CN113209767B - Physical separation adsorption gas-liquid-solid separation device and method - Google Patents
Physical separation adsorption gas-liquid-solid separation device and method Download PDFInfo
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- CN113209767B CN113209767B CN202110590703.4A CN202110590703A CN113209767B CN 113209767 B CN113209767 B CN 113209767B CN 202110590703 A CN202110590703 A CN 202110590703A CN 113209767 B CN113209767 B CN 113209767B
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- 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
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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
- B01D53/0407—Constructional details of adsorbing systems
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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
- B01D53/14—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
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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
- B01D53/14—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
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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
- B01D53/14—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
- B01D53/1487—Removing organic compounds
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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
- B01D53/14—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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/102—Carbon
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- 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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Abstract
The invention relates to a physical separation adsorption gas-liquid-solid separation device and a method thereof, wherein a multi-layer trapping beam interception is arranged on a circulating device through which flue gas passes, and adsorption or bonding trapping is carried out by selecting a material with small surface tension with a trapped substance. The flue gas is all produced the turbulent flow after being intercepted by every layer of entrapment bundle, and when the trapper was the fog drop, the mutual striking combined is grown up, gets into next level interception and catches and easily is caught, and the flue gas is because producing the turbulent flow, increases the probability that takes place the collision with the rear portion entrapment bundle, is more easily caught. The device and the method avoid the problem of system resistance increase caused by easy blockage and scaling of filtration and separation, have small system resistance and stable operation, and do not need external power. The trapping beam materials are longitudinally arranged, when the trapping object is in a liquid state, the trapping beam materials are self-cleaned by gravity, when the trapping object is in a solid state, the self-flowing viscous substance is coated on the trapping beam, the distance between the trapping beam materials is larger, and when the trapping object amount is not very large, the system resistance is not increased greatly, and the trapping beam materials can be cleaned periodically.
Description
Technical Field
The invention belongs to the technical field of industrial environmental protection, and particularly relates to a physical barrier adsorption gas-liquid-solid separation device and a physical barrier adsorption gas-liquid-solid separation method.
Background
In industrial and agricultural production and life, separation of gas-liquid, gas-solid two-state substances, or separation of gas-liquid-solid three-state substances is often involved. Typical separation methods are: gravity separation, cyclone separation, filtration separation, and electrostatic capture separation. The equipment for realizing the gravity separation method comprises a gravity dust remover, a gravity gas-liquid separator and the like; the equipment for realizing the cyclone separation method comprises a cyclone dust collector, a cyclone gas-liquid separator, a tube bundle demister for environmental protection flue gas treatment and the like; the equipment for realizing the filtration separation method comprises a cloth bag dust remover, a ceramic tube dust remover, a metal net dust remover and the like; the electrostatic separation method includes electrostatic precipitator, wet electric demister, etc. Gas-liquid-solid separators are process equipment commonly used in the field of industrial manufacturing. Especially in petrochemical and environmental protection industries, the method is widely applied in the field of environmental protection smoke treatment in recent years. The gas-liquid-solid separator is mainly divided into: gravity separators, cyclone separators, filter separators, and electrostatic mist eliminators. Wherein, gravity separator: the separation is realized by utilizing the difference of the densities of gas, liquid and solid, namely the difference of gravity; cyclone separator: the separation is realized by utilizing the different centrifugal forces applied to the rotation of gas, liquid and solid; filtration separator: separation is achieved by means of a filter element or medium on the air flow channel; the electrostatic precipitator, wet electric defroster work principle is that particulate matters or fog drops to be captured in flue gas are polarized electrically and then captured and separated by polar plates.
The environment-friendly wet desulfurization flue gas is a gas-liquid-solid tri-state mixture, and the flue gas contains nitrogen, oxygen, carbon dioxide, carbon monoxide, SO2, NOx, hg2 and other gases, and also contains escaped desulfurization liquid fog drops, wherein various dissolved substances, desulfurization products newly generated by desulfurization, fine desulfurizing agents and smoke dust are contained in the fog drops. Because the flue gas is in a supersaturated state, the flue gas can be changed into a suspension state of dust in water or mixed with desulfurization liquid, and partial hydrophobic substances can be dissociated outside fog drops, such as dioxin particles, carbon black particles and phenol drops. The smoke carries mist drops containing dissolved matters and suspended matters as main sources of PM2.5 precursors, hydrophobic matters are fine particulate matters of PM2.5 grade, and the theory is now common knowledge, so that defogging and deep dedusting are the main means for haze treatment in the future. Because these particles and droplets are very fine in size, it is difficult for current defogging and dust removal means to capture these fine particles and droplets.
The chemical industry field has many processes and needs gas-liquid separation, and firstly, the recovery product, secondly, the reduction of pollutant carried by discharged gas, and the high-efficiency low-cost gas-liquid separation technology and equipment are also urgently needed in the chemical industry field. In addition, cracking fractionation in the petrochemical industry is also highly desirable for efficient and low cost separation techniques and equipment. Firstly, the product quality can be improved, secondly, the production efficiency is improved, and meanwhile, the equipment investment is reduced. The existing gas-liquid separation technology has low capturing efficiency on fine mist drops, severely restricts the improvement of production efficiency, also influences product quality and product recovery rate, generally exceeds standard for directly discharged gas aerosol discharge, restricts the improvement of discharge standard, and causes pressure on atmosphere treatment.
