WO2013060244A1 - 一种活性焦再生混合汽的处理方法和装置 - Google Patents

一种活性焦再生混合汽的处理方法和装置 Download PDF

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Publication number
WO2013060244A1
WO2013060244A1 PCT/CN2012/083005 CN2012083005W WO2013060244A1 WO 2013060244 A1 WO2013060244 A1 WO 2013060244A1 CN 2012083005 W CN2012083005 W CN 2012083005W WO 2013060244 A1 WO2013060244 A1 WO 2013060244A1
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Prior art keywords
water
gas
condensation
zone
condensing
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PCT/CN2012/083005
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English (en)
French (fr)
Inventor
张大伟
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密西西比国际水务有限公司
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Priority to US14/354,018 priority Critical patent/US10207215B2/en
Publication of WO2013060244A1 publication Critical patent/WO2013060244A1/zh

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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
    • B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
    • B01D46/0027—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours with additional separating or treating functions
    • B01D46/003—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours with additional separating or treating functions including coalescing means for the separation of liquid
    • B01D46/0031—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours with additional separating or treating functions including coalescing means for the separation of liquid with collecting, draining means
    • 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
    • B01D47/05—Separating dispersed particles from gases, air or vapours by liquid as separating agent by condensation of the separating agent
    • 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
    • B01D47/12—Washers with plural different washing sections
    • 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
    • B01D53/002—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 condensation
    • 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
    • B01D53/1406—Multiple stage absorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
    • B01J20/20—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising free carbon; comprising carbon obtained by carbonising processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/34—Regenerating or reactivating
    • B01J20/3416—Regenerating or reactivating of sorbents or filter aids comprising free carbon, e.g. activated carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/34—Regenerating or reactivating
    • B01J20/345—Regenerating or reactivating using a particular desorbing compound or mixture
    • B01J20/3458—Regenerating or reactivating using a particular desorbing compound or mixture in the gas phase
    • B01J20/3466—Regenerating or reactivating using a particular desorbing compound or mixture in the gas phase with steam
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B27/00—Arrangements for withdrawal of the distillation gases
    • C10B27/06—Conduit details, e.g. valves
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/08—Production of synthetic natural gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin
    • C10L5/26—After-treatment of the shaped fuels, e.g. briquettes
    • C10L5/28—Heating the shaped fuels, e.g. briquettes; Coking the binders
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2247/00—Details relating to the separation of dispersed particles from gases, air or vapours by liquid as separating agent
    • B01D2247/04—Regenerating the washing fluid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2247/00—Details relating to the separation of dispersed particles from gases, air or vapours by liquid as separating agent
    • B01D2247/10—Means for removing the washing fluid dispersed in the gas or vapours
    • B01D2247/107—Means for removing the washing fluid dispersed in the gas or vapours using an unstructured demister, e.g. a wire mesh demister
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2247/00—Details relating to the separation of dispersed particles from gases, air or vapours by liquid as separating agent
    • B01D2247/14—Fan arrangements for providing induced draft
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/10—Inorganic absorbents
    • B01D2252/103—Water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/80—Water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
    • B01D45/04—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by utilising inertia
    • B01D45/08—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by utilising inertia by impingement against baffle separators
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0027—Condensation of vapours; Recovering volatile solvents by condensation by direct contact between vapours or gases and the cooling medium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0027—Condensation of vapours; Recovering volatile solvents by condensation by direct contact between vapours or gases and the cooling medium
    • B01D5/003—Condensation of vapours; Recovering volatile solvents by condensation by direct contact between vapours or gases and the cooling medium within column(s)
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/08—Drying or removing water

Definitions

  • the invention belongs to a steam treatment device, in particular to a split and partitioned treatment method for mixed steam generated during active coke regeneration.
  • the invention also relates to an apparatus for carrying out the above method. Background technique
  • Active coke filtration adsorption treatment of wastewater or sewage is an emerging wastewater or wastewater treatment method.
  • the activated coke filtration adsorption method is used to pretreat the water in the polluted urban water source to remove pollutants, fungi, smell and color in the water, so that the treated water quality can reach the first-class water source water quality standard.
  • the active coke filtration adsorption method is used to deeply treat the biochemically treated industrial wastewater, so that the treated water quality can reach the enterprise production water standard or the nationally specified industrial pollutant discharge standard.
