CN214075819U

CN214075819U - Energy-saving system for high-temperature oxygen-enriched flue gas purification and oxygen recycling

Info

Publication number: CN214075819U
Application number: CN202022892920.2U
Authority: CN
Inventors: 曾轲; 杨炯良; 李振东; 李伟; 胡学奎; 余浩; 梁东; 梁勇; 王毅; 邹康
Original assignee: Chengdu Yizhi Technology Co ltd
Current assignee: Chengdu Yizhi Technology Co ltd
Priority date: 2020-12-02
Filing date: 2020-12-02
Publication date: 2021-08-31
Anticipated expiration: 2030-12-02

Abstract

The utility model discloses an economizer system of high temperature oxygen boosting flue gas purification oxygen cyclic utilization, including the washing mechanism who inserts high temperature oxygen boosting flue gas, with washing system tube coupling's compressor unit, with compressor unit tube coupling's compressor export heat exchanger, with compressor export heat exchanger tube coupling's gas-liquid separation jar, with gas-liquid separation jar tube coupling's temperature swing adsorption isobaric drying mechanism and pressure swing adsorption purification mechanism insert the dust removal filtering mechanism of the gas after temperature swing adsorption isobaric drying mechanism and pressure swing adsorption purification mechanism handle to and be used for washing the cooling mechanism of mechanism and compressor export heat exchanger cooling to water. The utility model discloses a recovery cost is low, through with oxygen boosting flue gas etc. divide into two strands, the one carries out the thermal swing adsorption drying, and another strand carries out the pressure swing adsorption purification, can obtain high-purity oxygen, the cost of effectual reduction recovery after mixing two strands of product gas.

Description

Energy-saving system for high-temperature oxygen-enriched flue gas purification and oxygen recycling

Technical Field

The utility model relates to a gas separation technique and purification field, specifically say, relate to an economizer system of high temperature oxygen boosting flue gas purification oxygen cyclic utilization.

Background

The lithium ion battery has the advantages of high voltage, high energy density, low self-discharge efficiency, long cycle life, no memory effect, environmental protection and the like, so the lithium ion battery is widely applied to production and life. At present, a ternary cathode material (nickel cobalt lithium manganate) of a lithium battery is a novel cathode material and is prepared by taking nickel salt, cobalt salt and manganese salt as raw materials, and compared with other cathode materials, the ternary material has the most superior comprehensive performance and becomes the mainstream of the cathode material. The production process of the ternary positive electrode material comprises the steps of mixing a nickel compound, a cobalt compound and a manganese compound, preparing a ternary precursor at a high temperature, uniformly mixing the precursor with a lithium compound (lithium hydroxide or lithium carbonate), and sintering and synthesizing the precursor in an oxygen atmosphere. During the sintering process, the synthesis reaction can generate carbon dioxide and water vapor, so the generated high-temperature oxygen-enriched flue gas has components of carbon dioxide, water vapor and the like. In addition, the roller kiln synthesized by sintering is under micro negative pressure in the production process, mechanical gaps of the kiln body are more, and the oxygen-enriched smoke can suck air in the pumping process of the Roots blower, so that the oxygen-enriched smoke also contains nitrogen components.

Most of residual oxygen-enriched flue gas generated in the sintering process of the ternary cathode material of the lithium battery is directly discharged to the atmosphere as waste gas after being subjected to environment-friendly dust removal treatment, and the high-concentration oxygen in the oxygen-enriched flue gas is not considered to be purified and reused, so that the oxygen consumption is large in the production process, the energy consumption is high, and the production cost of mixed sintering is increased, so that the production cost of the cathode material of the lithium battery is increased. Only individual enterprises make oxygen-enriched flue gas recycling devices, although the production cost of the lithium battery anode material is reduced, a small amount of air is sucked before high-temperature oxygen-enriched flue gas is recycled, so that the oxygen recovery rate is low, and the recycling cost of a denitrification device is high, for example, in the prior art, the reference number "CN 108786371A" discloses a high-temperature oxygen-enriched flue gas recycling oxygen system and a recycling method thereof, which can purify and recycle the oxygen in the high-temperature oxygen-enriched flue gas, but does not process the nitrogen in the oxygen-enriched flue gas, can only process the high-temperature oxygen-enriched flue gas without nitrogen, and needs to rely on a nitrogen removal device, so that the required recycling cost is high; the recovery rate of oxygen is low, and the high-efficiency recovery of oxygen cannot be realized.

SUMMERY OF THE UTILITY MODEL

For overcoming the problems existing in the prior art, the utility model provides an energy-saving process system for purifying and recycling oxygen from high-temperature oxygen-enriched flue gas, which has low recovery cost, low recovery cost and high oxygen recovery rate.

In order to achieve the above object, the utility model adopts the following technical scheme:

an energy-saving system for purifying and recycling oxygen from high-temperature oxygen-enriched flue gas comprises a water washing mechanism connected with the high-temperature oxygen-enriched flue gas, a compressor unit connected with the water washing mechanism through a pipeline, a compressor outlet heat exchanger connected with the compressor unit through a pipeline, a gas-liquid separation tank connected with the pipeline of the compressor outlet heat exchanger, a temperature swing adsorption isobaric drying mechanism and a pressure swing adsorption purification mechanism connected with the pipeline of the gas-liquid separation tank, a dust removal filtering mechanism connected with the gas treated by the temperature swing adsorption isobaric drying mechanism and the pressure swing adsorption purification mechanism, and a cooling mechanism used for cooling the water washing mechanism and the compressor outlet heat exchanger, the output end of the temperature swing adsorption isobaric drying mechanism is connected with the output end pipeline of the pressure swing adsorption purification mechanism and is connected with the dust removal and filtration mechanism through a pipeline, and the pressure swing adsorption purification mechanism is connected with the washing mechanism.

Further, washing mechanism is including the flue gas intake pipe that is used for inserting high temperature oxygen boosting flue gas and fill the normal temperature water pipe into normal temperature water, respectively with flue gas intake pipe and normal temperature water piping connection's first washing tower, with drain pipe and the second washing tower that first washing tower is connected, and respectively with the pipeline of giving vent to anger that second washing tower and compressor unit are connected, wherein, cooling mechanism and second washing tower pipe connection, pressure swing adsorption purification mechanism is connected with first washing tower.

Specifically, the temperature swing adsorption isobaric drying mechanism comprises a drying air inlet pipe connected with a gas-liquid separation tank, a first gas pipe, a second gas pipe and a third gas pipe connected with the drying air inlet pipe, a fourth gas pipe connected with the third gas pipe, a first adsorption tower and a second adsorption tower respectively connected with the first gas pipe and the second gas pipe, a first output pipe and a second output pipe respectively connected with the bottoms of the first adsorption tower and the second adsorption tower, a dry product gas pipe respectively connected with the first output pipe and the second output pipe and used for outputting product gas, a predrying tower connected with the third gas pipe, a heater connected with the pipeline of the predrying tower, a fifth gas pipe with one end connected with the heater and the other end respectively connected with the first output pipe and the second output pipe through pipelines, and a condenser connected with the fourth gas pipe, a gas-liquid separator connected with the condenser pipeline, a sixth gas pipe connected between the third gas pipe and the fourth gas pipe, a seventh gas pipe with one end connected with the sixth gas pipe and the other end connected with the first output pipe and the second output pipe through pipelines, a plurality of first on-off valves respectively arranged on the first gas pipe, the second gas pipe, the third gas pipe, the fourth gas pipe, the first output pipe, the second output pipe, the connecting pipeline of the fifth gas pipe and the first output pipe, the connecting pipeline of the fifth gas pipe and the second output pipe, the connecting pipeline of the seventh gas pipe and the first gas pipe, and the connecting pipeline of the seventh gas pipe and the second gas pipe, and two second on-off valves arranged on the sixth gas pipe, wherein the gas-liquid separator is connected with the dry gas pipe through a pipeline, the seventh gas pipe is connected with the sixth gas pipe and is positioned between the two second on-off valves, and the dry product gas pipe is connected with an output end pipeline of the pressure swing adsorption purification mechanism.

