CN114017990B - Small air separation device for preparing low-pressure low-purity oxygen and medium-pressure nitrogen - Google Patents

Small air separation device for preparing low-pressure low-purity oxygen and medium-pressure nitrogen Download PDF

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Publication number
CN114017990B
CN114017990B CN202111306506.1A CN202111306506A CN114017990B CN 114017990 B CN114017990 B CN 114017990B CN 202111306506 A CN202111306506 A CN 202111306506A CN 114017990 B CN114017990 B CN 114017990B
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low
pressure
pipeline
oxygen
heat exchanger
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CN114017990A (en
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任文
莫方淑
黄震宇
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Sichuan Air Separation Plant Group Co ltd
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Sichuan Air Separation Plant Group 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
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of 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
    • 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
    • F25J3/04084—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 nitrogen
    • 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
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F25J3/04115—Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
    • 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
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest 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
    • F25J3/04151—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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary 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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or 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
    • F25J3/04406—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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/42—Nitrogen or special cases, e.g. multiple or low purity N2
    • 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
    • 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 invention provides a small air separation device for preparing low-pressure low-purity oxygen and medium-pressure nitrogen, which comprises a first raw material pipeline, a first heat exchanger, a second heat exchanger, an expander, a rectifying tower, a product low-purity oxygen pipeline and a product nitrogen pipeline; the rectifying tower is sequentially provided with a pressure tower, a condensing evaporator and an atmospheric tower from bottom to top; the first raw material pipeline is connected with the pressure tower through a first heat exchanger and an expander; the pressure tower is connected with the normal pressure tower through a second heat exchanger; the low-purity liquid oxygen extraction port arranged on the evaporation side of the condensing evaporator is connected with a low-purity liquid oxygen pump through a pipeline, and the outlet of the low-purity liquid oxygen pump is connected with a low-purity oxygen pipeline of a product after passing through the first heat exchanger through the pipeline; the liquid nitrogen extraction port arranged on the condensation side of the condensation evaporator is connected with a liquid nitrogen pump through a pipeline, and the outlet of the liquid nitrogen pump is connected with a product nitrogen pipeline after passing through the first heat exchanger through the pipeline. The invention has lower energy consumption and simplified configuration, and reduces investment cost and later maintenance cost.

Description

Small air separation device for preparing low-pressure low-purity oxygen and medium-pressure nitrogen
Technical Field
The invention relates to the technical field of low-temperature gas separation, in particular to a small air separation device for preparing low-pressure low-purity oxygen and medium-pressure nitrogen.
Background
In the air separation process of the conventional booster turbo expander refrigeration, an air compressor, a low-purity oxygen compressor or a nitrogen compressor with corresponding exhaust pressure is matched for obtaining the pressure of the corresponding low-purity oxygen or nitrogen product. If the manufacturer wants to increase the pressure of the nitrogen product, the above exhaust pressure needs to be increased accordingly.
Some manufacturers have smaller demand for oxygen and nitrogen products, and low-purity oxygen has high pressurization investment and high later maintenance cost if an oxygen compressor is adopted; the nitrogen is higher in cost if a nitrogen press is adopted, and if the nitrogen is directly pumped by a pressure tower, the working pressure of the pressure tower is required to be increased, so that the energy consumption is increased; if a conventional internal compression flow is adopted to configure a supercharger, the flow rate of the supercharger is small, the supercharger is not suitable for selection, and the investment is high. The air separation device with the configuration can correspondingly increase investment cost and later maintenance cost, and is not suitable for production enterprises with smaller oxygen and nitrogen product requirements.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a small air separation device for preparing low-pressure low-purity oxygen and medium-pressure nitrogen, which solves the problem that the air separation device with the existing configuration is not suitable for manufacturing enterprises with smaller oxygen and nitrogen product requirements.
