CN110283617A - A kind of high efficiency Waste plastic treatment apparatus and application method - Google Patents
A kind of high efficiency Waste plastic treatment apparatus and application method Download PDFInfo
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- CN110283617A CN110283617A CN201910656272.XA CN201910656272A CN110283617A CN 110283617 A CN110283617 A CN 110283617A CN 201910656272 A CN201910656272 A CN 201910656272A CN 110283617 A CN110283617 A CN 110283617A
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- 239000004033 plastic Substances 0.000 title claims abstract description 67
- 229920003023 plastic Polymers 0.000 title claims abstract description 67
- 239000002699 waste material Substances 0.000 title claims abstract description 31
- 238000000034 method Methods 0.000 title claims abstract description 19
- 238000005336 cracking Methods 0.000 claims abstract description 168
- 238000002485 combustion reaction Methods 0.000 claims abstract description 40
- 230000004927 fusion Effects 0.000 claims abstract description 39
- 230000003197 catalytic effect Effects 0.000 claims abstract description 35
- 238000003860 storage Methods 0.000 claims abstract description 25
- 238000012545 processing Methods 0.000 claims abstract description 21
- 239000012530 fluid Substances 0.000 claims abstract description 13
- 239000007789 gas Substances 0.000 claims description 88
- 239000003921 oil Substances 0.000 claims description 79
- 238000003756 stirring Methods 0.000 claims description 45
- 238000012546 transfer Methods 0.000 claims description 28
- 239000007788 liquid Substances 0.000 claims description 27
- 239000007787 solid Substances 0.000 claims description 24
- 238000006243 chemical reaction Methods 0.000 claims description 18
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 17
- 239000003546 flue gas Substances 0.000 claims description 17
- 239000000295 fuel oil Substances 0.000 claims description 17
- 239000000567 combustion gas Substances 0.000 claims description 14
- 239000010808 liquid waste Substances 0.000 claims description 14
- 238000010438 heat treatment Methods 0.000 claims description 12
- 238000002156 mixing Methods 0.000 claims description 11
- 238000003466 welding Methods 0.000 claims description 11
- 238000000746 purification Methods 0.000 claims description 10
- 239000000779 smoke Substances 0.000 claims description 10
- 239000003054 catalyst Substances 0.000 claims description 9
- 238000009833 condensation Methods 0.000 claims description 9
- 230000005494 condensation Effects 0.000 claims description 9
- 239000000446 fuel Substances 0.000 claims description 9
- 210000000481 breast Anatomy 0.000 claims description 8
- 238000006555 catalytic reaction Methods 0.000 claims description 8
- 239000000498 cooling water Substances 0.000 claims description 5
- 230000005484 gravity Effects 0.000 claims description 5
- 238000002844 melting Methods 0.000 claims description 5
- 230000008018 melting Effects 0.000 claims description 5
- 238000013461 design Methods 0.000 claims description 4
- 238000001514 detection method Methods 0.000 claims description 3
- 238000004880 explosion Methods 0.000 claims description 3
- 238000004523 catalytic cracking Methods 0.000 claims description 2
- 239000000203 mixture Substances 0.000 claims description 2
- 230000001939 inductive effect Effects 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 8
- 230000007613 environmental effect Effects 0.000 abstract description 7
- 238000007233 catalytic pyrolysis Methods 0.000 abstract description 5
- 230000000694 effects Effects 0.000 abstract description 3
- 238000001816 cooling Methods 0.000 description 8
- 239000010813 municipal solid waste Substances 0.000 description 6
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 238000007796 conventional method Methods 0.000 description 4
- 230000009089 cytolysis Effects 0.000 description 4
- 238000000197 pyrolysis Methods 0.000 description 4
- 239000002002 slurry Substances 0.000 description 4
- 238000004227 thermal cracking Methods 0.000 description 4
- 229910000831 Steel Inorganic materials 0.000 description 3
- 239000010959 steel Substances 0.000 description 3
- 230000032683 aging Effects 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 238000005520 cutting process Methods 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 230000003111 delayed effect Effects 0.000 description 2
- 239000003502 gasoline Substances 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 230000008439 repair process Effects 0.000 description 2
- 239000002910 solid waste Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 230000009429 distress Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000007499 fusion processing Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000003780 insertion Methods 0.000 description 1
- 230000037431 insertion Effects 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000011218 segmentation Effects 0.000 description 1
- -1 small molecule chain compound Chemical class 0.000 description 1
- 150000003384 small molecules Chemical group 0.000 description 1
- 210000000952 spleen Anatomy 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
- 238000013022 venting Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 238000003911 water pollution Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
Abstract
The present invention is a kind of high efficiency Waste plastic treatment apparatus and application method, processing unit includes sequentially connected pre-fusion tank, cracking still, catalytic tower, condensing tower, the condensing tower is successively connect with clarifier, surge tank, combustion furnace by gas pipeline, the condensing tower is connect by fluid pipeline with oil storage tank, the surge tank is connect by fluid pipeline with oil storage tank, the combustion furnace is connect with cracking still by gas pipeline, the combustion furnace is connect with blower inlet, and the blower export is connect with the cracking still and the catalytic tower simultaneously.The present invention is disposed with high temperature pre-fusion, high pressure-temperature cracking, catalytic pyrolysis, and the discomposing effect of plastics greatly improves, and the cracking gas for decomposing acquisition can be recycled, and not only reduce energy consumption, and clean and environmental protection, facilitate the continual and steady operation of system.
