CN116406346A - Sewage sludge fuel catalytic combustion device - Google Patents

Sewage sludge fuel catalytic combustion device Download PDF

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Publication number
CN116406346A
CN116406346A CN202180074224.5A CN202180074224A CN116406346A CN 116406346 A CN116406346 A CN 116406346A CN 202180074224 A CN202180074224 A CN 202180074224A CN 116406346 A CN116406346 A CN 116406346A
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sludge
gas
reactor
catalytic reactor
catalyst
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瓦列里·伊万诺维奇·布克提亚罗夫
尤里·弗拉基米罗维奇·杜比宁
安娜·亚历山大罗夫娜·列奥诺娃
安东·尤里耶维奇·米哈尔科夫
伊戈尔·阿纳托利维奇·费多罗夫
谢尔盖·尼古拉耶维奇·谢利特
瓦迪姆·阿纳托列维奇·亚科夫列夫
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Rvk Kataliz LLC
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Rvk Kataliz LLC
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Priority claimed from RU2020136580A external-priority patent/RU2752476C1/en
Priority claimed from RU2020136581A external-priority patent/RU2749063C1/en
Application filed by Rvk Kataliz LLC filed Critical Rvk Kataliz LLC
Publication of CN116406346A publication Critical patent/CN116406346A/en
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/06—Treatment of sludge; Devices therefor by oxidation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/18—Treatment of sludge; Devices therefor by thermal conditioning
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/01—Fluidised bed combustion apparatus in a fluidised bed of catalytic particles
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C13/00—Apparatus in which combustion takes place in the presence of catalytic material
    • F23C13/08—Apparatus in which combustion takes place in the presence of catalytic material characterised by the catalytic material
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C7/00—Combustion apparatus characterised by arrangements for air supply

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Analytical Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)
  • Catalysts (AREA)

Abstract

The invention relates to a device and a method for incinerating wet sludge containing organic substances in municipal sewage treatment facility sewage, and relates to a process method for catalytically combusting the wet sludge in the sewage in a catalyst fluidized bed reactor. The invention comprises a sewage sludge fuel catalytic combustion device and a catalytic reactor of the device. The technical achievements to be achieved by the invention are as follows: the operation performance of the sewage sludge fuel catalytic combustion device is improved.

Description

Sewage sludge fuel catalytic combustion device
Technical Field
The invention relates to a device and a method for incinerating wet sludge containing organic substances in municipal sewage treatment facility sewage, and relates to a process method for catalytically combusting the wet sludge in the sewage in a catalyst fluidized bed reactor.
Background
An inert ebullated-bed apparatus is known for recycling carbonaceous waste in municipal wastewater treatment facilities, comprising a boiler plant, an ebullated-bed combustion chamber and a natural gas power plant with an exhaust gas conduit, and a high pressure blower with a mixing chamber of fresh air and hot flue gas, the mixing chamber being connected to the natural gas power plant exhaust gas conduit; a box-shaped air heater through which the hot mixture passes by means of a blower into a ebullated-bed combustion chamber for burning moist carbonaceous deposits in the contaminated water on a hot inert ebullated bed; a settling chamber above the ebullated bed combustion chamber having a cross-section greater than the cross-section of said combustion chamber; and a side bag for collecting waste ash from the settling chamber with the screw unloader. When the moist sewage sludge falls onto the hot surface of the ebullated bed, the moisture evaporates instantaneously and the solid particles are burned off rapidly. Since the cross section of the ebullated bed combustion chamber is smaller than the cross section of the settling chamber, the formed waste ash slides down into the side discharge bag and is discharged from the combustion chamber by the screw unloader. The unburned fuel fine particles and the unburned combustible gas are combusted in the afterburner. (RU 2351847, publication date: 10/04/2009, international patent Classification: F23G5/30, F23C 10/00).
A disadvantage of the known solutions is the combustion in the inert material layer. Implementation of this procedure in this way will lead to the generation of large amounts of toxic substances in the exhaust gases, whereby a complex and expensive purification system has to be created. Furthermore, the use of inert materials determines that the process needs to be carried out in a high temperature environment (not lower than 800-1000 ℃), which results in high consumption of structural materials and increased demands on the materials themselves.
There is known a method for treating sewage sludge containing organic substances (patent RU No. 2568978) in which dewatered sludge is dried to a humidity of 1-2% at a temperature of 100-200 ℃ in contact with a fluidized bed of a dispersed particle mixture of catalyst and inert material in the upper part of an additional reactor. After separation of the sludge from the steam-gas mixture, about 60% of the sludge (humidity 1-2%) is treated in a fluidized bed of a mixture of dispersed particles of catalyst and inert material in the lower part of the reactor at a temperature of 700-750 ℃, said bed being controlled in sequence by means of fixed nozzles and a grid, wherein the grid parameters of the grid are such that the temperature gradient of the continuous fluidized bed above and below the grid is 500-550 ℃. The remainder of the sludge is heat treated in a fluidized bed of a dispersed particle mixture of catalyst and inert material controlled by fixed nozzles in a main reactor at 500-750 ℃. (RU 2568978, publication date: 11/20/2015, international patent Classification: C02F11/06, F23C 10/01).
