CN111271940A - Novel oxygen-enriched production method - Google Patents

Novel oxygen-enriched production method Download PDF

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Publication number
CN111271940A
CN111271940A CN202010057663.2A CN202010057663A CN111271940A CN 111271940 A CN111271940 A CN 111271940A CN 202010057663 A CN202010057663 A CN 202010057663A CN 111271940 A CN111271940 A CN 111271940A
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oxygen
pressure
liquid
sent
gas
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张育哲
刘金伟
梁泰航
王军辉
方亮
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Zhejiang Zhihai Chemical Equipment Engineering Co ltd
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Zhejiang Zhihai Chemical Equipment Engineering 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
    • F25J3/04248—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
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    • 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
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    • 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
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    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
    • C01B13/02—Preparation of oxygen
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    • C01B13/0248—Physical processing only
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    • F25J3/04309—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 nitrogen
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    • 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
    • F25J3/04418—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 with thermally overlapping high and low pressure columns
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    • 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
    • F25J3/0446—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 the heat generated by mixing two different phases
    • F25J3/04466—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 the heat generated by mixing two different phases for producing oxygen as a mixing column overhead gas by mixing gaseous air feed and liquid oxygen
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00—Purification or separation of specific gases
    • C01B2210/0001—Separation or purification processing
    • C01B2210/0009—Physical processing
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00—Purification or separation of specific gases
    • C01B2210/0043—Impurity removed
    • C01B2210/0051—Carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00—Purification or separation of specific gases
    • C01B2210/0043—Impurity removed
    • C01B2210/0062—Water
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
    • F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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    • 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
    • F25J2200/34—Processes or apparatus using separation by rectification using a side column fed by a stream from the low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
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    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
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    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • F25J2205/32—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes as direct contact cooling tower to produce a cooled gas stream, e.g. direct contact after cooler [DCAC]
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    • 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
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    • F25J2205/34—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes as evaporative cooling tower to produce chilled water, e.g. evaporative water chiller [EWC]
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    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
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Abstract

A novel oxygen-enriched production method comprises the following steps: the method is characterized by comprising the following steps: the raw material air is filtered by a self-cleaning air filter, the filtered gas is sent to a raw material supercharger to be pressurized to 5barG, H20, CO2 and macromolecular impurities are removed after the gas is subjected to a precooling system and a molecular sieve, so that the contents of H2O and CO2 are reduced to be below 0.1ppm, the method adopts cryogenic low-temperature rectification, 80-95% of O2 products can be prepared, and the pressure can be adjusted in a wide range according to the requirements of users. Compared with the conventional oxygen-enriched production process, the process is simple, the working state is more stable, the adjusting range is large, the energy consumption is lower, and the product structure has a wide application range.

