WO2023066105A1 - 一种锅炉烟道气同步回收氮气和二氧化碳的系统和方法 - Google Patents

一种锅炉烟道气同步回收氮气和二氧化碳的系统和方法 Download PDF

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WO2023066105A1
WO2023066105A1 PCT/CN2022/124845 CN2022124845W WO2023066105A1 WO 2023066105 A1 WO2023066105 A1 WO 2023066105A1 CN 2022124845 W CN2022124845 W CN 2022124845W WO 2023066105 A1 WO2023066105 A1 WO 2023066105A1
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carbon dioxide
nitrogen
gas
outlet
flue gas
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PCT/CN2022/124845
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English (en)
French (fr)
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陈绍云
李玉雪
戚励
张永春
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大连理工大学
碳和科技(北京)有限公司
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Publication of WO2023066105A1 publication Critical patent/WO2023066105A1/zh
Priority to US18/447,072 priority Critical patent/US20230381712A1/en

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • B01D53/053—Pressure swing adsorption with storage or buffer vessel
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B01D53/0423—Beds in columns
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B01D53/0446—Means for feeding or distributing gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0462—Temperature swing adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/26—Drying gases or vapours
    • B01D53/265—Drying gases or vapours by refrigeration (condensation)
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B21/00—Nitrogen; Compounds thereof
    • C01B21/04—Purification or separation of nitrogen
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/50—Carbon dioxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/10—Nitrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/22—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/302—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

Definitions

  • the invention belongs to the technical field of recovery and utilization of boiler flue gas, and in particular relates to a system and method for synchronous recovery of nitrogen and carbon dioxide from boiler flue gas.
  • the capture and reuse of carbon dioxide from the flue gas of coal-fired boilers is an important measure to achieve the double-carbon goal, and the nitrogen content in the vented air after recovering carbon dioxide is about 90%. Recycling it can not only increase the nitrogen production Air efficiency can reduce energy consumption and further reduce carbon emissions.
  • Chinese patent application CN107899376A discloses a combined capture and recovery device and method for carbon dioxide and nitrogen in flue gas, the device includes a flue gas treatment system, a first CO2 membrane separation unit, a second CO2 membrane separation unit and a N2 membrane separate unit.
  • the device belongs to the membrane recovery method. Although it can capture carbon dioxide and nitrogen at the same time, the product purity is low.
  • the membrane barrel has high requirements on the cleanliness of the gas source. The equipment is prone to blockage during use, the service life is short, and the price of the membrane barrel is high. Not suitable for industrialized mass production.
  • Chinese patent application CN110498416A discloses a system for synchronous recovery of carbon dioxide and nitrogen from boiler flue gas in a coal-fired power plant, including a flue gas pretreatment system, a PSA1 system, a PSA2 system, a carbon dioxide compression and purification system, a carbon dioxide rectification storage system, and a PSA high-purity nitrogen system.
  • the system can capture carbon dioxide and nitrogen to the greatest extent, and the product purity is high, but there are problems of inflexible equipment operation and high energy consumption.
  • the pressure compression value of the former stage is too high and the power consumption is large.
  • the object of the present invention is to provide a system and method for synchronous recovery of nitrogen and carbon dioxide from boiler flue gas, so as to solve or alleviate the problems existing in the prior art.
  • the present invention provides the following technical solutions:
  • a system for synchronously recovering nitrogen and carbon dioxide from boiler flue gas comprising:
  • Flue gas pretreatment system for dehydration and cooling of boiler flue gas
  • the carbon and nitrogen separation system is connected with the flue gas pretreatment system, and is used to separate the nitrogen-containing air and crude carbon dioxide from the flue gas after the pressure swing adsorption pretreatment.
  • the adsorption pressure of the carbon and nitrogen separation system is 0.20-0.40MPa;
  • the carbon dioxide secondary purification system is connected with the carbon and nitrogen separation system, and is used for secondary purification of the crude carbon dioxide gas separated by the carbon and nitrogen separation system;
  • the nitrogen concentration and purification system communicates with the carbon and nitrogen separation system and the carbon dioxide secondary purification system, and is used to discharge the nitrogen-containing air separated by the carbon and nitrogen separation system and the discharge air generated by the carbon dioxide secondary purification system Purify.
  • the flue gas pretreatment system includes a first cooler, a first gas-liquid separator and a flue gas induced draft fan, and the first The inlet of the cooler is connected to the boiler flue, the outlet of the first cooler is connected to the inlet of the first gas-liquid separator, and the outlet of the first gas-liquid separator is connected to the inlet of the flue gas induced draft fan, so The outlet of the flue gas induced draft fan is connected to the carbon and nitrogen separation system.
  • the carbon and nitrogen separation system includes a flue gas compressor, a second gas-liquid separator, a first dryer, a first adsorption tower group,
  • the first vacuum pump and the first buffer tank, the first adsorption tower group includes a plurality of first adsorption towers arranged in parallel, and each of the first adsorption towers is filled with a first adsorbent; wherein the flue gas
  • the inlet of the compressor is connected to the flue gas pretreatment system, the outlet of the flue gas compressor is connected to the inlet of the second gas-liquid separator, and the outlet of the second gas-liquid separator is connected to the first
  • the inlet of the dryer is connected, the outlet of the first dryer is connected with the inlet of the first adsorption tower group, the top outlet of the first adsorption tower group is nitrogen-containing air, and the bottom outlet is crude carbon dioxide gas, the gas outlet at the top of the first adsorption tower
  • the system for synchronously recovering nitrogen and carbon dioxide from boiler flue gas as described above optionally, the volume concentration of nitrogen in the nitrogen-containing venting air is 88%-90%, and the volume concentration of carbon dioxide in the crude carbon dioxide gas is 45% -80%.
  • the secondary purification system for carbon dioxide includes a first carbon dioxide compressor, a third gas-liquid separator, a second adsorption tower group, and a second vacuum pump and the second buffer tank, the second adsorption tower group includes a plurality of second adsorption towers arranged in parallel, each second adsorption tower is filled with a second adsorbent; wherein, the inlet of the first carbon dioxide compressor Connected to the carbon and nitrogen separation system, the outlet of the first carbon dioxide compressor is connected to the inlet of the third gas-liquid separator, and the outlet of the third gas-liquid separator is connected to the second adsorption tower group
  • the gas inlet at the top of the second adsorption tower group is connected to the nitrogen concentration and purification system, and the gas outlet at the bottom of the second adsorption tower group is connected to the inlet of the second vacuum pump.
  • the outlet of the second vacuum pump communicates with the inlet of the second buffer
  • the system for synchronously recovering nitrogen and carbon dioxide from boiler flue gas as described above optionally, the nitrogen concentration and purification system includes a third buffer tank, a nitrogen compressor, a second dryer, a filter and a third adsorption tower group,
  • the third adsorption tower group includes a plurality of third adsorption towers arranged in parallel, and the third adsorption tower is filled with a third adsorbent; wherein, the inlet of the third buffer tank is connected to the carbon and nitrogen separation system and The carbon dioxide secondary purification system is communicated, the outlet of the third buffer tank is communicated with the inlet of the nitrogen compressor, the outlet of the nitrogen compressor is communicated with the inlet of the second dryer, and the second dryer The outlet of the filter is communicated with the inlet of the filter, the outlet of the filter is communicated with the inlet of the third adsorption tower group, and the top gas outlet of the third adsorption tower group obtains product nitrogen.
