CN108048200A - Waste oil distills cracking and catalyzing system and production technology - Google Patents
Waste oil distills cracking and catalyzing system and production technology Download PDFInfo
- Publication number
- CN108048200A CN108048200A CN201810090714.4A CN201810090714A CN108048200A CN 108048200 A CN108048200 A CN 108048200A CN 201810090714 A CN201810090714 A CN 201810090714A CN 108048200 A CN108048200 A CN 108048200A
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- China
- Prior art keywords
- waste oil
- level
- collection port
- gaseous constituent
- distillation
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
- C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
- C10M175/0075—Working-up used lubricants to recover useful products ; Cleaning synthetic oil based
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/146—Multiple effect distillation
-
- 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
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
- C10G55/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one catalytic cracking step
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
Abstract
The invention discloses a kind of waste oil distillation cracking and catalyzing system and production technologies, including the level-one distilling apparatus, secondary distillation device and catalytic pyrolysis tower being sequentially communicated, there is gaseous constituent collection port I on the level-one distilling apparatus, on the catalytic pyrolysis tower there is gaseous constituent collection port II and gaseous constituent collection port III, negative pressure generator is connected on the catalytic pyrolysis tower.Cracking and catalyzing system and production technology are distilled using waste oil provided by the invention, structure novel, it is easily achieved, reliability is high, distills cracking and catalyzing system using a set of waste oil, can either be diesel oil by waste oil regeneration, again can will be oily based on waste oil regeneration, equipment purchase and cost of investment is greatly reduced, and site area demand is smaller, the burden of enterprise is effectively reduced, there is high economy and market value.
Description
Technical field
The invention belongs to oil recovery refinery technical fields, and in particular to a kind of waste oil distillation cracking and catalyzing system and production
Technique.
Background technology
The regeneration processing and utilization of waste lubricating oil (used oil) can not only generate huge economic benefit, and environment is protected
The meaning of shield is especially great, can effectively reduce the pollution of air, water source and soil.Therefore, waste lubricating oil is accelerated both at home and abroad
Regenerate the research dynamics of processing and utilization.
At present, regeneration method of used oil is divided into following three classes：1st, method of chemical treatment：Waste lubricating oil through pickling, alkali cleaning neutralize,
Decoloration and etc., it need to pass through for a long time and the reaction of a variety of chemical raw materials could realize waste lubricant oil regeneration, while can generate
The industrial wastes such as substantial amounts of acid sludge cause environmental pollution, therefore method of chemical treatment is a kind of national used oil forbidden in plain text now
Renovation process；2nd, the way of distillation：Traditional way of distillation is commonly called as soil and practices method, is to directly heat used oil to be vaporized evaporation, high temperature
Gaseous mist of oil is condensed into liquid oil content under the cooling effect of condenser and is collected, and greatest problem existing for the way of distillation is institute
The oil content degree of purity of collection low (including a variety of mixing oil contents such as gasoline, diesel oil), easy oxidation discoloration, production efficiency are low etc.；3rd, divide
The sub- way of distillation：Molecularly distilled can overcome the main problem of method of chemical treatment and the way of distillation, still, in three kinds of regenerating waste oils
Device structure employed in technique is the most complicated, and the manufacture and installation of equipment are more difficult, invest huge, operating cost
Height can not meet large-scale waste lubricant oil regeneration process requirements.
Existing a set of distillation cracking and catalyzing system can only produce one group of distillation pyrolysis product, be bavin usually by waste oil regeneration
Oil or base oil, again will be oily based on waste oil regeneration if waste oil regeneration should be diesel oil by an enterprise, then needs two sets
Cracking and catalyzing system is distilled, equipment purchase and cost of investment greatly improved, and site area demand is big, has aggravated enterprise
Burden.Solving problem above becomes the task of top priority.
The content of the invention
For solution more than technical problem, the present invention provides a kind of waste oil distillation cracking and catalyzing system and production technology, can
Two groups of distillation pyrolysis products are produced by switching.
To achieve the above object, technical solution of the present invention is as follows：
A kind of waste oil distills cracking and catalyzing system, including be sequentially communicated level-one distilling apparatus, secondary distillation device and urge
Change cleavage column, be characterized by：On the level-one distilling apparatus there is gaseous constituent collection port I, have on the catalytic pyrolysis tower
There are gaseous constituent collection port II and gaseous constituent collection port III, negative pressure generator is connected on the catalytic pyrolysis tower.