  • the activated coke after treatment of sewage and wastewater needs to be regenerated.
  • the water and organic matter in the activated coke are evaporated, pyrolyzed, and vaporized to form components containing water vapor, activated coke powder, formazan, and acetamidine. Mixed steam.
  • the mixed vapor body is sent out from the steam outlet of the regeneration equipment and sent to the steam inlet of the spray tower through the pipeline. Since the mixed vapor contains moisture and active coke dust, the activated coke dust in the mixed vapor is under the action of moisture. , adhered to the wall of the mixed steam transmission pipe, often causing blockage of the pipe, the regeneration equipment can not operate normally.
  • the present invention provides a method for treating activated coke regeneration mixed steam, which has the following processes:
  • the gas discharged from the upper portion of the second condensation zone is reused as a fuel; the spray water in the reduced diameter purification separator and the activated coke fine powder flow from the drain port at the lower portion of the condensation purification zone to the sedimentation tank through the drain pipe.
  • the device for realizing the above method provided by the invention mainly comprises two parts: a condensation dust remover and a variable diameter purification separator; wherein:
  • condensation dust collector One end of the condensation dust collector is provided with an inlet port of the mixed steam, the air inlet is connected to the steam outlet of the active coke regeneration unit, and the other end of the condensation dust collector is provided with a water gas outlet, and the water gas outlet is connected to a water gas inlet of a condensing purification zone at a lower portion of the variable diameter purifying separator, wherein at least one nozzle for spraying water is installed in the condensing dust collector to form a first condensation zone;
  • the lower part of the variable diameter purifying separator is a condensing purification zone, the upper part is a gas-water separation zone, and the diameter of the condensing purification zone is larger than the diameter of the gas-water separation zone;
  • the condensing purification zone is provided with a water gas inlet and a water outlet, and the upper part of the water gas inlet is an orifice plate, and at least one nozzle for spraying water is installed above the orifice plate to form a second condensation zone;
  • the gas-water separation zone There is at least one defogger in the gas-water separation zone, and the upper part of the gas-water separation zone is provided with an exhaust port; the mixed steam generated during the active coke regeneration process is introduced into the condensing dust collector by the nozzle water into the condensing dust collector.
  • the first water condensation, the spray water and the activated coke powder enter the condensing purification zone at the lower part of the variable diameter purification separator, and the water vapor in the gas and the activated coke dust are sprayed through the nozzle water above the orifice plate for the second time.
  • the water After the water is condensed and purified, it flows into the gas-water separation zone at the upper part of the variable-diameter purification separator, and the moisture in the gas is removed by the demister, and the remaining gas is discharged from the upper exhaust port, and the spray water in the variable-diameter purification separator is removed. And the activated coke fine powder is discharged from the drain port at the lower part of the condensation purification zone.
  • a nozzle for spraying water downwards between the two demisters In the device, wherein there are two defoggers in the gas-water separation zone, a nozzle for spraying water downwards between the two demisters; two holes are installed above the orifice plate of the condensing purification zone A nozzle that sprays water down.
  • the device wherein the mist eliminator is a flap type mist eliminator or/and a screen type defogger.
  • the device wherein three nozzles are installed in the condensation dust collector, one is disposed at the steam inlet and connected to the steam outlet of the active coke regeneration unit and faces the steam inlet, and the inside of the condensation dust collector is installed with two relative settings along the axis. Nozzle.
  • the device wherein all of the nozzles are connected to a water supply pipe.
  • the mixed steam is discharged from the activated coke regeneration equipment and directly enters the condensing dust collector.
  • the treated activated coke fine powder is transported by the condensed water and the spray water to the variable diameter purification separator to avoid blockage of the conveying pipeline.
  • the diameter of the lower condensing purification zone of the variable diameter purification separator is large, and the water vapor in the gas and the active coke dust have sufficient contact time with the spray water, so that they are condensed and purified.
  • the upper part of the gas-water separation zone of the variable-diameter purification separator has a small diameter, and the fast-flowing gas removes the moisture in the gas under the action of the defogger, and the remaining gas such as formazan and acetamidine is separated from the gas-water.
  • the exhaust port of the area is discharged. Since the discharged gas has low water content and is flammable, it can be used as a fuel. Condensed water, spray water and activated coke fines in the reduced-purification separator flow into the sedimentation tank from the lower drain of the condensate purification zone.
