CN116376603A - Micro-oxygen pyrolysis process of rotary pyrolysis reactor - Google Patents
Micro-oxygen pyrolysis process of rotary pyrolysis reactor Download PDFInfo
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- CN116376603A CN116376603A CN202310286712.3A CN202310286712A CN116376603A CN 116376603 A CN116376603 A CN 116376603A CN 202310286712 A CN202310286712 A CN 202310286712A CN 116376603 A CN116376603 A CN 116376603A
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 231
- 239000001301 oxygen Substances 0.000 title claims abstract description 56
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 56
- 238000000034 method Methods 0.000 title claims abstract description 42
- 239000007789 gas Substances 0.000 claims abstract description 80
- 239000000463 material Substances 0.000 claims abstract description 70
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 42
- 239000002910 solid waste Substances 0.000 claims abstract description 15
- 238000002156 mixing Methods 0.000 claims abstract description 9
- 238000001035 drying Methods 0.000 claims abstract description 8
- 239000010813 municipal solid waste Substances 0.000 claims abstract description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 33
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 24
- 239000010802 sludge Substances 0.000 claims description 19
- 229910052757 nitrogen Inorganic materials 0.000 claims description 12
- 239000004033 plastic Substances 0.000 claims description 11
- 229920003023 plastic Polymers 0.000 claims description 11
- 239000003973 paint Substances 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims description 7
- 238000005406 washing Methods 0.000 claims description 7
- 238000006243 chemical reaction Methods 0.000 abstract description 13
- 238000004519 manufacturing process Methods 0.000 abstract description 8
- 238000007254 oxidation reaction Methods 0.000 abstract description 8
- 239000002699 waste material Substances 0.000 abstract description 8
- 238000009833 condensation Methods 0.000 abstract description 4
- 230000005494 condensation Effects 0.000 abstract description 4
- 238000004140 cleaning Methods 0.000 abstract description 2
- 238000005516 engineering process Methods 0.000 abstract description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 12
- 239000003921 oil Substances 0.000 description 8
- 238000010438 heat treatment Methods 0.000 description 7
- 230000000052 comparative effect Effects 0.000 description 6
- 239000003345 natural gas Substances 0.000 description 6
- 238000002485 combustion reaction Methods 0.000 description 5
- 238000004880 explosion Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 238000004458 analytical method Methods 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 239000000295 fuel oil Substances 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- RNFJDJUURJAICM-UHFFFAOYSA-N 2,2,4,4,6,6-hexaphenoxy-1,3,5-triaza-2$l^{5},4$l^{5},6$l^{5}-triphosphacyclohexa-1,3,5-triene Chemical compound N=1P(OC=2C=CC=CC=2)(OC=2C=CC=CC=2)=NP(OC=2C=CC=CC=2)(OC=2C=CC=CC=2)=NP=1(OC=1C=CC=CC=1)OC1=CC=CC=C1 RNFJDJUURJAICM-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- -1 alkane olefin Chemical class 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000002354 daily effect Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 230000003203 everyday effect Effects 0.000 description 1
- 239000003063 flame retardant Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 239000010806 kitchen waste Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000010902 straw Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0956—Air or oxygen enriched air
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing
Abstract
The application relates to a rotary pyrolysis reactor micro-oxygen pyrolysis process, which relates to the field of waste pyrolysis treatment technology, and comprises the following steps: s1, primarily drying and crushing solid waste; s2, mixing and matching the crushed solid waste with other garbage to prepare a pyrolysis material; s3, throwing the pyrolyzed material into a rotary pyrolysis reactor, and introducing air with the oxygen content of 4.5-8% (v/v) for pyrolysis. According to the method, pyrolysis reaction is carried out in a micro-oxygen environment by introducing a small amount of oxygen, macromolecular organic gas in pyrolysis gas and oxygen are subjected to oxidation reaction, so that macromolecular organic gas components are subjected to oxidation reaction to generate micromolecular gas components, the content of tar gas in the pyrolysis gas is further reduced, condensation of the pyrolysis gas in a pipeline in the process of outward conveying can be effectively reduced, the frequency of cleaning and replacement of the pipeline is reduced, and the production efficiency is improved.