  • the adsorption pressure of the third adsorption tower is 0.7-1.0 MPa, and the volume concentration of the product nitrogen is 99%-99.999%.
  • the system for synchronously recovering nitrogen and carbon dioxide from boiler flue gas as described above optionally, the system further includes a carbon dioxide refining liquefaction system, and the carbon dioxide refining liquefaction system is connected to the carbon dioxide secondary purification system for refining carbon dioxide .
  • the carbon dioxide refining and liquefaction system includes a second cooler, a fourth gas-liquid separator, a second carbon dioxide compressor, a fourth buffer tank, Desulfurization tower group, drying tower group, third cooler, liquefaction module, rectification module and carbon dioxide storage tank; wherein, the inlet of the second cooler is connected to the carbon dioxide secondary purification system, and the second cooler
  • the outlet of the gas-liquid separator communicates with the inlet of the fourth gas-liquid separator
  • the outlet of the fourth gas-liquid separator communicates with the inlet of the second carbon dioxide compressor
  • Step (1) passing the boiler flue gas into the flue gas pretreatment system, performing dehydration and cooling to obtain the pretreated flue gas;
  • step (2) the pretreated flue gas is passed into the carbon and nitrogen separation system, and the pressure swing adsorption pretreatment is carried out to separate the nitrogen-containing release air and crude carbon dioxide gas, wherein the adsorption pressure of the carbon and nitrogen separation system is 0.20 -0.4MPa;
  • Step (3) passing the crude carbon dioxide gas separated by the carbon-nitrogen separation system into the carbon dioxide secondary purification system, performing secondary purification, obtaining purified carbon dioxide gas, and producing nitrogen-containing release air;
  • Step (4) the nitrogen-containing release air separated by the carbon-nitrogen separation system and the nitrogen-containing release air produced by the carbon dioxide secondary purification system are passed into the nitrogen concentration and purification system for purification to obtain product nitrogen;
  • the method further includes: step (31), passing the purified carbon dioxide gas into a carbon dioxide refining liquefaction system for refining treatment to obtain refined carbon dioxide gas.
  • the system for synchronously recovering nitrogen and carbon dioxide from boiler flue gas of the present invention can recover carbon dioxide and nitrogen to the greatest extent without producing three wastes.
  • the carbon and nitrogen separation system of the present invention adopts the low-pressure adsorption mode of 0.20-0.40MPa to separate carbon dioxide and nitrogen, which changes the situation of adsorption under 1.0MPa in the previous technology, and effectively reduces energy consumption.
  • the desorption gas is desorbed by a vacuum pump, which not only reduces energy consumption, but also improves the recovery rate of carbon dioxide.
  • the nitrogen concentration and purification system of the present invention adopts the secondary compression mode, and there will be a secondary pressure raising process, and the model and compression pressure of the compressor can be selected according to the actual nitrogen volume required by the user, thereby further achieving the purpose of energy saving.
  • FIG. 1 is a schematic flow diagram of a system for synchronously recovering nitrogen and carbon dioxide from boiler flue gas according to an embodiment of the present invention
  • FIG. 2 is a schematic flow diagram of a flue gas pretreatment system according to an embodiment of the present invention
  • FIG. 3 is a schematic flow diagram of a carbon and nitrogen separation system according to an embodiment of the present invention.
  • Fig. 4 is the schematic flow sheet of the carbon dioxide secondary purification system of the embodiment of the present invention.
  • FIG. 5 is a schematic flow diagram of a carbon dioxide refining and liquefaction system according to an embodiment of the present invention
  • Fig. 6 is a schematic flow diagram of a nitrogen concentration and purification system according to an embodiment of the present invention.
  • 21-flue gas compressor 22-second gas-liquid separator; 23-first dryer; 24-first adsorption tower group; 25-first vacuum pump;
  • the present invention proposes an energy-saving boiler flue gas synchronous nitrogen and carbon dioxide recovery system, as shown in Figure 1, the system includes a flue gas pretreatment system 1, a carbon and nitrogen separation system 2. Carbon dioxide secondary purification system 3. Carbon dioxide refined liquefaction system 4 and nitrogen concentration and purification system 5.
  • the flue gas pretreatment system 1 is used to dehydrate and cool down the boiler flue gas;
  • the carbon and nitrogen separation system 2 is connected to the flue gas pretreatment system 1, and is used to combine the flue gas after pressure swing adsorption pretreatment. Separation of nitrogen-containing air and crude carbon dioxide gas, the adsorption pressure of carbon and nitrogen separation system 2 is 0.20-0.40MPa;
  • carbon dioxide secondary purification system 3 is connected with carbon and nitrogen separation system 2, and is used to separate the Crude carbon dioxide gas is subjected to secondary purification;
  • the nitrogen concentration purification system 5 is connected with the carbon nitrogen separation system 2 and the carbon dioxide secondary purification system 3, and is used to vent the nitrogen-containing air separated by the carbon nitrogen separation system 2 and the carbon dioxide secondary purification system 3
  • the generated air is purified;
  • the carbon dioxide refining liquefaction system 4 is connected to the carbon dioxide secondary purification system 3 for refining carbon dioxide.
  • Carbon nitrogen separation system 2 of the present invention adopts the low-pressure adsorption mode separation carbon dioxide and Nitrogen has changed the situation of adsorption under 1.0MPa in the previous technology, and the energy consumption has been effectively reduced.
  • the flue gas pretreatment system 1 includes a first cooler 11, a first gas-liquid separator 12 and a flue gas induced draft fan 13, and the inlet of the first cooler 11 It is connected to the boiler flue, the outlet of the first cooler 11 is connected to the inlet of the first gas-liquid separator 12, the outlet of the first gas-liquid separator 12 is connected to the inlet of the flue gas induced fan 13, and the outlet of the flue gas induced fan 13 is connected to the carbon Nitrogen separation system 2.
  • the carbon and nitrogen separation system 2 includes a flue gas compressor 21, a second gas-liquid separator 22, a first dryer 23, a first adsorption tower group 24, a first Vacuum pump 25 and the first surge tank (not shown), the first adsorption tower group 24 comprises a plurality of first adsorption towers arranged in parallel, and all are filled with the first adsorbent in each first adsorption tower;
  • flue gas compression The inlet of the machine 21 is connected to the outlet of the flue gas induced draft fan 13 of the flue gas pretreatment system 1, the outlet of the flue gas compressor 21 is connected to the inlet of the second gas-liquid separator 22, and the outlet of the second gas-liquid separator 22 is connected to the second gas-liquid separator 22.
  • the inlet of a drier 23 is connected, the outlet of the first drier 23 is connected with the inlet of the first adsorption tower group 24, the top outlet of the first adsorption tower group 24 is nitrogen-containing air release, and the bottom outlet is crude carbon dioxide gas , the gas outlet at the top of the first adsorption tower group 24 is communicated with the nitrogen concentration and purification system 5, the gas outlet at the bottom of the first adsorption tower group 24 is communicated with the inlet of the first vacuum pump 25, and the outlet of the first vacuum pump 25 is connected with the first buffer The inlet of the tank is communicated, and the outlet of the first buffer tank is communicated with the carbon dioxide secondary purification system 3 .