  • Figure 1 is a schematic view of the structure of the present invention.
  • the treatment device for the activated coke regeneration mixed steam of the present invention is composed of two parts, a condensing dust collector and a variable diameter purification separator.
  • variable diameter purification separator is divided into two zones: a lower part is a condensing purification zone, and an upper part is a gas-water separation zone.
  • the diameter of the condensing purification zone is larger than the gas-water separation zone.
  • the condensing dust collector has a steam inlet, a water gas outlet, a nozzle and a water supply pipe; the inlet of the condensing dust collector is connected with the steam outlet of the activated coke regeneration device; the water gas outlet of the condensing dust collector passes through the pipeline and the variable diameter purification separator Water and gas inlet connection.
  • the condensing purification zone at the lower portion of the variable diameter purifying separator has a water gas inlet and a drain port, the upper portion of the water gas inlet is an orifice plate, and at least one nozzle is provided at an upper portion of the orifice plate (in order to improve the condensation effect, an embodiment of the present invention is Taking three sets as an example, the nozzle is connected to the water supply pipe. There is an access port on the outer wall of the condensing purification zone.
  • the gas-water separation zone in the upper part of the variable-purification separator is provided with at least one defogger (for improving the defogging effect, one embodiment of the present invention is to set two demisters as an example), and the defogger may be a flap type Or / and wire mesh, flap or / and wire mesh mist eliminators are well known products.
  • the defogger may be a flap type Or / and wire mesh, flap or / and wire mesh mist eliminators are well known products.
  • the inlet of the condensing dust collector is connected to the steam outlet of the activated coke regeneration device; the water outlet of the condensing dust collector is connected to the water gas inlet of the condensing purification zone through a pipe.
  • the drain of the condensing purification zone is connected to the sedimentation tank through a pipe.
  • the mixed steam generated in the active coke regeneration process enters the condensing dust collector from the steam outlet, and the mixed steam is in the condensing dust collector.
  • the water vapor is condensed by the spray water of the nozzle for the first time, and the activated coke powder in the mixed steam is nozzle. Spray water wash.
  • the non-condensable combustible gas, the condensed water, the spray water, and the activated coke powder entrained by the water are discharged from the water vapor outlet of the condensing dust collector, and are passed through the pipeline from the lower water gas inlet of the variable diameter purifying separator into the condensing purification zone.
  • the lower condensing purification zone of the variable diameter purifying separator has a large diameter, and the water vapor and the activated coke dust in the gas have sufficient contact time with the spraying water in the second water condensation to ensure further condensation and purification.
  • the gas flow rate in the condensing purification zone is controlled so that the water vapor and the activated coke dust have sufficient contact time with the spray water, and the preferred flow rate of the present invention is 0.5 to 1.5 m/s.
  • the gas that has been condensed and purified is flowed into the gas-water separation zone at the upper portion of the variable-purification separator.
  • the flowing gas is discharged by the defogger in addition to the moisture in the gas, and the remaining gas such as formazan and acetamidine is discharged from the exhaust port, the exhaust pipe and the draft fan at the upper portion of the gas-water separation zone.
  • the gas flow rate of the demisting gas is controlled to completely remove the moisture in the gas when the gas is demisted, and the preferred flow rate of the present invention is 3-5 m/s. Since the discharged gas has low moisture content and is flammable, it can be used as a fuel.
  • the condensed water, the spray water and the activated coke fine powder in the water purification purifier are discharged from the drain port at the lower part of the condensing purification zone, and flow into the sedimentation tank through the drain pipe.
  • the mixed vapor separation treatment device produced in the active coke regeneration process provided by the present invention is composed of two parts: a reduced diameter purification separator 23 and a condensation dust remover 5.
  • variable diameter purifying separator 23 The lower portion of the variable diameter purifying separator 23 is a condensing purification zone 12, and the upper part is a gas-water separation zone 15.
  • the diameter of the cold condensation purification zone 12 is larger than the diameter of the gas-water separation zone 15.
  • the condensing dust collector 5 has a cylindrical structure, and the end of one end is provided with a steam inlet 4, and the other end is provided with a water gas outlet 6; the condensation dust collector 5 is provided with three nozzles 2, and two nozzles are installed inside and behind the axis along the axis. 2. At the end of the inlet 4, there is a nozzle 2 which projects into the outlet 3 of the activated coke regeneration unit and outward; all the nozzles 2 are connected to the water supply pipe 7.
