CN113231451A - Continuous supercritical/subcritical water oxidation solid-liquid mixture co-disposal system and process - Google Patents
Continuous supercritical/subcritical water oxidation solid-liquid mixture co-disposal system and process Download PDFInfo
- Publication number
- CN113231451A CN113231451A CN202110665377.9A CN202110665377A CN113231451A CN 113231451 A CN113231451 A CN 113231451A CN 202110665377 A CN202110665377 A CN 202110665377A CN 113231451 A CN113231451 A CN 113231451A
- Authority
- CN
- China
- Prior art keywords
- gas
- solid
- liquid
- heating
- storage tank
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 239000007788 liquid Substances 0.000 title claims abstract description 73
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 53
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 39
- 230000003647 oxidation Effects 0.000 title claims abstract description 36
- 239000000203 mixture Substances 0.000 title claims abstract description 20
- 238000000034 method Methods 0.000 title claims abstract description 19
- 230000008569 process Effects 0.000 title claims abstract description 17
- 238000006243 chemical reaction Methods 0.000 claims abstract description 91
- 239000000463 material Substances 0.000 claims abstract description 55
- 239000007789 gas Substances 0.000 claims abstract description 45
- 239000007787 solid Substances 0.000 claims abstract description 41
- 238000003756 stirring Methods 0.000 claims abstract description 35
- 239000010881 fly ash Substances 0.000 claims abstract description 33
- 238000010438 heat treatment Methods 0.000 claims abstract description 28
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 27
- 239000001301 oxygen Substances 0.000 claims abstract description 27
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 27
- 238000002156 mixing Methods 0.000 claims abstract description 20
- 239000010813 municipal solid waste Substances 0.000 claims abstract description 15
- 239000000149 chemical water pollutant Substances 0.000 claims abstract description 13
- 238000000926 separation method Methods 0.000 claims abstract description 9
- 238000001816 cooling Methods 0.000 claims abstract description 5
- 238000001556 precipitation Methods 0.000 claims abstract description 4
- 238000005516 engineering process Methods 0.000 claims description 11
- 238000002347 injection Methods 0.000 claims description 11
- 239000007924 injection Substances 0.000 claims description 11
- 238000012545 processing Methods 0.000 claims description 8
- 238000004321 preservation Methods 0.000 claims description 5
- 238000005485 electric heating Methods 0.000 claims description 4
- 238000011278 co-treatment Methods 0.000 claims 3
- 230000007613 environmental effect Effects 0.000 abstract description 3
- 229910001385 heavy metal Inorganic materials 0.000 description 9
- 239000000843 powder Substances 0.000 description 9
- 238000004056 waste incineration Methods 0.000 description 8
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 6
- 230000008901 benefit Effects 0.000 description 6
- 239000002956 ash Substances 0.000 description 4
- 230000004048 modification Effects 0.000 description 4
- 238000012986 modification Methods 0.000 description 4
- 230000009471 action Effects 0.000 description 3
- 239000003921 oil Substances 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 238000007711 solidification Methods 0.000 description 3
- 230000008023 solidification Effects 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 2
- 230000008595 infiltration Effects 0.000 description 2
- 238000001764 infiltration Methods 0.000 description 2
- 238000002386 leaching Methods 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 150000003254 radicals Chemical class 0.000 description 2
- 230000002195 synergetic effect Effects 0.000 description 2
- 230000001988 toxicity Effects 0.000 description 2
- 231100000419 toxicity Toxicity 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000011038 discontinuous diafiltration by volume reduction Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 229910052736 halogen Inorganic materials 0.000 description 1
- 150000002367 halogens Chemical class 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000010169 landfilling Methods 0.000 description 1
- 229910052745 lead Inorganic materials 0.000 description 1
- 229910052748 manganese Inorganic materials 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000012454 non-polar solvent Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 238000006864 oxidative decomposition reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 150000005837 radical ions Chemical class 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052723 transition metal Inorganic materials 0.000 description 1
- 150000003624 transition metals Chemical class 0.000 description 1
- 229910052720 vanadium Inorganic materials 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B2101/00—Type of solid waste
- B09B2101/30—Incineration ashes
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention belongs to the technical field of environmental protection and resource comprehensive utilization, and provides a continuous supercritical/subcritical water oxidation solid-liquid mixture cooperative disposal system and a process, wherein the process comprises the following steps: stirring and mixing the garbage percolate and the incineration fly ash according to a set liquid-solid ratio to obtain a uniformly mixed material; carrying out high-temperature and high-pressure heating oxidation treatment on the uniformly mixed material under oxygen to obtain gaseous discharge and solid-liquid mixed discharge; and carrying out precipitation collection on the solid-liquid mixed state discharge material, sequentially carrying out gas-solid separation, cooling and gas-liquid separation on the gas state discharge material, and carrying out corresponding product classification collection. The system comprises a stirring container, a reaction unit, a gas-solid separator, a cooler, a gas-liquid separator and a gas storage tank, wherein the stirring container is used for stirring and mixing the garbage leachate and the incineration fly ash, the reaction unit is respectively connected with the stirring container, the gas-solid separator and the gas storage tank, and the cooler and the gas-liquid separator are sequentially connected behind the gas-solid separator. The process and the system can cooperatively treat the landfill leachate and the incineration fly ash.
