CN212133047U - Liquid oxygen evaporator system - Google Patents

Liquid oxygen evaporator system Download PDF

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Publication number
CN212133047U
CN212133047U CN202020760702.0U CN202020760702U CN212133047U CN 212133047 U CN212133047 U CN 212133047U CN 202020760702 U CN202020760702 U CN 202020760702U CN 212133047 U CN212133047 U CN 212133047U
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Prior art keywords
evaporator
liquid oxygen
oxygen
liquid
tower
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CN202020760702.0U
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Chinese (zh)
Inventor
李瀚�
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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
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04103—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression using solely hydrostatic liquid head
    • 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
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • 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
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • F25J3/04884—Arrangement of reboiler-condensers
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/46—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One fluid being air
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/50—One fluid being oxygen

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

Abstract

The utility model discloses a liquid oxygen evaporator system, liquid oxygen evaporator system includes: the air separation rectification equipment comprises an upper tower, a lower tower and a main condensation evaporator; the top of the liquid oxygen evaporator is lower than the bottom of the main condensation evaporator; the liquid oxygen evaporator is connected with the compressed air conveying device, the lower tower, the main condensation evaporator and the upper tower, and a pressure regulating valve is arranged between the liquid oxygen evaporator and the upper tower so as to regulate the pressure in the liquid oxygen evaporator by putting oxygen in the liquid oxygen evaporator into the upper tower through the pressure regulating valve. The top of the liquid oxygen evaporator is set to be lower than the bottom of the main condensation evaporator, so that a liquid oxygen pump is not needed to convey liquid oxygen in the main condensation evaporator to the liquid oxygen evaporator; a pressure regulating valve is arranged between the liquid oxygen evaporator and the upper tower, and the pressure at the upper part of the liquid oxygen evaporator can be regulated by regulating the pressure regulating valve, so that the pressure of oxygen delivery is regulated, and the regulation of the pressure regulating valve can also be beneficial to conveying liquid oxygen to the liquid oxygen evaporator.