  • the condensing purification zone 12 at the lower portion of the variable diameter purifying separator 23 has a water gas inlet 9, a drain port 10, an upper portion of the water gas inlet 9 is an orifice plate 11, and upper and lower nozzles 2 are provided at an upper portion of the orifice plate 11, and the nozzle 2 It is connected to the water supply pipe 7.
  • the outer wall of the condensing purification zone 12 has an access opening 13.
  • the gas-water separation zone 15 at the upper portion of the reduction purifier 23 has a first demister 14 and a second demister 17, and the first demister 14 and the second demister 17 may be folded. Mist or / and wire mesh defoggers, folding demister or / and wire mesh defogger are well known products.
  • the condensing purification zone at the lower portion of the variable diameter purifying separator 12 is designed to have a gas flow rate of 0.5-1.5 m/s, and the upper gas-water separation zone 15 has a design gas flow rate of 3-5 m/s.
  • the condensing dust collector 5 is designed to have a gas flow rate of 0.5-1.5 m/s.
  • the steam inlet 4 of the condensing dust collector 5 is connected to the steam outlet 3 of the activated coke regeneration device; the water gas outlet 6 of the condensing dust collector 5 is connected to the water gas inlet 9 of the condensing purification zone 12 through the pipe 8.
  • the drain port 10 of the condensing purification zone 12 is connected to the settling tank 22 through a pipe 21.
  • the mixed steam generated during the active coke regeneration process enters the condensing dust collector 5 from the steam outlet 3, the mixed steam is condensed in the condensing dust collector, the water vapor is condensed by the spray water of the nozzle 2, and the activated coke fine powder in the mixed steam is nozzle 2 Spray water wash.
  • the non-condensable combustible gas, the condensed water, the spray water, and the activated coke fine powder entrained by the water are discharged from the water vapor outlet 6 of the condensing dust collector 5, and enter the condensing purification zone 12 from the water gas inlet 9 through the pipe 8.
