CN113154796B - Variable multi-cycle oxygen-nitrogen cold energy utilization device and method for recycling oxygen-nitrogen resources - Google Patents

Variable multi-cycle oxygen-nitrogen cold energy utilization device and method for recycling oxygen-nitrogen resources Download PDF

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CN113154796B
CN113154796B CN202110309659.5A CN202110309659A CN113154796B CN 113154796 B CN113154796 B CN 113154796B CN 202110309659 A CN202110309659 A CN 202110309659A CN 113154796 B CN113154796 B CN 113154796B
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oxygen
nitrogen
pressure
valve
liquid
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CN113154796A (en
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刘道科
张得仑
李正录
张娟娟
曹和庆
张格亮
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Jinchuan Group Nickel Cobalt Co ltd
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Jinchuan 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
    • F25J3/04472—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 cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
    • F25J3/04496—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 cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist
    • 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
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
    • 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
    • F25J3/04472—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 cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
    • F25J3/04496—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 cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist
    • F25J3/04503—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 cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems
    • 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
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04612—Heat exchange integration with process streams, e.g. from the air gas consuming unit
    • 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
    • F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/42—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being 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
    • 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
    • F25J2250/42—One fluid being 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
    • 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
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/60—Details about pipelines, i.e. network, for feed or product distribution

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

Abstract

The invention discloses a variable multi-cycle oxygen and nitrogen cold energy utilization device and method for recovering oxygen and nitrogen resources, which take high-quality cold energy of oxygen and nitrogen low-temperature liquid as a medium, realize the high-efficiency recovery and utilization of the oxygen and nitrogen resources in a cyclic utilization mode, and provide a new way for a rapid emergency peak regulation mode of an air separation system, thereby greatly reducing the oxygen and nitrogen diffusion rate and effectively promoting the remarkable reduction of the oxygen and nitrogen utilization cost. The invention eliminates the defect of emergency guarantee by using steam to heat liquid oxygen for vaporization, has the advantages of recycling cold energy and reducing steam consumption, and can selectively convert liquid oxygen and liquid nitrogen products according to market demands, thereby realizing better economic benefit. The invention can also be provided with different recovery scales according to the characteristics of users, thereby achieving the best economic benefit.

Description

Variable multi-cycle oxygen-nitrogen cold energy utilization device and method for recycling oxygen-nitrogen resources
Technical Field
The invention belongs to the field of advanced energy conservation of air separation systems, and particularly relates to a variable multi-cycle oxygen-nitrogen cold energy utilization device and method for recovering oxygen-nitrogen resources.
Background
The large-scale air separation technology adopting a deep low-temperature freezing method is a main way for preparing oxygen and nitrogen products in a modern industrialized large scale, and the process has the advantages of abundant products, low comprehensive energy consumption, stable performance and the like, and also has the defects of incapability of starting and stopping at any time, small load variation range, long starting time, complex system operation and the like, so the process is particularly suitable for a long-term stable oxygen and nitrogen product supply environment.
However, in the actual production process, in the fields of large-scale chemical industry, steel and nonferrous smelting which need a large amount of oxygen and nitrogen, the situation that a user does not use oxygen for various reasons in a short time exists, a phenomenon of diffusing a large amount of oxygen is generated, and the loss caused by long-term accumulation is very large. Taking a certain nonferrous smelting enterprise as an example, 6.4 million standard oxygen scales are needed each year, about 3400 million standard oxygen needs to be diffused each year due to the change of short-time load requirements of users, the economic value is as high as ten million yuan, and the cost reduction of the enterprise is a heavy pressure.
In order to cope with the unfavorable condition, various methods are adopted for coping with the unfavorable condition by the large-scale enterprises, and an APC (automatic Power control) variable load operation mode is adopted, but the load adjustment can only be operated in a range of 75-105%, the bottleneck can be met in coping with the short-time oxygen strong discharge, and the oxygen discharge can not be reduced after the lower limit of the load is lower; there is a method for recovering liquefied oxygen by using cold energy generated by an expansion refrigeration cycle after nitrogen compression as mentioned in utility model 201420235030.6, which can design the liquefaction amount according to the dispersion amount, theoretically achieve zero emission, but have high energy consumption (0.8-1 kwh/Nm) for oxygen liquefaction 3 O 2 ) And the problem of high-quality cold energy loss exists when the recovered liquid oxygen is reused by air-temperature or water-bath type reheating, and a large amount of liquefaction energy consumption is consumed invisibly, and the method has the defects that the system equipment maintenance investment is high, and the economy is insufficient for areas with higher electricity prices; some methods adopt liquid nitrogen and gas oxygen to exchange heat and then liquefy and recover oxygen, and vaporized nitrogen is discharged, so that zero emission can be achieved theoretically, but nitrogen resources cannot be reasonably utilized, and the problems of high-quality cold energy loss when the recovered liquid oxygen is reused by air-temperature or water-bath type reheating exist, and the economical efficiency is obviously insufficient. In addition, the oxygen emergency standby system generally adopts a water bath type or air temperature type reheating method, so that the problem that high-quality cold energy cannot be recycled exists, and the problem that steam is consumed also exists.
Similarly, for compressed nitrogen, in order to respond to the requirement change of a user, generally, nitrogen is supplied by adopting a plurality of nitrogen compressors for centralized supply, a problem often occurs on production assembly, N sets are not enough, N +1 sets are required to be emptied, the load adjustment range is also limited by a surge area and can only be operated in a range of 75% -105%, in order to maintain normal production, only additional equipment is adopted to maintain the requirement of the user, so that the nitrogen compressors deviate from the designed optimal working condition or are emptied or are frequently started and stopped, and the integral operation economy is poor. Taking nonferrous smelting enterprises as an example, the annual demand of 2.6 million standard nitrogen scale is met, the amount of nitrogen released per year reaches 1300 ten thousand standard, and the economic value reaches 100 ten thousand yuan.