The disadvantages of the known solutions are: an additional pre-drying stage is required, which results in complex process links, significant increases in energy costs, and difficulty in controlling each stage of the process. In addition, river sand is used as an inert material for the bed in this method. River sand and catalyst particles are not completely homogeneous mixtures and have different strength characteristics, which may lead to uneven distribution of catalyst on the bed and a rapid attrition rate.
An apparatus comprising 3 reactor sets, 1 solid fuel supply system with spiral distributor, 1 liquid fuel supply apparatus, 1 liquid fuel ignition system, 1 rotary piston compressor for supplying air for catalyst bed liquefaction and fuel oxidation, 1 economizer and 1 flue gas cleaning system (cyclone and bag filter) was selected as a prototype of the present invention, wherein flue gas after passing through the cyclone and bag filter was discharged to the stack, and ash discharged from the cyclone and bag filter was fed into a pipe conveyor through which it was fed into a storage hopper. (literature: experience in use of water-boiling boilers which can catalytically burn liquid and solid fuels in fluidized beds, authors: west Meng Nuofu A.D., yajikov N.A., alf Liang Tunuo A.S., fexodorv I.A., yakev Hi.A., and Parr Mo Fu V.N., J.Engineer. Energy and ecology, 2014, no. 19 (159), pages 70-85, publication date: 2014, 12, 31).
The disadvantage of this prototype is that the heat generator has a large external size and high power consumption, and when burning fuels with a high total humidity, the catalyst consumption increases due to the increased velocity of the gas through the cross section of the device and the formation of additional water vapor, and the increased blowing out of catalyst particles. In addition, water cannot be added to the sludge. Since sludge is a non-uniform substance, it may occur that the sludge humidity is lower than the working value (75%), which will lead to a warming of the fluidized bed. In said invention it is possible to cool the bed by withdrawing part of the bed from the reactor, but this method is not optimal and is costly. Furthermore, there is no steam precipitation component (wet filter) in the device, which will result in excessive steam being vented to the atmosphere. Besides, the drawbacks of the prototype device include that the air is supplied from one point to the distribution device, which in this case has a total distribution pipe that combines all the lines together, so that the metal consumption is high.
Disclosure of Invention
A sewage sludge fuel catalytic combustion device which is different from a prototype device comprises a catalytic reactor for recycling sewage sludge, wherein a catalyst supply pipe is arranged at the upper part of a reactor shell, a hollow truncated cone-shaped gas-liquid separator is arranged below a top cover connected with a flue gas pipeline, and is downwards fixed on the reactor shell through a base with a smaller diameter, wherein the tip of a quadrangular pyramid is downwards fixed, the diagonal line of the base of the tip is larger than the diameter of a truncated cone-shaped small base of the gas-liquid separator, and a certain gap is formed between the base surface of the tip and the truncated cone-shaped small base surface of the gas-liquid separator; two completely opposite sewage sludge supply pipes are arranged in the oxidation area at the lower part of the catalytic reactor shell, a water supply pipe is welded on each sewage sludge supply pipe, a gas distribution mechanism is arranged between the catalyst removal connecting pipe and an unburned sludge unloading area connected with a spiral unloader connecting pipe, the gas distribution mechanism consists of two external distribution pipes which are positioned on the same plane and are parallel to each other at the completely opposite two walls of the reactor shell, and each distribution pipe is divided into 3 circular section pipes with perforations below the pipe walls through bent pipes; the catalytic combustion device also comprises a blower and a heat generator connected in series with the catalytic combustion device through an air supply line, a heat recovery device connected in series with the catalytic combustion device through an exhaust line, an economizer, a bag filter, a wet vortex filter, a high pressure fan and a flue, and a solid fuel supply system-a feed hopper with a spiral distributor, an unburned sludge unloading hopper.
A method for catalytic combustion of a sewage sludge fuel, said method being implemented by a sewage sludge fuel catalytic combustion device, wherein a heat treatment is carried out in a fluidized bed in the presence of a CO deep oxidation catalyst; carrying out heat treatment by continuously supplying sewage sludge into a catalytic reactor heated to 750 ℃ while feeding air required for maintaining a catalyst fluidized bed state, oxidizing sludge organic matters and CO and organic matters formed during reoxidation combustion into the reactor; the flue gas enters a heat recovery device from a catalytic reactor, then enters an internal space of an economizer tube, enters a bag filter for purification after being cooled by water, and enters a wet vortex dust filter for simultaneously condensing vapor formed in the catalytic combustion process of sewage sludge and neutralizing acid gas contained in the flue gas.