Description
Technical Field
The application relates to the field of waste pyrolysis treatment technology, in particular to a rotary pyrolysis reactor micro-oxygen pyrolysis process.
Background
The pyrolysis method of solid waste is a process of utilizing the thermal instability of organic matters in the garbage, heating and distilling the garbage under the anaerobic or anoxic condition to crack the organic matters, condensing the organic matters to form various new gases, liquids and solids, and extracting fuel oil and combustible gas from the fuel oil and the solids. The pyrolysis-treated waste mainly comprises municipal solid waste, sludge, waste plastics, waste rubber and the like. The pyrolysis process of the rotary pyrolysis reactor generally adopts an anaerobic pyrolysis process, external indirect heating is adopted during heating, and heat transfer is utilized to enable materials in the pyrolysis reactor to fully absorb heat and crack at high temperature, so that continuous heating is required during the reaction process, and the necessary pyrolysis temperature is maintained.
Because the pyrolysis feeding source of solid waste is complicated, besides small-molecular hydrocarbons and CO, the pyrolysis gas also contains more tar gas and carries more ash, when the temperature of the part of gas is reduced in the conveying process, the tar gas can be quickly condensed and then is condensed in a pyrolyzer pipeline, the pipeline is seriously blocked due to continuous tar gas accumulation, the pipeline needs to be frequently cleaned or replaced, the continuous operation time of the pyrolysis reactor is short, the production cost is obviously overhigh, and the production efficiency is seriously influenced.
Disclosure of Invention
To above-mentioned technical problem, this application provides a little oxygen pyrolysis process of rotary pyrolysis reactor to reduce the pipeline that tar gas piled up the production in the solid waste pyrolysis process and stop up, promote solid waste pyrolysis efficiency.
In a first aspect, the present application provides a micro-aerobic pyrolysis process of a rotary pyrolysis reactor, which adopts the following technical scheme: a rotary pyrolysis reactor micro-oxygen pyrolysis process, comprising the following steps:
s1, primarily drying and crushing solid waste;
s2, mixing and matching the crushed solid waste with other garbage to prepare a pyrolysis material;
s3, putting the pyrolysis material into a rotary pyrolysis reactor, and introducing air with the oxygen content of 4.5-8% (v/v) for pyrolysis;
s4, washing the pyrolysis gas to remove tar gas and ash, and then separating steam to obtain the purified pyrolysis gas.
By adopting the technical scheme, the pyrolysis gas generated by pyrolysis of the pyrolysis material comprises CH 4 、CO、C 2 H 4 And C m H n And a plurality of organic gases, wherein C m H n The macromolecular organic gas is the main component of tar gas and mainly comprises aromatic hydrocarbon, polycyclic aromatic hydrocarbon, alkane olefin and the like. In the pyrolysis process, the pyrolysis reaction is carried out in a micro-oxygen environment by introducing a small amount of oxygen, and macromolecular organic gas in the pyrolysis gas and the oxygen are subjected to oxidation reaction, so that macromolecular organic gas components are subjected to oxidation reaction to generate micromolecular gas components, the tar gas content in the pyrolysis gas is further reduced, condensation of the pyrolysis gas in a pipeline in the outward conveying process can be effectively reduced, the frequency of cleaning and replacement of the pipeline is reduced, and the production efficiency is improved. The content of oxygen in the introduced air is kept between 4.5 and 8 percent (v/v), tar gas in the pyrolysis reactor can react with oxygen, the content of oxygen is ensured to be below the explosion limit of combustible substances, dangerous conditions such as explosion and the like generated in the pyrolysis reactor are avoided, and the safety in the production process is improved.
Optionally, in step S3, the air is a mixed gas of oxygen and nitrogen, and the oxygen content is 4.5-8%.
By adopting the technical scheme, the air is formed by mixing oxygen and nitrogen, the nitrogen is inert gas, the property of the nitrogen is stable, the nitrogen does not react with components in pyrolysis gas in the pyrolysis process, and meanwhile, a certain explosion-proof and flame-retardant effect can be achieved.
