A float glass decompression nitrogen making device

Abstract

The utility model discloses a kind of float glass pressure reduction nitrogen production devices, it includes filter, the filter connects centrifugal compressor, centrifugal compressor connects pre-cooler, pre-cooler connects adsorption tower;The outlet of adsorption tower has two branches, one branch is connected main heat exchanger, then enters lower tower;The second branch of adsorption tower outlet connects expander;Expander enters upper tower bottom by connecting pipe;Upper tower is equipped with dirty nitrogen liquid level regulating valve V2 on the pipeline to subcooler;Subcooler is equipped with liquid nitrogen throttling into upper tower regulating valve V3 on the pipeline to upper tower;Liquid nitrogen storage tank is equipped with liquid nitrogen extraction valve V4.The utility model is conducive to the case that the set pressure of centrifugal compressor is adjusted, keeps the nitrogen gas flow unchanged.Can reduce power consumption.

Description

Technical Field

[0001] This utility model relates to a float glass decompression nitrogen generation device. Background Technology

[0002] Air separation towers are the mainstream equipment for modern nitrogen production. Among them, the KDN-9000 nitrogen production system currently used by glass companies requires compressed air at a pressure of 0.75MPa. The accompanying centrifuge operates under high load, and there is no room for adjustment when higher nitrogen flow rates are needed. The centrifuge also suffers from significant power consumption. Utility Model Content

[0003] The main objective of this invention is to provide a float glass depressurization nitrogen generation device.

[0004] The technical solution adopted by this utility model to solve its technical problem is:

[0005] A float glass vacuum nitrogen generation device includes a filter. Air filtered by the filter enters a centrifugal compressor. The outlet of the centrifugal compressor is connected to a precooler, and the outlet of the precooler is connected to an adsorption tower. The outlet of the adsorption tower has two branches, one of which enters a main heat exchanger through a connecting pipe L1. Air after heat exchange in the main heat exchanger enters a lower tower. The outlet of the lower tower is connected to a subcooler. The subcooler has multiple outlets, one of which enters an upper tower. In the upper tower, the airflow rises sequentially through trays or packing, while the liquid flows back downwards sequentially.

[0006] The second branch from the adsorption tower outlet enters the expander through connecting pipe L2; the air from the expander enters the bottom of the upper tower through connecting pipe as rising gas (participating in the rectification of the upper tower); the oxygen-enriched liquid air at the bottom of the lower tower enters the middle of the upper tower (participating in the rectification of the upper tower); after the nitrogen at the top of the lower tower is condensed into liquid nitrogen, part of it is used as the reflux liquid of the lower tower, part of it is sent to the top of the upper tower as reflux liquid after being subcooled by the cooler, and a small part is extracted as liquid nitrogen product and sent to the storage tank.

[0007] The pipeline from the upper tower to the subcooler is equipped with a sludge nitrogen liquid air level regulating valve V2; the pipeline from the subcooler to the upper tower is equipped with a liquid nitrogen throttling regulating valve V3; the liquid nitrogen storage tank is equipped with a liquid nitrogen extraction valve V4; the lower tower is equipped with a lower tower liquid nitrogen reflux valve V11; the connecting pipeline L1 has a size of DN300.

[0008] Furthermore, the adsorption tower includes a first adsorption tower and a second adsorption tower, which are arranged in parallel.

[0009] Furthermore, the expander includes a first expander and a second expander, which are connected in parallel.

[0010] Furthermore, the waste nitrogen gas is sent from the upper column through pipelines to the subcooler and main heat exchanger for reheating before being sent to the fractionation column. A portion of it is used as regeneration gas for the purification system and is sent through pipeline L3 to the heater to regenerate the adsorption column. Another small portion is used as sealing gas for the cold box, and the remaining waste nitrogen gas is vented.

[0011] Compared with the prior art, this technical solution has the following advantages:

[0012] This invention, through various design modifications and by upgrading the connecting pipe from the existing DN250 to DN300, allows for consistent nitrogen flow rate production by adjusting V2, V3, and V4 parameters while regulating the centrifugal compressor's set pressure. This reduces power consumption. This invention meets the needs of the glass industry for higher nitrogen flow rates. Attached Figure Description

[0013] The present invention will be further described below with reference to the accompanying drawings and embodiments.

[0014] Figure 1 This is a schematic diagram of a float glass depressurization nitrogen generation device according to a preferred embodiment.