A catalytic reactor for recovering sewage and sludge from sewage and sludge fuel catalytic combustion unit is composed of a vertical casing, a catalyst supplying pipe at the upper part of said casing, a sludge inlet pipe, a spiral coal feeding pipe, a catalyst removing pipe, a soft tissue filler at the middle part of said casing, and a spiral discharger for unloading the unburned sewage and sludge. Unlike the prototype, the gas-liquid separator is located at the upper part of the reactor shell and below the top cover connected with the flue gas pipeline, the gas-liquid separator is in the shape of a hollow truncated cone, and is downwards fixed on the reactor shell through a base with smaller diameter, wherein the tip head of the quadrangular pyramid is downwards fixed, the diagonal line of the tip base is larger than the diameter of the truncated cone small base of the gas-liquid separator, and therefore a certain gap is formed between the base surface of the tip and the truncated cone small base surface of the gas-liquid separator; the catalytic reactor comprises a catalytic reactor shell, a catalytic reactor, a spiral unloader, a catalyst removal connecting pipe, a spiral unloader connecting pipe, a gas distribution mechanism and a gas distribution mechanism, wherein the gas distribution mechanism is arranged between the catalytic reactor shell lower part in an oxidation area and an unburned sludge unloading area connected with the spiral unloader connecting pipe, the gas distribution mechanism is composed of two external distribution pipes which are positioned on the same plane and are parallel to each other on two diametrically opposite walls of the catalytic reactor shell, and each distribution pipe is provided with a perforated circular section pipe below 3 pipe walls through a bent pipe.
A sewage sludge recycling method, wherein heat treatment is carried out in a catalyst dispersion particle fluidized bed. Unlike the prototype of the invention, the process is carried out in a catalytic reactor for recycling sewage sludge of a catalytic combustion device for sewage sludge type fuel in the presence of a catalyst, by continuously feeding sewage sludge into the catalytic reactor, while feeding air required for maintaining the fluidization state of the catalyst bed into the catalytic reactor.
The gas-liquid separator is positioned at the upper part of the reactor shell and below the top cover connected with the flue gas pipeline, the gas-liquid separator is in the shape of a hollow truncated cone, and is downwards fixed on the reactor shell through a base with a smaller diameter, wherein the tip head of the quadrangular pyramid is downwards fixed, and the diagonal line of the tip base is larger than the diameter of the truncated cone small base of the gas-liquid separator, so that a certain gap is formed between the base surface of the tip and the truncated cone small base surface of the gas-liquid separator. The diameter of the large-diameter cone base of the gas-liquid separator is 40% larger than that of the flue gas pipeline. The structure of the gas-liquid separator in the reactor can ensure a reduction in the blowing-out amount of the material and the catalyst and the adhesion to the gas-liquid separator.
And a gas distribution mechanism is arranged between the catalyst removal connecting pipe and the spiral unloading machine at the lower part of the reactor shell. The gas distribution mechanism consists of two external distribution pipes which are positioned on the same plane and are parallel to each other on two completely opposite walls of the reactor shell, and each distribution pipe is divided into 3 circular section pipes with perforations below the pipe walls by the bent pipes; perforated circular section tubes are welded to the reactor shell below the tube wall, and the free weld end of each tube is inserted into a sleeve welded to the outside of the reactor shell on the side opposite the elbow, while all perforated tubes lie in one plane and leave a gap between the tubes for passage of unburned portions of sewage sludge when installed. The perforations of the tubes are inside the reactor shell and the total area of the perforations on the tubes is 2.5% of the cross-sectional area of the lower part of the reactor shell.
The structure of the gas distribution mechanism can ensure the boiling uniformity of the separation area and the oxidation area of the reactor, so that the adhesion degree of ash residues on an air distributor is reduced to the minimum, unburned large-particle sludge and catalyst enter an unloading area in the base of the reactor shell through a gap between air distributor pipes, a spiral unloading machine for unloading large-particle unburned sludge in sewage is arranged in the unloading area, and then the spiral unloading machine is removed from the reactor without closing the spiral unloading machine.
Selecting an inner diameter as a shell size optionThe main indexes selected are as follows: the diameter of the lower part of the reactor is 1.70m, and the cross-sectional area is 2.26m 2 The diameter of the middle part is 2.18m, and the diameter of the upper part is 2.8m. The height of the reactor cavity is 4.0m.
The filter after the bag filter is able to condense (precipitate) water in the steam-gas mixture to a large extent and neutralize the acid gas by alkali treatment. The problem of pre-cooling carbonaceous fuel or organic compounds to an acceptable temperature before their residual water vapour in the flue gas produced after combustion is vented to atmosphere is solved by a dust filter. Sulfur dioxide SO 2 I.e. the main acidic oxide in the exhaust gas component after passing through the reactor. The oxide is formed by oxidation of sulfur contained in the sewage sludge residue by oxygen in the ebullated bed of the catalyst. To neutralize the equilibrium form of sulfurous acid formed in the solution, an alkaline agent (NaOH or Na) is added to the water of the filter 2 CO 3 )。
Recovery (combustion) of sludge in the presence of a catalyst for the deep oxidation of CO and organic substances, containing alumina Al 2 O 3 An oxidation support having a content of not more than 50wt%, fe 2 O 3 48 to 75wt%, cuO 0wt%, 2 to 3wt%, 3.5 to 6wt%, and/or Mn 2 O 3 And/or Co 2 O 3 And/or Cr 2 O 3 An active ingredient in an amount of 2-10 wt%; the heat treatment is carried out by continuously feeding the sludge into a catalytic reactor heated to 750 ℃ which is fed with the air necessary for maintaining the fluidization and oxidation state of the organic fraction of the sludge and for reoxidation of the CO produced during combustion. And the excess air coefficient is similar to the stoichiometric coefficient (1<α≤1.2)。
The burn-up degree of sludge in the combustion process is selected as an index for measuring the catalytic activity of a catalyst in the sludge combustion process of municipal sewage treatment facilities, and the burn-up degree is 98.1-99.3%.
