CN108043145B - Turbulent jet coupling integrated flue gas purification process for complex and difficult-to-treat flue gas - Google Patents

Turbulent jet coupling integrated flue gas purification process for complex and difficult-to-treat flue gas Download PDF

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CN108043145B
CN108043145B CN201711390453.XA CN201711390453A CN108043145B CN 108043145 B CN108043145 B CN 108043145B CN 201711390453 A CN201711390453 A CN 201711390453A CN 108043145 B CN108043145 B CN 108043145B
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flue gas
liquid
turbulent
washing
section
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CN108043145A (en
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宋小良
徐光泽
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Shuangdun Environment Technology Co ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
    • B01D47/06—Spray cleaning
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
    • 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
    • B01D53/14—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 absorption
    • B01D53/1456—Removing acid components
    • 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
    • B01D53/14—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 absorption
    • B01D53/1456—Removing acid components
    • B01D53/1468—Removing hydrogen sulfide
    • 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
    • B01D53/14—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 absorption
    • B01D53/1456—Removing acid components
    • B01D53/1481—Removing sulfur dioxide or sulfur trioxide
    • 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
    • B01D53/14—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 absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/204—Inorganic halogen compounds
    • B01D2257/2045—Hydrochloric acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/204—Inorganic halogen compounds
    • B01D2257/2047—Hydrofluoric acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • 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

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  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

The invention discloses a turbulent impact injection coupling integrated flue gas purification process for complex and difficult-to-treat flue gas, which comprises the following steps of: a. the flue gas to be treated is vertically sent into a turbulent washing section through a flue; b. the turbulent flushing nozzle sprays washing absorption liquid from bottom to top to collide with the flue gas flowing from top to bottom at high speed, so as to capture dust and dissolve and absorb target components; c. the fume treated by the turbulent washing section continuously enters the scaling spraying section downwards and fully collides with the washing absorption liquid at the necking part of the scaling spraying section again to capture micron and submicron dust and further dissolve and absorb target components; d. the flue gas treated by the convergent-divergent jet section and the liquid drops carried by the flue gas continuously enter the gas-liquid separator downwards to separate partial liquid drops, and then the flue gas is discharged from the top of the gas-liquid separator. Compared with the conventional process, the process saves energy by more than 30 percent, saves equipment investment by more than 35 percent, saves occupied land by more than 40 percent, and improves the dust removal and washing efficiency by more than 5 to 20 percent.

Description

Turbulent jet coupling integrated flue gas purification process for complex and difficult-to-treat flue gas
Technical Field
The invention relates to the technical field of flue gas treatment, in particular to a turbulent jet coupling integrated flue gas purification process for removing particulate matters or heavy metals from flue gas, removing target components from the flue gas, and particularly removing high-concentration fine particulate matters with complex physical properties, wherein the process can play a good role in purifying, washing, absorbing and environment-friendly treatment of flue gas of various fuels, smelting and heating kilns.
Background
The flue gas discharged by various kilns is washed, purified and dedusted, and the target components (such as common SO)2、HF、HCl、NOx、H2S gas, etc.) is always an important process unit for flue gas cleaning treatment, and many methods are used: such as empty tower washing and purifying, packed tower washing and purifying, sieve plate tower washing and purifying, turbulent ball tower washing and purifying, dynamic wave washing and purifying, venturi tube washing and purifying and the like, but the method needs the split combination of a plurality of methods for the difficult-to-treat complex high-concentration dust-containing granular flue gas, and the one-step method is always difficult to completely purify.
Disclosure of Invention
The invention aims to provide a turbulent jet coupling integrated flue gas purification process for removing particulate matters or heavy metals in flue gas, removing target components in the flue gas, and particularly removing high-concentration fine particulate matters with complex physical properties, wherein the process can play a good role in removing complex and intractable flue gas.
The invention aims to solve the problems by the following technical scheme:
a turbulent impact injection coupling integrated flue gas purification process for complex and difficult-to-treat flue gas is characterized in that: the process comprises the following steps:
a. contains high-concentration difficult-to-process particles with complicated physical properties and SO which needs to be purified and absorbed2、HF、HCl、NOx、H2The flue gas of one or more target components in the S is vertically conveyed into a turbulent washing section through a flue;
b. the turbulent flushing nozzle positioned at the middle lower part of the turbulent flushing washing section sprays washing absorption liquid from bottom to top to collide with flue gas flowing rapidly from top to bottom at high speed so as to capture dust and dissolve and absorb target components;
c. the flue gas treated by the turbulent washing section continuously enters the scaling spraying section downwards, the washing absorption liquid under the turbulent washing section fully collides with the high-speed kinetic energy flue gas again at the necking part of the scaling spraying section to capture micron and submicron dust and further dissolve and absorb target components;
d. the flue gas treated by the convergent-divergent jet section and the liquid drops carried by the flue gas continuously enter the gas-liquid separator downwards to separate partial liquid drops, and then the flue gas is discharged from the top of the gas-liquid separator.