  • the volume concentration of nitrogen in the nitrogen-containing venting air of the present invention is 88%-90% (such as 88%, 89% or 90%), and the volume concentration of carbon dioxide in the crude carbon dioxide gas is 45%-80% (such as 45%, 46%) , 47%, 48%, 49%, 50%, 60%, 70% or 80%).
  • the pipe connecting the outlet of the flue gas compressor 21 is provided with a first pneumatic valve
  • the first pneumatic valve is provided with a first solenoid valve
  • the first solenoid valve is electrically connected to the PLC, so that the first pneumatic valve Controlled by PLC through the first solenoid valve.
  • the flue gas processed by the flue gas pretreatment system 1 is lifted to compressed flue gas of about 0.25MPa by the flue gas compressor 21, and enters the first adsorption tower group 24, and the PLC is controlled by the first solenoid valve
  • the first pneumatic valve is used to ensure the different working conditions of different first adsorption towers.
  • the gas at the top of the tower is nitrogen-rich gas and enters the nitrogen concentration and purification system as raw material gas.
  • the gas at the bottom of the tower is about 50% crude carbon dioxide gas as raw material gas for the lower stage.
  • the carbon dioxide secondary purification system 3 includes a first carbon dioxide compressor 31, a third gas-liquid separator 32, a second adsorption tower group 33, a second vacuum pump 34 and a second vacuum pump 34.
  • the second adsorption tower group 33 includes a plurality of second adsorption towers arranged in parallel, all filled with the second adsorbent in each second adsorption tower; wherein, the inlet of the first carbon dioxide compressor 31 is communicated with carbon dioxide
  • the outlet of the first buffer tank in the nitrogen separation system 2 the outlet of the first carbon dioxide compressor 31 is connected to the inlet of the third gas-liquid separator 32, and the outlet of the third gas-liquid separator 32 is connected to the second adsorption tower group 33
  • Air inlet, the gas outlet at the top of the second adsorption tower group 33 is communicated with the nitrogen concentration and purification system 5, the gas outlet at the bottom of the second adsorption tower group 33 is communicated with the inlet of the second vacuum pump 34, and the outlet of the second vacuum pump 34 is communicated with At the entrance of the second buffer tank 35.
  • the pipeline connected to the outlet of the first carbon dioxide compressor 31 is provided with a second pneumatic valve
  • the second pneumatic valve is provided with a second solenoid valve
  • the second solenoid valve is electrically connected to the PLC, so that the second pneumatic valve is controlled by The PLC is controlled by a second solenoid valve.
  • the PLC controls the second pneumatic valve through the second solenoid valve to ensure different working conditions of different second adsorption towers.
  • the purification system is used as raw material gas or vented, and the outlet gas at the bottom of the tower is about 95% carbon dioxide gas, which is used as raw material gas for refined carbon dioxide.
  • the carbon dioxide refining liquefaction system 4 includes a second cooler 41, a fourth gas-liquid separator 42, a second carbon dioxide compressor 43, a fourth buffer tank 43a, Desulfurization tower group 44, drying tower group 45, third cooler 46, liquefaction module 47, rectification module 48 and carbon dioxide storage tank 49; wherein, the inlet of the second cooler 41 is communicated with the desorption of carbon dioxide secondary purification system 3 Gas (that is, communicated with the outlet of the second buffer tank 35), the outlet of the second cooler 41 is communicated with the inlet of the fourth gas-liquid separator 42, and the outlet of the fourth gas-liquid separator 42 is communicated with the second carbon dioxide compressor 43
  • the inlet of the carbon dioxide gas compressed to 2.5MPa enters the inlet of the fourth buffer tank 43a from the outlet of the second carbon dioxide compressor 43, and the outlet of the fourth buffer tank 43a is communicated with the inlet of the desulfurization tower group 44, through the impurity sulfur After des
  • the outlet of the drying tower group 45 is connected to the inlet of the third cooler 46 for cooling treatment.
  • the third cooler 46 The outlet is connected to the inlet of the liquefaction module 47, and the outlet of the liquefaction module 47 enters the inlet of the rectification module 48, and what the rectification obtains is a food-grade carbon dioxide product with a volume concentration of ⁇ 99.9%, and enters the carbon dioxide from the bottom outlet of the rectification module 48 Storage tank 49 for storage.
  • the desulfurization tower group 44 includes a plurality of parallel desulfurization towers
  • the drying tower group 45 includes a plurality of parallel drying towers
  • the rectification module 48 includes a rectification tower.
  • the nitrogen concentration and purification system 5 includes a third buffer tank 51, a nitrogen compressor 52, a second drier 53, a filter 54 and a third adsorption tower group 55
  • the second Three adsorption tower groups 55 include multiple third adsorption towers arranged in parallel, filled with a third adsorbent in the third adsorption tower; wherein, the inlet of the third buffer tank 51 is connected to the carbon and nitrogen separation system 2 and the carbon dioxide secondary purification system 3
  • the outlet of the third buffer tank 51 is connected to the inlet of the nitrogen compressor 52, the outlet of the nitrogen compressor 52 is connected to the inlet of the second drier 53, and the outlet of the second drier 53 is connected to the inlet of the filter 54
  • the inlet and the outlet of the filter 54 communicate with the inlet of the third adsorption tower group 55, and the top gas outlet of the third adsorption tower group 55 obtains product nitrogen.
  • the adsorption pressure of the third adsorption tower is 0.7-1.0MPa (such as 0.7MPa, 0.75MPa, 0.8MPa, 0.9MPa or 1.0MPa), and the volume concentration of the product nitrogen is 99%-99.999%.
  • the nitrogen concentration and purification system 5 of the present invention recovers the two-stage venting air produced by the carbon and nitrogen separation system 2 and the carbon dioxide secondary purification system 3, and after compression and filtration, the gas with a pressure of 0.7-1.0 MPa enters the The third adsorption tower, the third adsorption tower is filled with the third adsorbent, which has a high recovery rate for the air with complex components. After separation by multi-tower pressure swing adsorption, the product with a volume concentration of 99%-99.999% is obtained at the top of the tower nitrogen.
  • first adsorbent, the second adsorbent and the third adsorbent used in the present invention are all existing adsorbents.
  • the present invention also proposes a method for synchronously recovering nitrogen and carbon dioxide from boiler flue gas, adopting the above-mentioned system for synchronously recovering nitrogen and carbon dioxide from boiler flue gas, said method comprising the following steps:
  • Step (1) passing the boiler flue gas into the flue gas pretreatment system, performing dehydration and cooling to obtain the pretreated flue gas;
  • step (2) the pretreated flue gas is passed into the carbon and nitrogen separation system, and the pressure swing adsorption pretreatment is carried out to separate the nitrogen-containing release air and crude carbon dioxide gas, wherein the adsorption pressure of the carbon and nitrogen separation system is 0.20 -0.40MPa;
  • step (3) the crude carbon dioxide gas separated by the carbon-nitrogen separation system is passed into the carbon dioxide secondary purification system for secondary purification to obtain purified carbon dioxide gas and generate air release;
  • step (4) the nitrogen-containing release air separated by the carbon-nitrogen separation system and the release air produced by the carbon dioxide secondary purification system are passed into the nitrogen concentration and purification system for purification to obtain product nitrogen;
  • the method further includes: step (31), passing the purified carbon dioxide gas into a carbon dioxide refining liquefaction system for refining treatment to obtain refined carbon dioxide gas.
  • the embodiment of the present invention is used for the recovery of carbon dioxide and nitrogen in the flue gas of a coal power plant, the carbon dioxide gas is used to increase the income of smart agriculture, and the nitrogen gas is used for the replacement and purging of the chemical workshop of the factory.
  • the composition of the flue gas is shown in Table 1.
  • Element sulfur dioxide Nitrogen oxides carbon monoxide carbon dioxide oxygen water measured value 0mg/ m3 31mg/ m3 not detected 13% 6.20% 12.50% The detection limit 2mg/ m3 2mg/ m3 20mg/ m3 0.03% —— ———
  • the required flue gas is drawn from the flue gas discharge chimney after desulfurization and denitrification, enters the first cooler 11 for preliminary cooling to about 35°C, and enters the first gas-liquid separator 12 for degassing. The liquid is separated, and then enters the flue gas induced draft fan 13, and the outlet pressure of the flue gas induced draft fan 13 is 5KPa.
  • the flue gas enters the flue gas compressor 21 from the outlet of the flue gas induced draft fan 13, and after being pressed to 0.23MPa, enters the second gas-liquid separator 22, and then enters the first dryer 23 for deep dehydration, and then enters the first adsorption tower group 24
  • Adsorption separation is carried out, and the vented air with a nitrogen content of 88-90% is obtained at the top of the tower, and the vented air is used as the raw material gas of the nitrogen concentration and purification system.
  • the stripping gas obtained after desorption by the first vacuum pump 25 at the bottom of the tower is crude carbon dioxide gas with a volume of carbon dioxide of 45% and a pressure of 15KPa.
  • Crude carbon dioxide gas with a content of 45% is compressed to 0.25 MPa by the first carbon dioxide compressor 31, enters the third gas-liquid separator 32 for gas-liquid separation, and then enters the second adsorption tower group 33 to further purify carbon dioxide, and the top of the tower obtains carbon dioxide Secondary purification releases air, introduces the raw material gas pipe of the nitrogen concentration and purification system 5, and desorbs the bottom of the tower through the second vacuum pump 34 to obtain carbon dioxide gas with a purity of 95% and a pressure of about 15kPa, which is stored in the second buffer tank 35.
  • the air released from the top of the adsorption tower in the carbon and nitrogen separation system 2 and the carbon dioxide secondary purification system 3 enters the third buffer tank 51, then enters the nitrogen compressor 52, raises the pressure to 0.8-1.0 MPa, and enters the second dryer 53 and filter 54 carry out dehydration, drying, filtration and purification, and then enter the third adsorption tower group 55 for pressure swing adsorption to obtain product nitrogen with a purity ranging from 99.5% to 99.9%.
  • the carbon and nitrogen separation system adopts the low-pressure adsorption mode, and the adsorption pressure is 0.25MPa, which changes the situation of adsorption under 1.0MPa in the previous technology, and the desorption gas is desorbed by a vacuum pump, which not only reduces energy consumption, but also increases the carbon dioxide concentration. recovery rate.