The environmental protection industry typically calls for demisting the gas-liquid separation process. There are many methods of demisting, including wet electric demisting, spray demisting, rotary active mechanical demisting, baffle mist device, tube bundle demister, etc. Wet electric mist eliminators are difficult to capture for fine particle size mist droplets, which are just precursors to PM 2.5; spray mist removal is less in investment and high in efficiency, but the concentration of dissolved matters in spray water needs to be controlled frequently, otherwise mist drops generated by spray escape can generate PM2.5 precursors, the water is unconsumed by wet desulfurization, waste water is treated, a mist eliminator is arranged at the rear part, and otherwise, mist drops can escape in spray. The investment of the rotary type active mechanical defogging equipment is relatively large, the stability is also problematic, the equipment maintenance amount is relatively large, and the energy consumption is relatively high. The existing baffle plate type and tube bundle type static mechanical defogging are influenced by air quantity change, the operation air quantity change and equipment scaling have great influence on defogging efficiency, the capturing efficiency of fine fog drops is low, and the maintenance and replacement are required to be stopped. The existing gas-liquid separation equipment in the chemical industry is also the gas-liquid separation equipment in the previous description, and the existing gas-liquid separation equipment has low separation efficiency, fine mist drops escape, influence the product quality and the product yield, or the exhaust gas discharged aerosol exceeds the standard.
Disclosure of Invention
The invention provides a physical separation adsorption gas-liquid-solid separation device and a method thereof, aiming at the technical problems. The flue gas can generate turbulent flow after being intercepted by each layer of trapping beams, and when the trapping objects are fog drops, the fog drops can mutually collide and grow up, and the flue gas can be easily trapped when entering the next stage of intercepting and trapping. The probability of collision with the rear trapping beam is also increased due to turbulence generated by the flue gas, and the flue gas is more easily trapped.
The separation method and the separation device of the invention avoid the problem of system resistance increase caused by easy blockage and scaling of filtration separation, have small system resistance and stable operation, and do not need external power. The trapping beams are longitudinally arranged, when the trapping objects are in a liquid state, the trapping beams can be cleaned by gravity, when the trapping objects are in a solid state, viscous substances capable of flowing automatically can be coated on the trapping beams, and because the distance between the trapping beam materials is relatively large, when the trapping objects are not very large, the system does not have too large resistance to increase, so that the trapping beams can be cleaned periodically.
The method is pure physical separation, adsorption, capture and separation. The device is simple, convenient to install, low in investment, stable in operation, low in running resistance and low in energy consumption. Can catch any particle size substance, and has high separation efficiency. By selecting different materials, various liquid and solid substances can be captured and separated.
When environmental protection flue gas is administered defogging, device accessible physical separation adsorbs and catches fog droplet and particulate matter, can high-efficient capture tiny fog droplet, can further remove dust simultaneously, and the surfactant is added or spouts surfactant before the defogging in addition in the desulfurizing liquid, can also catch the organic matter of dioxin class high gasification point. Some flue gas contains organic matters mixed by liquid and solid, and can be simultaneously bonded and adsorbed to capture solid particles when capturing liquid organic matters. Thus, organic solid particulate matter can be captured without the need for a viscous material spray treatment of the trapping beams.
The specific technical scheme is as follows:
a physical barrier adsorption gas-liquid-solid separation device, the device comprising: the device comprises a shell 1, a flue gas inlet 2, a pressure equalizing plate 3, a trapping chamber 4, an upper cover plate 5, a flue gas outlet 6, a main guide groove 7, an outgoing section guide groove 8, an outgoing section guide groove 9, an outgoing section isostatic pressure chamber 10, an outgoing section isostatic pressure chamber 11, an outgoing section isostatic pressure chamber valve plate 12, an outgoing section isostatic pressure chamber valve plate 13, a liquid collecting groove 14, a liquid outlet 15 and a trapping beam 16;
the front end of the shell 1 is provided with a flue gas inlet 2, a trapping chamber 4 is arranged in the shell, the tail end of the shell 1 is provided with a flue gas outlet 6, the bottom of the shell 1 is provided with a liquid collecting tank 14 and a liquid outlet 15, the upper part of the shell 1 is provided with an upper cover plate 5, the trapping chamber 4 consists of a plurality of groups of trapping beams 16, a leading groove 7, a moving-out section guide groove 8 and a moving-in section guide groove 9, the trapping beams 16 are fixed and directionally moved through the leading groove 7, the moving-out section guide groove 8 and the moving-in section guide groove 9, and a pressure equalizing plate 3 is arranged between the flue gas inlet 2 and the trapping chamber 4 for equalizing gas distribution;
the trapping chamber 4 is internally fixed and moved by trapping beams 16 which are vertically distributed and provided with main guide grooves 7 which are arranged at four corners, a limiting protruding strip is arranged on the trapping beam 16 frame, or a spacing clamping ring is additionally arranged, and the spacing between the trapping beams 16 is adjusted by adjusting the height of the protruding strip or the thickness of the spacing clamping ring; a pushing device or a guide chain pulling device is arranged on the main guide groove 7, so that the trapping beam 16 can freely slide in the main guide groove 7;