Using more than structure, waste oil is heated in level-one distilling apparatus, from gaseous constituent after the distillation gasification of waste oil part
Collection port I is discharged, and remaining liquid waste oil enters secondary distillation device, these waste oil are further added in secondary distillation device
Heat, distillation gasification obtains gaseous constituent, and enters catalytic pyrolysis tower, and the gaseous constituent cracked is collected respectively from gaseous constituent
Mouth II and gaseous constituent collection port III are discharged；The relatively low lighter component of boiling point is obtained from the collection of gaseous constituent collection port I, from gaseous state
Component collection port II, which is collected, has obtained the lighter component that boiling point is higher than gaseous constituent collection port I, is collected from gaseous constituent collection port III
Heavy component is obtained；When closing negative pressure generator, by controlling temperature, one group of distillation cracking based on diesel oil can be obtained
Product when closing negative pressure generator, by controlling temperature, can obtain another group of distillation cracking production based on base oil
Object；Structure is reliable, and equipment purchase and cost of investment is greatly reduced in easily fabricated and installation, and site area demand is smaller,
The burden of enterprise is effectively reduced, there is high economy and market value.
As preferred：The top of the catalytic pyrolysis tower is divided into low-temperature space and high-temperature region, and the low-temperature space is located at high temperature
Above area, atomising device is provided in the low-temperature space, the negative pressure generator and gaseous constituent collection port II are and low-temperature space
Connection, the gaseous constituent collection port III are connected with high-temperature region.Using more than structure, by the control of atomising device, make catalysis
Low-temperature space and high-temperature region, efficient, good reliability are formed at the top of cleavage column, realize from gaseous constituent collection port II and gaseous state group
Part collection port III discharges two kinds of different gaseous constituents.
As preferred：The gaseous constituent collection port II by condense collecting II successively with condensing tower I and collecting tank
II connection, the collecting tank II are connected by negative pressure line with negative pressure generator, which passes through feed flow circuit and atomization
Device connects.Using more than structure, the condensation for not only having realized lighter component is collected, but also lighter component can be utilized direct to atomising device
Feed flow, without additionally providing liquid supply for atomising device.
As preferred：The gaseous constituent collection port III by condense collecting III successively with condensing tower II and collecting tank
III connection, the collecting tank III for air circuit with secondary distillation device by connecting.Using more than structure, heavy component is both realized
Condensation is collected, and can the gaseous state heavy component in collecting tank III be transported to secondary distillation device, the combustion as secondary distillation device
Material.
As preferred：Preheating oil feed line, heat are provided between the level-one distilling apparatus and secondary distillation device
Feeding pipe and distillation oil feed line, are connected between the secondary distillation device and catalytic pyrolysis tower by gas transfer pipeline；
When waste oil enters level-one distilling apparatus, the gaseous constituent distilled is discharged by gaseous constituent collection port I, and remaining waste oil is through pre-
Hot oil feed line enters the heating of secondary distillation device, and the waste oil after heating is back to level-one distilling apparatus through heat feeding pipe,
As the heat source of level-one distilling apparatus, the waste oil for being back to level-one distilling apparatus turns again to secondary distillation through distilling oil feed line
Device, the gaseous constituent distilled enter catalytic pyrolysis tower through gas transfer pipeline.Using more than structure, pass through each disengaging
Mouth defines the internal structure of level-one distilling apparatus and secondary distillation device, makes level-one distilling apparatus and secondary distillation device with pre-
Hot oil feed line, heat feeding pipe and distillation oil feed line together constitute the specific waste oil secondary molecules of a line clear
Access is distilled, convenient for the concrete structure design and manufacture of level-one distilling apparatus and secondary distillation device.
As preferred：The inside of the level-one distilling apparatus includes level-one distillation chamber and for heating returning for level-one distillation chamber
Flow heat supply chamber；The secondary distillation device includes outer barrel and is arranged on the cartridge heater of the outer barrel, the cartridge heater it is interior
Portion has heat source chamber, and secondary distillation chamber is formed between the outer barrel and cartridge heater；The level-one distillation chamber and heat source chamber pass through pre-
Hot oil feed line connection, the heat source chamber are connected with reflux heat supply chamber by heat feeding pipe, the reflux heat supply chamber and two
Grade distillation chamber is connected by distilling oil feed line.Using more than structure, waste oil is heated in level-one distillation intracavitary, and waste oil part is steamed
It is discharged after evaporating gasification from gaseous constituent collection port I, remaining liquid waste oil flows into heat source chamber, and waste oil is after heat source intracavitary is heated
Reflux heat supply chamber is flowed into, the waste oil in the heat supply chamber that flows back provides heat to level-one distillation chamber, and is the unique of level-one distillation chamber
Origin of heat, flow back heat supply chamber in waste oil flow into secondary distillation chamber, heated in secondary distillation intracavitary by cartridge heater, distillation gasification
Gaseous constituent is obtained, and catalytic pyrolysis tower is introduced from gas transfer pipeline；Level-one distilling apparatus and secondary distillation device can be total to
With a heat source in cartridge heater, energy utilization rate greatly improved, reduce the consumption of the energy, so as to effectively reduce production
Operating cost；The structure novel of level-one distilling apparatus and secondary distillation device, it is simple and reliable, it is easily fabricated, it is of low cost.