  • the designed flow rate of the gas in the condensing purification zone 12 is 0.5-1.5 m/s, and the water vapor and the activated coke dust in the gas have sufficient contact time with the spray water, so that they are condensed and purified, and then flow into the variable diameter purifying separator.
  • the design flow rate of the gas in the gas-water separation zone 15 is 3-5 m/s, and the fast-flowing gas removes the moisture in the gas under the action of a defogger 14 and a two-way demister 17, and the remaining formazan, B
  • the gas such as helium is discharged from the exhaust port 18 at the upper portion of the gas-water separation zone 15, the exhaust pipe 19, and the draft fan 20.
  • the discharged gas is flammable because of its low water content, so it can be used as a fuel.
  • the condensed water, the spray water, and the activated coke fine powder in the water in the reduced-diameter purifier 23 are discharged from the drain port 10 at the lower portion of the condensing purification zone 12, and flow into the sedimentation tank 22 through the drain pipe 21.

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  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
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  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
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  • Geochemistry & Mineralogy (AREA)
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  • Life Sciences & Earth Sciences (AREA)
  • Combustion & Propulsion (AREA)
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  • Physics & Mathematics (AREA)
  • Inorganic Chemistry (AREA)
  • Separating Particles In Gases By Inertia (AREA)
  • Treating Waste Gases (AREA)
  • Separation Of Particles Using Liquids (AREA)

Abstract

一种活性焦再生混合汽的处理方法，其过程为：A）活性焦再生过程中产生的混合汽先在第一冷凝区由喷淋水进行第一次水冷凝；B）第一次水冷凝后的混合汽进入第二冷凝区由喷淋水进行第二次水冷凝，使混合汽进一步冷凝和净化；C）第二次水冷凝后的混合汽中的气体部分经除雾去除气体中的水分，剩余的气体从第二冷凝区的上部排出；D）第二次水冷凝后的混合汽中的活性焦微粉随冷凝水排出。以及一种实现上述方法的装置。

Description