the front end of the leading groove 7 is connected with a moving-out section guide groove 8, the moving-out section guide groove 8 moves outwards, and the trapping beam 16 moves out of the shell 1 for offline maintenance and cleaning; the tail end of the main guide groove 7 is connected with a moving-in section guide groove 9 for supplementing a new trapping beam 16; the moving-out section guide groove 8 is provided with a moving-out section isostatic pressing chamber 10, the moving-in section guide groove 9 is provided with a moving-in section isostatic pressing chamber 11, and smoke leakage or wild wind is avoided when moving out or moving in the collecting beam 16; the moving-in section isostatic pressure chamber is blocked and isolated from the shell 1 through a moving-out section isostatic pressure chamber closed valve plate 12, and the moving-out section isostatic pressure chamber 11 is blocked and isolated from the shell 1 through a moving-in section isostatic pressure chamber closed valve plate 13, so that system smoke leakage or wild wind is avoided when the trapping beam 16 is replaced;
the trapping beams 16 are formed of a square set longitudinal wire material. The silk thread material is a material which has good wettability with the trapped liquid and is not corroded, and the strength of the silk thread material is required to meet the process requirements. The wire diameter is greater than the droplet diameter; the distance between the wires is 3 times larger than the diameter of the maximum intercepted fog drop and the solid particle.
The trapping beams 16 are obliquely arranged in the trapping chamber 4, the number of the trapping beam grids is a plurality of the trapping beams, the distance between the trapping beam grids is larger than 3 times of the diameter of the largest liquid drop and particle, and a certain included angle is formed between the trapping beam grids and the horizontal plane, and the included angle is 30-150 degrees, so that the trapping materials can be adsorbed and flow downwards along the silk threads on the trapping beams 16.
The collecting beam 16 is arranged in a vertical horizontal plane.
The physical separation adsorption gas-liquid-solid separation method adopts the physical separation adsorption gas-liquid-solid separation device, and comprises the following steps:
step 1: the method comprises the steps that a physical separation adsorption gas-liquid-solid separation device is connected with a flue gas pipeline, flue gas enters a trapping chamber 4 through a flue gas inlet 2, and trapped liquid drops and particulate matters in the flue gas are adsorbed or cohesively trapped by a trapping beam 16 arranged in the chamber; the smoke will generate turbulence after being intercepted by the capturing bundles 16 of each layer, the liquid drops will mutually collide and grow up, the smoke is captured again when entering the capturing bundles 16 of the next stage, and the probability of collision between the captured substance and the rear capturing bundles 16 is increased due to the generated turbulence, so that the smoke is captured more easily; if the wettability of solid particles in the flue gas and captured liquid drops is good, the solid particles can be adhered and captured on the capturing beam 16 and flow into the liquid collecting tank along with the adsorption liquid or the adhesion liquid;
step 2: the captured droplets and particulate matter flow vertically downward into the liquid collection tank 14 and are discharged through the liquid discharge port 15;
step 3: when the bundle 16 has a large amount of adhered matter, the bundle 16 is replaced.
In the step 3, the replacement of the capturing bundle 16 adopts a split-flow switching mode, the capturing bundle 16 is led out through the moving-out section guide groove 8, the capturing bundle 16 is taken out for offline maintenance and cleaning, and meanwhile, a new capturing bundle 16 or the capturing bundle 16 after cleaning is led in through the moving-in section guide groove 9, and the insufficient capturing bundle 16 in the capturing chamber is supplemented.
In the step 3, the replacement of the trapping bundle 16 adopts a cover-removing mode, and the upper cover plate 5 of the trapping chamber is removed and the replacement of the trapping bundle 16 is performed during discontinuous production.
The invention relates to a physical separation adsorption gas-liquid-solid separation method and an adsorption separation principle of the device thereof, wherein the adsorption separation principle comprises the following steps:
the invention selects special material trapping beams, and a plurality of groups of special material trapping beams are arranged in a trapping chamber, so that turbulent flow impact is generated when smoke passes through the trapping beams, liquid drops and particulate matters in the smoke are adsorbed and trapped when the smoke is impacted with the special material trapping beams, and the adsorbed liquid-solid mixture flows into a liquid collecting tank at the bottom of the equipment under the action of gravity when the liquid-solid mixture is gathered to a certain amount, and is discharged, recovered and recycled. The droplets and the particles entrained in the flue gas can generate impact turbulence when passing through each layer of the collecting beam, the droplets can be mutually impacted and grow up, and the droplets can be adsorbed and polymerized with the particles. The density of fog drops or particles is far greater than that of gas, when the air flow collides with the trapping beam silk thread, the kinetic energy of the liquid drops or particles is large, the inertia is large, when the air flow collides with the trapping beam, the liquid drops or particles break through the air film to collide with the trapping beam silk thread, and as the material is a special material, the surface of the adsorbing material has small surface tension with the adsorbed substance, and when the adsorbed substance collides with the trapping beam silk thread, the adsorbed substance is adsorbed and trapped by the surface of the trapping beam silk thread.
