CN1019985C - Apparatus and method for reclaiming waste oil - Google Patents
Apparatus and method for reclaiming waste oil Download PDFInfo
- Publication number
- CN1019985C CN1019985C CN89108168A CN89108168A CN1019985C CN 1019985 C CN1019985 C CN 1019985C CN 89108168 A CN89108168 A CN 89108168A CN 89108168 A CN89108168 A CN 89108168A CN 1019985 C CN1019985 C CN 1019985C
- Authority
- CN
- China
- Prior art keywords
- oil
- waste oil
- evaporable
- boiler
- equipment
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Images
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
- C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
-
- 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
- C10M175/0025—Working-up used lubricants to recover useful products ; Cleaning by thermal processes
Abstract
An apparatus and a method are provided for reclaiming a useful oil product from waste oil, such as used lubricating oil. The apparatus comprises an oil feed means, a boiler, a heater and separating means. The heater is used to heat the waste oil in the boiler to a temperature such that lighter hydrocarbons of the waste oil volatilize, but such that heavier hydrocarbons remain unvolatilized, trapping contaminants therewith. The separating means separates the volatilized lighter hydrocarbons from the unvolatilized heavier hydrocarbons and contaminants.
Description
The present invention puts it briefly and relates to be used for the equipment and the method for reclaiming waste oil, more precisely is to be used for removing being present in the waste oil and waste oil being unsuitable for as heating fuel again the equipment of the various impurity of diesel oil etc. and method.
In this specification sheets, term " waste oil " is meant used automotive engine oil or some other lubricating oil, or hydraulic efficiency oil or the oil in other these classes application at some.In use, these oil will be replaced termly, and the waste oil of discharging and reclaiming contains a large amount of impurity usually, these impurity comprise greasy filth, metal particle (comprises heavy metal, molybdenum for example, chromium, cadmium, vanadium, copper or the like), oxide compound and salt, gasoline and gasoline dope (as tetraethyl lead), and purification agent and performance additive.
In North America, to produce millions of gallons this waste oil every year.In the past, waste oil is used for reducing dust on dirt road, or directly pours in the sewer line or made ground.Yet this treatment process it seems and more and more can not accept that reason is that hydrocarbon has polluted environment.Waste oil is re-refined and is entered the practical stage to a certain extent.Yet the method for the known waste oil that is used to re-refine need be carried out complex chemical treatment, usually, can not produce high-grade products.In addition, trucking costs also makes the practicality of this processing waste oil method be affected.
In the past, once the someone advised making heating fuel with waste oil, yet, do not succeed with the process furnace of the known type this oil that burns.Usually, when Waste-oil combustion, resistates accumulates in the burner, and resistates has formed various impurity, and heavy hydrocarbon has formed hard tackifying resin.The result is, must often remove the hard resistates that gathers on the burner, usually, and twice of every day.In order to clear up burner, stove must be out of service, allows its cooling, and this is very inconvenient, and it is low mainly to show as efficient.And the resistates of removing refrigerative hardening on the burner is the task of a difficulty, usually, needs the able-bodied laborer.
The objective of the invention is to overcome or slacken the shortcoming of state of the art.
First aspect the invention provides the equipment that obtains the useful oil product from waste oil regeneration.This equipment comprises: refueling device, boiler, well heater and tripping device.Refueling device is used for waste oil is added in this equipment, and boiler links to each other with refueling device, with the waste oil that is fit to accept to come from refueling device.Well heater is used for the waste oil in the heating boiler, reaches to make in the waste oil than the light hydrocarbon volatilization, but than the still nonvolatile temperature of heavy hydrocarbon, captures impurity with this.Tripping device is separated evaporable from nonvolatile than light hydrocarbon than heavy hydrocarbon and impurity.Have been found that surprisingly this equipment provides a kind of and removed the simple of impurity and effective device from waste oil,
And produced the clean oil production that in various application, (can be used as heating fuel or diesel-fuel especially) and be suitable for recirculation.
The well heater of aforesaid device preferably includes an oil-firing burner, and this burner links to each other with tripping device, is used for accepting the waste oil from tripping device, and burning derives from the oil salvage part of evaporable than light hydrocarbon.Boiler preferably becomes one with tripping device, boiler comprise be suitable for discharging evaporable than first vent pipe of light hydrocarbon be suitable for discharging nonvolatile second vent pipe than heavy hydrocarbon and impurity.This equipment preferably also comprises a condenser, is used for evaporable is condensed into regenerated petroleum liquid product than light hydrocarbon.In addition, comprise a recovered oil storage tank, be used for gathering and preserve the said products and a sludge jar, be used for storing isolated nonvolatile than heavy hydrocarbon and impurity so that regularly get rid of.
Second aspect, the invention provides a kind of method of handling waste oil, the method comprising the steps of: the waste oil in the boiler is heated to makes volatilizing than light hydrocarbon of waste oil, but than the nonvolatile temperature of heavy hydrocarbon, capture impurity with this, then evaporable is separated than heavy hydrocarbon and impurity from nonvolatile than light hydrocarbon.Preferred temperature range is about 600～800 °F, and preferably temperature is 650 °F.Preferably then evaporable is condensed into regenerated liquid oil product than light hydrocarbon, incites somebody to action wherein at least a portion oil firing then, come waste oil other in the heating boiler.
The invention provides a kind of safety, effectively, the device of general processing waste oil, this device has gone out a kind of useful petroleum products from waste oil regeneration, and this petroleum products has multiple use, in particular as heating fuel or diesel-fuel.Still must handle from the sludge by product that obtains than heavy hydrocarbon and impurity, yet this sludge is usually only for being added to about 1/10th of waste oil volume in this equipment.In some cases, the metal values of might from sludge, regenerating.
Equipment of the present invention just can be produced and be operated with the sub-fraction of the installation cost of re-refining.Therefore, industrial and commercial sector's (for example, the car service station) and other departments that stores a large amount of waste oil can utilize waste oil as valuable by product, and it need not be disposed.In order better to understand the present invention, the present invention will be described for description, wherein:
Fig. 1 is the schema of the embodiment of expression present device;
Fig. 2 is the schema of the another embodiment of expression present device;
Fig. 3 is the top view (plane that 3-3 along the line represents is cut open) of the equipment component of presentation graphs 2.
At first with reference to the equipment of figure 1, this equipment comprises the closed structure 10 of second Room 12 of first Room 11 that is provided with base closed and base closed.In fact, first Room 11 and the second Room common wall 13 of 12 usefulness are spaced from each other substantially, but they can interconnect by the perforate on the wall 13 14.Fire-box 15 in first Room 11 is made up of the distillation boiler 18 of independent combustion chamber 16 that comprises burner 17 and heating waste oil.Waste oil is added the boiler 18 from basin 19 by floating chamber 20.The oil level of boiler 18 can be controlled with floating chamber 20.Floating chamber 20 seals, but has a ventpipe 21 to pass through with equilibrium pressure between boiler 18 and floating chamber 20.Boiler 18 is arranged on the combustion chamber 16, and between the two distance should make the head temperature of (combustion oil) boiler 18 when operation of equipment be about 650 °F in fire-box 15.Under this temperature,,, discharge from boiler 18 by vent pipe 25 than light hydrocarbon volatilization and cracking.Assemble in the bottom 23 of boiler 18 gradually by the non-volatile sludge of forming than heavy hydrocarbon and impurity.Sludge flow in the sludge jar 24 by vent pipe 22, handles at last.Under the situation of not emptying of sludge, the liquid level of sludge in the boiler 18 and oil rises, 20 cutout up to the floating chamber, and waste oil no longer enters boiler 18, and last, this equipment is out of service automatically.
The evaporable of discharging from boiler 18 flows through vent pipe 25 than light hydrocarbon, flows through the heat exchanger 26 that is positioned at before the gas blower 27 then, and there, they are cooled and condensation.The airflow that the heat transferred gas blower 27 that heat exchanger 26 sheds produces also passes through second Room 12, imports first Room 11 into by perforate 14 then, recoverable like this heat.
Like this, having formed the liquid oil production of regeneration than light hydrocarbon and flowed into storage tank 28 of condensation, from storage tank 28, recovered oil can be unstowed will be with the elsewhere of oil, or is transported to burner 17 via pump 30.Combustion chamber 16 is similar with the combustion chamber of common oily process furnace.Heat from fire-box 15 sends the heating duct 31 that the buildings heating system connects to by first Room 11, and combustion product gases is discharged by flue 32.
Fig. 1 has shown that a simple embodiment of present device is so that the explanation basic principle of operation.A preferred embodiment of present device is described with Fig. 2 and Fig. 3 now.For the purpose of simple and clear, same section uses the Ref. No. identical with the simple embodiment of Fig. 1 to represent, is not repeated in this description these parts.
In the present embodiment, material storage tank 19 is contained in the enclosed construction 10, and when the waste oil liquid level was lower than predetermined liquid level in the material storage tank, floatswitch made the motor-mount pump starting, receives the pumping of storage setting tank from the outside and comes more waste oil.Work as power connection, when equipment was started working, magnetic valve was opened, and allowed liquid stream flow out from reinforced basin, and 45 startings of electric charging pump.At first pass through " Y " shape strainer 41, the moisture content of removing Particulate Inclusion and carrying secretly from the waste oil of reinforced basin 19.When oil was stored in the exterior storage setting tank, the most of water that is entrained with waste oil can be removed usually.Flow into water capture tank 42 by the effusive residue water entrainment of " Y " shape strainer, can be from water capture tank 42 water by opening valve 36 and regularly discharging through water discharge pipe 35.
When magnetic valve 43 was opened, waste oil also can be sent into by Johnson valve 44 and preheat jar 46 by charge pump 45.Johnson valve 44 can be up to 6 gallons flow volume delivery waste oil per hour.Charge pump is with 4 gallons flow volume delivery waste oil approximately per hour, and irrelevant with the flow rate of Johnson valve.Therefore, at run duration, the feed rate of waste oil can by per hour about 4 gallons become about 10 gallons.
At run duration, preheating can 46 is heated to about 200-300 °F with waste oil, and waste oil is from preheating jar 46 input boilers 18.In the present embodiment, boiler 18 has an inclined floor that is supported on the slide unit 45, boiler 18 is taken out of, so that routine cleaning or the like from fire-box 15 as drawer.The baffle plate 48 of two inclinations upwards and from the opposite flank of boiler 25 extends internally from base plate, like this, accumulates in sludge on boiler 18 bottoms 23 and can walk around baffle plate 48 flow to opposite side under inclined floor one side direction.Evaporable, is discharged by vent pipe 25 by jut 49 then than light hydrocarbon.
During low level float 72 is determined in waste oil liquid level in the boiler 18 reaches by floating chamber 20 predetermined height, switch open is connected burner 17 and combustion pump 30.Like this, burner 17 begins to light, and upwards heats the fire-box 15 that comprises boiler 18.Burner 17 usefulness are fixed in the heat-resisting fiery box 57 that supports with fiery box support 58.Burner 17 incendivities are from the recovered oil of the regular fuel of storage tank 28 or external store.The valve 51 and the artificial opening and closing of valve 52 that are used for regular fuel that are used for recovered oil are to select fuel for use.Pump 30 is installed in the immersion water pot 53 that temperature that electricity consumption heater coil 54 heats can be maintained at about 165.Heater coil 54 and supply with by independent power supply with the power of the cast well heater of the nozzle adjacency of burner 17, purpose is to make supply line, pump and burner fuel temperature remain enough height, to handle the recovered oil of the higher equipment self of viscosity ratio common heating furnace oil fuel.The pressure of fuel tube can be regulated with reducing valve 56, and available pressure table 55 is supervised.Have been found that working pressure is about 120P.S.i.(poundage per square inch) be desirable.
When 72 pairs of burners 17 of low level float switch and petrolift 30 worked, coil relay also stopped charge pump 45 and shut-off circuit valve 43 automatically, and at this moment, waste oil is input unit no longer.The waste oil in boiler 18 can heat gradually with burner 17, until reaching about 650 distillation temperature.Under this temperature, than the light hydrocarbon volatilization, and by vent pipe 25 inflow heat exchangers 25, sludge accumulates in the bottom 23 of boiler 18 simultaneously, discharges gradually by vent pipe 22.When evaporable escaped and enter heat exchanger 26 than light hydrocarbon, the temperature of heat exchanger 26 raise.The temperature of heat exchanger 26 rises and shows that the waste oil in the boiler 18 has reached volatilization temperature, and this can be used as and shows that this equipment has been in the signal of steady state operation.When coil relay works, when electric power is sent to the burner 17 that belongs to different circuit in order to carry out stable operation and petrolift 30 and makes temperature reach 130 °F, be installed in heat exchanger 26 intermediary thermopairs and react.This circuit comprises if gas blower is owing to some reasons shut down, the wing formula switch that power supply can be disconnected.Thermopair also can make magnetic valve 43 open and charge pump 45 is started, and the result is that waste oil continues by pre-heaters 46, to flow into boiler 18 from reinforced basin 19 again.The float 70 of floating chamber 20 can make the oil levels in the boiler 18 rise to predetermined liquid level, and float 70 is to regulate total feed rate by the opening and closing Johnson valve, controls operation liquid level in the boiler 18 with this.By this equipment is to carry out stable operation with about per hour feed rate of 6-10 gallon.Thermopair on heat exchanger 26 also can make sludge blowdown pump 66 start.
Sludge enters precipitation cooling tank 60 by vent pipe 22 and flows out from jar 60, flows into sludge pump 66 by heat exchanger 64 and magnetic valve.Sludge pump 66 enters outside sludge basin with 0.5～0.7 gallon speed per hour with sludge.Magnetic valve 65 bootable liquid streams are by an arm in two arms.Usually, magnetic valve 65 bootable liquid streams flow through the arm that leads to sludge pump 66, yet magnetic valve 65 also can substitute liquid stream introducing safety pump 67()."T"-shaped pipe coupling and leads to transfer pot 61 on the sludge escape route between precipitation cooling tank 60 and the heat exchanger 64, lead to floating chamber 20 again from jar 61.Transfer pot 61 has an air discharge pipe 62 that has valve 63, with the air that discharging is carried secretly, also can reduce heat passage to the floating chamber.
When this device power supply (DPS) of manual disconnection, the power supply that leads to charge pump 45 and sludge pump 66 is disconnected, and magnetic valve 43 cuts out.The oil level of the continuous operation of this equipment in boiler 18 drops to the liquid level of low level float switch 72.At this moment, the low level float switch disconnects the power supply that leads to burner 17 and combustion pump 30.Then, equipment laydown is cooled off about 2 hours.Sludge in vent pipe 22, when the temperature that just precipitates the rising logistics of cooling tank 60 was cooled to 140 °F, thermopair just made magnetic valve 65 startings, and the arm that leads to sludge pump 66 is closed, and made the arm that leads to safety pump 67 open, and safety pump 67 is started.Then, with safety pump 67 sludge and some irreducible oils are drained into from this equipment in the outside sludge basin fully.Sludge in vent pipe 22, when just the temperature of the rising logistics of the first precipitation cooling tank 60 was cooled to 100 °F, this showed the emptying of this pipeline, at this moment thermopair makes magnetic valve 65 commutations, and safety pump 67 is closed.
If this equipment overflows waste oil or filling tube stops up, then the oil level of boiler 18 can drop to the absolute altitude of low level float switch 72, and this can make the power supply that leads to burner 17 and petrolift 30 disconnect, and charge pump 45 is shut down and closes magnetic valve 43.Apparatus cools is also used the aforesaid method discharge.
If the downstream is stopped up, can the attain to a high place absolute altitude of float switch 71 of the oil level in the boiler 18 so also can make the power supply that leads to burner 17 and petrolift 30 disconnect, and charge pump is shut down and closes magnetic valve 43.This equipment is shelved again and cooled off, then, the slave unit discharge.
If, for example do not note inappropriate petroleum product such as gasoline have been added in the reinforced basin 19, when making the equipment local temperature surpass predetermined limit, to the high latching similarly of limitting yet of temperature of fire-box 15 and heat exchanger 26 controls.
Embodiment 1
Present embodiment illustrates operability of the present invention and economy.
Basically adopt the prototype equipment of tape drum formula burner shown in Figure 1, test by following method.25 gallons of samples (the exhausted automotive engine oil that obtains from the car service station) are added to reinforced basin, in floating chamber and the boiler.With 2 glasss of (16 ounces) common No. 1 oil fuel (kerosene) equipment is started working.The heating flame chamber makes boiler temperature near 650 °F, and this equipment moves 24 hours continuously.Run duration, this equipment per hour consume the waste oil of 4.25 imperial gallons approximately.Per hour burning and consume the waste oil of about 75 imperial gallons in the combustion chamber, produces 150000 British thermal unit (Btu)s (BTU)/hour be used for heating approximately.In addition, about 3.1 imperial gallons/hour additional recovered oil be collected in the storage tank and about 4 imperial gallons/hour sludge accumulate in the sludge jar.
Present embodiment further specifies operability of the present invention and economy.
Basically adopt the prototype equipment of Fig. 1, by testing similar in appearance to the method for embodiment 1.Test conditions is listed in table 1.To raw material waste oil, recovered oil and sludge carry out chemistry and physical analysis, and gained the results are shown in the table II.
The living rate of recovered oil is about 90%.Elementary composition and the calorific value and the commercial light fuel of this product are compared, yet, find its viscosity, the analog value of pour point and flash-point and commercial light Fuel has marked difference, and this is because form obviously different.Commercial light Fuel is made up of the narrow saturated alkane aliphatic hydrocrbon of boiling spread basically, and the analysis revealed of recovered oil it to contain a kind of common boiling point higher, the mixture of the saturated and unsaturated aliphatic paraffinic hydrocarbons that boiling spread is very wide.Yet it is very high that the cetane value (about 56) that should be noted that recovered oil is compared with North America diesel-fuel cetane number (scope is 40～45 usually).
Certainly might estimate many variablees of present device and method.
The table I
The operational condition of embodiment 2
Time:
Begin to produce recovered oil=about 4 hours
Produce 35 gallons of recovered oils time=about 6 hours
The total time=about 10 hours
Productive rate=about 3.6 Grams Per Hours
Temperature:
The boiler of production period=635 (335 ℃)
Produce boiler=645 (340 ℃) when finishing
The chimney of production period=595 (313 ℃)
Material balance:
Waste oil material quantity=40 gallon
Recovered oil total amount=36 that produce gallon
Efficient (percentage that recovered oil reclaims)=90%
Keep operation incendiary regeneration oil mass=about 0.7 gallons per hour
Sludge=3 gallon
The loss that leakage and volatilization cause=about 1 gallon
The table II
The analytical data of embodiment 2
Waste oil raw material recovered oil sludge
Appearance is opaque purified, and is opaque,
Black, the Huang one black viscosity of fluorescence
The orange flowable liquids of flowable liquid
Fluid
Smell is pungent, and is pungent, pungent,
Irritating smell irritating smell irritating smell
Water (%) 0.7＜0.05 0.05
Ash (%)
*0.99＜0.01 7.12
Sulphur (%) 0.36 0.20 1.02
Carbon (%) 83.14 84.62 81.76
Hydrocarbon (%) 12.96 13.27 11.75
Nitrogen (%) 0.12 0.05 0.28
Oxygen (%) difference
（by diff.） 1.73 1.81 （-1.98）
＊
Incendiary total heat (English heat
Unit (BTU)/pound) 19,159 19,548 17957
Proportion
Api gravity (calculated value) 26.5 33.7 14.55
Cloud point (°F) T.D. T.D. T.D.
Pour point (°F) 0-5+10
Flash-point (°F)
*220 95＞220
Viscosity:
50℃（cst） 45.9 5.69 156.4
T.D.=is too black so that can not observe
*The ash of oil samples is very high, and ash exists with oxide form, therefore, has seriously distorted the reaction formula that is used for obtaining " oxygen difference "
*Pensky-Martens closed cup
Claims (31)
1, a kind of being used for is characterized in that comprising from the equipment of waste oil regeneration useful oil product:
Refueling device is used for waste oil is added in the described equipment;
The boiler that is communicated with refueling device is to be fit to receiving waste oil from refueling device;
Well heater, the waste oil in the described boiler can be heated to its pressure and normal atmosphere do not have big difference too and make waste oil than the light hydrocarbon volatilization, but, capture impurity with this than the nonvolatile temperature of heavy hydrocarbon;
The tripping device that is connected with described boiler can be separated evaporable from nonvolatile than light hydrocarbon than heavy hydrocarbon and impurity, also comprise being used for evaporable than first vent pipe of light hydrocarbon be used for nonvolatile second vent pipe than heavy hydrocarbon.
2, equipment according to claim 1 is characterized in that described well heater comprises that one is connected on the described separator and suitable the reception and the oil-firing burner of described evaporable than light hydrocarbon that burn.
3, equipment according to claim 2 is characterized in that described boiler is provided with tripping device.
4, equipment according to claim 3 is characterized in that described boiler is arranged on the oil-firing burner separated by a distance, and the temperature that makes described boiler in operation is the scope at about 600-800.
5, equipment according to claim 4, it is characterized in that also comprising and be used for the condenser of the described evaporable of condensation than light hydrocarbon, this condenser is connected with described tripping device, receive evaporable than light hydrocarbon with suitable from tripping device, and be connected to be fit to that the evaporable of condensation is again supplied with oil-firing burner than the matter hydrocarbon with described oil-firing burner.
6, equipment according to claim 5 is characterized in that also comprising that control waste oil liquid stream flows to the valve system of described boiler from described refueling device.
7, equipment according to claim 6 is characterized in that also comprising the recovered oil storage tank that is communicated to described condenser, in addition, also comprises with described tripping device being connected, to be fit to receive the sludge storage tank of the sludge product that comprises heavy hydrocarbon and impurity.
8, equipment according to claim 7 is characterized in that described valve system comprises the floating chamber.
9, equipment according to claim 7 is characterized in that described condensing works comprises heat exchanging pipe, also comprises the blowing plant that is used for to described heat exchanging pipe blowing cold air.
10, equipment according to claim 9, it is characterized in that heat exchanging pipe comprises the several layers conduit, every layer in conduit all be tilt and every layer in conduit be parallel to each other, conduit interconnect make water of condensation flow through heat exchanging pipe basically downwards and in every layer of conduit from an effluent to opposite side.
11, equipment according to claim 10 is characterized in that conduit comprises extended thermal conduction face.
12, according to any described equipment in the claim 7 to 11, it is characterized in that the recovered oil storage tank links to each other with oil-firing burner.
13, equipment according to claim 9, it is characterized in that also comprising a body structure, this body structure has first Room of a base closed, in establish described oil-firing burner and described boiler, and second Room of a base closed, in establish described floating chamber, described heat exchanging pipe and air-blast device, first and second Room are separated by a shared partition wall, but are communicated with by the mutual fluid in the hole on the party wall between them; Also comprise a heating tube that is communicated with first Room, be used to discharge the air of heating, one is arranged in the fiery box that described oil-firing burner is established in first Room, and a flue that is communicated with fiery box, is used for discharging combustion product gases from fiery box.
14, according to claim 3,4 or 10 described equipment, it is characterized in that described boiler has the inclined floor of a band baffle plate, baffle plate extends upward from base plate, and evaporable does not flow to opposite side around baffle plate than heavy hydrocarbon under a side direction of inclined floor, and evaporable flows through from baffle plate than light hydrocarbon.
15, according to Claim 89 or 10 described equipment,, it is characterized in that described floating chamber comprises that float operates the first operation liquid level of described valve system, float is operated second low liquid level of described valve system and described oil-firing burner and the 3rd high liquid level that float is operated described valve system and described oil-firing burner.
16, equipment according to claim 10, it is characterized in that also comprising a pipe that extends between the top of described recovered oil storage tank and described flue and the top and the described flue of described recovered oil storage tank coupled together, this pipe can be used to get rid of any not condensation volatile matter that enters described recovered oil storage tank.
17, according to claim 2,5 or 10 described equipment, it is characterized in that described oil-firing burner is the spray-type burner that heats its nozzle with tubular heater, comprise in addition being placed in the hot water bath, be used for hydro-pump to described oil-firing burner charging.
18, according to Claim 89 or 10 described equipment,, the described refueling device of its feature comprises the charge pump of waste oil being imported described boiler with substantially invariable flow velocity, comprise in addition with variable flow rate, additional waste oil is imported the needle valve of described boiler floating chamber's response.
19, a method of handling waste oil is characterized in that comprising the following steps:
Under almost being equivalent to atmospheric pressure, the waste oil in the described boiler is heated to temperature range and is about 600-800 °F, make like this waste oil than light hydrocarbon volatilization, but non-volatile than heavy hydrocarbon, capture impurity with this;
Then, evaporable is nonvolatilely separated than heavy hydrocarbon and impurity from described than light hydrocarbon.
20, method according to claim 19 is characterized in that described temperature is about 650 °F.
21,, it is characterized in that also comprising that again the condensation evaporable is than the step of light hydrocarbon according to claim 19 or 20 described methods.
22, method according to claim 21, the evaporable of condensation is than the step of light hydrocarbon again to it is characterized in that also comprising burning at least a portion, and the heat that obtains can be used to heat the waste oil in the described boiler.
23, method according to claim 19 is characterized in that described temperature is greatly in 635 to 650 scopes.
24, method according to claim 23 is characterized in that comprising condensation again and reclaims isolating evaporable again than light hydrocarbon.
25, a kind of processing contains the method for the waste oil of impurity, it is characterized in that comprising the following steps:
(1) waste oil in the container is heated to about 600 °F to 800 °F;
(2) first part in the described waste oil is volatilized, mainly comprise the lighter hydrocarbons matter hydrocarbon in the waste oil in the described first part;
(3) evaporable first part is partly isolated from remaining not evaporable waste oil, described remainder mainly comprises light heavy hydrocarbon and the impurity in the waste oil;
(4) the described separated evaporable first part of condensation again; With
(5) first part that reclaims described condensation again is as useful oil production, and impurity wherein reduces greatly, and reclaims rest parts again as sludge.
26, method according to claim 25 is characterized in that described temperature is in 635 to 650 scopes.
27, method according to claim 25 is characterized in that described temperature is approximately 650 °F.
28, method according to claim 25 is characterized in that volatilizing the first part that accounts for waste oil 9/10ths under described temperature.
29, according to claim 25,27 or 28 described methods, (1) (2) and (3) step in it is characterized in that in container together, carry out claim 25.
30, according to claim 25,27 or 25 described methods, it is characterized in that the single container that carries out (1), (2) and (3) step has a base plate that tilts, this base plate has baffle plate, baffle plate extends upward from base plate, thereby baffle plate is flow through in evaporable first part, and described remainder flows downward on inclined floor around baffle plate.
31, according to claim 25,27 or 28 described methods, the step of the part of the useful oil production that it is characterized in that comprising that also burning is reclaimed in (5) step is with this at least a portion as heating steps (1).
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA577,895 | 1988-09-20 | ||
| CA000577895A CA1309370C (en) | 1988-09-20 | 1988-09-20 | Apparatus and method for reclaiming waste oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1041612A CN1041612A (en) | 1990-04-25 |
| CN1019985C true CN1019985C (en) | 1993-03-03 |
Family
ID=4138755
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN89108168A Expired - Fee Related CN1019985C (en) | 1988-09-20 | 1989-09-19 | Apparatus and method for reclaiming waste oil |
Country Status (21)
| Country | Link |
|---|---|
| EP (1) | EP0360500B1 (en) |
| JP (1) | JPH0819424B2 (en) |
| KR (1) | KR900004916A (en) |
| CN (1) | CN1019985C (en) |
| AT (1) | ATE98672T1 (en) |
| AU (1) | AU628079B2 (en) |
| CA (1) | CA1309370C (en) |
| CS (1) | CS537289A2 (en) |
| DD (1) | DD289555A5 (en) |
| DE (1) | DE68911448T2 (en) |
| DK (1) | DK454189A (en) |
| ES (1) | ES2049329T3 (en) |
| FI (1) | FI894426A (en) |
| HU (1) | HUT54915A (en) |
| IE (1) | IE64908B1 (en) |
| IL (1) | IL91635A0 (en) |
| MX (1) | MX172063B (en) |
| NO (1) | NO893721L (en) |
| NZ (1) | NZ230684A (en) |
| PL (1) | PL164829B1 (en) |
| ZA (1) | ZA897091B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1040125C (en) * | 1993-08-05 | 1998-10-07 | 德士古发展公司 | Reclamation of used lubricating oil |
| CN103881780A (en) * | 2014-04-04 | 2014-06-25 | 西南化工研究设计院有限公司 | Process of preparing liquefied natural gas by supplementing carbon dioxide with coke-oven gas |
Families Citing this family (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5286349A (en) * | 1988-09-20 | 1994-02-15 | Shurtleff Edward C | Apparatus for reclaiming useful oil products from waste oil |
| US5795462A (en) * | 1988-09-20 | 1998-08-18 | Patent Holdings Ltd. | Apparatus and method for reclaiming useful oil products from waste oil |
| US5271808A (en) * | 1988-09-20 | 1993-12-21 | Shurtleff Edward C | Apparatus from waste oil for reclaiming a useful oil product |
| US5143597A (en) * | 1991-01-10 | 1992-09-01 | Mobil Oil Corporation | Process of used lubricant oil recycling |
| DE4200270A1 (en) * | 1992-01-08 | 1993-07-15 | Seepe Karl Otto | Reconditioning used oil with min. use of energy - where distillate is continuously drawn off into separate condensn. chamber and hot flue gases are circulated to heat whole distn. chamber |
| US5885444A (en) * | 1992-11-17 | 1999-03-23 | Green Oasis Environmental, Inc. | Process for converting waste motor oil to diesel fuel |
| DE4343408C2 (en) * | 1993-12-18 | 1996-02-29 | Baufeld Mineraloelraffinerie G | Fuel for combustion and heat generation plants |
| KR0171501B1 (en) * | 1996-08-28 | 1999-03-20 | 이성래 | Apparatus and process for reclaiming waste oil |
| JP3961631B2 (en) * | 1997-08-01 | 2007-08-22 | 本田技研工業株式会社 | Covered light vehicle |
| CN1064984C (en) * | 1997-11-24 | 2001-04-25 | 中国石油化工总公司 | Wax composition for durably dustproofing metal products |
| CN100419053C (en) * | 2004-11-04 | 2008-09-17 | 田松庆 | Technology of waste oil regenerating and its used apparatus |
| JP2007291248A (en) * | 2006-04-25 | 2007-11-08 | Takamine Tsukamoto | Reformed fuel oil for internal, external combustion engine produced from waste edible oil and waste lubricant oil as raw material, method and apparatus for manufacturing the same, and method and apparatus for generating electricity using the same |
| CN104371753B (en) * | 2014-11-25 | 2016-03-30 | 烟台市牟平区留德润滑油销售有限公司 | A kind of method of waste lubricating oil distillation cutting and device thereof |
| CN109219649B (en) * | 2016-03-18 | 2021-01-15 | 韩国化学研究院 | Heavy oil conversion process with high asphaltene dispersancy |
| CN107321049B (en) * | 2016-04-30 | 2020-01-21 | 南京梅山冶金发展有限公司 | Waste oil separating device |
| CN106940019A (en) * | 2017-04-17 | 2017-07-11 | 东北师范大学 | Polycyclic aromatic hydrocarbon emission reduction device based on negative feedback control |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US1709230A (en) * | 1928-05-09 | 1929-04-16 | Journal Box Servicing Corp | Method of renovating journal-box oil |
| JPS48102104A (en) * | 1972-04-07 | 1973-12-22 | ||
| JPS52139106A (en) * | 1976-05-18 | 1977-11-19 | Okumura Kikai Seisakusho Kk | Regenerating apparatus of waste oil |
| FR2434865A3 (en) * | 1977-06-23 | 1980-03-28 | Beaumont Maurice | Re-use of used lubricating oil - by distn. to recover fuel oil |
| JPS6035000B2 (en) * | 1979-06-06 | 1985-08-12 | 株式会社日立製作所 | Waste oil treatment method and equipment |
| FR2467880A1 (en) * | 1979-10-18 | 1981-04-30 | Matthys Ets | Used oil regeneration by distn. and further treatment - using distn. bottoms as heat source for further treatment |
| DE3121246A1 (en) * | 1981-05-29 | 1982-12-23 | Drespa, Gerd, 4600 Dortmund | Process and apparatus for processing used oil to give gas oil or heating oil by distillation |
-
1988
- 1988-09-20 CA CA000577895A patent/CA1309370C/en not_active Expired - Fee Related
-
1989
- 1989-09-14 IL IL91635A patent/IL91635A0/en not_active IP Right Cessation
- 1989-09-14 DK DK454189A patent/DK454189A/en not_active Application Discontinuation
- 1989-09-14 DE DE89309360T patent/DE68911448T2/en not_active Expired - Fee Related
- 1989-09-14 EP EP89309360A patent/EP0360500B1/en not_active Expired - Lifetime
- 1989-09-14 AT AT89309360T patent/ATE98672T1/en not_active IP Right Cessation
- 1989-09-14 ES ES89309360T patent/ES2049329T3/en not_active Expired - Lifetime
- 1989-09-18 MX MX017582A patent/MX172063B/en unknown
- 1989-09-18 NZ NZ230684A patent/NZ230684A/en unknown
- 1989-09-18 ZA ZA897091A patent/ZA897091B/en unknown
- 1989-09-19 FI FI894426A patent/FI894426A/en not_active IP Right Cessation
- 1989-09-19 CN CN89108168A patent/CN1019985C/en not_active Expired - Fee Related
- 1989-09-19 AU AU41462/89A patent/AU628079B2/en not_active Ceased
- 1989-09-19 NO NO89893721A patent/NO893721L/en unknown
- 1989-09-19 IE IE298689A patent/IE64908B1/en not_active IP Right Cessation
- 1989-09-19 PL PL89281483A patent/PL164829B1/en not_active IP Right Cessation
- 1989-09-19 DD DD89332806A patent/DD289555A5/en unknown
- 1989-09-20 HU HU894896A patent/HUT54915A/en unknown
- 1989-09-20 JP JP1242420A patent/JPH0819424B2/en not_active Expired - Fee Related
- 1989-09-20 CS CS895372A patent/CS537289A2/en unknown
- 1989-09-20 KR KR1019890013593A patent/KR900004916A/en not_active Application Discontinuation
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1040125C (en) * | 1993-08-05 | 1998-10-07 | 德士古发展公司 | Reclamation of used lubricating oil |
| CN103881780A (en) * | 2014-04-04 | 2014-06-25 | 西南化工研究设计院有限公司 | Process of preparing liquefied natural gas by supplementing carbon dioxide with coke-oven gas |
Also Published As
| Publication number | Publication date |
|---|---|
| NO893721L (en) | 1990-03-21 |
| DK454189D0 (en) | 1989-09-14 |
| NO893721D0 (en) | 1989-09-19 |
| PL164829B1 (en) | 1994-10-31 |
| NZ230684A (en) | 1992-03-26 |
| DD289555A5 (en) | 1991-05-02 |
| ATE98672T1 (en) | 1994-01-15 |
| JPH02191696A (en) | 1990-07-27 |
| ES2049329T3 (en) | 1994-04-16 |
| IE892986L (en) | 1990-03-20 |
| JPH0819424B2 (en) | 1996-02-28 |
| ZA897091B (en) | 1990-06-27 |
| DK454189A (en) | 1990-03-21 |
| AU4146289A (en) | 1990-03-29 |
| IE64908B1 (en) | 1995-09-20 |
| DE68911448D1 (en) | 1994-01-27 |
| DE68911448T2 (en) | 1994-04-14 |
| EP0360500A3 (en) | 1990-12-19 |
| KR900004916A (en) | 1990-04-13 |
| CA1309370C (en) | 1992-10-27 |
| FI894426A0 (en) | 1989-09-19 |
| FI894426A (en) | 1990-03-21 |
| EP0360500B1 (en) | 1993-12-15 |
| AU628079B2 (en) | 1992-09-10 |
| IL91635A0 (en) | 1990-04-29 |
| CN1041612A (en) | 1990-04-25 |
| MX172063B (en) | 1993-12-01 |
| EP0360500A2 (en) | 1990-03-28 |
| HUT54915A (en) | 1991-04-29 |
| CS537289A2 (en) | 1991-07-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1019985C (en) | Apparatus and method for reclaiming waste oil | |
| TW393509B (en) | Apparatus and process for reclaiming fuel oil from waste oil | |
| CN104685033B (en) | For will get dirty or it is non-get dirty hydrocarbon material separation and be converted to the mixing heat treatment process of useful products, technique uses, the manufacture of corresponding system and equipment | |
| US4454427A (en) | Incinerator and fume separator system and apparatus | |
| EP0588854B1 (en) | Apparatus and method for reclaiming waste oil | |
| EP1877355A1 (en) | Biofuel conversion process | |
| SA95150447A (en) | " process to re-refine used oils " | |
| WO2011117819A1 (en) | Apparatus for cleaning gasifier produced gas | |
| CN105542854A (en) | Device and method for recovering paraffin from Fischer-Tropsch paraffin residues | |
| CN204824720U (en) | Oil field operation safeguard and parcel fatlute pyrolysis device | |
| CN102559359A (en) | Method and equipment for regenerating waste emulsified oil | |
| CN1157265A (en) | Method and device for treating dross and greasy dirt | |
| CN2934235Y (en) | Device for regeneration of lubrication oil fuel by oiliness waste slag waste oil | |
| CN102618315A (en) | Recovery device of waste and old plastic and rubber by cracking | |
| CN208532700U (en) | A kind of coal tar layering recovery system | |
| CN216473074U (en) | Continuous rotary dividing wall pyrolysis device and system | |
| RU79976U1 (en) | INDUSTRIAL TECHNOLOGICAL COMPLEX FOR THE PROCESSING AND DISPOSAL OF OIL-CONTAINING WASTE | |
| RU71730U1 (en) | INDUSTRIAL TECHNOLOGICAL COMPLEX FOR THE PROCESSING AND DISPOSAL OF OIL-CONTAINING WASTE | |
| RU53285U1 (en) | THERMOMODULE FOR CLEANING CONTAMINATED OIL MASSES FROM WATER AND MECHANICAL IMPURITIES | |
| EP0448178A1 (en) | Method and device for processing a waste product containing a metal fraction and a combustible material fraction | |
| CN108949204A (en) | A kind of multistage thermal desorption device | |
| US11788018B2 (en) | Processes for converting petroleum based waste oils into light and medium distillate | |
| CN209442832U (en) | A kind of mobile oil-bearing sludge treating system | |
| CN209442833U (en) | A kind of disposal of oily sludge cracker | |
| JP2021041352A (en) | Evaporation device and apparatus for separating mixture in liquid, including the same device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C53 | Correction of patent of invention or patent application | ||
| CB02 | Change of applicant information |
Applicant after: Patent reserve Ltd Applicant after: British West Indies Turks and Caicos Islands Applicant before: Eade Ward Kadon Gao Te F Applicant before: New Zealand province of Canada |
|
| COR | Change of bibliographic data |
Free format text: CORRECT: APPLICANT; FROM: YIDEWO A CARTOON SHITEFU TO: PATENT RESERVING LTD. |
|
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |