CN115406180A - Method for quickly starting oxygen generator in cold state - Google Patents

Method for quickly starting oxygen generator in cold state Download PDF

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Publication number
CN115406180A
CN115406180A CN202210326910.3A CN202210326910A CN115406180A CN 115406180 A CN115406180 A CN 115406180A CN 202210326910 A CN202210326910 A CN 202210326910A CN 115406180 A CN115406180 A CN 115406180A
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China
Prior art keywords
pressure
air
tower
air separation
valve
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Granted
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CN202210326910.3A
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CN115406180B (en
Inventor
王怀全
于泳
沈起祥
曹峥
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Angang Steel Co Ltd
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Angang Steel Co Ltd
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/04406—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
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    • 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
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    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/04818—Start-up of the process
    • 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
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    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
    • F25J3/04957—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipments upstream of the fractionation unit (s), i.e. at the "front-end"
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
    • F25J3/04963—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipment within or downstream of the fractionation unit(s)
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    • 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
    • F25J2230/40—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being air
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen

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

Abstract

The invention relates to a method for quickly starting an oxygen generator in a cold state, which comprises three stages in a starting time division control mode, wherein the first stage control mode is that after the outlet pressure of an air compressor exceeds 0.42MPa, air is guided to a lower tower of an air separation tower; the second stage of control, after the pressure of the air compressor is 0.46MPa, the supercharger is started; and in the third stage, the booster is raised to normal working pressure, and the upper tower pressure of the air separation tower is controlled to be 40-50KPa. And the opening degree of the switch key valve and the accurate control valve is orderly opened in each stage, so that the rectification can be quickly established when the oxygen generator set is started in a cold state, and the product is quickly qualified. The overpressure of the air separation column is prevented in the starting process, and the time for sending out the product oxygen and nitrogen is shortened from 4 hours to 1.5 hours; the argon gas delivery time was shortened from 24 hours to 5 hours.

Description

Method for quickly starting oxygenerator in cold state
Technical Field
The invention relates to an oxygen generator set, in particular to a method for quickly starting an oxygen generator in a cold state.
Background
The oxygenerator group is large-scale air separation plant, and oxygenerator group starts the initial stage at cold state, if it is too fast to go into the leading-in of tower air volume, will lead to the space to divide down the tower to step up too fast, at this moment, if do not open to go to tower throttle valve fast big aperture can directly cause down tower low temperature gas reflux to entry channel to it is below-15 ℃ to send this passageway temperature to reduce, and then leads to dividing the start failure. However, the rapid operation of the throttle valve can cause the pressure of the upper tower to rise rapidly, and each air flow in the double-plate heat exchanger is deflected, which seriously influences the starting safety of the air separation equipment.
Disclosure of Invention
The invention aims to solve the technical problem of providing a method for quickly starting an oxygen generator in a cold state, which can quickly ensure that oxygen, nitrogen and argon products are qualified.
In order to realize the purpose, the invention adopts the following technical scheme:
a method for quickly starting an oxygen generator in a cold state is controlled in a time division stage during starting and specifically comprises the following steps:
1) In the first stage of control, after the outlet pressure of an air compressor exceeds 0.42MPa, air is introduced to a lower tower of an air separation tower, and the pressure difference of the air before and after entering a main valve of the air separation tower is controlled to be below 20 KPa;
2) The second stage control, after the pressure of the air compressor is 0.46MPa, the supercharger is started; before the pressure of the air separation tower is increased to normal pressure, the low-temperature gas on the upper tower of the air separation tower is led out to the outside, the pressure on the upper tower of the air separation tower is increased to 20-26KPa, the pressure on the lower tower of the air separation tower is increased to 0.42-0.45MPa, an expansion machine is started, and 50-65% of the low-temperature gas in the air separation tower is controlled to flow to a high-pressure heat exchanger;
3) Controlling the third stage, namely increasing the pressure of a supercharger to normal working pressure, controlling the upper tower pressure of the air separation tower to be 40-50KPa, and sending liquid nitrogen into a pipe network after the oxygen content of liquid nitrogen in the lower tower of the air separation tower is lower than 10 ppm; when the oxygen purity in the air separation tower reaches more than 99.5 percent, high-pressure oxygen and medium-pressure oxygen are fed into a pipe network, the argon fraction reaches more than 88.5 percent, and the main cold liquid level reaches more than 20 percent, and an inlet valve of a crude argon tower is opened.