Description

Novel oxygen-enriched production method
Technical Field
The invention relates to a novel oxygen-enriched production method, and belongs to the technical field of oxygen-enriched production.
Background
Oxygen enrichment is widely used in the process, for example, in the steel industry, oxygen enrichment is used for blast furnace oxygen enrichment blast so as to improve smelting strength and yield; in other metallurgy industries such as copper smelting, oxygen with the purity of more than 80% -95% is also used. The energy consumption is higher by adopting the conventional air separation technology of a cryogenic method. The oxygen production by the VPSA technology cannot prepare high-purity oxygen enrichment, the product structure is limited, and the energy consumption is increased quickly after long-time operation.
Disclosure of Invention
The invention relates to a novel oxygen enrichment production method with low energy consumption, which adopts low-temperature high-purity liquid oxygen and low-temperature air to be mixed to obtain oxygen enrichment with required pressure and purity. The purpose of the invention is achieved by the following technical scheme: a novel oxygen-enriched production method comprises the following steps: the method comprises the following steps:
(1) the raw material air enters a self-cleaning air filter AF for filtration, the filtered gas is sent to a raw material supercharger MAC to be pressurized to 5barG, and H20, CO2 and macromolecular impurities are removed after the gas passes through a precooling system (AC) and molecular sieves (R01 and R02), so that the contents of H2O and CO2 are reduced to be below 0.1 ppm.
(2) And (2) dividing the gas subjected to impurity removal in the step (1) and the raw material gas into two parts, compressing one part of the gas by a pressurizing end of an expander, exchanging heat by a heat exchanger E01, entering the expander ET01, expanding to the pressure of the mixing tower, and then feeding the gas into the mixing tower K04 from the bottom. The other air directly enters a heat exchanger E01, after passing through a separation tank V01 in a heat exchanger E01, separated liquid is sent to a high-pressure rectifying tower K01, separated gas is divided into two parts, one part is directly sent to the high-pressure rectifying tower K01, the other part is used as a heat source of the rectifying tower in a liquid oxygen tower evaporator E101 to evaporate liquid oxygen, and then liquid air is obtained and sent to the high-pressure rectifying tower K01.
Preferably, the method comprises the following steps: in the step (2), the required oxygen-enriched gas obtained from the top of the mixing tower K04 is sent out as a product after heat exchange by a heat exchanger E01, the purity of the oxygen-enriched gas is controlled by the purity of high-purity liquid oxygen obtained from the bottom of the low-pressure distillation tower K02 and the amount of expanded air, the oxygen-enriched gas with the required purity can be obtained according to the requirement, the residual liquid in the mixing tower K04 is sent back to the low-pressure distillation tower K02 for re-rectification, the pressure of the mixing tower K04 is controlled by a liquid oxygen pump P03, and the oxygen-enriched gas with different pressure grades can be obtained.
Preferably, the method comprises the following steps: in the step (1), after the nitrogen obtained from the top of the high-pressure rectifying tower K01 is subjected to heat exchange by a heat exchanger E01, part of the nitrogen enters an expander ET03 to recover part of cold energy, the outlet pressure is normal pressure, part of the nitrogen can be output as a product, the nitrogen can enter the flow of the expander according to different working conditions, the oxygen-enriched liquid air at the bottom of the high-pressure rectifying tower K01 is sent to a low-pressure distilling tower K02 by a heat exchanger E03, part of the liquid nitrogen obtained from the high-pressure rectifying tower K01 is sent out as a liquid nitrogen product after the heat exchange by a heat exchanger E03, the liquid nitrogen is sent to a low-pressure distilling tower K02, and the low-pressure nitrogen obtained from the top of the low-pressure distilling tower K02 is sent out as.
Preferably, the method comprises the following steps: and a part of liquid oxygen obtained at the bottom of the low-pressure distillation tower K02 is pressurized by a pump and then sent into a mixing tower K04 to participate in rectification, a part of liquid oxygen is sent into a liquid oxygen tower T101 to be rectified to obtain high-purity liquid oxygen, and oxygen-enriched gas at the top of the liquid oxygen tower T101 is sent into a low-pressure distillation tower K02 to be recovered.
Compared with the conventional air separation device for producing high purity oxygen, the process of the invention can obviously reduce energy consumption after being optimized, and can generate oxygen with different purities, so that the types of the oxygen are more.
Drawings
FIG. 1 is a flow chart of the present invention.
Detailed Description
The invention will now be described in detail with reference to the accompanying drawings, in which: as shown in figure 1, raw air firstly enters a self-cleaning air filter AF for filtration, then is sent to a raw material supercharger MAC for pressurization to 5barG, and after passing through a precooling system (AC) and molecular sieves (R01 and R02), H20, CO2 and macromolecular impurities are removed, so that the contents of H2O and CO2 are reduced to be below 0.1 ppm. After impurity removal, the mixture is divided into two parts with feed gas, one part is compressed by a pressurizing end of an expander, enters the expander ET01 after heat exchange of a heat exchanger E01, is expanded to the pressure of a mixing tower and then is sent into the mixing tower K04 from the bottom. The other air directly enters a heat exchanger E01, liquid is sent to a rectifying tower K01 after passing through a separating tank V01, gas is divided into two parts, one part is directly sent to the rectifying tower K01, and the other part is subjected to heat exchange with liquid oxygen in E101 to obtain liquid air, and then the liquid air is sent to K01.
The required rich oxygen obtained from the top of K04 is sent out as a product after heat exchange by a heat exchanger E01. The purity of the oxygen-enriched gas is controlled by the purity of high-purity liquid oxygen obtained from the bottom of the rectifying tower K02 and the amount of expanded air, so that oxygen-enriched gas with the required purity can be obtained according to the requirement, and the residual liquid in the K04 is sent back to K02 for re-rectification. The pressure of K04 is controlled by P03, and oxygen-enriched gas with different pressure levels can be obtained.
The nitrogen obtained from the top of K01 is partially fed into an expansion machine ET03 after heat exchange by a heat exchanger E01 to recover part of cold, the outlet pressure is normal pressure, part of the nitrogen can be output as a product, and the flow of the nitrogen fed into the expansion machine can be adjusted according to different working conditions. The oxygen-enriched liquid at the bottom of K01 is fed to K02 through heat exchanger E03. After the heat exchange of the liquid nitrogen obtained by K01 by a heat exchanger E03, part of the liquid nitrogen is sent out as a liquid nitrogen product, and the rest of the liquid nitrogen is sent to K02. And low-pressure nitrogen obtained from the top of K02 is sent out as normal-pressure nitrogen after heat exchange of heat exchangers E03 and E01.
The liquid oxygen obtained from the bottom of K02 is pressurized by a pump and then sent to K04 to participate in rectification, part of the liquid oxygen is sent to T101 to be rectified to obtain high-purity liquid oxygen, and the oxygen-enriched gas at the top of T101 is sent to K02 to be recovered.
The invention has the following positive effects:
compared with the conventional air separation device for producing high purity oxygen, the process of the invention is optimized, and the energy consumption can be obviously reduced.
And (II) normal-pressure pure nitrogen and high-pressure nitrogen can be produced simultaneously for factories to use.
And thirdly, high-purity liquid oxygen products can be produced by changing the working conditions and can be used for backup storage.
And fourthly, producing oxygen with different purities by changing the working condition.
And (V) producing oxygen at different pressures by changing working conditions.
The process adopts cryogenic low-temperature rectification to prepare 80-95% of O2 product, and the pressure can be adjusted in a wide range according to the requirements of users. Compared with the conventional oxygen-enriched production process, the process is simple, the working state is more stable, the adjusting range is large, the energy consumption is lower, and the product structure has a wide application range. Is suitable for the gas use requirements of different pressure grades for 80-95% purity oxygen in industrial production.