In order to achieve the above purpose, the present invention provides the following technical solutions:
a small air separation plant for producing low pressure low purity oxygen and medium pressure nitrogen comprising:
The device comprises a first raw material pipeline, a first heat exchanger, a second heat exchanger, an expander, a rectifying tower, a product low-purity oxygen pipeline and a product nitrogen pipeline;
The expander is provided with a pressurizing end and an expansion end;
the rectifying tower is sequentially provided with a pressure tower, a condensing evaporator and an atmospheric tower from bottom to top;
The first raw material pipeline enters the first heat exchanger and is divided into a first branch and a second branch, the first branch returns to the first heat exchanger through the expansion end of the expander and is connected with the bottom of the pressure tower, and the second branch exits the first heat exchanger and is connected with the lower part of the pressure tower;
An oxygen-enriched liquid air outlet arranged at the bottom of the pressure tower is connected with an oxygen-enriched liquid air inlet arranged at the lower part or the middle part of the normal pressure tower after passing through the second heat exchanger through a pipeline;
The low-purity liquid oxygen extraction port arranged on the evaporation side of the condensation evaporator is connected with a low-purity liquid oxygen pump through a pipeline, and the outlet of the low-purity liquid oxygen pump is connected with the low-purity oxygen pipeline of the product after passing through the first heat exchanger through a pipeline;
The liquid nitrogen extraction port arranged on the condensation side of the condensation evaporator is connected with a liquid nitrogen pump through a pipeline, and the outlet of the liquid nitrogen pump is connected with the product nitrogen pipeline after passing through the first heat exchanger through a pipeline.
In one embodiment of the disclosure, the system further comprises a second raw material pipeline, a pressurized aftercooler, a low-purity liquid oxygen evaporator and a third heat exchanger;
the second raw material pipeline sequentially passes through the compression end of the expander, the post-pressurization cooler, the first heat exchanger, the low-purity liquid oxygen evaporator and the third heat exchanger and then is connected with the lower part of the pressure tower.
In one embodiment of the disclosure, the low-purity liquid oxygen pump outlet pipeline is connected with the low-purity liquid oxygen evaporator after passing through the third heat exchanger;
the top of the low-purity liquid oxygen evaporator is connected with the low-purity oxygen pipeline of the product after passing through the first heat exchanger through a pipeline.
In one embodiment of the application, the bottom of the low-purity liquid oxygen evaporator is provided with a low-purity liquid oxygen discharge port for extracting a small amount of low-purity liquid oxygen to be used as oxygen evaporation safety discharge or as low-purity liquid oxygen of a product.
In one embodiment of the disclosure, the liquid nitrogen extraction port on the condensation side of the condensation evaporator is provided with a third branch, a fourth branch and a fifth branch which are connected in parallel;
The third branch is connected with the inlet of the liquid nitrogen pump, the fourth branch is connected with the top of the pressure tower, and the fifth branch is connected with the top of the normal pressure tower after passing through the second heat exchanger.
In one embodiment of the disclosure, a sixth branch is connected after the fifth branch exits the second heat exchanger and is used for outputting product liquid nitrogen.
In one embodiment of the disclosure, a lean liquid air extraction port arranged at the lower part of the pressure tower is connected with the middle part of the atmospheric tower after passing through the second heat exchanger through a pipeline.
In one embodiment of the application, a dirty nitrogen outlet arranged at the top of the atmospheric tower is connected with a dirty nitrogen discharge pipeline after sequentially passing through the second heat exchanger and the first heat exchanger through pipelines.
In one embodiment of the present disclosure, the medium entering the first feed line is purified air at a pressure of about 8bar (G).
In one embodiment of the present disclosure, the medium entering the product low purity oxygen line is normal temperature low pressure low purity oxygen at a pressure of about 3bar (G), and the medium entering the product nitrogen line is normal temperature medium pressure nitrogen at a pressure of 5-8 bar (G).