[0015] In the picture

[0016] 1-Filter 2-Centrifugal Compressor 2-1 Centrifugal Compressor Cooler 3-Precooler 3-1 Precooler Cooler 3-2 Precooler Oil-Water Separator 4-First Adsorption Tower 5-Second Adsorption Tower 6-First Heater 7-Second Heater 8-First Expander 9-Second Expander 10-Main Heat Exchanger 11-Lower Tower 12-Upper Tower 13-Subcooler 14-Liquid Nitrogen Metering Cylinder

[0017] V1, V2, V3, V4, V11, V12, V101, and V102 are all valves.

[0018] L1 to L5 are all connecting pipes. Detailed Implementation

[0019] Please refer to Figure 1 A float glass vacuum nitrogen generation device includes a filter 1, a centrifugal compressor 2, a precooler 3, a first adsorption tower 4, a second adsorption tower 5, a first heater 6, a second heater 7, a first expander 8, a second expander 9, a main heat exchanger 10, a lower tower 11, an upper tower 12, and a subcooler 13.

[0020] Filter 1 is used to filter the air and remove dust and other impurities. The filtered air is then sent to centrifugal compressor 2, which has a centrifugal cooler 2-1. Centrifugal compressor 2 pre-compresses the air. Since the air generates heat when compressed, a cooler is needed to cool it.

[0021] The compressed air enters the precooler 3 for preliminary cooling. The precooler 3 includes a precooler cooler 3-1 and a precooler oil-water separator 3-2. The air undergoes preliminary cooling in the precooler 3, which reduces the water content in the compressed air. This pre-drying and cooling of the compressed air reduces the workload of the molecular sieve adsorber, further improves the working efficiency of the molecular sieve adsorber, and prevents moisture from entering the fractionation tower.

[0022] Pre-cooled air enters the first adsorption tower 4 and the second adsorption tower 5. The first adsorption tower 4 and the second adsorption tower 5 are connected in parallel. The first adsorption tower 4 and the second adsorption tower 5 are used to adsorb moisture, carbon dioxide, and hydrocarbons such as acetylene from the air, fixing gaseous and liquid substances in the air onto the surface of the adsorbent, thereby obtaining pure air. This process is a reversible physical reaction; during adsorption, the pressure must be raised to its maximum and the temperature lowered to its minimum. During desorption, the pressure must be lowered to its minimum and the temperature raised to its maximum.

[0023] The air exiting the first adsorption tower 4 and the second adsorption tower 5 has two branches. One branch enters the main heat exchanger 10 through the connecting pipe L1. In the main heat exchanger 10, the return nitrogen and waste nitrogen are reheated to room temperature, while the compressed air is cooled and liquefied. In this process, the energy exchange within the system is fully utilized.

[0024] After heat exchange in the main heat exchanger 8, the air enters the lower column 11. The air in the lower column 11 then enters the subcooler 13, which has multiple outlets, one of which enters the upper column 12. The distillation reaction takes place in the upper column 12. The gas stream rises sequentially through these trays or packing, while the liquid flows downwards in sequence. The air stream enters the distillation column from the bottom, rises through the trays or packing to the top, and some of the gas is extracted from the column. The remaining portion condenses and returns to the bottom of the column as liquid (this liquid is called reflux).

[0025] The second branch of air exiting the first adsorption tower 4 and the second adsorption tower 5 enters the first expander 8 and the second expander 9 via connecting pipe L2 for cooling. Most of the cooling is achieved through isentropic expansion of air in the expanders, with a small portion compensated by the isothermal throttling effect of the gas. Air exiting the first expander 8 and the second expander 9 enters the bottom of the upper column 12 via connecting pipe as rising gas to participate in the upper column's distillation. The products of the lower column 11's distillation are nitrogen and oxygen-enriched liquid air. The oxygen-enriched liquid air at the bottom of the lower column 11, after cooling and throttling, enters the middle of the upper column 12 to participate in the upper column's distillation. The nitrogen at the top of the lower column 11 is condensed into liquid nitrogen; a portion is used as reflux liquid in the lower column 11, a portion is subcooled by a cooler and sent to the top of the upper column 12 as reflux liquid, and a small portion is extracted as liquid nitrogen product and sent to storage tank 14.

[0026] The waste nitrogen gas is sent from the upper column 12 through the pipeline to the subcooler 13 and the main heat exchanger 10 for reheating before being sent to the outside of the fractionation column. A portion of it is used as regeneration gas for the purification system and is sent through the pipeline L3 to the first heater 6 and the second heater 7 to regenerate the first adsorption column 4 and the second adsorption column 5. A small portion is used as sealing gas for the cold box, and the remaining waste nitrogen gas is released into the air.