一种活性焦再生混合汽的处理方法和装置 技术领域
本发明属于汽体处理设备，特别涉及活性焦再生过程中所产生的混合 汽的一种分体、 分区式处理方法。
本发明还涉及一种实现上述方法的装置。 背景技术
活性焦过滤吸附处理废水或污水是一种新兴的废水或污水处理方法。 采用活性焦过滤吸附法， 对遭受污染的城市水源地的水进行预处理， 去除 水中的污染物、 菌类、 嗅味、 色度等， 使处理后的水质达到一级水源水质 标准。
采用活性焦过滤吸附法， 对经过生化处理的工业废水进行深处理， 可 以使处理后的水质达到企业生产用水标准或国家规定的行业污染物排放 标准。
处理污水、 废水后的活性焦吸附和大量的有机物， 并且含有大量的水 分。 处理污水、 废水后的活性焦需要进行再生， 在活性焦再生过程中， 活 性焦中的水分和有机物蒸发、热解、气化后形成含有水蒸汽、活性焦微粉、 甲垸、 乙垸等成分的混合汽。
活性焦再生过程中的混合汽如果采用传统的喷淋塔进行处理， 其存在 以下不足之处：
( 1 ) 混合汽体由再生设备出汽口出来后通过管道输送到喷淋塔进汽 口， 由于混合汽体中含有水分和活性焦粉尘， 混合汽体中的活性焦粉尘在 水分的作用下， 粘附在混合汽输送管道的壁上， 经常造成管道堵塞， 再生 设备无法正常运行。
( 2 ) 如果塔内的气体流速高， 混合汽中的水蒸汽无法完全冷凝， 处 理后的气体中夹带大量水分和活性焦粉末， 影响气水分离、 除尘效果， 处 理后的气体中由于含水率高而无法作为燃料回收利用。
( 3 ) 如果塔内的气体流速低， 混合汽中的水蒸汽大部分被冷凝， 混 合汽中夹带的活性焦粉末也能彻底净化， 但是， 由于气体流速低， 气水分 离、 除雾效果不好， 处理后的气体中由于含水率高而无法作为燃料利用。 因此， 提供一种混合汽分体、 分区式处理装置对活性焦再生过程中产 生的混合汽进行处理， 从而克服传统设备存在的不足， 是本发明的重点所 在。 发明内容
本发明的目的在于提供一种活性焦再生混合汽的处理方法。
本发明的又一目的在于提供一种实现上述方法的装置。
为实现上述目的， 本发明提供的活性焦再生混合汽的处理方法， 其过 程为：
A) 活性焦再生过程中产生的混合汽先在第一冷凝区由喷淋水进行第 一次水冷凝；
B) 第一次水冷凝后的混合汽进入第二冷凝区由喷淋水进行第二次水 冷凝， 使混合气进一歩冷凝和净化；
C)第二次水冷凝后的混合气中的气体部分经除雾去除气体中的水分， 剩余的气体从第二冷凝区的上部排出；
D) 第二次水冷凝后的混合气中的活性焦微粉随冷凝水排出。
所述的方法， 其中， 歩骤 B中混合汽进入第二冷凝区的流速控制在混 合汽中的水蒸汽和活性焦微尘与喷淋水有充分的接触时间， 从而被进一歩 冷凝和净化。
所述的方法， 其中， 歩骤 C中除雾的流速控制在气体在除雾时能完全 去除气体中的水分。
所述的方法， 其中， 歩骤 C中的气体是指甲垸和乙垸。
所述的方法， 其中， 第二冷凝区上部排出的气体作为燃料重复利用； 变径净化分离器内的喷淋水以及活性焦微粉从冷凝净化区下部的排水口 经排水管流入沉淀池。
本发明提供的实现上述方法的装置， 主要包括冷凝除尘器和变径净化 分离器两部分； 其中：
冷凝除尘器的一端设有混合汽的进汽口， 该进气口连接活性焦再生机 组的出汽口， 冷凝除尘器的另一端下方设有水气出口， 该水气出口连接至 变径净化分离器下部冷凝净化区的水气进口， 冷凝除尘器内均安装有至少 一个喷淋水的喷嘴， 形成第一冷凝区；
变径净化分离器的下部为冷凝净化区， 上部为气水分离区， 且冷凝净 化区的直径大于气水分离区的直径；
冷凝净化区设有水气进口和排水口， 位于水气进口的上部为孔板， 孔 板的上方安装有至少一个喷淋水的喷嘴， 形成第二冷凝区；
气水分离区内设有至少一道除雾器， 气水分离区的上部设有排气口； 活性焦再生过程中产生的混合汽由进汽口进入冷凝除尘器中被喷嘴 的喷淋水进行第一次水冷凝， 喷淋水以及活性焦微粉一起进入变径净化分 离器下部的冷凝净化区内， 气体中的水蒸汽和活性焦微尘经孔板上方喷嘴 的喷淋水进行第二次水冷凝和净化后， 流入变径净化分离器上部的气水分 离区， 经除雾器去除气体中的水分， 剩余的气体从上部的排气口排出， 变 径净化分离器内的喷淋水以及活性焦微粉从冷凝净化区下部的排水口排 出。
所述的装置， 其中， 气水分离区内设有两道除雾器， 在两道除雾器之 间设有一个朝下喷淋水的喷嘴； 冷凝净化区的孔板上方安装有两个朝下喷 淋水的喷嘴。
所述的装置， 其中， 除雾器是折板式除雾器或 /和丝网式除雾器。 所述的装置， 其中， 冷凝除尘器内安装有三个喷嘴， 一个设在进汽口 连接活性焦再生机组出汽口处并朝向进汽口， 冷凝除尘器内部沿轴线前后 安装有两个相对设置喷头。
所述的装置， 其中， 所有的喷嘴与供水管连接。
本发明的优点是：