The first stage comprises the following specific steps:
(1) After the air compressor is started, slowly opening a bypass valve of air entering an air separation column after the outlet pressure of the air compressor exceeds 0.42MPa, guiding air to a lower column of the air separation column, fully opening a bleeding valve of a crude argon column after the front-back pressure difference of the air entering a main valve of the air separation column is less than 20KPa, adjusting the opening of the main valve of the air entering the air separation column to 55-60%, and guiding air to the lower column of the air separation column;
(2) After the cold box is put into interlocking, manually adjusting the opening of a pressure adjusting valve of a lower tower of the air separation tower to be 100%; the pressure of the lower tower of the air separation tower is kept to be not more than 0.46MPa and is automatically controlled;
the second stage comprises the following specific steps:
(1) After the air compressor is boosted to 0.46MPa, the booster is started, meanwhile, the opening of a high-pressure air regulating valve of a high-pressure heat exchanger, which enters and exits from an air separation column, is adjusted to be 5% -10%, the opening of a high-pressure air regulating valve of a secondary outlet of the booster is adjusted to be 5% -8%, the pressure of a lower column of the air separation column is lower than the pressure of an upper column of the air separation column, and the low-temperature gas of the lower column of the air separation column is forbidden to flow back to an inlet channel;
(2) The method comprises the steps that the opening degree of a liquid air throttling valve from a lower tower to an upper tower of an air separation tower is 40-50%, the opening degree of a waste liquid nitrogen throttling valve is 40-50%, the opening degree of a pure liquid nitrogen throttling valve is 40-50%, the opening degree of an oxygen-enriched liquid air throttling valve is 40-50%, gas is slowly introduced to the upper tower of the air separation tower, meanwhile, the opening degree of a regulating valve PV1626A for conveying waste nitrogen of a high-pressure heat exchanger to a nitrogen water tower is regulated to be 5-8%, the opening degree of a regulating valve FV1626 for conveying waste nitrogen of a low-pressure heat exchanger to the nitrogen water tower is regulated to be 15-20%, the opening degree of a nitrogen diffusing valve FV1502B of a low-pressure heat exchanger is regulated to be 30-40%, and low-temperature gas of the upper tower of the air separation tower is led out;
(3) The opening degree of a high-pressure air regulating valve of the high-pressure heat exchanger is adjusted to be 15-18%, the opening degree of a high-pressure air regulating valve of a secondary outlet of the supercharger is adjusted to be 20-23%, and the temperature of a waste nitrogen outlet of the high-pressure heat exchanger, the temperature of a waste nitrogen outlet of the low-pressure heat exchanger and the temperature of a low-pressure nitrogen outlet of the low-pressure heat exchanger are all above 15 ℃; controlling the temperature difference between the high-pressure air at the fourth-stage outlet of the supercharger and the low-pressure air at the second-stage outlet of the supercharger within 5 ℃;
(4) Starting an expansion machine after the upper tower pressure of the air separation tower is increased to 20-26KPa and the lower tower pressure of the air separation tower is increased to 0.42-0.45 MPa; the opening degree of a nozzle of the expansion machine is adjusted to be 80-85%, and a circulating valve of the expansion machine is closed to be 55-60%; meanwhile, the opening degree of an adjusting valve for adjusting the waste nitrogen of the high-pressure heat exchanger to the nitrogen water tower is adjusted to be 30-35%, and the opening degree of an adjusting valve for adjusting the waste nitrogen of the low-pressure heat exchanger to the nitrogen water tower is adjusted to be 20-25%;
(5) Then keeping the opening degree of the regulating valve from the waste nitrogen of the low-pressure heat exchanger to the nitrogen water tower unchanged, regulating the opening degree of the regulating valve from the waste nitrogen of the high-pressure heat exchanger to the nitrogen water tower, controlling 50-65% of low-temperature gas in the air separation tower to pass through the high-pressure heat exchanger, and keeping the inlet temperature of the expansion machine above-145 ℃;
(6) Starting a liquid oxygen pump and a liquid nitrogen pump, and adjusting the opening degrees of a high-pressure oxygen delivery valve, a low-pressure oxygen delivery valve and a high-pressure nitrogen delivery valve of the air separation tower to be not higher than 20%;
the third stage comprises the following specific control steps:
(1) After the liquid oxygen pump and the liquid nitrogen pump are started, the four-stage pressure of the booster is set to be 4.4-4.6MPa, and the pressure of the air compressor is set to be 0.45-0.48MPa; controlling the upper tower pressure of the air separation tower at 40-50kPa until the air quantity entering the air separation tower reaches 260000m 3 Entering an air separation purification stage at the time of/h;
(2) The liquid air throttle valve, the waste liquid nitrogen throttle valve, the pure liquid nitrogen throttle valve and the oxygen-enriched liquid air throttle valve from the lower tower to the upper tower of the air separation tower are adjusted to the opening degree before the last shutdown and are put into automatic control,
(3) If the temperature of the waste nitrogen outlet of the high-pressure heat exchanger, the temperature of the waste nitrogen outlet of the low-pressure heat exchanger and the temperatures of the secondary high-pressure air outlet and the low-pressure air outlet of the supercharger are reduced by more than 10 ℃, the opening of a high-pressure air regulating valve FV1535 of the secondary outlet of the supercharger is reduced by 1-3%, and if the temperature of the waste nitrogen outlet of the high-pressure heat exchanger, the temperature of the waste nitrogen outlet of the low-pressure heat exchanger, the temperature of the secondary high-pressure air outlet of the supercharger and the temperature of the low-pressure air outlet of the supercharger are increased by more than 10 ℃, the opening of the high-pressure air regulating valve FV1535 of the secondary outlet of the supercharger is increased by 1-3%;
(4) After detecting that the oxygen content of liquid nitrogen in the lower tower of the air separation tower is lower than 10ppm, sending the liquid nitrogen into a pipe network; when the oxygen purity in the air separation tower reaches more than 99.5 percent, sending high-pressure oxygen and medium-pressure oxygen into a pipe network;
(5) The argon fraction in the air separation column reaches over 88.5 percent, the main cold liquid level reaches over 20 percent, and an inlet valve of a crude argon column is opened;
(6) Controlling the circulation multiplying power of the crude argon column to be 2.50-2.55 and the setting value of the evaporation capacity of the oxygen-enriched liquid air to be 77000m 3 /h-78000m 3 /h。
Compared with the prior art, the invention has the beneficial effects that:
the starting method for increasing the pressure of the air compressor and the amount of air entering the tower by stages comprises the steps of sequentially opening the switch key valve and accurately controlling the opening degree of the valve, so that when the oxygen generating unit is started in a cold state, rectification can be quickly established, and the product is quickly qualified.
The overpressure of the air separation column is prevented in the starting process, and the time for sending out the product oxygen and nitrogen is shortened from 4 hours to 1.5 hours; the argon gas delivery time was shortened from 24 hours to 5 hours.
Drawings
FIG. 1 is a schematic diagram of an oxygen generating plant.
Detailed Description
The invention is further illustrated by the following examples:
the following examples describe the invention in detail. These examples are merely illustrative of the best embodiments of the present invention and do not limit the scope of the invention.
A method for quickly starting an oxygen generator in a cold state comprises the following steps: cooling the compressed air prepared by the air compressor by an air cooling tower; purifying by a molecular sieve to further remove water and impurities; pressurizing again by a supercharger, directly feeding a part of the pressurized gas into an air separation tower, and feeding a part of the pressurized gas into an expansion machine for expansion cooling and liquefaction; then the liquid and the gaseous air are rectified in an air separation column to finally prepare oxygen and nitrogen products which are sent into a product pipe network, and the argon prepared by the air separation column enters a crude argon column; carry out pressure control stage by stage to the air compressor when oxygenerator cold state, specifically include:
the first stage is as follows:
1) After the air compressor is started, when an outlet pressure gauge PIC7038 of the air compressor exceeds 0.42MPa, slowly opening a bypass valve HV1296B of air entering the air separation column, introducing air to the lower column of the air separation column, and after the front-back pressure difference of the air entering a main valve HV1296A of the air separation column is less than 20KPa, completely opening a bleeding valve HV1720 of the crude argon column, adjusting the opening of the air entering the main valve HV1296A of the air separation column to 55-60%, and introducing air to the lower column of the air separation column;
2) After the cold box is put into interlocking, manually adjusting the opening of a pressure adjusting valve PIC1602 of the lower tower of the air separation tower to be 100 percent; the pressure of the lower tower of the air separation tower is kept to be not more than 0.46MPa, and the lower tower is automatically controlled;
and a second stage:
1) When the pressure of an air compressor is increased to 0.42-0.46MPa, starting a supercharger, simultaneously adjusting the opening of a high-pressure air regulating valve FV1530B of an air separation tower entering and exiting the high-pressure heat exchanger to be 5% -10%, adjusting the opening of a high-pressure air regulating valve FV1535 of a secondary outlet of the supercharger to be 5% -8%, enabling the pressure of a lower tower of the air separation tower to be lower than the pressure of an upper tower of the air separation tower, and prohibiting low-temperature gas of the lower tower of the air separation tower from flowing back to an inlet channel;
2) Opening 40-50% of a liquid-air throttle valve FV1556, 40-50% of a waste liquid nitrogen throttle valve FV1557, 40-50% of a pure liquid nitrogen throttle valve FV1558 and 40-50% of an oxygen-enriched liquid air throttle valve LV1601 from a lower tower to an upper tower of the air separation tower, slowly guiding gas to the upper tower of the air separation tower, adjusting the opening degree of waste nitrogen of a high-pressure heat exchanger to an adjusting valve PV1626A of a nitrogen water tower to 5-8%, adjusting the opening degree of waste nitrogen of a low-pressure heat exchanger to an adjusting valve FV1626 of the nitrogen water tower to 15-20%, adjusting the opening degree of a nitrogen blow-off valve FV1502B of a low-pressure heat exchanger to 30-40%, and guiding low-temperature gas of the upper tower of the air separation tower to the outside;
3) The opening degree of a high-pressure air regulating valve FV1530B of the high-pressure heat exchanger is adjusted to be 15-18%, the opening degree of a high-pressure air regulating valve FV1535 at the secondary outlet of the supercharger is adjusted to be 20-23%, and the temperature of the waste nitrogen outlet of the high-pressure heat exchanger, the temperature of the waste nitrogen outlet of the low-pressure heat exchanger and the temperature of the low-pressure nitrogen outlet of the low-pressure heat exchanger are all above 15 ℃; controlling the temperature difference between the high-pressure air at the fourth-stage outlet of the supercharger and the low-pressure air at the second-stage outlet of the supercharger within 5 ℃;
4) Starting an expansion machine after the upper tower pressure of the air separation tower is increased to 20-26KPa and the lower tower pressure of the air separation tower is increased to 0.42-0.45 MPa; the opening degree of a nozzle of the expansion machine is adjusted to be 80-85%, and the opening degree of a circulating valve PV7408 of the expansion machine is closed to be 55-60%; meanwhile, the opening degree of a regulating valve PV1626A for regulating the waste nitrogen of the high-pressure heat exchanger to the nitrogen water tower is regulated to 30-35%, and the opening degree of a regulating valve FV1626 for regulating the waste nitrogen of the low-pressure heat exchanger to the nitrogen water tower is regulated to 20-25%;