Description
Technical Field
The invention belongs to the technical field of environmental protection and resource comprehensive utilization, and particularly relates to a continuous supercritical/subcritical water oxidation solid-liquid mixture cooperative treatment system and process, which are used for realizing the cooperative treatment of garbage leachate and incineration fly ash and are also suitable for continuously and cooperatively treating waste liquid with high organic matter content and solid waste containing heavy metal and dioxin.
Background
The garbage incineration power generation technology can realize reduction, recycling and harmless treatment and disposal of domestic garbage, and through development of more than 100 years, the treatment process and technology thereof become mature day by day and become a main method for global garbage treatment. However, the harmless treatment and disposal of the landfill leachate and incineration fly ash generated in the process of waste incineration power generation are common and bottleneck problems restricting the development of the industry.
The landfill leachate is high-concentration organic wastewater with complex components, has strong odor, has the characteristics of high COD (chemical oxygen demand), high ammonia nitrogen and heavy metal contents, complex water quality, large change, high harmfulness and the like, needs to be deeply treated, and otherwise can cause serious pollution to the environment. The leachate treatment process and the leachate treatment method commonly used in the waste incineration industry can generate about 15-30% of concentrated solution, and the concentrated solution is mainly treated by back spraying to the incinerator, so that the heat energy utilization efficiency of the incinerator is reduced, the yield of polluted gas is increased, meanwhile, the furnace body of the incinerator is corroded, and the service life of the incinerator is seriously influenced.
The waste incineration fly ash is mainly residue collected in a waste incineration flue gas purification system, and accounts for about 2-5% of the total amount of waste incineration ash. The incineration fly ash contains a large amount of soluble heavy metals and dioxin, belongs to hazardous waste, and easily causes secondary pollution to the environment if proper treatment and disposal are not carried out. At present, the fly ash from waste incineration is mainly landfilled after solidification/stabilization treatment, the treatment cost is low, but the resource utilization of the fly ash cannot be realized by solidification landfilling, and the volume reduction rate are low, so that the storage capacity of an urban landfill site is occupied. Therefore, dioxin in the incineration fly ash is thoroughly removed, soluble heavy metals in the incineration fly ash are stably solidified, and harmless treatment and resource utilization of the incineration fly ash are imperative.
Research shows that under the conditions of high temperature and high pressure (300-400 ℃, 8-23 Mpa), the density, dielectric constant and the like of water can be obviously changed, the water becomes a nonpolar solvent, the solubility of organic matters and oxygen in the water is greatly increased, even the organic matters and the oxygen are completely mixed to form a homogeneous phase, and an oxidant can be subjected to a strong oxidation reaction with the organic matters, so that the organic matters are rapidly and deeply degraded into harmless inorganic matters, and hydrocarbon is oxidized into CO2And H2O, nitrogen element is oxidized into N2Sulfur, halogen and the like are precipitated and separated out as inorganic salts of acid radical ions. Compared with the traditional treatment process, the high-temperature and high-pressure water oxidation treatment technology is in the subcritical and supercritical states of water, and has the characteristics of thorough treatment, short reaction time, no secondary pollution, high controllability and the like.
