Air separation rectification device for reducing oxygen-enriched liquid air conveying energy consumption

Abstract

The utility model relates to an air separation rectification device capable of reducing oxygen-enriched liquid air conveying energy consumption, which comprises a rectification main tower, the rectification main tower comprises an upper tower, a main condensation evaporator and a lower tower, oxygen-enriched liquid air conveying pipes are arranged on the upper tower and the lower tower, a first compressed air conveying branch pipe is arranged on the lower tower, and a second compressed air conveying branch pipe is arranged on the lower tower. A first adjusting valve and a second compressed air conveying branch pipe are arranged on the first compressed air conveying branch pipe, a second adjusting valve is arranged on the second compressed air conveying branch pipe, and the oxygen-enriched liquid air conveying pipe is provided with a third adjusting valve, a first one-way valve and a gas supercharging device. The gas supercharging device comprises an inner pipe, an outer shell, an inter-shell cavity, a first vent hole group and a second vent hole group, the first vent hole group and the second vent hole group both comprise through holes, the second compressed air conveying branch pipe is communicated with the inter-shell cavity, and the inner pipe is installed on the oxygen-enriched liquid air conveying pipe. And the extra energy consumption required by the process of conveying the oxygen-enriched liquid air from the lower tower to the upper tower is reduced. The utility model has the advantages of convenient use and wide market prospect.

Description

Technical Field

[0001] The utility model relates to the field of air separation and distillation equipment, in particular to an air separation and distillation device capable of reducing energy consumption of oxygen-enriched liquid air transportation. Background Art

[0002] In the process flow of the air separation unit, the raw air enters the lower tower after a series of operations such as filtration, compression, precooling, purification, pressurization, expansion and heat exchange. After the air is initially distilled by the lower tower, oxygen-rich liquid air is obtained at the bottom of the lower tower, and pressurized nitrogen is obtained at the top of the lower tower and transported to the main condensing heat exchanger for heat exchange to obtain liquid nitrogen, which is divided into two parts. The first part of liquid nitrogen is transported to the lower tower as the reflux condensate of the lower tower, and the second part of liquid nitrogen is sent to and subcooled by the subcooler and divided into two parts again. The first part of the subcooled liquid nitrogen is transported to the liquid nitrogen storage tank, and the second part of the subcooled liquid nitrogen is sent to the upper tower as the reflux condensate of the upper tower; at the same time, the upper tower accepts the oxygen-rich liquid air from the lower tower as one of the distillation raw materials. After further distillation by the upper tower, the oxygen product is obtained at the bottom of the upper tower, and is compressed by the liquid oxygen pump and enters the main heat exchanger. After reheating, it exits the cold box as a gas oxygen product. Part of the liquid oxygen directly exits the cold box and enters the liquid oxygen storage tank as a liquid oxygen product; the liquid nitrogen product is extracted from the top of the upper tower and enters the liquid nitrogen storage tank.

[0003] In the classic air separation process, the oxygen-rich liquid air in the lower tower is transported from the lower tower to the upper tower by a cryogenic booster pump that provides partial power combined with the pressure of the lower tower itself. Since the work used to drive the cryogenic booster pump itself will inevitably cause energy consumption, for the simplest cryogenic air separation distillation process that produces nitrogen products and oxygen products at the same time, reducing the energy consumption of the output unit volume of nitrogen products and oxygen products has always been the unremitting goal pursued by workers in the field of air separation, and it is also one of the criteria for judging whether different cryogenic air separation processes are better. Reducing the energy consumption required in the process of transporting oxygen-rich liquid air from the lower tower to the upper tower, thereby reducing the energy consumption of the overall cryogenic air separation distillation system, is a technical direction worthy of consideration, which will better meet the market demand of customers for reducing overall energy consumption, thereby increasing the promotion of the cryogenic air separation distillation system. Summary of the invention

[0004] In view of the deficiencies in the prior art, the utility model provides an air fractionation and distillation device for reducing the extra energy consumption required for the process of transporting oxygen-enriched liquid air from a lower tower to an upper tower, which is used to overcome the defects in the prior art.