As preferred：It is outer on the cartridge heater to be cased with fluid distributor, the barrel of the fluid distributor and cartridge heater it
Between leave gap；After the waste oil on cartridge heater upper surface flows through gap, film-form is formed on the barrel of cartridge heater
Oil reservoir.Using more than structure, by the design of fluid distributor, make between waste oil flowed through between fluid distributor cartridge heater barrel
After gap, it can be attached in film-form on the barrel of cartridge heater, and thickness is uniform, so as to which used oil molecular distillation greatly improved
Efficiency, disclosure satisfy that large-scale waste oil regeneration process requirements, reduce the consumption of the energy, reduce production run cost.
As preferred：Fluid pre-distributor is provided with above the cartridge heater, the lower part tool of the fluid pre-distributor
There is the liquid outlet of a ring shape.Using more than structure, by fluid pre-distributor waste oil can be avoided to pour into the upper end of cartridge heater
Face, but be sprinkled upon in waterfall shape on the upper surface of cartridge heater, so as to coordinate fluid distributor, effectively increase in cartridge heater cylinder
The shaping efficiency of film-form oil reservoir is formed on wall, while prevents waste oil from outwards gushing out happening for fluid distributor.
As preferred：Inner canister is internally provided in the level-one distilling apparatus, between the inner canister and level-one distilling apparatus
The reflux heat supply chamber is formed, the inner cavity of the inner canister is distilled chamber for the level-one, set in the inside of the level-one distilling apparatus
There is blender；After waste oil enters level-one distillation chamber, the oil reservoir of film-form is formed on the inner wall of inner canister by blender.Using
More than structure, simple and reliable for structure, easily fabricated, of low cost, waste oil preheating is efficient, can be rapidly by blender
The oil reservoir of film-form is formed on the inner wall of inner canister, so as to which the efficiency of used oil preheating and molecular distillation greatly improved, is met
Large-scale waste oil regeneration process requirements, reduce the consumption of the energy, reduce production run cost.
A kind of production technology of waste oil distillation cracking and catalyzing, is characterized by, including following methods：
Method a, negative pressure generator is closed, the temperature of gaseous constituent collection port I is controlled to control gaseous state for 100 DEG C~150 DEG C
The temperature of component collection port II is 150 DEG C~260 DEG C, controls the temperature of gaseous constituent collection port III as 380 DEG C~420 DEG C, with
Obtain first group of distillation pyrolysis product；
Method b, negative pressure generator is opened, the temperature of gaseous constituent collection port I is controlled to control gaseous state for 100 DEG C~180 DEG C
The temperature of component collection port II is 150 DEG C~200 DEG C, controls the temperature of gaseous constituent collection port III as 220 DEG C~320 DEG C, with
Obtain second group of distillation pyrolysis product.
Using above method, collected by the opening and closing and gaseous constituent collection port I, gaseous constituent that control negative pressure generator
The temperature of mouth II and gaseous constituent collection port III, can obtain two groups of different distillation pyrolysis products；Wherein, method a, energy are passed through
It is enough to collect water and gasoline from gaseous constituent collection port I, light diesel fuel is collected from gaseous constituent collection port II, from gaseous constituent collection port
III collects heavy diesel fuel, and light diesel fuel and heavy diesel fuel account for producing the 85%~92% of object；By method b, can be received from gaseous constituent
Collect mouth I and collect water, gasoline and diesel oil, collect diesel oil from gaseous constituent collection port II, basis is collected from gaseous constituent collection port III
Oil, base oil account for producing the 75%~80% of object, and the lighter component based on petrol and diesel oil accounts for producing the 8%~12% of object；So as to
It realizes and distills cracking and catalyzing system using a set of waste oil, can either be diesel oil by waste oil regeneration, and can be base by waste oil regeneration
Plinth oil.
Compared with prior art, the beneficial effects of the invention are as follows：
Cracking and catalyzing system and production technology, structure novel are distilled using waste oil provided by the invention, it is easy to accomplish, reliably
Property it is high, distill cracking and catalyzing system using a set of waste oil, can either be diesel oil by waste oil regeneration, and can be base by waste oil regeneration
Plinth oil, is greatly reduced equipment purchase and cost of investment, and site area demand is smaller, is effectively reduced the burden of enterprise,
With high economy and market value.
Description of the drawings
Fig. 1 is the schematic diagram of the present invention；
Fig. 2 is the external structure schematic diagram of secondary distillation device；
Fig. 3 is the internal structure schematic diagram of secondary distillation device；
Fig. 4 is the enlarged drawing at A in Fig. 3；
Fig. 5 is the structure diagram of fluid pre-distributor；
Fig. 6 is the structure diagram of level-one distilling apparatus；
Fig. 7 is the structure diagram of catalytic pyrolysis tower.
Specific embodiment
The invention will be further described with attached drawing with reference to embodiments.
Refer to Fig. 1, a kind of waste oil distills cracking and catalyzing system, is steamed including the level-one distilling apparatus 2 that is sequentially communicated, two level
Distillation unit 1 and catalytic pyrolysis tower 3 have gaseous constituent collection port I 23, the catalytic pyrolysis tower 3 on the level-one distilling apparatus 2
It is upper that there is gaseous constituent collection port II 31 and gaseous constituent collection port III 32, it is connected with negative pressure generator on the catalytic pyrolysis tower 3
33。
It is emphasized that level-one distilling apparatus 2 can be arranged on the inside of catalytic pyrolysis tower 3, closed with catalytic pyrolysis tower 3
And be a device, similary level-one distilling apparatus 2 can also be separated with catalytic pyrolysis tower 3, split level-one distilling apparatus 2 and catalysis
Solution tower 3 is two independent devices.Such design substantially increases the flexibility of equipment installation and sale.
Fig. 1 and Fig. 7 are referred to, the top of the catalytic pyrolysis tower 3 is divided into low-temperature space 35 and high-temperature region 36, the low temperature
Area 35 is located at 36 top of high-temperature region, and atomising device 34, the negative pressure generator 33 and gaseous state group are provided in the low-temperature space 35
Part collection port II 31 is connected with low-temperature space 35, and the gaseous constituent collection port III 32 is connected with high-temperature region 36.
Specifically, the gaseous constituent collection port II 31 by condense collecting II 808 successively with condensing tower I 42 and
Collecting tank II 52 connects, and gaseous state lighter component is condensed into liquid on condensing tower I 42, is then collected by collecting tank II 52.
Further, the collecting tank II 52 is connected by feed flow circuit 811 with atomising device 34, using lighter component to mist
34 direct feed flows are put in makeup, without being additionally that atomising device 34 provides liquid supply.Also, it is provided on feed flow circuit 811
For the pressure oil pump I 61 of supercharging.
Further, the collecting tank II 52 is connected by negative pressure line 810 with negative pressure generator 33, the negative pressure generator
33 preferably using vacuum pump, reliable and stable, of low cost.Also, at least one surge tank is provided in negative pressure line 810
54, to ensure the stability of negative pressure state.
Refer to Fig. 1, the gaseous constituent collection port III 32 by condense collecting III 809 successively with condensing tower II 43
It is connected with collecting tank III 53, gaseous state heavy component is condensed into liquid on condensing tower II 43, is then collected by collecting tank III 53.
Further, the collecting tank III 53, can be by collecting tank by being connected for air circuit 812 with secondary distillation device 1
Gaseous state heavy component in III 53 is transported to secondary distillation device 1, the fuel as secondary distillation device 1.It is pointed out that
For being provided with water seal 71 and spark arrester 72 on air circuit 812, the security of supply is substantially increased.
Further, the catalytic pyrolysis tower 3 is connected by fluid circuit 813 with preheating oil feed line 801, will be uncracked
Component be recycled to preheating oil feed line 801, carry out molecular distillation again by level-one distilling apparatus 2 and secondary distillation device 1,
The conversion ratio of waste oil recycling greatly improved.Also, cooling device 77 is provided on fluid circuit 813, so as to be recycled back to
It is liquid component to preheat oil feed line 801, ensures the normal operation of whole system.
Fig. 1~Fig. 6 is referred to, the inside of the level-one distilling apparatus 2 includes level-one distillation chamber 21 and reflux heat supply chamber 22,
Reflux heat supply chamber 22 can be coated on the outside of level-one distillation chamber 21, can also be located at the inside of level-one distillation chamber 21, can be with
It is other structures, as long as reflux heat supply chamber 22 can be level-one, distillation chamber 21 provides heat.On the level-one distilling apparatus 2
It is provided with the gaseous constituent collection port I 23 connected with level-one distillation chamber 21.The secondary distillation device 1 includes outer barrel 11 and sets
The cartridge heater 12 inside the outer barrel 11 is put, secondary distillation chamber 13, the outer barrel are formed between the outer barrel 11 and cartridge heater 12
The gas vent 113 connected with secondary distillation chamber 13 is provided on 11, the gas vent 113 by gas transfer pipeline 806 with
Catalytic pyrolysis tower 3 connects.The inside of the cartridge heater 12 has heat source chamber 121.The level-one distillation chamber 21, heat source chamber 121 return
Stream heat supply chamber 22 and secondary distillation chamber 13 are sequentially communicated by pipeline, when waste oil is followed by level-one distillation chamber 21, heat source chamber
121st, flow back after heat supply chamber 22 and secondary distillation chamber 13, the gaseous constituent distilled is by gaseous constituent collection port I 23 and gas
113 discharge of outlet.
