JP2007224196A - Apparatus and method for converting waste oil into fuel source - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide an apparatus for converting a waste oil into a fuel source by which even a used oil containing a halogen element can be treated by using a reactor operated at a comparatively low pressure/temperature, and a dechlorinated reclaimed oil having a low chlorine content can be produced; and to provide a method therefor. <P>SOLUTION: The apparatus for converting the waste oil into the fuel source is equipped with an oil-reactive water-mixing means 10 for mixing an oil of a treating target with an aqueous solution of an alkali metal compound or an alkaline earth metal compound in a prescribed ratio, a high pressure feeding means 20 for feeding the oil-reactive water-mixed liquid to a dechlorination reactor at a pressure of treatment for removing the halogen, the dechlorination reactor 30 having a space in which the oil-reactive water-mixed liquid stays for a prescribed retention time under the pressure of the treatment for removing the halogen, a heat-feeding means 40 for feeding thermal energy for keeping the mixed liquid at the temperature of the treatment for removing the halogen, and a cooling type oil-recovering part 50 for recovering the dechlorinated reclaimed oil by cooling the oil-reactive water-mixed liquid subjected to the dechlorination treatment in the dechlorination reactor 30. <P>COPYRIGHT: (C)2007,JPO&INPIT

Description

  The present invention is suitable for use in regeneration processing of cutting oil used in machining and grinding in machining, and oil that reduces frictional resistance between mechanical parts that perform rotational and reciprocating movements such as an internal combustion engine. The present invention also relates to an apparatus and method for waste oil fuel recycling.

  Spent oil is used, for example, in the exchange of oil that reduces the frictional resistance between machine parts that perform rotational and reciprocating movements, such as internal combustion engines, after using cutting oil used in machining and grinding. appear. Here, the cutting oil often contains a halogen compound such as chlorine in order to extend the life of the blade. Also, in the case of oil, a halogen compound is often mixed in order to extend the life of machine parts.

  Therefore, cutting oil and oil processors currently recycle used oil as fuel or incinerate it as waste. The chlorine mixing ratio of used oil is, for example, about 2000 ppm. Spent oil containing such high concentrations of chlorine is used as fuel in facilities where measures against halogens, such as heavy oil containing salt, can be used as fuel, such as thermal power plants, paper mills, cement factories, and dye factories. Can be used.

  However, it is a competition to collect used oil discharged from machine shops and automobile maintenance shops distributed in various places and deliver it to consumers who use used oil containing high concentrations of chlorine. Considering the related heavy oil price and the transportation cost of recovered used oil, it is not practical. Similarly, the use of used oil as a substitute for crude oil in a large processing facility such as an oil refinery plant takes into account the price of heavy oil in a competitive relationship and the cost of transporting recovered used oil. There is a problem that it is not practical.

  Therefore, it is conceivable to remove halogen elements such as chlorine from the used oil to such an extent that they can be used in general combustion facilities that do not take measures against halogens. For example, it is conceivable to reduce the chlorine content of the used oil to the chlorine content standard (for example, 100 ppm) of the hydrocarbon oil set by the Packaging Container Recycling Association. However, compared with hydrocarbon oil extracted from plastic waste subject to the regulations of the Container Recycling Association, used oil is discharged from companies such as machine factories and automobile maintenance factories. The fact is that the waste was treated.

  By the way, the present applicant has proposed a plastic oil converting apparatus and method with a high oil recovery rate from plastic waste in Patent Document 1. And based on the experience with regenerated hydrocarbon oil in the plastic oil production equipment, it is presumed that the used desalted oil can be replaced with crude oil. And in recent years, the crude oil price is about 50 US dollars per barrel, which is several times higher than about 10 US dollars a few years ago. Not only in terms of treatment and environmental measures, it is also gaining importance as a resource and energy measure.

In addition, the Kyoto Protocol has set a target for reducing carbon dioxide (CO ₂ ), but used oil is contained in high-concentration halogen elements. The used oil that was used was incinerated as a waste treatment at a significant rate, so it was calculated as carbon dioxide consumption. However, if halogens such as chlorine are removed from the used oil and can be reused as fuel, the contribution to environmental measures is significant in terms of reducing carbon dioxide compared to incineration. It also contributes to fulfilling obligations under the Protocol.

JP 2005-306974 A JP 2003-34794 A

  By the way, used oil has the following features compared to plastic waste that is subject to regulation by the Container Recycling Association. First, used oil is mixed with metal chips and metal powder accompanying cutting. In addition, the used oil also contains moisture to cool the blade by cutting or the like.

  On the other hand, Patent Document 2 proposes a method of simultaneously performing a desalting process and a denitrogenation process on a cracked oil of plastic waste. However, although the halogen compound is mixed in the used oil, the possibility that the nitrogen compound is mixed is small. Nitrogen compounds in plastic waste are included as, for example, polyimide resin or vinylidene chloride. On the other hand, since, for example, vinyl chloride, polycarbonate resin, and polyolefin resin do not contain nitrogen compounds in plastic waste, a method of simultaneously treating the desalting treatment and the denitrifying treatment disclosed in Patent Document 2 is proposed. It does not apply.