Compared with the prior art, the invention has the beneficial effects that:
1. Under the condition of lower comprehensive energy consumption or equivalent, an oxygen compressor, a nitrogen compressor or a supercharger required by a conventional device is omitted, equipment configuration is simplified, equipment investment, factory building cost and later maintenance cost can be obviously reduced, and therefore economic benefits of enterprises are effectively improved, and the method is very suitable for production enterprises with smaller oxygen and nitrogen product requirements.
2. The refrigerated expansion air firstly enters the pressure tower for rectification, so that the comprehensive utilization rate of oxygen and nitrogen is high, and the comprehensive energy consumption of the device is reduced.
Drawings
In order to more clearly illustrate the embodiments of the application or the technical solutions in the prior art, the following description will briefly explain the drawings used in the embodiments or the description of the prior art, and it is obvious that the drawings in the following description are only some embodiments of the application, and that other drawings can be obtained according to these drawings without inventive effort to a person skilled in the art.
FIG. 1 is a schematic illustration of the process flow of the present invention.
Detailed Description
Hereinafter, only certain exemplary embodiments are briefly described. As will be recognized by those of skill in the pertinent art, the described embodiments may be modified in various different ways without departing from the spirit or scope of the present invention. Accordingly, the drawings and description are to be regarded as illustrative in nature and not as restrictive.
In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the present invention and simplifying the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present invention.
Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise.
In the present invention, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
In the present invention, unless expressly stated or limited otherwise, a first feature "above" or "below" a second feature may include both the first and second features being in direct contact, as well as the first and second features not being in direct contact but being in contact with each other through additional features therebetween. Moreover, a first feature being "above," "over" and "on" a second feature includes the first feature being directly above and obliquely above the second feature, or simply indicating that the first feature is higher in level than the second feature. The first feature being "under", "below" and "beneath" the second feature includes the first feature being directly under and obliquely below the second feature, or simply means that the first feature is less level than the second feature.
The following disclosure provides many different embodiments, or examples, for implementing different features of the invention. In order to simplify the present disclosure, components and arrangements of specific examples are described below. They are, of course, merely examples and are not intended to limit the invention.
Embodiments of the present invention will be described in detail below with reference to the accompanying drawings.
Referring to fig. 1, the present invention provides a small-sized air separation unit for preparing low-pressure low-purity oxygen and medium-pressure nitrogen, comprising:
the device comprises a first raw material pipeline, a first heat exchanger E1, an expander ET401, a rectifying tower, a second heat exchanger E2, a product low-purity oxygen pipeline and a product nitrogen pipeline;
the rectifying tower is provided with a pressure tower C1, a condensing evaporator K1 and an atmospheric tower C2 from bottom to top in sequence;
The first raw material pipeline enters the first heat exchanger E1 and then is divided into a first branch and a second branch, the first branch returns to the first heat exchanger E1 through the expansion end of the expander ET401 and then is connected with the bottom of the pressure tower C1, and the second branch exits the first heat exchanger E1 and then is connected with the lower part of the pressure tower C1;
the bottom of the pressure tower C1 is provided with an oxygen-enriched liquid air outlet which is connected with an oxygen-enriched liquid air inlet arranged at the lower part or the middle part of the atmospheric tower C2 after passing through the second heat exchanger E2 through a pipeline;
The low-purity liquid oxygen extraction port arranged on the evaporation side of the condensation evaporator K1 is connected with a low-purity liquid oxygen pump OP1 through a pipeline, and the outlet of the low-purity liquid oxygen pump OP1 is connected with a low-purity oxygen pipeline of a product after passing through the first heat exchanger E1 through the pipeline;
the liquid nitrogen extraction port arranged on the condensation side of the condensation evaporator K1 is connected with a liquid nitrogen pump NP1 through a pipeline, and the outlet of the liquid nitrogen pump NP1 is connected with a product nitrogen pipeline after passing through the first heat exchanger E1 through a pipeline.