Specifically, waste oil is heated in level-one distillation chamber 21, at this point, from gaseous constituent after the distillation gasification of waste oil part
Collection port I 23 is discharged, and remaining liquid waste oil flows into heat source chamber 121, and waste oil flows into reflux after being heated in heat source chamber 121 and supplies
Hot chamber 22, hotter waste oil provides heat to level-one distillation chamber 21 in reflux heat supply chamber 22, and be level-one distillation chamber 21 only
One origin of heat, the waste oil in reflux heat supply chamber 22 flow into secondary distillation chamber 13, in secondary distillation chamber 13 by cartridge heater 12 plus
Heat, distillation gasification obtains gaseous constituent, and is discharged from gas vent 113, and catalytic pyrolysis tower 3 is introduced through gas transfer pipeline 806.
More into specifically, on the level-one distilling apparatus 2 having, fluid exports 27, reflux heat supply import 221, reflux supplies
Heat outlet 222 and gaseous constituent collection port I 23, have on the secondary distillation device 1 preheating inlet 124, preheating outlet 125,
Distill import 112 and gas vent 113.
Preheating oil feed line 801, the preheating outlet 125 are connected between the fluid outlet 27 and preheating inlet 124
Be connected with heat feeding pipe 802 between reflux heat supply import 221, the reflux heat supply outlet 222 and distillation import 112 it
Between be connected with distillation oil feed line 803.
When waste oil enters level-one distilling apparatus 2, the gaseous constituent distilled is discharged by gaseous constituent collection port I 23, is remained
The preheated oil feed line 801 of remaining waste oil is heated into secondary distillation device 1, and the waste oil after heating is through heat feeding pipe 802
Level-one distilling apparatus 2 is back to, as the heat source of level-one distilling apparatus 2, the waste oil for being back to level-one distilling apparatus 2 is supplied through distillation
Oil pipe line 803 turns again to secondary distillation device 1, and the gaseous constituent distilled is discharged by gas vent 113, is conveyed through gas
Pipeline 806 introduces catalytic pyrolysis tower 3.
As shown in Fig. 2~Fig. 5, the concrete structure of the secondary distillation device 1 is as follows：
Fig. 2 and Fig. 3 are referred to, the secondary distillation device 1 includes outer barrel 11 and is arranged on adding inside the outer barrel 11
Hot cylinder 12, the inside of the cartridge heater 12 have heat source chamber 121, secondary distillation chamber are formed between the outer barrel 11 and cartridge heater 12
13, the preheating inlet 124 and preheating outlet 125 are connected with heat source chamber 121, and the distillation import 112 and gaseous constituent are collected
Mouth II 113 is connected with heat source chamber 121.
Fig. 3 is referred to, the cartridge heater 12 is columnar tank structure, internal to form the heat source chamber 121, should be added
The lower end of hot cylinder 12 is pierced by outer barrel 11, is provided with heat source import 123 on the cartridge heater 12 and is connected with heat source chamber 121
Smoke discharge tube 122, wherein, the heat source import 123 is located at the lower end of cartridge heater 12, the heat source import 123 and burner 73
It is connected, it should be pointed out that the outlet for air circuit 812 is located near heat source import 123, and position is reasonable, using abundant
Burning.The smoke discharge tube 122 is located at the upper end of cartridge heater 12, and the burner 73 provides hot gas into cartridge heater 12, and
Hot gas is finally discharged from smoke discharge tube 122.The design that so heat is propagated from the bottom up can improve heat source to cartridge heater 12
The efficiency of heating surface of barrel and pre-add heat pipe 16 improves the utilization ratio of the energy.The inlet end installation of the smoke discharge tube 122
It is connected in the upper surface of cartridge heater 12, and with heat source chamber 121, also, the smoke discharge tube 122 first upwardly extends outward bending again
" L " shape, and ultimately out outer barrel 11 are formed, installation fluid pre-distributor 14 is designed to facilitate as smoke discharge tube 122.
Pre-add heat pipe 16 is equipped in the cartridge heater 12, is equipped with what is be distributed in a spiral manner in the heat source chamber 121
Pre-add heat pipe 16, one end of the pre-add heat pipe 16 are connected by preheating oil feed line 801 and level-one distillation chamber 21, and the other end passes through
Heat feeding pipe 802 is connected with reflux heat supply chamber 22.It is pointed out that the input end of pre-add heat pipe 16 is located at the port of export
Lower section, such design can further improve the efficiency of preheating waste oil.Therefore, the preheating oil feed line 801 is through outer barrel 11
Insertion cartridge heater 12 is connected with the input end of pre-add heat pipe 16；The heat feeding pipe 802 is inserted into cartridge heater 12 through outer barrel 11
It is connected with the port of export of pre-add heat pipe 16.