Disclosure of Invention
Aiming at the problems in the prior art, the invention provides a variable multi-cycle oxygen-nitrogen cold energy utilization device and method for recovering oxygen-nitrogen resources, aiming at solving the economic problem of recovery and utilization when oxygen is temporarily diffused in a large scale, synchronously considering the problems of diffusion, deviation from the designed optimal working condition, difficult coordination, frequent on-off of nitrogen press equipment and the like caused by mismatched compressed nitrogen in normal operation, achieving the purpose of efficiently and low-cost recovery of all oxygen-nitrogen diffused resources, and providing a novel air separation load adjustment mode, thereby reducing the comprehensive energy consumption of an air separation system.
The invention adopts the following technical scheme:
the variable multi-cycle oxygen-nitrogen cold energy utilization device for recovering oxygen-nitrogen resources is characterized by comprising a liquid nitrogen storage tank (1), a plate heat exchanger (3), a compressed nitrogen pipe network (4), a high-pressure oxygen pipe network (5), a medium-pressure oxygen pipe network (6), a low-pressure oxygen pipe network (7), a liquid oxygen storage tank (8), a low-pressure nitrogen pipe network (11) and an air fractionation system (9); the liquid nitrogen storage tank (1) is connected with the plate type heat exchanger (3) through a pipeline provided with a centrifugal liquid nitrogen pump (2) and a valve, and the plate type heat exchanger (3) is connected with the liquid nitrogen storage tank (1) through a pipeline provided with a valve; the plate type heat exchanger (3) is connected with a compressed nitrogen pipe network (4) through a pipeline provided with a valve, the compressed nitrogen pipe network (4) is connected with a low-pressure nitrogen pipe network (11) through a pipeline provided with a nitrogen compressor group (10), and the plate type heat exchanger (3) is connected with the low-pressure nitrogen pipe network (11) through a pipeline provided with a valve; low pressure nitrogen gas pipe network (11) and air fractionation system (9) pass through the pipe connection, high-pressure oxygen pipe network (5), medium pressure oxygen pipe network (6), low pressure oxygen pipe network (7) pass through the pipe connection with air fractionation system (9) respectively, high-pressure oxygen pipe network (5), medium pressure oxygen pipe network (6), low pressure oxygen pipe network (7) are respectively with plate heat exchanger (3) through the pipe connection of installing the valve, plate heat exchanger (3) and liquid oxygen storage tank (8) are through the pipe connection of installing the valve.
The variable multi-cycle oxygen-nitrogen cold energy utilization device for recovering the oxygen-nitrogen resources is characterized in that a centrifugal liquid nitrogen pump inlet valve (12) is installed on a pipeline between the liquid nitrogen storage tank (1) and the centrifugal liquid nitrogen pump (2), and an automatic adjusting and cutting valve (13) is installed on a pipeline between the centrifugal liquid nitrogen pump (2) and the plate type heat exchanger (3); a pipeline between the centrifugal liquid nitrogen pump (2) and the automatic regulating cut-off valve (13) is connected with the liquid nitrogen storage tank (1) through a pipeline provided with a liquid nitrogen reflux valve (14); a pipeline between the automatic regulating cut-off valve (13) and the plate heat exchanger (3) is connected with the liquid nitrogen storage tank (1) through a pipeline provided with a liquid nitrogen throttling automatic regulating valve (15); the valve arranged on the pipeline between the plate heat exchanger (3) and the liquid oxygen storage tank (8) is a liquid oxygen bidirectional flow automatic regulating valve (16).
The variable multi-cycle oxygen-nitrogen cold energy utilization device for recovering oxygen-nitrogen resources is characterized in that a valve mounted on a pipeline between the high-pressure oxygen pipe network (5) and the plate heat exchanger (3) is an automatic high-pressure oxygen adjusting valve (20), a valve mounted on a pipeline between the medium-pressure oxygen pipe network (6) and the plate heat exchanger (3) is an automatic medium-pressure oxygen adjusting valve (21), and a valve mounted on a pipeline between the low-pressure oxygen pipe network (7) and the plate heat exchanger (3) is an automatic low-pressure oxygen adjusting valve (19); the valve of the pipeline installation between the plate heat exchanger (3) and the compressed nitrogen pipe network (4) is a nitrogen bidirectional flow automatic regulating valve (18), and the pipeline between the plate heat exchanger (3) and the nitrogen bidirectional flow automatic regulating valve (18) is connected with the low-pressure nitrogen pipe network (11) through the pipeline provided with the low-pressure nitrogen automatic regulating valve (17).