Specifically, the raw AIR for preparing oxygen and nitrogen is compressed and pretreated to obtain purified AIR at a pressure of about 8bar (G), and is divided into two parts of purified AIR 101 (the medium flowing in the pipeline in the figure is shown by pure numerals, and the same applies hereinafter) and purified AIR 121. The operation of the embodiment of the present application will be described with reference to the flow direction of the purified air 101, and further described with reference to the flow direction of the purified air 121.
Purified air 101 enters a first heat exchanger E1 from a first raw material pipeline and is cooled to a certain temperature and then is divided into two parts of cold air 102 and cold air 111: the cold air 102 enters a first branch and is pumped out from the middle section of the first heat exchanger E1, then enters an expansion end driven by an expander ET401 to expand and refrigerate, the expanded cold air 103 returns to the first heat exchanger E1 to be continuously cooled into cold air 104 with lower temperature, and the cold air 104 enters the bottom of the pressure tower C1 to participate in rectification; the cold air 111 enters the second branch, is continuously cooled in the first heat exchanger E1 and is liquefied into liquid air 112, and the liquid air 112 throttles into the lower part of the pressure tower C1 to participate in rectification.
After rectifying in the pressure column C1, an oxygen-enriched liquid space 201 is obtained at the bottom of the pressure column C1, a lean liquid space 221 is obtained at the lower part, and pressure nitrogen is obtained at the top. The oxygen-enriched liquid air 201 is supercooled into supercooled oxygen-enriched liquid air 202 through the second heat exchanger E2, and the supercooled oxygen-enriched liquid air 202 enters the lower part or the middle part of the atmospheric tower C2 in a throttling way to participate in rectification. Through rectification of the atmospheric tower C2, low-purity liquid oxygen is obtained at the bottom of the atmospheric tower C2, and dirty nitrogen 311 is obtained at the top. The low-purity liquid oxygen enters a condensation evaporator K1 and is divided into two parts: part of the low-purity liquid oxygen is evaporated into low-purity oxygen as a cold source to be used as rising gas of the atmospheric tower C2, the other part of the low-purity liquid oxygen 301 is pumped out from a low-purity liquid oxygen pumping port on the evaporation side of the condensation evaporator K1 to be pressurized by a low-purity liquid oxygen pump OP1, so that low-pressure low-purity liquid oxygen 302 with the pressure of about 3.2bar (G) is obtained, the low-pressure low-purity liquid oxygen 302 enters a first heat exchanger E1 to be reheated and then is used as normal-temperature low-pressure low-purity oxygen 305 with the pressure of about 3bar (G), and the normal-temperature low-pressure low-purity oxygen 305 enters a product low-purity oxygen pipeline to be sent out as product low-pressure pure oxygen GOX. The above is the low pressure low purity oxygen preparation route.
The pressure nitrogen at the top of the pressure tower C1 enters the condensing evaporator K1 as a heat source to be liquefied into pressure liquid nitrogen 211, the pressure liquid nitrogen 211 is divided into three parts, namely pressure liquid nitrogen 212, pressure liquid nitrogen 251 and pressure liquid nitrogen 213, wherein the pressure liquid nitrogen 251 is pressurized by a liquid nitrogen pump NP1 to obtain medium-pressure liquid nitrogen 252 with the pressure of about 8.2bar (G), the medium-pressure liquid nitrogen 252 is sent into the first heat exchanger E1 to be reheated to be normal-temperature medium-pressure nitrogen 253 with the pressure of about 8bar (G), and the normal-temperature medium-pressure nitrogen 253 enters a product nitrogen pipeline to be sent out as product nitrogen GAN. The above is the medium pressure nitrogen production route.
The small air separation device also comprises a second raw material pipeline, a boost aftercooler WE401, a low-purity liquid oxygen evaporator K2 and a third heat exchanger E3; the specific working principle is as follows:
the second raw material pipeline sequentially passes through the compression end of the expander ET401, the after-pressurization cooler WE401, the first heat exchanger E1, the low-purity liquid oxygen evaporator K2 and the third heat exchanger E3 and then is connected with the lower part of the pressure tower C1.
