CN109297043B - Low-energy-consumption stable gas supply method and system - Google Patents

Low-energy-consumption stable gas supply method and system Download PDF

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Publication number
CN109297043B
CN109297043B CN201811330454.XA CN201811330454A CN109297043B CN 109297043 B CN109297043 B CN 109297043B CN 201811330454 A CN201811330454 A CN 201811330454A CN 109297043 B CN109297043 B CN 109297043B
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tower
air
fluid
heat exchanger
rectifying tower
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CN109297043A (en
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杜鹏举
杨涛
杜大艳
袁有录
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Hubei Heyuan Gases Co ltd
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Hubei Heyuan 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
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L7/00—Supplying non-combustible liquids or gases, other than air, to the fire, e.g. oxygen, steam
    • F23L7/007—Supplying oxygen or oxygen-enriched 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
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04024—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of purified feed air, so-called boosted 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
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • 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
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • 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
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F25J3/0426—The cryogenic component does not participate in the fractionation
    • 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
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/50—Oxygen
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery

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

Abstract

The invention relates to a method and a system for stably supplying air with low energy consumption, wherein at least one part of each of first heat-exchange air flow, second heat-exchange air flow and third heat-exchange air flow is obtained by processing first air flow to be supplied and second air flow to be supplied; the system comprises a piston type air booster, a high-efficiency after cooler, a booster turboexpander, a main heat exchanger with five separated fluid loops, an upper tower of a rectifying tower, a lower tower of the rectifying tower, a subcooler with four separated fluid pipes, a low-temperature liquid nitrogen storage tank and a low-temperature liquid nitrogen storage tank; the invention liquefies the originally wasted nitrogen generated by air separation, and the liquefaction cost of the nitrogen is reduced because the cold energy of the liquid oxygen is fully utilized, the increased cost of the liquid oxygen is basically offset by the benefit generated by the liquid nitrogen, and the comprehensive energy consumption is reduced.

Description

Low-energy-consumption stable gas supply method and system
Technical Field
The invention relates to the technical field of air separation, in particular to a low-energy-consumption stable air supply method and system.
Background
The oxygen is widely applied in industry, the fluctuation of the oxygen consumption is large in many industries (such as electric arc furnace steelmaking), the production capacity is large at night and small in daytime in some industries because of depending on electric power, and the oxygen consumption is large at night and small in daytime.
Generally, these industries have a large average amount of oxygen, so many use cryogenic air separation units (hereinafter referred to as air separation units) to supply oxygen.
Based on such air fluctuation problem, the current solution mainly has following several, one is to adjust a whole set of air separation plant for the device adapts to new operating mode, however, air separation plant designs a whole set of equipment, including compressor, clarifier, expander, rectifying column, in case the air use operating mode changes and just needs to adjust a whole set of technology, this is unusual numerous and diverse, especially rectifying column, rectifying column is difficult to adjust, and air separation plant its energy consumption is minimum at specific design operating mode, and the energy consumption also can increase after the operating mode changes. Alternatively, the oxygen production is designed to be average oxygen usage, excess usage is liquefied to liquid oxygen when the oxygen usage is below the average usage, and the liquefied liquid oxygen is used to supplement the portion above the average usage when the oxygen usage is above the average usage; the disadvantage of this solution is the high energy consumption of the plant, since the production costs of liquid oxygen, regardless of the way it is produced, are necessarily higher than those of gaseous oxygen; the second defect is that the air separation device which generates liquid oxygen and does not generate liquid oxygen is in two working states, the cold quantity requirements are different, the system cold quantity requirement is larger when the liquid oxygen is generated, therefore, the air separation device also needs to be adjusted, although the adjustment mode is simpler than the former scheme, the operation is complex, and the air separation device deviates from a stable design value, so that the energy consumption is high.
The other scheme is that the lowest gas consumption is positioned for the air separation design gas production rate, and then outsourcing liquid oxygen is used for supplementing the oxygen consumption rate which is larger than the design amount.
In addition, the air separation plant generally produces nitrogen while producing oxygen, however, such oxygen customers often use little or no nitrogen, which causes most of the nitrogen produced by the air separation plant to be emptied whitely except for a small portion of the nitrogen used for purifier regeneration or for their own instrument gas; there is certainly a proposal to liquefy this part of the nitrogen (called external liquefaction) and then export it, but the external liquefaction investment is high and the liquefaction cost of the nitrogen is high, so that it is not market competitive.