The flue gas flow is a very thin layer when contacting with the trapping beam silk threads, and can only be partially intercepted and captured each time, so that the flue gas flow is easy to intercept and capture with large particle size and easy to escape with small particle size, and therefore, the trapping beam silk threads need to be captured for multiple times by adjusting the trapping beam structure form. The larger the particle diameter is, the larger the kinetic energy of the liquid drop or particle is, when the airflow is blocked to change the flow direction, the liquid drop or particle can break through the air film due to inertia and collide with the interception trapping beam wire, so that the liquid drop or particle is intercepted and trapped. The larger the diameter the more capable the droplet or particulate will break through the gas film, the more readily it will be adsorbed. Conversely, the smaller the liquid drop and the particulate matters are, the smaller the kinetic energy is, and the worse the capability of breaking through the air film is, the less easily the liquid drop and the particulate matters are absorbed and captured; the trapping harness wire has adsorption force on the adsorbed substances, the adsorbed substances have desorption escape force due to inertia, and the larger the flue gas flow velocity is, the larger the inertia of the adsorbed substances is, and the larger the desorption escape force is. The adsorption force of the trapping harness cord to the adsorbed substance is also related to the adsorption area of the adsorbent and the particle diameter of the adsorbed substance. The larger the diameter of the adsorption material, the larger the adsorption area and the stronger the adsorption capacity. However, the larger the diameter of the adsorbent material, the smaller the specific adsorption surface area in a certain space, and the larger the size of the apparatus. The larger the particle diameter of the adsorbed substance, the larger the desorption escape force, and in order to effectively capture the adsorbed substance, the diameter of the adsorption material needs to be increased, and the flow rate of the flue gas needs to be reduced. Otherwise, new liquid drops and particulate matters can be formed to escape, and the capturing and separating efficiency is reduced.
The flow rate of the flue gas is high, the system resistance is high, and the energy consumption is high. After passing through the collecting beam, the gas flow forms turbulence and is in unordered collision with the rear turbulent device collecting beam wires and is intercepted again, and the more the interception times are, the higher the demisting efficiency is.
The greater the thread density of the trapping bundle, the greater the probability of liquid droplets and particulate matter being trapped by interception. The quotient of the sum of the interception and capturing efficiency and the surface area of the interception and capturing beam wire divided by the airflow cross-sectional area between interception and capturing beams is called an interception specific surface area, and the adsorption efficiency is positively correlated with the interception specific surface area and positively correlated with the interception times. The finer the trapping strands, the greater the number of trapping strands arranged in a space, the greater the sum of the trapping strand surface areas, the greater the chances of the trapped material striking the trapping strands, with the device of the invention having a constant geometry and a constant device resistance. However, when the trapping harness wire is too thin, the trapping harness wire cannot adsorb the liquid drops and the particulate matters due to insufficient adsorption area and small adsorption force when capturing the large liquid drops, and even the large liquid drops are cut into small liquid drops to escape. It is therefore required that the diameter of the trapping wires is greater than the maximum intercepting droplet diameter.
The actual wind velocity through the separator depends on the adsorbed species particle size, the interception adsorption material diameter, and the adsorption force between the adsorbed species and the interception adsorption material. When specific working conditions and selective adsorption materials are involved, related small tests are needed to be carried out, or the surface tension of related materials is checked to calculate and obtain, and the proper flue gas flow rate, the trapping yarn material, the yarn diameter and the trapping chamber size are determined.
In summary, the method of vertical interception of the silk thread is used for adsorbing and intercepting, and the intercepted liquid substance flows down along the silk thread. The mode avoids the blocking of the airflow channel by the intercepted liquid and solid, has small smoke resistance and can not generate liquid drops secondarily.
Compared with the prior art, the physical separation adsorption gas-liquid-solid separation method and the device thereof have the beneficial effects that:
1. in the wet desulfurization process, the flue gas from the desulfurization tower is saturated flue gas, certain temperature reduction is carried out in the transmission process, supersaturated water is separated out, new fog drops are produced by the separated water, and the surface energy is relatively large, so that the needed generation is attached to the original fog drops or dust surfacesThe surface energy is very small, so that the precipitated water is mostly attached to the surface of the original fog drops or dust. At the moment, the surface of hydrophilic dust in the flue gas is basically wrapped by water, and the hydrophilic dust is captured when meeting the capturing beam, so that the purposes of demisting and dedusting are achieved. The flue gas to be treated contains SO 2 、SO 3 Or other acid gases, when the flue gas collides with the trapping beam, water adsorbed on the surface of the trapping beam can react with various acid gases to further remove the acid gases. The mist droplets actually captured contain part of sulfurous acid or bisulphite, and part of SO2 is released after the mist droplets escape to the atmosphere, SO that the mist droplets are captured and are equivalent to further desulfurization, and therefore, the device has the function of further removing acid gas.