Therefore, the supercritical (subcritical) water oxidation technology is applied to the waste incineration industry, and the synergistic treatment of the waste leachate and the incineration fly ash has obvious environmental protection benefits. However, most inorganic salts in the reaction materials are separated out under the high-temperature and high-pressure state of water, which easily causes equipment blockage, and when the reaction materials are solid-liquid mixtures, the blockage and discharge problems of solid powder and inorganic salts are more prominent, thereby being difficult to realize continuous reaction of the system and further limiting the popularization and application of the high-temperature and high-pressure water oxidation technology.
Disclosure of Invention
In view of the above, the present invention aims to provide a continuously operable process and system for co-treating a solid-liquid mixture by supercritical (sub) critical water oxidation, which utilizes the interaction between leachate and incineration fly ash to realize harmless treatment of two pollutants.
The invention is realized by the following technical scheme:
the invention provides a continuous supercritical/subcritical water oxidation solid-liquid mixture co-processing technology, which comprises the following steps: stirring and mixing the garbage percolate and the incineration fly ash according to a set liquid-solid ratio to obtain a uniformly mixed material; carrying out high-temperature and high-pressure heating oxidation treatment on the uniformly mixed material under oxygen to obtain gaseous discharge and solid-liquid mixed discharge; and carrying out precipitation collection on the solid-liquid mixed state discharge material, and carrying out gas-solid separation, cooling, gas-liquid separation and corresponding product classification collection on the gas-state discharge material in sequence.
Preferably, the liquid-solid ratio of the landfill leachate to the incineration fly ash is set to be 4: 1-10: 1, mL/g; setting the temperature of the heating oxidation treatment of the uniformly mixed material under oxygen to be 300-400 ℃, the pressure to be 8-23 Mpa, and determining the liquid-solid ratio, the temperature and the pressure according to the characteristics of the reaction materials.
Preferably, the preheating treatment is carried out on the uniformly mixed material and oxygen before the heating oxidation treatment, and the preheating treatment on the uniformly mixed material is as follows: the electric heating or oil heating can be utilized, and the hot water discharged by a power plant can also be utilized for direct mixed heating or indirect heat exchange.
Preferably, the heating and oxidation treatment of the uniformly mixed materials under oxygen comprises the following steps: heating is carried out by using an electric heating device or an oil heating device.
Preferably, the treated blending material and oxygen are continuously fed.
The invention also provides a continuous supercritical/subcritical water oxidation solid-liquid mixture cooperative treatment system for realizing the process, which comprises a stirring container, a reaction unit, a gas-solid separator, a cooler, a gas-liquid separator and a gas storage tank, wherein the stirring container is used for stirring and mixing the garbage leachate and the incineration fly ash, the reaction unit is respectively connected with the stirring container, the gas-solid separator and the gas storage tank, and the cooler and the gas-liquid separator are sequentially connected behind the gas-solid separator.
Furthermore, the stirring container is also connected with a water storage tank through a liquid injection pump, and a piston for isolating water from the water storage tank is arranged in the stirring container.
Further, the reaction unit comprises a reaction kettle A, a reaction kettle B, a reaction kettle C and a settling kettle which are sequentially communicated from top to bottom, the stirring container is connected between the reaction kettle A and the reaction kettle B, the gas storage tank is respectively connected with the reaction kettle A, the reaction kettle B and the reaction kettle C, the outer wall of each reaction kettle is provided with a heating device with a heat preservation outer layer, and the settling kettle and the outer wall of a pipeline of the settling kettle are both provided with heat preservation layers.
Furthermore, a back pressure valve is arranged on a pipeline between the cooler and the gas-liquid separator, and a gas flowmeter and an air pressure pump are arranged on the gas storage tank.
Further, a preheater A is arranged on a pipeline between the stirring container and the reaction unit, and a preheater B is arranged on a pipeline between the gas storage tank and the reaction unit.