Another conventional idea is to liquefy the nitrogen gas by venting it through a heat exchanger, which reduces the cost of liquefying the nitrogen gas, but the temperature of the liquid oxygen is only about 180 ℃, while the nitrogen gas liquefaction requires a low temperature of about-196 ℃, unless the nitrogen gas is raised to a higher pressure, but such liquid nitrogen is easily gasified in a cryogenic storage tank due to the low self-contained cold, is not easily accepted by general customers, and is not well-suited for market use, so that it is difficult to liquefy the nitrogen gas simply through a heat exchanger.
Based on this, aiming at the defects in the prior art, a method and a system for stably supplying gas with low energy consumption are needed to be designed, and stable and low-energy-consumption gas supply for users with large fluctuation of gas consumption by using an air separation device can be realized.
Disclosure of Invention
The invention aims to overcome the defects of the prior art, and provides a method and a system for stably supplying gas with low energy consumption, which are designed to realize stable and low-energy-consumption gas supply for users with large fluctuation of gas consumption by using an air separation device.
The invention is realized by the following technical scheme:
a method of low energy consumption stable air supply, through compressing, cooling and purification dewatering and carbon dioxide processing to the air, obtain the air that waits to supply the air, divide into two parts with the air that waits to supply the air, obtain first air current that waits to supply and second air current that waits to supply includes:
providing a primary heat exchanger having at least five separate fluid circuits such that a first air stream to be supplied is provided to a first fluid circuit of the primary heat exchanger, a second air stream to be supplied is provided to a second fluid circuit of the primary heat exchanger, a first heat exchange air stream is provided to a third fluid circuit of the primary heat exchanger, a second heat exchange air stream is provided to a fourth fluid circuit of the primary heat exchanger, and a third heat exchange air stream is provided to a fifth fluid circuit of the primary heat exchanger, whereby the first air stream to be supplied, the second air stream to be supplied are cooled by indirect heat exchange with the first, second, third heat exchange air streams;
discharging the cooled first air flow to be supplied and the cooled second air flow to be supplied from the main heat exchanger;
discharging the heated first, second, and third heat exchange gas streams from the main heat exchanger;
wherein at least a portion of each of the first, second, and third heat exchange air streams is obtained by processing the first and second air streams to be supplied.
Furthermore, the first air flow to be supplied is subjected to pressurization through a pressurization end of the pressurization turboexpander before entering the main heat exchanger, and enters the main heat exchanger after being cooled.
Further, the second air flow to be supplied is subjected to the processing steps of pressurization and cooling before entering the main heat exchanger, and the second air flow to be supplied is partially liquefied and cooled when being discharged from the main heat exchanger.
Further, at least a part of each of the first heat-exchange air flow, the second heat-exchange air flow and the third heat-exchange air flow is obtained by processing the first air flow to be supplied and the second air flow to be supplied through a rectifying tower, and the rectifying tower is divided into an upper rectifying tower and a lower rectifying tower.
Furthermore, the first to-be-supplied gas flow discharged from the main heat exchanger enters the expansion end of the booster turboexpander, and is sent to the upper tower of the rectifying tower to participate in rectification after being expanded, cooled and depressurized.
Furthermore, the second gas flow to be supplied discharged from the main heat exchanger enters a lower tower of the rectifying tower, part of oxygen-enriched liquid air is extracted from the bottom of the lower tower of the rectifying tower, and the oxygen-enriched liquid air enters the subcooler to be subcooled and then is sent to an upper tower of the rectifying tower to participate in rectification.
Further, high-purity nitrogen gas extracted from the top of the lower tower of the rectifying tower is sent to a condensation evaporator of the upper tower of the rectifying tower for liquefaction, one part of liquefied liquid nitrogen is used as reflux liquid of the lower tower of the rectifying tower, the other part of liquefied liquid nitrogen enters a subcooler for supercooling and then enters the upper tower of the rectifying tower to be used as reflux liquid of the upper tower of the rectifying tower, and the rest part of liquefied liquid nitrogen is extracted to a low-temperature liquid nitrogen storage tank to be used as product liquid nitrogen.