The high-concentration difficult-to-process particles with complicated physical properties in the step (a) mean that the dust content is 0.5g/m3～50g/m3And dust having a particle diameter of 0.01 to 3.0 μm.
And (b) the turbulent flushing nozzle sprays a washing absorption liquid column with the height of 5-7 m from bottom to top, the liquid column rises spirally and is dispersed into fine water drops to collide with the flue gas with the flow rate of 13-30 m/s from top to bottom at high speed to form a suspended foam gas-liquid mixed phase, and dust collection and dissolution and absorption of target components are carried out.
The liquid spraying amount of the turbulent spray nozzle in the step (b) is 1.5L/m3～7.0L/m3。
The turbulent spray heads in the step (b) are large open-hole spray heads made of corrosion-resistant alloy steel or engineering plastics F4/F46/HPE/FRP/SiC, and the number of the turbulent spray heads is 1-6.
The scaling and spraying section in the step (c) is coaxially and vertically arranged below the turbulent washing section, the inner cavity of the scaling and spraying section is subjected to necking treatment, the inlet angle and the outlet angle of the scaling and spraying section are respectively 20-30 degrees and 7-15 degrees, the flow rate of flue gas at the throat is 25-50 m/s, washing absorption liquid under the turbulent washing section is fully subjected to transverse impact and longitudinal friction chopping with high-speed kinetic energy flue gas at the necking of the scaling and spraying section to carry out flue gas scaling type spraying and washing, the washing absorption liquid is broken into finer liquid drops again to form a gas-liquid highly-mixed dispersion region, micron and submicron dust is captured, and target components are further dissolved and absorbed.
And (d) arranging a prismatic bar type uniform distribution type liquid catcher or demister in the gas-liquid separator in the step (d), wherein the prismatic bar type uniform distribution type liquid catcher or demister is arranged at a position 1.2-6.0 m above a flue gas inlet of the gas-liquid separator, the flow velocity of flue gas reaching the prismatic bar type uniform distribution type liquid catcher or demister is 0.8-3.5 m/s, part of liquid drops of the flue gas carrying the liquid drops are removed by the prismatic bar type uniform distribution type liquid catcher or demister, and the flue gas is uniformly dispersed above the prismatic bar type uniform distribution type liquid catcher or demister so as to be beneficial to convergence, sedimentation and separation of the liquid drops.
The prismatic rod type uniform distribution type liquid catcher or the demister in the step (d) is arranged in a single layer or multiple layers, a flushing spray head is arranged above the prismatic rod type uniform distribution type liquid catcher or the demister in the single layer, the flushing spray head is arranged in the middle of the prismatic rod type uniform distribution type liquid catcher or the demister in the multiple layer arrangement, and a liquid inlet of the flushing spray head is communicated with the flushing pipe.
And (d) connecting the bottom liquid storage area of the gas-liquid separator in the step (d) with the liquid inlet of the turbulent nozzle through a circulating pipe with a circulating pump.
And a liquid supplementing port communicated with the liquid supplementing pipe is arranged on the upper side of the liquid storage area at the bottom of the gas-liquid separator, and the liquid supplementing port is positioned on the lower side of the flue gas inlet.
The circulating pumps are arranged on the circulating pipe in parallel.
The circulating pipe is provided with a side branch pipe, the outlet end of the side branch pipe is communicated with the raw material inlet of the concentrator, and the side branch pipe runs on line to densely concentrate dust and mud in the washing absorption liquid and discharge the dust and mud out of the washing absorption liquid circulating system; the overflow groove of the concentrator is communicated with the clear liquid groove through a clear liquid pipe.
The clear liquid groove is connected with an annular overflow weir at the top end of the turbulent washing section through a water curtain liquid supply pipe with a clear liquid pump, and clear liquid in the annular overflow weir descends on the vertical inner pipe wall of the turbulent washing section to form a water curtain so as to protect the impact erosion of high-temperature flue gas.
The content of dust particles in the flue gas discharged from the top of the gas-liquid separator in the step (d) is 0.05g/m3～0.35g/m3And a tail exhaust gas analysis device is arranged at the flue gas outlet at the top of the gas-liquid separator.