The invention has the advantages that: the process and the system are based on the water oxidation technology under the high-temperature and high-pressure state, fully utilize the synergistic effect of the garbage leachate and the incineration fly ash, realize the harmless treatment of the garbage leachate and the incineration fly ash, and lay a foundation for further resource utilization; meanwhile, the liquid discharged by the system contains a small amount of COD and a certain amount of ammonia nitrogen, and can reach the discharge standard after biochemical treatment without generating concentrated liquid; the gas is discharged after reaching the standard, no pollution is generated, and the solid residue can be recycled. The invention has important promotion function for solving the difficulties and pain points in the waste incineration industry.
Additional advantages, objects, and features of the invention will be set forth in part in the description which follows and in part will become apparent to those having ordinary skill in the art upon examination of the following or may be learned from practice of the invention. The objectives and other advantages of the invention may be realized and attained by the means of the instrumentalities and combinations particularly pointed out hereinafter.
Drawings
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be further described in detail with reference to the accompanying drawings, in which:
FIG. 1 is a schematic diagram of the present system;
FIG. 2 is a process flow diagram of the present system;
reference numerals: 1. the system comprises a water storage tank, 2 liquid injection pumps, 3 stirring containers, 4 preheaters A, 5 reaction kettles A, 6 reaction kettles B, 7 reaction kettles C, 8 settling kettles, 9 gas-solid separators, 10 coolers, 11 back pressure valves, 12 gas-liquid separators, 13 preheaters B, 14 gas flow meters, 15 gas storage tanks and 16 air pressure pumps.
Detailed Description
The embodiments of the present invention are described below with reference to specific embodiments, and other advantages and effects of the present invention will be easily understood by those skilled in the art from the disclosure of the present specification. The invention is capable of other and different embodiments and of being practiced or of being carried out in various ways, and its several details are capable of modification in various respects, all without departing from the spirit and scope of the present invention. It should be noted that the drawings provided in the following embodiments are only for illustrating the basic idea of the present invention in a schematic way, and the features in the following embodiments and examples may be combined with each other without conflict.
As shown in fig. 1, the continuous supercritical/subcritical water oxidation solid-liquid mixture cooperative disposal system provided in this embodiment includes a stirring container 3, a reaction unit, a gas-solid separator 9, a cooler 10, a gas-liquid separator 12 and a gas storage tank 15, wherein the stirring container 3 is used for stirring and mixing a certain proportion of landfill leachate and incineration fly ash, so that the leachate and the fly ash are fully mixed to form a uniformly mixed material; the reaction unit is respectively connected with the stirring container 3, the gas-solid separator 9 and the gas storage tank 15, and is used for receiving the uniformly mixed material supplied by the stirring container 3 and the industrial oxygen supplied by the gas storage tank 15, reacting the uniformly mixed material and the industrial oxygen under the condition of high-pressure and high-temperature water oxidation to obtain gaseous discharge and solid-liquid mixed discharge, and receiving the gaseous discharge discharged by the reaction unit through the gas-solid separator 9; and the gas-solid separator 9 is connected with a cooler 10 and a gas-liquid separator 12 in sequence to separate and collect or discharge gas, solid and liquid in the gas discharge.
The incineration fly ash contains heavy metals and dioxin, the garbage infiltration contains a large amount of organic matters, oxides of transition metals such as V, Mn, Cu, Cr, Fe, Ni and the like in the incineration fly ash can be used as active components in an environment with sufficient oxygen at the temperature range of 300-400 ℃ and the pressure range of 8-23 MPa, a large amount of hydroxyl free radicals are generated, the strong oxidation effect of the hydroxyl free radicals can obviously promote the oxidative decomposition of the organic matters in the uniformly mixed materials, and the removal efficiency of the organic matters and the dioxin in the uniformly mixed materials is effectively improved. Meanwhile, the exchange state and carbonate combined state heavy metal ions (Zn, Pb and the like) which are very easy to leach out from the fly ash can be effectively fixed in mineral crystal lattices such as silicon, calcium and the like in the severe oxidation reaction process of the organic matters of the landfill leachate, so that the leaching toxicity of the heavy metals is greatly reduced. Therefore, the removal of organic matters in the landfill leachate and the solidification of heavy metals in the incineration fly ash are mutually promoted and associated, and finally, liquid with lower COD content, residues which can be recycled and harmless gas are formed.
