CN102041010B - Innocent treatment and oily recovery device of polymer waste - Google Patents
Innocent treatment and oily recovery device of polymer waste Download PDFInfo
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- CN102041010B CN102041010B CN2009101976903A CN200910197690A CN102041010B CN 102041010 B CN102041010 B CN 102041010B CN 2009101976903 A CN2009101976903 A CN 2009101976903A CN 200910197690 A CN200910197690 A CN 200910197690A CN 102041010 B CN102041010 B CN 102041010B
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Abstract
The invention discloses an innocent treatment and oily recovery device of polymer waste, comprising a dry distillation and thermal decomposition system, a high-boiling-point oil recovery system and a low-boiling-point oil recovery system. The innocent treatment and oily recovery device is characterized in that three systems are connected in sequence; finally, oily recovery is carried out on the polymer waste according to difference of boiling points, after the polymer waste is thermally-decomposed by low-temperature dry distillation in the dry distillation and thermal decomposition system, the generated thermal decomposition gas is temperature-controlled and is subjected to backflow by the high-boiling-point oil recovery system so as to realize separation of low-boiling-point oil and high-boiling-point oil; and low-boiling-point is cooled and condensed in the low-boiling-point oil recovery system and then is further recovered as low-boiling-point oil. In the innocent treatment and oily recovery device, the operating efficiency of the equipment is high, the separation and the modification of the low-boiling-point oil and the high-boiling-point oil can be successfully realized, low energy consumption is realized by heat circulation, and therefore, the device disclosed by the invention is a novel innocent treatment and oily recovery device.
Description
Technical field
The present invention relates to a kind of harmless treatment to polymer wastes such as plastic waste, waste rubbers and oiling retrieving arrangement, in particular, relate to a kind of with high molecular waste material by low-temperature pyrolysis Heat of Formation decomposition gas, and high efficiency separation and reclaim the oiling treatment unit of high boiling point oil and lower boiling oil.
Background technology
Resource reutilization is the prerequisite of Sustainable development, and the processing of high molecular waste material and recycling are the recycling research emphasis of resource.High molecular waste material not only comprises the high molecular waste material of the single-materials such as plastics, rubber, and comprises the waste of the composite shape matl of inorganic macromolecule material and the inorganic materials such as metal and pottery.
There has been now corresponding technology that high molecular waste material is recycled, number be that 97182331.6 name is called " method and apparatus for preparing hydro carbons from organic or high molecular waste material " such as Chinese patent application, this application discloses the method that high molecular waste material is resolved into gas, and prepares corresponding hydrocarbon compound; Application number is that 03134178.0 name is called " utilizing high molecular waste material to produce the method for matrix material ", is after high molecular waste material is carried out the modification of chemistry and physics, prepares different matrix materials carrying out different demands.It is relatively ripe that the technology of similar above-mentioned document has developed, and this type of prerequisite with the high molecular waste material recycling is decomposed it exactly, and the decomposition method of above-mentioned technology is comparatively simple, basically so that high molecular waste material is gasified as purpose.Many patent documentations have also been reported the method with the high molecular waste material gasification, but the gas storage after the gasification is inconvenient, and if not using especially targetedly, storage facilities needs sealing, low temperature or do not produce corrosion etc., consumes great amount of cost.
The nearest patent report of the oiling treatment facility of existing many circulations and resource utilization, these equipment technical ways are that the high molecular waste material thermolysis is become gas, and with the Oil recovery of thermolysis gas.Substantially can be divided into the oiling recovery of melting heat decomposition and the oiling of destructive distillation thermolysis reclaims.But the oil content composition that reclaims is comparatively complicated, practicality is not high, if directly can with the oil content Separation and Recovery, for example separate different oil contents according to the difference of boiling point in a whole set of recovery system, carry out harmless treatment, so resulting product using value will be very high.
Summary of the invention
For solving the problems of the technologies described above, the invention provides a kind of running efficiency height, can successfully realize lower boiling oil and the transformation of the way of high boiling point oil separating, by the heat recycle, realize harmless treatment and the oiling retrieving arrangement of the high molecular waste material of less energy-consumption.