2. The dust in the wet desulfurization flue gas is in a state that most of the dust is already wetted or in a dust-in-water state except that part of organic matters or carbon black particles are not wetted with water. At the same time as demisting, the dust is also captured. Therefore, the device is a good wet flue gas dust removal device. The device and the method are also suitable for dedusting the low-temperature high-humidity flue gas.
3. Various dissolved compounds exist in the desulfurizing liquid fog drops carried by the flue gas, and meanwhile, ultrafine particles of a desulfurizing product newly generated by a desulfurizing reaction are also generated. These particles escape to the atmosphere to produce fine particles having various particle diameters such as PM10, PM2.5, and PM 1.0. They are an important source of supply that leads to the occurrence of haze particles, so defogging is the most effective haze treatment.
4. The flue gas has high melting point or high gasification point organic matters, such as dioxin particles or phenol liquid drops, a proper amount of special surfactant is added into the desulfurization liquid, or the mixture is uniformly sprayed for reaction before defogging, at the rear defogging temperature, the substances are solid or liquid and exist in the form of small particles or small fog drops, the surface tension of the organic matters and water-based substances can be reduced after the surfactant is added into the desulfurization liquid, the organic matters and the water-based substances can be partially adsorbed and captured in a defogging link, and carbon black substances can be adsorbed and captured.
5. When the liquid and solid organic matter smoke is treated independently, the liquid and solid organic matter can be captured only by changing the material for capturing the beam or carrying out surface modification treatment on the adsorption material, and the grease material has very good adsorption and dissolution effects on dioxin and benzopyrene. And a plurality of organic matters with different melting points are associated in some smoke, so long as the smoke contains low-melting-point organic matters, other high-melting-point solid organic matters can be captured simultaneously. Many low-melting-point organic matters are accompanied in many flue gases containing dioxin and benzopyrene, and when the low-melting-point organic matters are trapped when the equipment is adopted for treatment, the dioxin and the benzopyrene can be cooperatively trapped. Therefore, the device is the simplest and effective device for treating dioxin and benzopyrene. The gas-liquid separation device with low cost is very effective in the petrochemical industry, and can improve the production efficiency of the devices and the product quality. Similarly, the solid or liquid heavy metal substances can be captured and removed.
6. The device is also a previous procedure for removing the oil fume, and the active carbon adsorption material is used for adsorbing the gaseous organic matters after the liquid and solid organic matters in the oil fume are removed. The apparatus and method can thus also be used for removing oil smoke.
7. The device is a very effective gas-liquid-solid separation device in the fields of environmental protection, chemical evaporation drying and concentration.
8. The device is of a modular structure, can realize unpowered defogging, dedusting and desulfurizing, effectively combines the internal fluid characteristics of the defogging reactor by utilizing the inertia and gravity properties of air flow, realizes the efficient interception function by the internal combined turbulence device, does not generate more energy consumption and does not generate secondary pollutants.
9. When the front end trapping beam is scaled, the smoke resistance can be increased, and then the front end trapping beam can be started to move out of the guide groove, and the front end scaling trapping beam side can be moved out for offline maintenance. The moving-out guide groove is used for sending out the to-be-maintained collecting beam and then returning to the flue, then a pushing device or a traction chain arranged at the tail end of the device pushes the turbulence device forwards, so that the front collecting beam enters the moving-out guide groove, then the moving-in guide groove is used for feeding the new collecting beam into the device, and the supplementing blank section is used for supplementing the dust, and most of the dust is adhered to the front collecting beam, so that the supplementing moving-in guide groove is arranged behind the moving-out guide groove. The length of the moving-out section guide slot is the same as that of the moving-in section guide slot. The device can realize online replacement of the collecting beam without stopping production and maintenance.
In conclusion, the device has the advantages of low investment and low running cost; the operation is stable, and the maintenance is simple; the separation efficiency is high; the multifunctional wet desulfurizing fume treating process includes simultaneous desalting, dedusting, desulfurizing, dioxin eliminating and charcoal eliminating.
Drawings
FIG. 1 is a front view of a physical barrier adsorption gas-liquid-solid separation apparatus according to an embodiment of the present invention;
FIG. 2 is a top view of a physical separation adsorption gas-liquid-solid separation device according to an embodiment of the present invention;
FIG. 3 is a left side view of FIG. 2 of a physical barrier adsorption gas-liquid-solid separation apparatus according to an embodiment of the present invention;
FIG. 4 is a schematic view of a trapping beam structure of a physical separation adsorption gas-liquid-solid separation device according to an embodiment of the present invention;
in the figure: 1-shell, 2-flue gas inlet, 3-equalizing plate, 4-collecting chamber, 5-upper cover plate, 6-flue gas outlet, 7-main guide groove, 8-out section guide groove, 9-in section guide groove, 10-out section isostatic pressing chamber, 11-in section isostatic pressing chamber, 12-out section isostatic pressing chamber valve plate, 13-in section isostatic pressing chamber valve plate, 14-collecting tank, 15-liquid outlet and 16-collecting beam.