The stirring container 3 in this embodiment is further connected with a water storage tank 1 through a liquid injection pump 2, and a piston (not marked) for isolating water from the water storage tank 1 is arranged in the stirring container 3, and clear water in the water storage tank 1 is injected into the stirring container 3 through the liquid injection pump 2 to push the piston in the stirring container 3 to move, so that the uniformly mixed material below the piston is pressed into the reaction unit to participate in the high-temperature water oxidation reaction. Because the flying ash is insoluble in filtration liquid, use liquid injection pump 2 can cause the equipment to block up, simultaneously, the mixing material of flying ash and filtration liquid will stratify after standing, in order to make the mixing material inject reaction system in succession, this patent proposes to use the clear water to promote the design of infiltration liquid and flying ash mixing material in the stirred vessel to realize the injection of mixing material, and liquid injection pump 2 has the measurement function, and can directly reflect the volume of impressing of mixing material.
The reaction unit in this embodiment is composed of a reaction kettle A5, a reaction kettle B6, a reaction kettle C7 and a settling kettle 8 which are sequentially communicated from top to bottom, a stirring container 3 is connected between the reaction kettle A5 and the reaction kettle B6, and a gas storage tank 15 is respectively connected with the reaction kettle A5, the reaction kettle B6 and the reaction kettle C7. Thus, the reaction unit is of a three-section reaction kettle and settling kettle structure. The three-stage formula reation kettle includes: a reaction kettle A5, a reaction kettle B6 and a reaction kettle C7, wherein the three reaction kettles are communicated. The reason for setting up syllogic reation kettle is in improving the dwell time of material in the cauldron, makes the material fully react. Each section of reaction kettle is provided with an oxygen filling opening, and oxygen is fully contacted with materials. The mixed material of solid and liquid is injected between the reactor A5 and the reactor B6, part of the liquid is changed into gas at high temperature, and the gas reacts mainly in the reactor A5, and part of the liquid and solid powder which are not gasified react mainly in the reactor B6 and the reactor C7 under the influence of gravity. And reaction kettle C7 is communicated with settling kettle 8, and the solid powder generated in reaction kettle C7 and a small amount of unevaporated liquid enter settling kettle 8 and further settle under the action of gravity. And the gas in the reaction unit flows out from a discharge port above the reaction kettle A5 to enter subsequent cooling and separation. In the high-temperature high-pressure reaction process, most of liquid is evaporated into a gaseous state, so that solid powder in reaction materials and reaction products is separated out, and the solid powder is increased along with the reaction, so that the problem of blockage of a reaction system, particularly a pipeline, is caused, and the continuous reaction is influenced. This system is through setting up settling tank 8, collects solid powder, reduces the pipeline and blocks up, guarantees going on in succession of reaction.
The gas tank 15 in this embodiment is provided with a gas flow meter 14 and an air pressure pump 16. Before the reaction, an air pressure pump 16 is used for pressing oxygen into a closed gas storage tank 15, so that the pressure in the gas storage tank 15 is higher than that in the reaction unit, the oxygen is conveniently injected into the reaction system, and a gas flow meter 14 is used for controlling the flow of the oxygen.
In this embodiment, a preheater a4 is provided in the piping between the agitation vessel 3 and the reaction unit, and a preheater B13 is provided in the piping between the gas holder 15 and the reaction unit. So that the uniformly mixed material and oxygen entering the reaction unit can be preheated, the oxidation efficiency of the reaction unit is improved, and the continuous and rapid reaction of the material in the reaction kettle is ensured.