The method for utilizing the variable multi-cycle oxygen-nitrogen cold energy utilization device for recovering the oxygen-nitrogen resource is characterized by comprising the following steps of:
step (I): firstly, opening an inlet valve of a centrifugal liquid nitrogen pump, and then sequentially opening an automatic adjusting and cutting valve and a low-pressure nitrogen automatic adjusting valve; controlling the opening of the medium-pressure oxygen automatic regulating valve to pressurize the pipeline provided with the medium-pressure oxygen automatic regulating valve, the pipeline between the plate heat exchanger and the liquid oxygen bidirectional flow automatic regulating valve;
step (II): when the medium-pressure oxygen is recovered, when the temperature of a liquid nitrogen inlet in the plate heat exchanger is reduced to be lower than-195 ℃ and the temperature of a liquid oxygen outlet in the plate heat exchanger is lower than-180 ℃, opening the liquid oxygen bidirectional flow automatic regulating valve, and controlling the opening value of the liquid oxygen bidirectional flow automatic regulating valve to be lower than 5%; starting the centrifugal liquid nitrogen pump, and controlling the opening of the liquid nitrogen reflux valve to ensure that the outlet pressure of the centrifugal liquid nitrogen pump is 0.05-0.1 Mpa higher than the nitrogen pressure in the compressed nitrogen pipe network; inputting the liquefied medium-pressure oxygen in the plate heat exchanger into a liquid oxygen storage tank for storage;
step (three): when the high-pressure oxygen is recovered, opening the high-pressure oxygen automatic regulating valve, and controlling the pressure of the pipeline provided with the high-pressure oxygen automatic regulating valve to be 0.8-1.25 Mpa; then closing the medium-pressure oxygen automatic regulating valve, opening the liquid oxygen bidirectional flow automatic regulating valve, and inputting the liquefied high-pressure oxygen in the plate heat exchanger into a liquid oxygen storage tank for storage;
step (IV): when pressure nitrogen is recovered, closing the automatic regulating and cutting valve, opening the liquid nitrogen reflux valve and the low-pressure oxygen automatic regulating valve, and opening the liquid nitrogen throttling automatic regulating valve and the liquid oxygen bidirectional flow automatic regulating valve; controlling the opening value of the low-pressure oxygen automatic regulating valve to be 27% -35%; and inputting the pressure nitrogen liquefied in the plate heat exchanger into a liquid nitrogen storage tank for storage.
The utilization method of the variable multi-cycle oxygen-nitrogen cold energy utilization device for recovering the oxygen-nitrogen resource is characterized in that the absolute value of the difference between the temperature of a nitrogen inlet and a nitrogen outlet in the plate type heat exchanger and the temperature of an oxygen inlet and a oxygen outlet in the plate type heat exchanger in the steps (II), (III) and (IV) is less than 15 ℃; putting a liquid nitrogen reflux valve into constant pressure control in the step (II); and (3) putting the liquid oxygen bidirectional flow automatic regulating valve into constant temperature control in the step (II) and the step (III), wherein the temperature setting range of the constant temperature control of the liquid oxygen bidirectional flow automatic regulating valve is-180 ℃ to-183 ℃.
The method for utilizing the variable multi-cycle oxygen-nitrogen cold energy utilization device for recovering the oxygen-nitrogen resource is characterized in that in the step (II), the liquid nitrogen reflux valve is controlled by constant pressure, and the pressure setting range of the constant pressure control is 0.7-0.9 MPa; and (C) adopting constant temperature control by the liquid nitrogen throttling automatic regulating valve in the step (IV), wherein the temperature setting range of the constant temperature control is-172 ℃ to-175 ℃.
The invention has the beneficial technical effects that: the liquid oxygen and liquid nitrogen byproducts generated by the air separation system are stored in a low-temperature container, when abnormal production is performed, the liquid nitrogen generated by the air separation system is pressurized by a centrifugal liquid nitrogen pump to enter a plate heat exchanger to exchange heat with temporary large-scale diffused oxygen, the liquid nitrogen is changed into compressed nitrogen after reheating to enter a pipe network for users to use, at the moment, a corresponding nitrogen compressor is stopped to realize energy conservation (the unit energy consumption of the compressed low-temperature liquid is only within 5 percent of the unit energy consumption of the compressed medium gas), and the oxygen absorbs the cold energy of the liquid nitrogen, is liquefied and throttled and then enters a liquid oxygen storage tank for later use; during normal production, recovered liquid oxygen enters the plate heat exchanger to exchange heat with diffused pressure nitrogen, the liquid oxygen enters the oxygen pipe network after being reheated to be used by a user, the pressure nitrogen is liquefied and then throttled to enter the liquid nitrogen storage tank to prepare for the next round of oxygen recovery, and the automatic variable load system is utilized in the period to reduce the load of the oxygen generator set, and meanwhile, the advantages of the nitrogen compressor in the design working condition can be fully exerted, and the purpose of energy conservation is achieved. The method can take the oxygen-nitrogen cold energy as a medium, can efficiently recover oxygen-nitrogen resources for cyclic utilization, and can provide an effective variable load operation method of the air separation system, greatly reduce the oxygen and nitrogen diffusion rate and effectively promote the remarkable reduction of the oxygen-nitrogen utilization cost; as long as the reasonable recovery scale is configured, the complete recovery and utilization of oxygen and nitrogen resources can be realized, the cost is reduced by more than 95 percent compared with the traditional expansion refrigeration liquefaction method, and the steam consumption is reduced. The method of the invention eliminates the defect of the traditional emergency guarantee by using steam to heat liquid oxygen for vaporization, has the advantages of recycling cold energy and reducing steam consumption, and can selectively convert liquid oxygen and liquid nitrogen products according to market demands, thereby realizing better economic benefit; the method can also be provided with different recycling scales according to the characteristics of users, thereby achieving the best economic benefit.
Drawings
FIG. 1 is a schematic view of the structure of the apparatus of the present invention.