Description

Liquid oxygen evaporator system
Technical Field
The utility model relates to an industry oxygen preparation technical field especially relates to a liquid oxygen evaporator system.
Background
At present, the high-purity oxygen used in industry is generally realized by adopting an air separation cryogenic rectification process. The air separation rectification mostly uses an upper tower, a lower tower and main condensationThe evaporator is used for preparing liquid oxygen, then the liquid oxygen is pressurized through the liquid oxygen pump, and the liquid oxygen is gasified into oxygen for customers to use through heat exchange with the high-pressure main heat exchanger. The process is suitable for 10000NM3Large air separation above the oxygen/h, but low requirements on oxygen pressure and low customer applicability. The process needs to pressurize the liquid oxygen through the liquid oxygen pump, so that the cost is increased, the liquid oxygen pump needs to be maintained when in failure, the operation cost of equipment is high, and the oxygen quality is difficult to ensure.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a liquid oxygen evaporimeter system to need set up liquid oxygen pump and come pressure boost liquid oxygen when solving among the prior art preparation oxygen, equipment cost and maintenance cost are all higher, and the problem that the oxygen quality is difficult to the assurance.
To achieve the purpose, the utility model adopts the following technical proposal:
a liquid oxygen vaporizer system, comprising:
the air separation rectification equipment comprises an upper tower, a lower tower and a main condensation evaporator;
the top of the liquid oxygen evaporator is lower than the bottom of the main condensation evaporator;
the liquid oxygen evaporator is connected with a compressed air conveying device, so that the compressed air conveying device conveys compressed air into the liquid oxygen evaporator;
the liquid oxygen evaporator is connected with the lower tower, so that compressed air in the liquid oxygen evaporator flows into the lower tower;
the liquid oxygen evaporator is connected with the main condensation evaporator so that liquid oxygen in the main condensation evaporator flows into the liquid oxygen evaporator;
the liquid oxygen evaporator is connected with the upper tower, and a pressure regulating valve is arranged between the liquid oxygen evaporator and the upper tower, so that oxygen in the liquid oxygen evaporator is put into the upper tower through the pressure regulating valve to regulate the pressure in the liquid oxygen evaporator.
Optionally, a liquid oxygen delivery valve is arranged between the main condensation evaporator and the liquid oxygen evaporator.
Optionally, a pneumatic valve for compressed air to enter the tower is arranged between the liquid oxygen evaporator and the lower tower.
Optionally, a liquid oxygen discharge valve is arranged at the bottom of the liquid oxygen evaporator.
Optionally, the top of the liquid oxygen evaporator is connected with an oxygen conveying pipeline to convey oxygen outwards.
Optionally, a main heat exchanger is arranged between the liquid oxygen evaporator and the oxygen conveying pipeline.
Optionally, the oxygen delivery pipeline includes an oxygen delivery pipeline and an oxygen emptying pipeline.
Optionally, an oxygen delivery valve is arranged on the oxygen delivery pipe, and an oxygen release valve is arranged on the oxygen release pipe.
Optionally, the top of the liquid oxygen evaporator is 15-23m lower than the bottom of the main condensing evaporator.
Compared with the prior art, the beneficial effects of the utility model are that:
the top of the liquid oxygen evaporator is set to be lower than the bottom of the main condensation evaporator, so that a liquid oxygen pump is not needed to convey liquid oxygen in the main condensation evaporator to the liquid oxygen evaporator;
a pressure regulating valve is arranged between the liquid oxygen evaporator and the upper tower, and the upper pressure of the liquid oxygen evaporator is regulated by regulating the pressure regulating valve, so that the purpose of regulating the oxygen output pressure is achieved;
the pressure regulating valve can be opened to be larger when the actual pressure of the liquid oxygen evaporator exceeds a set pressure value, redundant oxygen in the liquid oxygen evaporator is discharged back to the upper tower, and then the upper tower is pressurized, namely the upper pressure of the liquid oxygen liquid level of the main condensation evaporator is increased, so that the pressure difference between the liquid oxygen liquid level in the main condensation evaporator and the liquid oxygen liquid level in the liquid oxygen evaporator is increased, the liquid oxygen is conveyed to the liquid oxygen evaporator, and a virtuous cycle is formed.
Drawings
Fig. 1 is a schematic structural diagram of a liquid oxygen evaporator system in an embodiment of the present invention.
In the figure:
100. a liquid oxygen evaporator system; 10. a liquid oxygen evaporator; 20. feeding the tower; 30. descending the tower; 40. a main condensing evaporator; 50. an oxygen delivery line; 60. a primary heat exchanger;
11. a liquid oxygen discharge valve; 21. a pressure regulating valve; 31. compressed air enters a tower pneumatic valve; 41. a liquid oxygen delivery valve; 51. an oxygen delivery pipeline; 52. an oxygen vent line; 53. an oxygen delivery valve; 54. an oxygen emptying valve.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings and examples. 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 of the structures related to the present invention are shown in the drawings, not all of the structures.
In the description of the present invention, unless expressly stated or limited otherwise, the terms "connected," "connected," and "fixed" are to be construed broadly, e.g., as meaning permanently connected, detachably connected, or integral to one another; can be mechanically or electrically connected; either directly or indirectly through intervening media, either internally or in any other relationship. The meaning of the above terms in the present invention can be understood by those of ordinary skill in the art as the case may be.
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.
The technical solution of the present invention is further explained by the following embodiments with reference to the accompanying drawings.
The utility model provides a liquid oxygen evaporator system, figure 1 is the utility model discloses in the embodiment of the structural schematic of liquid oxygen evaporator system, as shown in figure 1, liquid oxygen evaporator system 100 includes empty rectifying equipment and liquid oxygen evaporator 10 that divides, and empty rectifying equipment that divides includes tower 20, lower tower 30 and main condensation evaporator 40. The top of the liquid oxygen evaporator 10 is lower than the bottom of the main condensation evaporator 40, so that the height difference exists between the liquid oxygen evaporator 10 and the main condensation evaporator 40, the liquid oxygen prepared by the main condensation evaporator 40 can flow into the liquid oxygen evaporator 10 through pressure difference without being conveyed through a liquid oxygen pump, the use of the liquid oxygen pump can be omitted, the equipment cost and the maintenance cost are reduced, and the quality of the liquid oxygen can be better ensured without the liquid oxygen pump. Generally, the height difference between the liquid oxygen evaporator 10 and the main condensing evaporator 40 is 15-23m, preferably 18m, that is, compared with the prior art, the liquid oxygen evaporator 10 is moved down by 18m in the present application, so that the height difference between the bottom of the main condensing evaporator 40 and the top of the liquid oxygen evaporator 10 is 18m, plus the height of the main condensing evaporator 40 is about 2m, the static pressure difference reaches 20m, according to the static pressure difference formula gh ρ, the generated static pressure difference of liquid oxygen is 1.14 × 9.8 × 20 — 2.23bar, and the oxygen supply pressure required by the customer is not high, which is about 1.6bar, so that the customer demand can be met, and the liquid oxygen pump is not needed, the cost is low, and the oxygen quality is good.