Optionally, the interior of the rotary pyrolysis reactor is in a micro-positive pressure state, and the pressure is 1.5-3 KPa.
Through adopting above-mentioned technical scheme, control the inside pressure of rotation pyrolysis reactor in the state of micro-positive pressure, can avoid outside air to get into the inside of pyrolysis reactor, avoid outside air to interfere the inside environment of reactor and lead to oxygen content to rise and make the system get into dangerous situation.
Optionally, the pyrolyzed material comprises one or more of paint, oil sludge, plastic bags and water-containing sludge.
By adopting the technical scheme, the pyrolysis material prepared by combining the waste components such as paint, oil sludge, plastic bags, water-containing sludge and the like has a certain heat value, and each effective gas component in pyrolysis gas generated in the pyrolysis process is kept at a relatively balanced level. In addition, through the compatibility of various types of wastes, the solid wastes with different water contents are compatible, so that the viscosity and the fluidity of the pyrolysis material are kept in a good state, and convenience is provided for the feeding and the internal treatment of the subsequent pyrolysis process.
Optionally, the pyrolysis materials comprise a first-stage pyrolysis material and a second-stage pyrolysis material, wherein the water content of the first-stage pyrolysis material is 45-80% (m/m), and the water content of the second-stage pyrolysis material is not higher than 30% (m/m); the first-stage pyrolysis material is input from the first stage of the rotary pyrolysis reactor, and the second-stage pyrolysis material is input from the second stage of the rotary pyrolysis reactor.
Through adopting above-mentioned technical scheme, divide into first section pyrolysis material and second section pyrolysis material with the pyrolysis reaction material according to the height of moisture content in the pyrolysis material, the rotary pyrolysis reactor is two-section pyrolysis reactor, through throwing into the pyrolysis material of different moisture content from the different material ends of throwing of rotary pyrolysis reactor, first section pyrolysis material of high moisture content is first high temperature heating stoving after the first section of rotary pyrolysis reactor is thrown into, evaporate and discharge moisture wherein, reduce the moisture content in the pyrolysis material and merge with the second section pyrolysis material of throwing into from the both ends of pyrolysis reactor again and carry out high temperature pyrolysis. By separately feeding and heating pyrolysis materials with high water content and low water content, part of water vapor in pyrolysis gas can be rapidly separated, and if the separation of the water vapor and the pyrolysis gas is carried out in two stages, the whole water vapor needs to be heated to more than one thousand degrees, a large amount of fuel needs to be consumed, and high economic cost is generated.
Optionally, the internal temperature of the first section of the rotary pyrolysis reactor is 300-350 ℃, and the internal temperature of the second section is 500-550 ℃.
Through adopting above-mentioned technical scheme, the temperature setting in one section makes its speed that is higher than conventional moisture evaporation at 300~350 ℃, and the moisture in the pyrolysis material can comparatively fully evaporate and get rid of under this temperature, plays the effect of dry pyrolysis material, and the active ingredient in the pyrolysis material can carry out preliminary pyrolysis under this temperature simultaneously, can take place pyrolysis reaction fast when the follow-up second section that lets in pyrolysis reactor, promotes pyrolysis reaction efficiency. The temperature of the second section of the pyrolysis reactor is set at 500-550 ℃, and at the temperature, organic components in the pyrolysis material are rapidly cracked to generate pyrolysis gas.
Optionally, in step S3, air is introduced from the second stage of the rotary reactor.
By adopting the technical scheme, the air with the oxygen content of 4.5-8% (v/v) is introduced into the second section of the pyrolysis reactor, so that a micro-oxygen environment is formed in the second section of the pyrolysis reactor, the content of tar gas in pyrolysis gas is reduced through oxidation reaction of oxygen and macromolecular organic gas, and condensation of the tar gas on a pyrolysis reactor pipeline is reduced. The air is not introduced from one section of the reactor, so that the influence of the generated vapor generated in one section on the micro-oxygen environment can be avoided, and the phenomenon that the oxidation reaction is insufficiently carried out due to the influence of partial oxygen and vapor discharged together to the content of oxygen in the pyrolysis reactor is avoided.