Detailed Description
Referring to fig. 1, the variable multicycle oxygen-nitrogen cold energy utilization device for recovering oxygen-nitrogen resources of the present invention includes a liquid nitrogen storage tank 1, a plate heat exchanger 3, a compressed nitrogen pipe network 4, a high pressure oxygen pipe network 5, a medium pressure oxygen pipe network 6, a low pressure oxygen pipe network 7, a liquid oxygen storage tank 8, a low pressure nitrogen pipe network 11, and an air fractionation system 9; the liquid nitrogen storage tank 1 is connected with the plate type heat exchanger 3 through a pipeline provided with a centrifugal liquid nitrogen pump 2 and a valve, and the plate type heat exchanger 3 is connected with the liquid nitrogen storage tank 1 through a pipeline provided with a valve; the pipeline provided with the centrifugal liquid nitrogen pump 2 is connected with the liquid nitrogen storage tank 1 through a pipeline provided with a valve; the plate heat exchanger 3 is connected with the compressed nitrogen pipe network 4 through a pipeline provided with a valve, the compressed nitrogen pipe network 4 is connected with the low-pressure nitrogen pipe network 11 through a pipeline provided with a nitrogen compressor group 10, a pipeline between the plate heat exchanger 3 and the compressed nitrogen pipe network 4 is connected with the low-pressure nitrogen pipe network 11 through a pipeline provided with a valve, and the valve arranged on the pipeline between the plate heat exchanger 3 and the compressed nitrogen pipe network 4 is an automatic regulating valve 18 for nitrogen bidirectional flow. And a pipeline between the plate heat exchanger 3 and the nitrogen bidirectional flow automatic regulating valve 18 is connected with the low-pressure nitrogen pipe network 11 through a pipeline provided with a low-pressure nitrogen automatic regulating valve 17. The low pressure nitrogen pipe network 11 passes through the pipe connection with air fractionation system 9, high pressure oxygen pipe network 5, middling pressure oxygen pipe network 6, low pressure oxygen pipe network 7 passes through the pipe connection with air fractionation system 9 respectively, high pressure oxygen pipe network 5, middling pressure oxygen pipe network 6, low pressure oxygen pipe network 7 passes through the pipe connection of installing the valve with plate heat exchanger 3 respectively, the valve of the pipe installation between high pressure oxygen pipe network 5 and plate heat exchanger 3 is high pressure oxygen automatically regulated valve 20, the valve of the pipe installation between middling pressure oxygen pipe network 6 and plate heat exchanger 3 is middling pressure oxygen automatically regulated valve 21, the valve of the pipe installation between low pressure oxygen pipe network 7 and plate heat exchanger 3 is low pressure oxygen automatically regulated valve 19. The plate heat exchanger 3 is connected with the liquid oxygen storage tank 8 through a pipeline provided with a valve. A pipeline between the liquid nitrogen storage tank 1 and the centrifugal liquid nitrogen pump 2 is provided with a centrifugal liquid nitrogen pump inlet valve 12, and a pipeline between the centrifugal liquid nitrogen pump 2 and the plate type heat exchanger 3 is provided with an automatic adjusting cut-off valve 13; a pipeline between the centrifugal liquid nitrogen pump 2 and the automatic regulating cut-off valve 13 is connected with the liquid nitrogen storage tank 1 through a pipeline provided with a liquid nitrogen reflux valve 14; the pipeline between the automatic regulating cut-off valve 13 and the plate heat exchanger 3 is connected with the liquid nitrogen storage tank 1 through a pipeline provided with a liquid nitrogen throttling automatic regulating valve 15; the valve arranged on the pipeline between the plate heat exchanger 3 and the liquid oxygen storage tank 8 is a liquid oxygen bidirectional flow automatic regulating valve 16.
A method for utilizing a variable multicycle oxygen-nitrogen cold energy utilization device for recovering oxygen-nitrogen resources, comprising the steps of:
step (I): all valves in the device are closed, then an inlet valve 12 of the centrifugal liquid nitrogen pump is opened, and an automatic regulating and cutting valve 13 is opened, so that liquid nitrogen slowly flows into a nitrogen channel of the plate heat exchanger 3 along a pipeline by self flow to pre-cool the liquid nitrogen. And opening the low-pressure nitrogen automatic regulating valve 17, and allowing the vaporized low-pressure nitrogen obtained after the liquid nitrogen in the liquid nitrogen storage tank 1 enters the plate heat exchanger 3 to enter the low-pressure nitrogen pipe network 11. And opening the medium-pressure oxygen automatic regulating valve 21 and controlling the opening degree of the medium-pressure oxygen automatic regulating valve to pressurize the pipeline provided with the medium-pressure oxygen automatic regulating valve 21 and the pipeline between the plate heat exchanger 3 and the liquid oxygen bidirectional flow automatic regulating valve 16. The key point of this step is to guarantee that the oxygen passageway in the plate heat exchanger 3 avoids forming the negative pressure, and each part cooling is even. The device can recover medium-pressure oxygen, high-pressure oxygen and pressure nitrogen, and concretely comprises the steps (two) to (four).
Step (II): when the medium-pressure oxygen is recovered, after sufficient heat exchange, when the temperature of a liquid nitrogen inlet in the plate heat exchanger 3 is reduced to be less than-195 ℃ and the temperature of a liquid oxygen outlet in the plate heat exchanger 3 is less than-180 ℃, the liquid oxygen bidirectional flow automatic regulating valve 16 is manually and gradually opened, and the opening value of the liquid oxygen bidirectional flow automatic regulating valve 16 is controlled to be less than 5%. Starting the centrifugal liquid nitrogen pump 2, and controlling the opening of the liquid nitrogen reflux valve 14 to ensure that the outlet pressure of the centrifugal liquid nitrogen pump 2 is 0.05-0.1 Mpa higher than the nitrogen pressure in the compressed nitrogen pipe network 4; the liquid nitrogen reflux valve 14 adopts constant pressure control, and the pressure setting range of the constant pressure control is 0.7 Mpa-0.9 Mpa. The liquefied medium-pressure oxygen in the plate heat exchanger 3 is input into a liquid oxygen storage tank 8 for storage. The operation key point is that the absolute value of the difference value of the temperature of the nitrogen inlet and the temperature of the nitrogen outlet in the plate heat exchanger 3 and the temperature of the oxygen inlet and the oxygen outlet in the plate heat exchanger 3 is less than 15 ℃.