Claims (4)

1. A novel oxygen-enriched production method comprises the following steps: the method is characterized by comprising the following steps:
(1) feeding raw material air into a self-cleaning Air Filter (AF) for filtration, feeding the filtered gas into a raw material supercharger (MAC) for pressurization to 5barG, removing H20, CO2 and macromolecular impurities after passing through a precooling system (AC) and molecular sieves (R01 and R02) so as to reduce the content of H2O and CO2 to be below 0.1ppm, (2) dividing the gas subjected to impurity removal in the step (1) and the raw material gas into two streams, compressing one stream by a pressurization end of an expander, feeding the compressed gas into an expander (ET 01) after heat exchange by a heat exchanger (E01), feeding the expanded gas into a mixing tower (K04) from the bottom after expanding to the pressure of the mixing tower, directly feeding the other stream of air into a heat exchanger (E01), feeding the separated liquid into a high-pressure rectifying tower (K01) after passing through a separation tank (V01) in the heat exchanger (E01), dividing the separated gas into two streams, directly feeding the one stream into a high-pressure rectifying tower (K01), and taking the other stream as a liquid oxygen evaporator (E101) of a liquid oxygen evaporator for, then liquid air is obtained and sent into a high-pressure rectifying tower (K01).
2. A novel oxygen-enriched production method as claimed in claim 1, characterized in that the required oxygen-enriched gas obtained from the top of the mixing column (K04) in step (2) is sent out as a product after heat exchange by a heat exchanger (E01), the purity of the oxygen-enriched gas is controlled by the purity of high-purity liquid oxygen obtained from the bottom of the low-pressure distillation column (K02) and the amount of expanded air, oxygen-enriched gas with the required purity can be obtained according to the requirement, the liquid remaining in the mixing column (K04) is sent back to the low-pressure distillation column (K02) for re-rectification, the pressure of the mixing column (K04) is controlled by a liquid oxygen pump (P03), and oxygen-enriched gas with different pressure grades can be obtained.
3. A novel oxygen-enriched production method as claimed in claim 1, characterized in that nitrogen obtained from the top of the high-pressure rectification column (K01) in step (1) enters an expander (ET 03) after heat exchange by a heat exchanger (E01) to recover part of cold, the outlet pressure is normal pressure, part of nitrogen can be output as product, the nitrogen can enter the expander according to different working conditions, the oxygen-enriched liquid air at the bottom of the high-pressure rectification column (K01) is sent to the low-pressure distillation column (K02) through the heat exchanger (E03), the liquid nitrogen obtained from the high-pressure rectification column (K01) is sent as liquid nitrogen product after heat exchange by the heat exchanger (E03), part of liquid nitrogen is sent to the low-pressure distillation column (K02), and the low-pressure nitrogen obtained from the top of the low-pressure distillation column (K02) is sent as normal-pressure nitrogen after heat exchange by the heat exchanger (E03) heat exchanger (E01).
4. A novel oxygen-enriched production method as claimed in claim 1, 2 or 3, characterized in that the liquid oxygen obtained from the bottom of the low-pressure distillation column (K02) is partially pumped into a mixing column (K04) to participate in rectification, and the liquid oxygen is partially sent into a liquid oxygen column (T101) to be rectified to obtain high-purity liquid oxygen, and the oxygen-enriched gas at the top of the liquid oxygen column (T101) is sent into the low-pressure distillation column (K02) to be recovered.
CN202010057663.2A 2020-01-19 2020-01-19 Novel oxygen-enriched production method Pending CN111271940A (en)

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Application publication date: 20200612