Method and device for generating gaseous compressed nitrogen
Method and device for generating gaseous compressed nitrogen by the low-temperature separation of air in a distillation column system, having a pre-column, a high-pressure column and a low-pressure column. The feed air is compressed, purified in a purification apparatus and cooled. A first sub-flow of the cooled feed air is introduced in a predominantly liquid state into the distillation column system. A gaseous fraction from the pre-column in introduced into the liquefaction chamber of a pre-column head condenser with liquid formed therein fed as reflux into the pre-column. A first gaseous nitrogen product fraction is drawn from the high-pressure column, heated, and obtained as first gaseous compressed nitrogen product. At least a part of the second sub-flow is introduced into the evaporation chamber of the pre-column head condenser. A third sub-flow of the cooled feed air is expanded to perform work and subsequently introduced into the liquefaction chamber.
1. A method for generating gaseous compressed nitrogen by low-temperature separation of air in a distillation column system having a pre-column which has a pre-column head condenser/evaporator having a liquefaction chamber and an evaporation chamber, a high-pressure column and a low-pressure column, said process comprising:
compressing input air in a main air compressor to form compressed input air,
cleaning the compressed input air in a cleaning device to form cleaned input air,
cooling the cleaned input air in a main heat exchanger to form cooled input air,
feeding a first partial stream of the cooled input air in gaseous form into the pre-column,
feeding a second partial stream of the cooled input air in a predominantly liquid state into the distillation column system,
feeding a gaseous fraction from an upper region of the pre-column into the liquefaction chamber of the head condenser/evaporator wherein liquid is formed in said liquefaction chamber, and
returning at least part of the liquid formed in the liquefaction chamber to the pre-column,
wherein said low-pressure column has a low-pressure column sump condenser/evaporator which has a liquefaction chamber and an evaporation chamber,
withdrawing a first nitrogen product fraction from the high-pressure column in gaseous form, warming said first nitrogen product fraction in the main heat exchanger, and removing warmed first nitrogen product fraction from the main heat exchanger to form a first gaseous compressed nitrogen product,
feeding at least a first substream of the second partial stream into the evaporation chamber of the pre-column head condenser/evaporator,
subjecting a third partial stream of the cooled input air to pressure reduction whereby work is performed,
wherein, after said pressure reduction, the third partial stream has a pressure which is higher than an operating pressure of the low-pressure column,
wherein, after said pressure reduction, the third partial stream is fed into the liquefaction chamber of the low-pressure column sump condenser/evaporator and is at least partly liquefied there to form liquefied third partial stream,
feeding at least a substream of the liquefied third partial stream into the low-pressure column, wherein said sub stream of the liquefied third partial stream is liquefied air,
wherein the low-pressure column has an intermediate condenser/evaporator having a liquefaction chamber and an evaporation chamber,
evaporating at least part of an intermediate liquid of the low-pressure column in the evaporation chamber of the intermediate condenser/evaporator,
liquefying at least part of a gaseous head fraction from the high-pressure column in the liquefaction chamber of the intermediate condenser/evaporator to form liquid, and returning at least part of the liquid formed in the liquefaction chamber of the intermediate condenser/evaporator to the high-pressure column, and
wherein said first gaseous compressed nitrogen product is more than 35 mol % of said input air.
2. The method as claimed in claim 1 , wherein a second gaseous nitrogen product fraction is withdrawn from the pre-column in gaseous form, warmed in the main heat exchanger and removed from the main heat exchanger to form a second gaseous compressed product.
3. The method as claimed in claim 1 , wherein less than 30 mol % of said input air is fed in the liquid state into the distillation column system.
4. The method as claimed in claim 1 , wherein the quantity of oxygen-enriched streams fed in the liquid state from the pre-column and the evaporation chamber of the pre-column head condenser/evaporator into the high-pressure column and the low-pressure column is less than 14 mol % of said input air.
5. The method as claimed in claim 1 , wherein
the second partial stream is compressed, before being cooled in the main heat exchanger, to a pressure that is higher than an operating pressure of the pre-column, and is liquefied or pseudo-liquefied in the main heat exchanger, and
a liquid stream is removed from the distillation column system, brought to an elevated pressure in the liquid state, evaporated or pseudo-evaporated in the main heat exchanger.
6. The method as claimed in claim 1 , wherein a gaseous fraction from the evaporation chamber of the pre-column head condenser/evaporator is fed, in the form of a gaseous input stream, into the high-pressure column.
7. The method as claimed in claim 1 , wherein at least some sump liquid of the pre-column is fed into the evaporation chamber of the pre-column head condenser/evaporator.
8. The method as claimed in claim 1 , wherein the third partial stream is further compressed before being cooled in the main heat exchanger.
9. The method as claimed in claim 1 , wherein, after said reducing, the pressure of the third partial stream is lower than an operating pressure of the high-pressure column.
10. The method as claimed in claim 4 , wherein the total quantity of oxygen-enriched streams fed in the liquid state from the pre-column and the evaporation chamber of the pre-column head condenser/evaporator into the high-pressure column and the low-pressure column is less than 1 mol % of said input air.
11. The method as claimed in claim 1 , wherein more than 45 mol % of the input air, in the form of the first nitrogen product fraction, is withdrawn in gaseous form from the high-pressure column and warmed in the main heat exchanger.
12. The method as claimed in claim 1 , wherein
the second partial stream is compressed, before being cooled in the main heat exchanger, to a pressure that is higher than an operating pressure of the pre-column, and is liquefied or pseudo-liquefied in the main heat exchanger, and
a liquid oxygen stream is removed from the distillation column system, brought to an elevated pressure in the liquid state, and evaporated or pseudo-evaporated in the main heat exchanger.
13. The method according to claim 1 , wherein the pre-column has a head, the low-pressure column has a head, and the high-pressure column has a head, and an operating pressure at the head of the pre-column is 6 to 9 bar, an operating pressure at the head of the high-pressure column is 3 to 6 bar, and an operating pressure at the head of the low-pressure column is 1.25 to 1.7 bar.
14. A method for generating gaseous compressed nitrogen by low-temperature separation of air in a distillation column system having a pre-column which has a pre-column head condenser/evaporator having a liquefaction chamber and an evaporation chamber, a high-pressure column and a low-pressure column, said process comprising:
compressing input air in a main air compressor to form compressed input air,
cleaning the compressed input air in a cleaning device to form cleaned input air,
cooling the cleaned input air in a main heat exchanger to form cooled input air,
feeding a first partial stream of the cooled input air in gaseous form into the pre-column,
feeding a second partial stream of the cooled input air in a predominantly liquid state into the distillation column system,
feeding a gaseous fraction from an upper region of the pre-column into the liquefaction chamber of the head condenser/evaporator wherein liquid is formed in said liquefaction chamber, and
returning at least part of the liquid formed in the liquefaction chamber to the pre-column,
wherein said low-pressure column has a low-pressure column sump condenser/evaporator which has a liquefaction chamber and an evaporation chamber,
withdrawing a first nitrogen product fraction from the high-pressure column in gaseous form, warming said first nitrogen product fraction in the main heat exchanger, and removing warmed first nitrogen product fraction from the main heat exchanger to form a first gaseous compressed nitrogen product,
feeding at least a first substream of the second partial stream into the evaporation chamber of the pre-column head condenser/evaporator,
subjecting a third partial stream of the cooled input air to pressure reduction whereby work is performed,
wherein, after said pressure reduction, the third partial stream has a pressure which is higher than an operating pressure of the low-pressure column,
wherein, after said pressure reduction, the third partial stream is fed into the liquefaction chamber of the low-pressure column sump condenser/evaporator and is at least partly liquefied there to form liquefied third partial stream,
feeding at least a substream of the liquefied third partial stream into the low-pressure column, wherein said sub stream of the liquefied third partial stream is liquefied air,
wherein the low-pressure column has an intermediate condenser/evaporator having a liquefaction chamber and an evaporation chamber,
evaporating at least part of an intermediate liquid of the low-pressure column in the evaporation chamber of the intermediate condenser/evaporator,
liquefying at least part of a gaseous head fraction from the high-pressure column in the liquefaction chamber of the intermediate condenser/evaporator to form liquid, and returning at least part of the liquid formed in the liquefaction chamber of the intermediate condenser/evaporator to the high-pressure column,
wherein said first gaseous compressed nitrogen product is more than 35 mol % of said input air, and
wherein less than 30 mol % of said input air is fed in the liquid state into the distillation column system.
15. A method for generating gaseous compressed nitrogen by low-temperature separation of air in a distillation column system having a pre-column which has a pre-column head condenser/evaporator having a liquefaction chamber and an evaporation chamber, a high-pressure column and a low-pressure column, said process comprising:
compressing input air in a main air compressor to form compressed input air,
cleaning the compressed input air in a cleaning device to form cleaned input air,
cooling the cleaned input air in a main heat exchanger to form cooled input air,
feeding a first partial stream of the cooled input air in gaseous form into the pre-column,
feeding a second partial stream of the cooled input air in a predominantly liquid state into the distillation column system,
feeding a gaseous fraction from an upper region of the pre-column into the liquefaction chamber of the head condenser/evaporator wherein liquid is formed in said liquefaction chamber, and
returning at least part of the liquid formed in the liquefaction chamber to the pre-column,
wherein said low-pressure column has a low-pressure column sump condenser/evaporator which has a liquefaction chamber and an evaporation chamber,
withdrawing a first nitrogen product fraction from the high-pressure column in gaseous form, warming said first nitrogen product fraction in the main heat exchanger, and removing warmed first nitrogen product fraction from the main heat exchanger to form a first gaseous compressed nitrogen product,
feeding at least a first substream of the second partial stream into the evaporation chamber of the pre-column head condenser/evaporator,
subjecting a third partial stream of the cooled input air to pressure reduction whereby work is performed,
wherein, after said pressure reduction, the third partial stream has a pressure which is higher than an operating pressure of the low-pressure column,
wherein, after said pressure reduction, the third partial stream is fed into the liquefaction chamber of the low-pressure column sump condenser/evaporator and is at least partly liquefied there to form liquefied third partial stream,
feeding at least a substream of the liquefied third partial stream into the low-pressure column, wherein said sub stream of the liquefied third partial stream is liquefied air,
wherein the low-pressure column has an intermediate condenser/evaporator having a liquefaction chamber and an evaporation chamber,
evaporating at least part of an intermediate liquid of the low-pressure column in the evaporation chamber of the intermediate condenser/evaporator,
liquefying at least part of a gaseous head fraction from the high-pressure column in the liquefaction chamber of the intermediate condenser/evaporator to form liquid, and returning at least part of the liquid formed in the liquefaction chamber of the intermediate condenser/evaporator to the high-pressure column,
wherein said first gaseous compressed nitrogen product is more than 35 mol % of said input air, and
wherein, after said reducing, the pressure of the third partial stream is lower than an operating pressure of the high-pressure column.
16. The method as claimed in claim 1 , further comprising splitting said second partial stream of the cooled input air, before being introduced into the distillation column system, into said first substream of the second partial stream and a second substream of the second partial stream, and feeding said second substream of the second partial stream into the pre-column.
17. The method as claimed in claim 1 , further comprising removing a liquid flushing stream from the evaporation chamber of the pre-column head condenser/evaporator, warming the liquid flushing stream in a heat exchanger, and then feeding the flushing stream into the low-pressure column.