[0005] The technical solution adopted by the utility model is: an air fractionation and distillation device for reducing the energy consumption of oxygen-enriched liquid air transportation, comprising a main distillation tower, the main distillation tower comprising an upper tower, a main condenser evaporator and a lower tower from top to bottom, oxygen-enriched liquid air transportation pipes are arranged on the upper tower and the lower tower, a first compressed air transportation branch pipe is arranged on the lower tower, the first compressed air transportation branch pipe is arranged with a first regulating valve and an inlet end of a second compressed air transportation branch pipe in a direction from close to the lower tower to far away from the lower tower, a second regulating valve is arranged on the second compressed air transportation branch pipe, and the oxygen-enriched liquid air transportation pipe is arranged along the lower tower. A third regulating valve, a first non-return valve and a gas pressurizing device are sequentially arranged in the direction from the lower tower to the upper tower. The gas pressurizing device comprises an inner tube, an outer shell arranged outside the inner tube, an intershell cavity arranged between the outer shell and the inner tube, and a first vent group and a second vent group arranged between the intershell cavity and the inner tube. The first vent group and the second vent group both comprise a plurality of through holes arranged on the inner tube and distributed in a star shape outside the central axis of the inner tube. The outlet end of the second compressed air delivery branch pipe is connected to the intershell cavity, and the inner tube is installed on the oxygen-enriched liquid air delivery pipe.

[0006] Preferably, a flash tank is provided in the upper tower, the flash tank comprises a tank body, a gas phase discharge port provided at the top of the tank body, a liquid phase discharge port provided at the bottom of the tank body and a mixed liquid delivery port provided in the middle of the tank body, and the outlet end of the oxygen-enriched liquid air delivery pipe is connected to the mixed liquid delivery port.

[0007] Preferably, a dirty nitrogen gas delivery pipe is provided on the upper tower, and a first subcooler is provided on the oxygen-enriched liquid air delivery pipe between the third regulating valve and the lower tower and the dirty nitrogen gas delivery pipe.

[0008] Preferably, a first pressure sensor is provided on the oxygen-enriched liquid air delivery pipe between the third regulating valve and the first one-way valve, and a second pressure sensor is provided on the second compressed air delivery branch pipe between the gas boosting device and the second regulating valve.

[0009] Preferably, the inlet end of the heat source channel of the main condenser evaporator is connected to the top of the lower tower, and a liquid nitrogen delivery main pipe is provided on the inlet end of the heat source channel of the main condenser evaporator. The liquid nitrogen delivery main pipe is provided with an inlet end of a first liquid nitrogen delivery branch pipe, an inlet end of a second liquid nitrogen delivery branch pipe and a fourth regulating valve in sequence from close to the main condenser evaporator to far away from the main condenser evaporator. The first liquid nitrogen delivery branch pipe and the second liquid nitrogen delivery branch pipe are respectively provided with a fifth regulating valve, the outlet end of the first liquid nitrogen delivery branch pipe is connected to the lower tower, and the outlet end of the second liquid nitrogen delivery branch pipe is connected to the upper tower.

[0010] Preferably, a finished nitrogen gas delivery pipe is provided on the upper tower, and a second subcooler is provided on the liquid nitrogen delivery main pipe between the first liquid nitrogen delivery branch pipe and the second liquid nitrogen delivery branch pipe and the finished nitrogen gas delivery pipe.

[0011] Preferably, it also includes a main heat exchanger, and the second compressed air delivery branch is installed on the main heat exchanger away from the first compressed air delivery branch on one side of the first regulating valve. The main heat exchanger is provided with a third compressed air delivery branch, and a compressed air delivery main pipe is provided on the inlet end of the third compressed air delivery branch and the inlet end of the first compressed air delivery branch. The boosting end of the turbine expander and the sixth regulating valve are sequentially provided on the third compressed air delivery branch along the direction from the compressed air delivery main pipe to the main heat exchanger, the outlet end of the third compressed air delivery branch is connected to the inlet end of the turbine expander, and the outlet end of the turbine expander is connected to the upper tower.