Specifically, the purified air 121 enters a compression end driven by the expander ET401 to be continuously pressurized and cooled by the post-pressurization cooler WE401 to obtain the pressurized air 122, the pressurized air 122 enters the first heat exchanger E1 to be cooled into the low-temperature pressurized air 123, the low-temperature pressurized air 123 enters the low-purity liquid oxygen evaporator K2 as a heat source to be liquefied and then enters the third heat exchanger E3 to be supercooled into the supercooled liquid air 124, and the supercooled liquid air 124 enters the middle part of the pressure tower C1 to participate in rectification after being throttled.
The outlet pipeline of the low-purity liquid oxygen pump OP1 is connected with the low-purity liquid oxygen evaporator K2 after passing through the third heat exchanger E3, and the top of the low-purity liquid oxygen evaporator K2 is connected with the low-purity oxygen pipeline of the product after passing through the first heat exchanger E1 through a pipeline.
Specifically, the low-pressure low-purity liquid oxygen 302 is sent to the third heat exchanger E3 to be reheated with the supercooled liquid air 124 to a certain temperature, then enters the low-purity liquid oxygen evaporator K2 to be evaporated, the oxygen 304 evaporated by the low-purity liquid oxygen evaporator K2 enters the first heat exchanger E1 to be reheated to be the normal-temperature low-pressure low-purity oxygen 305 with the pressure of about 3bar (G), and the normal-temperature low-pressure low-purity oxygen 305 enters the product low-purity oxygen pipeline to be sent out as the product low-purity oxygen GOX. Before the low-pressure low-purity liquid oxygen 302 enters the first heat exchanger E1 for reheating, the low-pressure low-purity liquid oxygen enters the third heat exchanger E3 for recovering the supercooling state cold energy of the low-pressure low-purity liquid oxygen so as to reduce the air quantity of the pressurized air 122 and reduce the energy consumption, and then enters the low-pressure low-purity liquid oxygen evaporator K2 for evaporation phase change, so that the risk of hydrocarbon accumulation possibly occurring when the low-pressure low-purity liquid oxygen directly enters the first heat exchanger E1 for evaporation is prevented.
The evaporation side of the low-purity liquid oxygen evaporator K2 is provided with a low-purity liquid oxygen discharge port for extracting a small amount of low-purity liquid oxygen to be used as oxygen evaporation safety discharge or as low-purity liquid oxygen of a product. Specifically, a small amount of low-purity liquid oxygen 303 is extracted from the low-purity liquid oxygen discharge port for safe discharge as oxygen evaporation or for use as product low-purity liquid oxygen LOX.
The liquid nitrogen extraction port on the condensation side of the condensation evaporator K1 is provided with a third branch, a fourth branch and a fifth branch which are connected in parallel, the third branch is connected with the inlet of the liquid nitrogen pump NP1, the fourth branch is connected with the top of the pressure tower C1, and the fifth branch is connected with the top of the atmospheric tower C2 after passing through the second heat exchanger E2. And a sixth branch is connected after the fifth branch goes out of the second heat exchanger E2 and is used for outputting product liquid nitrogen.
Specifically, the pressure liquid nitrogen 211 is divided into three parts, namely pressure liquid nitrogen 212, pressure liquid nitrogen 251 and pressure liquid nitrogen 213, wherein the pressure liquid nitrogen 251 enters a third branch to be pressurized by a liquid nitrogen pump NP 1; pressure liquid nitrogen 212 enters a fourth branch and flows back to the top of the pressure tower C1; the pressure liquid nitrogen 213 enters a fifth branch and is supercooled into supercooled pressure liquid nitrogen 214 through a second heat exchanger E2, the supercooled pressure liquid nitrogen 214 is divided into two parts, the supercooled pressure liquid nitrogen 215 and the supercooled pressure liquid nitrogen 216 are further used, the supercooled pressure liquid nitrogen 215 enters the top of the atmospheric tower C2 after throttling and participates in rectification, and the supercooled pressure liquid nitrogen 216 is sent out as a product liquid nitrogen LIN.