Meanwhile, the low-pressure nitrogen automatic regulating valve 17 for allowing the plate heat exchanger 3 to enter the low-pressure nitrogen pipe network 11 is closed, and the nitrogen bidirectional flow automatic regulating valve 18 for gradually opening the plate heat exchanger 3 to the compressed nitrogen pipe network 4 is opened. The liquid oxygen bidirectional flow automatic regulating valve 16 is opened. At the moment, the cold energy of liquid nitrogen and the heat energy of medium-pressure oxygen can be utilized to achieve the purpose that liquid nitrogen is converted into pressure nitrogen through vaporization and enters the compressed nitrogen pipe network 4 for users to use, and the medium-pressure oxygen is liquefied and then enters the liquid oxygen storage tank 8 through a pipeline between the plate heat exchanger 3 and the liquid oxygen storage tank 8 to be stored. The operation key point is that a liquid oxygen bidirectional flow automatic regulating valve arranged on a pipeline between the plate type heat exchanger 3 and the liquid oxygen storage tank 8 is put into operation automatically, a constant temperature control mode is adopted, the temperature is set to be-180 ℃ to-183 ℃, the valve is opened greatly when the temperature is reduced, the valve is closed small when the temperature is increased, and meanwhile, the absolute value of the difference value between the temperature of a nitrogen inlet and a nitrogen outlet in the plate type heat exchanger 3 and the temperature of an oxygen inlet and a oxygen outlet in the plate type heat exchanger 3 is ensured to be less than 15 ℃.
Step (III): when the high-pressure oxygen is recovered, slowly opening the high-pressure oxygen automatic regulating valve 20, and controlling the pressure of the pipeline provided with the high-pressure oxygen automatic regulating valve 20 to be 0.8-1.25 Mpa; then closing the medium-pressure oxygen automatic regulating valve 21, opening the liquid oxygen bidirectional flow automatic regulating valve 16, and inputting the liquefied high-pressure oxygen in the plate heat exchanger 3 into the liquid oxygen storage tank 8 for storage; the liquid oxygen bidirectional flow automatic regulating valve 16 adopts a constant temperature control mode, and the temperature is set to be-180 ℃ to-183 ℃. At the moment, the cold energy of liquid nitrogen and the heat energy of high-pressure oxygen can be utilized to achieve the purpose that liquid nitrogen is converted into pressure nitrogen through vaporization and enters the compressed nitrogen pipe network 4 for users to use, and the high-pressure oxygen is liquefied and then enters the liquid oxygen storage tank 8 through a pipeline between the plate heat exchanger 3 and the liquid oxygen storage tank 8 to be stored. The operation key points are that the high-pressure oxygen automatic regulating valve 20 in the oxygen passage from the high-pressure oxygen pipe network 5 to the plate heat exchanger 3 is automatically put into operation, a constant pressure control mode is adopted, when the pressure value of an oxygen channel in the plate heat exchanger 3 is higher than a set value, the valve is closed and is small, when the pressure value is lower than the set value, the valve is opened and other valves are operated and automatically set unchanged. The absolute value of the difference between the temperature of the nitrogen inlet and the temperature of the nitrogen outlet in the plate heat exchanger 3 and the temperature of the oxygen inlet and the oxygen outlet in the plate heat exchanger 3 is less than 15 ℃.
Step (IV): when pressure nitrogen is recovered, the automatic regulating and cutting valve 13 is closed, the liquid nitrogen reflux valve 14 and the low-pressure oxygen automatic regulating valve 19 are opened, the liquid nitrogen throttling automatic regulating valve 15 and the liquid oxygen bidirectional flow automatic regulating valve 16 are opened, and the liquid oxygen bidirectional flow automatic regulating valve 16 is regulated at 1% -100% according to the requirement; the liquid nitrogen throttling automatic regulating valve 15 adopts constant temperature control, and the temperature setting range of the constant temperature control is-172 ℃ to-175 ℃. Controlling the opening value of the low-pressure oxygen automatic regulating valve 19 to be 27-35%; and inputting the pressure nitrogen liquefied in the plate heat exchanger 3 into a liquid nitrogen storage tank 1 for storage. At the moment, the liquid oxygen cold energy and the compressed nitrogen heat energy can be utilized to achieve the purpose that the liquid oxygen is vaporized into low-pressure oxygen to enter a low-pressure oxygen pipe network 7 for users to use, and the compressed nitrogen is liquefied and then enters the liquid nitrogen storage tank 1 for storage through a pipeline between the plate heat exchanger 3 and the liquid nitrogen storage tank 1. The operation key point is that an automatic regulating valve between the plate heat exchanger 3 and the liquid nitrogen storage tank 1 is automatically put into operation, a constant temperature control mode is adopted, the temperature setting range is-172 ℃ to-175 ℃, when the temperature of liquid nitrogen discharged from the plate heat exchanger 3 is higher than the setting temperature, the valve is closed to be small, when the temperature of the liquid nitrogen is lower than the setting temperature, the valve is opened to be large, and meanwhile, the absolute value of the difference value between the temperature of a nitrogen inlet and a nitrogen outlet and the temperature of an oxygen inlet and a oxygen outlet in the plate heat exchanger 3 is ensured to be less than 15 ℃.