[0012] The beneficial effects of the utility model are as follows: firstly, the utility model utilizes that the oxygen-enriched liquid air transported to the inner tube is continuously mixed with the compressed air transported through the first vent hole group and the second vent hole group to form a jet liquid flow, and the gas phase part and the liquid phase part in the jet liquid flow continue to exchange heat to promote the vaporization of the liquid phase part, thereby realizing the use of the pressure carried by the liquid phase part itself and the pressure directly carried by the gas phase part and then utilizing the partially vaporized liquid phase part to form the power of the jet liquid flow to overcome gravity to do work, changing the traditional process of using a low-temperature booster pump to provide power to realize the transport of oxygen-enriched liquid air from the lower tower to the upper tower and reducing the additional energy consumption required for the process of transporting oxygen-enriched liquid air from the lower tower to the upper tower.

[0013] Secondly, a first pressure sensor is provided on the oxygen-rich liquid air delivery pipe between the third regulating valve and the first one-way valve described in the utility model, and a second pressure sensor is provided on the second compressed air delivery branch pipe between the gas boosting device and the second regulating valve; the first pressure sensor and the second pressure sensor are installed to facilitate the feedback of pressure parameters.

[0014] Finally, the tank body of the flash tank of the utility model and the bottom of the lower tower are respectively provided with liquid level sensors; the installation of the liquid level sensors facilitates the feedback of liquid level parameters.

[0015] The utility model has the advantages of simple structure, convenient operation, ingenious design, greatly improved working efficiency, good social and economic benefits, and is a product that is easy to promote and use. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] Figure 1 It is a structural schematic diagram of the utility model.

[0017] Figure 2 for Figure 1 A partial enlarged schematic diagram of detail A. DETAILED DESCRIPTION

[0018] like Figure 1 and Figure 2As shown, an air fractionation and distillation device for reducing energy consumption of oxygen-enriched liquid air transportation comprises a main distillation tower, wherein the main distillation tower comprises an upper tower 1, a main condenser evaporator 2 and a lower tower 3 from top to bottom, an oxygen-enriched liquid air transportation pipe 4 is provided on the upper tower 1 and the lower tower 3, a first compressed air transportation branch pipe 5 is provided on the lower tower 3, the first compressed air transportation branch pipe 5 is provided with a first regulating valve 6 and an inlet end of a second compressed air transportation branch pipe 7 in a direction from close to the lower tower 3 to away from the lower tower 3, a second regulating valve 8 is provided on the second compressed air transportation branch pipe 7, and the oxygen-enriched liquid air transportation pipe 4 is provided with a first regulating valve 6 and an inlet end of a second compressed air transportation branch pipe 7 in a direction from close to the lower tower 3 to away from the lower tower 3. A third regulating valve 9, a first non-return valve 10 and a gas boosting device are sequentially arranged, the gas boosting device comprises an inner tube 11, an outer shell 12 arranged outside the inner tube 11, a shell cavity arranged between the outer shell 12 and the inner tube 11, and a first vent group and a second vent group arranged between the shell cavity and the inner tube 11, the first vent group and the second vent group both comprise a plurality of through holes 13 arranged on the inner tube 11 and distributed in a star shape outside the central axis of the inner tube 11, the outlet end of the second compressed air delivery branch pipe 7 is connected to the shell cavity, and the inner tube 11 is installed on the oxygen-enriched liquid air delivery pipe 4. The central axis of one through hole 13 in the second vent group is located on the central axis of two adjacent through holes 13 in the first vent group. The number of the first ventilation hole group and the second ventilation hole group are both multiple, and the first ventilation hole group and the second ventilation hole group are alternately distributed on the inner tube 11 in the shell cavity along the direction from the bottom of the inner tube 11 to the top of the inner tube 11.