  The present invention solves the above-described problems, and even a used oil containing a halogen element can be treated using a reaction vessel having a relatively low pressure and temperature, and the chlorine content of the desalted regenerated oil. An object of the present invention is to provide a waste oil fuel recycling apparatus and method with low fuel consumption.

  As shown in FIG. 1, for example, as shown in FIG. 1, the waste oil fuel recycling apparatus of the present invention that achieves the above object is an oil reaction water mixing system that mixes a target oil and an aqueous solution of an alkali metal compound or alkaline earth metal compound at a predetermined ratio. Means 10, high-pressure supply means 20 for supplying the oil reaction water mixed solution to the desalination reaction vessel 30 at the halogen desorption treatment pressure, and the oil reaction water mixed solution in the space previously maintained at the halogen desorption treatment temperature A desalination reaction vessel 30 having a space shape that stays for a predetermined residence time at a desorption treatment pressure, and a heat supply means 40 for supplying thermal energy for maintaining the halogen desorption treatment temperature to the desalination reaction vessel 30; The oil reaction water mixture that has been desalted in the desalination reaction vessel 30 is cooled, and a cooling type oil content recovery unit 50 that recovers desalted regenerated oil is provided.

  In the apparatus thus configured, the oil reaction water mixing means 10 previously mixes the oil to be treated with an aqueous solution of an alkali metal compound or an alkaline earth metal compound at a predetermined ratio to obtain an oil reaction water mixed solution. Is generated. Since the oil reaction water mixed solution is mixed before being supplied to the desalting reaction vessel 30, an optimal ratio of an aqueous solution of an alkali metal compound or an alkaline earth metal compound to the oil to be treated before the desalting treatment. Can be mixed. Since the desalination reaction vessel 30 is maintained at the halogen element separation temperature and the halogen element separation pressure and dehalogenates the oil reaction water mixture, the halogen elements contained in the oil reaction water mixture are greatly reduced. To do. The halogen element separation temperature is typically set to a temperature of 250 ° C. to 375 ° C. and a pressure of 80 atm to 200 atm. A typical residence time is, for example, about 3 to 15 minutes. When the oil reaction water mixture is supplied to the desalting reaction vessel 30, the high-pressure supply unit 20 supplies the mixture at the halogen element separation pressure to maintain the reaction conditions in the desalting reaction vessel 30. The heat supply means 40 supplies the thermal energy for maintaining the halogen desorption treatment temperature to the desalination reaction vessel 30 to maintain the reaction conditions in the desalination reaction vessel 30. The cooling oil recovery unit 50 cools the oil reaction water mixture that has been desalted in the desalination reaction vessel 30 to recover desalted regenerated oil.

  In the waste oil fuel recycling apparatus according to the present invention, for example, as shown in FIG. 1, when the desalted regenerated oil recovered by the cooling oil recovery unit 50 is used as fuel for the heat supply means 40, The desalted regenerated oil can be used as a fuel for heating the salt reaction vessel, and the reuse of the desalted regenerated oil can proceed smoothly without incurring the cost of transporting the desalted regenerated oil, and the operation cost can be reduced. Preferably, when the desalted regenerated oil storage unit 60 for storing the desalted regenerated oil recovered by the cooling type oil recovery unit 50 is provided, the supply and demand of the generated amount of the desalted regenerated oil and the fuel consumption of the heat supply means 40 The balance can be easily adjusted.

  In the waste oil fuel recycling apparatus of the present invention, for example, as shown in FIG. 1, it further has a metal removing means 13 for removing metal chips and metal powder contained in the oil to be treated. When the removed oil to be treated is supplied to the oil reaction water mixing means 10, the oil reaction water mixed solution does not contain a metal harmful to the desalination treatment in the desalination reaction vessel 30, and the oil reaction water mixing is performed. The homogeneity of the oil to be treated in the means 10 is increased.

  For example, as shown in FIG. 3, the waste oil fuel recycling method of the present invention that achieves the above object comprises mixing a target oil and an aqueous solution of an alkali metal compound or an alkaline earth metal compound at a predetermined ratio (S104), The oil reaction water mixture is supplied to the desalination reaction vessel 30 at a halogen desorption treatment pressure (S106), and the oil reaction water mixture is heated to the halogen desorption treatment temperature (S108), and is previously maintained at the halogen desorption treatment temperature. In the desalination reaction vessel, the oil reaction water mixture stays at the halogen desorption treatment pressure for a predetermined residence time (S110), and the oil reaction water mixture desalted in the desalination reaction vessel 30 is cooled. (S112) and a step of recovering the desalted regenerated oil (S114).