Specifically, the pressure swing adsorption purification mechanism comprises a pressure swing adsorption air inlet pipe connected with a gas-liquid separation tank, a plurality of pressure swing adsorption towers with the bottoms connected with the pressure swing adsorption air inlet pipe, a pressure swing adsorption output air pipe connected with the top of the pressure swing adsorption tower, a pressure swing adsorption product air pipe connected with each pressure swing adsorption output air pipe and connected with a drying product air pipe, a pressure equalizing mechanism connected with each pressure swing adsorption output air pipe, a first regulating valve with two ends respectively connected with the pressure swing adsorption product air pipe and the pressure equalizing mechanism, a pressure swing adsorption exhaust pipe connected with the bottom of each pressure swing adsorption tower, a pressure swing adsorption recovery pipe with one end connected with the bottom of each pressure swing adsorption tower and the other end connected with a first water washing tower, a pressure swing adsorption air inlet pipe connected with the bottom of the pressure swing adsorption tower, a pressure swing adsorption recovery pipe connected with the pressure recovery pipe, a pressure recovery pipe connected with the bottom of each pressure swing adsorption output air pipe, a pressure recovery pipe connected with the pressure adsorption air inlet pipe, a pressure recovery pipe connected with the bottom of each pressure adsorption tower, a pressure recovery pipe, a pressure recovery, The third break valve on the connecting pipeline at the bottom of pressure swing adsorption exhaust pipe and pressure swing adsorption tower, on the connecting pipeline at the bottom of pressure swing adsorption recovery pipe and pressure swing adsorption tower, install in pressure regulating valve and dust removal filtration system on the pressure swing adsorption product trachea install in recovery regulating valve on the pressure swing adsorption recovery pipe, and install in vacuum pump on the pressure swing adsorption exhaust pipe, wherein, pressure swing adsorption product trachea is connected with dust removal filtration mechanism.

Specifically, the pressure equalizing mechanism comprises a plurality of pressure equalizing pipes respectively connected with each pressure swing adsorption output gas pipe pipeline, and a pressure equalizing switching valve arranged on a connecting pipeline of the pressure equalizing pipes and each pressure swing adsorption output gas pipe, wherein the first regulating valve is connected with one pressure equalizing pipe.

Specifically, the number of the pressure swing adsorption towers is at least 3.

Specifically, the cooling mechanism connection comprises a water chilling unit connected with a compressor outlet heat exchanger pipeline and a low-temperature heat exchanger respectively connected with the water chilling unit and a second washing tower pipeline.

The process of the energy-saving system for purifying the oxygen from the high-temperature oxygen-enriched flue gas and recycling the oxygen comprises the following steps:

s1, washing: washing the accessed high-temperature oxygen-enriched flue gas by a washing mechanism to obtain low-temperature oxygen-enriched mixed gas, and inputting the low-temperature oxygen-enriched mixed gas into a compressor unit;

s2, compression and condensation: compressing the low-temperature oxygen-enriched mixed gas in a compressor unit, heating, inputting the compressed low-temperature oxygen-enriched mixed gas into a heat exchanger at the outlet of the compressor for heat exchange and cooling, and inputting the cooled gas into a gas-liquid separation tank for gas-liquid separation to obtain high-pressure low-temperature oxygen-enriched mixed gas;

s3, temperature swing adsorption isobaric drying and pressure swing adsorption purification: the method comprises the following steps of (1) dividing high-pressure low-temperature oxygen-enriched mixed gas into two equal parts by adopting a temperature swing adsorption isobaric drying and pressure swing adsorption purification parallel process, inputting one part into a temperature swing adsorption isobaric drying mechanism for drying, and removing redundant water to obtain low dew point oxygen-enriched flue gas; the other strand is input into a pressure swing adsorption purification mechanism to remove redundant water, carbon dioxide and nitrogen to obtain low dew point high purity oxygen, and the low dew point oxygen-enriched flue gas and the low dew point high purity oxygen are mixed and then input into a dedusting filtering mechanism;

and S4, performing dust removal and filtration on the mixed gas of the low dew point oxygen-enriched flue gas and the low dew point high-purity oxygen through a dust removal and filtration mechanism, and outputting the mixed gas as product gas.

Further, the temperature swing adsorption isobaric drying of the step S3 includes the following steps:

a1, hot blowing: treating a part of high-pressure low-temperature oxygen-enriched mixed gas from a drying gas inlet pipe by a pre-drying tower and a heater in sequence to heat the gas to 150-170 ℃, inputting the gas into a second adsorption tower for hot blowing, cooling by a condenser and a gas-liquid separator in sequence after the hot blowing, separating liquid water, inputting the gas into a drying gas inlet pipe, conveying the gas into a first adsorption tower for adsorption, and outputting the gas from a dry product gas main pipe after the gas is adsorbed by the first adsorption tower;

a2, cold blowing: a part of high-pressure low-temperature oxygen-enriched mixed gas is sequentially subjected to cold blowing in a second adsorption tower from a drying gas inlet pipe, conveyed to a heater and heated to 150-170 ℃, then conveyed to a pre-drying tower for heating and regeneration treatment, sequentially cooled in a condenser and a gas-liquid separator and separated into liquid water after treatment, finally conveyed to a drying gas inlet pipe and conveyed to a first adsorption tower for adsorption, and the gas is adsorbed in the first adsorption tower and then output from a dry product gas main pipe;

a3, exchanging the work of the first adsorption tower and the second adsorption tower, so that the first adsorption tower is subjected to hot blowing and cold blowing in sequence, the second adsorption tower is subjected to adsorption, and the other adsorbed products are output from a dry product gas main pipe;

a4, repeating the steps A1-A3 to realize the continuous drying of the high-pressure low-temperature oxygen-enriched mixed gas.

Further, the pressure swing adsorption purification of step S3 includes the following steps:

b1, adsorption: inputting high-pressure low-temperature oxygen-enriched mixed gas into a pressure swing adsorption tower from bottom to top from a pressure swing adsorption gas inlet pipe, inputting product gas into a pressure swing adsorption product gas pipe from the top of the pressure swing adsorption tower through a pressure swing adsorption output gas pipe after the product gas is adsorbed by the pressure swing adsorption tower, and finally inputting the product gas into a dust removal filtering mechanism;

b2, pressure equalizing and reducing: inputting the high-pressure gas in the pressure swing adsorption tower after adsorption into the other pressure swing adsorption tower through a pressure equalizing mechanism to balance the air pressure of the two towers;

b3, reverse playing: against the adsorption direction, inputting the gas in the pressure-equalizing and pressure-reducing pressure-swing adsorption tower into a first water scrubber through a pressure-swing adsorption recovery pipe for recovery, and reducing the pressure in the pressure-swing adsorption tower to the normal pressure;

b4, vacuumizing: against the adsorption direction, pumping out the gas in the pressure swing adsorption tower after reverse release through a vacuum pump and discharging the gas from a pressure swing adsorption exhaust pipe;

b5, voltage equalizing and boosting: after the vacuum pumping is finished, the pressure swing adsorption tower receives the high-pressure gas output by the pressure swing adsorption tower in the step B2 through a pressure equalizing mechanism, and the pressure of the two towers is balanced;

b6, final liter: the product gas is input into the pressure swing adsorption tower after pressure equalization and boosting sequentially through a pressure swing adsorption product gas pipe, a first regulating valve, a pressure equalization mechanism and a pressure swing adsorption output gas pipe, so that the gas pressure in the pressure swing adsorption tower (31) is uniformly boosted to the adsorption pressure;

b7, repeating the steps B1-B6, and continuously removing water, carbon dioxide and nitrogen from the high-pressure low-temperature oxygen-enriched mixed gas in the pressure swing adsorption purification mechanism.

Compared with the prior art, the utility model discloses following beneficial effect has:

(1) the utility model discloses it is with low costs to the recovery of oxygen, get into the isobaric drying mechanism of temperature swing adsorption with 50% oxygen boosting flue gas, remaining 50% oxygen boosting flue gas gets into pressure swing adsorption purification mechanism, the product gas after two systems are handled is sent into dust removal filtration system after mixing, the operation can adopt pressure swing adsorption denitrogenation to 50% oxygen boosting flue gas through pressure swing adsorption purification mechanism like this and handle, can deviate from nitrogen gas and water in the raw material gas (oxygen boosting flue gas), and do not rely on the device of outside desorption nitrogen gas (its oxygen rate of recovery is not high), consequently if all adopt pressure swing adsorption denitrogenation to handle can reduce the holistic oxygen rate of recovery of system, and adopt pressure swing adsorption denitrogenation to 50% oxygen boosting flue gas and handle, adopt the isobaric drying process of temperature swing adsorption again with other 50% oxygen boosting flue gas, and handle the gas mixture after both, can make oxygen purity satisfy the demand (be greater than 98.5%), effectively improves the oxygen recovery rate (can improve about 8%).