And (d) connecting a flue gas discharge port at the top of the gas-liquid separator in the step (d) with a wet electric dust collector through a flue gas discharge pipe for subsequent flue gas treatment, and realizing dust removal and ultra-clean discharge.
The turbulent washing section and the zooming injection section are of an upper-lower integrated coupling structure, the bottom of the zooming injection section is connected with the gas-liquid separator, and the turbulent washing section is made of corrosion-resistant alloy steel, metal lining ceramic tiles, graphite bricks, or high-temperature resistant engineering plastics FRP/PP/PE/CPVC/PVD/PTFE or engineering plastics; the zooming injection section is made of corrosion-resistant alloy steel, lead-antimony alloy or engineering plastic FRP/F4/F46/HPE/CPVC/SiC or a compound of engineering plastic.
Compared with the prior art, the invention has the following advantages:
the invention couples the vertical turbulent washing section and the convergent-divergent jet section into the turbulent jet washer to wash, purify and absorb the complex and difficult-to-treat flue gas and carry out gas-liquid separation, wherein the content of dust particles in the treated flue gas is 0.05g/m3～0.35g/m3Compared with the traditional flue gas multistage washing process, the power consumption of the energy-saving pump is more than 30%, the equipment investment is saved by more than 35%, the occupied land is saved by more than 40%, the dust removal washing efficiency is improved by more than 5-20%, and the subsequent flue gas treatment can be realized by adding humidityThe electric dust remover is further processed to realize dust removal and ultra-clean discharge; the process has the advantages of high flue gas purification strength, investment saving, high efficiency and obvious energy-saving effect, and is suitable for popularization and application.
Drawings
FIG. 1 is a schematic structural diagram of a device used in the turbulent jet coupling integrated flue gas purification process of the present invention.
Wherein: 1-turbulent jet washer; 2, an annular overflow weir; 3-turbulent washing section; 4-turbulent flushing spray head; 5, a zooming injection section; 6-gas-liquid separator; 7-a prismatic bar type uniform distribution type catcher or demister; 8-washing the spray head; 9-tail exhaust gas analysis equipment; 10-a flushing pipe; 11-fluid infusion tube; 12-a circulating pump; 13-circulation pipe; 14-a bypass pipe; 15-a concentrator; 16-a clear liquid pipe; 17-a clear liquid groove; 18-clear liquid pump; 19-water curtain liquid supply pipe.
Detailed Description
The invention is further described with reference to the following figures and examples.
As shown in fig. 1: a turbulent impact injection coupling integrated flue gas purification process for complex and difficult-to-treat flue gas comprises the following steps: a. contains high-concentration difficult-to-process particles with complicated physical properties and SO which needs to be purified and absorbed2、HF、HCl、NOx、H2The flue gas of one or more target components in S is vertically sent into a turbulent washing section 3 through a flue, wherein the high-concentration difficult-to-treat physical property complex particulate matters mean that the dust content is 0.5g/m3～50g/m3The dust with the grain diameter of 0.01-3.0 μm has the characteristics of high viscosity and weak hydrophilicity; b. the turbulent flushing nozzle 4 positioned at the middle lower part of the turbulent flushing washing section 3 sprays a washing absorption liquid column with the height of 5 m-7 m from bottom to top, the liquid column rises spirally and disperses to form fine water drops which collide with flue gas with the flow rate of 13 m/s-30 m/s from top to bottom at high speed to form a suspended foam gas-liquid mixed phase for dust capture and dissolution and absorption of target components; c. the flue gas treated by the turbulent washing section 3 continuously enters the scaling spraying section 5 downwards, and washing absorption liquid falling from the turbulent washing section 3 fully performs transverse impact and longitudinal friction with the high-speed kinetic energy flue gas at the necking part of the scaling spraying section 5Cutting up the powder, spraying and washing the powder in a smoke scaling mode, scattering the washing absorption liquid into finer liquid drops again to form a gas-liquid high-degree mixed dispersion area, capturing micron and submicron-grade dust, and further dissolving and absorbing target components; d. the flue gas treated by the convergent-divergent jet section 5 and the liquid drops carried by the flue gas continuously enter a gas-liquid separator 6 downwards to separate partial liquid drops, and the content of dust particle substances is 0.05g/m3～0.35g/m3Is discharged from the top of the gas-liquid separator 6. The turbulent washing section 3 and the zooming injection section 5 are of an upper-lower integrated coupling structure, the bottom of the zooming injection section 5 is connected with a gas-liquid separator 6, wherein the turbulent washing section 3 is made of corrosion-resistant alloy steel, metal-lined ceramic tiles, graphite bricks, or high-temperature-resistant engineering plastics FRP/PP/PE/CPVC/PVD/PTFE or engineering plastics, the turbulent washing section 3 has no obstacles, is self-flushing and clean, does not accumulate mud and is not blocked, and is suitable for treating smoke containing high-concentration difficult-to-treat physical-property complex particles; the turbulent spray heads 4 are large-opening spray heads made of corrosion-resistant alloy steel or engineering plastics F4/F46/HPE/FRP/SiC, the number of the turbulent spray heads 4 is 1-6, and the liquid injection amount of the turbulent spray heads 4 is 1.5L/m3～7.0L/m3(ii) a The scaling and spraying section 5 is made of corrosion-resistant alloy steel, lead-antimony alloy or engineering plastics FRP/F4/F46/HPE/CPVC/SiC or engineering plastics, the scaling and spraying section 5 is coaxially and vertically arranged below the turbulent washing section 3, the inner cavity of the scaling and spraying section 5 is necked-treated and can be assembled in a modular mode, the inlet angle of the scaling and spraying section 5 is 20-30 degrees, the outlet angle is 7-15 degrees, the flue gas flow rate at the throat is 25-50 m/s, the scaling and spraying section 5 fully utilizes washing absorption liquid falling from the turbulent washing section 3, and pumping liquid is not needed again, so that energy consumption is saved.