  According to the apparatus and method for converting waste oil into fuel according to the present invention, the oil to be treated is mixed with the aqueous solution of the alkali metal compound or alkaline earth metal compound by the oil reaction water mixing means. An oil reaction water mixture kept at the optimum value is obtained. Further, since the dehalogenation treatment is carried out while maintaining the halogen element separation temperature and the halogen element separation pressure in the desalination reaction vessel, the halogen elements contained in the oil reaction water mixture are greatly reduced. The cooling type oil component recovery unit cools the oil reaction water mixture that has been desalted in the desalination reaction vessel, and recovers the desalted regenerated oil.

  Hereinafter, embodiments of the present invention will be described with reference to the drawings.

  FIG. 1 is a functional block diagram for explaining a waste oil fuel recycling apparatus according to a first embodiment of the present invention. In the figure, the waste oil fuel recycling apparatus includes an oil reaction water mixing means 10, a high pressure supply means 20, a desalination reaction vessel 30, a heat supply means 40, and a cooling type oil content recovery unit 50 as main components. Furthermore, it is preferable to include a desalted regenerated oil storage unit 60 and a metal removing unit 13.

In the oil reaction water mixing means 10, the oil to be treated and the aqueous solution of the alkali metal compound or alkaline earth metal compound are mixed at a predetermined ratio. Examples of alkali metals include lithium, sodium, potassium, rubidium, cesium and the like. Examples of alkaline earth metals include magnesium, calcium, strontium, barium and the like. Examples of the alkali metal compound or alkaline earth metal compound include hydroxides, oxides, carbonates, hydrogen carbonates, basic carbonates, fatty acid salts, phosphates, and hydrogen phosphates. The predetermined ratio is determined such that, for example, a 0.05N to 0.5N NaOH aqueous solution as an alkali metal compound is used in an amount of 2 to 0.50 weight per 1 weight of the oil to be treated. Here, N used to indicate the concentration of the alkali metal compound is a specified concentration indicating that 1 gram equivalent of the alkali metal compound is present in the aqueous solution, and the molar concentration (mol / m ³ ) is measured. It is a legal correspondence concept. The concentration of the NaOH aqueous solution is particularly preferably 0.2 N to 0.4 N (= mol / liter), and the amount used per 1 weight of the oil to be treated is 1 weight to 0.50 weight.

Here, when an aqueous solution of an alkali metal compound or alkaline earth metal compound is mixed with the oil to be treated at a predetermined ratio, the halogen desorption treatment temperature and the halogen desorption treatment are lower than when only water is mixed with the oil to be treated. Halogen detachment treatment can be performed by pressure. The halogen elimination treatment reaction in the case of water typically needs to be performed at a critical temperature of 374.2 ° C. and a critical pressure of around 22.12 MPa, which are typically the critical constants of water. In the case of water, the halogen elimination treatment reaction is performed under supercritical conditions. For example, in the case of a batch reaction using a reactor having an internal volume of 4.0 cm ³ , if the volume of the oil to be treated is ignored, For example, the partial pressure of water when using 1 g is approximately equal to 22 MPa at 375 ° C., and 33 MPa at 425 ° C. Accordingly, in order to ensure the desired halogen elimination treatment while maintaining the halogen elimination treatment temperature and the halogen elimination treatment pressure in the desalination reaction vessel 30 low, not only water but also an aqueous solution of an alkali metal compound or an alkaline earth metal compound Is preferably mixed with the oil to be treated at a predetermined ratio.

  The high pressure supply means 20 supplies the oil reaction water mixed solution to the desalting reaction vessel 30 at a halogen desorption processing pressure. The desalination reaction vessel 30 has a space shape in which the oil reaction water mixture stays at a halogen removal treatment pressure for a predetermined residence time in a space previously maintained at a halogen removal treatment temperature. In the desalination reaction vessel 30, as a halogen elimination treatment reaction condition as a reforming reaction, an alkali metal having a pH of 7 or more at a temperature of at least 250 ° C. in the desalination reaction vessel 30 as a hermetically sealed container containing oil containing chlorine. The chlorine in the oil to be treated is reacted with the reaction water by contacting with an aqueous solution (reaction water) of the compound or alkaline earth metal compound. That is, under typical operating conditions, when a 0.2N to 0.4N NaOH aqueous solution as an alkali metal is used in an amount of 1 to 0.50 wt. At 375 ° C., the halogen desorption treatment pressure is 8 MPa to 20 MPa (80 atmospheres to 200 atmospheres), preferably 10 MPa to 15 MPa (100 atmospheres to 150 atmospheres), and the residence time is about 3 minutes to 15 minutes. Particularly preferably, when the halogen desorption treatment temperature is 325 ° C., the halogen desorption treatment pressure is 14 MPa to 14.5 MPa, and the residence time is 10 minutes, the halogen desorption treatment reaction proceeds almost completely.