The present invention realizes by following technical scheme:
A kind of harmless treatment of high molecular waste material and oiling retrieving arrangement, comprise destructive distillation thermolysis system, high boiling point oil recovery system and lower boiling oil recovery system, it is characterized in that described destructive distillation thermolysis system, high boiling point oil recovery system be connected with the lower boiling oil recovery system and connect, wherein:
Described destructive distillation thermolysis system comprises outer cylinder, heating tank, retort, thermolysis gas pipe arrangement, liquid nitrogen gas tank and nitrogen gas supply pipe arrangement, retort is installed in the heating tank, outer cylinder is arranged on a side of heating tank outside, the liquid nitrogen gas tank is connected with retort by the nitrogen gas supply pipe arrangement, and retort is connected with the high boiling point oil recovery system by thermolysis gas pipe arrangement;
Described high boiling point oil recovery system comprises distillation tower, high boiling point recovery of oil groove, with heat exchanger and the oil circulation pipe arrangement of temperature regulator, described distillation tower is connected with described retort by thermolysis gas pipe arrangement one side, the bottom is connected with described high boiling point recovery of oil groove, the top is connected with described lower boiling oil recovery system, described heat exchanger with temperature regulator is connected with distillation tower by oil circulation pipe arrangement top, and the bottom is connected with high boiling point recovery of oil groove;
Described lower boiling oil recovery system comprises cooling condensing tower, cooling water circulating device and lower boiling recovery of oil groove, described cooling water circulating device is installed on the condensing tower of cooling, and the condensing tower of described cooling connects lower boiling recovery of oil groove by the distillation tower bottom that thermolysis gas pipe arrangement top connects described high boiling point oil recovery system.
Described destructive distillation thermolysis system can also add the catalytic reforming tower and in and scavenging tower, described retort by thermolysis gas pipe arrangement connect successively described catalytic reforming tower and in and scavenging tower.
The retort of described destructive distillation thermolysis system designs for chuck mode, and quantity has 2-6, and wherein during a retort job, other retorts are in holding state.
The heating tank inboard of described destructive distillation thermolysis system is provided with thermofin, and the gas sensing fan machine is set above the described thermofin.
Described destructive distillation thermolysis system is in adding and during scavenging tower, distillation tower one side of described high boiling point oil recovery system with described in be connected with scavenging tower.
The gas escape orifice of the raw material ingress pipe of the distillation tower bottom of described high boiling point oil recovery system is the breach design.
Described heating tank, catalytic reforming tower, in and scavenging tower, distillation tower, high boiling point recovery of oil groove and cool off condensing tower vapor pipe all is set, form exhaust system, gas is discharged atmosphere or is finally connected a gas sweetening roasting kiln.
Described lower boiling recovery of oil groove can also connect fuel distribution tube, fuel is provided for the combustion chamber of described destructive distillation thermolysis system by external device.
Beneficial effect of the present invention is: equipment operating efficiency is high, can successfully realize lower boiling oil and high boiling point oil separating upgrading, by heat recycle realization less energy-consumption, is a kind of harmless treatment and oiling retrieving arrangement of novel high molecular waste material.
Description of drawings
Fig. 1 is the harmless treatment of high molecular waste material and the schema of oiling retrieving arrangement
Fig. 2 is the front elevation of retort in the destructive distillation thermolysis system
Fig. 3 is side elevational view and the vertical view of heating tank and combustion chamber in the destructive distillation thermolysis system
Fig. 4 is the structure iron of distillation tower in the high boiling point oil recovery system
Fig. 5 is that polyacrylic heat decomposition temperature variation diagram is processed in apparatus of the present invention destructive distillation
Embodiment
Such as Fig. 1, the present invention includes destructive distillation thermolysis system, high boiling point oil recovery system and lower boiling oil recovery system, it is characterized in that described destructive distillation thermolysis system, high boiling point oil recovery system be connected with the lower boiling oil recovery system and connect, wherein:
Described destructive distillation thermolysis system comprises outer cylinder 34, heating tank 26, retort 32, thermolysis gas pipe arrangement 28, liquid nitrogen gas tank 22 and nitrogen gas supply pipe arrangement 24, retort 32 is installed in the heating tank 26, outer cylinder 34 is arranged on a side of heating tank 26 outsides, liquid nitrogen gas tank 22 is connected with retort 26 by nitrogen gas supply pipe arrangement 24, and retort 26 is connected with the high boiling point oil recovery system by thermolysis gas pipe arrangement 28;
Described high boiling point oil recovery system comprises distillation tower 44, high boiling point recovery of oil groove 46, with heat exchanger 56 and the oil circulation pipe arrangement 54 of temperature regulator 57, described distillation tower 44 is connected with retort 32 by thermolysis gas pipe arrangement 28 1 sides, the bottom is connected with described high boiling point recovery of oil groove 46, the top is connected with described lower boiling oil recovery system, described heat exchanger 56 with temperature regulator 57 is connected with distillation tower 44 by oil circulation pipe arrangement 54 tops, and the bottom is connected with high boiling point recovery of oil groove 46;
Described lower boiling oil recovery system comprises cooling condensing tower 58, cooling water circulating device 58a and lower boiling recovery of oil groove 60, described cooling water circulating device 58a is installed on the condensing tower 58 of cooling, and the condensing tower 58 of described cooling connects lower boiling recovery of oil groove 60 by distillation tower 44 bottoms that thermolysis gas pipe arrangement 28 tops connect described high boiling point oil recovery system.
More than be that one-piece construction of the present invention is described.
The present invention will be described below in conjunction with each view.
In destructive distillation thermolysis system, can also add catalytic reforming tower 14 and in and scavenging tower 16, retort 32 by thermolysis gas pipe arrangement 28 connect successively described catalytic reforming tower 14 and in and scavenging tower 16.According to the kind of high molecular waste material, catalytic reforming tower 14 and in and scavenging tower 16 can arrange also and can not arrange.When raw material has better pyrolytic, and can generate the thermolysis gas of homogeneous the time, just need not to arrange catalytic reforming tower 14.In addition, if when not containing mineral acid or other pollutant components in the raw material, in just need not to arrange and scavenging tower 16.In whole reactive system, when above-mentioned two devices are not set, retort 32 will directly connect distillation tower 44.When arrange these two when device retort 32 connect first catalytic reforming tower 14, during catalytic reforming tower 14 connects again with upgrading tower 16, in are connected with the upgrading tower and connect again distillation tower 44.
In addition, in equipment implementation state, when the tar component that produces when destructive distillation causes the thermolysis gas pipe arrangement between each reaction unit and even the reaction tower to stop up, special design the quick chilling system that is formed by liquid nitrogen gas tank 22 and the liquid nitrogen supplying tubing 24 that is attached thereto.This quick chilling system is characterised in that and the thermolysis gas cooling in the retort 32 can be liquefied, and the interior pressure of control thermolysis gas pipe arrangement 28, is to avoid it can't rise to the above safety control of specified pressure.
In addition, in equipment implementation state, catalytic reforming tower 14 and in and scavenging tower 16 need successively up and down configuration, and the introducing port of the thermolysis gas of catalytic reforming tower 14 need be arranged on cat head one side.When catalytic reforming tower 14 and in and scavenging tower 16 when disposing on the contrary up and down, be during the introducing port of the thermolysis gas of catalytic reforming tower 14 is arranged on and during the downside of scavenging tower, hydrogenation catalyst, in limited with contacting of thermolysis gas with scavenging agent, can reduce upgrading reaction with in and the efficient of purification.Connect first catalytic reforming tower 14 so the order of connection is retort 32, during catalytic reforming tower 14 connects again and upgrading tower 16, in are connected with the upgrading tower and connect again distillation tower 44.
Destructive distillation thermolysis system realizes high molecular waste material the thermal decomposer system of low-temperature pyrolysis.So-called low-temperature pyrolysis is exactly to stop destructive distillation behind the continuous heating to 600 ℃ to process.
As shown in Figure 2, wherein retort 32 is chuck mode, can be convenient to like this to realize the dismounting between heating tank 26 and the retort 32.Retort 32 is made of the closed cover 32b of still body 32a and pressure resistant type, wherein the paper pulp looped pipeline joint on the closed cover 32b 33 and thermolysis gas pipe arrangement 28 simple connections.The compressive strength of reactor 32 can reach about 1MPa usually.
The interior high H of the inside diameter D of retort 32 and still body 32a has certain proportion requirement.Be the balance that the volume that reaches retort 32 and internal heat are decomposed, the optimum range of general D/H is about 1.2～1.6, is preferably 1.3～1.5, and better is 1.42～1.48.