Problems to be solved by the invention
The invention aims to solve the technical problems of developing a method and a device for recycling sewage and sludge, which can effectively utilize heat energy generated by incinerating sludge, and the device can ensure that waste flue gas is environment-friendly and safe, the process is continuously carried out, the consumption of a full oxidation catalyst is possibly reduced, and the efficiency of the sewage and sludge recycling process in a boiling bed is improved.
Means for solving the problems
The present invention is characterized in that the proposed catalytic reactor structure is not known in the prior art, the prior art reactor is not provided with a gas grid plate with an air distribution cover, the novel structure of the gas distribution mechanism can ensure the uniformity of boiling of a separation area and an oxidation area of the reactor, the adhesion degree of ash residues on an air distributor is minimized, the ash residues enter an unloading area in a base of a shell of the reactor through a gap between air distributor pipes, a spiral unloading machine for unloading unburned sewage sludge is arranged in the unloading area, the spiral unloading machine is removed from the reactor without stopping the spiral unloading machine, and the novel structure of a gas-liquid separator in the reactor can ensure the reduction of the blowing-out amount of materials and catalysts and the adhesion degree of the gas-liquid separator, thereby solving the existing technical problems.
ADVANTAGEOUS EFFECTS OF INVENTION
The invention has the following technical results: the boiling uniformity of the ebullated bed is improved, it is ensured that large-particle impurities formed during the combustion of sewage sludge are discharged from the ebullated bed region, and then the large-particle impurities are removed therefrom without shutting down the reactor, the blowing-out amount of materials and catalysts is reduced, the adhesion thereto is reduced without changing the pressure difference on the gas-liquid separator device, and it is ensured that highly oxidizable high-activity catalysts can be used, which not only affect the degree of burn-out of municipal sewage treatment facility sludge in the combustion process but also affect the concentration of harmful substances in exhaust gas, and can effectively precipitate steam and neutralize acid gas in one apparatus, a wet vortex filter.
Drawings
In order to illustrate the possibilities of implementing the invention and to understand the nature more fully, embodiments thereof are listed below, which may be modified or supplemented in any form, while the invention is not limited to the listed embodiments.
The catalytic reactor (fig. 1) is a vertical shell 1, wherein the diameter of the lower part of the reactor is 1.70m, the diameter of the middle part is 2.18m, and the diameter of the upper part is 2.8m. The height of the reactor cavity is 4.0m.
The upper part of the reactor shell 1 is provided with a catalyst feed connection pipe 2 and a hollow frusto-conical gas-liquid separator 10 below a top cover 8 to which a flue gas duct 9 is attached. The middle part inside the shell 1 is provided with a soft tissue packing 7 for reducing fluidized bed non-uniformity, i.e. destroying large bubbles in the reactor. Two sludge supply pipes 4 and two spiral coal supply connecting pipes 3 and a catalyst removal connecting pipe 6 are arranged at the lower part of the shell. Sludge (filter residue) is fed into the reactor through two diametrically opposed connection pipes 4, on which a water feed pipe 5 is installed, whereby overheating of the reactor due to non-uniformity of sludge components can be effectively controlled. A gas distributing mechanism 12 is arranged between the catalyst removing connecting pipe 6 and an unburned sludge unloading zone 24, wherein the unburned sludge unloading zone is provided with a connecting pipe of a spiral unloading machine 18, and the outlet of the spiral unloading machine is provided with a gate valve 19. The gas distribution mechanism 12 (fig. 2) comprises two distribution pipes 13, two bent pipes 14 and a pipe 15 with perforations 16 below the two pipe walls, the open ends of which are inserted into a sleeve 17.
The gas-liquid separator shown in fig. 3 and 4 comprises a housing 10 of frustoconical shape and a rectangular pyramid-shaped tip 11.
As shown in fig. 1: a separation zone 21 of the catalytic reactor, an oxidation, coal and sludge supply zone 22, an air distribution zone 23 and an unburned sludge unloading zone 24.
An apparatus for catalytic combustion of sewage sludge (fig. 5) comprises: a blower 34 and a heat generator 33 connected in series with the catalytic reactor 25 by air transfer lines, a recuperator 26 connected in series with the catalytic reactor by exhaust lines, an economizer 27, a bag filter 28, a wet vortex filter 29, a high pressure fan (exhaust fan) 30 and an exhaust stack 31, and a solid fuel supply system 35 (flow control trough with spiral distributor) and an unburned sludge unloading trough 32.
FIG. 1 is a schematic diagram of a catalytic reactor.
FIG. 2 is a schematic diagram of a gas separation mechanism of a reactor.
FIG. 3 is a schematic view (longitudinal section) of a gas-liquid separator.