1 ) 混合汽从活性焦再生设备排出后直接进入冷凝除尘器处理， 处理 后的活性焦微粉由冷凝水和喷淋水夹带输送到变径净化分离器， 避免输送 管道堵塞。
2) 变径净化分离器下部冷凝净化区直径大， 气体中的水蒸汽和活性 焦微尘与喷淋水有充分的接触时间， 从而被进一歩冷凝、 净化。
3 ) 变径净化分离器上部气水分离区直径小， 快速流动的气体在除雾 器的作用下， 去除了气体中的水分， 剩余的甲垸、 乙垸等气体从气水分离 区的排气口排出。 排出的气体由于含水率低， 具有可燃性， 因此可以作为 燃料利用。 变径净化分离器内的冷凝水、 喷淋水以及水中的活性焦微粉从 冷凝净化区下部排水口流入沉淀池。
上述装置至今未见有报道。 附图说明
图 1是本发明的结构示意图。
附图中主要组件标记说明：
1活性焦再生设备； 2喷嘴； 3 出汽口； 4进汽口； 5冷凝除尘器； 6 水气出口； 7供水管； 8管道； 9水气进口； 10排水口； 11孔板； 12冷凝 净化区； 13 检修口； 14第一道除雾器； 15气水分离区； 16检修孔； 17 第二道除雾器； 18排气口； 19排气管； 20引风机； 21排水管； 22沉淀池；
23变径净化分离器。 具体实施方式
本发明的活性焦再生混合汽的处理装置由冷凝除尘器和变径净化分 离器两个部分组成。
变径净化分离器分为两个区：下部为冷凝净化区，上部为气水分离区。 冷凝净化区的直径大于气水分离区。
冷凝除尘器有进汽口、 水气出口、 喷头和供水管； 冷凝除尘器的进汽 口与活性焦再生设备出汽口连接； 冷凝除尘器的水气出口通过管道与变径 净化分离器的水气进口连接。
变径净化分离器下部的冷凝净化区有水气进口和排水口， 水气进口的 上部为孔板， 在孔板的上部设有至少一个喷嘴（为提高冷凝效果， 本发明 的一个实施例是以设置三个为例）， 喷嘴与供水管道连接。 冷凝净化区外 壁有检修口。
变径净化分离器上部的气水分离区设有至少一道除雾器（为提高除雾 效果， 本发明的一个实施例是以设置两道除雾器为例）， 除雾器可以是折 板式或 /和丝网式， 折板式或 /和丝网式除雾器为公知产品。 设置两道除雾 器时， 在两道除雾器之间设有一向下喷淋水的喷嘴和检修孔， 喷嘴与供水 管道连接。 在气水分离区的顶部有排气口。
冷凝除尘器的进汽口与活性焦再生设备出汽口连接； 冷凝除尘器的水 气出口通过管道与冷凝净化区的水气进口连接。冷凝净化区的排水口通过 管道与沉淀池连接。
活性焦再生过程中产生的混合汽由出汽口进入冷凝除尘器， 混合汽在 冷凝除尘器中， 水蒸汽被喷嘴的喷淋水进行第一次水冷凝， 混合汽中的活 性焦微粉被喷嘴的喷淋水洗涤。 不凝可燃气、 冷凝水、 喷淋水以及被水夹 带的活性焦微粉一起由冷凝除尘器的水气出口流出， 通过管道从变径净化 分离器下部水气进口进入冷凝净化区内。
变径净化分离器下部冷凝净化区直径大， 气体中的水蒸汽和活性焦微 尘在第二次水冷凝时与喷淋水有充分的接触时间， 保证进一歩冷凝和净 化。在冷凝净化区内气体流速控制在水蒸汽和活性焦微尘与喷淋水有充分 的接触时间， 本发明优选的流速为 0.5-1.5m/s。 被进一歩冷凝和净化后的 气体流入变径净化分离器上部的气水分离区。流动的气体在除雾器的作用 下去除了气体中的水分， 剩余的甲垸、 乙垸等气体从气水分离区上部的排 气口、 排气管和引风机排出。 除雾的气体流速控制在气体在除雾时能完全 去除气体中的水分， 本发明优选的流速为 3-5m/s。 排出的气体由于含水率 低， 具有可燃性， 因此可以作为燃料利用。 变径净化分离器内的冷凝水、 喷淋水以及水中的活性焦微粉从冷凝净化区下部的排水口排出， 通过排水 管流入沉淀池。
以下结合附图和实施例对本发明作详细描述。
实施例
如图 1所示， 本发明提供的活性焦再生过程中产生的混合汽分体式处 理装置由两部分组成： 变径净化分离器 23和冷凝除尘器 5。
变径净化分离器 23下部为冷凝净化区 12， 上部为气水分离区 15。 冷 凝净化区 12的直径大于气水分离区 15的直径。
冷凝除尘器 5为圆柱体结构， 一端的端頭设有进汽口 4， 另一端的下 方设有水气出口 6; 冷凝除尘器 5安装有三个喷嘴 2， 内部沿轴线前后安 装有两个喷头 2， 在进汽口 4一端有一伸入到活性焦再生机组出汽口 3内 并且向外的喷嘴 2; 所有的喷嘴 2与供水管 7连接。 变径净化分离器 23下部的冷凝净化区 12有水气进口 9、 排水口 10， 水气进口 9的上部为孔板 11， 在孔板 11的上部有上、 下两个喷嘴 2， 喷 嘴 2与供水管 7连接。 冷凝净化区 12外壁有检修口 13。
变径净化分离器 23上部的气水分离区 15有第一道除雾器 14和第二 道除雾器 17，第一道除雾器 14和第二道除雾器 17可以是折板式除雾器或 /和丝网式除雾器， 折板式除雾器或 /和丝网式除雾器为公知产品。