The lean liquid air extraction port arranged at the lower part of the pressure tower C1 is connected with the upper part of the atmospheric tower C2 after passing through the second heat exchanger E2 through a pipeline.
Specifically, a proper amount of lean liquid air 221 is extracted from a lean liquid air extraction port at the lower part of the pressure tower C1, and is supercooled into a supercooled lean liquid air 222 after being supercooled by the second heat exchanger E2, and the supercooled lean liquid air 222 enters the upper part of the atmospheric tower C2 after being throttled to participate in rectification, namely, the cold energy and the reflux liquid are supplemented for the atmospheric tower C2, so that the rectification effect is ensured.
The dirty nitrogen gas export that atmospheric tower C2 top set up is connected with dirty nitrogen gas emission pipeline behind second heat exchanger E2, first heat exchanger E1 through the pipeline in proper order.
Specifically, the polluted nitrogen 311 at the top of the atmospheric tower C2 is reheated to a certain temperature by the second heat exchanger E2 to form polluted nitrogen 312, and the polluted nitrogen 312 enters the first heat exchanger E1 for reheating and then enters the polluted nitrogen discharge pipeline to be sent out as normal-temperature polluted nitrogen 313.
The advantages of the invention over conventional plants are illustrated below by way of example with a low pure oxygen yield of 2100Nm 3/h, a purity of 96% O 2, a pressure of 3bar (G) and a nitrogen yield of 1850Nm 3/h, a purity of 2ppmO 2 and a pressure of 8bar (G), the comparison results being given in Table 1 below.
TABLE 1 comparison of the invention with conventional protocol
From the tabular comparison above, it can be seen that the present invention has the following advantages:
(1) Compared with the oxygen-nitrogen external compression device in the conventional scheme 1, the invention can simplify 4 compressors configured by the conventional device into 1 compressor, a low-purity liquid oxygen pump and a liquid nitrogen pump (namely, an oxygen compressor, a nitrogen compressor or a booster compressor required by the conventional device is omitted), simplifies equipment configuration, can prepare low-pressure low-purity oxygen and medium-pressure nitrogen by only providing purified air (raw materials) with proper pressure, can obviously reduce equipment investment, factory building cost and later maintenance cost, thereby effectively improving the economic benefit of enterprises and being very suitable for production enterprises with smaller oxygen-nitrogen product demand.
(2) Compared with the low-pressure low-purity oxygen internal compression device in the conventional scheme 2, the refrigerated expansion air firstly enters the pressure tower C1 for rectification, the comprehensive utilization rate of oxygen and nitrogen is high, and the energy consumption can be reduced by about 9.3 percent, namely the comprehensive energy consumption of the device is reduced.
The above embodiments are only preferred embodiments of the present invention, and are not limiting to the technical solutions of the present invention, and any technical solution that can be implemented on the basis of the above embodiments without inventive effort should be considered as falling within the scope of protection of the patent claims of the present invention.

Claims (8)

1. A small air separation plant for producing low pressure low purity oxygen and medium pressure nitrogen, comprising:
The device comprises a first raw material pipeline, a first heat exchanger, a second heat exchanger, an expander, a rectifying tower, a product low-purity oxygen pipeline and a product nitrogen pipeline;
the rectifying tower is sequentially provided with a pressure tower, a condensing evaporator and an atmospheric tower from bottom to top;
The first raw material pipeline enters the first heat exchanger and is divided into a first branch and a second branch, the first branch returns to the first heat exchanger through the expansion end of the expander and is connected with the bottom of the pressure tower, and the second branch exits the first heat exchanger and is connected with the lower part of the pressure tower;
An oxygen-enriched liquid air outlet arranged at the bottom of the pressure tower is connected with an oxygen-enriched liquid air inlet arranged at the lower part or the middle part of the normal pressure tower after passing through the second heat exchanger through a pipeline;
The low-purity liquid oxygen extraction port arranged on the evaporation side of the condensation evaporator is connected with a low-purity liquid oxygen pump through a pipeline, and the outlet of the low-purity liquid oxygen pump is connected with the low-purity oxygen pipeline of the product after passing through the first heat exchanger through a pipeline;
a liquid nitrogen extraction port arranged on the condensation side of the condensation evaporator is connected with a liquid nitrogen pump through a pipeline, and an outlet of the liquid nitrogen pump is connected with a product nitrogen pipeline after passing through the first heat exchanger through a pipeline;
the device also comprises a second raw material pipeline, a post-pressurizing cooler, a low-purity liquid oxygen evaporator and a third heat exchanger, wherein the second raw material pipeline sequentially passes through the compression end of the expander, the post-pressurizing cooler, the first heat exchanger, the low-purity liquid oxygen evaporator and the third heat exchanger and then is connected with the lower part of the pressure tower;
The liquid nitrogen extraction port of condensation side of condensation evaporator is equipped with parallelly connected third branch road, fourth branch road and fifth branch road, the third branch road with liquid nitrogen pump inlet connection, the fourth branch road with the top of pressure tower is connected, the fifth branch road is passed through the second heat exchanger back with the top of atmospheric tower is connected.
2. The small-sized air separation unit for preparing low-pressure low-purity oxygen and medium-pressure nitrogen according to claim 1, wherein:
The outlet pipeline of the low-purity liquid oxygen pump is connected with the low-purity liquid oxygen evaporator after passing through the third heat exchanger;
the top of the low-purity liquid oxygen evaporator is connected with the low-purity oxygen pipeline of the product after passing through the first heat exchanger through a pipeline.
3. The small-sized air separation unit for preparing low-pressure low-purity oxygen and medium-pressure nitrogen according to claim 1 or 2, wherein the evaporation side of the low-purity liquid oxygen evaporator is provided with a low-purity liquid oxygen discharge port for extracting a small amount of low-purity liquid oxygen to be safely discharged as oxygen evaporation or used as low-purity liquid oxygen of a product.
4. The small air separation unit for preparing low-pressure low-purity oxygen and medium-pressure nitrogen according to claim 1, wherein the fifth branch is connected with a sixth branch after exiting the second heat exchanger and is used for outputting product liquid nitrogen.
5. The small-sized air separation unit for preparing low-pressure low-purity oxygen and medium-pressure nitrogen according to claim 1, wherein a lean liquid air extraction port arranged at the lower part of the pressure tower is connected with the upper part of the atmospheric tower after passing through the second heat exchanger through a pipeline.
6. The small air separation device for preparing low-pressure low-purity oxygen and medium-pressure nitrogen according to claim 1, wherein a dirty nitrogen outlet arranged at the top of the atmospheric tower is connected with a dirty nitrogen discharge pipeline after sequentially passing through the second heat exchanger and the first heat exchanger through pipelines.
7. A small air separation plant for the production of low pressure, low purity oxygen and medium pressure nitrogen according to any one of claims 1, 5, 6 wherein the medium entering said first feed line is purified air at a pressure of 8bar (G).
8. The small-sized air separation unit for preparing low-pressure low-purity oxygen and medium-pressure nitrogen according to claim 7, wherein the medium entering the product low-purity oxygen pipeline is normal-temperature low-purity oxygen with pressure of 3bar (G), and the medium entering the product nitrogen pipeline is normal-temperature medium-pressure nitrogen with pressure of 5-8 bar (G).
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CN203687518U (en) * 2014-01-24 2014-07-02 四川空分设备(集团)有限责任公司 Low-purity oxygen preparing device with auxiliary rectifying tower
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CN107940896B (en) * 2017-11-02 2019-06-18 河南大学 A kind of device and method using heat pump techniques production oxygen rich air and high pressure, high purity nitrogen

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