The liquid oxygen evaporator 10 is connected to a compressed air delivery device, which is generally an expander, as shown in fig. 1, the expander delivers compressed air into the liquid oxygen evaporator 10, and the liquid oxygen in the liquid oxygen evaporator 10 exchanges heat with the compressed air from the expander to evaporate the liquid oxygen, and then delivers the evaporated liquid oxygen.
The liquid oxygen evaporator 10 is connected to the lower column 30 so that the compressed air in the liquid oxygen evaporator 10 flows into the lower column 30, and then air-separated rectification is performed on the compressed air in the lower column 30, the upper column 20 and the main condensation evaporator 40 to prepare liquid oxygen, and the compressed air rises from the lower column 30 to the upper column 20 and is condensed into liquid oxygen in the main condensation evaporator 40. The principle of the space division rectification is the prior art, and the detailed description is not repeated here.
The liquid oxygen evaporator 10 is also connected to the main condensing evaporator 40 so that the liquid oxygen in the main condensing evaporator 40 flows into the liquid oxygen evaporator 10, is evaporated again in the liquid oxygen evaporator 10, and is transported to the outside.
The liquid oxygen evaporator 10 is connected with the upper tower 20, and a pressure regulating valve 21 is arranged between the liquid oxygen evaporator 10 and the upper tower 20, so that the pressure in the liquid oxygen evaporator 10 is regulated by putting oxygen in the liquid oxygen evaporator 10 into the upper tower 20 through the pressure regulating valve 21, and the upper pressure of the liquid oxygen evaporator 10 is regulated by regulating the pressure regulating valve 21, thereby realizing the purpose of regulating the oxygen sending pressure.
In addition, the pressure regulating valve 21 can be opened slightly when the actual pressure of the liquid oxygen evaporator 10 exceeds the set pressure value, so that the redundant oxygen in the liquid oxygen evaporator 10 is discharged back to the upper tower 20, and the upper tower 20 is pressurized, that is, the upper pressure of the liquid oxygen liquid level in the main condensation evaporator 40 is increased, so that the pressure difference between the liquid oxygen liquid level in the main condensation evaporator 40 and the liquid oxygen liquid level in the liquid oxygen evaporator 10 is increased, and the liquid oxygen in the main condensation evaporator 40 is conveyed to the liquid oxygen evaporator 10 to form a virtuous cycle.
Referring to fig. 1, a liquid oxygen delivery valve 41 is disposed between the main condensing evaporator 40 and the liquid oxygen evaporator 10, and the liquid oxygen delivery valve 41 can control the on/off and the flow rate of the flow path from the main condensing evaporator 40 to the liquid oxygen evaporator 10.
With continued reference to fig. 1, a compressed air inlet pneumatic valve 31 is disposed between the liquid oxygen evaporator 10 and the lower tower 30, and the compressed air inlet pneumatic valve 31 can control the on/off of the compressed air flow path and the flow rate of the compressed air flowing into the lower tower 30 from the liquid oxygen evaporator 10.
As shown in FIG. 1, a liquid oxygen discharge valve 11 is provided at the bottom of the liquid oxygen evaporator 10, so that the excess liquid oxygen in the liquid oxygen evaporator 10 can be discharged out of the system to produce liquid oxygen.
Referring to fig. 1, the top of the liquid oxygen evaporator 10 is connected to an oxygen supply line 50, and the oxygen supply line 50 supplies oxygen evaporated in the liquid oxygen evaporator 10 to the outside.
Further, a main heat exchanger 60 is disposed between the liquid oxygen evaporator 10 and the oxygen delivery pipeline 50, so that the oxygen can be temperature-regulated by the main heat exchanger 60 to reach a temperature suitable for being delivered to the outside.
Further, the oxygen delivery pipeline 50 includes an oxygen delivery pipeline 51 and an oxygen emptying pipeline 52, the oxygen delivery pipeline 51 is used for delivering oxygen to the customer, and the oxygen emptying pipeline 52 is used for emptying oxygen in the system to stabilize the oxygen flow.
Further, an oxygen delivery valve 53 is disposed on the oxygen delivery line 51, and an oxygen release valve 54 is disposed on the oxygen release line 52 to control the on-off and flow rate of each line.
In one embodiment, the liquid oxygen delivery valve 41, the compressed air inlet tower pneumatic valve 31, the liquid oxygen discharge valve 11, the oxygen delivery valve 53, and the oxygen purge valve 54 are all pneumatic valves, and the control of each pneumatic valve is written into a PLC (Programmable Logic Controller) control program and controlled by an upper computer.
The working process of the liquid oxygen evaporator system 100 of the present invention is (please refer to fig. 1):
compressed air from the expander enters the liquid oxygen evaporator 10 and enters the lower tower 30 from the liquid oxygen evaporator 10;
the compressed air ascends in the lower tower 30 and ascends to the upper tower 20, and liquid oxygen production is performed in the main condensing evaporator 40;
the liquid oxygen in the main condensing evaporator 40 flows into the liquid oxygen evaporator 10 under the effect of the static pressure difference;
the liquid oxygen in the liquid oxygen evaporator 10 exchanges heat with the compressed air, evaporates into oxygen, and is delivered to the customer from the oxygen delivery pipeline 51;
when the pressure in the liquid oxygen evaporator 10 is too high, the pressure regulating valve 21 is regulated, so that the oxygen in the liquid oxygen evaporator 10 enters the upper tower 20, the regulation of the pressure in the liquid oxygen evaporator 10 is realized, and after the oxygen enters the upper tower 20, the upper pressure of the liquid oxygen liquid level of the main condensation evaporator 40 can be increased, which is favorable for conveying the liquid oxygen in the main condensation evaporator 40 to the liquid oxygen evaporator 10 to form a virtuous cycle;
when the system needs maintenance, the oxygen of the system is discharged through the liquid oxygen discharging valve 11 arranged at the bottom of the liquid oxygen evaporator 10 and the oxygen gas discharging valve 54 of the oxygen gas discharging pipeline 52.
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. Numerous obvious variations, rearrangements and substitutions will now occur to those skilled in the art without departing from the scope of the invention. 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 (9)