The utilization method of the invention enables the oxygen, liquid oxygen, nitrogen and liquid nitrogen mediums with different pressure grades to be reconfigured by the low-temperature liquid storage system, the pressurization system, the heat exchange system, the pipe network system, the air separation device and the automatic control device, thereby being capable of utilizing the oxygen and nitrogen cold energy circularly to the maximum extent. In the abnormal production process, the high-pressure normal-temperature oxygen and the medium-pressure normal-temperature oxygen which need to be diffused are subjected to full heat exchange with a pressurized liquid nitrogen medium, the oxygen is liquefied and cooled to about-183 ℃, then is throttled and stored in a low-temperature normal-pressure liquid oxygen storage tank, reheated pressure nitrogen enters a compressed nitrogen pipe network, and at the moment, a nitrogen compressor is stopped to realize energy conservation; in the normal production process, liquid oxygen recovered to the storage tank and nitrogen diffused by the nitrogen compressor are utilized to fully exchange heat, the nitrogen is liquefied and cooled to about 174.5 ℃, then is throttled and stored to the low-temperature normal-pressure liquid nitrogen storage tank, reheated oxygen enters the low-pressure oxygen pipe network, the load of the oxygen generator set can be reduced to realize energy conservation, the oxygen emergency peak regulation function can be realized by opening the nitrogen compressor to recover liquid oxygen cold energy, and steam loss and cold energy loss caused by steam gasification liquid oxygen peak regulation are avoided. The utilization method can realize the utilization function of variable multi-cycle oxygen-nitrogen cold energy, and a small amount of cold loss caused by irreversible heat exchange in the process is provided by liquid oxygen or liquid nitrogen of an air separation system.
The device of the invention must be provided with a liquid nitrogen and liquid oxygen cold energy storage system, and the total volume of the liquid oxygen storage system is required to meet the requirement that the diffused oxygen can be continuously and completely recycled and the liquid nitrogen storage system which is equal to the diffused oxygen and is more than 1.2 times. The temperature difference of the phase change heat transfer of the low-temperature oxygen-nitrogen liquid medium and the gaseous oxygen-nitrogen medium in the heat exchange system under various working conditions needs to meet the requirement that the temperature is not lower than 10 ℃ so as to reduce the irreversible loss of cold energy. The design of the heat exchange area of the plate heat exchanger not only needs to meet the requirement of recovering oxygen with the maximum diffusing pressure grade, but also needs to meet the heat exchange area required by the maximum oxygen requirement increment during peak shaving of equipment, and simultaneously needs to meet the highest pressure bearing grade of a recovery medium. The gas medium participating in the utilization of the circulating oxygen-nitrogen cooling energy cannot contain impurities such as moisture and the like and has the use requirements, so that the phenomenon of freezing and blocking of the plate heat exchanger is prevented, and the reasonable utilization of resources is realized. The device of the invention must be provided with a centrifugal liquid nitrogen pump with a frequency converter, thereby ensuring good pressure adaptation range and multi-cycle load complex change conditions; an oxygen step pressure reduction system and a perfect oxygen and nitrogen parallel pipe network system are also required to be configured to meet the requirements of recovering and releasing various oxygen and nitrogen resources. Different recovery scales and parameters can be configured according to the requirements of users and the requirement that the temperature difference of the hot end of the plate heat exchanger is not more than 15 ℃ so as to reduce irreversible loss.
When the medium-pressure and high-pressure oxygen recovery is realized, the pressure of liquid nitrogen is gradually increased by using a frequency converter, and the constant-pressure control of a liquid nitrogen reflux valve is used for adapting to the change of the nitrogen requirement of a user so as to prevent the cavitation phenomenon; the amount of oxygen recovered and diffused is controlled by the automatic regulating valve of liquid oxygen bidirectional flow and the amount of vaporized nitrogen. And the corresponding nitrogen compressor is stopped according to the amount of the vaporized nitrogen, so that the electric energy consumption of the nitrogen compressor is reduced. Compared with the compression efficiency of gas and liquid, the energy consumption required by the centrifugal liquid nitrogen pump is less than 5% of that of the nitrogen compressor, and the equivalent compression effect can be realized.
When the recovery of rich compressed nitrogen is realized, the centrifugal liquid nitrogen pump is stopped, and the entering amount of liquid oxygen is regulated by controlling the pressure of the compressed nitrogen pipe network to be not less than 0.66Mpa, so that the effect of completely recovering the required diffused compressed nitrogen into the liquid nitrogen storage tank is achieved. The recovered liquid oxygen is released by the liquid oxygen bidirectional flow automatic regulating valve, and enters a low-pressure oxygen pipe network after being heated and vaporized by compressed nitrogen, so that the overall load of an air separation system can be reduced, and the aim of saving energy is fulfilled. By increasing the nitrogen compressor and utilizing the compressed nitrogen to carry out oxygen load peak regulation, a large amount of steam energy waste caused by supplementing oxygen by using a steam vaporization liquid oxygen system can be avoided, and high-quality liquid oxygen cold energy is recovered by using the nitrogen for storage and standby application, wherein the energy consumption index is about 25% of the energy consumption of oxygen production of an air separation device.