  In general, increasing the halogen desorption treatment temperature and halogen desorption treatment pressure shortens the residence time and lowers the mixing ratio of the alkali metal compound. Conversely, decreasing the halogen desorption treatment temperature and halogen desorption treatment pressure increases the residence time. In addition, a certain halogen elimination treatment can be performed by increasing the mixing ratio of the alkali metal compound. Therefore, if the capacity of the desalting reaction vessel 30 is increased to increase the halogen desorption treatment temperature and the halogen desorption treatment pressure, the residence time can be shortened, so that the halogen desorption treatment capacity per unit volume is increased. On the other hand, even if the capacity of the same desalting reaction vessel 30 is decreased, the capacities of the high-pressure supply means 20 and the heat supply means 40 can be suppressed by lowering the halogen desorption treatment temperature and the halogen desorption treatment pressure, and energy consumption per unit treatment target oil. Less. Therefore, when the required oil capacity to be treated is determined, the halogen desorption treatment temperature, halogen desorption treatment pressure, residence time, and reaction water mixing ratio are designed so that the total operating and equipment costs are optimized. To do.

  In the desalination reaction vessel 30, the batch type reactor may be used, and the continuous type may be used as a flow-through packed bed tubular reactor. In the batch method, since the reaction is performed at a high temperature in a sealed container using water, the pressure in the desalination reaction container rises, and the reaction temperature rises to around 20 MPa, which is an internal pressure close to the critical condition of water. Therefore, in the batch reaction, the reaction is performed under subcritical or supercritical conditions of water. Here, the critical condition of water means a gas-liquid coexistence state, and the partial pressure of water is almost equal to the saturated vapor pressure of water. In the continuous method, the halogen elimination treatment reaction is performed under the subcritical condition of water. Under the subcritical condition of water, the total pressure is, for example, the value obtained by adding 0.5 MPa to the saturated vapor pressure of water, so that the halogen elimination treatment reaction is an almost complete liquid phase reaction.

  The heat supply means 40 supplies thermal energy for maintaining the halogen desorption treatment temperature to the desalting reaction vessel 30. The cooling oil recovery unit 50 cools the oil reaction water mixture that has been desalted in the desalination reaction vessel 30 to recover desalted regenerated oil. The oil reaction water mixture is not necessarily limited to the liquid phase in the atmosphere of the halogen desorption treatment temperature and the halogen desorption treatment pressure, but is in a boundary state (critical state or subcritical state) of the liquid phase or gas phase. Desalted regenerated oil is obtained by cooling and liquefying the oil reaction water mixture to remove moisture, and the oil component also contains components having various evaporation temperatures.

  The desalted regenerated oil storage unit 60 stores the desalted regenerated oil recovered by the cooling oil content recovery unit 50. Here, the desalted regenerated oil stored in the desalted regenerated oil storage unit 60 includes heavy naphtha, light oil, and heavy oil components suitable for fuel use in the heat supply means 40. Therefore, when the desalted regenerated oil is used as a fuel for heating the desalted reaction vessel, the desalted regenerated oil can be reused smoothly without incurring the transportation cost of the desalted regenerated oil and contribute to the reduction of the operating cost. .

  The oil refining unit 70 is a facility for refining the desalted regenerated oil stored in the desalted regenerated oil storage unit 60. Here, refining refers to distillation using the difference in boiling points of components, and petroleum products include liquefied petroleum gas, gasoline, naphtha, kerosene, jet fuel oil, light oil, lubricant base oil, heavy oil, asphalt, etc. is there. In petroleum refining, distillation processes include atmospheric distillation and vacuum distillation, and processes involving chemical reactions include hydrodesulfurization, catalytic reforming, and catalytic cracking. For example, there are light naphtha (for example, boiling point 30 ° C to 100 ° C), heavy naphtha (for example, boiling point 100 ° C to 200 ° C), light oil (for example, boiling point 180 ° C to 350 ° C), and heavy oil (for example, boiling point 300 ° C or higher). The oil refining unit 70 is constructed as a petrochemical plant, and has a high capital investment. Therefore, the oil refining unit 70 may be added when a large-scale desalted regenerated oil storage unit 60 is constructed.

  The metal removing means 13 removes metal chips and metal powder contained in the oil to be treated, and separates using, for example, the specific gravity difference between the oil and the metal. When the processing target oil from which the metal component has been removed by the metal removing unit 13 is supplied to the oil reaction water mixing unit 10, the quality of the oil reaction water mixed solution is stabilized and the halogen desorption process can be performed stably.

  Next, FIG. 2 is an overall block diagram of the waste oil fuel recycling apparatus according to the second embodiment of the present invention, which is a concrete implementation of the functional block diagram of FIG. The part 70 shows a format that is not installed. In the figure, an oil reaction water mixing means 10 includes a suction tank 11, a merging valve 12, a precipitation tank 13a as a metal removing means 13, a separation tank 13b, a centrifuge 14, a return pump 15, a regulating valve 16, an intermediate oil to be treated. A tank 17, an oil reaction water mixing tank 18, a reaction water return tank 19, an alkali metal compound tank 19b, and an adjustment valve 19c are provided.