In the above process, a prismatic bar type uniform distribution type catch or demister 7 is arranged in the gas-liquid separator 6 to improve the gas-liquid separation effect and reduce the entrainment of droplets of the discharged flue gas, the prismatic bar type uniform distribution type catch or demister 7 is arranged at a position 1.2m to 6.0m above the flue gas inlet of the gas-liquid separator 6, the flow rate of the flue gas reaching the prismatic bar type uniform distribution type catch or demister 7 is 0.8m/s to 3.5m/s, the prismatic bar type uniform distribution type catch or demister 7 is arranged in a single layer or multiple layers, a flushing nozzle 8 is arranged above the prismatic bar type uniform distribution type catch or demister 7 when the single layer is arranged, a flushing nozzle 8 is arranged in the middle of the multilayer arrangement, a liquid inlet of the flushing nozzle 8 is communicated with a flushing pipe 10, the flushing nozzle 8 flushes the prismatic bar type uniform distribution type catch or demister 7 to keep the prismatic bar type uniform distribution type catch or demister 7 from being accumulated, and the flue gas entraining the droplets is partially removed by the prismatic bar type uniform distribution type catch or demister 7, and the flue gas is uniformly dispersed above the edge-bar-type uniform distribution type catcher or demister 7 so as to be beneficial to the convergence, sedimentation and separation of liquid drops; the liquid storage area at the bottom of the gas-liquid separator 6 is connected with the liquid inlet of the turbulent nozzle 4 through a circulating pipe 13 with a circulating pump 12, and the circulating pump 12 is generally arranged on the circulating pipe 13 in parallel; a liquid supplementing port communicated with the liquid supplementing pipe 11 is arranged on the upper side of a liquid storage area at the bottom of the gas-liquid separator 6 and is positioned on the lower side of the flue gas inlet; a side branch pipe 14 is arranged on the circulating pipe 13, the outlet end of the side branch pipe 14 is communicated with the raw material inlet of a concentrator 15 (such as a horizontal flow type settler, a conical settler, an inclined plate settler, an inclined pipe settler and the like), the online operation is carried out to densely concentrate dust and mud in the washing absorption liquid and discharge the dust and mud out of a washing absorption liquid circulating system, and the circulating liquid amount and the absorption power of the washing absorption liquid are kept by supplementing fresh liquid or absorbent; the overflow groove of the concentrator 15 is communicated with a clear liquid groove 17 through a clear liquid pipe 16; in addition, the clear liquid groove 17 is connected with the annular overflow weir 2 at the top end of the turbulent washing section 3 through a water curtain liquid supply pipe 19 with a clear liquid pump 18, and clear liquid in the annular overflow weir 2 descends on the vertical inner pipe wall of the turbulent washing section 3 to form a water curtain so as to protect the impact erosion of high-temperature flue gas. All the discharging, replenishing, adding and liquid-liquid control of the gas-liquid separator 6 are set to automatic or manual control.