Claims (5)

1. A utilization method of a variable multi-cycle oxygen-nitrogen cold energy utilization device for recovering oxygen-nitrogen resources is characterized by comprising a liquid nitrogen storage tank (1), a plate heat exchanger (3), a compressed nitrogen pipe network (4), a high-pressure oxygen pipe network (5), a medium-pressure oxygen pipe network (6), a low-pressure oxygen pipe network (7), a liquid oxygen storage tank (8), a low-pressure nitrogen pipe network (11) and an air fractionation system (9); the liquid nitrogen storage tank (1) is connected with the plate type heat exchanger (3) through a pipeline provided with a centrifugal liquid nitrogen pump (2) and a valve, and the plate type heat exchanger (3) is connected with the liquid nitrogen storage tank (1) through a pipeline provided with a valve; the plate type heat exchanger (3) is connected with the compressed nitrogen pipe network (4) through a pipeline provided with a valve, the compressed nitrogen pipe network (4) is connected with the low-pressure nitrogen pipe network (11) through a pipeline provided with a nitrogen compressor group (10), and the plate type heat exchanger (3) is connected with the low-pressure nitrogen pipe network (11) through a pipeline provided with a valve; the low-pressure nitrogen pipe network (11) is connected with the air fractionation system (9) through a pipeline, the high-pressure oxygen pipe network (5), the medium-pressure oxygen pipe network (6) and the low-pressure oxygen pipe network (7) are respectively connected with the air fractionation system (9) through pipelines, the high-pressure oxygen pipe network (5), the medium-pressure oxygen pipe network (6) and the low-pressure oxygen pipe network (7) are respectively connected with the plate heat exchanger (3) through a pipeline provided with a valve, and the plate heat exchanger (3) is connected with the liquid oxygen storage tank (8) through a pipeline provided with a valve; the method comprises the following steps:
step (I): firstly, opening an inlet valve of a centrifugal liquid nitrogen pump, and then sequentially opening an automatic adjusting and cutting valve and a low-pressure nitrogen automatic adjusting valve; controlling the opening of the medium-pressure oxygen automatic regulating valve to pressurize the pipeline provided with the medium-pressure oxygen automatic regulating valve, the pipeline between the plate heat exchanger and the liquid oxygen bidirectional flow automatic regulating valve;
step (II): when the medium-pressure oxygen is recovered, when the temperature of a liquid nitrogen inlet in the plate heat exchanger is reduced to be lower than-195 ℃ and the temperature of a liquid oxygen outlet in the plate heat exchanger is lower than-180 ℃, opening the liquid oxygen bidirectional flow automatic regulating valve, and controlling the opening value of the liquid oxygen bidirectional flow automatic regulating valve to be lower than 5%; starting the centrifugal liquid nitrogen pump, and controlling the opening of the liquid nitrogen reflux valve to ensure that the outlet pressure of the centrifugal liquid nitrogen pump is 0.05-0.1 Mpa higher than the nitrogen pressure in the compressed nitrogen pipe network; inputting the liquefied medium-pressure oxygen in the plate heat exchanger into a liquid oxygen storage tank for storage;
step (three): when the high-pressure oxygen is recovered, opening the high-pressure oxygen automatic regulating valve, and controlling the pressure of the pipeline provided with the high-pressure oxygen automatic regulating valve to be 0.8-1.25 Mpa; then closing the medium-pressure oxygen automatic regulating valve, opening the liquid oxygen bidirectional flow automatic regulating valve, and inputting the liquefied high-pressure oxygen in the plate heat exchanger into a liquid oxygen storage tank for storage;
step (IV): when pressure nitrogen is recovered, closing the automatic regulating and cutting valve, opening the liquid nitrogen reflux valve and the low-pressure oxygen automatic regulating valve, and opening the liquid nitrogen throttling automatic regulating valve and the liquid oxygen bidirectional flow automatic regulating valve; controlling the opening value of the low-pressure oxygen automatic regulating valve to be 27% -35%; and inputting the pressure nitrogen liquefied in the plate heat exchanger into a liquid nitrogen storage tank for storage.
2. The method for utilizing a variable multi-cycle oxygen and nitrogen cold energy utilization device for recovering oxygen and nitrogen resources as claimed in claim 1, wherein a centrifugal liquid nitrogen pump inlet valve (12) is installed on a pipeline between the liquid nitrogen storage tank (1) and the centrifugal liquid nitrogen pump (2), and an automatic adjusting cut-off valve (13) is installed on a pipeline between the centrifugal liquid nitrogen pump (2) and the plate heat exchanger (3); a pipeline between the centrifugal liquid nitrogen pump (2) and the automatic regulating cut-off valve (13) is connected with the liquid nitrogen storage tank (1) through a pipeline provided with a liquid nitrogen reflux valve (14); the pipeline between the automatic regulating cut-off valve (13) and the plate heat exchanger (3) is connected with the liquid nitrogen storage tank (1) through a pipeline provided with a liquid nitrogen throttling automatic regulating valve (15); the valve arranged on the pipeline between the plate heat exchanger (3) and the liquid oxygen storage tank (8) is a liquid oxygen bidirectional flow automatic regulating valve (16).
3. The utilization method of the variable multi-cycle oxygen-nitrogen cold energy utilization device for recovering oxygen-nitrogen resources as claimed in claim 1, wherein the valve installed in the pipeline between the high-pressure oxygen pipe network (5) and the plate heat exchanger (3) is an automatic high-pressure oxygen adjustment valve (20), the valve installed in the pipeline between the medium-pressure oxygen pipe network (6) and the plate heat exchanger (3) is an automatic medium-pressure oxygen adjustment valve (21), and the valve installed in the pipeline between the low-pressure oxygen pipe network (7) and the plate heat exchanger (3) is an automatic low-pressure oxygen adjustment valve (19); the valve of the pipeline installation between the plate heat exchanger (3) and the compressed nitrogen pipe network (4) is a nitrogen bidirectional flow automatic regulating valve (18), and the pipeline between the plate heat exchanger (3) and the nitrogen bidirectional flow automatic regulating valve (18) is connected with the low-pressure nitrogen pipe network (11) through the pipeline provided with the low-pressure nitrogen automatic regulating valve (17).