Figure 4 is a schematic diagram (cross section) of a gas-liquid separator.
FIG. 5 is a view of a sewage sludge thermocatalytic oxidation apparatus.
FIG. 6 is a comparative property of a deep oxidation catalyst.
Detailed Description
Will be 2.5m 3 Is charged into the empty reactor 25 through the connection pipe 2, the high-pressure fan 30, the blower 34, the water circulation in the economizer 27, and the heat generator 33 are turned on. The flue gas generated in the heat generator under diesel flame combustion is mixed with air at a temperature of around 700 c, wherein the temperature is set by adjusting the air flow of the blower. The mixture is fed into the reactor through a gas-dividing mechanism 12. Air is fed through perforations 16 in the walls of the two distribution pipes 13 and the gas distribution pipe 15, thereby ensuring uniformity of the distribution of air in the zone 23 and the oxidation zone 22 of the reactor. While changing the air flow from horizontal to vertical and uniformly distributed in the oxidation zone 22 of the reactor. To ensure a uniform distribution of the catalyst fluidized bed and to avoid catalyst particles falling onto the inlet pipe, the perforated pipe should have a perforated area of 2.5% and correspondingly the gas flow rate from the perforations should be 24m/s. The proposed gas distribution structure ensures a more uniform fluidized bed. The perforation at the lower part of the pipe wall ensures that the gas distributing mechanism is not blocked. To ensure free thermal expansion of the perforated tube 15, its free weld ends are provided with voids and are inserted into the sleeve 17, which is welded from the outside to the reactor shell 1 and is arranged on the outside so that the lower cross section of the reactor can be used to the greatest extent.
The heated flue gas passes through the catalyst bed. After heating the catalyst bed to a temperature of 350-400 deg., the necessary additional amount of air (up to 8500Nm 3 /h, while pressurizing to 40 KPa). At the same time, the catalyst bed is in a fluidized state, while crushed coal is fed from the hopper 35 via the connecting pipe 3 to the reactor 25 in small amounts by the spiral distributor, and the bed is fedThe temperature in the body is controlled to be raised to 600-700 ℃. When the temperature rise is fixed by increasing the consumption of coal, the temperature of the bed body is raised to 750 ℃. The catalyst was gradually added to the reactor through the pipe connection 2 until the total volume of the catalyst reached 9m 3 At the same time, the coal supply was gradually increased, the hot gas supply was turned off, and the temperature was maintained at 750 ℃. The additional uniformity of the gas flow in the reactor can be further ensured by the soft tissue fillers 7 which can be used to reduce the non-uniformity of the fluidized bed, i.e. to destroy large gas bubbles in the reactor. The heat generator 33 is then turned off. After the catalyst is heated, sewage sludge with the humidity of 73-75% is added into the reactor through two connecting pipes with positive phases completely opposite to each other, and the inlet of each connecting pipe is arranged in an oxidation, coal feeding and sludge supplying area arranged at the lower part of the reactor. The water adding pipe 5 is installed on the sludge supply connecting pipe 4 in the reactor, so that the overheat phenomenon generated in the reactor due to the uneven sludge components can be effectively controlled. Gradually increasing the flow of sewage sludge and controlling the temperature of the oxidation, coal feed and sludge supply areas. As the temperature increases, the supply of crushed coal decreases. When the sewage sludge (wet sludge 6 t/h) reaches the standard consumption, the temperature of the oxidation, coal feed and sludge supply zone 22 is maintained at 750 ℃. When the supply of the supplementary fuel is completely stopped and the temperature is further raised above the temperature (750 ℃) required for heat-treating the sludge, water is added to the sludge supply connection pipe 4 through the connection pipe 5.
After switching off the heat generator 33, air is supplied in the inter-tube space by the recuperation device 26. The air is heated by extracting heat from the flue gas exiting the reactor 25.
When the temperature drops below the standard temperature of 750 ℃, the humidity of the sewage and sludge is increased by more than 75%, at the moment, the power of the spiral distributor is regulated to be minimum, the crushed coal supply system 35 is started, and then the power of the spiral distributor is regulated to increase the consumption of the crushed coal, so that the bed temperature reaches the standard temperature of 750 ℃.
As the bed temperature increases above 750 ℃, i.e. the sewage sludge humidity decreases below 73-75%, the amount of air passing through the recuperator 26 is reduced while the air coming directly out of the blower 34 into the reactor 25 is increasedAir flow, at which time the total air flow is maintained at 8273-8300m 3 And/h. In this case the air temperature is reduced and the bed temperature of the reactor 25 is reduced. No regeneration device 26 is used for all air flows. As the humidity of the sewage sludge further decreases and the bed temperature further increases, water is supplied through the connection pipe 5, and the flow rate is from minimum to maximum. When the water flow reaches a maximum and the bed temperature tends to rise, the sewage sludge flow fed into the reactor is reduced.
When the catalyst bed height decreases due to catalyst attrition, the catalyst is charged to standard levels with no shut down of the reactor.