Detailed Description
The invention will be further described with reference to specific embodiments and figures 1-4, but the invention is not limited to these embodiments.
Example 1
The smoke inlet in the embodiment is SO in the smoke after wet desulphurization 2 Concentration is 60mg/m 3 ，SO 3 Concentration is 2mg/m 3 NOx concentration 48mg/m 3 Dust 18mg/m 3 The free water content is 150mg/m 3 The method comprises the steps of carrying out a first treatment on the surface of the The flue gas temperature is 52 ℃ and the flue gas flow is 18 ten thousand m 3 /h。
A physical separation adsorption gas-liquid-solid separation device, the front view is shown in fig. 1, the top view is shown in fig. 2, the left view of A-A section is shown in fig. 3, the schematic view of a trapping beam structure is shown in fig. 4, and the device comprises: 1-shell, 2-flue gas inlet, 3-equalizing plate, 4-collecting chamber, 5-upper cover plate, 6-flue gas outlet, 7-main guide groove, 8-out section guide groove, 9-in section guide groove, 10-out section isostatic pressing chamber, 11-in section isostatic pressing chamber, 12-out section isostatic pressing chamber valve plate, 13-in section isostatic pressing chamber valve plate, 14-collecting tank, 15-liquid outlet and 16-collecting beam.
The front end of the shell 1 is provided with a smoke inlet 2, smoke enters through an air inlet, uniformly presses and distributes flows through a pressure equalizing plate 3, enters a trapping chamber 4 for adsorption trapping, and is discharged through a smoke outlet 6 arranged at the tail end of the shell 1 after adsorption trapping;
the bottom of the shell 1 is provided with a liquid collecting tank 14 and a liquid outlet 15; an upper cover plate 5 is arranged at the upper part of the shell 1; a trapping chamber is arranged inside the shell 1; the catching bundle 16 is fixed or moved through the main guide groove 7, the moving-out section guide groove 8 and the moving-in section guide groove 9;
the trapping chamber is composed of a trapping bundle 16, a leading groove 7, a moving-out section guide groove 8 and a moving-in section guide groove 9, wherein the trapping bundle 16 is vertically arranged on the ground. Limiting protruding strips are arranged on the frames of the trapping beams 16, or interval clamping rings are additionally arranged on the frames of the trapping beams, and the spacing between the trapping beams 16 is adjusted by adjusting the height of the protruding strips or the thickness of the interval clamping rings; the said guide channels 7, 8, 9 are provided with pushing or pulling means in which the trapping beams 16 move forward;
the front end of the leading groove 7 is connected with a moving-out section guide groove 8, the moving-out section guide groove 8 moves outwards, and the trapping beam 16 moves out of the shell 1 for offline maintenance and cleaning; the tail end of the main guide groove 7 is connected with a moving-in section guide groove 9 for supplementing a new trapping beam 16; the moving-out section guide groove 8 is provided with a moving-out section isostatic pressing chamber 10, the moving-in section guide groove 9 is provided with a moving-in section isostatic pressing chamber 11, and smoke leakage or wild wind is avoided when moving out or moving in the collecting beam 16; the moving-in section isostatic pressure chamber 10 is blocked and isolated from the shell 1 through a moving-out section isostatic pressure chamber valve plate 12, and the moving-out section isostatic pressure chamber 11 is blocked and isolated from the shell 1 through a supplementary section isostatic pressure chamber valve plate 13, so that system smoke leakage or air inlet is avoided when the trapping beam 16 is replaced;
the collector bundle 16 is composed of a frame and longitudinal wires fixed thereon. The material, diameter and distance between the silk threads are specifically designed according to the characteristics of the treated smoke and the site space;
the trapping beam 16 wires need to be perpendicular to the ground, so that the adsorption trapping substances can flow downwards along the trapping beam 16 wires.
The physical separation adsorption gas-liquid-solid separation method adopts the physical separation adsorption gas-liquid-solid separation device, and comprises the following steps:
(1) The physical separation adsorption gas-liquid-solid separation device is connected with a flue gas pipeline, and flue gas enters a trapping chamber 4 through a flue gas inlet 2 and uniform pressure gas distribution through a uniform pressure plate 3 for adsorption or bonding trapping; the smoke will generate turbulence after being intercepted by the capturing bundles 16 of each layer, the liquid drops will mutually collide and grow up, the smoke is captured when entering the capturing bundles 16 of the next stage, the probability of collision with the rear capturing bundles 16 is increased due to the generated turbulence, and the smoke is more easily captured; the solid particles adhere to and flow themselves on the trapping beam 16;
(2) The captured droplets and particles flow vertically downward into the liquid sump 14 and are discharged through the liquid discharge port 15;
(3) When the adhered objects of the trapping beam 16 are more, the trapping beam 16 is led out through the moving-out section guide groove 8, the taken trapping beam 16 is subjected to offline maintenance and cleaning, and meanwhile, a new trapping beam 16 or the cleaned trapping beam 16 is led in through the moving-in section guide groove 9 to supplement the insufficient trapping beam 16 in the trapping chamber.