Furthermore, qualified liquid oxygen is produced at the bottom of the upper tower of the rectifying tower after rectification and is converged with liquid oxygen supplemented from a low-temperature liquid oxygen storage tank, and then the liquid oxygen is pressurized by a low-temperature liquid oxygen pump and enters a main heat exchanger, and the liquid oxygen is gasified into gas oxygen with certain pressure and capable of being used by utilizing cold energy in the main heat exchanger; meanwhile, high-purity nitrogen generated at the top of the upper tower of the rectifying tower and part of impure nitrogen required to be pumped out at the upper part of the upper tower of the rectifying tower are used as regeneration gas of the air separation purifier, and redundant nitrogen is discharged.
Furthermore, liquid oxygen supplemented from the low-temperature liquid oxygen storage tank is gasified at the bottom of the upper tower of the rectifying tower, and then is merged with liquid oxygen produced at the bottom of the upper tower of the rectifying tower after rectification.
Another object of the present invention is a low energy consumption stable gas supply system comprising a main heat exchanger with five divided fluid circuits, a rectifying tower upper column, a rectifying tower lower column, a subcooler with four divided fluid tubes, a cryogenic liquid oxygen storage tank and a cryogenic liquid nitrogen storage tank; the fluid loops of the main heat exchanger are respectively a first fluid loop, a second fluid loop, a third fluid loop, a fourth fluid loop and a fifth fluid loop in sequence; the fluid pipes of the subcooler are a first fluid pipe, a second fluid pipe, a third fluid pipe and a fourth fluid pipe in sequence; the air supply pipeline inlet is divided into a first air supply pipeline inlet and a second air supply pipeline inlet; wherein the content of the first and second substances,
the inlet of the first gas supply pipeline is connected to the input end of a first fluid loop, the output end of the first fluid loop is connected to the upper part of an upper tower of the rectifying tower, the inlet of the second gas supply pipeline is connected to the input end of a second fluid loop, the output end of the second fluid loop is connected to the lower part of a lower tower of the rectifying tower, the lower part of the lower tower of the rectifying tower is connected to the input end of a fourth fluid pipe of the subcooler, the output end of the fourth fluid pipe is connected to the upper tower of the rectifying tower, the upper part of the upper tower of the rectifying tower is respectively connected to the second fluid pipe and the third fluid pipe, the second fluid pipe is connected to the input end of a third fluid loop, the output end of the third fluid loop is connected to a high-purity nitrogen conveying pipeline, the third fluid pipe is connected to the input end of the fourth fluid loop, and the, the lower part of rectifying column upper tower is connected to the input of fifth fluid circuit, low temperature liquid oxygen storage tank and rectifying column upper tower are parallelly connected or are established ties in proper order to the input of fifth fluid circuit along liquid oxygen direction of delivery, the output of fifth fluid circuit is connected to and is waited to use the oxygen pipeline, the bottom of rectifying column upper tower and the top of rectifying column lower tower are connected and are set up liquid nitrogen circulating line, liquid nitrogen circulating line includes first liquid nitrogen circulating line and second liquid nitrogen circulating line, second liquid nitrogen circulating line still is connected to the input of first fluid pipe in the subcooler, the output of first fluid pipe is connected to the top and the low temperature liquid nitrogen storage tank of rectifying column upper tower respectively.
Furthermore, the system also comprises a booster turboexpander, wherein a boosting end inlet of the booster turboexpander is connected with an inlet of a first gas supply pipeline, a boosting end outlet of the booster turboexpander is connected with an input end of a first fluid loop, an output end of the first fluid loop is connected with an expansion end of the booster turboexpander, and the expansion end of the booster turboexpander is connected with the upper part of an upper tower of the rectifying tower.
Further, the system still includes piston air booster compressor and high-efficient aftercooler, the second gas supply line entry is connected to the input of piston air booster compressor, the input of high-efficient aftercooler is connected to the output of piston air booster compressor, the input of second fluid circuit is connected to the output of high-efficient aftercooler.
Compared with the prior art, the invention has the beneficial effects that:
1. the originally wasted nitrogen generated by air separation is liquefied, the liquefaction cost of the nitrogen is reduced due to the full utilization of the cold energy of the liquid oxygen, the increased cost of the liquid oxygen is basically offset by the benefit generated by the liquid nitrogen, and the comprehensive energy consumption is reduced as a whole;
2. the air separation device designed by the invention has the advantages that the working condition is always stable in the designed working condition, the air separation energy consumption is lowest, the operation is most stable and the operation is simple only by micro-adjustment.