Through the gaps between the tubes 15 of the gas dividing means 12, the large unburned fractions of the sewage sludge enter an unloading zone 24 (fig. 2) in the bottom of the housing of the reactor 1, in which unloading zone the screw discharger 18 for unloading the unburned sewage sludge is located. The unburned portions of the bulk impurities in the sewage sludge are periodically unloaded by the unloader 18, which is required to pass through an unburned impurity unloading zone 24 at the bottom of the reactor. Unloading does not require shutting down the reactor.
In order to reduce the occurrence of the blowing-out phenomenon of the catalyst from the reactor together with the flue gas formed by burning the sewage sludge, a gas-liquid separator 10 is provided in the separation zone 21. The flue gas from the incineration of sludge in the separation zone 21 collides with the catalyst particles into the hollow truncated cone-shaped gas-liquid separator 10 with the tip 11 of the quadrangular pyramid shape. The gas-liquid separator 10 is fixed downward below the flue gas duct 9 on the reactor housing 1 by a smaller diameter base with the tip 11 of the quadrangular pyramid fixed downward, the diagonal of the tip base being larger than the diameter of the small base of the gas-liquid separator truncated cone. The structure of the gas-liquid separator ensures a uniform distribution of the fluid over the reactor cross-section without aerodynamic impediments. Catalyst solid particles and ash particles are broken up and returned to the separation zone 21-ebullated bed and burned off or passed through the gap of perforated pipe 15 of the gas separation mechanism 12 into the unburned sludge unloading zone 24. The small catalyst or ash particles that enter the vertebral cavity of the gas-liquid separator are poured into the gap formed by the tip base surface and the small base surface of the truncated cone shape of the gas-liquid separator. The remaining ash stream leaves the reactor through the flue gas duct 9 of the top cover 8 and enters the next stage of the process chain.
From the reactor 25, the flue gas at a temperature of 750 ℃ enters a recuperator 26, in which it is cooled to 660 ℃. The air flowing through the regenerator 26 is heated to a design temperature of 239 ℃. From the recuperator 26, the flue gas enters the pipe space of an economizer 27 where it is cooled to 185-200 ℃ using water circulated through the inter-pipe space and then enters the bag filter 28 for cleaning. Mechanical suspension of the flue gas is removed in a bag filter 28. The cleaned flue gas enters a filter 29 (fig. 1) in which the steam in the flue gas is "precipitated" at a rate of 3.5t/h and the acidic oxides are recovered by combination with alkaline agent added to the water of the filter 29. The components of the vapor gas mixture include: smoke is not less than 11600kg/h, ash is 0.9kg/h, water vapor with temperature of 185-200deg.C is not less than 4500kg/h, and temperature is 25-30deg.C and not less than 240m 3 The horizontal row of/h is injected into the dust filter. This condition ensures that the steam gas mixture can be cooled to 60-70 c while condensing not less than 3500kg/h of water vapour from the cooled steam gas mixture, the temperature of the water coming from the dust filter being 10-20 c higher than the temperature of the injected water.
The water entering the dust filter passes through alkaline agent (NaOH or Na) 2 CO 3 ) The alkaline agent is continuously formulated to ensure the presence of acidic oxides (mainly SO 2 ) Effectively dissolves and bonds. Through chemical analysis data, the sulfur content of combustible substances in the sludge reaches 0.8wt%. The consumption of sludge in the thermocatalytic oxidation process is 1050kg/h calculated according to combustible substances and is converted into SO 2 16.8kg/h. Ash formed during the combustion of the sludge captures not less than 90% or not less than 15.12kg/h of dioxide (salt formation). Thus, there will be no more than 1.68kg/h SO 2 Falls onto the dust filter. It is assumed that all the dissolved sulphur dioxide is converted into the sulphite equilibrium form, in which case it is assumed that the concentration [ H ]]Will be 1.08X10 -4 About mol/l. The pH of the solution will therefore be around 4.0.
To neutralize the solution, a concentration of 1X 10 can be used -4 Sodium base (NaOH) in mol/l or 24 mol/h. Therefore, about 960g/h of NaOH must be added to the water of the filter. When sodium carbonate (Na 2 CO 3 ) For neutralization, it is necessary to use 0.5X10 -4 mol/l or 12mol/h of salt. The corresponding flow rate was 1.272kg/h.
Flue gas from the dust filter 29 containing 1t/h of steam passes along the flue gas duct via the high pressure fan 30 into the exhaust stack 31.
The activity of the catalyst in the CO oxidation reaction was measured by pulsing on a "chemisorption" instrument at a temperature of 50% conversion of CO.
Examples
Example 1
The pseudo-boehmite aluminum hydroxide is stirred in distilled water added with concentrated nitric acid. The acidity factor (molar ratio of acid to alumina) was 0.01. The suspension was stirred for 1 hour. Adding grinding powder of active ingredient (surface is not less than 10m by calcining nitrate 2 The preparation of per g of the nanocomposite is as described in the paper (Fei Duoluo v, tesabana a.m., brav Shen Ke o.a., sala v a.a., aldova g.v., phyllomagav d.y., zu Bawei chus y.v., jacob v.a., kevlar v.v., cu-Fe-Al structure and chemical composition of the nanocomposite catalyst for CO oxidation, catalysis Letters, 2018-v.148, N12-3715-3722 pages, DOI:10.1007/s 10562-018-2539-5)), while producing a plasticized mass. The water content of the plasticised material was 80wt%. 20wt% ammonia was formed dropwise through the hydrocarbon liquid layer. The pellets were air dried for 24 hours, 110℃for 2 hours and 700℃for 1 hour. The catalyst prepared contained 3.0wt% of CuO, 50.0wt% of Fe 2 O 3 And 47.0% Al 2 O 3 。
The temperature at which 50% of the CO is converted is 215 ℃. The burnout of the residue was 98.1%.
Example 2. Similar to example 1.
The catalyst prepared contained 75.0wt% Fe 2 O 3 And 250% Al 2 O 3 。
The temperature at which 50% of the CO is converted is 225 ℃. The burnout of the residue was 97.5%.
Example 3. Similar to example 1.
The catalyst prepared contained 5.0wt% Mn 2 O 3 60.0wt% Fe 2 O 3 And 35.0% Al 2 O 3 。
The temperature at which 50% of the CO is converted is 230 ℃. The burnout of the residue was 98.5%.
Example 4. Similarly to example 1.
The catalyst prepared contained 4.5wt% Cr 2 O 3 60.0wt% Fe 2 O 3 And 35.5% Al 2 O 3 。
The temperature at which 50% of the CO is converted is 230 ℃. The burnout of the residue was 98.0%.
Example 5. Similar to example 1.
The catalyst prepared contained 4.0wt% Co 2 O 3 61.0wt% Fe 2 O 3 And 35.0% Al 2 O 3 。
The temperature at which 50% of the CO is converted is 200 ℃. The burnout of the residue was 98.9%.
Example 6. Similarly to example 1.
The catalyst prepared contained 4.0wt% Co 2 O 3 6.0wt% of CuO, 55.0wt% of Fe 2 O 3 And 35.0% Al 2 O 3 。
The temperature at which 50% of the CO is converted is 180 ℃. The burnout of the residue was 99.6%.
Example 7. Similarly to example 1.
The catalyst prepared contained 7.0wt% Mn 2 O 3 3.0wt% of CuO,52.0wt% of Fe 2 O 3 And 38.0% Al 2 O 3 。
The temperature at which 50% of the CO was converted was 185 ℃. The burnout of the residue was 99.3%.
The comparative properties of the deeply oxidized catalyst are shown in the table in fig. 6.
Industrial applicability
The invention can be realized by known means, using known materials, which, in this respect, prove to be in accordance with the claims of the patent "industrial availability".
Patent literature
Patent document 1: patent document RU2351847, publication date 2009, 04 month and 10 days
Patent document 2: patent document RU2568978, publication date 2015, 11, 20
Non-patent literature
Non-patent literature: experience in water-boiling boilers which can catalytically burn liquid and solid fuels in fluidized beds, authors: west Meng Nuofu a.d., ataxiv n.a., alf Liang Tunuo a.s., ferox i.a., jacob v.a., and paler Mo Fu v.n., journal: alternative energy and ecology, 2014, no. 19 (159), pages 70-85, publication date: 12 months 31 days 2014.

Claims (10)

1. The utility model provides a sewage sludge class fuel catalytic combustion device which characterized in that includes a catalytic reactor that is used for recycling sewage sludge, wherein the catalyst feed tube is located the upper portion of reactor casing, and hollow truncated cone-shaped gas-liquid separator is located the top cap that connects the flue gas pipeline below, and this gas-liquid separator is fixed on the reactor casing downwards through the base that the diameter is less simultaneously, and wherein the tip of four pyramid is fixed downwards, the diagonal of tip base is greater than the diameter of gas-liquid separator truncated cone little base, has consequently produced certain space between the base face of tip and gas-liquid separator truncated cone little base face; a gas distribution mechanism is arranged between a catalyst removal connecting pipe and an unburned sludge unloading area connected with a spiral unloader connecting pipe in the oxidation area at the lower part of the catalytic reactor shell, the gas distribution mechanism consists of two external distributing pipes which are positioned on the same plane and are parallel to each other at the two completely opposite walls of the reactor shell, and each distributing pipe is provided with a perforated circular section pipe below 3 pipe walls by a bent pipe; the catalytic reactor also comprises a blower and a heat generator connected in series with the catalytic reactor through an air supply pipeline, a heat returning device connected in series with the catalytic reactor through an exhaust pipeline, an economizer, a bag filter, a wet vortex dust filter, a high-pressure blower and a discharge flue, and a solid fuel supply system, namely a feed hopper with a spiral distributor, and an unburned sludge unloading hopper.
2. A method of catalytic combustion of a sewage sludge fuel, the method being effected by a sewage sludge fuel catalytic combustion apparatus according to claim 1, wherein the heat treatment is carried out in a fluidized bed in the presence of a CO deep oxidation catalyst; carrying out heat treatment by continuously supplying sewage sludge into a catalytic reactor heated to 750 ℃, and simultaneously feeding air required for maintaining the fluidization state of the catalyst, oxidizing sludge organic matters and forming CO in the reoxidation combustion process into the reactor; the flue gas enters a heat recovery device from a catalytic reactor, then enters an internal space of an economizer tube, enters a bag filter for purification after being cooled by water, and enters a wet vortex dust filter for simultaneously condensing vapor formed in the catalytic combustion process of sewage sludge and neutralizing acid gas contained in the flue gas.