  The suction tank 11 is a receiving tank that stores used oil discharged from operators such as machine shops and automobile maintenance shops. Used oil from the suction tank 11 and untreated oil returned from the centrifugal separator 14 via the return pump 15 and the junction valve 12 are sent to the precipitation tank 13a. In the separation tank 13b, a large particle size or large shape metal mixture or dust that settles due to a difference in specific gravity in the precipitation tank 13a is stored. In the processing object oil intermediate tank 17, the processing object oil from which the metal component has been removed by the centrifuge 14 is stored via the adjustment valve 16. Preferably, a flow meter is provided in the adjustment valve 16 to measure the flow rate of the processing target oil.

  The reaction water return tank 19 is fed back with the treated water (RWR) after being separated by the oil / water separator 53 and supplied with sodium hydroxide (NaOH) from the alkali metal compound tank 19b. The processing target oil is sent from the processing target oil intermediate tank 17 to the oil reaction water mixing tank 18, and the reaction water is sent from the reaction water return tank 19 via the adjustment valve 19c. The opening of the control valve 19c is mixed at the predetermined ratio according to the concentration of the NaOH aqueous solution as the aqueous solution of the alkali metal compound or alkaline earth metal compound in the reaction water return tank 19 and the amount of oil to be treated in the intermediate tank 17 supplied. It is preferable to control with a controller (not shown). In this case, the concentration of the NaOH aqueous solution may be measured with a densitometer, or the amount of sodium hydroxide supplied from the alkali metal compound tank 19b may be used. The amount of oil to be processed in the intermediate tank 17 is preferably measured with a flow meter, for example.

  The high-pressure supply means 20 has an inlet pipe 21, a high-pressure pump 22, a release valve 23, and an outlet pipe 24. An oil reaction water mixture (OS) is supplied to the inlet line 21 from the oil reaction water mixing tank 18. In the outlet line 24, the oil reaction water mixture sent from the inlet line 21 is pressurized by the high-pressure pump 22 and sent to the desalination reaction vessel 30. The release valve 23 allows the oil-reacted water mixture to escape to the outside air in order to prevent the outlet line 24 from being clogged for some reason or to prevent abnormal high pressure from proceeding in the desalination reaction vessel 30. It is an emergency safety device.

  The desalination reaction vessel 30 has a base 31, an outer shell 32, a support leg 33, a superheated steam inlet 34, a steam outlet 35, a reaction pipe inlet 36, a medium superheating pipe 37, an inner shell 38, and a flange outlet 39. ing. The base 31 is a base on which the entire desalting reaction vessel 30 is fixed, and preferably the high pressure pump 22 may be commonly attached. The outer shell 32 is a steel cylindrical container that can withstand high temperatures and high pressures for maintaining the inside at a halogen removal temperature, and is fixed to the base 31 by support legs 33. The superheated steam inlet 34 is supplied with superheated steam (SsS) from the heat supply means 40 and is provided on the base 31 side of the outer shell 32 here. Since the steam outlet 35 supplies the heat energy by the external shell 32, the steam whose temperature has decreased is discharged from the external shell 32, and the discharged steam (SsR) is returned to the heat supply means 40.

  The reaction line inlet 36 is provided on the top side of the outer shell 32, and the oil reaction water mixed liquid whose pressure is increased to the halogen desorption processing pressure by the high-pressure pump 22 is sent to the reaction pipe inlet 36. The medium overheating pipe 37 is a loop-like pipe having one end attached to the reaction pipe inlet 36 and the other end attached to the base 31 side inlet of the inner shell 38. The temperature is raised to the halogen removal temperature by the superheated steam sent to. In order to secure the heat exchange time required for raising the temperature of the oil reaction water mixture to the halogen removal temperature, for example, it has several to several tens of turns along the outer periphery of the inner shell 38. Further, in order to facilitate heat exchange, a pipe line is configured using a metal such as copper having a low thermal resistance. Since the oil reaction water mixture already contains an aqueous NaOH solution that is an alkali metal compound, the halogen desorption treatment reaction also proceeds in the medium overheating conduit 37.

  The inner shell 38 is a high-temperature and high-pressure reaction space that secures the residence time of the oil reaction water mixture heated near the halogen desorption treatment temperature in the medium overheating pipe 37 and promotes the halogen desorption treatment reaction. . Since the inner shell 38 is located inside the outer shell 32, the desalting reaction vessel 30 as a whole has a double tube structure or a jacket type reaction vessel. The inner shell 38 has a medium overheating pipe 37 attached to the base 31 side inlet, and a flange outlet 39 attached to the top side outlet.