[0027] The upper tower is equipped with a condenser, the lower tower is a high-pressure tower, and an evaporator is located between the upper tower 10 and the lower tower 9.

[0028] The pipeline from the upper column to the subcooler is equipped with a sludge nitrogen liquid air level regulating valve V2; the pipeline from the subcooler to the upper column is equipped with a liquid nitrogen throttling regulating valve V3; the liquid nitrogen storage tank is equipped with a liquid nitrogen extraction valve V4; and the lower column is equipped with a lower column liquid nitrogen reflux valve V11.

[0029] In a typical air separation tower, where the required compressed air pressure is 0.75 MPa, the pipeline is typically DN250. In this invention, pipeline L1 uses a DN300 pipeline.

[0030] This invention facilitates the adjustment of the centrifuge's set pressure. The specific adjustment method is as follows:

[0031] (1) The centrifuge set pressure is reduced to 0.71MPa. Based on the changes in parameters such as nitrogen flow rate, nitrogen outlet pressure, and upper tower pressure, and based on the liquid level of the upper tower evaporator, the V4 liquid nitrogen extraction valve is gradually adjusted to ensure the balance of cooling capacity in the fractionation tower and maintain stable nitrogen pipeline pressure.

[0032] (2) Slightly open the V11 lower column liquid nitrogen reflux valve, finely adjust the V2 waste nitrogen liquid air level regulating valve and the V3 liquid nitrogen throttling inlet regulating valve. As the set pressure of the new centrifuge and the air flow of the expander gradually decrease, open the expander inlet valve to control the cooling balance of the fractionation tower.

[0033] (3) Through adjustment, the new nitrogen generation system reaches a new balance, the set pressure of the new centrifuge is reduced from 0.75MPa to 0.71MPa, the output nitrogen flow rate remains unchanged, the centrifuge energy consumption is reduced, and the energy-saving and pressure-reducing technology adjustment operation is completed.

[0034] The above description is only a preferred embodiment of the present utility model, and therefore cannot be used to limit the scope of the present utility model. All equivalent changes and modifications made in accordance with the scope of the present utility model patent and the contents of the specification should still fall within the scope of the present utility model.

Claims

1. A float glass vacuum nitrogen generation device, characterized in that: The system includes a filter, through which filtered air enters a centrifugal compressor. The outlet of the centrifugal compressor is connected to a precooler, and the outlet of the precooler is connected to an adsorption tower. The outlet of the adsorption tower has two branches, one of which enters the main heat exchanger through a connecting pipe L1. The air after heat exchange in the main heat exchanger enters the lower tower, and the outlet of the lower tower is connected to a subcooler. The subcooler has multiple outlets, one of which enters the upper tower. In the upper tower, the airflow rises sequentially through trays or packing, while the liquid flows back downwards sequentially. The second branch of the adsorption tower outlet enters the expander through connecting pipe L2; the air from the expander enters the bottom of the upper tower as rising air through connecting pipe; the oxygen-enriched liquid air at the bottom of the lower tower enters the middle of the upper tower; after the nitrogen at the top of the lower tower is condensed into liquid nitrogen, part of it is used as the reflux liquid of the lower tower, part of it is sent to the top of the upper tower as reflux liquid after being subcooled by the cooler, and a small part is extracted as liquid nitrogen product and sent to the storage tank. The pipeline from the upper tower to the subcooler is equipped with a sludge nitrogen liquid air level regulating valve V2; the pipeline from the subcooler to the upper tower is equipped with a liquid nitrogen throttling regulating valve V3; the liquid nitrogen storage tank is equipped with a liquid nitrogen extraction valve V4; the lower tower is equipped with a lower tower liquid nitrogen reflux valve V11; the connecting pipeline L1 has a size of DN300.

2. The float glass vacuum nitrogen generation device according to claim 1, characterized in that: The adsorption tower includes a first adsorption tower and a second adsorption tower, which are arranged in parallel.

3. The float glass vacuum nitrogen generation device according to claim 1, characterized in that: The expander includes a first expander and a second expander, which are connected in parallel.

4. The float glass vacuum nitrogen generation device according to claim 1, characterized in that: The waste nitrogen gas is sent from the upper column through pipelines to the subcooler and the main heat exchanger for reheating before being sent to the fractionation column. A portion of it is used as regeneration gas for the purification system and is sent through pipeline L3 to the heater to regenerate the adsorption column. Another small portion is used as sealing gas for the cold box, and the remaining waste nitrogen gas is vented.

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