In this embodiment, the gaseous discharge discharged from the reaction unit may contain a small amount of solid powder, the gaseous discharge discharged from the reaction vessel a5 first enters the gas-solid separator 9, the solid powder is intercepted by the filter screen, and the gaseous discharge continues to enter the cooler 10 to cool the high-temperature and high-pressure gas after the reaction. The cooled gaseous discharge enters a back pressure valve 11, the pressure of the discharged gas is reduced, the gas enters a gas-liquid separator 12 provided with a cooler, the water vapor is changed into liquid water and is discharged into a liquid collecting tank, and the non-condensable gas is discharged into a gas collecting bag. A back pressure valve 11 is arranged on a pipeline between the cooler 10 and the gas-liquid separator 12, the back pressure valve is mainly used for stabilizing and controlling the pressure in the reaction system, and a gas-solid separator 9 and the cooler 10 are arranged in front of the back pressure valve 11 and are mainly used for protecting the back pressure valve 11.
In addition, the material injection pipeline (mixing material and oxygen) of the system is provided with a one-way valve to ensure that the material does not flow back, and simultaneously, the system is also provided with a safety valve for overpressure protection. The reaction pressure of the whole system is controlled by a back pressure valve 11, the liquid injection pump has the functions of pressurization and metering, and the oxygen flow is controlled by a gas flowmeter 14, so that materials can enter the reaction unit according to the set pressure and the set flow. And the outer sides of the preheater and each reaction kettle are respectively provided with a heating device and a heat preservation device, the heating devices adopt electric heating devices or oil heating devices for heating, the preheating temperature of the preheater is determined by the reaction temperature and the residence time of materials, and the outer wall of the pipeline is respectively provided with a heat preservation layer.
As shown in fig. 2, the reaction materials of the continuous supercritical/subcritical water oxidation solid-liquid mixture co-processing technology include garbage leachate, incineration fly ash and oxygen, and the garbage leachate and the incineration fly ash are stirred and mixed in a stirring container 3 according to a set liquid-solid ratio of 4: 1-10: 1(mL/g) to obtain a uniform mixing material; then the mixed material is quantitatively injected into the reaction kettle through a water storage tank 1 and a liquid injection pump 2, and continuous high-pressure high-temperature heating oxidation treatment is carried out in the reaction kettle under the action of oxygen supplied by a gas storage tank 15 to obtain gas discharge and solid-liquid mixed discharge; then, the solid-liquid mixed state discharge material is precipitated and collected through a precipitation kettle 8, the gas state discharge material is sequentially subjected to gas-solid separation of a gas-solid separator 9, cooling action of a cooler 10 and gas-liquid separation of a gas-liquid separator 12 to obtain liquid, gas and solid products, and finally, corresponding product classification collection or discharge is carried out.
In a specific embodiment, the landfill leachate and the incineration fly ash are both from a domestic garbage incineration plant, and the incinerator is a grate furnace. The COD of the landfill leachate is 65000mg/L, the solid-to-liquid ratio of the landfill leachate to the incineration fly ash is 6:1(mL/g) at the reaction temperature of 350 ℃ and under the pressure of 16MPa, the preheating temperature is 300 ℃, and the reaction residence time is 30 min. The detection result of the reacted solid powder shows that the heavy metal leaching toxicity and the dioxin both reach the relevant standard (GB8978 standard).
In another embodiment, the pre-heating treatment of the blending material can be performed by directly mixing and heating with hot water discharged from a power plant. For example, primary or secondary hot water discharged by a waste heat boiler of a power plant, or waste hot water and the like participate in mixing the landfill leachate and the incineration fly ash, and the preheating purpose can also be realized.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and it is apparent that those skilled in the art can make various changes and modifications to the present invention without departing from the spirit and scope of the present invention. Thus, if such modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is also intended to include such modifications and variations.
Claims (10)
1. The continuous supercritical/subcritical water oxidation solid-liquid mixture co-treatment process is characterized by comprising the following steps:
stirring and mixing the garbage percolate and the incineration fly ash according to a set liquid-solid ratio to obtain a uniformly mixed material;
carrying out high-temperature and high-pressure heating oxidation treatment on the uniformly mixed material under oxygen to obtain gaseous discharge and solid-liquid mixed discharge;
carrying out precipitation collection on the solid-liquid mixed state discharge material; and sequentially carrying out gas-solid separation, cooling and gas-liquid separation on the gaseous discharge materials, and carrying out corresponding product classification and collection.