  The heat supply means 40 includes a steam boiler 41, a superheated furnace 44, a burner 45, and a steam recovery tank 46. The steam boiler 41 heats hot water heated by steam recovered from the steam outlet 35 in clean water or a steam recovery tank 46 by an internal burner, and typically provides heat energy necessary for the heat of vaporization of water. Supply steam to generate steam at 105 ° C to 150 ° C.

  The superheated furnace 44 superheats the steam generated by the steam boiler 41, and the temperature of the superheated steam (SsS) is 250 ° C. to 375 ° C., which is the halogen desorption processing temperature, and is located in the inner shell 38. For example, the steam is heated to 300 ° C. to 400 ° C. for example. The burner 45 is used for overheating of the superheated furnace 44, and preferably, desalted regenerated oil purified by the desalted regenerated oil storage unit 60 is used as fuel. The steam recovery tank 46 returns steam (SsR) discharged from the steam outlet 35, exchanges heat with clean water, raises the temperature, and uses the hot water in the steam boiler 41. Preferably, heat exchange is used for the steam recovery tank 46.

  The cooling type oil component recovery unit 50 includes a cooler 51, a cooling tower 52, an oil / water separator 53, an instrument panel 54, a pump 55, a control valve 56, and an oil circulation tank 57. The cooler 51 cools the oil reaction water mixture as the oil reaction water mixture sent from the flange outlet 39 to, for example, about several tens of degrees Celsius. The cooling tower 52 cools the cooling water used in the cooler 51 and circulates and uses the cooling water. For example, an air cooling method using the heat of vaporization of water is used. The oil / water separator 53 separates the oil and water from the oil reaction water mixture cooled by the cooler 51 using a specific gravity difference like a centrifuge. The instrument panel 54 monitors the operation state of the oil / water separator 53 and accommodates a control device such as a controller. The pump 55 is a fluid machine that sends the oil reaction water mixed liquid cooled by the cooler 51 to the oil / water separator 53. The adjustment valve 56 adjusts the amount of water (RWR) separated by the oil / water separator 53 to be returned to the reaction water return tank 19. The oil circulation tank 57 stores the desalted regenerated oil separated by the oil / water separator 53, and also removes water contained in the desalted regenerated oil from the salt regenerated oil using the specific gravity difference between water and oil. is doing. In addition, although the case of the cooler 51, the oil-water separator 53, and the oil circulation tank 57 is illustrated, it can be appropriately arranged according to the processing capacity and the oil recovery rate, for example, two or more in series Or may be connected in parallel.

  The desalted regenerated oil storage unit 60 has an oil storage tank 61 and an oil storage tank 62. The oil storage tank 61 temporarily stores the desalted and regenerated oil stored in the oil circulation tank 57. Preferably, the oil storage tank 61 is a light oil / heavy liquid that is liquid at room temperature by removing asphalt and pitch components by a specific gravity difference. Desalinated regenerated oil containing oil components. When the raw material is used oil discharged from a company such as a machine factory or an automobile maintenance factory, the amount of discharge may change seasonally, and the fuel consumption of the burner 45 may become excessive or insufficient. It is done. Therefore, the desalted regenerated oil supplied to the oil storage tank 61 is supplied to the fuel conduit in principle as it is circulated and used as fuel for the burner 45. On the other hand, the surplus fuel for the burner 45 is stored in the oil storage tank 62 and can be transported to other facilities by a tank truck or the like.

  The operation of the apparatus configured as described above will be described. FIG. 3 is a flowchart for explaining the method of recycling waste oil as a fuel resource according to the present invention, which is indicated here as an advanced recycling method for waste oil. First, metal chips and metal powder contained in the oil to be treated are removed by the metal removing means 13 (S102). Then, the oil to be treated and an aqueous solution of an alkali metal compound or an alkaline earth metal compound (for example, NaOH) are mixed at a predetermined ratio (S104) and stored in the oil reaction water mixing tank 18. This predetermined ratio is set to a value at which the required halogen desorption treatment can be performed according to the halogen desorption treatment pressure, halogen desorption treatment temperature, and residence time in the desalting reaction vessel.

  This oil reaction water mixture is supplied to the desalination reaction vessel 30 at a halogen desorption treatment pressure using the high-pressure pump 22 (S106). The oil reaction water mixture is heated to a temperature near the halogen desorption treatment temperature in the medium superheating line 37 provided in the desalination reaction vessel 30 (S108). Next, the residence time of the oil reaction water mixture in the inner shell 38 maintained at the halogen desorption treatment pressure / halogen desorption treatment temperature is secured (S110). This promotes the halogen elimination treatment reaction in the oil reaction water mixture.

  Then, the desalted oil reaction water mixture is cooled using the cooler 51 and the oil / water separator 53 (S112). And the desalted regenerated oil which can be reused by the oil circulation tank 57 is recovered (S114). At this time, it is preferable to remove water contained in the desalted regenerated oil. In the oil storage tank 61, the desalted regenerated oil is used as fuel for the burner 45, and the surplus desalted regenerated oil is stored in the oil storage tank 62 (S116). The desalted regenerated oil stored in the oil storage tank 62 can be reused as various fuels and petrochemical raw materials (S118). This reuse contributes to the reduction of carbon dioxide generation because the oil to be treated, which has been previously incinerated, is reused as desalted regenerated oil.

  In the above-described embodiment, the oil to be treated and an aqueous solution of an alkali metal compound or alkaline earth metal compound (for example, NaOH) are mixed at a predetermined ratio, and the halogen desorption treatment pressure and halogen desorption are compared with water alone. This shows a case where the necessary halogen desorption treatment is performed by adjusting the residence time while keeping the treatment temperature low. However, there are various combinations of oils contained in the oil to be treated, and the optimum operating conditions of the desalination reaction vessel also vary according to changes in crude oil prices and power prices. Therefore, a separate total instrumentation management system is provided to adjust the halogen desorption treatment temperature, halogen desorption treatment pressure, residence time, and reaction water mixing ratio as needed to optimize the total operating and equipment costs. You may be able to do it.

  FIG. 4 is a functional block diagram for explaining a waste oil fuel recycling apparatus equipped with a comprehensive instrumentation management system, which is shown here as an advanced waste oil recycling plant. In the figure, the advanced waste oil recycling plant is a functional block diagram similar to the waste oil fuel recycling apparatus shown in FIG. The integrated instrument management system 80 includes a processing target oil arrival monitoring unit 81, an alkali metal-containing reaction water supply control unit 82, an oil reaction water mixing ratio control unit 83, an oil reaction water mixture residence time control unit 84, and a halogen desorption processing pressure. It has a control unit 85, a halogen removal processing temperature control unit 86, a residual halogen detection unit 87, a desalted regenerated oil production amount detection unit 88, and an oil component cooling unit control unit 89. The integrated instrumentation management system 80 includes information processing equipment such as a process computer, sensors such as a thermometer, pressure gauge, flow meter, and component meter, and a controller having an actuator function such as a valve opening controller. It is comprised from.

  The processing target oil arrival monitoring unit 81 monitors the arrival state of the processing target oil, and inputs, for example, the weight and volume of the loaded processing target oil to the process computer as the integrated instrumentation management system 80. The alkali metal-containing reaction water supply control unit 82 adjusts the alkali metal concentration of the reaction water or the reaction water supply amount of the oil reaction water mixing means 10 according to the arrival state of the processing target oil. For example, in the case of the apparatus of FIG. 2, the valve opening of the adjustment valve 19c is adjusted according to the amount of the processing target oil sent from the processing target oil intermediate tank 17, and the oil reaction water mixing is performed from the reaction water return tank 19. The amount of reaction water sent to the tank 18 is controlled so as to obtain an appropriate oil reaction water mixing ratio.

  The oil reaction water mixing ratio control unit 83 can obtain a desalted and regenerated oil of an appropriate quality according to the properties of the desalted and regenerated oil detected by the residual halogen detecting unit 87 and the desalted and regenerated oil production amount detecting unit 88. Thus, the oil reaction water mixing ratio in the oil reaction water mixing tank 18 is adjusted. In other words, the oil reaction water mixing ratio control unit 83 adjusts the set values of the processing object oil arrival monitoring unit 81 and the alkali metal-containing reaction water supply control unit 82 to adjust the alkali metal according to the properties of the processing target oil to be received. The reaction water is supplied and controlled so as to obtain an appropriate quality desalted regenerated oil.

  The oil reaction water mixture residence time control unit 84 determines whether the desalted regenerated oil having an appropriate quality depends on the properties of the desalted regenerated oil detected by the residual halogen detecting unit 87 and the desalted regenerated oil production amount detecting unit 88. The supply amount of the oil reaction water mixture in the desalination reaction vessel 30 and the supply pressure of the high-pressure supply means 20 are determined so as to obtain an optimum production rate. The halogen desorption processing pressure control unit 85 performs desalting so that an appropriate quality desalted reclaimed oil can be obtained at an optimum production rate in accordance with the arrival state of the processing target oil and the properties of the desalted reclaimed oil to be processed. The halogen desorption processing pressure in the reaction vessel 30 and the supply pressure of the high-pressure supply means 20 are controlled. The halogen desorption processing temperature control unit 86 performs desalting so that an appropriate quality desalted regenerated oil can be obtained at an optimum production rate in accordance with the state of arrival of the processing target oil and the properties of the desalted regenerated oil to be processed. The halogen desorption processing temperature in the reaction vessel 30 and the supply heat energy of the heat supply means 40 are controlled. In the desalination reaction vessel 30, there is a mutual interference between temperature and pressure, and the reaction rate of halogen elimination treatment also affects the residence time. Therefore, the oil reaction water mixture residence time control unit 84 and the halogen elimination treatment pressure control unit 85. The halogen desorption processing temperature control unit 86 performs each control in consideration of the influence of mutual interference.