Meanwhile, a tail exhaust gas analysis device 9 is arranged at a flue gas outlet at the top of the gas-liquid separator 6, the tail exhaust gas analysis device 9 is used for measuring the dust content and the target component content in the flue gas discharged by the gas-liquid separator 6, measuring the resistance drop of the flue gas, adjusting the liquid supply amount of the pump and adjusting the liquid supply component content so as to achieve the set purifying and washing or absorbing effect, and further improving the washing and purifying and absorbing effect. In addition, the flue gas discharge port at the top of the outer gas-liquid separator 6 can be connected with a wet electric dust collector through a flue gas discharge pipe for subsequent flue gas treatment, so that dust removal and ultra-clean discharge are realized.
When the process is implemented, the process contains high-concentration particles with complex physical properties and difficult to treat and SO which needs to be purified and absorbed2、HF、HCl、NOx、H2The flue gas of one or more target components in the S is vertically conveyed into the turbulent washing section 3 through a flue; the turbulent washing nozzle 4 positioned at the middle lower part of the turbulent washing section 3 sprays a washing absorption liquid column with the height of 5 m-7 m from bottom to top, the liquid column rises spirally and disperses into fine water drops to collide with flue gas with the flow velocity of 13 m/s-30 m/s from top to bottom at high speed to form a suspended foam gas-liquid mixed phase, and the gas-liquid two phases are in violent contact to finish the processes of adsorption absorption and adiabatic evaporation so as to capture dust and dissolve and absorb target components; the flue gas treated by the turbulent washing section 3 continuously enters the scaling spraying section 5 downwards, washing absorption liquid falling from the turbulent washing section 3 is fully subjected to transverse impact and longitudinal friction chopping with high-speed kinetic energy flue gas at the necking part of the scaling spraying section 5 to carry out flue gas scaling type spraying washing, the washing absorption liquid is broken into finer liquid drops again to form a gas-liquid high-mixing dispersion area, the gas-liquid mixture is rapidly diffused after passing through a throat pipe area to capture micron and submicron-level dust, and target components are further dissolved and absorbed; the flue gas treated by the convergent-divergent jet section 5 and the liquid drops carried by the flue gas continuously enter a gas-liquid separator 6 downwards, and after the flue gas passes through a prismatic rod type uniform distribution type liquid catcher or demister 7 to separate partial liquid drops, the content of dust particle matters is 0.05g/m3～0.35g/m3Is discharged from the top of the gas-liquid separator 6. Measuring the dust content and the target component content of the flue gas at the outlet of the gas-liquid separator 6, measuring the resistance drop of the flue gas, adjusting the liquid supply amount of the pump and the liquid supply component content, and automatically or manually controlling the liquid supply amount of the pump and the liquid supply component content to ensure that the content of the particles of the purified flue gas dust is 0.05g/m3～0.35g/m3So as to achieve the set purifying washing or absorbing effect. A wet electric dust remover can be additionally arranged in the subsequent flue gas treatment, so that the dust removal and ultra-clean emission are realized.
Example one
5000 tons/year of noble metal anode mud is treated by a certain Kaldo furnace, and the smoke gas volume is 7000-10000 m3The smoke contains 15g/m of powder containing lead oxide, selenium oxide, mirabilite and the like3～40g/m3The temperature of the inlet of the flue gas is 300-600 ℃, and SO in the flue gas2Content 31500mg/Nm3And small amounts of HF, HCl, NOx, H2Se and the like need purification and absorption treatment. The inner wall of the smoke tube is protected by a water curtain on an annular overflow weir 2, high-temperature smoke enters a turbulent washing section 3 through the annular overflow weir 2, washing absorption liquid sent by a circulating pump 12 is sprayed out through a large-opening turbulent nozzle 4, the smoke and the washing absorption liquid form a suspended dynamic foam area, the gas phase and the liquid phase are in violent contact to finish adsorption, absorption and adiabatic evaporation processes, a gas-liquid mixture moves downwards and enters a scaling and spraying section 5, the gas and the liquid are compressed and sprayed to be dispersed into a finer contact dispersion area, the gas-liquid mixture is rapidly diffused through a throat pipe area, the smoke and liquid drops carried by the smoke leave the scaling and spraying section 5 and enter a gas-liquid separator 6 for preliminary separation, and the gas and the liquid are further separated after the smoke passes through a prismatic-rod-type uniform distribution type liquid trap or demister 7; in order to ensure the cleanness of the arris rod type uniform distribution type catcher or demister 7, a washing spray head 8 is arranged to regularly wash the arris rod type uniform distribution type catcher or demister. The inner diameter of a flue gas pipeline of the turbulent washing section 3 is 600mm, the flow rate of flue gas is 25m/s, and the ejection quantity of the turbulent spray nozzles 4 is 105m3H; the inner diameter of the throat of the scaling injection section 5 is 375mm, the flue gas flow velocity at the throat is 40m/s, and the inner diameter of the gas-liquid separator 6 is 2500 mm.