In this embodiment, the desulfurized flue gas is introduced into a physical barrier adsorption gas-liquid-solid separation device through a pipeline, and the device is shown in fig. 1-4. The internal cross-sectional area of the device is designed to be 17 square meters and 12 meters long. After passing through the device, the flue gas is in: SO (SO) 2 Is at a concentration of 42mg/m 3 The removal rate is 30%; SO (SO) 3 Is 0.8mg/m 3 The removal rate is 60%; NOx concentration 48mg/m 3 Almost no removal; dust 5mg/m 3 The removal rate is 72%; free water content 15mg/m 3 The removal rate is 90%; the flue gas temperature was 51 ℃. The smoke is obviously not tailing after demisting.
Example 2
The smoke inlet of the embodiment is that,SO in desulphurized flue gas 2 Is 45mg/m 3 ，SO 3 Is 3mg/m 3 ，NO X Is 45mg/m 3 11mg/m of dust 3 The free water content was 130mg/m 3 The method comprises the steps of carrying out a first treatment on the surface of the The temperature of the flue gas is 54 ℃, and the flow rate of the flue gas is 22 ten thousand meters 3 /h。
A physical separation adsorption gas-liquid-solid separation device, the front view is shown in fig. 1, the top view is shown in fig. 2, the left view of A-A section is shown in fig. 3, the schematic view of a trapping beam structure is shown in fig. 4, and the device comprises: 1-shell, 2-flue gas inlet, 3-equalizing plate, 4-collecting chamber, 5-upper cover plate, 6-flue gas outlet, 7-main guide groove, 8-out section guide groove, 9-in section guide groove, 10-out section isostatic pressing chamber, 11-in section isostatic pressing chamber, 12-out section isostatic pressing chamber valve plate, 13-in section isostatic pressing chamber valve plate, 14-collecting tank, 15-liquid outlet and 16-collecting beam.
The front end of the shell 1 is provided with a smoke inlet 2, smoke enters through an air inlet, uniformly presses and distributes flows through a pressure equalizing plate 3, enters a trapping chamber 4 for adsorption trapping, and is discharged through a smoke outlet 6 arranged at the tail end of the shell 1 after adsorption trapping;
the bottom of the shell 1 is provided with a liquid collecting tank 14 and a liquid outlet 15; an upper cover plate 5 is arranged at the upper part of the shell 1; a trapping chamber is arranged inside the shell 1; the catching bundle 16 is fixed or moved through the main guide groove 7, the moving-out section guide groove 8 and the moving-in section guide groove 9;
the trapping chamber is composed of a trapping bundle 16, a main guide groove, an outgoing guide groove and an incoming guide groove, wherein the trapping bundle 16 is arranged on the vertical ground of the silk threads. Limiting protruding strips are arranged on the frames of the trapping beams 16, or interval clamping rings are additionally arranged on the frames of the trapping beams, and the spacing between the trapping beams 16 is adjusted by adjusting the height of the protruding strips or the thickness of the interval clamping rings; the said guide channels 7, 8, 9 are provided with pushing or pulling means in which the trapping beams 16 move forward;
the front end of the leading groove 7 is connected with a moving-out section guide groove 8, the moving-out section guide groove 8 moves outwards, and the trapping beam 16 moves out of the shell 1 for offline maintenance and cleaning; the tail end of the main guide groove 7 is connected with a moving-in section guide groove 9 for supplementing a new trapping beam 16; the moving-out section guide groove 8 is provided with a moving-out section isostatic pressing chamber 10, the moving-in section guide groove 9 is provided with a moving-in section isostatic pressing chamber 11, and smoke leakage or wild wind is avoided when moving out or moving in the collecting beam 16; the moving-in section isostatic pressure chamber 10 is blocked and isolated from the shell 1 through a moving-out section isostatic pressure chamber valve plate 12, and the moving-out section isostatic pressure chamber 11 is blocked and isolated from the shell 1 through a supplementary section isostatic pressure chamber valve plate 13, so that system smoke leakage or air inlet is avoided when the trapping beam 16 is replaced;
the collector bundle 16 is composed of a frame and longitudinal wires fixed thereon. The material, diameter and distance between the silk threads are specifically designed according to the characteristics of the treated smoke and the site space;
the trapping beam 16 wires need to be perpendicular to the ground, so that the adsorption trapping substances can flow downwards along the trapping beam 16 wires.
The physical separation adsorption gas-liquid-solid separation method adopts the physical separation adsorption gas-liquid-solid separation device, and comprises the following steps:
(1) The physical separation adsorption gas-liquid-solid separation device is connected with a flue gas pipeline, and flue gas enters a trapping chamber 4 through a flue gas inlet 2 and uniform pressure gas distribution through a uniform pressure plate 3 for adsorption or bonding trapping; the smoke will generate turbulence after being intercepted by the capturing bundles 16 of each layer, the liquid drops will mutually collide and grow up, the smoke is captured when entering the capturing bundles 16 of the next stage, the probability of collision with the rear capturing bundles 16 is increased due to the generated turbulence, and the smoke is more easily captured; the solid particles adhere to and flow themselves on the trapping beam 16;
(2) The captured droplets and particles flow vertically downward into the liquid sump 14 and are discharged through the liquid discharge port 15;
(3) When the adhered objects of the trapping beam 16 are more, the trapping beam 16 is led out through the moving-out section guide groove 8, the taken trapping beam 16 is subjected to offline maintenance and cleaning, and meanwhile, a new trapping beam 16 or the cleaned trapping beam 16 is led in through the moving-in section guide groove 9 to supplement the insufficient trapping beam 16 in the trapping chamber.