1. A liquid oxygen vaporizer system, comprising:
the air separation rectification equipment comprises an upper tower (20), a lower tower (30) and a main condensation evaporator (40);
a liquid oxygen evaporator (10), the top of the liquid oxygen evaporator (10) being lower than the bottom of the main condensing evaporator (40);
the liquid oxygen evaporator (10) is connected with a compressed air conveying device, so that the compressed air conveying device conveys compressed air into the liquid oxygen evaporator (10);
the liquid oxygen evaporator (10) is connected with the lower tower (30) so that the compressed air in the liquid oxygen evaporator (10) flows into the lower tower (30);
the liquid oxygen evaporator (10) is connected with the main condensation evaporator (40) so that the liquid oxygen in the main condensation evaporator (40) flows into the liquid oxygen evaporator (10);
the liquid oxygen evaporator (10) is connected with the upper tower (20), and a pressure regulating valve (21) is arranged between the liquid oxygen evaporator (10) and the upper tower (20) so as to regulate the pressure in the liquid oxygen evaporator (10) by putting oxygen in the liquid oxygen evaporator (10) into the upper tower (20) through the pressure regulating valve (21).
2. The liquid oxygen evaporator system according to claim 1, wherein a liquid oxygen delivery valve (41) is provided between the main condensing evaporator (40) and the liquid oxygen evaporator (10).
3. The liquid oxygen evaporator system according to claim 1, wherein a compressed air inlet tower pneumatic valve (31) is provided between the liquid oxygen evaporator (10) and the lower tower (30).
4. The liquid oxygen evaporator system according to claim 1, wherein a liquid oxygen discharge valve (11) is provided at the bottom of the liquid oxygen evaporator (10).
5. The liquid oxygen evaporator system according to claim 1, wherein the top of the liquid oxygen evaporator (10) is connected with an oxygen delivery line (50) to deliver oxygen outwards.
6. The liquid oxygen evaporator system according to claim 5, wherein a main heat exchanger (60) is provided between the liquid oxygen evaporator (10) and the oxygen delivery line (50).
7. The liquid oxygen vaporizer system of claim 5, wherein the oxygen delivery line (50) comprises an oxygen egress line (51) and an oxygen vent line (52).
8. The liquid oxygen evaporator system according to claim 7, wherein an oxygen delivery valve (53) is provided on the oxygen delivery line (51), and an oxygen release valve (54) is provided on the oxygen release line (52).
9. The liquid oxygen evaporator system according to claim 1, wherein the top of the liquid oxygen evaporator (10) is 15-23m lower than the bottom of the main condenser evaporator (40).
CN202020760702.0U 2020-05-09 2020-05-09 Liquid oxygen evaporator system Active CN212133047U (en)

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Application Number Priority Date Filing Date Title
CN202020760702.0U CN212133047U (en) 2020-05-09 2020-05-09 Liquid oxygen evaporator system

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Application Number Priority Date Filing Date Title
CN202020760702.0U CN212133047U (en) 2020-05-09 2020-05-09 Liquid oxygen evaporator system

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