(2) The utility model discloses a pressure swing adsorption purification mechanism adopts the oxygen recovery rate that pressure swing adsorption denitrogenation can also improve (can improve about 8%) to 50% oxygen boosting flue gas, this is because carry out the pressure swing adsorption purification to 50% oxygen boosting flue gas and can obtain the oxygen that purity is greater than 99.2%, simultaneously through carrying out the isobaric drying process of temperature swing adsorption to other 50% oxygen boosting flue gas, because temperature swing adsorption mainly is the water in the desorption oxygen boosting flue gas, the process flow adopts isobaric drying, the regenerating gas adopts a small part of oxygen boosting flue gas, after regenerating, high temperature oxygen boosting flue gas cooling separates the liquid water back to return to the temperature swing adsorption entry again, dry after converging with most oxygen boosting flue gas, the whole flow does not have the gas of emptying, the regenerating gas is only through after rising temperature and analyzing water and after cooling liquefied water become liquid water in the oxygen boosting flue gas and separate from the mechanism in gaseous water, therefore the yield is greater than 99.9%, the oxygen yield of the treatment is high; and finally, mixing the product gas after the temperature swing adsorption isobaric drying treatment and the pressure swing adsorption purification treatment to obtain oxygen with the purity of more than 98.5%, and meanwhile, freely selecting temperature swing adsorption drying or pressure swing adsorption purification according to the components of the oxygen-enriched flue gas, so that the flexibility of the device is increased, the oxygen recovery rate is improved, and the economic benefit of enterprises is obviously improved.

(3) The utility model discloses a recovery cost is low, and temperature swing adsorption drying technology is advanced, and easy operation compares the pressure swing adsorption purification and has the characteristics that the construction investment is economized, area is little, the yield is high, through dividing the oxygen boosting flue gas etc. into two strands, one carries out the temperature swing adsorption drying, and another strand carries out the pressure swing adsorption purification, can obtain high-purity oxygen after mixing two strands of product gas, can compensate the problem that the pressure swing adsorption purification is with high costs, the rate of recovery is low to the cost of effectual reduction recovery.

(3) The utility model discloses in the temperature swing adsorption drying process, use through the cooperation of first adsorption tower, second adsorption tower and predrying tower to rely on moisture in condenser and vapour and liquid separator further separation oxygen boosting flue gas. The adsorbent bed layer is subjected to hot blowing, cold blowing and adsorption, the principle is that moisture is adsorbed by the adsorbent in the first adsorption tower or the second adsorption tower at low temperature, and the moisture adsorbed by the adsorbent is resolved out at high temperature, so that after the adsorbent is saturated in adsorption, the adsorbent bed layer is heated in a hot blowing mode firstly, the moisture adsorbed by the adsorbent is resolved out, and the adsorbent is thoroughly regenerated. After the hot blowing is finished, because the bed temperature of the adsorbent is higher, the adsorption performance of the adsorbent is poorer, the temperature of the adsorbent bed is reduced to normal temperature in a cold blowing mode, then the adsorbent bed is in a conversion adsorption state, no oxygen is lost in the whole process, and the regenerated water vapor is cooled and then becomes condensed water to be separated from the gas.

(4) The utility model discloses in the pressure swing adsorption purification process, through the cooperation of uniform pressure pipeline, pressure swing adsorption tower, obtain the oxygen that purity is greater than 99.2%, put the in-process in the contrary, by absorbent impurity desorption from the adsorbent, the desorption gas that releases in the contrary contains partial oxygen and returns to first scrubbing tower and reprocess, has increased the system oxygen rate of recovery, has improved adsorbent availability factor simultaneously, the lowering system cost.

(5) The utility model discloses a dust removal filtering mechanism carries out filtration treatment through its product gas mixture after to the isobaric drying process of temperature swing adsorption and the purification of pressure swing adsorption, and the product gas that obtains at last simultaneously removes dust through dust removal filtration system, obtains the final gas of product oxygen dust content less than or equal to 1 mu m, and effectual improvement product oxygen quality widens the product usage.

(6) The utility model removes the dust particles in the mixed gas through the washing mechanism, and mainly removes the dust particles in the mixed gas through the normal temperature water washing of the first washing tower, thereby avoiding the harm of corrosion and abrasion to equipment and pipelines caused by the deposition of the rear-section low-temperature water particles; the second water washing tower is washed by low-temperature water to reduce the temperature, so that the water vapor content of the oxygen-enriched flue gas is reduced, the volume flow of the oxygen-enriched flue gas is reduced, and the energy consumption of the rear-section compression work is reduced; no condensed water is separated out in the compression process, so that the abrasion in the compression process of the oxygen compressor is reduced; after compression, low-temperature condensation is used, so that the water removal load of temperature change and pressure swing adsorption at the later stage can be reduced, and the total energy consumption of the system is reduced.

Drawings

Fig. 1 is a flow chart of the system of the present invention.

Fig. 2 is a connection structure diagram of the temperature swing adsorption isobaric drying mechanism of the utility model.

Fig. 3 is a connection structure diagram of the pressure swing adsorption purification mechanism of the present invention.

Fig. 4 is a connection structure diagram of a pressure swing adsorption purification mechanism in embodiment 3 of the present invention.

Wherein, the names corresponding to the reference numbers are:

1-a compressor unit, 2-a compressor outlet heat exchanger, 3-a gas-liquid separation tank, 4-a dedusting filter mechanism, 5-a flue gas inlet pipe, 6-a normal temperature water pipe, 7-a first water washing tower, 8-a water discharge pipe, 9-a second water washing tower, 10-a gas outlet pipeline, 11-a dry gas inlet pipe, 12-a first gas pipe, 13-a second gas pipe, 14-a third gas pipe, 15-a fourth gas pipe, 16-a first adsorption tower, 17-a second adsorption tower, 18-a first output pipe, 19-a second output pipe, 20-a dry product gas pipe, 21-a pre-drying tower, 22-a heater, 23-a fifth gas pipe, 24-a condenser, 25-a gas-liquid separator, 26-a sixth gas pipe, 27-a seventh gas pipe, 28-a first on-off valve, 29-a second on-off valve, 30-a pressure swing adsorption air inlet pipe, 31-a pressure swing adsorption tower, 32-a pressure swing adsorption air outlet pipe, 33-a pressure swing adsorption product air pipe, 34-a first regulating valve, 35-a pressure swing adsorption air outlet pipe, 36-a pressure swing adsorption recovery pipe, 37-a third on-off valve, 38-a pressure regulating valve, 39-a recovery regulating valve, 40-a vacuum pump, 41-a pressure equalizing pipe, 42-a pressure equalizing switching valve, 43-a water chilling unit, 44-a low temperature heat exchanger, 45-a temperature swing adsorption isobaric drying mechanism, 46-a pressure swing adsorption purification mechanism and 47-a dust removal filtering system.

Detailed Description

The present invention will be further described with reference to the following description and examples, which include but are not limited to the following examples.

Example 1

As shown in fig. 1 to 3, the energy saving system for the high-temperature oxygen-enriched flue gas purification and oxygen recycling comprises a water washing mechanism, a compressor unit 1, a compressor outlet heat exchanger 2, a gas-liquid separation tank 3, a temperature swing adsorption isobaric drying mechanism 45, a pressure swing adsorption purification mechanism 46, a dust removal filtering mechanism 4, a cooling mechanism and the like.

The water washing mechanism is used for removing dust particles in mixed gas and comprises a flue gas inlet pipe 5, a normal-temperature water pipe 6, a first water washing tower 7, a drain pipe 8, a second water washing tower 9 and an air outlet pipeline 10. The flue gas inlet pipe 5 is used for accessing flue gas of external high-temperature oxygen-enriched flue gas and is connected with an air inlet of the first water scrubber 7; the normal-temperature water pipe 6 is connected to a water inlet at the upper part of the first water washing tower 7 and is used for filling normal-temperature water into the first water washing tower 7, so that the first water washing tower 7 is filled with enough normal-temperature water to reduce the temperature of the high-temperature oxygen-enriched flue gas; regular packing is filled in the first washing tower 7 and used for removing dust particles in the mixed gas, so that the damage of corrosion and abrasion of equipment and pipelines caused by the deposition of low-temperature water particles at the rear section is avoided, the temperature of high-temperature oxygen-enriched flue gas is reduced by normal-temperature water, and an air inlet of the first washing tower is connected with a pressure swing adsorption recovery pipe 36 and used for retreating the flue gas purified and recovered by pressure swing adsorption; the drain pipe 8 is connected with a water outlet at the bottom and used for automatically returning water and discharging the used normal-temperature water; the air inlet of the second water scrubber 9 is connected with the air outlet of the first water scrubber 7, and is used for reducing the water vapor content of the low-temperature oxygen-enriched flue gas treated by the first water scrubber 7, the volume flow of the oxygen-enriched flue gas and reducing the energy consumption of the compression work of the rear section, the water inlet and the water outlet of the second water scrubber are respectively connected with the hot side water outlet and the hot side water inlet of the low-temperature heat exchanger 44 through pipelines and are used for inputting and outputting heat exchange water in the low-temperature heat exchanger 44, and the oxygen-enriched flue gas treated by the secondary water scrubbing is input into the air outlet pipeline 10; one end of the gas outlet pipeline 10 is connected with the gas outlet of the second washing tower 9, and the other end of the gas outlet pipeline is connected with the gas inlet of the compressor unit 1, and is used for outputting the oxygen-enriched flue gas to the compressor unit 1 for processing.