In this embodiment, the desulfurized flue gas is introduced into a physical barrier adsorption gas-liquid-solid separation device through a pipeline, and the device is shown in fig. 1-4. The internal cross-sectional area of the device is designed to be 17 square meters and the length is 12 meters. After passing through the device, the flue gas is in: s is SO 2 Is 34mg/m 3， The removal rate is 24%; SO (SO) 3 Is 1.5mg/m 3 The removal rate is 50%; NO (NO) X Is 45mg/m 3 Almost no removal; dust 4.4mg/m 3 The removal rate is 60%; free water content 20mg/m 3 The removal rate is 85%; the flue gas temperature was 53 ℃. The smoke is obviously not tailing after demisting.
Claims (4)
1. The physical separation adsorption gas-liquid-solid separation device is characterized by comprising a shell, a flue gas inlet, a pressure equalizing plate, a trapping chamber, an upper cover plate, a flue gas outlet, a main guide groove, a moving-out section guide groove, a moving-in section guide groove, a moving-out section isostatic pressing chamber, a moving-in section isostatic pressing chamber, a moving-out section isostatic pressing chamber valve plate, a moving-in section isostatic pressing chamber valve plate, a liquid collecting groove, a liquid draining port and a trapping beam;
the front end of the shell is provided with a flue gas inlet, the shell is internally provided with a trapping chamber, the tail end of the shell is provided with a flue gas outlet, the bottom of the shell is provided with a liquid collecting tank and a liquid outlet, the upper part of the shell is provided with an upper cover, the trapping chamber consists of a plurality of groups of trapping beams, a main guide groove, a moving-out section guide groove and a moving-in section guide groove, and a pressure equalizing plate is arranged between the flue gas inlet and the trapping chamber for equalizing gas distribution;
the trapping chamber is internally fixed and moved by vertically distributed trapping beams and four corners of the trapping chamber, and a limiting raised strip or an interval clamping ring is arranged on the trapping beam frame; a pushing device or a guide chain pulling device is arranged on the main guide groove;
the front end of the main guide groove is connected with a moving-in section guide groove, the tail end of the main guide groove is connected with a moving-out section guide groove, the moving-out section guide groove is provided with a moving-out section isostatic pressure chamber, the moving-in section guide groove is provided with a moving-in section isostatic pressure chamber, the moving-out section isostatic pressure chamber is blocked and isolated from the shell through a moving-out section isostatic pressure chamber closed valve plate, and the moving-in section isostatic pressure chamber is blocked and isolated from the shell through a moving-in section isostatic pressure chamber closed valve plate;
the trapping beam is composed of a square frame-arranged longitudinal silk thread material, the diameter of the silk thread is larger than that of a liquid drop, and the distance between the silk threads is larger than 3 times of the diameter of the maximum intercepted fog drop and solid particles;
the trapping beams are obliquely arranged in the trapping chamber or perpendicular to the horizontal plane, and the number of the trapping beams is a plurality of trapping beams.
2. A physical separation adsorption gas-liquid-solid separation method, which is characterized by adopting the physical separation adsorption gas-liquid-solid separation device as claimed in claim 1, and specifically comprising the following steps:
step 1: the physical separation adsorption gas-liquid-solid separation device is communicated with a flue gas pipeline, flue gas enters a trapping chamber through a flue gas inlet, and trapped liquid drops and particulate matters in the flue gas are adsorbed or cohesively trapped by a trapping beam arranged in the chamber; the flue gas is intercepted by the trapping beams of each layer, turbulence is generated, liquid drops mutually collide and grow up, the flue gas is captured again when entering the next-stage trapping beam, solid particles in the flue gas are adhered and captured on the trapping beams, and the solid particles flow into the liquid collecting tank along with the adsorption liquid or the adhesion liquid;
step 2: the captured liquid drops and the captured particulate matters vertically flow downwards to enter the liquid collecting tank and are discharged through the liquid outlet;
step 3: when the trapped bundle is more adhered, the trapped bundle is replaced.
3. The method according to claim 2, wherein in the step 3, the replacement of the trapping beam is performed by a split-flow switching method, the trapping beam is led out through the removal section guide slot, the trapping beam is taken out for offline maintenance and cleaning, and a new trapping beam or the cleaned trapping beam is led in through the removal section guide slot, so as to supplement the insufficient trapping beam in the trapping chamber.
4. The method for physically separating and adsorbing gas, liquid and solid as claimed in claim 3, wherein in the step 3, the replacement of the trapping bundle is performed by uncovering an upper cover of the trapping chamber during discontinuous production.
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