  • the nitrogen concentration and purification system adopts the secondary compression mode to increase the pressure from 0.23MPa to 0.8-1.0MPa, and only selects the model of the compressor for the amount of nitrogen required by the actual user. Compared with the compressor for compressing a large amount of flue gas , the gas volume compressed here is only 68% of the flue gas compression.
  • the flue gas compression is raised from 0.01 MPa to 0.8-1.0 MPa, and the air release compression is raised from 0.23 MPa to 0.8-1.0 MPa.
  • the compressed gas volume is also reduced to 68%. It can be seen from this that the energy-saving effect of the system of the present invention is obvious.

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Abstract

一种锅炉烟道气同步回收氮气和二氧化碳的系统和方法，所述系统包括：烟道气预处理系统（1），用于对锅炉烟道气进行脱水和降温；碳氮分离系统（2）与烟道气预处理系统（1）连通，用于变压吸附预处理后的烟道气并分离出含氮放空气和粗二氧化碳气体，碳氮分离系统（2）的吸附压力为0.20-0.40MPa；二氧化碳二次提纯系统（3）与碳氮分离系统（2）连通，用于对碳氮分离系统（2）分离出的粗二氧化碳气体进行二次提纯；氮气浓缩提纯系统（5）与碳氮分离系统（2）和二氧化碳二次提纯系统（3）连通，用于对碳氮分离系统（2）分离出的含氮放空气和二氧化碳二次提纯系统（3）产生的放空气进行提纯。该系统能够最大程度的回收二氧化碳和氮气，无三废产生，且能耗较低。

Description

一种锅炉烟道气同步回收氮气和二氧化碳的系统和方法 技术领域
本发明属于锅炉烟道气的回收利用技术领域，具体涉及一种锅炉烟道气同步回收氮气和二氧化碳的系统和方法。
背景技术
对燃煤锅炉烟道气的二氧化碳捕集再利用是实现双碳目标的一种重要措施，且回收二氧化碳后的放空气中，氮气含量在90％左右，对其进行回收，既可以提高氮气产气效率，又能降低能耗，进一步减少碳排放。
中国专利申请CN107899376A公开了一种烟气中二氧化碳和氮气的联合捕集回收装置及方法，该装置包括烟气处理系统，第一CO 2膜分离单元，第二CO 2膜分离单元以及N 2膜分离单元。该装置属于膜回收方式，虽然能同时捕集二氧化碳和氮气，但是产品纯度低，膜桶对气源洁净度要求很高，设备使用过程中容易产生堵塞，寿命短，且膜桶价格较高，不适合工业化大生产。
中国专利申请CN110498416A公开了一种燃煤电厂锅炉烟气同步回收二氧化碳及氮气的系统，包括烟气预处理系统、PSA1系统、PSA2系统、二氧化碳压缩提纯系统、二氧化碳精馏贮存系统、PSA制高纯氮系统。该系统能最大程度的捕集二氧化碳和氮气，产品纯度较高，但是存在设备操作不灵活，能耗高的问题。当后级氮气产量降低或者不进行捕集时，前级的压力压缩值过高，耗电量较大。
因此，需要提供一种针对上述现有技术不足的改进技术方案。
发明内容
本发明的目的在于提供一种锅炉烟道气同步回收氮气和二氧化碳的系统和方法，以解决或缓解现有技术中存在的问题。
为了实现上述目的，本发明提供如下技术方案：
一种锅炉烟道气同步回收氮气和二氧化碳的系统，所述系统包括：
烟道气预处理系统，用于对锅炉烟道气进行脱水和降温；
碳氮分离系统，与所述烟道气预处理系统连通，用于变压吸附预处理后的烟道气并分离出含氮放空气和粗二氧化碳气体，所述碳氮分离系统的吸附压力为0.20-0.40MPa；
二氧化碳二次提纯系统，与所述碳氮分离系统连通，用于对所述碳氮分离系统分离出的粗二氧化碳气体进行二次提纯；
氮气浓缩提纯系统，与所述碳氮分离系统和所述二氧化碳二次提纯系统连通，用于对所述碳氮分离系统分离出的含氮放空气和所述二氧化碳二次提纯系统产生的放空气进行提纯。
如上所述的锅炉烟道气同步回收氮气和二氧化碳的系统，可选地，所述烟道气预处理系统包括第一冷却器、第一气液分离器和烟气引风机，所述第一冷却器的入口连通锅炉烟道，所述第一冷却器的出口连通所述第一气液分离器的入口，所述第一气液分离器的出口连通所述烟气引风机的入口，所述烟气引风机的出口连通所述碳氮分离系统。
如上所述的锅炉烟道气同步回收氮气和二氧化碳的系统，可选地，所述碳氮分离系统包括烟气压缩机、第二气液分离器、第一干燥器、第一吸附塔组、第一真空泵和第一缓冲罐，所述第一吸附塔组包括多台并联设置的第一吸附塔，每一所述第一吸附塔内均填充有第一吸附剂；其中，所述烟气压缩机的入口连通所述烟道气预处理系统，所述烟气压缩机的出口与所述第二气液分离器的入口连通，所述第二气液分离器的出口与所述第一干燥器的入口连通，所述第一干燥器的出口连通与所述第一吸附塔组的进气口连通，所述第一吸附塔组的顶部出气为含氮放空气，底部出气为粗二氧化碳气体，所述第一吸附塔组的塔顶出气口与所述氮气浓缩提纯系统连通，所述第一吸附塔组的塔底出气口与所述第一真空泵的入口连通，所述第一真空泵的出口与所述第一缓冲罐的入口连通，所述第一缓冲罐的出口与所述二氧化碳二次提纯系统连通。
如上所述的锅炉烟道气同步回收氮气和二氧化碳的系统，可选地，所述含氮放空气中氮气体积浓度为88％-90％，所述粗二氧化碳气体中二氧化碳的体积浓度为45％-80％。
如上所述的锅炉烟道气同步回收氮气和二氧化碳的系统，可选地，所述二氧化碳二次提纯系统包括第一二氧化碳压缩机、第三气液分离器、第二吸附塔组、第二真空泵和第二缓冲罐，所述第二吸附塔组包括多台并联设置的第二吸附塔，每一个第二吸附塔内均填充有第二吸附剂；其中，所述第一二氧化碳压缩机的入口连通于所述碳氮分离系统，所述第一二氧化碳压缩机的出口连通于所述第三气液分离器的入口，所述第三气液分离器的出口连通于所述第二吸附塔组的进气口，所述第二吸附塔组的塔顶出气口连通于所述氮气浓缩提纯系统，所述第二吸附塔组的塔底出气口连通于所述第二真空泵的入口，所述第二真空泵的出口连通于所述第二缓冲罐的入口。
如上所述的锅炉烟道气同步回收氮气和二氧化碳的系统，可选地，所述氮气浓缩提纯系统包括第三缓冲罐、氮气压缩机、第二干燥器、过滤器和第三吸附塔组，所述第三吸附塔组包括并联设置的多台第三吸附塔，所述第三吸附塔内填充有第三吸附剂；其中，所述第三缓冲罐的入口与所述碳氮分离系统和所述二氧化碳二次提纯系统连通，所述第三缓冲罐的出口连通于所述氮气压缩机的入口，所述氮气压缩机的出口连通于所述第二干燥器的入口，所述第二干燥器的出口连通于所述过滤器的入口，所述过滤器的出口与所述第三吸附塔组的进气口连通，所述第三吸附塔组的顶部出气口得到产品氮气。