Refer to Fig. 2 and Fig. 3, the outer barrel 11 is columnar tank structure, and the bottom wall 111 of the outer barrel 11 is from outer barrel 11
Side wall extend to the barrel of cartridge heater 12 obliquely, up-small and down-big cone structure is formed, under 11 side wall of outer barrel
End is provided with slag notch 115, even if making the impurity such as remaining heavy oil, pitch in secondary distillation chamber 13 non-stop-machine in complete equipment
In the case of can also discharge, not only maintained the cleannes of secondary distillation chamber 13, but also improved the efficiency of waste oil molecular distillation.And
And be connected in slag notch 115 by pipeline 805 of slagging tap with waste residue collecting box 74, in order to centralized collection and processing heavy oil, pitch
Wait impurity.
Gaseous constituent collection port II 113 is provided on the outer barrel 11, the gaseous constituent collection port II 113 is located at outer
The upper end of cylinder 11, in favor of the discharge of gaseous constituent.The distillation distillation import 112 of the oil feed line 803 through outer barrel 11 is inserted into
In secondary distillation chamber 13, and the oil outlet for distilling oil feed line 803 is located at the top of 12 upper surface of cartridge heater, can draw waste oil
To the upper surface of cartridge heater 12, in order to form the oil reservoir of film-form on the barrel of cartridge heater 12.Also, in the outer barrel 11
Lower part be provided with oil return opening 114, the position of the oil return opening 114 is less than the upper surface of cartridge heater 12, and higher than slag notch 115
Position, it should be pointed out that the position of oil return opening 114 is unsuitable excessively high, in order to avoid influence the film-form formed on 12 barrel of cartridge heater
The area of oil reservoir, so as to ensure that the efficiency of molecular distillation.In addition, the oil return opening 114 is supplied by oil return line 804 and distillation
Oil pipe line 803 connects, and realizes the cycling supplement of waste oil.Fuel reserve tank 75 is provided on the oil return line 804, in the fuel reserve tank
Liquid level gauge 76 is installed, the supply that can realize fluid by fuel reserve tank 75 is adjusted, and further prevents secondary distillation chamber 13 on 75
The fluid of bottom accumulation is excessive, meanwhile, the oil mass in fuel reserve tank 75 can be accurately known by liquid level gauge 76, is that this is opened with control
Fuel reserve tank 75 is opened to distillation 803 fuel feeding of oil feed line or opens reflux heat supply chamber 22 to distillation 803 fuel feeding of oil feed line.
Fig. 3 and Fig. 4 are referred to, fluid distributor 15 is installed in the upper end of the cartridge heater 12, the fluid distributor
Gap 17 is left between 15 and the barrel of cartridge heater 12, makes the waste oil that 12 upper surface of cartridge heater is led to from distillation oil feed line 803
Flow through the oil reservoir for forming film-form behind gap 17 on the barrel of cartridge heater 12.Specifically, the fluid distributor 15 is circle
Annular, and be sleeved on beyond cartridge heater 12, between formation is described between the inner wall of the fluid distributor 15 and the barrel of cartridge heater 12
Gap 17, also, the upper limb of the fluid distributor 15 is higher than the upper surface of cartridge heater 12, and lower edge is less than the upper surface of cartridge heater 12,
It can effectively prevent that the waste oil positioned at 12 upper surface of cartridge heater from outwards gushing out, and enables waste oil to continue efficiently in cartridge heater 12
The fluid layer of film-form is formed on barrel.In addition, the lower edge of fluid distributor 15 inwardly narrows, make to be formed on 12 barrel of cartridge heater
Film-form core intersection it is thinner, so as to further improve the molecular distillation efficiency of waste oil.
Fig. 3 and Fig. 5 are referred to, the top of the cartridge heater 12 is provided with fluid pre-distributor 14, which is distributed in advance
The lower part of device 14 has the liquid outlet 141 of a ring shape, and the oil outlet of the distillation oil feed line 803 is located at fluid pre-distributor
14 inside.Specifically, the fluid pre-distributor 14 includes the collection portion 143 of discoidal mounting portion 142 and circular ring shape,
The mounting portion 142 and collection portion 143 surround the tubular structure to form open topped, and the liquid outlet 141 takes shape in collection portion
Between 143 lower edge and the outer rim of mounting portion 142.Also, the mounting portion 142 is set on smoke discharge tube 122, and installation is held
Easily, it is reliable and stable.The distillation oil feed line 803 is inserted into from the open-mouth of fluid pre-distributor 14.