4. The utilization method of the variable multicycle oxygen and nitrogen cold energy utilization device for recovering oxygen and nitrogen resources as claimed in claim 1, wherein the absolute value of the difference between the temperature of the nitrogen inlet and outlet in the plate heat exchanger and the temperature of the oxygen inlet and outlet in the plate heat exchanger in step (II), step (III) and step (IV) is less than 15 ℃; putting a liquid nitrogen reflux valve into constant pressure control in the step (II); and (3) putting the liquid oxygen bidirectional flow automatic regulating valve into constant temperature control in the step (II) and the step (III), wherein the temperature setting range of the constant temperature control of the liquid oxygen bidirectional flow automatic regulating valve is-180 ℃ to-183 ℃.
5. The method for utilizing a variable multi-cycle oxygen-nitrogen heat utilization apparatus for recovering an oxygen-nitrogen resource according to claim 1, wherein in the step (II), the liquid nitrogen reflux valve is controlled at a constant pressure, and the pressure setting range of the constant pressure control is 0.7Mpa to 0.9Mpa; and (C) adopting constant temperature control by the liquid nitrogen throttling automatic regulating valve in the step (IV), wherein the temperature setting range of the constant temperature control is-172 ℃ to-175 ℃.
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Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114484263A (en) * 2022-01-07 2022-05-13 首钢京唐钢铁联合有限责任公司 Automatic load changing method and system for nitrogen-oxygen liquefaction device
CN114576552A (en) * 2022-01-25 2022-06-03 杭州制氧机集团股份有限公司 Energy storage production equipment and energy storage production method for air separation device

Family Cites Families (26)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2683806B2 (en) * 1988-03-17 1997-12-03 住友精化株式会社 Concentrated oxygen recovery method
US5004482A (en) * 1989-05-12 1991-04-02 Union Carbide Corporation Production of dry, high purity nitrogen
US5042994A (en) * 1990-05-25 1991-08-27 Union Carbide Industrial Gases Technology Corporation Control of pressure swing adsorption operations
US5114452A (en) * 1990-06-27 1992-05-19 Union Carbide Industrial Gases Technology Corporation Cryogenic air separation system for producing elevated pressure product gas
DE4126945A1 (en) * 1991-08-14 1993-02-18 Linde Ag METHOD FOR AIR DISASSEMBLY BY RECTIFICATION
FR2706195B1 (en) * 1993-06-07 1995-07-28 Air Liquide Method and unit for supplying pressurized gas to an installation consuming an air component.
FR2712383B1 (en) * 1993-11-12 1995-12-22 Air Liquide Combined installation of a metal production unit and an air separation unit.
US5666823A (en) * 1996-01-31 1997-09-16 Air Products And Chemicals, Inc. High pressure combustion turbine and air separation system integration
JP2000064813A (en) * 1998-08-25 2000-02-29 Toshiba Corp Cold storage type load leveling power generating system and power generating method using this system
US6119479A (en) * 1998-12-09 2000-09-19 Air Products And Chemicals, Inc. Dual mixed refrigerant cycle for gas liquefaction
US6276170B1 (en) * 1999-05-25 2001-08-21 Air Liquide Process And Construction Cryogenic distillation system for air separation
US6182471B1 (en) * 1999-06-28 2001-02-06 Praxair Technology, Inc. Cryogenic rectification system for producing oxygen product at a non-constant rate
CN1239875C (en) * 2002-02-07 2006-02-01 北京燕化高新技术股份有限公司 Method of recovering oxygen, nitrogen and air exhausted from air separator
CN200958887Y (en) * 2006-10-10 2007-10-10 山西新临钢钢铁有限公司 Cryogenic oxygen-nitrogen liquid converter
CN100494839C (en) * 2007-04-11 2009-06-03 杭州杭氧股份有限公司 Air separation system for generating liquid oxygen and liquid nitrogen
US9222725B2 (en) * 2007-06-15 2015-12-29 Praxair Technology, Inc. Air separation method and apparatus
CN101274750B (en) * 2007-12-29 2010-06-30 江苏晟宜环保科技有限公司 Tail gas-recycled sulfur recovery method
KR101676069B1 (en) * 2010-03-31 2016-11-14 오르트로프 엔지니어스, 리미티드 Hydrocarbon gas processing
CN101922850B (en) * 2010-09-15 2012-01-04 煤炭科学研究总院重庆研究院 Method for utilizing coalbed methane containing oxygen to prepare liquefied natural gas
CN105571270B (en) * 2014-10-14 2017-12-22 中国石油化工股份有限公司 A kind of device and method of air separation oxygen quick load change
CN104807289B (en) * 2014-10-31 2016-02-03 刘继福 LNG cold energy sky point is utilized to produce the method for liquid oxygen liquid nitrogen
CN104807292B (en) * 2015-04-13 2017-03-22 河南开元空分集团有限公司 Device and method for comprehensively utilizing nitrogen gas emptying energy and liquid argon gasification cold energy
CN106367778B (en) * 2016-08-29 2018-11-09 金川集团股份有限公司 A kind of device and method recycling heat in high temperature moist chlorine
CN106285944B (en) * 2016-09-13 2017-12-01 中国华能集团公司 A kind of IGCC peak-load regulation device and methods using space division system energy storage
TW202117248A (en) * 2019-09-18 2021-05-01 法商液態空氣喬治斯克勞帝方法研究開發股份有限公司 High-purity oxygen production system
CN211526879U (en) * 2020-02-11 2020-09-18 北京石油化工工程有限公司 Air separation system for semi-continuous medium-pressure nitrogen supply

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