According to above-mentioned D/H ratio, the general volume scope of retort 32 is 20～6000L, is preferably 50～5000L.When volume was too small, the batch processing amount was less, caused production efficiency lower; Otherwise when volume is excessive, the heat transfer efficiency of donor center section will be reduced to.
The inside diameter D of retort 32 is excessive, will reduce the heat transfer efficiencies of retort 32 central parts, takes advantage of in raw material (such as plastic waste, the waste rubber etc.) thermolysis of the central part of retort 32 not thorough.Otherwise, if the interior high H of retort is too high, also can cause the thermolysis of high molecular waste material at retort 32 tops not thorough.
Therefore, retort 32 generally needs to prepare 2～6.When wherein a retort was worked, other retorts were in holding state, and each retort 32 enters working order needs other external devices to transport.Raw material drop into retort 32 and airtight after, in heating tank 26 by the destructive distillation thermal decomposition process.In the destructive distillation thermal decomposition process, can in the retort 32 of another standby, drop into raw material simultaneously.After finishing etc. initial retort 32 destructive distillation thermal decomposition process, the retort 32 of standby can exchange operation, so basically the continuous operation of implement device.When operating condition was 2 times/day, the number that retort 32 needs was 3; When operating condition was 24 hours continuous operations, the number that retort 32 needs was 4～6.
The heating means of heating tank there is no particular requirement, only need make retort 32 inside be warming up to pyrolysis temperature, can select arbitrarily such as type of heating such as steam heating, electromagnetic induction heating, resistance (electric furnace) heating.
The device that is used for heating mainly comprises outer cylinder 34 and heating tank 26.Combustion chamber 34 is installed in a side of heating tank outside.As described in Figure 3, heating tank 26 inboards are provided with thermofin 36, give prominence to that between the outside of thermofin 36 inboards and retort 32 gas sensing fanner 38 being set, and this gas sensing fanner 38 can form spiral type heated gas flow path P.
When angle of elevation alpha was too small, heated air can not rise smoothly, caused easily the phenomenon of the upper and lower temperature difference of retort 32 bottom high temperature, top low temperature namely to heat non-uniform phenomenon.
Otherwise, when angle of elevation alpha is excessive, cause easily retort 32 bottom low temperature, up and down the phenomenon of the opposite temperature difference.Simultaneously, can cause that also the Exhaust Gas thermosteresis of venting port is excessive, thermo-efficiency is lower.
Such as the vertical view of heating tank among Fig. 3, when the interior girth of heating tank 26 is 4 five equilibriums, just can realize alternately design.The amplitude w of gas sensing fanner 38 is from the about 100～300mm of thermofin 36 beginnings, is preferably 100～200mm, the interior side-prominent setting that gas sensing fanner 38 needs at retort 32.When the amplitude of gas sensing fanner 38 was larger, the external diameter of heating tank 26 is corresponding increase also, thereby caused the heat release area to become the large thermo-efficiency that reduces.
Thermofin 36 usually preferred materials are mixing materials of refractory brick and refractory cements.If only use refractory brick, because the cohesive strength of the tectosome of itself and steel class is lower, cause peeling phenomenon because of bump easily; If only use refractory cements, its heat-proof quality is not good.Therefore, both matrix materials not only have higher impact resistance, and can also guarantee that good heat-proof quality is heat-insulating property.Such as, use the thermal cement layer of 10～30mm in the steel tectosome outside of heating tank 26 outer walls, next use one deck heat resisting brick, re-use at last the thermal cement of 30～50mm, aggregate thickness is about 90～150mm, and its best aggregate thickness is about 100mm.If the thickness of thermofin 36 is too thin, can't guarantee certain heat-proof quality; If instead thickness is too thick, when promoting thermo-efficiency, also can increase the weight of all installation weights of heating tank 26, be unfavorable for actual motion.
The size of outer cylinder 34 is that the size by corresponding quantity combusted decides.The combustion chamber is larger, and flame also increases thereupon, and it is more to disperse heat, and thermo-efficiency is lower.
Such as, burned flame length is 1.2～1.5 times of design height approximately, the width of flame is 1.1～1.5 times of intended diameter approximately.
As shown in figures 1 and 3, outer cylinder 34 preferably is arranged on the tangent line place of heating tank 26 1 sides.Such design can import heated air the above-mentioned gas sensing fanner 38 through heated air ingress pipe 40 from outer cylinder 34, and makes this heat air physical efficiency form screw type stream along the extended line direction of entrance.
In addition, the venting port 42 of heated air is in order to affect the exhaust efficiency of heating tank 26, preferably along the tangential direction setting of the inwall of heating tank 26.
In the high boiling point oil recovery system, mainly comprise distillation tower 44 and high boiling point recovery of oil groove 46.The feature of distillation tower 44 be with by the modification gas behind the hydro-upgrading after cooling distillation and separate lower boiling oil and high boiling point oily.
As shown in Figure 4, the ingress pipe 48 of the raw material of distillation tower 44 (the thermolysis gas that namely destructive distillation obtains from destructive distillation thermolysis system) preferably be arranged on distillation tower 44 device central authorities highly to lower part 1/3～1/2 highly.Along with thermograde, the thermolysis gas of rising forms with refrigeration cycle oil (high boiling point oil) and more contacts cooling, the better effects if of separating like this.
Raw material ingress pipe 48 inserts from the middle body of distillation tower 44, and intubating length is generally 4/5～3/4 of tower body diameter.The gas escape orifice 48a of raw material ingress pipe is the design of top breach normally.The notch length L general range of gas escape orifice 48a is that half of distillation tower 44 internal diameters is to total length.In addition, the common scope of gap width W of gas escape orifice 48a be the raw material ingress pipe internal diameter 1/3～1/2.
The inside of distillation tower 44 alternately need arrange porous plate 49 and the baffle plate 50 of plural number section (hop count is 4～6 sections usually), and the pallet hop count is used for regulating the flow direction of thermolysis gas.
The shape of tray rack comprises perforated metal, sloping baffle, middle baffle plate jaggy etc.General existing using method can both be controlled the flow direction of thermolysis gas.
The volume of distillation tower 44 determines according to the volume of retort 32.(distillation tower 44: retort 32) be generally 1/10～1/2, be preferably volumetric ratio is 1/10～1/5 to the volumetric ratio of distillation tower 44 and retort 32.When volumetric ratio was too small, gas flow can't satisfy the cooling process amount, otherwise when volumetric ratio was excessive, the naturally cooling that causes that sharply expands can cause the high boiling point oil separating incomplete.
The cat head centre of distillation tower 44 arranges distillations outlet 51, is provided with cooling oil spray tube 52 in a side of distillations outlet 51, and these cooling oil spray tube 52 front ends are provided with atomizer 52a.
The bore of distillations outlet 51 is generally 1/10～1/2 of distillation tower 44 internal diameters, is preferably 1/5～1/3.When the bore of distillations outlet 51 less than the distillation tower internal diameter 1/10 the time, the discharging performance of the thermolysis gas that does not condense reduces, thereby causes distillation tower 44 inside to be full of thermolysis gas (inflammable gas).When the bore of distillations outlet 51 greater than the distillation tower internal diameter 1/2 the time, thermolysis gas can't move to lower boiling oil recovery apparatus 20 before distillation tower 44 coolings, thereby has reduced high boiling point oil recovery rate.
In addition, between cooling oil spray tube 52 and high boiling point recovery of oil groove 46, be connected with recycle pump 53 through oil circulation pipe arrangement 54, the heat exchanger 56 with temperature regulator is set in the middle of oil circulation pipe arrangement 54 in addition.When this heat exchanger 56 has surpassed design temperature (such as 80～100 ℃) at cooling oil, the cooling temperature of controlled cooling oil processed.
If cooling oil spray tube 52 is selected 45 ° angle of inclination, just need other middle position at distillation tower 44 that radiation is set and spray possible fog nozzle 52a (for example spraying 90 ° of opening angles), not noncondensing gas relief outlet 44b is set in addition.
In the lower boiling oil recovery system, comprise and cool off condense tower 58 and lower boiling recovery of oil groove 60, wherein cool off the tower 58 that condenses and set up cooling water circulating device 58a.
The outlet of the distillations of distillation tower 44 and the cooling of lower boiling oil recovery system are condensed and are connected by thermolysis gas (being distillations) pipe arrangement 28 between the gas introduction port of tower 58.