The compressor unit 1 is used for compressing the oxygen-enriched flue gas and then conveying the oxygen-enriched flue gas to the compressor outlet heat exchanger 2.

The compressor outlet heat exchanger 2 is used for exchanging heat for oxygen-enriched flue gas, a gas outlet at the hot side of the compressor is connected with an inlet of the gas-liquid separation tank 3 through a pipeline, and a water outlet and a water inlet of the compressor are respectively connected with a water inlet and a water outlet of the water chilling unit 43 through pipelines.

The gas-liquid separation tank 3 is connected with the oxygen-enriched flue gas after heat exchange to separate the moisture in the oxygen-enriched flue gas and improve the purity of the oxygen-enriched flue gas, and an exhaust port of the gas-liquid separation tank is connected with a drying gas inlet pipe 11 and a pressure swing adsorption gas inlet pipe 30 through pipelines and is used for inputting the separated oxygen-enriched flue gas into a temperature swing adsorption isobaric drying mechanism 45 and a pressure swing adsorption purification mechanism 46 for processing.

The temperature swing adsorption isobaric drying mechanism 45 comprises a drying air inlet pipe 11, a first air inlet pipe 12, a second air inlet pipe 13, a third air inlet pipe 14, a fourth air inlet pipe 15, a first adsorption tower 16, a second adsorption tower 17, a first output pipe 18, a second output pipe 19, a dried product air pipe 20, a pre-drying tower 21, a heater 22, a fifth air inlet pipe 23, a condenser 24, a gas-liquid separator 25, a sixth air inlet pipe 26, a seventh air inlet pipe 27, a first on-off valve 28 and a second on-off valve 29. Wherein, the dry gas inlet pipe 11 is connected with the gas outlet of the gas-liquid separation tank 3 and is used for accessing oxygen-enriched flue gas to be processed; one end of a first air delivery pipe 12 is connected with the drying air inlet pipe 11, the other end of the first air delivery pipe is connected with the first adsorption tower 16 and used for delivering air, and a first on-off valve 28 for controlling the on-off of a pipeline is arranged on the first air delivery pipe; one end of a second gas pipe 13 is connected with the drying gas inlet pipe 11, the other end of the second gas pipe is connected with a second adsorption tower 17 and used for conveying gas, and a first on-off valve 28 for controlling the on-off of a pipeline is arranged on the second gas pipe; one end of a third air delivery pipe 14 is connected with the drying air inlet pipe 11, the other end of the third air delivery pipe is connected with the pre-drying tower 21 and used for delivering air, and a first on-off valve 28 for controlling the on-off of a pipeline is arranged on the third air delivery pipe; the fourth air pipe 15 is connected with the third air pipe 14, is connected with the condenser 24 and is provided with a first on-off valve 28 for controlling the on-off of the pipeline; the first adsorption tower 16 and the second adsorption tower 17 are used for adsorbing gas; the first output pipe 18 is connected to the bottom of the first adsorption tower 16 and is used for outputting the adsorbed gas to a dry product gas main pipe 20, and a first on-off valve 28 for controlling the on-off of the pipeline is mounted on the first output pipe; the second output pipe 19 is connected to the bottom of the second adsorption tower 17, and is used for outputting the adsorbed gas to a dry product gas main pipe 20, and a first on-off valve 28 for controlling the on-off of the pipeline is mounted on the second output pipe; the dry product gas pipe 20 is connected with the pressure swing adsorption output gas pipe 32, so that the temperature swing adsorption isobaric dry gas and the pressure swing adsorption purified gas are mixed and then are input into the dust removal filtering mechanism 4 for dust removal and filtration; the pre-drying tower 21 is used for drying the gas again to remove moisture in the gas, and is connected with the heater 22 through a pipeline; the heater 22 is used for heating the gas to 150-170 ℃, and two ends of the heater are respectively connected with the fifth gas transmission pipe 23 and the pre-drying tower 21 and used for outputting the gas; the fifth gas pipe 23 is respectively connected with the first output pipe 18 and the second output pipe 19 through pipelines and is used for conveying gas, a first on-off valve 28 for controlling the on-off of the pipeline is arranged on a connecting pipeline of the fifth gas pipe 23 and the first output pipe 18, and a first on-off valve 28 for controlling the on-off of the pipeline is arranged on a connecting pipeline of the fifth gas pipe and the second output pipe 19; one end of the condenser 24 is connected with the fourth gas transmission pipe 15, and the other end is connected with the gas-liquid separator 25, and the condenser is used for condensing the gas and sending the gas to the gas-liquid separator 25 for separating moisture again to ensure the purity of the gas; the gas-liquid separator 25 is used for separating gas moisture and conveying the separated gas back to the drying gas inlet pipe 11 for retreatment, and the separated condensed water is discharged out of the system; the sixth air delivery pipe 26 is connected between the third air delivery pipe 14 and the fourth air delivery pipe 15; one end of the seventh air pipe 27 is connected with the sixth air pipe 26, the other end of the seventh air pipe is connected with the first air pipe 12 and the second air pipe 13 through pipelines, a first on-off valve 28 for controlling the on-off of the pipelines is arranged on a connecting pipeline of the seventh air pipe 27 and the first air pipe 12, and a first on-off valve 28 for controlling the on-off of the pipelines is arranged on a connecting pipeline of the seventh air pipe 27 and the second air pipe 13; the first on-off valves 28 are used for controlling the on-off of the pipeline, and the number of the first on-off valves is multiple; the second shut-off valves 29 are 2 in number and are installed on both sides of the seventh air delivery pipe 27.

The pressure swing adsorption purification mechanism 46 comprises a pressure swing adsorption gas inlet pipe 30, a pressure swing adsorption tower 31, a pressure swing adsorption gas outlet pipe 32, a pressure swing adsorption product gas pipe 33, a pressure equalizing mechanism, a pressure swing adsorption gas outlet pipe 35, a pressure swing adsorption recovery pipe 36, a third cut-off valve 37, a pressure regulating valve 38, a dust removal filtration system 47, a recovery regulating valve 39 and a vacuum pump 40. Wherein, the pressure swing adsorption inlet pipe 30 is connected with the air outlet of the gas-liquid separation tank 3, and is connected with the bottom of each pressure swing adsorption tower 31 through a pipeline, and a third cut-off valve 37 is arranged on the connecting pipeline of the pressure swing adsorption tower 31; the number of the pressure swing adsorption towers 31 is multiple and at least 3, one end of each pressure swing adsorption tower is connected with a pressure swing adsorption air inlet pipe 30 through a pipeline, and the other end of each pressure swing adsorption tower is connected with a pressure swing adsorption output air pipe 32 through a pipeline; the pressure swing adsorption output gas pipe 32 is used for outputting the gas after the adsorption treatment to a pressure swing adsorption product gas pipe 33; the pressure swing adsorption product gas pipe 33 is connected with the dust removal filtering mechanism 4; the pressure equalizing mechanism is used for equalizing the pressure of each pressure swing adsorption tower 31 and comprises at least 2 pressure equalizing pipes 41, each pressure equalizing pipe 41 is not connected with each other, each pressure equalizing pipe 41 is connected with each pressure swing adsorption tower 31 through a pipeline, and a pressure equalizing switching valve 42 is arranged on a connecting pipeline of each pressure equalizing pipe 41 and each pressure swing adsorption tower 31; the pressure swing adsorption exhaust pipe 35 is connected with each pressure swing adsorption tower 31 through a pipeline, a third cut-off valve 37 for controlling the on-off of the pipeline is arranged on the pipeline connected with each pressure swing adsorption tower 31, and a vacuum pump 35 for outputting external exhaust gas is arranged on the third cut-off valve; the pressure swing adsorption recovery pipe 36 is connected with each pressure swing adsorption tower 31 through a pipeline, a third cut-off valve 37 for controlling the on-off of the pipeline is arranged on the pipeline connected with each pressure swing adsorption tower 31, a recovery regulating valve 39 is arranged on the third cut-off valve and used for controlling the on-off of the pipeline of the pressure swing adsorption recovery pipe 36, and the other end of the third cut-off valve is connected with the air inlet of the first washing tower 7; the pressure regulating valve 38 is installed on the pressure swing adsorption product gas pipe 33, and is used for stabilizing the gas pressure; the dust removal filtration system 47 is installed on the pressure swing adsorption product gas pipe 33, and is used for filtering the product gas to further ensure the purity of the output gas.