A side branch pipe 14 (10 m) is arranged on a circulating pipe 13 for conveying washing absorption liquid3H) feeding liquid into a deep cone settling tank (phi 5000 multiplied by 8200), carrying out on-line operation, enabling solid sludge and dust to pass through an advection gravity settler, carrying out dense concentration on the sludge and dust in the washing absorption liquid in time, and discharging the sludge and dust out of a circulating liquid system; the circulating liquid amount and the absorption power of the washing absorption liquid are maintained by supplementing new water or sodium alkali.
Measuring the dust content and the target component content of the flue gas at the outlet of the gas-liquid separator 6, measuring the resistance drop of the flue gas, measuring the pH value of the washing absorption liquid to be approximately equal to 2-3, controlling the density rho of the washing absorption liquid to be approximately equal to 1.05-1.25, adjusting the liquid supply amount of the pump and adjusting the content of the liquid supply component so as to achieve the set purifying washing or absorption effect; the liquid supply amount of the pump and the liquid supply component content are adjusted to be automatically or manually controlled in an integrated way, so that the purified flue gas dust particlesThe content of the substance is less than or equal to 0.35g/m3. The subsequent flue gas treatment can be realized by additionally arranging a section of wet electric dust remover, a desulfurizing tower and an electric demister so that the dust in the finally discharged flue gas is less than or equal to 5mg/m3、SO2The content is less than or equal to 20mg/m3Acid mist is less than or equal to 5mg/m3And the ultra-clean emission of dust removal is realized.
Example two
The flue gas volume of a boiler and a multi-pipe dust remover discharged from a 40 ten thousand tons pyrite acid plant in a certain year is 115000m3H, 15g/m of dust containing iron oxide, silicon oxide, calcium oxide, aluminum oxide, magnesium oxide and the like3～20g/m3The temperature of the flue gas inlet is 300-360 ℃, and the temperature of the flue gas is SO 211 percent of the flue gas contains a small amount of HF, HCl and SO3 And the like, need purification and absorption treatment. The inner wall of the smoke tube is protected by a water curtain on an annular overflow weir 2, high-temperature smoke enters a turbulent washing section 3 through the annular overflow weir 2, washing absorption liquid sent by a circulating pump 12 is sprayed out through a large-opening turbulent nozzle 4, the smoke and the washing absorption liquid form a suspended dynamic foam area, the gas phase and the liquid phase are in violent contact to finish adsorption, absorption and adiabatic evaporation processes, a gas-liquid mixture moves downwards and enters a scaling and spraying section 5, the gas and the liquid are compressed and sprayed to be dispersed into a finer contact dispersion area, the gas-liquid mixture is rapidly diffused through a throat pipe area, the smoke and liquid drops carried by the smoke leave the scaling and spraying section 5 and enter a gas-liquid separator 6 for preliminary separation, and the gas and the liquid are further separated after the smoke passes through a prismatic-rod-type uniform distribution type liquid trap or demister 7; in order to ensure the cleanness of the arris rod type uniform distribution type catcher or demister 7, a washing spray head 8 is arranged to regularly wash the arris rod type uniform distribution type catcher or demister. The inner diameter of a flue gas pipeline of the turbulent washing section 3 is 1850mm, the flow rate of the flue gas is 25m/s, and the ejection quantity of the turbulent spray nozzles 4 is 1200m3H; the inner diameter of the throat of the scaling injection section 5 is 1400mm, and the flue gas flow velocity at the throat is 36 m/s.
The circulation pipe 13 for conveying the washing absorption liquid is provided with a side branch pipe 14 (60 m)3H) feeding liquid into a deep cone center transmission settling tank (phi 9000 multiplied by 10500), carrying out online operation, enabling solid mud and dust to pass through an advection gravity settler, carrying out dense concentration on the mud and dust in the washing absorption liquid in time, and discharging the mud and dust out of a circulating liquid system; maintaining the amount of circulating liquid and suction of washing absorbent by supplementing fresh water or sodium baseAnd (5) power is collected.
Measuring the dust content and the target component content of the flue gas at the outlet of the gas-liquid separator 6, measuring the resistance drop of the flue gas, measuring the sulfuric acid content of the washing absorption liquid to be 10-15%, controlling the density rho of the washing absorption liquid to be approximately equal to 1.05, and adjusting the liquid supply amount of the pump and the liquid supply component content to achieve the set purifying washing or absorption effect; the liquid supply amount of the pump and the content of the liquid supply components are adjusted to be automatically or manually controlled in an integrated way, so that the content of the particles of the purified flue gas dust is less than or equal to 0.10g/m3. The subsequent flue gas treatment can be realized by adding a section of cooling packed tower and a two-stage wet electric dust remover, so that the dust in the finally discharged flue gas is less than or equal to 2mg/m3F content is less than or equal to 0.5mg/m3、As≤1.0mg/m3Acid mist is less than or equal to 5mg/m3And the purification index is conveyed to the lower section.