[0019] The upper tower 1 is provided with a flash tank 14, which includes a tank body, a gas phase discharge port provided at the top of the tank body, a liquid phase discharge port provided at the bottom of the tank body, and a mixed liquid delivery port provided in the middle of the tank body. The outlet end of the oxygen-enriched liquid air delivery pipe 4 is connected to the mixed liquid delivery port. This facilitates the separation of the gas-liquid mixture delivered to the upper tower 1, and enables the delivery of the ascending gas phase medium to the upper tower 1 through the gas phase discharge port as a distillation raw material, and at the same time, enables the delivery of the descending liquid phase medium to the upper tower 1 through the liquid phase discharge port as a distillation raw material and provides cooling capacity at the same time; further, the upper tower 1 is provided with a dirty nitrogen gas delivery pipe 15, and the oxygen-enriched liquid air delivery pipe 4 and the dirty nitrogen gas delivery pipe 15 between the third regulating valve 9 and the lower tower 3 are provided with a first subcooler 16; the oxygen-enriched liquid air at the bottom of the lower tower 3 is delivered to the heat source channel of the first subcooler 16 After exchanging heat with the dirty nitrogen gas transported through the dirty nitrogen gas transport pipe 15 which is continuously transported to the cold source channel of the first subcooler 16, the subcooled oxygen-rich liquid air is discharged from the outlet of the heat source channel of the first subcooler 16 and continues to pass through the valve cavity of the third regulating valve 9 along the oxygen-rich liquid air transport pipe 4 and is then transported to the inner tube 11. In the process of transporting the subcooled oxygen-rich liquid air from the first subcooler 16 to the inner tube 11, the oxygen-rich liquid air is subcooled by the dirty nitrogen gas transported through the dirty nitrogen gas transport pipe 15 to form a completely liquefied state, thereby making it easier to use the pressure in the lower tower 3 as the power for the subcooled oxygen-rich liquid air to continue to move forward.

[0020] A first pressure sensor 17 is provided on the oxygen-enriched liquid air delivery pipe 4 between the third regulating valve 9 and the first one-way valve 10, and a second pressure sensor 18 is provided on the second compressed air delivery branch pipe 7 between the gas boosting device and the second regulating valve 8; a second one-way valve 32 is provided on the second compressed air delivery branch pipe 7 between the second pressure sensor 18 and.

[0021] The inlet end of the heat source channel of the main condenser evaporator 2 is connected to the top of the lower tower 3, and a liquid nitrogen delivery main pipe 19 is provided on the inlet end of the heat source channel of the main condenser evaporator 2. The liquid nitrogen delivery main pipe 19 is provided with the inlet end of the first liquid nitrogen delivery branch pipe 20, the inlet end of the second liquid nitrogen delivery branch pipe 21 and the fourth regulating valve 22 in sequence from the main condenser evaporator 2 to the direction away from the main condenser evaporator 2. The first liquid nitrogen delivery branch pipe 20 and the second liquid nitrogen delivery branch pipe 21 are respectively provided with a fifth regulating valve 23. The outlet end of the first liquid nitrogen delivery branch pipe 20 is connected to the lower tower 3, and the outlet end of the second liquid nitrogen delivery branch pipe 21 is connected to the upper tower 1. A finished nitrogen delivery pipe 24 is provided on the upper tower 1, and a second subcooler 25 is provided on the liquid nitrogen delivery main pipe 19 between the first liquid nitrogen delivery branch pipe 20 and the second liquid nitrogen delivery branch pipe 21 and the finished nitrogen delivery pipe 24.