Optionally, in step S1, the moisture content of the solid waste after drying is not more than 15% (m/m).
Through adopting above-mentioned technical scheme, solid waste includes plant stump, gardens rubbish, plastic products etc. and wherein moisture that contains can detach fast through heating stoving, reduces the water content in the pyrolysis material to the solid waste after the stoving adds more easily in follow-up feeding process, provides convenience for follow-up operation.
In summary, the present application includes at least one of the following beneficial technical effects:
1. in this technical scheme, in the pyrolysis process, make pyrolysis reaction go on in little oxygen environment through letting in a small amount of oxygen, the macromolecular organic gas in the pyrolysis gas takes place oxidation reaction with oxygen, makes the organic gas composition of macromolecule generate the micromolecular gas composition after oxidation reaction, and then reduces the content of tar gas in the pyrolysis gas, and the pyrolysis gas can effectively reduce in the in-process of outwards carrying in the pipeline condensation, reduces the frequency of pipeline clearance and change, promotes production efficiency.
2. The content of oxygen in the introduced air is kept between 4.5 and 8 percent (v/v), tar gas in the pyrolysis reactor can react with oxygen, the content of oxygen is ensured to be below the explosion limit of combustible substances, dangerous conditions such as explosion and the like generated in the pyrolysis reactor are avoided, and the safety in the production process is improved.
3. The pressure in the rotary pyrolysis reactor is controlled in a micro positive pressure state, so that external air can be prevented from entering the pyrolysis reactor, and the dangerous condition that the system enters due to the fact that the oxygen content rises as the external air interferes with the internal environment of the reactor is avoided.
Detailed Description
The present application is described in further detail below in conjunction with the specific details.
Example 1
The micro-oxygen pyrolysis process includes mixing pyrolyzed material comprising paint slag, oil sludge, plastic bag and water-containing sludge, stoving at 120 deg.c for 2 hr, and element analysis in the pyrolyzed material to obtain the element analysis results shown in the following table 1:
table 1: the content of the main element (wt%) in example 1
The specific pyrolysis process is as follows:
s1, drying large paint residues until the water content is lower than 15% (m/m), crushing, and mixing with oil sludge, a plastic bag and water-containing sludge to prepare a pyrolysis material;
s2, continuously feeding the pyrolysis material into a rotary pyrolysis reactor for one section, and simultaneously introducing nitrogen and oxygen mixed gas with the oxygen content of 8% (v/v), and carrying out pyrolysis reaction at 500 ℃, wherein the inside of the pyrolysis reactor is kept at micro positive pressure, and the pressure is 3KPa;
s3, collecting pyrolysis gas from an exhaust port of the rotary pyrolysis reactor, washing to remove ash, and separating steam to obtain the pyrolysis gas.
Tested, the natural gas consumption for processing one ton of pyrolysis material was 50.1Nm 3 The duration taken for the pyrolysis gas duct to completely block was 42 days.
Example 2
Example 2 a pyrolysis material of the same composition as in example 1 was used, the pyrolysis process being as follows:
s1, drying large paint residues until the water content is lower than 15% (m/m), crushing, and mixing with oil sludge, a plastic bag and water-containing sludge to prepare a pyrolysis material;
s2, continuously feeding the pyrolysis material into a rotary pyrolysis reactor for one section, and simultaneously introducing nitrogen and oxygen mixed gas with the oxygen content of 4.5% (v/v), and carrying out pyrolysis reaction at 500 ℃, wherein the inside of the pyrolysis reactor is kept at micro positive pressure, and the pressure is 3KPa;
s3, collecting pyrolysis gas from an exhaust port of the rotary pyrolysis reactor, washing to remove ash, and separating steam to obtain the pyrolysis gas.
The natural gas consumption for processing one ton of pyrolysis material was tested to be 53.8Nm 3 The duration taken for the pyrolysis gas duct to completely block was 38 days.
Comparative example 1
Comparative example 1 a pyrolysis material of the same composition as in example 1 was used, the pyrolysis process being as follows:
s1, drying large paint residues until the water content is lower than 15% (m/m), crushing, mixing with oil sludge, a plastic bag and water-containing sludge to prepare a pyrolysis material, wherein the water content of the pyrolysis material is not more than 40% (m/m);
s2, continuously throwing the pyrolysis into one section of a rotary pyrolysis reactor, and simultaneously introducing nitrogen and oxygen mixed gas with oxygen content lower than 0.1% (v/v), and carrying out pyrolysis reaction at 500 ℃, wherein the inside of the pyrolysis reactor is kept at micro positive pressure, and the pressure is 3KPa; s3, collecting pyrolysis gas from an exhaust port of the rotary pyrolysis reactor, washing to remove ash, and separating steam to obtain the pyrolysis gas.
Tested, process one tonThe natural gas consumption of the pyrolysis feed was 61.1Nm 3 The duration taken for complete blockage of the pyrolysis gas duct was 7 days.
Comparative example 2
Comparative example 1 a pyrolysis material of the same composition as in example 1 was used, the pyrolysis process being as follows:
s1, drying large paint residues until the water content is lower than 15% (m/m), crushing, and mixing with oil sludge, a plastic bag and water-containing sludge to prepare a pyrolysis material;
s2, continuously feeding the pyrolysis material into a rotary pyrolysis reactor, and simultaneously introducing nitrogen and oxygen mixed gas with the oxygen content of 9% (v/v) to carry out pyrolysis reaction at the temperature of 500 ℃;
s3, collecting pyrolysis gas from an exhaust port of the rotary pyrolysis reactor, washing to remove ash, and separating steam to obtain the pyrolysis gas.
After about 1 hour from the start of pyrolysis, a local combustion phenomenon occurs inside the pyrolysis reactor.
As can be seen from the test results in examples 1 and 2 and comparative examples 1 and 2, pyrolysis is carried out in a micro-aerobic environment, compared with an anaerobic environment with the oxygen content of less than 0.1% (v/v), the blockage condition of a pyrolysis gas pipeline is obviously improved, and the period of time is prolonged to more than one month from the conventional 7 days, and the maximum period of time is 42 days. Meanwhile, the pyrolysis efficiency of the micro-oxygen pyrolysis process is higher, and one ton of pyrolysis materials with the same composition can save 10Nm in the micro-oxygen environment 3 The fuel can be calculated according to the method, and a pyrolysis device for treating 60 tons daily can save 2500Nm of natural gas every day 3 The above.
In comparative example 2, pyrolysis was performed using air having an oxygen content exceeding 89% (v/v), and in the course of a small batch test, it was found by a tester that 9% (v/v) of oxygen content exceeded the explosion limit of the combustible gas inside the pyrolysis reactor, and combustion easily occurred.
Example 3
The proportion of pyrolysis materials in this example was kept consistent with that in example 1, and the pyrolysis materials were divided into a first-stage pyrolysis material and a second-stage pyrolysis material according to the water content, the first-stage pyrolysis material comprising oil sludge and sludge water, the water content exceeding 50% (m/m), and the second-stage pyrolysis material comprising paint slag and plastic bags, the water content being lower than 30% (m/m).
The specific pyrolysis process is as follows:
feeding a first-stage pyrolysis material from a first stage of a rotary pyrolysis reactor, feeding a second-stage pyrolysis material from a second stage, setting the internal temperature of the first stage to 350 ℃, setting the internal temperature of the second stage to 500 ℃, introducing nitrogen and oxygen mixed gas with 8% (v/v) of oxygen into the second stage to carry out pyrolysis reaction, collecting pyrolysis gas from an exhaust port of the rotary pyrolysis reactor, washing to remove ash, and separating water vapor to obtain the pyrolysis gas.
Tested, the natural gas consumption for processing one ton of pyrolysis material was 46.5Nm 3 The pyrolysis gas line was completely plugged for 45 days.
Example 4
This example differs from example 3 in that the mixed gas of nitrogen and oxygen is introduced from a section of the rotary pyrolysis reactor, the remainder remaining in accordance with example 3.
Example 5
The difference between this example and example 1 is that the solid pyrolysis material further includes kitchen waste and plant straw, and the analysis results of the pyrolysis material component elements are shown in table 2 below:
table 2: the content of the main element (wt%) in example 5
The specific pyrolysis process was consistent with example 1.
Tested, the natural gas consumption for processing one ton of pyrolysis material was 47.8Nm 3 The duration taken for the pyrolysis gas duct to completely block was 42 days.
The test results in the above embodiments show that the micro-oxygen pyrolysis process has good pyrolysis treatment effect on waste pyrolysis materials with high water content and low water content, and can effectively reduce the tar gas content in pyrolysis gas, so that the continuous operation working time of the pyrolysis reactor is obviously prolonged, and the pyrolysis reactor has lower fuel consumption. Meanwhile, most tar gas in pyrolysis gas is oxidized and decomposed in the pyrolysis reaction process, so that the volatile matters entering the secondary combustion chamber are obviously reduced, and the problem that a large amount of volatile matters enter the secondary combustion chamber and water spraying and cooling are needed when the temperature of the secondary combustion chamber is too high is solved to a certain extent.
The foregoing are all preferred embodiments of the present application, and are not intended to limit the scope of the present application in any way, therefore: all equivalent changes in structure, shape and principle of this application should be covered in the protection scope of this application.
Claims (8)
1. The micro-oxygen pyrolysis process of the rotary pyrolysis reactor is characterized by comprising the following steps of:
s1, primarily drying and crushing solid waste;
s2, mixing and matching the crushed solid waste with other garbage to prepare a pyrolysis material;
s3, throwing the pyrolyzed material into a rotary pyrolysis reactor, and introducing air with the oxygen content of 4.5-8% (v/v) for pyrolysis;
s4, washing the pyrolysis gas to remove tar gas and ash, and then separating steam to obtain the purified pyrolysis gas.
2. The rotary pyrolysis reactor micro-aerobic pyrolysis process according to claim 1, wherein in the step S3, air is a mixed gas of oxygen and nitrogen, and the oxygen content is 4.5-8%.
3. The micro-aerobic pyrolysis process of the rotary pyrolysis reactor according to claim 1, wherein the interior of the rotary pyrolysis reactor is in a micro-positive pressure state, and the pressure is 1.5-3 KPa.
4. The rotary pyrolysis reactor micro-aerobic pyrolysis process of claim 1 wherein the pyrolysis material comprises a mixture of one or more of paint, sludge, plastic bags, and water-containing sludge.
5. The rotary pyrolysis reactor micro-aerobic pyrolysis process according to claim 4, wherein the pyrolysis materials comprise a first-stage pyrolysis material and a second-stage pyrolysis material, the water content of the first-stage pyrolysis material is 45-80% (m/m), and the water content of the second-stage pyrolysis material is not higher than 30% (m/m); the first-stage pyrolysis material is input from the first stage of the rotary pyrolysis reactor, and the second-stage pyrolysis material is input from the second stage of the rotary pyrolysis reactor.
6. The micro-aerobic pyrolysis process of a rotary pyrolysis reactor according to claim 5, wherein the internal temperature of the first section of the rotary pyrolysis reactor is 300-350 ℃ and the internal temperature of the second section is 500-550 ℃.
7. The micro-aerobic pyrolysis process of claim 5, wherein in the step S3, air is introduced from the second stage of the rotary reactor.
8. The rotary pyrolysis reactor micro-aerobic pyrolysis process of claim 1, wherein in step S1, the water content of the solid waste is not more than 15% (m/m).
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| Application Number | Priority Date | Filing Date | Title |
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| CN202310286712.3A CN116376603A (en) | 2023-03-23 | 2023-03-23 | Micro-oxygen pyrolysis process of rotary pyrolysis reactor |
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| CN202310286712.3A CN116376603A (en) | 2023-03-23 | 2023-03-23 | Micro-oxygen pyrolysis process of rotary pyrolysis reactor |
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