The invention couples the vertical turbulent washing section and the convergent-divergent jet section into the turbulent jet washer to wash, purify and absorb the complex and difficult-to-treat flue gas and carry out gas-liquid separation, wherein the content of dust particles in the treated flue gas is 0.05g/m3～0.35g/m3Compared with the traditional flue gas multistage washing process, the power consumption of the energy-saving pump is more than 30%, the equipment investment is saved by more than 35%, the occupied land is saved by more than 40%, the dust removal washing efficiency is improved by more than 5-20%, and the subsequent flue gas treatment can be further treated by additionally arranging a wet electric dust remover to realize dust removal and ultra-clean emission; the process has the advantages of high flue gas purification strength, investment saving, high efficiency and obvious energy-saving effect, and is suitable for popularization and application.
The above embodiments are only for illustrating the technical idea of the present invention, and the protection scope of the present invention cannot be limited thereby, and any modification made on the basis of the technical scheme according to the technical idea proposed by the present invention falls within the protection scope of the present invention; the technology not related to the invention can be realized by the prior art.

Claims (12)

1. A turbulent impact injection coupling integrated flue gas purification process for complex and difficult-to-treat flue gas is characterized in that: the process comprises the following steps:
a. contains high-concentration particles with difficult-to-process physical propertiesGranular material and SO to be purified and absorbed2、HF、HCl、NOx、H2The flue gas of one or more target components in the S is vertically conveyed into a turbulent washing section through a flue;
b. the turbulent flushing nozzle positioned at the middle lower part of the turbulent flushing washing section sprays washing absorption liquid from bottom to top to collide with flue gas flowing rapidly from top to bottom at high speed so as to capture dust and dissolve and absorb target components;
c. the flue gas treated by the turbulent washing section continuously enters the scaling spraying section downwards, the washing absorption liquid under the turbulent washing section fully collides with the high-speed kinetic energy flue gas again at the necking part of the scaling spraying section to capture micron and submicron dust and further dissolve and absorb target components;
d. the flue gas treated by the convergent-divergent jet section and the liquid drops carried by the flue gas continuously enter the gas-liquid separator downwards to separate partial liquid drops, and then the flue gas is discharged from the top of the gas-liquid separator;
the turbulent flushing nozzle in the step (b) sprays a washing absorption liquid column with the height of 5 m-7 m from bottom to top, the liquid column rises spirally and disperses to form fine water drops which collide with flue gas with the flow rate of 13 m/s-30 m/s from top to bottom at high speed to form a suspended foam gas-liquid mixed phase, and dust collection and dissolution and absorption of target components are carried out; the liquid spraying amount of the turbulent spray nozzle in the step (b) is 1.5L/m3～7.0L/m3；
The zooming and spraying section in the step (c) is coaxially and vertically arranged below the turbulent washing section, the inner cavity of the zooming and spraying section is subjected to necking treatment, the inlet angle and the outlet angle of the zooming and spraying section are respectively 20-30 degrees and 7-15 degrees, the flow rate of flue gas at the throat is 25-50 m/s, washing absorption liquid under the zooming and spraying section is fully subjected to transverse impact and longitudinal friction chopping with high-speed kinetic energy flue gas at the necking part of the zooming and spraying section to carry out scaled spraying and washing of the flue gas, the washing absorption liquid is broken into finer liquid drops again to form a gas-liquid highly-mixed dispersion region, micron and submicron-level dust is captured, and target components are further dissolved and absorbed;
the vertically arranged tubular torrent washing section and the tubular convergent-divergent jet section are coupled into a tubular torrent jet washer;
the high-concentration difficult-to-process particles with complicated physical properties in the step (a) mean that the dust content is 0.5g/m3～50g/m3And dust having a particle diameter of 0.01 to 3.0 μm.
2. The turbulent injection coupling integrated flue gas purification process of complex and difficult-to-treat flue gas as claimed in claim 1, wherein: the turbulent spray heads in the step (b) are large open-hole spray heads made of corrosion-resistant alloy steel or engineering plastics F4/F46/HPE/FRP/SiC, and the number of the turbulent spray heads is 1-6.