Fig. 1 and Fig. 6 are referred to, the concrete structure of the level-one distilling apparatus 2 is as follows：
Inner canister 24 is internally provided in level-one distilling apparatus 2, shape between the inner canister 24 and the inner wall of level-one distilling apparatus 2
Into the reflux heat supply chamber 22, chamber 21 is distilled in the inner cavity of the inner canister 24 for the level-one.In the level-one distilling apparatus 2
Portion is provided with blender 25, in the blender 25 insertion level-one distillation chamber 21, after waste oil enters level-one distillation chamber 21, by stirring
The oil reservoir that device 25 forms film-form on the inner wall of inner canister 24 is mixed, the effect of waste oil preheating and lighter component distillation gasification greatly improved
Rate.
Further, Fig. 1 is referred to, the gaseous constituent collection port I 23 is by condensing collecting I 807 successively with changing
Hot device 41 is connected with collecting tank I 51, and gaseous state lighter component is condensed into liquid on heat exchanger 41, is then collected by collecting tank I 51.
Fig. 6 is referred to, the bottom of the reflux heat supply chamber 22 has reflux heat supply import 221, and top has reflux heat supply
Outlet 222, the reflux heat supply import 221 are connected by heat feeding pipe 802 with the port of export of pre-add heat pipe 16, described time
Stream heat supply outlet 222 is connected with distillation oil feed line 803.
The level-one distilling apparatus 2 has fluid import 26 and fluid outlet 27, and the fluid import 26 is located at level-one steaming
The upper end of distillation unit 2, fluid outlet 27 are located at the lower end of level-one distilling apparatus 2, and the fluid outlet 27 passes through pipeline and pre-add
The input end connection of heat pipe 16.
Fig. 6 is referred to, the pressure oil pump II 62 for supercharging is provided on preheating oil feed line 801, in oil return line
The pressure oil pump III 63 for supercharging is provided on 804, to provide the pressure of fluid flowing.
Further, check valve is mounted on each pipeline, to prevent backflow, while cutting convenient for control piper
It changes.
A kind of production technology of waste oil distillation cracking and catalyzing, which is characterized in that including following methods：
Method a, negative pressure generator 33 is closed, controls the temperature of gaseous constituent collection port I 23 as 100 DEG C~150 DEG C, control
The temperature of gaseous constituent collection port II 31 be 150 DEG C~260 DEG C, control gaseous constituent collection port III 32 temperature be 380 DEG C~
420 DEG C, to obtain first group of distillation pyrolysis product.
It, can be from the lighter component that gaseous constituent collection port I is collected mainly comprising water and gasoline, from gaseous state group by method a
Part collection port II collects light diesel fuel, collects heavy diesel fuel from gaseous constituent collection port III, light diesel fuel and heavy diesel fuel account for producing object
85%~92%, residue 8%~12%.
Method b, negative pressure generator 33 is opened, controls the temperature of gaseous constituent collection port I 23 as 100 DEG C~180 DEG C, control
The temperature of gaseous constituent collection port II 31 be 150 DEG C~200 DEG C, control gaseous constituent collection port III 32 temperature be 220 DEG C~
320 DEG C, to obtain second group of distillation pyrolysis product.
By method b, water, gasoline and diesel oil etc. can be mainly included from the lighter component that gaseous constituent collection port I is collected, from
Gaseous constituent collection port II collects diesel oil, collects base oil from gaseous constituent collection port III, base oil accounts for producing the 75% of object
~80%, the lighter component based on petrol and diesel oil accounts for producing the 8%~12% of object, residue 5%~8%.
Finally it should be noted that foregoing description is only the preferred embodiment of the present invention, the ordinary skill people of this field
Member on the premise of without prejudice to present inventive concept and claim, can make table as multiple types under the enlightenment of the present invention
Show, such conversion is each fallen within protection scope of the present invention.
Claims (10)
1. a kind of waste oil distills cracking and catalyzing system, including level-one distilling apparatus (2), the secondary distillation device (1) being sequentially communicated
With catalytic pyrolysis tower (3), it is characterised in that：There is gaseous constituent collection port I (23) on the level-one distilling apparatus (2), it is described
There is gaseous constituent collection port II (31) and gaseous constituent collection port III (32), the catalytic pyrolysis tower (3) on catalytic pyrolysis tower (3)
On be connected with negative pressure generator (33).
2. waste oil according to claim 1 distills cracking and catalyzing system, it is characterised in that：The catalytic pyrolysis tower (3)
Top is divided into low-temperature space (35) and high-temperature region (36), and the low-temperature space (35) is located above high-temperature region (36), in the low-temperature space
(35) it is provided with atomising device (34) in, the negative pressure generator (33) and gaseous constituent collection port II (31) are and low-temperature space
(35) connect, the gaseous constituent collection port III (32) connects with high-temperature region (36).