Drawings
FIG. 1 is a schematic diagram of a low temperature liquid oxygen storage tank 3 and a rectification column upper column 5 connected in parallel to the input of a fifth fluid loop 1-5 in the liquid oxygen transfer direction in one embodiment of the present invention;
fig. 2 is a schematic diagram of a low temperature liquid oxygen storage tank 3 and an upper rectifying column 5 connected in series to the input end of a fifth fluid loop 1-5 in the liquid oxygen transfer direction in sequence in one embodiment of the present invention.
The reference numbers are as follows:
1. the system comprises a main heat exchanger, 1-1, a first fluid circuit, 1-2, a second fluid circuit, 1-3, a third fluid circuit, 1-4, a fourth fluid circuit, 1-5, a fifth fluid circuit, 2, a piston type air supercharger, 3, a low-temperature liquid oxygen storage tank, 4, a low-temperature liquid nitrogen storage tank, 5, an upper rectifying tower, 6, a lower rectifying tower, 7, a subcooler, 7-1, a first fluid pipe, 7-2, a second fluid pipe, 7-3, a third fluid pipe, 7-4, a fourth fluid pipe, 8, a pressurization turboexpander, 9, an air supply pipeline inlet, 9-1, a first air supply pipeline inlet, 9-2, an air supply pipeline inlet, 10, a high-purity nitrogen conveying pipeline, 11, a waste nitrogen removal purification system, 12 and an oxygen pipeline to be used.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is described in further detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
As shown in fig. 1, a method for stably supplying air with low energy consumption, which obtains air to be supplied by compressing, cooling, purifying to remove water and carbon dioxide, divides the air to be supplied into two parts, and obtains a first air flow to be supplied and a second air flow to be supplied, includes:
providing a main heat exchanger 1 having at least five separate fluid circuits such that a first air to be supplied is provided to a first fluid circuit 1-1 of the main heat exchanger 1, a second air to be supplied is provided to a second fluid circuit 1-2 of the main heat exchanger 1, a first heat exchange air flow is provided to a third fluid circuit 1-3 of the main heat exchanger 1, a second heat exchange air flow is provided to a fourth fluid circuit 1-4 of the main heat exchanger 1, a third heat exchange air flow is provided to a fifth fluid circuit 1-5 of the main heat exchanger 1, whereby the first air to be supplied, the second air to be supplied are cooled by indirect heat exchange with the first, the second, the third heat exchange air flow;
discharging the cooled first air flow to be supplied and the cooled second air flow to be supplied from the main heat exchanger 1;
discharging the heated first, second and third heat exchange gas streams from the main heat exchanger 1;
wherein at least a portion of each of the first, second, and third heat exchange air streams is obtained by processing the first and second air streams to be supplied.
In specific implementation, the first air flow to be supplied is subjected to pressurization at the pressurization end of the pressurization turboexpander 8 before entering the main heat exchanger 1, and enters the main heat exchanger 1 after being cooled.
In specific implementation, the second air flow to be supplied is sequentially subjected to pressurization and cooling before entering the main heat exchanger 1, and the second air flow to be supplied is partially liquefied and cooled when being discharged from the main heat exchanger 1.
In specific implementation, at least a part of each of the first heat-exchange air flow, the second heat-exchange air flow and the third heat-exchange air flow is obtained by processing the first air flow to be supplied and the second air flow to be supplied through a rectifying tower, and the rectifying tower is divided into an upper rectifying tower 5 and a lower rectifying tower 6.
During specific implementation, a first to-be-supplied gas flow discharged from the main heat exchanger 1 enters an expansion end of a booster turboexpander 8, and is sent to an upper tower 5 of a rectifying tower to participate in rectification after being expanded, cooled and depressurized.
During specific implementation, a second gas flow to be supplied, which is discharged from the main heat exchanger 1, enters the lower rectifying tower 6, part of oxygen-enriched liquid air is extracted from the bottom of the lower rectifying tower 6, enters the subcooler 7, is subcooled, and then is sent to the upper rectifying tower 5 to participate in rectification.
During specific implementation, high-purity nitrogen extracted from the top of a lower tower 6 of a rectifying tower is sent to a condensing evaporator of an upper tower 5 of the rectifying tower for liquefaction, one part of liquefied liquid nitrogen is used as reflux liquid of the lower tower 6 of the rectifying tower, the other part of liquefied liquid nitrogen enters a subcooler 7 for subcooling and then enters the upper tower 5 of the rectifying tower to be used as reflux liquid of the upper tower 5 of the rectifying tower, and the rest part of liquefied liquid nitrogen is extracted to a low-temperature liquid nitrogen storage tank 4 to be used as product liquid nitrogen.
During specific implementation, qualified liquid oxygen is produced at the bottom of the upper tower 5 of the rectifying tower after rectification, is converged with liquid oxygen supplemented from the low-temperature liquid oxygen storage tank 3, is pressurized by a low-temperature liquid oxygen pump and enters the main heat exchanger 1, and is gasified into gas oxygen with certain pressure and capable of being used by using cold energy in the main heat exchanger 1; meanwhile, high-purity nitrogen generated at the top of the upper tower 5 of the rectifying tower and part of impure nitrogen required to be pumped out from the upper part of the upper tower 5 of the rectifying tower are used as regeneration gas of an air separation purifier, and redundant nitrogen is discharged.
In specific implementation, as shown in fig. 2, liquid oxygen supplemented from the low-temperature liquid oxygen storage tank 3 firstly passes through the bottom of the upper tower 5 of the rectifying tower for gasification treatment, and then joins with liquid oxygen produced at the bottom of the upper tower 5 of the rectifying tower after rectification, and the gasified oxygen becomes ascending steam, so that the problem that liquid oxygen circulation is not smooth due to the fact that the pipeline is blocked by the gasification bubbles of the liquid oxygen in the original process can be prevented.
The invention also provides a low-energy-consumption stable gas supply system, which comprises a main heat exchanger 1 with five separated fluid loops, an upper rectifying tower 5, a lower rectifying tower 6, a subcooler 7 with four separated fluid pipes, a low-temperature liquid oxygen storage tank 3 and a low-temperature liquid nitrogen storage tank 4; the fluid loops of the main heat exchanger 1 are respectively a first fluid loop 1-1, a second fluid loop 1-2, a third fluid loop 1-3, a fourth fluid loop 1-4 and a fifth fluid loop 1-5 in sequence; the fluid pipes of the subcooler 7 are a first fluid pipe 7-1, a second fluid pipe 7-2, a third fluid pipe 7-3 and a fourth fluid pipe 7-4 in sequence; the gas supply pipeline inlet 9 is divided into a first gas supply pipeline inlet 9-1 and a second gas supply pipeline inlet 9-2; wherein the content of the first and second substances,
the first gas supply pipeline inlet 9-1 is connected to the input end of a first fluid loop 1-1, the output end of the first fluid loop 1-1 is connected to the upper part of an upper tower 5 of the rectifying tower, the second gas supply pipeline inlet 9-2 is connected to the input end of a second fluid loop 1-2, the output end of the second fluid loop 1-2 is connected to the lower part of a lower tower 6 of the rectifying tower, the lower part of the lower tower 6 of the rectifying tower is connected to the input end of a fourth fluid pipe 7-4 of a subcooler 7, the output end of the fourth fluid pipe 7-4 is connected to the upper tower 5 of the rectifying tower, the upper part of the upper tower 5 of the rectifying tower is respectively connected to the second fluid pipe 7-2 and a third fluid pipe 7-3, the second fluid pipe 7-2 is connected to the input end of the third fluid loop 1-3, the output end of the third fluid loop 1-3 is connected to a high-purity nitrogen conveying, the third fluid pipe 7-3 is connected to the input end of a fourth fluid circuit 1-4, the output end of the fourth fluid circuit 1-4 is connected to a waste nitrogen purification system 11, the lower part of the upper tower 5 of the rectification tower is connected to the input end of a fifth fluid circuit 1-5, the low-temperature liquid oxygen storage tank 3 and the upper tower 5 of the rectification tower are connected in parallel or in series in sequence to the input end of the fifth fluid circuit 1-5 along the liquid oxygen conveying direction, the output end of the fifth fluid circuit 1-5 is connected to an oxygen pipeline 12 to be used, the bottom of the upper tower 5 of the rectification tower and the top of the lower tower 6 of the rectification tower are connected to be provided with a liquid nitrogen circulating pipeline, the liquid nitrogen circulating pipeline comprises a first liquid nitrogen circulating pipeline and a second liquid nitrogen circulating pipeline (not shown), the second liquid nitrogen circulating pipeline is also connected to the input end of the first fluid pipe 7-1 in the subcooler 7, the output end of the first fluid pipe 7-1 is respectively connected to the top of the upper tower 5 of the rectifying tower and the low-temperature liquid nitrogen storage tank 4.
As shown in fig. 2, the low-temperature liquid oxygen storage tank 3 and the upper rectifying tower 5 are sequentially connected in series to the input end of the fifth fluid loop 1-5 along the liquid oxygen conveying direction. Liquid oxygen supplemented from the low-temperature liquid oxygen storage tank 3 is gasified through the bottom of the upper tower 5 of the rectifying tower, and then is converged with liquid oxygen produced at the bottom of the upper tower 5 of the rectifying tower after rectification, and the gasified oxygen becomes ascending steam, so that the problem that liquid oxygen circulation is not smooth due to the fact that the pipeline is blocked by the original process liquid oxygen gasification bubbles can be prevented.
On the basis of the technical scheme, in the specific implementation, the system further comprises a booster turboexpander 8, wherein a boosting end inlet of the booster turboexpander 8 is connected with a first gas supply pipeline inlet 9-1, a boosting end outlet of the booster turboexpander 8 is connected with an input end of a first fluid loop 1-1, an output end of the first fluid loop 1-1 is connected with an expansion end of the booster turboexpander 8, and an expansion end of the booster turboexpander 8 is connected with the upper part of an upper tower 5 of the rectifying tower.
On the basis of the technical scheme, in the concrete implementation, the system further comprises a piston type air supercharger 2 and a high-efficiency after-cooler (not shown in the figure), wherein the input end of the piston type air supercharger 2 is connected with the inlet 9-2 of the second air supply pipeline, the output end of the piston type air supercharger 2 is connected with the input end of the high-efficiency after-cooler, and the output end of the high-efficiency after-cooler is connected with the input end of the second fluid loop 1-2.
The working principle of the invention is as follows:
a conventional air separation plant (using the well-known technology of oxygen production by double-column rectification) is designed to have the output of the lowest gas consumption of the fluctuation of the gas consumption of a client (during normal gas consumption), and if the gas consumption of the client fluctuates at 1200 and 2000 square/hour, the output of the air separation plant is designed to be 1200 square/hour of the oxygen output.
And (3) describing an air separation flow: one part of air (which is a known conventional technology) which is subjected to compression, cooling and water and carbon dioxide purification enters a supercharging end of a supercharging turboexpander 8 for supercharging, enters a main heat exchanger 1 for further cooling after being cooled, then passes through an expansion end of the supercharging turboexpander 8, is sent into an upper tower 5 of a rectifying tower for participating in rectification after being expanded, cooled and depressurized, and the other part of air directly enters the main heat exchanger 1 for reducing the temperature and partially liquefies, and then enters a lower tower 6 of the rectifying tower. Part of the oxygen-enriched liquid air is extracted from the bottom of the lower tower 6 of the rectifying tower, enters a subcooler 7 for subcooling, and then is sent to the upper tower 5 of the rectifying tower to participate in rectification. The high-purity nitrogen gas extracted from the top of the lower tower 6 of the rectifying tower enters a condensing evaporator of an upper tower 5 of the rectifying tower to be liquefied, one part of the liquefied liquid nitrogen is used as reflux liquid of the lower tower 6 of the rectifying tower, one part of the liquefied liquid nitrogen enters a subcooler 7 to be subcooled and then enters the upper tower 5 of the rectifying tower to be used as reflux liquid of the upper tower 5 of the rectifying tower, and the other part of the liquefied liquid nitrogen is extracted into a low-temperature liquid nitrogen storage tank 4 to be used as product liquid nitrogen.
The bottom of the upper tower 5 of the rectifying tower after rectification produces qualified liquid oxygen, the qualified liquid oxygen is converged with liquid oxygen supplemented from a low-temperature liquid oxygen tank, then the liquid oxygen is pressurized by a low-temperature liquid oxygen pump and enters the main heat exchanger 1, the liquid oxygen is gasified into gaseous oxygen with certain pressure by utilizing cold in the main heat exchanger 1, and the gaseous oxygen is supplied to customers for use.
High-purity nitrogen generated at the top of the upper tower 5 of the rectifying tower, part of impure nitrogen needs to be pumped out from the upper part of the upper tower 5 of the rectifying tower, the part of high-purity nitrogen and the impure nitrogen are used as regeneration gas of an air separation purifier, and the redundant part of the high-purity nitrogen is discharged.
When the gas consumption of a user is more than 1200 square/hour, such as 1800 square/hour, the liquid oxygen in the storage tank (at the moment, 600 square/hour is supplemented) is used for supplementing the inlet of the low-temperature liquid oxygen pump through a pipeline, so that the consumption of the oxygen of the user is ensured, at the moment, the cold energy of the system is surplus, and a part of liquid nitrogen which is extracted from the liquid nitrogen extracted from the condensing evaporator of the upper tower 5 of the rectifying tower can be extracted as a product to enter the low-temperature liquid nitrogen storage tank 4 (about 600 square/hour by calculation); this results in a slight reduction in the liquid nitrogen reflux in the upper column 5 of the rectification column and, ultimately, in the liquid oxygen produced at the bottom of the upper column 5 of the rectification column, so that in practice, a little more liquid oxygen must be replenished in the storage tank, e.g. 650 square/hour.
By the technical scheme of the invention, the working condition of the air separation device is always stabilized at the design working condition, only micro-adjustment is needed, the air separation energy consumption is lowest, the operation is most stable, and the operation is simple. Through calculation, 650 standard square liquid oxygen is supplemented to generate about 600 standard square liquid nitrogen, the energy consumption of the increased compressor is only about 50KW, and the energy consumption of the liquid nitrogen is only 0.09KWh/Nm3If the added cost of using liquid oxygen is calculated (the difference between the production cost per square of liquid oxygen and that of gaseous oxygen is about 0.4kWh), the energy consumption of liquid nitrogen is 0.5kWh/Nm3Compared with the common liquid nitrogen production cost, the production cost is 0.7KWh/Nm3But is also low.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents and improvements made within the spirit and principle of the present invention are intended to be included within the scope of the present invention.

Claims (4)

1. The utility model provides a method of stable air feed of low energy consumption, is through compressing, cooling and purification dewatering and carbon dioxide processing to the air, obtains the air that waits to supply air, divide into two parts with the air that waits to supply air, obtains first air current that waits to supply and the second air current that waits to supply, its characterized in that includes:
providing a main heat exchanger (1) having at least five separate fluid circuits such that a first air to be supplied is provided to a first fluid circuit (1-1) of the main heat exchanger (1), a second air to be supplied is provided to a second fluid circuit (1-2) of the main heat exchanger (1), a first heat exchange air flow is provided to a third fluid circuit (1-3) of the main heat exchanger (1), a second heat exchange air flow is provided to a fourth fluid circuit (1-4) of the main heat exchanger (1), a third heat exchange air flow is provided to a fifth fluid circuit (1-5) of the main heat exchanger (1), whereby the first air to be supplied, the second air to be supplied air flow are indirectly heat exchanged with the first, the second and the third heat exchange air flow to enable the first air to be supplied flow, The second gas stream to be supplied is cooled;
discharging the cooled first air flow to be supplied and the cooled second air flow to be supplied from the main heat exchanger (1);
discharging the heated first, second and third heat exchange air streams from the main heat exchanger (1);
wherein at least a portion of each of the first, second, and third heat exchange air streams is obtained by processing a first air stream to be supplied and a second air stream to be supplied;
at least one part of each of the first heat-exchange air flow, the second heat-exchange air flow and the third heat-exchange air flow is obtained by processing a first air flow to be supplied and a second air flow to be supplied through a rectifying tower, and the rectifying tower is divided into an upper rectifying tower (5) and a lower rectifying tower (6);
a first to-be-supplied gas flow discharged from the main heat exchanger (1) enters an expansion end of a booster turboexpander (8), and is sent to an upper tower (5) of a rectifying tower to participate in rectification after being expanded, cooled and depressurized;
a second gas flow to be supplied, which is discharged from the main heat exchanger (1), enters a lower tower (6) of the rectifying tower, part of oxygen-enriched liquid air is extracted from the bottom of the lower tower (6) of the rectifying tower, enters a subcooler (7) for subcooling, and then is sent to an upper tower (5) of the rectifying tower to participate in rectification;
sending high-purity nitrogen gas extracted from the top of a lower tower (6) of a rectifying tower into a condensing evaporator of an upper tower (5) of the rectifying tower for liquefaction, wherein one part of liquefied liquid nitrogen is used as reflux liquid of the lower tower (6) of the rectifying tower, the other part of liquefied liquid nitrogen enters a subcooler (7) for subcooling and then enters the upper tower (5) of the rectifying tower to be used as reflux liquid of the upper tower (5) of the rectifying tower, and the rest part of liquefied liquid nitrogen is extracted into a low-temperature liquid nitrogen storage tank (4) to be used as product liquid nitrogen;
the upper tower (5) of the rectifying tower is rectified to produce qualified liquid oxygen at the bottom, the qualified liquid oxygen is converged with liquid oxygen supplemented from the low-temperature liquid oxygen storage tank (3), the liquid oxygen is pressurized by a low-temperature liquid oxygen pump to enter the main heat exchanger (1), and the liquid oxygen is gasified into gas oxygen with certain pressure and capable of being used by utilizing cold energy in the main heat exchanger (1); meanwhile, high-purity nitrogen generated at the top of the upper tower (5) of the rectifying tower and part of impure nitrogen required to be extracted from the upper part of the upper tower (5) of the rectifying tower are used as regeneration gas of an air separation purifier, and the redundant nitrogen is discharged;
liquid oxygen supplemented from the low-temperature liquid oxygen storage tank (3) is gasified at the bottom of the upper tower (5) of the rectifying tower and then is converged with liquid oxygen produced at the bottom of the upper tower (5) of the rectifying tower after rectification.
2. A method for supplying gas stably with low energy consumption as claimed in claim 1, wherein: the first air flow to be supplied is also subjected to pressurization through a pressurization end of a pressurization turboexpander (8) before entering the main heat exchanger (1), and enters the main heat exchanger (1) after being cooled.
3. A method for supplying gas stably with low energy consumption as claimed in claim 1, wherein: the second air flow to be supplied is sequentially subjected to the steps of pressurization and cooling before entering the main heat exchanger (1), and is partially liquefied and cooled when being discharged from the main heat exchanger (1).
4. A low energy consumption stable gas supply system based on the method of any one of claims 1 to 3, characterized by comprising a main heat exchanger (1) with five divided fluid circuits, a rectifying column upper column (5), a rectifying column lower column (6), a subcooler (7) with four divided fluid tubes, a cryogenic liquid oxygen storage tank (3) and a cryogenic liquid nitrogen storage tank (4); the fluid circuits of the main heat exchanger (1) are respectively a first fluid circuit (1-1), a second fluid circuit (1-2), a third fluid circuit (1-3), a fourth fluid circuit (1-4) and a fifth fluid circuit (1-5) in sequence; fluid pipes of the subcooler (7) are a first fluid pipe (7-1), a second fluid pipe (7-2), a third fluid pipe (7-3) and a fourth fluid pipe (7-4) in sequence; the air supply pipeline inlet (9) is divided into a first air supply pipeline inlet (9-1) and a second air supply pipeline inlet (9-2); wherein the content of the first and second substances,
the first gas supply pipeline inlet (9-1) is connected to the input end of a first fluid circuit (1-1), the output end of the first fluid circuit (1-1) is connected to the upper part of an upper rectifying tower (5), the second gas supply pipeline inlet (9-2) is connected to the input end of a second fluid circuit (1-2), the output end of the second fluid circuit (1-2) is connected to the lower part of a lower rectifying tower (6), the lower part of the lower rectifying tower (6) is connected to the input end of a fourth fluid pipe (7-4) of a subcooler (7), the output end of the fourth fluid pipe (7-4) is connected to the upper rectifying tower (5), the upper part of the upper rectifying tower (5) is respectively connected to the second fluid pipe (7-2) and the third fluid pipe (7-3), the second fluid pipe (7-2) is connected to the input end of a third fluid loop (1-3), the output end of the third fluid loop (1-3) is connected to a high-purity nitrogen conveying pipeline (10), the third fluid pipe (7-3) is connected to the input end of a fourth fluid loop (1-4), the output end of the fourth fluid loop (1-4) is connected to a sewage nitrogen purification system (11), the lower part of an upper tower (5) of the rectification tower is connected to the input end of a fifth fluid loop (1-5), the low-temperature liquid oxygen storage tank (3) and the upper tower (5) of the rectification tower are connected in parallel or in series in sequence to the input end of the fifth fluid loop (1-5) along the liquid oxygen conveying direction, and the output end of the fifth fluid loop (1-5) is connected to an oxygen pipeline (12) to be used, the bottom of rectifying column upper tower (5) is connected with the top of rectifying column lower tower (6) and is set up liquid nitrogen circulating line, liquid nitrogen circulating line includes first liquid nitrogen circulating line and second liquid nitrogen circulating line, second liquid nitrogen circulating line still is connected to the input of first fluid pipe (7-1) in subcooler (7), the output of first fluid pipe (7-1) is connected to the top and low temperature liquid nitrogen storage tank (4) of rectifying column upper tower (5) respectively.
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