如上所述的锅炉烟道气同步回收氮气和二氧化碳的系统，可选地，所述第三吸附塔的吸附压力为0.7-1.0MPa，所述产品氮气的体积浓度为99％-99.999％。
如上所述的锅炉烟道气同步回收氮气和二氧化碳的系统，可选地，所述系统还包括二氧化碳精制液化系统，所述二氧化碳精制液化系统连通于所述二氧化碳二次提纯系统，用于精制二氧化碳。
如上所述的锅炉烟道气同步回收氮气和二氧化碳的系统，可选地，所述二氧化碳精制液化系统包括第二冷却器、第四气液分离器、第二二氧化碳压缩机、第四缓冲罐、脱硫塔组、干燥塔组、第三冷却器、液化模块、精馏模块和二氧化碳储罐；其中，所述第二冷却器的入口连通于所述二氧 化碳二次提纯系统，所述第二冷却器的出口连通于所述第四气液分离器的入口，所述第四气液分离器的出口连通于所述第二二氧化碳压缩机的入口，所述第二二氧化碳压缩机的出口连通于所述第四缓冲罐的入口，所述第四缓冲罐的出口连通于所述脱硫塔组的入口，所述脱硫塔组的出口连通于所述干燥塔组的入口，所述干燥塔组的出口连通于所述第三冷却器的入口，所述第三冷却器的出口连通于所述液化模块的入口，所述液化模块的出口连通于所述精馏模块的入口，所述精馏模块的底部出口连通于所述二氧化碳储罐。本发明还提出了一种锅炉烟道气同步回收氮气和二氧化碳的方法，采用如上所述的锅炉烟道气同步回收氮气和二氧化碳的系统同步回收氮气和二氧化碳，所述方法包括以下步骤：
步骤(1)，将锅炉烟道气通入烟道气预处理系统中，进行脱水和降温，得到预处理后的烟道气；
步骤(2)，将预处理后的烟道气通入碳氮分离系统中，进行变压吸附预处理并分离出含氮放空气和粗二氧化碳气体，其中，碳氮分离系统的吸附压力为0.20-0.4MPa；
步骤(3)，将碳氮分离系统分离出的粗二氧化碳气体通入二氧化碳二次提纯系统中，进行二次提纯，得到提纯二氧化碳气体，并产生含氮放空气；
步骤(4)，将碳氮分离系统分离出的含氮放空气和二氧化碳二次提纯系统产生的含氮放空气通入氮气浓缩提纯系统中，进行提纯，得到产品氮气；
优选地，步骤(3)之后还包括：步骤(31)，将提纯二氧化碳气体通入二氧化碳精制液化系统中，进行精制处理，得到精制二氧化碳气体。
本发明相对于现有技术取得了以下技术效果：
(1)本发明的锅炉烟道气同步回收氮气和二氧化碳的系统能够最大程度的回收二氧化碳和氮气，无三废产生。并且，本发明的碳氮分离系统，采用0.20-0.40MPa的低压吸附模式分离二氧化碳和氮气，改变了以往技术在1.0MPa下吸附的情况，能耗有效降低。
(2)本发明的碳氮分离系统中解吸气采用真空泵解吸，不但降低了 能耗，而且还提高了二氧化碳的回收率。
(3)本发明的氮气浓缩提纯系统，采用二次压缩模式，会有二次提压过程，能够根据实际用户需求的氮气量选择压缩机的型号及压缩压力，从而进一步起到节能的目的。
附图说明
构成本发明的一部分的说明书附图用来提供对本发明的进一步理解，本发明的示意性实施例及其说明用于解释本发明，并不构成对本发明的不当限定。其中：
图1为本发明实施例的锅炉烟道气同步回收氮气和二氧化碳的系统的流程示意图；
图2为本发明实施例的烟气预处理系统的流程示意图；
图3为本发明实施例的碳氮分离系统的流程示意图；
图4为本发明实施例的二氧化碳二次提纯系统的流程示意图；
图5为本发明实施例的二氧化碳精制液化系统的流程示意图；
图6为本发明实施例的氮气浓缩提纯系统的流程示意图。
附图标记说明：1-烟气预处理系统；2-碳氮分离系统；3-二氧化碳二次提纯系统；4-二氧化碳精制液化系统；5-氮气浓缩提纯系统；11-第一冷却器；12-第一气液分离器；13-烟气引风机；
21-烟气压缩机；22-第二气液分离器；23-第一干燥器；24-第一吸附塔组；25-第一真空泵；
31-第一二氧化碳压缩机；32-第三气液分离器；33-第二吸附塔组；34-第二真空泵；35-第二缓冲罐；
41-第二冷却器；42-第四气液分离器；43-第二二氧化碳压缩机；43a-第四缓冲罐；44-脱硫塔组；45-干燥塔组；46-第三冷却器；47-液化模块；48-精馏模块；49-二氧化碳储罐；
51-第三缓冲罐；52-氮气压缩机；53-第二干燥器；54-过滤器；55-第三吸附塔组。
具体实施方式
下面将对本发明实施例中的技术方案进行清楚、完整地描述，显然， 所描述的实施例仅仅是本发明的一部分实施例，而不是全部的实施例。基于本发明中的实施例，本领域普通技术人员所获得的所有其他实施例，都属于本发明保护的范围。
下面将结合实施例来详细说明本发明。需要说明的是，在不冲突的情况下，本发明中的实施例及实施例中的特征可以相互组合。
针对现有技术存在的问题，本发明提出了一种节能型的锅炉烟道气同步回收氮气和二氧化碳的系统，如图1所示，该系统包括烟道气预处理系统1、碳氮分离系统2、二氧化碳二次提纯系统3、二氧化碳精制液化系统4和氮气浓缩提纯系统5。
其中，烟道气预处理系统1，用于对锅炉烟道气进行脱水和降温；碳氮分离系统2与烟道气预处理系统1连通，用于变压吸附预处理后的烟道气并分离出含氮放空气和粗二氧化碳气体，碳氮分离系统2的吸附压力为0.20-0.40MPa；二氧化碳二次提纯系统3与碳氮分离系统2连通，用于对碳氮分离系统2分离出的粗二氧化碳气体进行二次提纯；氮气浓缩提纯系统5与碳氮分离系统2和二氧化碳二次提纯系统3连通，用于对碳氮分离系统2分离出的含氮放空气和二氧化碳二次提纯系统3产生的放空气进行提纯；二氧化碳精制液化系统4连通于二氧化碳二次提纯系统3，用于精制二氧化碳。
本发明的碳氮分离系统2，采用0.20-0.40MPa(比如0.20MPa、0.22MPa、0.25MPa、0.27MPa、0.30MPa、0.32MPa、0.35MPa、0.37MPa或0.40MPa)的低压吸附模式分离二氧化碳和氮气，改变了以往技术在1.0MPa下吸附的情况，能耗有效降低。
如图2所示，本发明的可选实施例中，烟道气预处理系统1包括第一冷却器11、第一气液分离器12和烟气引风机13，第一冷却器11的入口连通锅炉烟道，第一冷却器11的出口连通第一气液分离器12的入口，第一气液分离器12的出口连通烟气引风机13的入口，烟气引风机13的出口连通碳氮分离系统2。
如图3所示，本发明的可选实施例中，碳氮分离系统2包括烟气压缩机21、第二气液分离器22、第一干燥器23、第一吸附塔组24、第一真空泵25和第一缓冲罐(未图示)，第一吸附塔组24包括多台并联设置的第 一吸附塔，每一第一吸附塔内均填充有第一吸附剂；其中，烟气压缩机21的入口连通烟道气预处理系统1的烟气引风机13出口，烟气压缩机21的出口与第二气液分离器22的入口连通，第二气液分离器22的出口与第一干燥器23的入口连通，第一干燥器23的出口连通与第一吸附塔组24的进气口连通，第一吸附塔组24的顶部出气为含氮放空气，底部出气为粗二氧化碳气体，第一吸附塔组24的塔顶出气口与氮气浓缩提纯系统5连通，第一吸附塔组24的塔底出气口与第一真空泵25的入口连通，第一真空泵25的出口与第一缓冲罐的入口连通，第一缓冲罐的出口与二氧化碳二次提纯系统3连通。
本发明的含氮放空气中氮气体积浓度为88％-90％(比如88％、89％或90％)，粗二氧化碳气体中二氧化碳的体积浓度为45％-80％(比如45％、46％、47％、48％、49％、50％、60％、70％或80％)。
进一步地，连接所述烟气压缩机21出口的管道上设置有第一气动阀，第一气动阀上设置有第一电磁阀，第一电磁阀与PLC电性连接，如此，第一气动阀由PLC通过第一电磁阀控制。
本实施例中，经烟道气预处理系统1处理后的烟道气经烟气压缩机21提到0.25MPa左右的压缩烟气，进入第一吸附塔组24，PLC通过第一电磁阀控制第一气动阀来保证不同第一吸附塔的不同工作状态，塔顶出气为富氮气体进入氮气浓缩提纯系统作为原料气，塔底出气为50％左右的粗二氧化碳气体，作为下级的原料气。
如图4所示，本发明的可选实施例中，二氧化碳二次提纯系统3包括第一二氧化碳压缩机31、第三气液分离器32、第二吸附塔组33、第二真空泵34和第二缓冲罐35，第二吸附塔组33包括多台并联设置的第二吸附塔，每一个第二吸附塔内均填充有第二吸附剂；其中，第一二氧化碳压缩机31的入口连通于碳氮分离系统2中第一缓冲罐的出口，第一二氧化碳压缩机31的出口连通于第三气液分离器32的入口，第三气液分离器32的出口连通于第二吸附塔组33的进气口，第二吸附塔组33的塔顶出气口连通于氮气浓缩提纯系统5，第二吸附塔组33的塔底出气口连通于第二真空泵34的入口，第二真空泵34的出口连通于第二缓冲罐35的入口。
优选地，连接第一二氧化碳压缩机31出口的管道上设置有第二气动阀，第二气动阀上设置有第二电磁阀，第二电磁阀与PLC电性连接，如此，第二气动阀由PLC通过第二电磁阀控制。
本实施例中，第二吸附塔设置有多台，并由PLC通过第二电磁阀控制第二气动阀，来保证不同第二吸附塔的不同工作状态，塔顶出气为富氮气体进入氮气浓缩提纯系统作为原料气或者放空，塔底出气为95％左右的二氧化碳气体，作为精制二氧化碳的原料气。
如图5所示，本发明的可选实施例中，所述二氧化碳精制液化系统4包括第二冷却器41、第四气液分离器42、第二二氧化碳压缩机43、第四缓冲罐43a、脱硫塔组44、干燥塔组45、第三冷却器46、液化模块47、精馏模块48和二氧化碳储罐49；其中，第二冷却器41的入口连通于二氧化碳二次提纯系统3的解吸气(即连通于第二缓冲罐35的出口)，第二冷却器41的出口连通于第四气液分离器42的入口，第四气液分离器42的出口连通于第二二氧化碳压缩机43的入口，压缩到2.5MPa的二氧化碳气体，从第二二氧化碳压缩机43的出口进入到第四缓冲罐43a的入口，第四缓冲罐43a的出口连通于脱硫塔组44的入口，经过杂质硫的脱硫后，由脱硫塔组44的出口进入干燥塔组45的入口，进行深度干燥除水，干燥塔组45的出口连通于第三冷却器46的入口，进行降温处理，第三冷却器46的出口连通于液化模块47的入口，液化模块47的出口进入精馏模块48的入口，精馏得到的是体积浓度为≥99.9％的食品级二氧化碳产品，从精馏模块48的底部出口进入至二氧化碳储罐49进行储存。
需要说明的是，脱硫塔组44包括多个并联设置的脱硫塔，干燥塔组45包括多个并联设置的干燥塔，精馏模块48包括精馏塔。
如图6所示，本发明的可选实施例中，氮气浓缩提纯系统5包括第三缓冲罐51、氮气压缩机52、第二干燥器53、过滤器54和第三吸附塔组55，第三吸附塔组55包括并联设置的多台第三吸附塔，第三吸附塔内填充有第三吸附剂；其中，第三缓冲罐51的入口与碳氮分离系统2和二氧化碳二次提纯系统3的放空气连通，第三缓冲罐51的出口连通于氮气压缩机52的入口，氮气压缩机52的出口连通于第二干燥器53的入口，第二干燥器53的出口连通于过滤器54的入口，过滤器54的出口与第三吸 附塔组55的进气口连通，第三吸附塔组55的顶部出气口得到产品氮气。
可选地，第三吸附塔的吸附压力为0.7-1.0MPa(比如0.7MPa、0.75MPa、0.8MPa、0.9MPa或1.0MPa)，所述产品氮气的体积浓度为99％-99.999％。
可以理解的，本发明的氮气浓缩提纯系统5，将碳氮分离系统2和二氧化碳二次提纯系统3所产生的两段放空气进行回收，经压缩过滤后，0.7-1.0MPa压力的气体，进入第三吸附塔，第三吸附塔装填有第三吸附剂，针对成分复杂的放空气，具有高的回收率，经过多塔变压吸附分离，塔顶得到体积浓度为99％-99.999％的产品氮气。
需要说明的是，本发明所采用的第一吸附剂、第二吸附剂及第三吸附剂均为现有吸附剂。
本发明还提出了一种锅炉烟道气同步回收氮气和二氧化碳的方法，采用如上所述的锅炉烟道气同步回收氮气和二氧化碳的系统，所述方法包括以下步骤：
步骤(1)，将锅炉烟道气通入烟道气预处理系统中，进行脱水和降温，得到预处理后的烟道气；
步骤(2)，将预处理后的烟道气通入碳氮分离系统中，进行变压吸附预处理并分离出含氮放空气和粗二氧化碳气体，其中，碳氮分离系统的吸附压力为0.20-0.40MPa；
步骤(3)，将碳氮分离系统分离出的粗二氧化碳气体通入二氧化碳二次提纯系统中，进行二次提纯，得到提纯二氧化碳气体，并产生放空气；
步骤(4)，将碳氮分离系统分离出的含氮放空气和二氧化碳二次提纯系统产生的放空气通入氮气浓缩提纯系统中，进行提纯，得到产品氮气；
优选地，步骤(3)之后还包括：步骤(31)，将提纯二氧化碳气体通入二氧化碳精制液化系统中，进行精制处理，得到精制二氧化碳气体。
下面通过一具体实施例对本发明的锅炉烟道气同步回收氮气和二氧化碳的系统和方法进行详细说明。
本发明实施例用于某煤电厂的烟道气中二氧化碳和氮气回收，二氧化碳气体用于智慧农业的增收，氮气用于本厂化工车间的置换和吹扫。其中 烟道气的成分如表1所示。
表1烟道气的成分
成分 二氧化硫 氮氧化物 一氧化碳 二氧化碳 氧气 水
实测值 0mg/m 3 31mg/m 3 未检出 13％ 6.20％ 12.50％
检出限 2mg/m 3 2mg/m 3 20mg/m 3 0.03％ —— ——
参考图1至图6所示，从脱硫脱硝后的烟气排放烟囱引出所需烟道气，进入第一冷却器11进行初步降温至35℃左右，进入第一气液分离器12中进行气液分离，然后进入烟气引风机13，烟气引风机13的出气压力为5KPa。
烟气自烟气引风机13出口，进入烟气压缩机21，压至0.23MPa后，进入第二气液分离器22，然后进入第一干燥器23深度脱水后，进入第一吸附塔组24进行吸附分离，塔顶得到含氮量88～90％的放空气，该放空气作为氮气浓缩提纯系统的原料气。塔底经第一真空泵25解吸后得到的解吸气为二氧化碳体积为含量45％，压力15KPa的粗二氧化碳气体。
含量45％的粗二氧化碳气体，经第一二氧化碳压缩机31压缩至0.25MPa，进入第三气液分离器32中进行气液分离，然后进入第二吸附塔组33进一步提纯二氧化碳，塔顶得到二氧化碳二次提纯放空气，引入氮气浓缩提纯系统5的原料气管，塔底经第二真空泵34解吸得到纯度为95％，压力15kPa左右的二氧化碳气体，储存在第二缓冲罐35中。
95％的二氧化碳气体经第二冷却器41和第四气液分离器42，再次进行降温除水后，经第二二氧化碳压缩机43提升压力至2.5MPa，然后进入第四缓冲罐43a的入口，第四缓冲罐43a的出口连通于脱硫塔组44的入口，之后依次进入脱硫塔组44和干燥塔组45进行脱硫除杂干燥后，进入第三冷却器46降温后，进入液化模块47，降温至-18℃后至液体状态，液态二氧化碳进入精馏模块48精制提纯后，塔底为99.9％食品级二氧化碳，进入二氧化碳储罐49储存。塔顶放空气作为脱硫塔组和干燥塔组的再生气源，节约产品气，降低能耗。
碳氮分离系统2和二氧化碳二次提纯系统3中吸附塔塔顶产出的放空 气，进入第三缓冲罐51，然后进入氮气压缩机52，提压至0.8～1.0MPa，进入第二干燥器53和过滤器54中进行除水干燥、过滤净化后，进入第三吸附塔组55变压吸附得产品氮气，纯度从99.5％～99.9％不等。
本实施例中，碳氮分离系统采用低压吸附模式，吸附压力为0.25MPa，改变了以往技术在1.0MPa下吸附的情况，且解吸气采用真空泵解吸，不但降低了能耗，而且提高了二氧化碳的回收率。氮气浓缩提纯系统，采用二次压缩模式，将压力从0.23MPa提高至0.8～1.0MPa，且只针对根据实际用户需求的氮气量选择压缩机的型号，比起针对大量烟气进行压缩的压缩机，此处压缩的气量为仅为烟气压缩的68％。本实施例中，烟气压缩从0.01MPa提至0.8～1.0MPa，放空气压缩是从0.23MPa提至0.8～1.0MPa。压缩的气量还减小为68％，由此可看出，本发明的系统节能效果显而易见。
以上所述仅为本发明的优选实施例，并不用于限制本发明，对于本领域的技术人员来说，本发明可以有各种更改和变化。凡在本发明的精神和原则之内，所作的任何修改、等同替换、改进等，均应包含在本发明的保护范围之内。

Claims (10)

  1. 一种锅炉烟道气同步回收氮气和二氧化碳的系统，其特征在于，所述系统包括：
    烟道气预处理系统，用于对锅炉烟道气进行脱水和降温；
    碳氮分离系统，与所述烟道气预处理系统连通，用于变压吸附预处理后的烟道气并分离出含氮放空气和粗二氧化碳气体，所述碳氮分离系统的吸附压力为0.20-0.40MPa；
    二氧化碳二次提纯系统，与所述碳氮分离系统连通，用于对所述碳氮分离系统分离出的粗二氧化碳气体进行二次提纯；
    氮气浓缩提纯系统，与所述碳氮分离系统和所述二氧化碳二次提纯系统连通，用于对所述碳氮分离系统分离出的含氮放空气和所述二氧化碳二次提纯系统产生的放空气进行提纯。
  2. 如权利要求1所述的锅炉烟道气同步回收氮气和二氧化碳的系统，其特征在于，所述烟道气预处理系统包括第一冷却器、第一气液分离器和烟气引风机，所述第一冷却器的入口连通锅炉烟道，所述第一冷却器的出口连通所述第一气液分离器的入口，所述第一气液分离器的出口连通所述烟气引风机的入口，所述烟气引风机的出口连通所述碳氮分离系统。
  3. 如权利要求1所述的锅炉烟道气同步回收氮气和二氧化碳的系统，其特征在于，所述碳氮分离系统包括烟气压缩机、第二气液分离器、第一干燥器、第一吸附塔组、第一真空泵和第一缓冲罐，所述第一吸附塔组包括多台并联设置的第一吸附塔，每一所述第一吸附塔内均填充有第一吸附剂；
    其中，所述烟气压缩机的入口连通所述烟道气预处理系统，所述烟气压缩机的出口与所述第二气液分离器的入口连通，所述第二气液分离器的出口与所述第一干燥器的入口连通，所述第一干燥器的出口连通与所述第一吸附塔组的进气口连通，所述第一吸附塔组的顶部出气为含氮放空气，底部出气为粗二氧化碳气体，所述第一吸附塔组的塔顶出气口与所述氮气 浓缩提纯系统连通，所述第一吸附塔组的塔底出气口与所述第一真空泵的入口连通，所述第一真空泵的出口与所述第一缓冲罐的入口连通，所述第一缓冲罐的出口与所述二氧化碳二次提纯系统连通。
  4. 如权利要求3所述的锅炉烟道气同步回收氮气和二氧化碳的系统，其特征在于，所述含氮放空气中氮气体积浓度为88％-90％，所述粗二氧化碳气体中二氧化碳的体积浓度为45％-80％。
  5. 如权利要求1所述的锅炉烟道气同步回收氮气和二氧化碳的系统，其特征在于，所述二氧化碳二次提纯系统包括第一二氧化碳压缩机、第三气液分离器、第二吸附塔组、第二真空泵和第二缓冲罐，所述第二吸附塔组包括多台并联设置的第二吸附塔，每一个第二吸附塔内均填充有第二吸附剂；
    其中，所述第一二氧化碳压缩机的入口连通于所述碳氮分离系统，所述第一二氧化碳压缩机的出口连通于所述第三气液分离器的入口，所述第三气液分离器的出口连通于所述第二吸附塔组的进气口，所述第二吸附塔组的塔顶出气口连通于所述氮气浓缩提纯系统，所述第二吸附塔组的塔底出气口连通于所述第二真空泵的入口，所述第二真空泵的出口连通于所述第二缓冲罐的入口。
  6. 如权利要求1所述的锅炉烟道气同步回收氮气和二氧化碳的系统，其特征在于，所述氮气浓缩提纯系统包括第三缓冲罐、氮气压缩机、第二干燥器、过滤器和第三吸附塔组，所述第三吸附塔组包括并联设置的多台第三吸附塔，所述第三吸附塔内填充有第三吸附剂；
    其中，所述第三缓冲罐的入口与所述碳氮分离系统和所述二氧化碳二次提纯系统连通，所述第三缓冲罐的出口连通于所述氮气压缩机的入口，所述氮气压缩机的出口连通于所述第二干燥器的入口，所述第二干燥器的出口连通于所述过滤器的入口，所述过滤器的出口与所述第三吸附塔组的进气口连通，所述第三吸附塔组的顶部出气口得到产品氮气。
  7. 如权利要求6所述的锅炉烟道气同步回收氮气和二氧化碳的系统，其特征在于，所述第三吸附塔的吸附压力为0.7-1.0MPa，所述产品氮气的体积浓度为99％-99.999％。
  8. 如权利要求1-7中任一项所述的锅炉烟道气同步回收氮气和二氧化碳的系统，其特征在于，所述系统还包括二氧化碳精制液化系统，所述二氧化碳精制液化系统连通于所述二氧化碳二次提纯系统，用于精制二氧化碳。
  9. 如权利要求8所述的锅炉烟道气同步回收氮气和二氧化碳的系统，其特征在于，所述二氧化碳精制液化系统包括第二冷却器、第四气液分离器、第二二氧化碳压缩机、第四缓冲罐、脱硫塔组、干燥塔组、第三冷却器、液化模块、精馏模块和二氧化碳储罐；
    其中，所述第二冷却器的入口连通于所述二氧化碳二次提纯系统，所述第二冷却器的出口连通于所述第四气液分离器的入口，所述第四气液分离器的出口连通于所述第二二氧化碳压缩机的入口，所述第二二氧化碳压缩机的出口连通于所述第四缓冲罐的入口，所述第四缓冲罐的出口连通于所述脱硫塔组的入口，所述脱硫塔组的出口连通于所述干燥塔组的入口，所述干燥塔组的出口连通于所述第三冷却器的入口，所述第三冷却器的出口连通于所述液化模块的入口，所述液化模块的出口连通于所述精馏模块的入口，所述精馏模块的底部出口连通于所述二氧化碳储罐。
  10. 一种锅炉烟道气同步回收氮气和二氧化碳的方法，其特征在于，采用如权利要求1-9中任一项所述的锅炉烟道气同步回收氮气和二氧化碳的系统同步回收氮气和二氧化碳，所述方法包括以下步骤：
    步骤(1)，将锅炉烟道气通入烟道气预处理系统中，进行脱水和降温，得到预处理后的烟道气；
    步骤(2)，将预处理后的烟道气通入碳氮分离系统中，进行变压吸附 预处理并分离出含氮放空气和粗二氧化碳气体，其中，碳氮分离系统的吸附压力为0.20-0.40MPa；
    步骤(3)，将碳氮分离系统分离出的粗二氧化碳气体通入二氧化碳二次提纯系统中，进行二次提纯，得到提纯二氧化碳气体，并产生含氮放空气；
    步骤(4)，将碳氮分离系统分离出的含氮放空气和二氧化碳二次提纯系统产生的含氮放空气通入氮气浓缩提纯系统中，进行提纯，得到产品氮气；
    步骤(3)之后还包括：步骤(31)，将提纯二氧化碳气体通入二氧化碳精制液化系统中，进行精制处理，得到精制二氧化碳气体。
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