3. The turbulent injection coupling integrated flue gas purification process of complex and difficult-to-treat flue gas as claimed in claim 1, wherein: and (d) arranging a prismatic bar type uniform distribution type liquid catcher or demister in the gas-liquid separator in the step (d), wherein the prismatic bar type uniform distribution type liquid catcher or demister is arranged at a position 1.2-6.0 m above a flue gas inlet of the gas-liquid separator, the flow velocity of flue gas reaching the prismatic bar type uniform distribution type liquid catcher or demister is 0.8-3.5 m/s, part of liquid drops of the flue gas carrying the liquid drops are removed by the prismatic bar type uniform distribution type liquid catcher or demister, and the flue gas is uniformly dispersed above the prismatic bar type uniform distribution type liquid catcher or demister so as to be beneficial to convergence, sedimentation and separation of the liquid drops.
4. The turbulent injection coupling integrated flue gas purification process of complex and difficult-to-treat flue gas as claimed in claim 3, wherein: the prismatic rod type uniform distribution type liquid catcher or the demister in the step (d) is arranged in a single layer or multiple layers, a flushing spray head is arranged above the prismatic rod type uniform distribution type liquid catcher or the demister in the single layer, the flushing spray head is arranged in the middle of the prismatic rod type uniform distribution type liquid catcher or the demister in the multiple layer arrangement, and a liquid inlet of the flushing spray head is communicated with the flushing pipe.
5. The turbulent injection coupling integrated flue gas purification process of complex and difficult-to-treat flue gas as claimed in claim 1 or 4, wherein: and (d) connecting the bottom liquid storage area of the gas-liquid separator in the step (d) with the liquid inlet of the turbulent nozzle through a circulating pipe with a circulating pump.
6. The turbulent injection coupling integrated flue gas purification process of complex and difficult-to-treat flue gas as claimed in claim 5, wherein: and a liquid supplementing port communicated with the liquid supplementing pipe is arranged on the upper side of the liquid storage area at the bottom of the gas-liquid separator, and the liquid supplementing port is positioned on the lower side of the flue gas inlet.
7. The turbulent injection coupling integrated flue gas purification process of complex and difficult-to-treat flue gas as claimed in claim 5, wherein: the circulating pumps are arranged on the circulating pipe in parallel.
8. The turbulent injection coupling integrated flue gas purification process of complex and difficult-to-treat flue gas as claimed in claim 5, wherein: the circulating pipe is provided with a side branch pipe, the outlet end of the side branch pipe is communicated with the raw material inlet of the concentrator, and the side branch pipe runs on line to densely concentrate dust and mud in the washing absorption liquid and discharge the dust and mud out of the washing absorption liquid circulating system; the overflow groove of the concentrator is communicated with the clear liquid groove through a clear liquid pipe.
9. The turbulent injection coupling integrated flue gas purification process of complex and difficult-to-treat flue gas as claimed in claim 8, wherein: the clear liquid groove is connected with an annular overflow weir at the top end of the turbulent washing section through a water curtain liquid supply pipe with a clear liquid pump, and clear liquid in the annular overflow weir descends on the vertical inner pipe wall of the turbulent washing section to form a water curtain so as to protect the impact erosion of high-temperature flue gas.
10. The turbulent injection coupling integrated flue gas purification process of complex and difficult-to-treat flue gas as claimed in claim 1, wherein: the content of dust particles in the flue gas discharged from the top of the gas-liquid separator in the step (d) is 0.05g/m3～0.35g/m3And a tail exhaust gas analysis device is arranged at the flue gas outlet at the top of the gas-liquid separator.
11. The turbulent injection coupling integrated flue gas purification process of complex and difficult-to-treat flue gas as claimed in claim 1, wherein: and (d) connecting a flue gas discharge port at the top of the gas-liquid separator in the step (d) with a wet electric dust collector through a flue gas discharge pipe for subsequent flue gas treatment, and realizing dust removal and ultra-clean discharge.
12. The turbulent injection coupling integrated flue gas purification process of complex and difficult-to-treat flue gas as claimed in claim 1, wherein: the turbulent washing section and the zooming injection section are of an upper-lower integrated coupling structure, the bottom of the zooming injection section is connected with the gas-liquid separator, and the turbulent washing section is made of corrosion-resistant alloy steel, metal lining ceramic tiles, graphite bricks, or high-temperature resistant engineering plastics FRP/PP/PE/CPVC/PVD/PTFE or engineering plastics; the zooming injection section is made of corrosion-resistant alloy steel, lead-antimony alloy or engineering plastic FRP/F4/F46/HPE/CPVC/SiC or a compound of engineering plastic.
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