[0022] In addition, the product also includes a main heat exchanger 26, and the first compressed air delivery branch 5 on the side of the second compressed air delivery branch 7 away from the first regulating valve 6 is installed on the main heat exchanger 26. The main heat exchanger 26 is provided with a third compressed air delivery branch 27, and a compressed air delivery main pipe 28 is provided on the inlet end of the third compressed air delivery branch 27 and the inlet end of the first compressed air delivery branch 5. The boosting end of the turbine expander 29 and the sixth regulating valve 30 are sequentially arranged on the third compressed air delivery branch 27 along the direction from the compressed air delivery main pipe 28 to the main heat exchanger 26, the outlet end of the third compressed air delivery branch 27 is connected to the inlet end of the turbine expander 29, and the outlet end of the turbine expander 29 is connected to the upper tower 1. The upper tower 1 and the main heat exchanger 26 are provided with a finished oxygen delivery pipe 31, the part of the dirty nitrogen delivery pipe 15 of the first subcooler 16 away from the upper tower 1 is installed on the main heat exchanger 26, and the part of the finished nitrogen delivery pipe 24 of the second subcooler 25 away from the upper tower 1 is installed on the main heat exchanger 26. The tank body of the flash tank 14 and the bottom of the lower tower 3 are respectively provided with a liquid level sensor 33. The bottom of the lower tower 3 is provided with a sewage pipe 34, and the sewage pipe 34 is provided with a sewage valve 35.

[0023] The usage of this product is as follows: Figure 1 and Figure 2 As shown, the following steps are included:

[0024] S1, the compressed air delivery main pipe 28 receives the purified compressed air delivered from the upstream, and then divides it into two parts, namely the first part of compressed air and the second part of compressed air. The first part of compressed air is delivered to the first compressed air delivery branch pipe 5, and the second part of compressed air is delivered to the third compressed air delivery branch pipe 27; the second part of compressed air entering the third compressed air delivery branch pipe 27 is pressurized at the boosting end of the turbine expander 29, and then enters the first heat source channel of the main heat exchanger 26 from the high temperature end of the main heat exchanger 26 and is continuously delivered to the cold source of the main heat exchanger 26 for heat exchange before being delivered The compressed air enters the expansion end of the turbine expander 29 for expansion and cooling, and then is sent to the upper tower 1 as one of the gaseous distillation raw materials of the upper tower 1; the first part of the compressed air entering the first compressed air delivery branch pipe 5 is delivered to the second heat source channel of the main heat exchanger 26 and continuously delivered to the cold source of the main heat exchanger 26 for heat exchange, and then is divided into two parts again, namely the third part of the compressed air and the fourth part of the compressed air. The third part of the compressed air continues to move along the first compressed air delivery branch pipe 5 and is finally sent to the lower tower 3 as the distillation raw material of the lower tower 3, and the fourth part of the compressed air is delivered to the second compressed air delivery branch pipe 7.

[0025] S2, the third part of compressed air enters the lower tower 3 to form a first ascending airflow and continuously ascends along the inner cavity of the lower tower 3 and performs countercurrent heat exchange with the first reflux condensate continuously descending along the inner cavity of the lower tower 3. During this period, the oxygen component in the first ascending airflow is continuously liquefied and merged with the first reflux condensate to form a first descending liquid flow, and the nitrogen component in the first reflux condensate is continuously vaporized and continuously merged into the first ascending airflow, and finally a first nitrogen enrichment zone is formed at the top of the lower tower 3, and an oxygen-rich liquid air enrichment zone is formed at the bottom of the lower tower 3. The oxygen-rich liquid air in the oxygen-rich liquid air enrichment zone is transported to the oxygen-rich liquid air transport pipe 4, first sent to the heat source channel of the first subcooler 16 and continuously transported to the medium of the cold source channel of the first subcooler 16 for heat exchange, and then transported to the inner pipe 11 and through the second compressed air transport branch The fourth part of the compressed air delivered to the shell cavity through the pipe 7 and then delivered to the inner pipe 11 through the first vent group and the second vent group is directly mixed to form a jet liquid flow, and the jet liquid flow continues to ascend along the oxygen-enriched liquid air delivery pipe 4 and is finally delivered to the flash tank 14. In the process of direct mixing of the oxygen-enriched liquid air and the fourth part of the compressed air, the fourth part of the compressed air is firstly uniformly delivered to the oxygen-enriched liquid air that continues to move forward through the first vent group and the second vent group, so as to be directly mixed to form a jet liquid flow, and the gas phase part and the liquid phase part in the jet liquid flow continue to exchange heat to promote the vaporization of the liquid phase part, so as to realize the use of the pressure carried by the liquid phase part itself and the pressure directly carried by the gas phase part, and then use the partially vaporized liquid phase part to form the power of the jet liquid flow to overcome gravity and do work. The jet liquid flow enters the flash tank 14 for gas-liquid separation, and the gas phase portion of the jet liquid flow enters the upper tower 1 through the gas phase discharge port of the flash tank 14 and continues to ascend to form one of the gaseous distillation raw materials of the upper tower 1, while the liquid phase portion of the jet liquid flow enters the upper tower 1 through the liquid phase discharge port of the flash tank 14 to form the liquid distillation raw material of the upper tower 1.