在变径净化分离器 23上部气水分离区 15的第一道除雾器 14和第二 道除雾器 17之间有向下的喷嘴 2和检修孔 16， 喷嘴 2与供水管 7连接。 在气水分离区 15的顶部有排气口 18。
变径净化分离器 23下部的冷凝净化区 12设计气体流速为 0.5-1.5m/s， 上部的气水分离区 15设计气体流速为 3-5m/s。 冷凝除尘器 5设计气体流 速为 0.5-1.5m/s。
冷凝除尘器 5的进汽口 4与活性焦再生设备出汽口 3连接； 冷凝除尘 器 5的水气出口 6通过管道 8与冷凝净化区 12的水气进口 9连接。 冷凝 净化区 12的排水口 10通过管道 21与沉淀池 22连接。
活性焦再生过程中产生的混合汽由出汽口 3进入冷凝除尘器 5， 混合 汽在冷凝除尘器中， 水蒸汽被喷嘴 2的喷淋水冷凝， 混合汽中的活性焦微 粉被喷嘴 2的喷淋水洗涤。 不凝可燃气、 冷凝水、 喷淋水以及被水夹带的 活性焦微粉一起由冷凝除尘器 5的水气出口 6流出， 通过管道 8从水气进 口 9进入冷凝净化区 12内。冷凝净化区 12气体的设计流速为 0.5-1.5m/s， 气体中的水蒸汽和活性焦微尘与喷淋水有充分的接触时间， 从而被进一歩 冷凝、 净化后流入变径净化分离器 23上部的气水分离区 15。 气水分离区 15气体的设计流速为 3-5m/s， 快速流动的气体在一道除雾器 14和二道除 雾器 17 的作用下， 去除了气体中的水分， 剩余的甲垸、 乙垸等气体从气 水分离区 15上部的排气口 18、 排气管 19和引风机 20排出。 排出的气体 由于含水率低， 具有可燃性， 因此可以作为燃料利用。 变径净化分离器 23 内的冷凝水、 喷淋水以及水中的活性焦微粉从冷凝净化区 12下部的排水 口 10排出， 通过排水管 21 流入沉淀池 22。

Claims

权 利 要 求
1、 一种活性焦再生混合汽的处理方法， 其过程为：
A) 活性焦再生过程中产生的混合汽先在第一冷凝区由喷淋水进行第 一次水冷凝；
B ) 第一次水冷凝后的混合汽进入第二冷凝区由喷淋水进行第二次水 冷凝， 使混合气进一歩冷凝和净化；
C)第二次水冷凝后的混合气中的气体部分经除雾去除气体中的水分， 剩余的气体从第二冷凝区的上部排出；
D) 第二次水冷凝后的混合气中的活性焦微粉随冷凝水排出。
2、 根据权利要求 1所述的方法， 其中， 歩骤 B中混合汽进入第二冷 凝区的流速控制在混合汽中的水蒸汽和活性焦微尘与喷淋水有充分的接 触时间， 从而被进一歩冷凝和净化。
3、 根据权利要求 1所述的方法， 其中， 歩骤 C中除雾的流速控制在 气体在除雾时能完全去除气体中的水分。
4、 根据权利要求 1所述的方法， 其中， 歩骤 C中从第二冷凝区上部 排出的气体是指甲垸和乙垸。
5、 根据权利要求 1或 4所述的方法， 其中， 第二冷凝区上部排出的 气体作为燃料重复利用； 变径净化分离器内的喷淋水以及活性焦微粉从冷 凝净化区下部的排水口经排水管流入沉淀池。
6、 一种实现权利要求 1 所述方法的装置， 主要包括冷凝除尘器和变 径净化分离器两部分； 其中：
冷凝除尘器的一端设有混合汽的进汽口， 该进气口连接活性焦再生机 组的出汽口， 冷凝除尘器的另一端下方设有水气出口， 该水气出口连接至 变径净化分离器下部冷凝净化区的水气进口， 冷凝除尘器内均安装有至少 一个喷淋水的喷嘴， 形成第一冷凝区；
变径净化分离器的下部为冷凝净化区， 上部为气水分离区， 且冷凝净 化区的直径大于气水分离区的直径；
冷凝净化区设有水气进口和排水口， 位于水气进口的上部为孔板， 孔 板的上方安装有至少一个喷淋水的喷嘴， 形成第二冷凝区； 气水分离区内设有至少一道除雾器， 气水分离区的上部设有排气口； 活性焦再生过程中产生的混合汽由进汽口进入冷凝除尘器中被喷嘴 的喷淋水进行第一次水冷凝； 喷淋水以及活性焦微粉一起由冷凝除尘器水 气出口排出， 进入变径净化分离器下部的冷凝净化区内， 气体中的水蒸汽 和活性焦微尘经孔板上方喷嘴的喷淋水进行第二次水冷凝和净化后， 流入 变径净化分离器上部的气水分离区， 经除雾器去除气体中的水分， 剩余的 气体从上部的排气口排出， 变径净化分离器内的喷淋水以及活性焦微粉从 冷凝净化区下部的排水口排出。
7、 根据权利要求 6所述的装置， 其中， 气水分离区内设有两道除雾 器， 在两道除雾器之间设有一个朝下喷淋水的喷嘴； 冷凝净化区的孔板上 方安装有两个朝下喷淋水的喷嘴。
8、 根据权利要求 6或 7所述的装置， 其中， 除雾器是折板式除雾器 或 /和丝网式除雾器。
9、 根据权利要求 6所述的装置， 其中， 冷凝除尘器内安装有三个喷 嘴， 一个设在进汽口连接活性焦再生机组出汽口处并朝向进汽口， 冷凝除 尘器内部沿轴线前后安装有两个相对设置的喷头。
10、 根据权利要求 6、 7或 9所述的装置， 其中， 所有的喷嘴与供水 管连接。
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