2. The continuous supercritical/subcritical water oxidation solid-liquid mixture co-treatment process according to claim 1, wherein the liquid-solid ratio of landfill leachate to incineration fly ash is set to be 4: 1-10: 1, mL/g; setting the temperature of the heating oxidation treatment of the uniformly mixed material under oxygen to be 300-400 ℃, the pressure to be 8-23 Mpa, and determining the liquid-solid ratio, the temperature and the pressure according to the characteristics of the reaction materials.
3. The continuous supercritical/subcritical water oxidation solid-liquid mixture co-processing technology according to claim 1, characterized in that the pre-heating treatment is performed on the blending material and oxygen before the heating oxidation treatment, and the pre-heating treatment on the blending material is as follows: the electric heating or the oil heating is utilized, or the hot water source discharged by a power plant is utilized for direct mixed heating or indirect heat exchange.
4. The continuous supercritical/subcritical water oxidation solid-liquid mixture co-processing technology according to claim 1, characterized in that the heating and oxidation treatment of the uniformly mixed materials under oxygen is as follows: heating is carried out by an electric or oil heating device.
5. The continuous supercritical/subcritical water oxidation solid-liquid mixture co-processing technology according to claim 1, characterized in that a continuous feeding mode is adopted for the treated uniformly mixed material and oxygen.
6. The continuous supercritical/subcritical water oxidation solid-liquid mixture co-treatment system is characterized by comprising a stirring container (3), a reaction unit, a gas-solid separator (9), a cooler (10), a gas-liquid separator (12) and a gas storage tank (14), wherein the stirring container is used for stirring and mixing landfill leachate and incineration fly ash, the reaction unit is respectively connected with the stirring container, the gas-solid separator and the gas storage tank, and the cooler and the gas-liquid separator are sequentially connected behind the gas-solid separator.
7. The continuous supercritical/subcritical water oxidation solid-liquid mixture co-processing system according to claim 6, wherein the stirring container is further connected with a water storage tank (1) through a liquid injection pump (2), and a piston for isolating water from the water storage tank is arranged in the stirring container.
8. The continuous supercritical/subcritical water oxidation solid-liquid mixture coprocessing system according to claim 6, characterized in that the reaction unit consists of a reaction kettle A (5), a reaction kettle B (6), a reaction kettle C (7) and a settling kettle (8) which are sequentially communicated from top to bottom, the stirring vessel is connected between the reaction kettle A and the reaction kettle B, the gas storage tank is respectively connected with the reaction kettle A, the reaction kettle B and the reaction kettle C, and the outer wall of each reaction kettle is provided with a heating device with a heat preservation outer layer.
9. The continuous supercritical/subcritical water oxidation solid-liquid mixture co-processing system according to claim 6, wherein a back pressure valve (11) is arranged on a pipeline between the cooler and the gas-liquid separator, and a gas flowmeter (14) and an air pressure pump (15) are arranged on the gas storage tank.
10. The continuous supercritical/subcritical water oxidation solid-liquid mixture co-processing system according to claim 6, wherein a preheater A (4) is arranged on a pipeline between the stirring container and the reaction unit, and a preheater B (13) is arranged on a pipeline between the gas storage tank and the reaction unit.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110665377.9A CN113231451B (en) | 2021-06-16 | 2021-06-16 | Continuous supercritical/subcritical water oxidation solid-liquid mixture co-treatment system and process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110665377.9A CN113231451B (en) | 2021-06-16 | 2021-06-16 | Continuous supercritical/subcritical water oxidation solid-liquid mixture co-treatment system and process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN113231451A true CN113231451A (en) | 2021-08-10 |
| CN113231451B CN113231451B (en) | 2023-10-17 |
Family
ID=77140013
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110665377.9A Active CN113231451B (en) | 2021-06-16 | 2021-06-16 | Continuous supercritical/subcritical water oxidation solid-liquid mixture co-treatment system and process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113231451B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115555376A (en) * | 2022-10-20 | 2023-01-03 | 镇江新区固废处置股份有限公司 | Resource treatment equipment and process for incineration waste fly ash |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20060022743A (en) * | 2004-09-07 | 2006-03-13 | 한화석유화학 주식회사 | The process for oxidative decomposition of wastewater containing organic material by supercritical conditions |
| CN206494787U (en) * | 2016-08-31 | 2017-09-15 | 北京首创北科环境科技研究院有限公司 | A kind of coprocessing system of incineration of refuse flyash and percolate |
| CN110937731A (en) * | 2019-11-01 | 2020-03-31 | 浙江大学 | Method for co-processing garbage percolate/concentrated solution and household garbage incineration fly ash |
-
2021
- 2021-06-16 CN CN202110665377.9A patent/CN113231451B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20060022743A (en) * | 2004-09-07 | 2006-03-13 | 한화석유화학 주식회사 | The process for oxidative decomposition of wastewater containing organic material by supercritical conditions |
| CN206494787U (en) * | 2016-08-31 | 2017-09-15 | 北京首创北科环境科技研究院有限公司 | A kind of coprocessing system of incineration of refuse flyash and percolate |
| CN110937731A (en) * | 2019-11-01 | 2020-03-31 | 浙江大学 | Method for co-processing garbage percolate/concentrated solution and household garbage incineration fly ash |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115555376A (en) * | 2022-10-20 | 2023-01-03 | 镇江新区固废处置股份有限公司 | Resource treatment equipment and process for incineration waste fly ash |
Also Published As
| Publication number | Publication date |
|---|---|
| CN113231451B (en) | 2023-10-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103880242B (en) | A kind of coal chemical industrial waste water advanced treatment process | |
| KR100914150B1 (en) | Method and system for the recycling of municipal solid wastes, and exploitation of the Wasted Solid Recovery Fuel | |
| CN106630526B (en) | Sludge hydro-thermal oxidation reaction system and method with product backflow pretreatment | |
| EP2534105A1 (en) | Compact wastewater concentrator and contaminant scrubber | |
| WO2010118103A1 (en) | Method for converting organic material into a renewable fuel | |
| CN113172081B (en) | Waste incineration fly ash recycling treatment process and system | |
| CN206607136U (en) | A kind of sludge water thermal oxidative reaction system for pretreatment of being backflowed with product | |
| CN105254146A (en) | Supercritical water oxidation treatment system and technology for dyeing sludge | |
| CN111100719A (en) | Preparation method of water-washed fly ash derived fuel | |
| CN112875838A (en) | Supercritical oxidation wastewater treatment method | |
| CN104759462B (en) | A kind of Soil leaching upgrading prosthetic device with tail gas treating function | |
| CN108840544A (en) | A kind of reclaiming industrial sludge processing method | |
| CN101690934A (en) | Method for stabilizing fly ash from refuse incineration by combination of complementary type medicaments | |
| CN116689445A (en) | System and method for detoxication of waste incineration fly ash | |
| CN114229800B (en) | Harmless and recycling method for gasification and high-temperature melting of full-industrial organic hazardous waste | |
| CN113231451B (en) | Continuous supercritical/subcritical water oxidation solid-liquid mixture co-treatment system and process | |
| CN110451752A (en) | The integrated conduct method and device of a kind of self-heating sludge and salkali waste waste liquid | |
| ITCR20100004A1 (en) | PLANT FOR THE TREATMENT OF BIOLOGICAL SLUDGE WITH RECOVERY OF RAW MATERIALS SECOND AND ENERGY | |
| KR101549959B1 (en) | System and method for processing wast liquid using supercritical water | |
| CN215143307U (en) | Continuous supercritical/subcritical water oxidation solid-liquid mixture co-processing system | |
| CN101734776B (en) | Method for processing and utilizing wastewater and waste material in steel production and processing system thereof | |
| CN111524633B (en) | Volume reduction treatment method for radioactive organic waste | |
| CN101280205B (en) | Recovery processing and comprehensive utilization process for oily sediment | |
| CN109809553B (en) | Supercritical water oxidation treatment continuous experimental system for high-solid organic waste liquid | |
| CN208604069U (en) | A kind of useless organic matter comprehensive utilization processing system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |