CN215412752U - Double-tower low-temperature rectification high-purity nitrogen preparation device - Google Patents
Double-tower low-temperature rectification high-purity nitrogen preparation device Download PDFInfo
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- CN215412752U CN215412752U CN202121233261.XU CN202121233261U CN215412752U CN 215412752 U CN215412752 U CN 215412752U CN 202121233261 U CN202121233261 U CN 202121233261U CN 215412752 U CN215412752 U CN 215412752U
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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
- F25J3/04406—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
- F25J3/0443—A main column system not otherwise provided, e.g. a modified double column flowsheet
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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
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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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
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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 utility model belongs to the technical field of air separation, and discloses a device for preparing high-purity nitrogen by double-tower low-temperature rectification, which comprises a main heat exchanger, a subcooler, a nitrogen tower, a first condensation evaporator, an oxygen tower, a turbo expander and a second condensation evaporator; the air outlet of the main heat exchanger is communicated with the air inlet at the lower part of the nitrogen tower through a pipeline; a high-purity nitrogen outlet at the top of the nitrogen tower is respectively connected with high-purity nitrogen inlets of the main heat exchanger, the first condensation evaporator and the second condensation evaporator through pipelines; an oxygen-enriched waste gas outlet at the top of the first condensation evaporator is sequentially communicated with an oxygen-enriched waste gas inlet of the subcooler and the main heat exchanger through pipelines, and an oxygen-enriched liquid air outlet at the bottom of the first condensation evaporator is communicated with an oxygen-enriched liquid air inlet at the upper part of the oxygen tower through a pipeline; and a waste nitrogen outlet at the top of the oxygen tower is communicated with the subcooler and a waste nitrogen inlet of the main heat exchanger in sequence through pipelines. The utility model sets the oxygen tower process, not only can generate high-purity nitrogen with the purity of not less than 99.999 percent, but also can produce oxygen or liquid oxygen products with the purity of 99.6 percent.
Description
Technical Field
The utility model belongs to the technical field of air separation, and particularly relates to a device for preparing high-purity nitrogen by double-tower cryogenic rectification.
Background
As an important chemical raw material, nitrogen is widely applied to the fields of smelting, chemical fertilizers, coal chemical industry and the like. According to different processes, nitrogen with different purities is needed, and in combination with the requirements of users on the pressure and the gas quantity of the nitrogen, oxygen has certain economic value as a byproduct. The current high-purity nitrogen device produces high-purity nitrogen gas, and meanwhile, a byproduct is low-purity oxygen-enriched gas. In general, because the oxygen-containing purity of the part of gas is only about 36%, the utilization value is not large, the part of oxygen-rich gas is generally discharged as waste gas after being discharged from a cooling box, and energy waste is caused. In order to meet the requirement on low-purity oxygen and avoid resource waste, research and development of a device capable of avoiding the waste of low-concentration oxygen in the production process of high-purity nitrogen and preparing low-concentration oxygen are urgently needed.
Disclosure of Invention
The utility model aims to provide a device for preparing high-purity nitrogen by double-tower cryogenic rectification, which can not only produce high-purity nitrogen with the purity of not less than 99.999 percent, but also produce oxygen or liquid oxygen products with the purity of 99.6 percent.
In order to achieve the purpose, the utility model adopts the following technical scheme:
a double-tower low-temperature rectification high-purity nitrogen preparation device comprises a main heat exchanger, a subcooler, a nitrogen tower, a first condensation evaporator, an oxygen tower, a turbo expander and a second condensation evaporator, wherein the first condensation evaporator is arranged at the upper part of the nitrogen tower, and the second condensation evaporator is arranged at the lower part of the oxygen tower; the air inlet of the main heat exchanger is an inlet for filtered, purified and cooled air, and the air outlet of the main heat exchanger is communicated with the air inlet at the lower part of the nitrogen tower through a pipeline; a high-purity nitrogen outlet at the top of the nitrogen tower is respectively connected with high-purity nitrogen inlets of the main heat exchanger, the first condensation evaporator and the second condensation evaporator through pipelines, a liquid air outlet at the bottom of the nitrogen tower is communicated with a liquid air inlet of the subcooler, and the liquid air outlet of the subcooler is communicated with the liquid air inlet of the first condensation evaporator through a pipeline; an oxygen-enriched waste gas outlet at the top of the first condensation evaporator is sequentially communicated with an oxygen-enriched waste gas inlet of the subcooler and an oxygen-enriched waste gas inlet of the main heat exchanger through pipelines, an oxygen-enriched waste gas outlet of the main heat exchanger is communicated with an oxygen-enriched waste gas inlet of the turboexpander through a pipeline, an expanded oxygen-enriched waste gas outlet of the turboexpander is communicated with an expanded oxygen-enriched waste gas inlet of the subcooler through a pipeline, an expanded oxygen-enriched waste gas outlet of the subcooler is communicated with an oxygen-enriched waste gas inlet of the main heat exchanger through a pipeline, and an oxygen-enriched liquid air outlet at the bottom of the first condensation evaporator is communicated with an oxygen-enriched liquid air inlet at the upper part of the oxygen tower through a pipeline; a waste nitrogen outlet at the top of the oxygen tower is sequentially communicated with a waste nitrogen inlet of the subcooler and the main heat exchanger through pipelines, an oxygen outlet at the lower part of the oxygen tower is communicated with an oxygen inlet of the main heat exchanger through a pipeline, and a liquid oxygen outlet at the bottom of the oxygen tower is connected with a liquid oxygen storage tank through a pipeline; and a liquid nitrogen outlet of the second condensation evaporator is connected with a liquid nitrogen storage tank through a pipeline.
Preferably, the nitrogen column and the oxygen column are both packed columns.
Preferably, a nitrogen outlet at the bottom of the first condensing evaporator is connected with a reflux liquid inlet at the upper part of the nitrogen tower through a pipeline.
Preferably, the liquid-air outlet at the lower part of the nitrogen tower is sequentially connected with the liquid-air inlet of the subcooler and the liquid-air inlet at the upper part of the nitrogen tower 3 through pipelines.
Preferably, the liquid nitrogen outlet of the second condensing evaporator is also connected with a liquid nitrogen inlet at the upper part of the nitrogen tower through a pipeline.
Compared with the prior art, the utility model has the beneficial effects that:
the device provided by the utility model is provided with an oxygen tower process, so that high-purity nitrogen with the purity not lower than 99.999% can be generated, and oxygen or liquid oxygen products with the purity of 99.6% can be produced; the nitrogen tower and the oxygen tower in the whole device both adopt regular packing towers, the total investment increase is limited, but the pressure discharge of the air compressor can be reduced to 0.48MPa, the pressure of the nitrogen product is increased to 0.43MPa, the energy consumption of the air compressor and the nitrogen compressor is greatly reduced, and the operation elasticity of the nitrogen product can be adjusted to 50-110%.
Drawings
FIG. 1 is a schematic structural diagram of a device for preparing high-purity nitrogen by double-tower low-temperature rectification.
In the drawings, the reference numbers: the system comprises a main heat exchanger 1, a subcooler 2, a nitrogen tower 3, a first condensing evaporator 4, an oxygen tower 5, a turboexpander 6 and a second condensing evaporator 7.
Detailed Description
The following examples are intended to illustrate the utility model, but are not intended to limit the scope of the utility model.
As shown in fig. 1, a double-tower low-temperature rectification high-purity nitrogen preparation device comprises a main heat exchanger 1, a subcooler 2, a nitrogen tower 3, a first condensation evaporator 4, an oxygen tower 5, a turbo expander 6 and a second condensation evaporator 7, wherein the first condensation evaporator 4 is arranged at the upper part of the nitrogen tower 3, and the second condensation evaporator 7 is arranged at the lower part of the oxygen tower 5; the air inlet of the main heat exchanger 1 is an inlet for filtered, purified and cooled air, and the air outlet of the main heat exchanger 1 is communicated with the air inlet at the lower part of the nitrogen tower 3 through a pipeline; a high-purity nitrogen outlet at the top of the nitrogen tower 3 is respectively connected with high-purity nitrogen inlets of the main heat exchanger 1, the first condensation evaporator 4 and the second condensation evaporator 7 through pipelines, a liquid air outlet at the bottom of the nitrogen tower 3 is communicated with a liquid air inlet of the subcooler 2, and a liquid air outlet of the subcooler 2 is communicated with a liquid air inlet of the first condensation evaporator 4 through a pipeline; an oxygen-enriched waste gas outlet at the top of the first condensation evaporator 4 is sequentially communicated with an oxygen-enriched waste gas inlet of the subcooler 2 and an oxygen-enriched waste gas inlet of the main heat exchanger 1 through a pipeline, an oxygen-enriched waste gas outlet of the main heat exchanger 1 is communicated with an oxygen-enriched waste gas inlet of the turbo expander 6 through a pipeline, an expanded oxygen-enriched waste gas outlet of the turbo expander 6 is communicated with an expanded oxygen-enriched waste gas inlet of the subcooler 2 through a pipeline, an expanded oxygen-enriched waste gas outlet of the subcooler 2 is communicated with an oxygen-enriched waste gas inlet of the main heat exchanger 1 through a pipeline, and an oxygen-enriched liquid air outlet at the bottom of the first condensation evaporator 4 is communicated with an oxygen-enriched liquid air inlet at the upper part of the oxygen tower 5 through a pipeline; a waste nitrogen outlet at the top of the oxygen tower 5 is sequentially communicated with the subcooler 2 and a waste nitrogen inlet of the main heat exchanger 1 through pipelines, an oxygen outlet at the lower part of the oxygen tower 5 is communicated with an oxygen inlet of the main heat exchanger 1 through a pipeline, and a liquid oxygen outlet at the bottom of the oxygen tower 5 is connected with a liquid oxygen storage tank through a pipeline; and a liquid nitrogen outlet of the second condensation evaporator 7 is connected with a liquid nitrogen storage tank through a pipeline.
In the present embodiment, both the nitrogen column 3 and the oxygen column 5 are packed columns.
In a preferred embodiment, the nitrogen outlet at the bottom of the first condenser-evaporator 4 of the present invention is connected to the reflux inlet at the upper part of the nitrogen column 3 through a pipe.
In a preferred embodiment, the liquid air outlet at the lower part of the nitrogen tower 3 of the present invention is connected to the liquid air inlet of the subcooler 2 and the liquid air inlet at the upper part of the nitrogen tower 3 in this order through pipes.
As a preferred embodiment, the liquid nitrogen outlet of the second condensing evaporator 7 of the present invention is further connected to the liquid nitrogen inlet of the upper portion of the nitrogen column 3 through a pipe.
The utility model adopts a cryogenic separation method, purified compressed air (0.48 MPa) enters a fractionating tower, exchanges heat with return low-temperature waste gas and product nitrogen through a main heat exchanger 1, is cooled to-174 ℃, enters the bottom of a nitrogen tower 3, and is separated into product nitrogen with the purity of 99.999 percent and liquid air with the oxygen content of 38.1 percent through rectification. Liquid air with the oxygen content of 38.1% at the bottom of the nitrogen tower 3 passes through the cooler 2 and then enters the first condensation evaporator 4 to perform phase change heat exchange with high-purity nitrogen from the top of the nitrogen tower 3, the liquid air is evaporated into waste gas, oxygen-enriched liquid air with the oxygen content of 54.5% generated at the bottom of the first condensation evaporator 4 enters the upper part of the oxygen tower 3, and the nitrogen is condensed and then used as reflux liquid of the nitrogen tower 3. And part of 99.999 percent high-purity nitrogen from the top of the nitrogen tower 3 is used as a heat evaporation source of the oxygen tower 3, is liquefied into a liquid nitrogen product and is sent out, and the other part of the liquid nitrogen enters the main heat exchanger 1 to be reheated to the normal temperature and is sent out as the nitrogen product. The waste gas is led out from the top of the first condensation evaporator 4, reheated by the cooler 2 and then sent to the turbine expander 6 for expansion, the cooling capacity of the device is supplemented, the expanded waste gas is reheated to normal temperature by the cooler 2 and the main heat exchanger 1 and then output, part of the expanded waste gas is used as regeneration gas of a purification system, and the rest of the expanded waste gas is sent to a water cooling tower. Oxygen-enriched liquid air with the oxygen content of 54.5% enters the upper part of an oxygen tower 5 from the bottom of a first condensation evaporator 4 through a subcooler 2 in a cold throttling mode, dirty nitrogen is obtained at the top of the oxygen tower 5 through rectification and separation, and the dirty nitrogen is reheated to normal temperature through the subcooler 2 and a main heat exchanger 1 and then is output to serve as cold source gas of a water cooling tower; oxygen with the purity of 99.6 percent and product liquid oxygen are respectively obtained at the lower part and the bottom of the oxygen tower 5, and the oxygen is reheated and output through the main converter 1.
Compared with other processes for preparing high-purity nitrogen, the utility model has the following advantages:
1) the nitrogen tower and the oxygen tower in the device both adopt regular packing towers, the total investment is increased limitedly, but the pressure discharge of the air compressor can be reduced to 0.48MPa, the pressure of the nitrogen product is increased to 0.43MPa, the energy consumption of the air compressor and the nitrogen compressor is greatly reduced, and meanwhile, the operation elasticity of 50-110% of the nitrogen product can be adjusted.
2) The device is provided with an oxygen tower process, so that high-purity nitrogen with the purity not lower than 99.999 percent can be generated, and oxygen or liquid oxygen products with the purity of 99.6 percent can also be produced.
The above-mentioned embodiments are merely preferred embodiments of the present invention, which are merely illustrative and not restrictive, and it should be understood that other embodiments may be easily made by those skilled in the art by replacing or changing the technical contents disclosed in the specification, and therefore, all changes and modifications that are made on the principle of the present invention should be included in the scope of the claims of the present invention.
Claims (5)
1. A double-tower low-temperature rectification high-purity nitrogen preparation device comprises a main heat exchanger (1), a subcooler (2), a nitrogen tower (3), a first condensation evaporator (4), an oxygen tower (5), a turboexpander (6) and a second condensation evaporator (7), and is characterized in that the first condensation evaporator (4) is arranged at the upper part of the nitrogen tower (3), and the second condensation evaporator (7) is arranged at the lower part of the oxygen tower (5); the air inlet of the main heat exchanger (1) is an inlet for filtered, purified and cooled air, and the air outlet of the main heat exchanger (1) is communicated with the air inlet at the lower part of the nitrogen tower (3) through a pipeline; a high-purity nitrogen outlet at the top of the nitrogen tower (3) is respectively connected with high-purity nitrogen inlets of the main heat exchanger (1), the first condensation evaporator (4) and the second condensation evaporator (7) through pipelines, a liquid air outlet at the bottom of the nitrogen tower (3) is communicated with a liquid air inlet of the subcooler (2), and a liquid air outlet of the subcooler (2) is communicated with a liquid air inlet of the first condensation evaporator (4) through a pipeline; an oxygen-enriched waste gas outlet at the top of the first condensation evaporator (4) is sequentially communicated with an oxygen-enriched waste gas inlet of the subcooler (2) and an oxygen-enriched waste gas inlet of the main heat exchanger (1) through pipelines, an oxygen-enriched waste gas outlet of the main heat exchanger (1) is communicated with an oxygen-enriched waste gas inlet of the turboexpander (6) through a pipeline, an expanded oxygen-enriched waste gas outlet of the turboexpander (6) is communicated with an expanded oxygen-enriched waste gas inlet of the subcooler (2), an expanded oxygen-enriched waste gas outlet of the subcooler (2) is communicated with an oxygen-enriched waste gas inlet of the main heat exchanger (1) through a pipeline, and an oxygen-enriched liquid air outlet at the bottom of the first condensation evaporator (4) is communicated with an oxygen-enriched liquid air inlet at the upper part of the oxygen tower (5) through a pipeline; a waste nitrogen outlet at the top of the oxygen tower (5) is sequentially communicated with the subcooler (2) and a waste nitrogen inlet of the main heat exchanger (1) through pipelines, an oxygen outlet at the lower part of the oxygen tower (5) is communicated with an oxygen inlet of the main heat exchanger (1) through a pipeline, and a liquid oxygen outlet at the bottom of the oxygen tower (5) is connected with a liquid oxygen storage tank through a pipeline; and a liquid nitrogen outlet of the second condensation evaporator (7) is connected with a liquid nitrogen storage tank through a pipeline.
2. The apparatus for producing high-purity nitrogen by double-column cryogenic rectification as claimed in claim 1, wherein the nitrogen column (3) and the oxygen column (5) are both packed columns.
3. The double-tower cryogenic rectification high-purity nitrogen gas production device as claimed in claim 1, characterized in that a nitrogen gas outlet at the bottom of the first condensing evaporator (4) is connected with a reflux liquid inlet at the upper part of the nitrogen tower (3) through a pipeline.
4. The double-tower cryogenic rectification high-purity nitrogen gas production device as claimed in claim 1, wherein a liquid air outlet at the lower part of the nitrogen tower (3) is connected with a liquid air inlet of the subcooler (2) and a liquid air inlet at the upper part of the nitrogen tower (3) in sequence through pipelines.
5. The apparatus for producing high-purity nitrogen by double column cryogenic rectification as claimed in claim 1, wherein the liquid nitrogen outlet of the second condensing evaporator (7) is further connected to the liquid nitrogen inlet at the upper part of the nitrogen column (3) through a pipeline.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202121233261.XU CN215412752U (en) | 2021-06-03 | 2021-06-03 | Double-tower low-temperature rectification high-purity nitrogen preparation device |
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| CN202121233261.XU CN215412752U (en) | 2021-06-03 | 2021-06-03 | Double-tower low-temperature rectification high-purity nitrogen preparation device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114413570A (en) * | 2022-01-19 | 2022-04-29 | 四川空分设备(集团)有限责任公司 | Double-tower floor type nitrogen making device |
| CN114413569A (en) * | 2022-01-19 | 2022-04-29 | 四川空分设备(集团)有限责任公司 | Double-tower nitrogen production device and method |
-
2021
- 2021-06-03 CN CN202121233261.XU patent/CN215412752U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114413570A (en) * | 2022-01-19 | 2022-04-29 | 四川空分设备(集团)有限责任公司 | Double-tower floor type nitrogen making device |
| CN114413569A (en) * | 2022-01-19 | 2022-04-29 | 四川空分设备(集团)有限责任公司 | Double-tower nitrogen production device and method |
| CN114413570B (en) * | 2022-01-19 | 2023-01-31 | 四川空分设备(集团)有限责任公司 | Double-tower floor type nitrogen making device |
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