and absorbing heat in the first evaporation cavity (3) to remove part of heavy components, lean hydrocarbon oxygen enters the second rectifying tower (6) from the evaporator discharge inlet after being output from the second evaporator (10), high-purity oxygen is obtained after absorbing cold in the second condensation cavity (7) and absorbing heat in the second evaporation cavity (8) to remove light components and residual heavy components, and high-purity oxygen is output from the high-purity oxygen outlet and enters the third condenser (11) to be condensed to obtain high-purity liquid oxygen.
2. The apparatus for preparing high purity liquid oxygen according to claim 1, further comprising a first pressurizing device (20), wherein the first condensation chamber (2) is provided with a first liquid nitrogen inlet and a first nitrogen gas outlet, the high pressure nitrogen gas enters the first evaporator (5) to absorb cold energy to generate liquid nitrogen, the liquid nitrogen enters the first condensation chamber (2) from the first liquid nitrogen inlet to release cold energy and generate nitrogen gas, and the nitrogen gas is discharged from the first condensation chamber (2) from the first nitrogen gas outlet and is pressurized by the first pressurizing device (20) to obtain the high pressure nitrogen gas.
3. The apparatus for preparing high-purity liquid oxygen according to claim 2, wherein the second condensation chamber (7) is provided with a second liquid nitrogen inlet and a second nitrogen outlet, part of the liquid nitrogen enters the second condensation chamber (7) from the second liquid nitrogen inlet to release cold energy and generate nitrogen gas, and the nitrogen gas is discharged from the second condensation chamber (7) from the second nitrogen outlet and is pressurized by the first pressurizing device (20) to obtain the high-pressure nitrogen gas.
4. The apparatus for producing high purity liquid oxygen according to claim 3, wherein a part of the liquid nitrogen enters the third condenser (11) to release cold and generate nitrogen gas, and the nitrogen gas is pressurized by the first pressurizing device (20) to obtain the high pressure nitrogen gas.
5. The apparatus for preparing high purity liquid oxygen according to claim 4, further comprising a heat exchanger (21), wherein the lean hydrocarbon oxygen is absorbed in the heat exchanger (21) after being output from the lean hydrocarbon oxygen outlet and before entering the second evaporator (10).
6. The apparatus for producing high purity liquid oxygen according to claim 5, further comprising a second pressurizing means (25), said second pressurizing means (25) being adapted to pressurize said lean hydrocarbon oxygen prior to introduction into said heat exchanger (21).
7. The apparatus for producing high purity liquid oxygen according to claim 5, wherein a portion of the nitrogen gas discharged from the first condensation chamber (2) is introduced into the heat exchanger (21) to absorb heat before being pressurized;
and/or a part of the nitrogen discharged from the second condensation chamber (7) is introduced into the heat exchanger (21) to absorb heat before being pressurized;
and/or a part of the nitrogen evaporated from the third condenser (11) is introduced into the heat exchanger (21) to absorb heat before being pressurized.
8. The apparatus for producing high purity liquid oxygen according to claim 4, further comprising a supplementary liquid nitrogen mixed with a portion of the liquid nitrogen which enters the second condensation chamber (7) and releases the cold;
and/or the supplementary liquid nitrogen is mixed with the part of the liquid nitrogen which enters the third condenser (11) and releases cold.
9. The apparatus for producing high purity liquid oxygen according to any one of claims 5 to 6, wherein a light component outlet is provided at an upper portion of the second rectifying column (6) below the second condensing chamber (7), and the light component is discharged from the light component outlet and enters the heat exchanger (21) to absorb heat.
10. The high purity liquid oxygen production apparatus according to any one of claims 1 to 8, wherein a first heavy component discharge port is provided at the bottom of the first evaporation chamber (3), and the part of the heavy component is discharged from the first heavy component discharge port;
the bottom of the second evaporation cavity (8) is provided with a second heavy component outlet from which the residual heavy component is discharged.
CN202120367682.5U 2021-02-07 2021-02-07 High-purity liquid oxygen preparation facilities Active CN214469628U (en)

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