3. waste oil according to claim 2 distills cracking and catalyzing system, it is characterised in that：The gaseous constituent collection port II
(31) connected successively with condensing tower I (42) and collecting tank II (52) by condensing collecting II (808), the collecting tank II
(52) connected by negative pressure line (810) with negative pressure generator (33), which passes through feed flow circuit (811) and mist
(34) connection is put in makeup.
4. waste oil according to claim 2 distills cracking and catalyzing system, it is characterised in that：The gaseous constituent collection port III
(32) connected successively with condensing tower II (43) and collecting tank III (53) by condensing collecting III (809), the collecting tank III
(53) by being connected for air circuit (812) with secondary distillation device (1).
5. waste oil according to any one of claims 1 to 4 distills cracking and catalyzing system, it is characterised in that：Described one
Grade distilling apparatus (2) and secondary distillation device (1) between be provided with preheat oil feed line (801), heat feeding pipe (802) and
Oil feed line (803) is distilled, passes through gas transfer pipeline (806) between the secondary distillation device (1) and catalytic pyrolysis tower (3)
Connection；
When waste oil enters level-one distilling apparatus (2), the gaseous constituent distilled is discharged by gaseous constituent collection port I (23), is remained
The preheated oil feed line of remaining waste oil (801) is heated into secondary distillation device (1), and the waste oil after heating is through heat feeding pipe
(802) level-one distilling apparatus (2) is back to, as the heat source of level-one distilling apparatus (2), is back to level-one distilling apparatus (2)
Waste oil turns again to secondary distillation device (1) through distilling oil feed line (803), and the gaseous constituent distilled is through air shooter
Road (806) enters catalytic pyrolysis tower (3).
6. waste oil according to claim 5 distills cracking and catalyzing system, it is characterised in that：The level-one distilling apparatus (2)
Inside include level-one distillation chamber (21) and for heat level-one distillation chamber (21) reflux heat supply chamber (22)；
The secondary distillation device (1) includes outer barrel (11) and is arranged on the internal cartridge heater (12) of the outer barrel (11), described
The inside of cartridge heater (12) has heat source chamber (121), and secondary distillation chamber is formed between the outer barrel (11) and cartridge heater (12)
(13)；
The level-one distillation chamber (21) is connected with heat source chamber (121) by preheating oil feed line (801), the heat source chamber (121)
It is connected with reflux heat supply chamber (22) by heat feeding pipe (802), the reflux heat supply chamber (22) and secondary distillation chamber (13)
It is connected by distilling oil feed line (803).
7. waste oil according to claim 6 distills cracking and catalyzing system, it is characterised in that：It is outer on the cartridge heater (12)
Fluid distributor (15) is cased with, gap (17) is left between the fluid distributor (15) and the barrel of cartridge heater (12)；
After the waste oil on cartridge heater (12) upper surface flows through gap (17), film is formed on the barrel of cartridge heater (12)
The oil reservoir of shape.
8. waste oil according to claim 6 distills cracking and catalyzing system, it is characterised in that：In the upper of the cartridge heater (12)
Side is provided with fluid pre-distributor (14), and the lower part of the fluid pre-distributor (14) has the liquid outlet (141) of a ring shape.
9. waste oil according to any one of claims 1 to 4 distills cracking and catalyzing system, it is characterised in that：Described one
Grade distilling apparatus (2) is internally provided with inner canister (24), and the reflux is formed between the inner canister (24) and level-one distilling apparatus (2)
Heat supply chamber (22), the inner cavity of the inner canister (24) are distilled chamber (21) for the level-one, are set in the inside of the level-one distilling apparatus (2)
It is equipped with blender (25)；
After waste oil enters level-one distillation chamber (21), the oil of film-form is formed on the inner wall of inner canister (24) by blender (25)
Layer.
10. a kind of production technology of waste oil distillation cracking and catalyzing, which is characterized in that including following methods：
Method a, negative pressure generator (33) is closed, controls the temperature of gaseous constituent collection port I (23) as 100 DEG C~150 DEG C, control
The temperature of gaseous constituent collection port II (31) is 150 DEG C~260 DEG C, and the temperature for controlling gaseous constituent collection port III (32) is 380
DEG C~420 DEG C, to obtain first group of distillation pyrolysis product；
Method b, negative pressure generator (33) is opened, controls the temperature of gaseous constituent collection port I (23) as 100 DEG C~180 DEG C, control
The temperature of gaseous constituent collection port II (31) is 150 DEG C~200 DEG C, and the temperature for controlling gaseous constituent collection port III (32) is 220
DEG C~320 DEG C, to obtain second group of distillation pyrolysis product.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116426314A (en) * | 2023-05-16 | 2023-07-14 | 重庆工商大学 | Method for catalytically thermally cracking industrial waste oil by microwaves |
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