5) Then keeping the opening degree of the waste nitrogen of the low-pressure heat exchanger to the regulating valve FV1626 of the nitrogen water tower unchanged, regulating the opening degree of the waste nitrogen of the high-pressure heat exchanger to the regulating valve PV1626A of the nitrogen water tower, controlling 50-65% of low-temperature gas in the air separation tower to pass through the high-pressure heat exchanger, and keeping the temperature of the inlet of the expansion machine above-145 ℃;
6) Starting a liquid oxygen pump and a liquid nitrogen pump, and adjusting the opening degrees of a high-pressure oxygen sending valve FV1511A, a low-pressure oxygen sending valve FV1510A and a high-pressure nitrogen sending valve FV1500A of the air separation column to be not higher than 20%;
and a third stage:
1) After the liquid oxygen pump and the liquid nitrogen pump are started, the four-stage pressure of the supercharger is set to be 4.4-4.6MPa, and the pressure of the air compressor is set to be 0.45-0.48MPa; controlling the upper tower pressure of the air separation tower at 40-50KPa until the air quantity entering the air separation tower reaches 260000m 3 Entering an air separation purification stage at the hour of the air separation purification stage;
2) A liquid-air throttle valve FV1556, a waste liquid nitrogen throttle valve FV1557, a pure liquid nitrogen throttle valve FV1558 and an oxygen-enriched liquid-air throttle valve LV1601 from the lower tower to the upper tower of the air separation tower are adjusted to open before the last shutdown and are put into automatic control,
3) If the temperature of the waste nitrogen outlet of the high-pressure heat exchanger, the temperature of the waste nitrogen outlet of the low-pressure heat exchanger and the temperatures of the secondary high-pressure air outlet and the low-pressure air outlet of the supercharger are reduced by more than 10 ℃, the opening of a high-pressure air regulating valve FV1535 of the secondary outlet of the supercharger is reduced by 1-3%, and if the temperature of the waste nitrogen outlet of the high-pressure heat exchanger, the temperature of the waste nitrogen outlet of the low-pressure heat exchanger, the temperature of the secondary high-pressure air outlet of the supercharger and the temperature of the low-pressure air outlet of the supercharger are increased by more than 10 ℃, the opening of the high-pressure air regulating valve FV1535 of the secondary outlet of the supercharger is increased by 1-3%;
4) After detecting that the oxygen content of liquid nitrogen in the lower tower of the air separation tower is lower than 10ppm, sending the liquid nitrogen into a pipe network; when the oxygen purity in the air separation tower reaches more than 99.5 percent, sending high-pressure oxygen and medium-pressure oxygen into a pipe network;
5) The argon fraction in the air separation column reaches over 88.5 percent, the main cold liquid level reaches over 20 percent, and an inlet valve of a crude argon column is opened;
6) Controlling the circulation multiplying power of the crude argon column to be 2.50-2.55, opening a regulating valve FIC1712 of the crude argon column to have the opening degree of 65-70 percent, and setting the evaporation capacity of the oxygen-enriched liquid air to be 77000m 3 /h-78000m 3 /h。

Claims (4)

1. A method for rapidly starting an oxygen generator in a cold state is characterized by comprising the following steps of starting time division stage control:
1) In the first stage of control, after the outlet pressure of an air compressor exceeds 0.42MPa, air is introduced to a lower tower of an air separation tower, and the pressure difference of the air before and after entering a main valve of the air separation tower is controlled to be below 20 KPa;
2) The second stage control, after the pressure of the air compressor is 0.46MPa, the supercharger is started; before the pressure of the air separation tower is increased to normal pressure, externally leading out low-temperature gas of an upper tower of the air separation tower, increasing the pressure of the upper tower of the air separation tower to 20-26KPa, and increasing the pressure of a lower tower of the air separation tower to 0.42-0.45MPa, starting an expansion machine, and controlling 50-65% of low-temperature gas in the air separation tower to flow to a high-pressure heat exchanger;
3) Controlling the third stage, namely increasing the pressure of a supercharger to normal working pressure, controlling the upper tower pressure of the air separation tower to be 40-50KPa, and sending liquid nitrogen into a pipe network after the oxygen content of liquid nitrogen in the lower tower of the air separation tower is lower than 10 ppm; when the oxygen purity in the air separation tower reaches more than 99.5 percent, high-pressure oxygen and medium-pressure oxygen are fed into a pipe network, the argon fraction reaches more than 88.5 percent, and the main cold liquid level reaches more than 20 percent, and an inlet valve of a crude argon tower is opened.
2. The method for rapidly starting the oxygen generator in the cold state as claimed in claim 1, wherein the first stage control comprises the following specific steps:
(1) After the air compressor is started, slowly opening a bypass valve of air entering an air separation column after the outlet pressure of the air compressor exceeds 0.42MPa, guiding air to a lower column of the air separation column, fully opening a bleeding valve of a crude argon column after the front-back pressure difference of the air entering a main valve of the air separation column is less than 20KPa, adjusting the opening of the main valve of the air entering the air separation column to 55-60%, and guiding air to the lower column of the air separation column;
(2) After the cold box is put into interlocking, manually adjusting the opening of a pressure adjusting valve of a lower tower of the air separation tower to be 100%; the pressure of the lower tower of the air separation tower is kept to be not more than 0.46MPa and is automatically controlled.
3. The method for rapidly starting the oxygen generator in the cold state as claimed in claim 1, wherein the second stage control specific steps are as follows:
(1) After the pressure of an air compressor is increased to 0.46MPa, starting a booster, simultaneously adjusting the opening of a high-pressure air regulating valve of a high-pressure heat exchanger, which enters and exits from an air separation tower, to 5-10%, adjusting the opening of a high-pressure air regulating valve of a secondary outlet of the booster to 5-8%, enabling the pressure of a lower tower of the air separation tower to be lower than the pressure of an upper tower of the air separation tower, and forbidding low-temperature gas of the lower tower of the air separation tower to flow back to an inlet channel;
(2) The opening degree of a liquid air throttling valve from a lower tower to an upper tower of the air separation tower is 40-50%, the opening degree of a waste liquid nitrogen throttling valve is 40-50%, the opening degree of a pure liquid nitrogen throttling valve is 40-50%, the opening degree of an oxygen-enriched liquid air throttling valve is 40-50%, air is slowly led to the upper tower of the air separation tower, meanwhile, the opening degree of a regulating valve PV1626A for leading waste nitrogen of a high-pressure heat exchanger to a nitrogen water tower is adjusted to be 5-8%, the opening degree of a regulating valve FV1626 for leading waste nitrogen of a low-pressure heat exchanger to the nitrogen water tower is adjusted to be 15-20%, the opening degree of a nitrogen diffusing valve FV1502B for leading the nitrogen of a low-pressure heat exchanger is adjusted to be 30-40%, and low-temperature gas of the upper tower of the air separation tower is led out;
(3) The opening degree of a high-pressure air regulating valve of the high-pressure heat exchanger is adjusted to be 15-18%, the opening degree of a high-pressure air regulating valve at a secondary outlet of the supercharger is adjusted to be 20-23%, and the temperature of a waste nitrogen outlet of the high-pressure heat exchanger, the temperature of a waste nitrogen outlet of the low-pressure heat exchanger and the temperature of a low-pressure nitrogen outlet of the low-pressure heat exchanger are all above 15 ℃; controlling the temperature difference between the high-pressure air at the fourth-stage outlet of the supercharger and the low-pressure air at the second-stage outlet of the supercharger within 5 ℃;
(4) Starting an expansion machine after the upper tower pressure of the air separation tower is increased to 20-26KPa and the lower tower pressure of the air separation tower is increased to 0.42-0.45 MPa; the opening degree of a nozzle of the expansion machine is adjusted to be 80-85%, and a circulating valve of the expansion machine is closed to be 55-60%; meanwhile, the opening degree of an adjusting valve for adjusting the waste nitrogen of the high-pressure heat exchanger to the nitrogen water tower is adjusted to be 30-35%, and the opening degree of an adjusting valve for adjusting the waste nitrogen of the low-pressure heat exchanger to the nitrogen water tower is adjusted to be 20-25%;
(5) Then keeping the opening degree of the regulating valve from the waste nitrogen of the low-pressure heat exchanger to the nitrogen water tower unchanged, regulating the opening degree of the regulating valve from the waste nitrogen of the high-pressure heat exchanger to the nitrogen water tower, controlling 50-65% of low-temperature gas in the air separation tower to pass through the high-pressure heat exchanger, and keeping the inlet temperature of the expansion machine above-145 ℃;
(6) And starting the liquid oxygen pump and the liquid nitrogen pump, and adjusting the opening degrees of a high-pressure oxygen delivery valve, a low-pressure oxygen delivery valve and a high-pressure nitrogen delivery valve of the air separation column to be not higher than 20%.
4. The method for rapidly starting the cold state of the oxygen generator as claimed in claim 1, wherein the third stage controls the specific steps of:
(1) After the liquid oxygen pump and the liquid nitrogen pump are started, the four-stage pressure of the booster is set to be 4.4-4.6MPa, and the pressure of the air compressor is set to be 0.45-0.48MPa; the upper tower pressure of the air separation tower is controlled to be 40-50kPa, and the air quantity entering the air separation tower reaches 260000m 3 Entering an air separation purification stage at the hour of the air separation purification stage;
(2) The liquid air throttle valve, the waste liquid nitrogen throttle valve, the pure liquid nitrogen throttle valve and the oxygen-enriched liquid air throttle valve from the lower tower to the upper tower of the air separation tower are adjusted to the opening degree before the last shutdown and are put into automatic control,
(3) If the temperature of the waste nitrogen outlet of the high-pressure heat exchanger, the temperature of the waste nitrogen outlet of the low-pressure heat exchanger and the temperature of the secondary high-pressure air outlet and the low-pressure air outlet of the supercharger are reduced by more than 10 ℃, closing the opening of a high-pressure air regulating valve FV1535 at the secondary outlet of the supercharger by 1-3 percent, and if the temperature of the waste nitrogen outlet of the high-pressure heat exchanger, the temperature of the waste nitrogen outlet of the low-pressure heat exchanger, the temperature of the secondary high-pressure air outlet of the supercharger and the temperature of the low-pressure air outlet are increased by more than 10 ℃, opening the high-pressure air regulating valve FV1535 at the secondary outlet of the supercharger by 1-3 percent;
(4) After detecting that the oxygen content of liquid nitrogen in the lower tower of the air separation tower is lower than 10ppm, sending the liquid nitrogen into a pipe network; when the oxygen purity in the air separation tower reaches more than 99.5 percent, sending high-pressure oxygen and medium-pressure oxygen into a pipe network;
(5) The argon fraction in the air separation column reaches over 88.5 percent, the main cold liquid level reaches over 20 percent, and an inlet valve of the crude argon column is opened;
(6) Controlling the circulation multiplying power of the crude argon tower to be 2.50-2.55 and setting the evaporation capacity of the oxygen-enriched liquid air to be 77000m 3 /h-78000m 3 /h。
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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH03199882A (en) * 1989-12-27 1991-08-30 Fuji Electric Co Ltd Operation of plant including air liquefying and separating device
CN101684982A (en) * 2008-09-28 2010-03-31 鞍钢股份有限公司 Thermal-state starting method of air separation equipment
CN109186179A (en) * 2018-09-30 2019-01-11 苏州制氧机股份有限公司 Full distillation proposes the oxygen-enriched air separation unit of argon and technique
WO2019127343A1 (en) * 2017-12-29 2019-07-04 乔治洛德方法研究和开发液化空气有限公司 Method and device for producing air product based on cryogenic rectification
CN112984955A (en) * 2021-03-15 2021-06-18 鞍钢股份有限公司 Starting method of plate-fin heat exchanger of air separation equipment

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH03199882A (en) * 1989-12-27 1991-08-30 Fuji Electric Co Ltd Operation of plant including air liquefying and separating device
CN101684982A (en) * 2008-09-28 2010-03-31 鞍钢股份有限公司 Thermal-state starting method of air separation equipment
WO2019127343A1 (en) * 2017-12-29 2019-07-04 乔治洛德方法研究和开发液化空气有限公司 Method and device for producing air product based on cryogenic rectification
CN109186179A (en) * 2018-09-30 2019-01-11 苏州制氧机股份有限公司 Full distillation proposes the oxygen-enriched air separation unit of argon and technique
CN112984955A (en) * 2021-03-15 2021-06-18 鞍钢股份有限公司 Starting method of plate-fin heat exchanger of air separation equipment

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