  The residual halogen detector 87 is a detector that detects residual halogen in the desalted and regenerated oil processed by the cooling oil recovery unit 50. For example, a residual chlorine concentration detector is used. The desalted regenerated oil production amount detection unit 88 is a meter that measures the production amount of the desalted regenerated oil processed by the cooling type oil component recovery unit 50. For example, a flow meter that measures the flow rate in a pipe line, a tank A level gauge or pressure gauge is used to measure the liquid level. The oil component cooling unit control unit 89 controls the cooling function of the cooling type oil component recovery unit 50. For example, in the case of the apparatus of FIG. 2, flow rate control and temperature control necessary for controlling the cooler 51 and the cooling tower 52 are performed. Preferably, as an additional function of the oil component cooling unit controller 89, the operation state of the oil / water separator 53 may be monitored by a communication function with the instrument panel 54, and the pump 55, the adjustment valve 56, and the oil circulation tank 57 may be monitored. Etc. may be comprehensively controlled.

  As described above, according to the present invention, the cooling oil recovery unit can recover the desalted regenerated oil by cooling the oil reaction water mixture that has been desalted in the desalting reaction vessel. Then, halogen elements such as chlorine can be removed from used oil and reused as fuel, reducing carbon dioxide compared to incineration, and contributing to fulfilling the obligations under the Kyoto Protocol. The effect is great.

  In addition, since the oil to be treated is mixed with the aqueous solution of the alkali metal compound or alkaline earth metal compound by the oil reaction water mixing means, the halogen element separation temperature and the halogen element separation pressure in the desalination reaction vessel are Dehalogenation can be performed at a lower temperature and pressure than when dehalogenation is performed using a critical state or a subcritical state. Then, the desalination reaction vessel can be easily designed and manufactured as a pressure vessel, and the price competitiveness of the desalted regenerated oil is comparable to that of fuel oil, and the use of waste oil as a fuel resource can be promoted. .

It is a functional block diagram explaining the fuel resource utilization apparatus of the waste oil as the 1st Embodiment of this invention. It is a whole block diagram of the waste oil fuel-recycling apparatus as the 2nd Embodiment of this invention. It is a flowchart explaining the fuel resource recycling method of the waste oil of this invention. It is a functional block diagram explaining the fuel resource conversion apparatus of the waste oil which attached the integrated instrumentation management system as the 3rd Embodiment of this invention.

Explanation of symbols

DESCRIPTION OF SYMBOLS 10 Oil reaction water mixing means 13 Metal removal means 20 High-pressure supply means 30 Desalination reaction container 40 Heat supply means 50 Cooling type oil content collection | recovery part 60 Desalination reproduction | regeneration oil storage part 70 Oil content refinement | purification part 80 Total instrumentation management system

Claims (4)

Oil reaction water mixing means for mixing the oil to be treated and reaction water containing at least one of an alkali metal compound or an alkaline earth metal compound at a predetermined ratio;
High-pressure supply means for supplying this oil reaction water mixed solution to the desalination reaction vessel at a halogen desorption treatment pressure;
In the space previously maintained at the halogen desorption treatment temperature, the desalination reaction vessel having a space shape in which the oil reaction water mixture stays at the halogen desorption treatment pressure for a predetermined residence time;
Heat supply means for supplying thermal energy for maintaining the halogen desorption treatment temperature at the desalination reaction vessel;
A cooling type oil recovery unit that cools the oil reaction water mixture desalted in the desalination reaction vessel and recovers the desalted regenerated oil;
A waste oil fuel recycling device comprising:   Furthermore, the waste-oil fuel-recycling apparatus of Claim 1 which uses the desalted regenerated oil collect | recovered by the said cooling type oil component collection | recovery part as a fuel of the said heat supply means. In the waste oil fuel recycling apparatus according to claim 1 or 2,
Furthermore, it has a metal removal means for removing metal chips and metal powder contained in the oil to be treated,
An apparatus for converting waste oil into a fuel resource, wherein the oil to be treated from which the metal component has been removed is supplied to the oil reaction water mixing means. Mix the oil to be treated and the aqueous solution of the alkali metal compound or alkaline earth metal compound at a predetermined ratio,
This oil reaction water mixture is supplied to the desalination reaction vessel at the halogen elimination pressure.
Raising the temperature of the oil reaction water mixture to the halogen elimination temperature,
In the desalination reaction vessel previously maintained at the halogen desorption treatment temperature, the oil reaction water mixture stays at the halogen desorption treatment pressure for a predetermined residence time,
The oil reaction water mixture desalted in the desalting reaction vessel is cooled to recover the desalted regenerated oil.
A method for converting waste oil into fuel resources having each process.

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