Description
Technical field
The present invention relates to cracking waste plastics engineering device technique fields, and in particular to a kind of high efficiency Waste plastic treatment apparatus, with
And the application method of the device.
Background technique
Plastic garbage compression in distress, airtight, expansive property, be easy to cause water pollution, land occupation, sewer stifled
The problems such as plug, however plastic garbage is extracted from petroleum with the chemical substance compared with high heating value, it is in house refuse
Mean calorie highest, plastic garbage energy and economization can be made, such as can be by plastics by way of catalytic pyrolysis
High molecular polymer macromolecular chain is opened, and the compound of small molecule chain is reduced to, wherein small molecule chain compound is mostly
Hydrocarbon, available gasoline and combustion gas etc., provide while solving plastics problem of environmental pollution after post treatment
The renewable sources of energy.But the processing units such as existing autoclave refining equipment, there are energy consumption height, safety is excessively poor, and treatment effeciency is low etc.
Problem.
206751739 U of CN discloses a kind of full-automatic cracking waste plastics device, and waste plastic passes through crushing device powder
It is broken, then metal steel wire absorption is walked by concentration equipment, steel wire is collected in steel wire collector, and waste plastic can pass through nothing
Oxygen is thermally cracked to as oil and gas, then by desulfurizing dust-collector in oil gas hydrogen sulfide and hydrogen chloride gas remove, oil gas passes through again
Catch pot separates gasoline and diesel oil.Although however the technical solution be provided with pretreatment procedure, processing be not thorough,
Cracking temperature and pressure normal pressure, it is difficult to which high efficiency decomposes waste plastics.
107201244 A of CN discloses cracking waste plastics oil refining process and equipment, first Pintsch process catalytic pyrolysis again, drop
Solution is more thorough；Product after Pintsch process, which enters, is not only further cracked into short chain compound in catalytic tower, moreover it is possible to eliminate oil
Ash impurities in vapour.The step of technical solution treatment process is relatively reasonable, and waste plastics segmentation is preheated to molten condition, will
The waste plastics of molten condition carry out the step of Pintsch process also can more efficient treatment of waste plastics, but the process flow is not
There is the open equipment that can be realized, i.e., do not disclose the method for melting and cracking corresponding equipment and combustible gas recycling,
And it is particularly harsh to realize that the process flow requires the service condition of equipment, and the technical solution is also without providing solution.
In conclusion the prior art still lack it is a kind of can be realized high efficiency, low energy consumption and the Treatment of Waste Plastics of environmental protection dress
It sets.
Summary of the invention
It, can be efficient object of the present invention is in view of the drawbacks of the prior art, design a kind of high efficiency Waste plastic treatment apparatus
Rate treatment of waste plastics rubbish.Detailed technology scheme of the invention is as follows.
A kind of high efficiency Waste plastic treatment apparatus, including sequentially connected pre-fusion tank, cracking still, catalytic tower, condensing tower,
The condensing tower successively connect by gas pipeline with clarifier, surge tank, combustion furnace, the condensing tower by fluid pipeline and
Oil storage tank connection, the surge tank are connect by fluid pipeline with oil storage tank, and the combustion furnace and cracking still pass through gas pipeline
Connection, the combustion furnace are connect with blower inlet, and the blower export connects with the cracking still and the catalytic tower simultaneously
It connects, the catalytic tower is connected with heat transfer oil heater, column for smoke purification, cooling tower in turn by gas pipeline.
When using the present apparatus, waste plastics is put into pre-fusion tank, liquid, high viscosity are melt under the conditions of 220-250 DEG C
Liquid waste plastics is pumped to cracking still through main delivery pump, and liquid waste plastics is pressurized thermal cracking in cracking still, cracks operating temperature
It is 450-650 DEG C, cracking gas is automatically drained out from the outlet of the cracking gas of cracking still automatically after reaching setting pressure, cracking gas outlet
202 pressure release threshold values is adjustable, preferably 0.8-1.6MPa.Cracking gas enters catalytic tower, contacts with the catalyst of catalytic tower, carries out
Quadric catalysis cracking reaction, the operating temperature section of catalytic tower are 300-450 DEG C.After the completion of quadric catalysis cracking reaction, cracking
Gas forms fuel oil and incoagulability combustion gas after passing into condensing tower B-grade condensation.Incoagulability combustion gas is purified laggard by clarifier
Enter surge tank storage, surge tank is connect by fluid pipeline with oil storage tank, and the fuel oil of condensation is input to oil storage tank, described slow
It rushes tank to connect with combustion furnace, pressure can be pumped to combustion chambers burn after reaching 0.2MPa by air-introduced machine in surge tank, and gas exists
It burns in combustion furnace, then provides high-temperature gas heat supply to cracking still, so that cracking operating temperature reaches 450-650 DEG C,
So that cracking gas can be recycled, clean and environmental protection.Obtained fuel oil is cracked to store by flow by gravity to oil storage tank,
For final products.
When flue gas by combustion chamber heat, when cracking still operating temperature having been made to reach 450-650 DEG C, at this time without
It must flue gas.At this point it is possible to which small part flue gas is recycled by cracking still, most flue gas will be delivered to by air blower
In catalytic tower, second of catalysis reaction occurs, by opening high temperature butterfly valve, extra flue gas is entered by the top of catalytic tower is led
Hot oil heating furnace provides heat to heat transfer oil heater, and then flue gas is purified by column for smoke purification, then passes through cooling tower
Atmosphere is discharged into after cooling.
First inventive point of the invention is high temperature pre-fusion, high pressure-temperature cracking, catalytic pyrolysis, the discomposing effect of plastics
It greatly improves, and decompose the cracking gas obtained to be recycled, not only reduces energy consumption, and clean and environmental protection, initial rank
After section needs to carry out the processing of early period by extra power, subsequent cracking gas decomposition amount is relatively high, can guarantee sufficient heat
Amount supply, and when cracking gas too high levels, heat transfer oil heater can be given, empties, facilitates finally by purified treatment
The continual and steady operation of system.
Preferably, the catalytic tower is directly connect by gas pipeline with column for smoke purification, the catalytic tower with it is thermally conductive
It is provided with high temperature butterfly valve between oily heating furnace, is provided with high temperature butterfly valve between the catalytic tower and column for smoke purification.
After thermally conductive oil temperature reaches 300 DEG C, when continuing heating without using flue gas, switching high temperature butterfly valve arranges flue gas
Enter, is emptied after gas cleaning by cooling tower.
Preferably, the combustion furnace is connect with fuel cartridge, the fuel cartridge is connect with air pump, the combustion furnace and institute
State air pump.
Fuel cartridge directly can be conveyed air to combustion furnace, can also be fired with condition as initial heat source, air pump
The gas proportion of gas tank, so that combustion gas is easier to burn.
Preferably, the condensing tower is connect with cooling water pump, the condensing tower is second level shell and tube condenser.
Preferably, pre-fusion tank top central axes direction is provided with stirring motor, the side of the stirring motor
It is provided with feeding port, the other side is provided with repairing hand hole, and the stirring motor is provided with agitating shaft, described in the agitating shaft insertion
Pre-fusion tank inner space is provided in the middle part of the agitating shaft and blade is mixed, bottom is provided with bottom stirring blade, institute
The bottom for stating pre-fusion tank is provided with molten liquid outlet, and the molten liquid outlet is connect with the main delivery pump, the main conveying
Pump is connect with cracking still entrance, and the molten liquid outlet is provided with gate valve；The pre-fusion tank is provided with heat conducting oil inlet and leads
Hot oil outlet, the heat conducting oil inlet and the conduction oil outlet are connect with the heat transfer oil heater by pipeline, the institute
It states and is provided with heat conduction oil circulating pump between heat conducting oil inlet and the heat transfer oil heater.
Second inventive point of the invention is to increase pre-fusion tank, and waste plastics is not added directly in cracking still, but
It is put into pre-fusion tank after being melted into liquid first, liquid waste plastics is transported in cracking still using high temperature gear pump and is carried out
Reaction, it is ensured that space can make full use of in cracking still, and liquid waste plastics heat and mass efficiency is much higher than solid-state waste plastics, mentions
High lysis efficiency, reduces energy consumption.Pre-fusion tank is designed using conduction oil independent heat supply, it is ensured that pre-fusion process accurate temperature
Control reduces product caused by overreaction and loses.
Preferably, the cracking still includes the end socket on top and the autoclave body of lower part, the end socket and the autoclave body pass through
Precision welding forms welding circle in junction, and welding circle 100% passes through carrying out flaw detection, on the top central axes of the end socket
It is provided with cracking still entrance, the cracking still inlet side is provided with cracking gas outlet, the other side is provided with emergency mouth, described to split
Outlet of venting one's spleen is provided with pressure sensor and relief valve, and the relief valve finds out pressure in kettle in pressure sensor and reaches cracking pressure
It is automatically turned on when power, the emergency mouth is internally provided with rupture disk and temperature sensor, and rupture disk pressure in kettle reaches
Automatic-explosion depressurizes when early warning pressure, and the bottom of the autoclave body is provided with breast hole, is provided with fin on the outer wall of the autoclave body,
Cracking still collet is provided with outside the cracking still autoclave body, the combustion furnace is connected to by hot-gas channel with cracking still collet,
State cracking still in the cracking still collet sealed envelope residence.
Third inventive point of the invention is that cracking still is the integral type autoclave body formed by welding.The one of welded connecting
Formula autoclave body, without leaning on flange and bolt fastening, is not needed to install gasket additional, can effectively be kept away compared with conventional split type cracking still
Exempt to generate cracking gas leakage because pressure change leads to bolt looseness, is also avoided that caused by gasket aging and cracks gas leakage, subtract
Small product loss late, integral type autoclave body can high temperature and pressure work, when pressure is not up to relief valve limit value in kettle, cracking gas
It is stored in and continues to be thermally decomposed in kettle, it is ensured that abundant cracking reaction, pyrolysis product molecular weight is smaller compared with conventional techniques, has
Higher economic value added.
When the present invention handles solid waste plastics, first passes through in feeding port investment pre-fusion tank, be provided on agitating shaft more
On the one hand a stirring blade blends solid plastic, on the other hand increase heat transfer efficiency, and be recycled by heat transfer oil heater
Hot oil helps solid plastic to melt, and the molten liquid outlet is provided with gate valve, keeps closing by gate valve when liquid does not melt
It closes.Solid plastic enters cracking still by main delivery pump after melting and cracks, and gas passes through cracking gas outlet and carries out after cracking
Recovery processing, extra residue are discharged by breast hole.Combustion furnace can give autoclave body heat supply, and fin can increase heat transfer efficiency,
High-temperature gas heating can be in order to controlling the rate of heat addition.The operating temperature of cracking still 2 is 400-650 DEG C, and using gas heats more
Add economic and environment-friendly.
Preferably, the cracking pressure is 0.8-1.6MPa, and the early warning pressure is 2-2.5MPa.Cracking pressure is 0.8-
1.6MPa, pressure compared with prior art is higher, and when pressure not up to cracks pressure limit in kettle, cracking gas is stored in kettle
Continue to be thermally decomposed, it is ensured that abundant cracking reaction, pyrolysis product molecular weight is smaller compared with conventional techniques, has higher economy attached
It is value added.Early warning pressure and the power limit of autoclave body are close, can prevent accident.The main delivery pump is high temperature gear pump,
The high temperature gear pump is by heat-conducting oil heating, when normal work, pump in temperature maintain 150 DEG C.The gear pump is that high temperature resistant is high
The pump of pressure is capable of the liquid of pumping high viscosity, can work at a high temperature of 150 DEG C.
Preferably, the bottom stirring blade is anchor formula stirring blade, the mixing blade is propeller blade,
The internal diameter blade of the anchor formula stirring blade is the 2/3-9/10, mixing speed 50-70r/min of autoclave body internal diameter.Anchor formula stirring
The bottom shape of blade is similar with reaction kettle lower head shape, smaller with kettle wall gap, is conducive to the progress of diabatic process, quickly
When rotation, the liquid that mixing arm is driven gets off quiescent layer from band on reaction kettle wall；When rotating at a slow speed, there is stirring for scraper plate
Good heat transfer can be generated by mixing device, be usually used in heat transfer, partial crystallization operation and high viscosity liquid, high concentration slurry and settleability slurry
Stirring.Be mixed blade mainly make up anchor formula stirring blade bottom work when middle section undermixing and be arranged
's.
Preferably, the agitating shaft is additionally provided with solid stirring blade, the solid stirring blade is located at mixing and stirs
The top of blade is mixed, the solid stirring blade is high strength helical paddle blade, the blade edge of the high strength helical paddle blade
Edge is provided with broached-tooth design.Increase solid stirring blade, is to can be improved when handling the solid plastic rubbish of high rigidity
Cutting efficiency faster cuts solid refuse.
Preferably, the ratio between working volume of the working volume of the pre-fusion tank and the cracking still is (1-5): 1, institute
It states main delivery pump and is connected with several cracking stills, the cracking still can crack simultaneously.The working volume of pre-fusion tank is long-range
When cracking still, pre-fusion tank 1 can disposably melt large batch of solid plastic, and lysis efficiency can be improved in this way.
The present invention also protects the application method of the processing unit, including the following steps:
(1) waste plastics investment pre-fusion tank to be processed is pre-processed, heat transfer oil heater is opened, in 220-250
Liquid is melt under the conditions of DEG C；
(2) the liquid waste plastics that (1) obtains is pumped to cracking still through main delivery pump, liquid waste plastics increases in cracking still
Thermal cracking is pressed, cracking operating temperature is 450-650 DEG C；
(3) the obtained cracking gas of (2) processing is entered into catalytic tower, is contacted with the catalyst of catalytic tower, 300-450 DEG C into
Row quadric catalysis cracking reaction；
(4) fuel oil and incoagulability combustion gas are formed after the cracking gas that (3) obtain being passed into condensing tower B-grade condensation, no
Solidifying property combustion gas enters surge tank after purifying by clarifier and stores, and it is final that fuel oil is stored by flow by gravity to oil storage tank
Product；
(5) gas stored in surge tank is connect by fluid pipeline with oil storage tank, and pressure can pass through after reaching 0.2MPa
Air-introduced machine is pumped to combustion chambers burn, and gas burns in combustion furnace, then provides high-temperature gas heat supply to cracking still, is delayed
The fuel oil for rushing middle condensation in tank is input to oil storage tank；
Wherein, the residue of pre-fusion tank is periodically discharged by breast hole in step (1).
The beneficial effects of the present invention are as follows:
(1) present invention is disposed with high temperature pre-fusion, high pressure-temperature cracking, catalytic pyrolysis, and the discomposing effect of plastics is big
Width improves, and the cracking gas for decomposing acquisition can be recycled, and not only reduce energy consumption, and clean and environmental protection, initial stage
After the processing for needing to carry out early period by extra power, subsequent cracking gas decomposition amount is relatively high, can guarantee sufficient heat
Supply, and when cracking gas too high levels, heat transfer oil heater can be given, is emptied finally by purified treatment, facilitates body
The continual and steady operation of system.
(2) the integral type autoclave body being welded to connect is not necessarily to lean on flange and bolt fastening compared with conventional split type cracking still,
It does not need to install gasket additional, can effectively avoid generating cracking gas leakage because pressure change leads to bolt looseness, be avoided that pad yet
Crack gas leakage caused by piece aging, reduce product loss late, integral type autoclave body can high temperature and pressure work, when pressure in kettle
Not up to relief valve limit value when, cracking gas, which is stored in, to be continued to be thermally decomposed in kettle, it is ensured that abundant cracking reaction, pyrolysis product molecule
Amount is smaller compared with conventional techniques, has higher economic value added；
(3) pre-fusion tank, waste plastics are not added directly in cracking still, but put into pre-fusion tank be melted into first
After liquid, liquid waste plastics is transported in cracking still using high temperature gear pump and is reacted, it is ensured that space can be in cracking still
It makes full use of, and liquid waste plastics heat and mass efficiency is much higher than solid-state waste plastics, improves lysis efficiency, reduce energy consumption；
(4) cracking still can handle various plastic refuses, and use scope is wide, and cracking still can more kettles it is used in parallel,
The service efficiency of pre-fusion tank and cracking still is further improved, the speed of cracking is improved.
Detailed description of the invention
Fig. 1 present apparatus flow diagram；
Fig. 2 pre-fusion tank arrangement enlarged drawing；
Fig. 3 cracks kettle device enlarged drawing.
Detailed description of the invention: pre-fusion tank 1, stirring motor 102, agitating shaft 103, repairs hand hole 104, conduction oil at feeding port 101
Solid stirring blade 106, blade 107, bottom stirring blade 108, conduction oil outlet 109, molten liquid is mixed in entrance 105
Outlet 110, gate valve 111, cracking still 2, cracking still entrance 201, cracking gas outlet 202, emergency mouth 203, welding circle 204, fin
205, temperature sensor 206, breast hole 207, main delivery pump 3, heat transfer oil heater 4, combustion furnace 5, heat conduction oil circulating pump 6, cigarette
Gas purifying column 7, cooling tower 8, catalytic tower 9, condensing tower 10, clarifier 11, surge tank 12, oil storage tank 13, cooling water pump 14, sky
Air pump 15, fuel cartridge 16, air blower 17.
Specific embodiment
Specific embodiments of the present invention will be further explained with reference to the accompanying drawing:
A kind of high efficiency Waste plastic treatment apparatus, as shown in Figure 1, including sequentially connected pre-fusion tank 1, cracking still 2, urging
Change tower 9, condensing tower 10, the condensing tower 10 is successively connect with clarifier 11, surge tank 12, combustion furnace 5 by gas pipeline, institute
Condensing tower 10 to be stated to connect by fluid pipeline with oil storage tank 13, the surge tank 12 is connect by fluid pipeline with oil storage tank 13,
The combustion furnace 5 is connect with cracking still 2 by gas pipeline, and the combustion furnace 5 is connect with 17 entrance of air blower, the air blower
17 outlets are connect with the cracking still 2 and the catalytic tower 9 simultaneously, and the catalytic tower 9 is connected in turn by gas pipeline leads
Hot oil heating furnace 4, column for smoke purification 7, cooling tower 8.
When using the present apparatus, waste plastics is put into pre-fusion tank 1, liquid, high viscosity are melt under the conditions of 220-250 DEG C
Liquid waste plastics is pumped to cracking still 2 through main delivery pump 3, and liquid waste plastics is pressurized thermal cracking in cracking still 2, cracks work temperature
Degree is 450-650 DEG C, and cracking gas exports 202 (as shown in Figure 3) automatically from the cracking gas of cracking still 2 automatically after reaching setting pressure
The pressure release threshold values of discharge, cracking gas outlet 202 is adjustable, preferably 0.8-1.6MPa.Cracking gas enters catalytic tower 9, with catalytic tower 9
Catalyst contact, carry out quadric catalysis cracking reaction, the operating temperature section of catalytic tower 9 is 300-450 DEG C.Quadric catalysis is split
After the reaction was completed, cracking gas enters 6 and forms fuel oil and incoagulability combustion gas after 10 B-grade condensation of condensing tower solution.Incoagulability combustion
Gas enters surge tank 12 after purifying by clarifier 11 and stores, and surge tank 12 is connect by fluid pipeline with oil storage tank 13, will be cold
Solidifying fuel oil is input to oil storage tank 13, and the surge tank 12 is connect with combustion furnace 5, after pressure reaches 0.2MPa in surge tank 12
It can be pumped by air-introduced machine to combustion chambers burn, gas burns in combustion furnace 5, then provides High Temperature Gas to cracking still 2
Body heat supply, so that cracking operating temperature reaches 450-650 DEG C, so that cracking gas can be recycled, clean and environmental protection.Cracking
Obtained fuel oil is stored by flow by gravity to oil storage tank 13, is final products.
When flue gas by combustion chamber heat, when cracking still operating temperature having been made to reach 450-650 DEG C, at this time without
It must flue gas.At this point it is possible to which small part flue gas is recycled by cracking still 2, most flue gas will be defeated by air blower 17
It send into catalytic tower 9, second of catalysis reaction occurs, by opening high temperature butterfly valve, extra flue gas passes through the top of catalytic tower 9
Into heat transfer oil heater 4, heat is provided to heat transfer oil heater 4, then flue gas is purified by column for smoke purification 7, then logical
Atmosphere is discharged into after supercooling water tower 8 is cooling.
As preferred embodiment, the catalytic tower 9 is directly connect with column for smoke purification 7 by gas pipeline, described to urge
Change and be provided with high temperature butterfly valve between tower 9 and heat transfer oil heater 4, is provided with high temperature between the catalytic tower 9 and column for smoke purification 7
Butterfly valve.
After thermally conductive oil temperature reaches 300 DEG C, when continuing heating without using flue gas, switching high temperature butterfly valve is discharged into flue gas
10, it is emptied after gas cleaning by cooling tower 8.
As preferred embodiment, the combustion furnace 5 is connect with fuel cartridge 16, and the fuel cartridge 16 connects with air pump 15
It connects, the combustion furnace 5 and the air pump 15.
Fuel cartridge 16 directly can convey air to combustion furnace 5 as initial heat source, air pump 15, can also item
The gas proportion of part fuel cartridge 16, so that combustion gas is easier to burn.
As preferred embodiment, the condensing tower 10 is connect with cooling water pump 14, and the condensing tower 10 is second level tubulation
Formula condenser.
As preferred embodiment, as shown in Fig. 2, 1 top central axes direction of the pre-fusion tank is provided with stirring motor
102, the side of the stirring motor 102 is provided with feeding port 101, and the other side, which is provided with, repairs hand hole 104, the stirring motor
102 are provided with agitating shaft 103, and the agitating shaft 103 is inserted into 1 inner space of pre-fusion tank, the middle part of the agitating shaft 103
It is provided with and blade 107, bottom is mixed is provided with bottom stirring blade 108, the bottom of the pre-fusion tank 1 is provided with melting
Liquid outlet 110, the molten liquid outlet 110 are connect with the main delivery pump 3, and the main delivery pump 3 connects with cracking still entrance 201
It connects, the molten liquid outlet 110 is provided with gate valve 111；The pre-fusion tank 1 is provided with heat conducting oil inlet 105 and conduction oil goes out
Mouth 109, the heat conducting oil inlet 105 and the conduction oil outlet 109 are connect with the heat transfer oil heater 4 by pipeline, institute
It states and is provided with heat conduction oil circulating pump 6 between the heat conducting oil inlet 105 and the heat transfer oil heater 4.
As preferred embodiment, as shown in figure 3, the cracking still 2 includes end socket (not shown) and the lower part on top
Autoclave body (not shown), the end socket and the autoclave body form welding circle 204, the welding circle in junction by precision welding
204 100% pass through carrying out flaw detection, are provided with cracking still entrance 201 on the top central axes of the end socket, the cracking still enters
201 sides of mouth are provided with cracking gas outlet 202, the other side is provided with emergency mouth 203, and the cracking gas outlet 202 is provided with pressure
Force snesor (not shown) and relief valve (not shown), the relief valve find out pressure in kettle in pressure sensor and reach cracking pressure
It is automatically turned on when power, the emergency mouth 203 is internally provided with rupture disk and temperature sensor 206, and the rupture disk is in kettle internal pressure
Automatic-explosion depressurizes when power reaches early warning pressure, and the bottom of the autoclave body is provided with breast hole 207, sets on the outer wall of the autoclave body
It is equipped with fin 205, is provided with cracking still collet (not shown) outside 2 autoclave body of cracking still, the combustion furnace 5 passes through high-temperature gas
Pipeline is connected to cracking still collet (not shown), and cracking still 2 is stated in cracking still collet (not shown) sealed envelope residence.
When the present invention handles solid waste plastics, first passes through feeding port 101 and put into pre-fusion tank 1, set on agitating shaft 103
Multiple stirring blades are equipped with, solid plastic is on the one hand blended, on the other hand increase heat transfer efficiency, and pass through heat transfer oil heater 4
Hot oil is recycled, solid plastic is helped to melt, the molten liquid outlet 110 is provided with gate valve 111, leads to when liquid does not melt
Gate valve 111 is crossed to remain turned-off.Solid plastic enters cracking still 2 by main delivery pump 3 after melting and cracks, and gas is logical after cracking
It crosses cracking gas outlet 202 to be recycled, extra residue is discharged by breast hole 207.Combustion furnace 5 can be supplied to autoclave body
Heat, fin 205 can increase heat transfer efficiency, and high-temperature gas heating can be in order to controlling the rate of heat addition.The operating temperature of cracking still 2
It is 400-650 DEG C, the more economical environmental protection of using gas heating.
As preferred embodiment, the cracking pressure is 0.8-1.6MPa, and the early warning pressure is 2-2.5MPa.Cracking
Pressure is 0.8-1.6MPa, and pressure compared with prior art is higher, when pressure not up to cracks pressure limit in kettle, cracking gas
It is stored in and continues to be thermally decomposed in kettle, it is ensured that abundant cracking reaction, pyrolysis product molecular weight is smaller compared with conventional techniques, has
Higher economic value added.Early warning pressure and the power limit of autoclave body are close, can prevent accident.
As preferred embodiment, the main delivery pump 3 is high temperature gear pump, and the high temperature gear pump is added by conduction oil
Heat, when normal work, pump in temperature maintain 150 DEG C.The gear pump is high-temperature and high-presure resistent pump, is capable of the liquid of pumping high viscosity
Body can work at a high temperature of 150 DEG C.
As preferred embodiment, the bottom stirring blade 108 is anchor formula stirring blade, the mixing blade
107 be propeller blade, and the internal diameter blade of the anchor formula stirring blade is the 2/3-9/10, mixing speed 50- of autoclave body internal diameter
70r/min.The bottom shape of anchor formula stirring blade is similar with reaction kettle lower head shape, smaller with kettle wall gap, is conducive to pass
The progress of thermal process, quickly when rotation, the liquid that mixing arm is driven gets off quiescent layer from band on reaction kettle wall；At a slow speed
When rotation, there is the blender of scraper plate that can generate good heat transfer, is usually used in heat transfer, partial crystallization operation and high viscosity liquid, highly concentrated
Spend the stirring of slurry and settleability slurry.Be mixed blade 107 mainly make up anchor formula stirring blade bottom work when in
Between part undermixing and be arranged.
As preferred embodiment, the agitating shaft 103 is additionally provided with solid stirring blade 106, the solid stirring
Blade 106 is located at the top that blade 107 is mixed, and the solid stirring blade 106 is high strength helical paddle blade, the height
The blade edge of strength helical paddle blade is provided with broached-tooth design.Increase solid stirring blade 106, is in order in processing high rigidity
Solid plastic rubbish when, can be improved cutting efficiency, faster cut solid refuse.
As preferred embodiment, the working volume of the pre-fusion tank 1 and the ratio between the working volume of the cracking still 2 are
(1-5): 1, the main delivery pump 3 is connected with several cracking stills 2, and the cracking still 2 can crack simultaneously.Pre-fusion tank 1
Working volume be much larger than cracking still 2 when, pre-fusion tank 1 can disposably melt large batch of solid plastic, can mention in this way
High lysis efficiency.
Application Example
Using processing unit of the invention, go to handle with PE plastics weight ratio be more than 90% waste plastics, including following step
It is rapid:
(1) PE waste plastics investment pre-fusion tank 1 to be processed is pre-processed, heat transfer oil heater is opened, at 250 DEG C
Under the conditions of be melt into liquid；
(2) the liquid waste plastics that (1) obtains is pumped to cracking still through main delivery pump, liquid waste plastics increases in cracking still
Thermal cracking is pressed, cracking operating temperature is 650 DEG C, sets cracking pressure as 1.4MPa, when cracking gas reaches cracking pressure, stops splitting
Solution, cracking gas are exported by cracking gas and are discharged；
(3) cracking gas that (2) processing obtains is entered into catalytic tower, is contacted with the catalyst of catalytic tower, carry out two at 450 DEG C
Secondary catalytic cracking reaction, the catalyst select iron Si catalyst Fe-SBA-15, and the mass ratio of catalyst and waste plastics is
0.01, wherein Fe-SBA-15 specific surface area of catalyst > 600m2/g；Hole holds > 0.60cm3/g；Aperture size 6-7nm, wall
Thickness 4-6nm, iron content 0.01-7wt%；
(4) fuel oil and incoagulability combustion gas are formed after the cracking gas that (3) obtain being passed into condensing tower B-grade condensation, no
Solidifying property combustion gas enters surge tank after purifying by clarifier and stores, and fuel oil is stored by flow by gravity to oil storage tank, fuel oil
For final products；
(5) gas stored in surge tank is connect by fluid pipeline with oil storage tank, and pressure can pass through after reaching 0.2MPa
Air-introduced machine is pumped to combustion chambers burn, and gas burns in combustion furnace, then provides high-temperature gas heat supply to cracking still, is delayed
The fuel oil for rushing middle condensation in tank is input to oil storage tank.
PE waste plastics is handled using the present apparatus, the yield of fuel oil is more than 60%, and energy consumption substantially reduces.
According to the disclosure and teachings of the above specification, those skilled in the art in the invention can also be to above-mentioned embodiment party
Formula is changed and is modified.Therefore, the invention is not limited to the specific embodiments disclosed and described above, to the one of invention
A little modifications and changes should also be as falling into the scope of the claims of the present invention.In addition, although being used in this specification
Some specific terms, these terms are merely for convenience of description, does not limit the present invention in any way.
Claims (10)
1. a kind of high efficiency Waste plastic treatment apparatus, which is characterized in that including sequentially connected pre-fusion tank, cracking still, catalysis
Tower, condensing tower, the condensing tower are successively connect with clarifier, surge tank, combustion furnace by gas pipeline, and the condensing tower passes through
Fluid pipeline is connect with oil storage tank, and the surge tank is connect by fluid pipeline with oil storage tank, and the combustion furnace and cracking still are logical
Cross gas pipeline connection, the combustion furnace connect with blower inlet, the blower export at the same with the cracking still and institute
Catalytic tower connection is stated, the catalytic tower is connected with heat transfer oil heater, column for smoke purification, cooling water in turn by gas pipeline
Tower.
2. processing unit according to claim 1, which is characterized in that the catalytic tower by gas pipeline directly and flue gas
Purifying column connection, is provided with high temperature butterfly valve, the catalytic tower and column for smoke purification between the catalytic tower and heat transfer oil heater
Between be provided with high temperature butterfly valve.
3. processing unit according to claim 2, which is characterized in that the combustion furnace is connect with fuel cartridge, the combustion gas
Tank is connect with air pump, the combustion furnace and the air pump.
4. processing unit according to claim 3, which is characterized in that the condensing tower is connect with cooling water pump, described cold
Solidifying tower is second level shell and tube condenser.
5. processing unit according to claim 3 or 4, which is characterized in that pre-fusion tank top central axes direction is set
It is equipped with stirring motor, the side of the stirring motor is provided with feeding port, and the other side is provided with repairing hand hole, the stirring motor
It is provided with agitating shaft, the agitating shaft is inserted into pre-fusion tank inner space, is provided with mixing in the middle part of the agitating shaft and stirs
Mix blade, bottom is provided with bottom stirring blade, the bottom of the pre-fusion tank is provided with molten liquid outlet, and the molten liquid goes out
Mouth is connect with main delivery pump, and the main delivery pump is connect with cracking still entrance, and the molten liquid outlet is provided with gate valve；It is described pre-
Melting tank is provided with heat conducting oil inlet and conduction oil outlet, the heat conducting oil inlet and the conduction oil outlet and the conduction oil
Heating furnace is connected by pipeline, and conduction oil circulation is provided between the heat conducting oil inlet and the heat transfer oil heater
Pump.
6. processing unit according to claim 5, which is characterized in that the cracking still includes end socket and the lower part on top
Autoclave body, the end socket and the autoclave body form welding circle in junction by precision welding, and the welding circle 100% passes through flaw detection
It detects, is provided with cracking still entrance on the top central axes of the end socket, the cracking still inlet side is provided with cracking gas and goes out
Mouth, the other side are provided with emergency mouth, and the cracking gas outlet is provided with pressure sensor and relief valve, and the relief valve is in pressure
Sensor finds out automatic opening when pressure in kettle reaches cracking pressure, and the emergency mouth is internally provided with rupture disk and temperature sensing
Device, automatic-explosion depressurizes when rupture disk pressure in kettle reaches early warning pressure, and the bottom of the autoclave body is provided with breast hole,
It is provided with fin on the outer wall of the autoclave body, is provided with cracking still collet outside the cracking still autoclave body, the combustion furnace passes through height
Warm gas pipeline is connected to cracking still collet, and cracking still is stated in the cracking still collet sealed envelope residence, and the cracking pressure is
0.8-1.6MPa, the early warning pressure are 2-2.5MPa, and the main delivery pump is high temperature gear pump, and the high temperature gear pump is led
Hot oil heating, when normal work, pump in temperature maintain 150 DEG C.
7. processing unit according to claim 6, which is characterized in that the bottom stirring blade is anchor formula stirring blade,
The mixing blade is propeller blade, and the internal diameter blade of the anchor formula stirring blade is the 2/3-9/10 of autoclave body internal diameter,
Mixing speed is 50-70r/min.
8. processing unit according to claim 6, which is characterized in that the agitating shaft is additionally provided with solid paddle
Piece, the solid stirring blade are located at the top that blade is mixed, and the solid stirring blade is high strength helical paddle blade,
The blade edge of the high strength helical paddle blade is provided with broached-tooth design.
9. processing unit according to claim 6, which is characterized in that the working volume of the pre-fusion tank and the cracking
The ratio between working volume of kettle is (1-5): 1, the main delivery pump is connected with several cracking stills, and the cracking still can be simultaneously
Cracking.
10. the application method of -9 described in any item processing units according to claim 1, characterized in that it comprises the following steps:
(1) waste plastics investment pre-fusion tank to be processed is pre-processed, heat transfer oil heater is opened, in 220-250 DEG C of item
Liquid is melt under part；
(2) the liquid waste plastics that (1) obtains is pumped to cracking still through main delivery pump, liquid waste plastics is pressurized heat in cracking still
Cracking, cracking operating temperature are 450-650 DEG C；
(3) cracking gas that (2) processing obtains is entered into catalytic tower, is contacted with the catalyst of catalytic tower, carry out two at 300-450 DEG C
Secondary catalytic cracking reaction；
(4) fuel oil and incoagulability combustion gas, incoagulability are formed after the cracking gas that (3) obtain being passed into condensing tower B-grade condensation
Combustion gas enters surge tank after purifying by clarifier and stores, and fuel oil is stored by flow by gravity to oil storage tank, is final products；
(5) gas stored in surge tank is connect by fluid pipeline with oil storage tank, and pressure can pass through air inducing after reaching 0.2MPa
Machine is pumped to combustion chambers burn, and gas burns in combustion furnace, then provides high-temperature gas heat supply, surge tank to cracking still
The fuel oil of interior middle condensation is input to oil storage tank；
Wherein, the residue of pre-fusion tank is periodically discharged by breast hole in step (1).
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| CN201910656272.XA CN110283617A (en) | 2019-07-19 | 2019-07-19 | A kind of high efficiency Waste plastic treatment apparatus and application method |
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| CN201910656272.XA CN110283617A (en) | 2019-07-19 | 2019-07-19 | A kind of high efficiency Waste plastic treatment apparatus and application method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110627071A (en) * | 2019-11-12 | 2019-12-31 | 四川永祥新能源有限公司 | Polychlorosilane processing apparatus in polycrystalline silicon production |
| WO2023011875A1 (en) | 2021-08-03 | 2023-02-09 | Basell Poliolefine Italia S.R.L. | Plastic depolymerization using silica based catalysts |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1392224A (en) * | 2001-06-14 | 2003-01-22 | 上海市环境工程设计科学研究院 | Oil refining process of waste plastic and equipment |
| CN106281396A (en) * | 2016-08-31 | 2017-01-04 | 蓝德环保科技集团股份有限公司 | Waste plastic cracking equipment and method |
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- 2019-07-19 CN CN201910656272.XA patent/CN110283617A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1392224A (en) * | 2001-06-14 | 2003-01-22 | 上海市环境工程设计科学研究院 | Oil refining process of waste plastic and equipment |
| CN106281396A (en) * | 2016-08-31 | 2017-01-04 | 蓝德环保科技集团股份有限公司 | Waste plastic cracking equipment and method |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110627071A (en) * | 2019-11-12 | 2019-12-31 | 四川永祥新能源有限公司 | Polychlorosilane processing apparatus in polycrystalline silicon production |
| CN110627071B (en) * | 2019-11-12 | 2021-08-10 | 四川永祥新能源有限公司 | Polychlorosilane processing apparatus in polycrystalline silicon production |
| WO2023011875A1 (en) | 2021-08-03 | 2023-02-09 | Basell Poliolefine Italia S.R.L. | Plastic depolymerization using silica based catalysts |
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