The dust removal filtering mechanism 4 is connected with a pressure swing adsorption product gas pipe 33 and is used for enabling product oxygen to enter a dust removal filtering system 47, so that the dust content of the product oxygen is less than or equal to 1 mu m, and the final product oxygen is transported out through a pipeline for cyclic utilization.

Example 2

As shown in FIGS. 1 to 3, the process of the energy-saving system for purifying oxygen from high-temperature oxygen-enriched flue gas and recycling oxygen comprises the following steps:

s1, washing: 16000Nm of high-temperature oxygen-enriched flue gas (80 ℃, oxygen concentration of 95-96%, water content of 1-2%, carbon dioxide content of 100ppm, nitrogen and argon content of 2%)³H and 32 ℃ normal temperature water of 30m³The water enters a first water washing tower 7 through a flue gas inlet pipe 5 and a normal temperature water pipe 6 respectively, under the action of regular packing, normal temperature water is used as washing water to wash the high temperature oxygen-enriched flue gas to remove particle impurities in the high temperature oxygen-enriched flue gas, meanwhile, the high temperature oxygen-enriched flue gas is contacted with the washing water to exchange heat to obtain 35 ℃ oxygen-enriched mixed gas, the washing water after heat exchange automatically flows back through a drain pipe 8,the oxygen-rich mixed gas enters a second water scrubber 9 through a gas path, and is mixed with 7 ℃ low-temperature water 33m from a low-temperature heat exchanger 44 under the action of a structured packing³The low-temperature washing water is subjected to contact heat exchange to obtain oxygen-rich mixed gas with the temperature lower than 12 ℃, and the oxygen-rich mixed gas with the temperature lower than 12 ℃ is output from the top of the second water washing tower 9 through an air outlet pipeline 10;

the washing water of the first water washing tower 7 is subjected to a first closed cycle, and the first closed cycle is specifically: the normal-temperature water at 32 ℃ outside the boundary region enters a first water washing tower 7 through a normal-temperature water pipe 6, in the first water washing tower 7, washing water and oxygen-enriched flue gas at 80 ℃ are subjected to normal-temperature contact washing heat exchange under the action of structured packing, and the washing water after washing heat exchange automatically flows back through a drain pipe 8;

the washing water at 7 ℃ of the second water washing tower 9 is subjected to a second closed cycle, and the second closed cycle specifically comprises: washing water returning water of the second washing tower 9 enters the hot side of the low-temperature heat exchanger 44 through a pipeline, low-temperature water obtained through heat exchange returns to the second washing tower 9 through a pipeline, in the second washing tower 9, washing water at 7 ℃ performs low-temperature contact heat exchange with oxygen-rich mixed gas discharged from the first washing tower 7 under the action of structured packing, and the washing water after low-temperature heat exchange is conveyed to the hot side of the low-temperature heat exchanger 44 through a pipeline;

in this step, the cold side of the cryogenic heat exchanger G2 is subjected to a first cold side closed loop cycle, and the first cold side closed loop cycle is specifically: the low-temperature water prepared by the water chilling unit 43 enters the cold side of the low-temperature heat exchanger 44 through a pipeline, and the medium-temperature water obtained by heat exchange returns to the inlet of the water chilling unit 43 through the pipeline.

S2, compression and condensation: the oxygen-enriched mixed gas which is obtained after water washing and temperature reduction and is lower than 12 ℃ enters a compressor unit 1 through an air outlet pipeline 10 to be compressed to obtain 0.4MPa.G oxygen-enriched mixed gas, the 0.4MPa.G oxygen-enriched mixed gas enters a hot side of a heat exchanger 2 at an outlet of a compressor through a pipeline to perform wall type heat exchange with low-temperature water at the cold side of the heat exchanger to obtain the oxygen-enriched mixed gas and condensed water which are lower than 15 ℃, the 0.4MPa.G oxygen-enriched mixed gas and the condensed water which are lower than 15 ℃ enter a gas-liquid separation tank 3 through pipelines to perform gas-liquid separation, the condensed water is discharged from a water outlet at the bottom of the gas-liquid separation tank 3 through the pipeline to be recovered, and the 0.4MP.G oxygen-enriched mixed gas at the temperature of 15 ℃ is output to;

the cold side water of the compressor outlet heat exchanger 2 is subjected to a second cold side closed loop circulation, and the second cold side closed loop circulation specifically comprises the following steps: the low-temperature water prepared by the water chilling unit 43 enters the cold side of the compressor outlet heat exchanger 2 through a pipeline, and the medium-temperature water obtained through heat exchange returns to the inlet of the water chilling unit 43 through the pipeline.

S3, temperature swing adsorption isobaric drying and pressure swing adsorption purification: the method comprises the following steps of (1) dividing high-pressure low-temperature oxygen-enriched mixed gas into two gas sources by adopting a temperature swing adsorption isobaric drying and pressure swing adsorption purification parallel process, wherein one gas source enters a temperature swing adsorption isobaric drying mechanism 45 to remove redundant water to obtain low dew point oxygen-enriched flue gas, and the low dew point oxygen-enriched flue gas is output through a dry product gas main pipe 20; the other strand enters a pressure swing adsorption purification mechanism 46 to remove redundant water, carbon dioxide and nitrogen to obtain low dew point high purity oxygen, the low dew point high purity oxygen is output through a pressure swing adsorption product gas pipe 33, the low dew point oxygen-enriched flue gas output through a drying product gas main pipe 20 is input into the pressure swing adsorption product gas pipe 33 and mixed with the low dew point high purity oxygen output by the pressure swing adsorption product gas pipe 33, the purity of the final product oxygen is larger than 98.5%, and the mixed gas is input into a dust removal filtering mechanism 4.

S4, dedusting and filtering, wherein the product oxygen with the purity of more than 98.5 percent enters the dedusting and filtering mechanism 4, the dust content of the product oxygen is less than or equal to 1 mu m, and the final product oxygen is output for cyclic utilization through a pipeline P9.

The cycle time sequence of the temperature swing adsorption isobaric drying mechanism 45 is shown in table 1, and the specific working steps are as follows:

step a1, adsorption in the first adsorption tower 16, hot blowing in the second adsorption tower 17: a part of the oxygen-rich gas mixture is conveyed to the first adsorption tower 16 from the drying gas inlet pipe 11 through the first on-off valve 28, moisture in the oxygen-rich gas mixture is adsorbed, dehydrated and dried in the first adsorption tower 16, and the dried gas is output to the pressure swing adsorption product gas pipe 33 for mixing through the first output pipe 18 and the dried product gas main pipe 20 in sequence; conveying another part of the oxygen-enriched mixed gas to a pre-drying tower 21 through a third gas conveying pipe 14 for pre-drying, heating the oxygen-enriched mixed gas to 150-170 ℃ through a heater 22, then feeding the oxygen-enriched mixed gas into a second adsorption tower 17 from a fifth gas conveying pipe 23, carrying out hot blowing on the second adsorption tower 17 for 4 hours continuously, feeding the hot-blown mixed gas into a condenser 24 through a seventh gas conveying pipe 27, a sixth gas conveying pipe 26 and a fourth gas conveying pipe 15 in sequence, condensing the mixed gas in the condenser 24 to obtain moisture, discharging the moisture out of the system through a gas-liquid separator 25, and returning the rest of the mixed gas to the drying gas inlet pipe 11 from the top of the gas-liquid separator 25;

step a2, adsorption by the first adsorption tower 16, cold blowing by the second adsorption tower 17: a part of the oxygen-rich gas mixture is conveyed to the first adsorption tower 16 from the drying gas inlet pipe 11 through the first on-off valve 28, moisture in the oxygen-rich gas mixture is adsorbed, dehydrated and dried in the first adsorption tower 16, and the dried gas is output to the pressure swing adsorption product gas pipe 33 for mixing through the first output pipe 18 and the dried product gas main pipe 20 in sequence; the other part of the oxygen-enriched mixed gas is input into the second gas pipe 13 through the third gas pipe 14, the sixth gas pipe 26 and the seventh gas pipe 27 in sequence, finally enters the second adsorption tower 17, cold blowing is carried out on the second adsorption tower 17, cold blowing lasts for 1-4 hours, the mixed gas after cold blowing sequentially passes through the second output pipe 19 and the fifth gas pipe 23, enters the heater 22, the mixed gas enters the pre-drying tower 21 after being heated, hot blowing is carried out on the pre-drying tower 21, the mixed gas after hot blowing sequentially passes through the third gas pipe 14 and the fourth gas pipe 15 and enters the condenser 24, the mixed gas is condensed out of the system through the condenser 24, moisture is discharged out of the system through the gas-liquid separator 25, and the rest mixed gas returns to the drying gas inlet pipe 11 from the top of the gas-liquid separator 25;

step a3, adsorbing by the second adsorption tower 17, hot blowing by the first adsorption tower 16: a part of the oxygen-enriched mixed gas is conveyed to the second adsorption tower 17 from the drying air inlet pipe 11 through the second air conveying pipe 13, moisture in the oxygen-enriched mixed gas is adsorbed, dehydrated and dried in the second adsorption tower 17, and the dried gas is output to the pressure swing adsorption product air pipe 33 through the second output pipe 19 and the dried product air main pipe 20 to be mixed; conveying another part of the oxygen-enriched mixed gas to a pre-drying tower 21 through a third gas conveying pipe 14 for pre-drying, heating the oxygen-enriched mixed gas to 150-170 ℃ through a heater 22, then sequentially entering a first adsorption tower 16 through a fifth gas conveying pipe 23 and a first output pipe 18, performing hot blowing on the first adsorption tower 16 for 4 hours continuously, sequentially entering a condenser 24 through a seventh gas conveying pipe 27, a sixth gas conveying pipe 26 and a fourth gas conveying pipe 15, condensing the mixed gas to obtain moisture, discharging the moisture out of the system through a gas-liquid separator 25, and returning the rest of the mixed gas to the drying gas inlet pipe 11 from the top of the gas-liquid separator 25;

step a4, adsorbing by the second adsorption tower 17, cold blowing by the first adsorption tower 16: a part of the oxygen-enriched mixed gas is conveyed to the second adsorption tower 17 from the drying air inlet pipe 11 through the second air conveying pipe 13, moisture in the oxygen-enriched mixed gas is adsorbed, dehydrated and dried in the second adsorption tower 17, and the dried gas is output to the pressure swing adsorption product air pipe 33 through the second output pipe 19 and the dried product air main pipe 20 to be mixed; the other part of the oxygen-rich mixed gas is sequentially input into the first adsorption tower 16 through a third gas pipe 14, a sixth gas pipe 26 and a seventh gas pipe 27, cold blowing is carried out on the first adsorption tower 16, cold blowing is continuously carried out for 1-4 hours, the cold-blown mixed gas sequentially passes through a first output pipe 18 and a fifth output pipe 23 and enters a heater 22, the mixed gas enters the pre-drying tower 21 after being heated, hot blowing is carried out on the pre-drying tower 21, the hot-blown mixed gas sequentially passes through the third gas pipe 14 and the fourth gas pipe 15 and enters a condenser 24, the mixed gas is condensed to generate moisture in the condenser 24, the moisture is discharged out of the system through a gas-liquid separator 25, and the rest of the mixed gas returns to the drying gas inlet pipe 11 from the top of the gas-liquid separator 25;

and step A5, repeating the steps A1-A4 to realize continuous drying of the high-pressure low-temperature oxygen-enriched mixed gas to obtain the mixed gas with the dew point lower than-47 ℃ and the water content lower than 50 ppm.

TABLE 1

The cycle sequence of the pressure swing adsorption purification mechanism 46 is shown in table 2, and the specific working steps are as follows:

the pressure swing adsorption column 31 has 6 stages (FT1, FT2, FT3, FT4, FT5, and FT6), and the whole process steps of the main process will be described by taking one pressure swing adsorption column 31(FT1) as an example, and the process steps of the remaining pressure swing adsorption columns 31 are completely the same.

Step B1, adsorption: the high-pressure low-temperature oxygen-enriched mixed gas conveyed from the pressure swing adsorption gas inlet pipe 30 enters a pressure swing adsorption tower 31(FT1) through a pipeline, wherein water, carbon dioxide and nitrogen impurity components are selectively adsorbed by a plurality of adsorbents filled in the pressure swing adsorption tower 31 in sequence, product oxygen with the carbon dioxide content of less than 50ppm, the water content of less than 50ppm and the oxygen content of more than 99% is obtained and discharged through a pressure swing adsorption output gas pipe 32, most of the product oxygen is stabilized by a pressure regulating valve 38 and then is sent into a dust removal filtering mechanism 4 through a pressure swing adsorption product gas pipe 33 to filter dust of the adsorbents, the dust content in the product oxygen is controlled to be less than 1 mu m, and a small part of the product oxygen is used for final rising and pressure rising of the rest pressure swing adsorption towers 31; with the adsorption, when the front edge of the impurity (i.e. adsorption front) rises to a certain height close to the adsorption bed, the third cut-off valve 37 on the pipeline connected with the pressure swing adsorption gas inlet pipe 30 and the third cut-off valve 37 arranged on the pressure swing adsorption output gas pipe 32 are closed, and the adsorption is stopped; at this time, a section of adsorbent which is not adsorbed and saturated is left between the adsorption front and the outlet of the adsorption bed, and the section is called a reserved section;

step B2, pressure equalizing and reducing: after the adsorption process is finished, opening a pressure equalizing switching valve 42 arranged on a connecting pipeline of one pressure equalizing pipe 41 and the pressure swing adsorption output gas pipe 32 and a pressure equalizing switching valve 42 arranged on a connecting pipeline of the pressure equalizing pipe 41 and the other pressure swing adsorption output gas pipe 32, and putting the product oxygen with higher pressure in the pressure swing adsorption tower 31(FT1) into the pressure swing adsorption tower 31(FT4) through the pressure equalizing pipe 41 until the pressures of the two pressure swing adsorption towers 31 are basically equal; this process is not only a depressurization process, but also recovers oxygen in the dead space of the bed of the pressure swing adsorption tower 31 after completion of adsorption, during which the adsorption front of the pressure swing adsorption tower 31(FT1) will continue to move forward but still not reach the outlet;

step B3, pressure equalizing and reducing: after the pressure equalizing and reducing process is completed, the pressure equalizing and switching valve 42 installed on the connecting pipeline between the other pressure equalizing pipe 41 and the pressure swing adsorption output air pipe 32 and the pressure equalizing and switching valve 42 installed on the connecting pipeline between the pressure equalizing pipe 41 and the other pressure swing adsorption output air pipe 32 are used for putting the product oxygen with higher pressure in the pressure swing adsorption tower 31(FT1) into the pressure swing adsorption tower 31(FT5) through the pressure equalizing pipe 41 and for pressure equalizing and reducing of the pressure swing adsorption tower 31 for two times. The process continues to recover oxygen in the dead space of the bed layer of the pressure swing adsorption tower 31(FT1), and the adsorption front of the pressure swing adsorption tower 31 after the adsorption is finished is also continuously pushed forwards but still does not reach the outlet;

step B4, reverse playback: after the continuous forward depressurization process is completed, the adsorption front of the pressure swing adsorption column 31(FT1) has substantially reached the bed outlet; at this time, the three-way shut-off valve 37 attached to the connecting line between the pressure swing adsorption recovery pipe 36 and the pressure swing adsorption column 31(FT1) is opened, and the pressure in the pressure swing adsorption column 31(FT1) is reduced to near atmospheric pressure against the adsorption direction, and at this time, the adsorbed impurities such as water, carbon dioxide, and nitrogen begin to be desorbed from the adsorbent; the reverse desorption gas returns to the air inlet of the first water scrubber 7 through a recovery regulating valve 39;

step B5, vacuumizing: after the reverse release is finished, opening a third cut-off valve 37 on a pipeline connecting the pressure swing adsorption tower 31(FT1) and the pressure swing adsorption exhaust pipe 35, vacuumizing the pressure swing adsorption tower 31(FT1), desorbing a large amount of adsorbed impurities, and releasing the impurities to the local high point by a vacuum pump 40 against the adsorption direction;

step B6, voltage equalizing and boosting: after the vacuumizing process is finished, opening a pressure equalizing switching valve 42 on a pipeline connecting a pressure equalizing output gas pipe 41 for secondary pressure equalizing and reducing with a pressure equalizing output gas pipe 32 of a pressure swing adsorption tower 31(FT1), the pressure equalizing switching valve 42 on a pipeline connecting the pressure equalizing output gas pipe 32 for the pressure swing adsorption tower 31(FT4) with the pressure equalizing switching valve 41 for the secondary pressure equalizing and reducing, and performing secondary pressure equalizing and pressure increasing on the pressure swing adsorption tower 31(FT1) by using oxygen with higher pressure during secondary pressure equalizing and reducing of the pressure swing adsorption tower 31(FT 4);

step B7, voltage equalizing and boosting: after the secondary pressure equalizing process is finished, opening a pressure equalizing pipe 41 for pressure equalizing and pressure reducing to connect a pressure equalizing switching valve 42 on a pipeline connecting a pressure equalizing adsorption output gas pipe 32 of a pressure equalizing adsorption tower 31(FT1), a pressure equalizing adsorption output gas pipe 32 connected with the pressure equalizing adsorption tower 31(FT5) and a pressure equalizing switching valve 42 on a pipeline connecting the pressure equalizing adsorption pipe 41 for pressure equalizing and pressure reducing, and then recovering oxygen with higher pressure in the pressure equalizing adsorption tower 31(FT5) into the pressure equalizing adsorption tower 31(FT1) which has just finished the secondary pressure equalizing;

step B8, final rising: after the pressure equalizing and boosting processes are carried out twice, the pressure of the pressure swing adsorption tower 31(FT1) still does not reach the adsorption pressure, at this time, the pressure equalizing switching valve 42 on the pipeline connecting the pressure equalizing pipe 41 connected with the first regulating valve 34 and the pressure swing adsorption output gas pipe 32 of the pressure swing adsorption tower 31(FT1) is opened, and the pressure of the pressure swing adsorption tower 31(FT1) is slowly boosted by the product oxygen through the first regulating valve 34 until the pressure of the pressure swing adsorption tower 31(FT1) is increased to the adsorption pressure.

After the series of the pressure reduction and the pressure increase, the pressure swing adsorption tower 31(FT1) completes the entire regeneration process, and is ready for the next adsorption and thus enters the next adsorption cycle.

The process steps of the adsorption columns FT 2-6 are completely the same as FT 1. The tower 1 is always in an adsorption state, and the tower 5 is respectively in different regeneration states, so that the continuous separation and purification of the high-pressure low-temperature oxygen-enriched mixed gas are ensured.

TABLE 2

Example 3

As shown in fig. 1, 2 and 4, the process of the energy saving system for purifying oxygen from high-temperature oxygen-enriched flue gas and recycling oxygen comprises the following steps:

s1, washing: the amount of high-temperature oxygen-enriched flue gas (80 ℃, the oxygen concentration is 95-96%, the water content is 1-2%, the carbon dioxide content is 100ppm, and the nitrogen and argon content is 2%) is 16000Nm3/h and the temperature of 32 ℃ normal temperature water is 30m³The water enters a first water washing tower 7 through a flue gas inlet pipe 5 and a normal temperature water pipe 6 respectively, under the action of regular packing, normal temperature water is used as washing water to wash high temperature oxygen-enriched flue gas to remove particle impurities in the high temperature oxygen-enriched flue gas, meanwhile, the high temperature oxygen-enriched flue gas is contacted with the washing water for heat exchange to obtain 35 ℃ oxygen-enriched mixed gas, the washing water after heat exchange is returned by a drain pipe 8, and the oxygen-enriched mixed gas enters a second water washing tower through a gas pathThe water washing tower 9 is used for mixing with the 7 ℃ low-temperature water 33m from the low-temperature heat exchanger 44 under the action of the regular packing³The low-temperature washing water is subjected to contact heat exchange to obtain oxygen-rich mixed gas with the temperature lower than 12 ℃, and the oxygen-rich mixed gas with the temperature lower than 12 ℃ is output from the top of the second water washing tower 9 through an air outlet pipeline 10;

in this step, the cold side of the cryogenic heat exchanger 44 is subjected to a first cold side closed loop cycle, and the first cold side closed loop cycle is specifically: the low-temperature water prepared by the water chilling unit 43 enters the cold side of the low-temperature heat exchanger 44 through a pipeline, and the medium-temperature water obtained by heat exchange returns to the inlet of the water chilling unit 43 through the pipeline.

S2, compression and condensation: the oxygen-enriched mixed gas which is obtained after water washing and temperature reduction and is lower than 12 ℃ enters a compressor unit 1 through an air outlet pipeline 10 to be compressed to obtain 0.4MPa.G oxygen-enriched mixed gas, the 0.4MPa.G oxygen-enriched mixed gas enters a hot side of a heat exchanger 2 at an outlet of a compressor through a pipeline to perform wall type heat exchange with low-temperature water at the cold side of the heat exchanger to obtain the oxygen-enriched mixed gas and condensed water which are lower than 15 ℃, the 0.4MPa.G oxygen-enriched mixed gas and the condensed water which are lower than 15 ℃ enter a gas-liquid separation tank 3 through pipelines to perform gas-liquid separation, the condensed water is discharged from a water outlet at the bottom of the gas-liquid separation tank 3 through the pipeline to be recovered, and the 0.4MP.G oxygen-enriched mixed gas at the temperature of 15 ℃ is output to a drying air inlet pipe 11 and a pressure swing adsorption air inlet pipe 30 through the pipelines from the top of the gas-liquid separation tank 3;

The cycle sequence of the pressure swing adsorption purification mechanism 46 is shown in table 3, and the specific working steps are as follows:

the pressure swing adsorption tower 31 has 8 stations (FT1, FT2, FT3, FT4, FT5, FT6, FT7 and FT8), the whole process step process of the main process is described by taking one pressure swing adsorption tower 31(FT1) as an example, and the process processes of the other pressure swing adsorption towers 31 are completely the same; the pressure equalizing mechanism comprises three pressure equalizing tubes 41.

Step B1, adsorption: the high-pressure low-temperature oxygen-enriched mixed gas conveyed from the pressure swing adsorption gas inlet pipe 30 enters a pressure swing adsorption tower 31(FT1) through a pipeline, wherein water, carbon dioxide and nitrogen impurity components are selectively adsorbed by a plurality of adsorbents filled in the pressure swing adsorption tower 31 in sequence, product oxygen with the carbon dioxide content of less than 50ppm, the water content of less than 50ppm and the oxygen content of more than 99% is obtained and discharged through a pressure swing adsorption output gas pipe 32, most of the product oxygen is stabilized by a pressure regulating valve 38 and then is sent into a dust removal filtering mechanism 4 through a pressure swing adsorption product gas pipe 33 to filter dust of the adsorbents, the dust content in the product oxygen is controlled to be less than 1 mu m, and a small part of the product oxygen is used for final rising and pressure rising of the rest pressure swing adsorption towers 31 through a first regulating valve 34; with the adsorption, when the front edge of the impurity (i.e. adsorption front) rises to a certain height close to the adsorption bed, the third cut-off valve 37 on the pipeline connected with the pressure swing adsorption gas inlet pipe 30 and the third cut-off valve 37 arranged on the pressure swing adsorption output gas pipe 32 are closed, and the adsorption is stopped; at this time, a section of adsorbent which is not adsorbed and saturated is left between the adsorption front and the outlet of the adsorption bed, and the section is called a reserved section;

step B2, pressure equalizing and reducing: after the adsorption process is finished, opening a pressure equalizing switching valve 42 arranged on a connecting pipeline between a first pressure equalizing pipe 41 and the pressure swing adsorption output gas pipe 32 and a pressure equalizing switching valve 42 arranged on a connecting pipeline between the pressure equalizing pipe 41 and the other pressure swing adsorption output gas pipe 32, and putting the product oxygen with higher pressure in the pressure swing adsorption tower 31(FT1) into the pressure swing adsorption tower 31(FT4) through the pressure equalizing pipe 41 until the pressures of the two pressure swing adsorption towers 31 are basically equal; this process is not only a depressurization process, but also recovers oxygen in the dead space of the bed of the pressure swing adsorption tower 31 after completion of adsorption, during which the adsorption front of the pressure swing adsorption tower 31(FT1) will continue to move forward but still not reach the outlet;

step B3, pressure equalizing and reducing: after the pressure equalizing and reducing process is completed, the pressure equalizing and switching valve 42 installed on the connecting pipeline between the second pressure equalizing pipe 41 and the pressure swing adsorption output gas pipe 32 and the pressure equalizing and switching valve 42 installed on the connecting pipeline between the second pressure equalizing pipe 41 and the other pressure swing adsorption output gas pipe 32 are used for putting the product oxygen with higher pressure in the pressure swing adsorption tower 31(FT1) into the pressure swing adsorption tower 31(FT5) through the pressure equalizing pipe 41 and for pressure equalizing and reducing of the pressure swing adsorption tower 31 for two times. The process continues to recover oxygen in the dead space of the bed layer of the pressure swing adsorption tower 31(FT1), and the adsorption front of the pressure swing adsorption tower 31 after the adsorption is finished is also continuously pushed forwards but still does not reach the outlet;

TABLE 3

The above embodiment is only one of the preferred embodiments of the present invention, and should not be used to limit the protection scope of the present invention, but all the insubstantial changes or modifications made in the spirit and the idea of the main design of the present invention, the technical problems solved by the embodiment are still consistent with the present invention, and all should be included in the protection scope of the present invention.