[0026] S3, the first nitrogen enrichment zone at the top of the lower tower 3 continuously transports high-pressure nitrogen to the heat source channel of the main condenser evaporator 2 for heat exchange with the medium in the cold source channel of the main condenser evaporator 2, and the heat source channel of the main condenser evaporator 2 continuously transports liquid nitrogen to the liquid nitrogen delivery main pipe 19, and the liquid nitrogen is first divided into two parts. The first part of the liquid nitrogen is returned to the lower tower 3 through the first liquid nitrogen delivery branch pipe 20 as the first reflux condensate; the second part of the liquid nitrogen continues to move along the liquid nitrogen delivery main pipe 19 and is transported to the heat source channel of the second subcooler 25 and continuously transported to the cold source of the second subcooler 25 for heat exchange to form subcooled liquid nitrogen, and the outlet of the heat source channel of the second subcooler 25 discharges the subcooled liquid nitrogen and is divided into two parts again, the first part of the subcooled liquid nitrogen continues to move forward through the liquid nitrogen delivery main pipe 19 and is transported to the liquid nitrogen storage tank for storage as a liquid nitrogen product; the second part of the subcooled liquid nitrogen is transported to the upper tower 1 through the second liquid nitrogen delivery branch pipe 21 as the second condensate reflux liquid.

[0027] S4, the second part of the compressed air entering the upper tower 1 forms a second rising airflow and then continues to ascend along the inner cavity of the upper tower 1, the gas phase part of the jet liquid flow entering the upper tower 1 forms a third rising airflow and then continues to ascend along the inner cavity of the upper tower 1, the second rising airflow first performs countercurrent heat exchange with the liquid phase part of the jet liquid flow entering the upper tower 1 during the upward process, during the countercurrent heat exchange of the second rising airflow, the oxygen component in the second rising airflow is liquefied and continuously merged into the liquid phase part of the jet liquid flow, and the nitrogen component in the liquid phase part of the jet liquid flow is continuously vaporized and merged into the second rising airflow, the second rising airflow continues to ascend and merges with the third rising airflow to form a fourth rising airflow and continues to ascend along the inner cavity of the upper tower 1, during the continuous upward process of the fourth rising airflow, it performs countercurrent heat exchange with the second reflux condensate entering the upper tower 1, during the countercurrent heat exchange of the fourth rising airflow and the second reflux condensate During the countercurrent heat exchange process, the oxygen component in the fourth rising airflow is liquefied and merged into the second reflux condensate, and the nitrogen component in the second reflux condensate is continuously vaporized and continuously merged into the fourth rising airflow, and finally a second nitrogen-enriched zone is formed at the top of the upper tower 1. The second reflux condensate continues to descend and merges with the liquid phase of the jet liquid flow to form a second descending liquid flow, which continues to descend along the inner cavity of the upper tower 1 and enters the cold source channel of the main condenser evaporator 2 and is continuously transported to the heat source of the main condenser evaporator 2 for heat exchange; during the continuous heat exchange process between the medium in the cold source channel of the main condenser evaporator 2 and the heat source continuously transported to the main condenser evaporator 2, the cold source channel of the main condenser evaporator 2 continuously generates a fifth rising airflow, and the fifth rising airflow continuously performs countercurrent heat exchange with the second descending liquid flow, and the nitrogen component in the fifth rising airflow remains in a gaseous state and continues to ascend along the upper tower 1 and continuously merges into the second rising airflow; thereby forming an oxygen-enriched zone at the bottom of the upper tower 1.

[0028] S5. The nitrogen in the top of the second nitrogen enrichment zone carries a small amount of non-condensable gas to form dirty nitrogen and is transported to the dirty nitrogen delivery pipe 15. The dirty nitrogen entering the dirty nitrogen delivery pipe 15 is firstly transported to the cold source channel of the first subcooler 16 and the medium continuously transported to the heat source channel of the first subcooler 16 for heat exchange, and then transported to the first cold source channel of the main heat exchanger 26 and the heat source continuously transported to the main heat exchanger 26 for heat exchange, and then transported to the target user through the outlet end of the dirty nitrogen delivery pipe 15; the finished nitrogen is transported to the finished nitrogen delivery pipe 24 from the bottom of the top of the second nitrogen enrichment zone, and the finished nitrogen entering the finished nitrogen delivery pipe 24 is transported to the target user through the outlet end of the dirty nitrogen delivery pipe 15. The finished nitrogen first passes through the cold source channel of the second supercooler 25 and the medium continuously transported to the heat source channel of the second supercooler 25 for heat exchange, and then is transported to the second cold source channel of the main heat exchanger 26 and the heat source continuously transported to the main heat exchanger 26 for heat exchange, and then is transported to the target user through the outlet end of the finished nitrogen delivery pipe 24; the oxygen enrichment zone transports the finished oxygen to the finished oxygen delivery pipe 31, and the finished oxygen entering the finished oxygen delivery pipe 31 is transported to the third cold source channel of the main heat exchanger 26 and the heat source continuously transported to the main heat exchanger 26 for heat exchange, and then is transported to the target user through the outlet end of the finished oxygen delivery pipe 31.

[0029] Through this embodiment, the oxygen-rich liquid air delivered to the inner tube 11 is continuously mixed with the compressed air delivered through the first vent group and the second vent group to form a jet liquid flow, and the gas phase and liquid phase in the jet liquid flow continue to exchange heat to promote the vaporization of the liquid phase, thereby utilizing the pressure of the liquid phase itself and the pressure directly carried by the gas phase to reuse the partially vaporized liquid phase to form the power of the jet liquid flow to overcome gravity and do work, changing the traditional process of using a low-temperature booster pump to provide power to realize the transportation of oxygen-rich liquid air from the lower tower to the upper tower and reducing the additional energy consumption required for the process of transporting oxygen-rich liquid air from the lower tower to the upper tower.

[0030] The embodiments described above are only preferred embodiments of the present invention and are not intended to limit the scope of implementation of the present invention. Therefore, any equivalent changes or modifications made based on the structures, features and principles described in the patent scope of the present invention should be included in the patent application scope of the present invention.

Claims

1. An air fractionation and distillation device for reducing energy consumption of oxygen-enriched liquid air transportation, comprising a main distillation tower, wherein the main distillation tower comprises, from top to bottom, an upper tower (1), a main condenser evaporator (2) and a lower tower (3), the upper tower (1) and the lower tower (3) are provided with oxygen-enriched liquid air transportation pipes (4), and the lower tower (3) is provided with a first compressed air transportation branch pipe (5), characterized in that: The first compressed air delivery branch pipe (5) is provided with a first regulating valve (6) and an inlet end of a second compressed air delivery branch pipe (7) in sequence along a direction from close to the lower tower (3) to far from the lower tower (3); the second compressed air delivery branch pipe (7) is provided with a second regulating valve (8); the oxygen-enriched liquid air delivery pipe (4) is provided with a third regulating valve (9), a first non-return valve (10) and a gas boosting device in sequence along a direction from the lower tower (3) to the upper tower (1); the gas boosting device comprises an inner pipe (11), an inner pipe (11 ), an outer shell (12) arranged on the outside of the outer shell (12), an intershell cavity arranged between the outer shell (12) and the inner tube (11), and a first vent hole group and a second vent hole group arranged between the intershell cavity and the inner tube (11), the first vent hole group and the second vent hole group both comprising a plurality of through holes (13) arranged on the inner tube (11) and distributed in a star shape on the outside of the central axis of the inner tube (11), the outlet end of the second compressed air delivery branch pipe (7) being connected to the intershell cavity, and the inner tube (11) being mounted on the oxygen-enriched liquid air delivery pipe (4).

2. The air fractionation and rectification device for reducing the energy consumption of oxygen-rich liquid air transportation according to claim 1, characterized in that: A flash tank (14) is arranged in the upper tower (1), and the flash tank (14) comprises a tank body, a gas phase discharge port arranged at the top of the tank body, a liquid phase discharge port arranged at the bottom of the tank body, and a mixed liquid delivery port arranged in the middle of the tank body, and the outlet end of the oxygen-enriched liquid air delivery pipe (4) is connected to the mixed liquid delivery port.

3. The air fractionation and rectification device for reducing the energy consumption of oxygen-rich liquid air transportation according to claim 1, characterized in that: The upper tower (1) is provided with a dirty nitrogen gas delivery pipe (15), and a first subcooler (16) is provided on the oxygen-rich liquid air delivery pipe (4) between the third regulating valve (9) and the lower tower (3) and the dirty nitrogen gas delivery pipe (15).

4. The air fractionation and rectification device for reducing the energy consumption of oxygen-rich liquid air transportation according to claim 1, characterized in that: A first pressure sensor (17) is provided on the oxygen-enriched liquid air delivery pipe (4) between the third regulating valve (9) and the first non-return valve (10), and a second pressure sensor (18) is provided on the second compressed air delivery branch pipe (7) between the gas boosting device and the second regulating valve (8).

5. The air fractionation and rectification device for reducing the energy consumption of oxygen-rich liquid air transportation according to claim 1, characterized in that: The inlet end of the heat source channel of the main condenser evaporator (2) is connected to the top of the lower tower (3); a liquid nitrogen delivery main pipe (19) is provided on the inlet end of the heat source channel of the main condenser evaporator (2); the inlet end of a first liquid nitrogen delivery branch pipe (20), the inlet end of a second liquid nitrogen delivery branch pipe (21) and a fourth regulating valve (22) are sequentially provided on the liquid nitrogen delivery main pipe (19) in a direction from close to the main condenser evaporator (2) to far away from the main condenser evaporator (2); a fifth regulating valve (23) is provided on each of the first liquid nitrogen delivery branch pipe (20) and the second liquid nitrogen delivery branch pipe (21); the outlet end of the first liquid nitrogen delivery branch pipe (20) is connected to the lower tower (3), and the outlet end of the second liquid nitrogen delivery branch pipe (21) is connected to the upper tower (1).

6. The air fractionation and rectification device for reducing the energy consumption of oxygen-rich liquid air transportation according to claim 5, characterized in that: The upper tower (1) is provided with a finished nitrogen gas delivery pipe (24), and a second subcooler (25) is provided on the liquid nitrogen delivery main pipe (19) between the first liquid nitrogen delivery branch pipe (20) and the second liquid nitrogen delivery branch pipe (21) and the finished nitrogen gas delivery pipe (24).

7. The air fractionation and rectification device for reducing the energy consumption of oxygen-rich liquid air transportation according to claim 1, characterized in that: The invention also comprises a main heat exchanger (26), wherein the first compressed air delivery branch pipe (5) on the side of the second compressed air delivery branch pipe (7) away from the first regulating valve (6) is installed on the main heat exchanger (26), and a third compressed air delivery branch pipe (27) is arranged on the main heat exchanger (26), and a compressed air delivery main pipe (28) is arranged on the inlet end of the third compressed air delivery branch pipe (27) and the inlet end of the first compressed air delivery branch pipe (5), and the boosting end of a turbine expander (29) and a sixth regulating valve (30) are arranged in sequence on the third compressed air delivery branch pipe (27) along the direction from the compressed air delivery main pipe (28) to the main heat exchanger (26), and the outlet end of the third compressed air delivery branch pipe (27) is connected to the inlet end of the expansion end of the turbine expander (29), and the outlet end of the expansion end of the turbine expander (29) is connected to the upper tower (1).

Images