In this enforcement state, be to realize the used heat utilization of destructive distillation thermolysis system, the venting port of heating tank 26, catalytic reforming tower 14, in are connected with scavenging tower in addition individual thermal insulation casing of high boiling point recovery of oil groove 46 all by 62 connections of exhaust pipe arrangement.Connecting such as the dotted line among Fig. 1 is exactly the exhaust connected system.In addition, expellant gas from the sleeve pipe 46a of high boiling point recovery of oil groove 46 after being directed into gas sweetening roasting kiln 64, is disposed in the atmosphere.
In addition, the distillation tower 44 of high boiling point oil recovery apparatus 18 and the cooling of lower boiling oil recovery system condense in the tower 58 condense and non coagulation gas can be used as secondary fuel, be directed in the roasting kiln of outer cylinder 34 through fuel distribution tube, perhaps be directed into Fuel Furnace 64 for gas sweetening by exhaust.In addition, the combustion gases that gas sweetening rate of combustion 64 produces also can be realized by exhaust pipe arrangement 62 recycling of heat energy.
In addition, the lower boiling oil of lower boiling recovery of oil groove 60 also can be by arranging fuel distribution tube 61, by external device 65 lower boiling of lower boiling recovery of oil groove 60 oil is imported combustion chamber 34 and use as the fuel of the gaseous combustion stove of thermal decomposer 12, realize heat energy recycle.
Following service condition according to above-mentioned oiling treatment facility will describe harmless treatment and the oiling recovery and treatment method of high molecular waste material in detail:
The high molecular waste material that can drop into retort 32 comprises polyethylene (PE), polypropylene (PP), polystyrene (PS), polyvinyl chloride (PVC), ABS (acrylonitrile-butadiene-styrene copolymer) resin, polyester (such as PET, PBT etc.), various thermoplasticity, the thermosetting plastics such as urethanum, Resins, epoxy, phenolic resin.For keeping carrying out smoothly of thermolysis, the lower plastics varieties of heat decomposition temperature such as preferred PE, PP, PS.In addition, the plastics of other kinds, rubber, leather, coating, tackiness agent etc. all can drop in the retort 32.
When dropping into trade waste in retort 32, this retort can not only be processed has the thermal decomposition performance high molecular waste material, can process too other metals, ceramic and other composite material waste.When retort 32 was provided with utility appliance, the inorganic wastes such as other metals without the destructive distillation thermal decomposition performance beyond the polymer, glass, pottery can drop into as raw material.
The trade waste that can drop into retort comprises: the plastics waste material of damaged tire, useless crawler belt, useless household electrical appliances fragment, scraped car fragment, waste electric wire, Biohazard Waste, useless coating, general combustible waste, moulding, useless container for paint, shoemaking waste, waste fishing net, hulk, mobile phone, useless wiring board, useless X-ray, trade waste solid fuel (REF) etc.
That hydrogenation catalyst in the catalytic reforming tower 14 can be selected is silica-based, alumina type, nickel class, platinum class etc. be as weighting material.In addition, can select lime, burning ash etc. as weighting material with the electrodeless alkaline adsorbent of scavenging tower 16 in.In addition, realize cooling in order to make high boiling point recovery of oil groove in when beginning running, need to fill the limit the quantity of high boiling point oil (the 3rd class oil) of (be generally accumulator tank volume 1/5～1/2) of minimum.The harmless treatment of high molecular waste material and oiling recovery and treatment method:
(1) at first, drop into the oiling materials such as polymer waste such as plastic waste in the retort 32.
(2) with after retort 32 sealings, heating tank 26 is set.After setting completed, light the roasting kiln of outer cylinder 34, the heated air that produces from the combustion chamber is directed in the heating tank 26 and forms spiral type heated gas flow path P, thus indirect heating retort 32.
The span of control of the Heating temperature of retort 32 (temperature in the kettle) is normal temperature to 600 ℃.When the high molecular waste material of processing is oiling that waste electric wire, waste printed circuit board, damaged tire, useless mobile phone, useless X-ray etc. contain the valency metal when processing residue, do not contain the plastic waste composition in the metallic residue in order to make, needing to heat up be heated to 500 ℃.But, if when only processing is hanged down the plastics of heat decomposition temperature such as PE, PP, PS etc., get final product in the time of only need being heated to 450 ℃.
In addition, when processing the polymer waste such as PP (polypropylene), its heat decomposition temperature variation diagram as shown in Figure 5, its heat-up rate is 1～4 ℃/minute, the destructive distillation total ascent time is 5～8 hours.
(3) when the plastic waste in the retort 32 is heated to anaerobic state, after producing water vapour, formed 180～250 ℃ melting (liquefaction) state.
After the melting, continue to be heated to 220～400 ℃ and finish destructive distillation thermolysis (aerification).This thermolysis gas is through thermolysis gas pipe arrangement, be delivered to successively catalytic reforming tower 14 and in and scavenging tower 16.
Catalytic reforming tower 14 is after importing thermolysis gas, and by long chain molecule and the upgrading in the hydrogenation catalyst cut-out raw material, thereby control generates the hydrocarbon compound of certain chain length.Catalytic reforming tower 14 is mainly controlled upgrading temperature of reaction (100～350 ℃) by used heat and the well heater of exhaust.
In and scavenging tower 16 be that upgrading thermolysis gas with the certain chain length after regulating neutralizes, and the device of Adsorption impurity.
(4) next, will through in and the scavenging tower 16 highly purified upgrading thermolysis gas (hydrocarbon compound) after processing be directed in the distillation tower 44 of high boiling point oil recovery apparatus 18.
(5) the distillation tower 44 interior general control temperature of high boiling point oil recovery apparatus 18 are at 50～100 ℃, the optimum control temperature is 60～80 ℃ (high boiling point oil i.e. boiling spreads of the 3rd class oil), and the turning oil in the high boiling point recovery of oil groove 46 sprays from cat head and forms circulation.The temperature of this reaction unit is mainly controlled by the heat exchanger 56 of oil circulation pipe arrangement 54.
Be further to realize rectification effect, thermolysis gas is through after the cooling once, the lower boiling oil component in the high boiling point oil (such as boiling point more than 50 ℃) can be separated and reclaim out.The circulation of refiltered oil only needs just can realize by simple distillation.Can make like this high boiling point oil after the recovery can sneak into hardly the oil (lower boiling oil) of the following boiling point of cooling temperature.
(6) the thermolysis gas after distillation tower 44 cooling liquids (condensing) are processed (lower boiling oil) is by the thermolysis gas pipe arrangement 28 (distillations pipe arrangement) of distillation tower 44 cats head, be directed into the cooling of the setting up cooling water circulating device tower 58 that condenses, condense to water temperature by cooling, finish end boiling point oil recovery.
After lower boiling oil after the recovery entered 60 recovery of lower boiling recovery of oil groove, wherein a part was used as the roasting kiln fuel of the outer cylinder of destructive distillation thermal decomposer.
The volume of the treatment time of the plastic waste in the retort 32 and retort 32 is irrelevant, only needs to guarantee to get final product more than 5 hours.This time has also comprised to retort for subsequent use 32 drops into useless moulding and setup time.In addition, if retort 32 is adopted the methods such as insulation or pre-heated mode (as utilizing solar heat), just can effectively shorten the treatment time.
Thermal decomposition process unloads former retort 32 after finishing, and take retort for subsequent use 32 and heating tank 26 is set, thus the continuous operation of the equipment of realization.
Claims (8)
1. the harmless treatment of a high molecular waste material and oiling retrieving arrangement, comprise destructive distillation thermolysis system, high boiling point oil recovery system and lower boiling oil recovery system, it is characterized in that described destructive distillation thermolysis system, high boiling point oil recovery system be connected with the lower boiling oil recovery system and connect, wherein:
Described destructive distillation thermolysis system comprises outer cylinder, heating tank, retort, thermolysis gas pipe arrangement A, liquid nitrogen gas tank and nitrogen gas supply pipe arrangement, retort is installed in the heating tank, outer cylinder is arranged on a side of heating tank outside, the liquid nitrogen gas tank is connected with retort by the nitrogen gas supply pipe arrangement, and retort is connected with the high boiling point oil recovery system by thermolysis gas pipe arrangement A;
Described high boiling point oil recovery system comprises distillation tower, high boiling point recovery of oil groove, with heat exchanger and the oil circulation pipe arrangement of temperature regulator, described distillation tower is connected with described retort by thermolysis gas pipe arrangement B one side, the bottom is connected with described high boiling point recovery of oil groove, the top is connected with described lower boiling oil recovery system, described heat exchanger with temperature regulator is connected with distillation tower by oil circulation pipe arrangement top, and the bottom is connected with high boiling point recovery of oil groove;
Described lower boiling oil recovery system comprises cooling condensing tower, cooling water circulating device and lower boiling recovery of oil groove, described cooling water circulating device is installed on the condensing tower of cooling, and the condensing tower of described cooling connects lower boiling recovery of oil groove by the distillation tower bottom that thermolysis gas pipe arrangement C top connects described high boiling point oil recovery system.
2. the harmless treatment of high molecular waste material as claimed in claim 1 and oiling retrieving arrangement, it is characterized in that described destructive distillation thermolysis system add the catalytic reforming tower and in and scavenging tower, retort by thermolysis gas pipe arrangement A connect successively described catalytic reforming tower and in and scavenging tower.
3. the harmless treatment of high molecular waste material as claimed in claim 1 and oiling retrieving arrangement, the retort that it is characterized in that described destructive distillation thermolysis system designs for chuck mode, quantity has 2～6, and when wherein a retort was worked, other retorts were in holding state.
4. the harmless treatment of high molecular waste material as claimed in claim 1 and oiling retrieving arrangement is characterized in that the heating tank inboard of described destructive distillation thermolysis system is provided with thermofin, and the gas sensing fan machine is set above the described thermofin.
5. the harmless treatment of high molecular waste material as claimed in claim 1 and oiling retrieving arrangement, it is characterized in that described destructive distillation thermolysis system in adding and during scavenging tower, distillation tower one side of described high boiling point oil recovery system with described in be connected with scavenging tower.
6. the harmless treatment of high molecular waste material as claimed in claim 1 and oiling retrieving arrangement is characterized in that the gas escape orifice of raw material ingress pipe of the distillation tower bottom of described high boiling point oil recovery system is the breach design.
7. the harmless treatment of high molecular waste material as claimed in claim 1 and oiling retrieving arrangement, it is characterized in that described heating tank, catalytic reforming tower, in and scavenging tower, distillation tower, high boiling point recovery of oil groove and cool off condensing tower vapor pipe all is set, form exhaust system, gas is discharged atmosphere or finally connected a gas sweetening roasting kiln.
8. the harmless treatment of high molecular waste material as claimed in claim 1 and oiling retrieving arrangement is characterized in that described lower boiling recovery of oil groove connects fuel distribution tube, fuel are provided for the combustion chamber of described destructive distillation thermolysis system by external device.
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| CN102041010B true CN102041010B (en) | 2013-01-30 |
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| CN102284267A (en) * | 2011-06-01 | 2011-12-21 | 蚌埠市天星树脂有限责任公司 | Reaction kettle with cement outer wall |
| CN105038829B (en) * | 2015-07-10 | 2018-07-27 | 宜宾市永骅环保科技有限责任公司 | A kind of processing system of Biohazard Waste, method and application thereof |
| CN106701122A (en) * | 2017-01-24 | 2017-05-24 | 北京国佳新创科技发展有限公司 | Treatment method of special retirement police garments |
| CN108342226A (en) * | 2018-03-30 | 2018-07-31 | 吴宽永 | A kind of device producing reclaimed oil using pyrolysis of waste vaporized carbon metaplasia |
| CN108410512B (en) * | 2018-04-23 | 2023-09-15 | 中国石油大学(华东) | Solar energy gasification comprehensive utilization system based on all-weather solar energy gasification reactor |
| KR102228583B1 (en) * | 2019-04-30 | 2021-03-16 | 한국에너지기술연구원 | Pyrolysis oil production system from plastic waste and use thereof |
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| CN101328414A (en) * | 2007-12-21 | 2008-12-24 | 杨绍基 | Oiling solvent oil of waste high polymer, novel process and apparatus of lubricating material |
| CN101343137A (en) * | 2008-05-28 | 2009-01-14 | 罗德春 | Method for innocent treatment of bottom oil sludge, scruff and active sludge in petro-chemical industry |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101328414A (en) * | 2007-12-21 | 2008-12-24 | 杨绍基 | Oiling solvent oil of waste high polymer, novel process and apparatus of lubricating material |
| CN101343137A (en) * | 2008-05-28 | 2009-01-14 | 罗德春 | Method for innocent treatment of bottom oil sludge, scruff and active sludge in petro-chemical industry |
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