Claims

1. The utility model provides an economizer system that high temperature oxygen boosting flue gas purification oxygen cyclic utilization, including the washing mechanism who inserts high temperature oxygen boosting flue gas, with washing mechanism tube coupling's compressor unit (1), with compressor outlet heat exchanger (2) of compressor unit (1) tube coupling, with gas-liquid separation jar (3) of compressor outlet heat exchanger (2) tube coupling, its characterized in that, include with the isobaric drying mechanism of temperature swing adsorption (45) and pressure swing adsorption purification mechanism (46) of gas-liquid separation jar (3) tube coupling insert isobaric drying mechanism of temperature swing adsorption (45) and pressure swing adsorption purification mechanism (46) and handle gaseous dust removal filtering mechanism (4) of back to and be used for washing the mechanism and the cooling mechanism of compressor outlet heat exchanger (2) cooling down, wherein, the isobaric drying mechanism of temperature swing adsorption (45) output and pressure swing adsorption purification mechanism (46) output tube coupling and through pipeline and dust removal filtering mechanism (4) And the pressure swing adsorption purification mechanism (46) is connected with the water washing mechanism.

2. The energy-saving system for recycling purified oxygen from high-temperature oxygen-enriched flue gas according to claim 1, wherein the washing mechanism comprises a flue gas inlet pipe (5) for accessing high-temperature oxygen-enriched flue gas, a normal-temperature water pipe (6) for charging normal-temperature water, a first washing tower (7) connected with the flue gas inlet pipe (5) and the normal-temperature water pipe (6), a drain pipe (8) and a second washing tower (9) connected with the first washing tower (7), and an air outlet pipeline (10) connected with the second washing tower (9) and the compressor unit (1), wherein the cooling mechanism is connected with the second washing tower (9) through a pipeline, and the pressure swing adsorption purification mechanism (46) is connected with the first washing tower (7).

3. The energy-saving system for recycling purified oxygen from high-temperature oxygen-enriched flue gas according to claim 2, wherein the temperature swing adsorption isobaric drying mechanism (45) comprises a drying air inlet pipe (11) connected with the gas-liquid separation tank (3), a first air delivery pipe (12), a second air delivery pipe (13) and a third air delivery pipe (14) connected with the drying air inlet pipe (11), a fourth air delivery pipe (15) connected with the third air delivery pipe (14), a first adsorption tower (16) and a second adsorption tower (17) respectively connected with the first air delivery pipe (12) and the second air delivery pipe (13), a first output pipe (18) and a second output pipe (19) respectively connected with the bottoms of the first adsorption tower (16) and the second adsorption tower (17), and a dry product air pipe (20) respectively connected with the first output pipe (18) and the second output pipe (19) and used for outputting product gas, with predrying tower (21) that third gas-supply pipe (14) are connected, with heater (22) of predrying tower (21) pipe connection, one end is connected with heater (22) and the other end passes through fifth gas-supply pipe (23) that the pipeline is connected with first output tube (18) and second output tube (19) respectively, with condenser (24) that fourth gas-supply pipe (15) are connected, with gas-liquid separator (25) of condenser (24) pipe connection, connect sixth gas-supply pipe (26) between third gas-supply pipe (14) and fourth gas-supply pipe (15), one end is connected with sixth gas-supply pipe (26) and the other end passes through the pipeline and is connected with first output tube (18) and second output tube (19) seventh gas-supply pipe (27), install respectively on first gas-supply pipe (12), on second gas-supply pipe (13), on third gas-supply pipe (14), A plurality of first on-off valves (28) arranged on a fourth air conveying pipe (15), a first output pipe (18), a second output pipe (19), a connecting pipeline of a fifth air conveying pipe (23) and the first output pipe (18), a connecting pipeline of the fifth air conveying pipe (23) and the second output pipe (19), a connecting pipeline of a seventh air conveying pipe (27) and the first air conveying pipe (12) and a connecting pipeline of the seventh air conveying pipe (27) and the second air conveying pipe (13), and two second on-off valves (29) arranged on a sixth air conveying pipe (26), wherein the gas-liquid separator (25) is connected with the dry air inlet pipe (11) through a pipeline, the seventh air delivery pipe (27) is connected to the sixth air delivery pipe (26) and is positioned between the two second stop valves (29), the dry product gas pipe (20) is connected with an output end pipeline of the pressure swing adsorption purification mechanism (46).

4. The energy-saving system for recycling purified oxygen from high-temperature oxygen-enriched flue gas as claimed in claim 3, wherein the pressure swing adsorption purification mechanism (46) comprises a pressure swing adsorption gas inlet pipe (30) connected to the gas-liquid separation tank (3), a plurality of pressure swing adsorption towers (31) with bottoms connected to the pressure swing adsorption gas inlet pipe (30) via pipelines, pressure swing adsorption gas outlet pipes (32) connected to the tops of the pressure swing adsorption towers (31), pressure swing adsorption product gas pipes (33) connected to each pressure swing adsorption gas outlet pipe (32) and connected to the dry product gas pipe (20), a pressure equalizing mechanism connected to each pressure swing adsorption gas outlet pipe (32), a first regulating valve (34) with two ends connected to the pressure swing adsorption product gas pipes (33) and the pressure equalizing mechanism, and a pressure swing adsorption gas outlet pipe (35) connected to the bottom of each pressure swing adsorption tower (31) via pipelines, a pressure swing adsorption recovery pipe (36) with one end connected with a pipeline at the bottom of each pressure swing adsorption tower (31) and the other end connected with the first water scrubber (7), third breaking valves (37) respectively arranged on a pressure swing adsorption output gas pipe (32), a pressure swing adsorption gas inlet pipe (30) and a connecting pipeline at the bottom of the pressure swing adsorption tower (31), a pressure swing adsorption recovery pipe (36) and a connecting pipeline at the bottom of the pressure swing adsorption tower (31), a pressure regulating valve (38) and a dedusting filtering system (47) arranged on the pressure swing adsorption product gas pipe (33), and a recovery regulating valve (39) arranged on the pressure swing adsorption recovery pipe (36), and a vacuum pump (40) installed on the pressure swing adsorption exhaust pipe (35), wherein, the pressure swing adsorption product air pipe (33) is connected with the dust removal filtering mechanism (4).

5. The energy-saving system for recycling purified oxygen from high-temperature oxygen-enriched flue gas according to claim 4, wherein the pressure equalizing mechanism comprises a plurality of pressure equalizing pipes (41) respectively connected with each pressure swing adsorption output gas pipe (32) in a pipeline manner, and a pressure equalizing switching valve (42) installed on the pipeline connecting the pressure equalizing pipes (41) and each pressure swing adsorption output gas pipe (32), wherein the first regulating valve (34) is connected with one pressure equalizing pipe (41).

6. The energy-saving system for recycling purified oxygen in high-temperature oxygen-enriched flue gas as claimed in claim 4, wherein the number of the pressure swing adsorption towers (31) is at least 3.

7. The energy-saving system for recycling purified oxygen from high-temperature oxygen-enriched flue gas as claimed in claim 2, wherein the cooling mechanism connection comprises a water chilling unit (43) connected with the pipeline of the compressor outlet heat exchanger (2) and a low-temperature heat exchanger (44) respectively connected with the water chilling unit (43) and the second water scrubber (9).