3. A catalytic reactor for recovering sewage and sludge from sewage and sludge fuel catalytic combustion unit is composed of a vertical casing, a catalyst supplying pipe at the upper part of said casing, a sludge inlet pipe, a spiral coal feeding pipe, a catalyst discharging pipe, a soft tissue filler at the middle part of said casing, and a spiral discharger for unloading the unburned sewage and sludge. Unlike the prototype, the gas-liquid separator is located at the upper part of the reactor shell and below the top cover connected with the flue gas pipeline, the gas-liquid separator is in the shape of a hollow truncated cone, and is downwards fixed on the reactor shell through a base with smaller diameter, wherein the tip head of the quadrangular pyramid is downwards fixed, the diagonal line of the tip base is larger than the diameter of the truncated cone small base of the gas-liquid separator, and therefore a certain gap is formed between the base surface of the tip and the truncated cone small base surface of the gas-liquid separator; the catalytic reactor comprises a catalytic reactor shell, a catalytic reactor, a spiral unloader, a catalyst removal connecting pipe, a spiral unloader connecting pipe, a gas distribution mechanism and a gas distribution mechanism, wherein the gas distribution mechanism is arranged between the catalytic reactor shell lower part in an oxidation area and an unburned sludge unloading area connected with the spiral unloader connecting pipe, the gas distribution mechanism is composed of two external distribution pipes which are positioned on the same plane and are parallel to each other on two diametrically opposite walls of the catalytic reactor shell, and each distribution pipe is provided with a perforated circular section pipe below 3 pipe walls through a bent pipe.
4. A catalytic reactor according to claim 3, wherein the diameter of the larger diameter base of the gas-liquid separator is 40% larger than the diameter of the flue gas duct.
5. A catalytic reactor according to claim 3, comprising two diametrically opposed feed sludge connection pipes, each welded with a water connection pipe.
6. A catalytic reactor according to claim 3, wherein the total area of perforations in the tubes is 2.5% of the cross-sectional area of the lower portion of the reactor shell.
7. A catalytic reactor according to claim 3, wherein the reactor shell is welded with perforated circular cross-section tubes below the tube wall and the free welded end of each tube is inserted into a sleeve welded to the outside of the reactor shell on the side opposite the elbow, with all perforated tubes lying in a single plane and leaving a void between the tubes when installed and the perforated portion of the tubes being located inside the reactor shell.
8. A method for recycling sewage sludge, which is realized by the catalytic reactor capable of thermally treating catalyst dispersed particles in a fluidized bed according to claim 3, characterized in that the prototype device is a catalytic reactor for recycling sewage sludge in a sewage sludge-type fuel catalytic combustion device, burning wet sewage sludge in the presence of a catalyst, wherein the thermal treatment is performed by continuously feeding sludge to the catalytic reactor while feeding air required for maintaining the catalyst in a fluidized state into the catalytic reactor.
9. The method according to claim 8, wherein the heat treatment is performed by continuously feeding sludge into a catalytic reactor heated to 750 ℃.
10. The process of claim 8 wherein the catalyst comprises alumina Al 2 O 3 An oxidation support having a content of not more than 50wt%, fe 2 O 3 48 to 75wt%, cuO 0wt%, 2 to 3wt%, 3.5 to 6wt%, and/or Mn 2 O 3 And/or Co 2 O 3 And/or Cr 2 O 3 The content of active ingredient is 2-10wt%.
CN202180074224.5A 2020-11-08 2021-10-07 Sewage sludge fuel catalytic combustion device Pending CN116406346A (en)

Applications Claiming Priority (5)

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RU2020136581 2020-11-08
RU2020136580A RU2752476C1 (en) 2020-11-08 2020-11-08 Catalytic reactor for the disposal of sediments from municipal wastewater treatment plants and a method for disposal
RU2020136580 2020-11-08
RU2020136581A RU2749063C1 (en) 2020-11-08 2020-11-08 Installation for catalytic combustion of fuel in form of sewage sludge from municipal treatment plants and method for its combustion
PCT/RU2021/050330 WO2022098262A1 (en) 2020-11-08 2021-10-07 Plant for catalytic incineration of fuel in the form of sewage sludge

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CN115818911B (en) * 2023-02-24 2023-05-05 国能龙源环保有限公司 Sludge distributing device and fire coal conveying line
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RU2456248C1 (en) * 2010-12-23 2012-07-20 Учреждение Российской академии наук Институт катализа им. Г.К. Борескова Сибирского отделения РАН Catalytic reactor for treatment of eflluents sediments and method of their treatment (versions)
RU2568978C1 (en) * 2014-10-17 2015-11-20 Федеральное государственное бюджетное учреждение науки Институт катализа им. Г.К. Борескова Сибирского отделения Российской академии наук Method for catalytic treatment of sewage sludge

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