CN108048200B - Waste oil distillation cracking catalytic system and production process - Google Patents
Waste oil distillation cracking catalytic system and production process Download PDFInfo
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- CN108048200B CN108048200B CN201810090714.4A CN201810090714A CN108048200B CN 108048200 B CN108048200 B CN 108048200B CN 201810090714 A CN201810090714 A CN 201810090714A CN 108048200 B CN108048200 B CN 108048200B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
- C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
- C10M175/0075—Working-up used lubricants to recover useful products ; Cleaning synthetic oil based
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/146—Multiple effect distillation
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
- C10G55/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one catalytic cracking step
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
Abstract
The invention discloses a waste oil distillation cracking catalysis system and a production process, which comprises a primary distillation device, a secondary distillation device and a catalytic cracking tower which are sequentially communicated, wherein the primary distillation device is provided with a gaseous component collecting port I, the catalytic cracking tower is provided with a gaseous component collecting port II and a gaseous component collecting port III, and the catalytic cracking tower is connected with a negative pressure generator. The waste oil distillation cracking catalytic system and the production process provided by the invention have the advantages of novel structure, easiness in realization and high reliability, and by utilizing one set of waste oil distillation cracking catalytic system, the waste oil can be regenerated into diesel oil and base oil, so that the equipment purchase and investment cost is greatly reduced, the site area demand is small, the burden of enterprises is effectively reduced, and the economic and market values are extremely high.
Description
Technical Field
The invention belongs to the technical field of oil recovery and refining, and particularly relates to a waste oil distillation cracking catalytic system and a production process.
Background
The regeneration processing and utilization of the waste lubricating oil (waste engine oil) not only can generate great economic benefit, but also has great significance for environmental protection, and can effectively reduce the pollution to the atmosphere, water sources and soil. Therefore, research on recycling of waste lubricating oil is accelerated at home and abroad.
Currently, methods for regenerating used oil are classified into the following three categories: 1. chemical treatment method: the waste lubricating oil is subjected to steps of acid washing, alkali washing neutralization, decoloration and the like, long time and reaction of various chemical raw materials are needed to realize the regeneration of the waste lubricating oil, and meanwhile, a large amount of industrial waste materials such as acid sludge and the like are generated to cause environmental pollution, so that the chemical treatment method is a waste engine oil regeneration method prohibited by the present plain text of China; 2. a distillation method: the traditional distillation method, commonly known as the clay scouring method, is to directly heat the waste engine oil to gasify and evaporate the waste engine oil, and the high-temperature gaseous oil mist is condensed into liquid oil under the cooling effect of a condenser to be collected, wherein the biggest problems of the distillation method are that the purity of the collected oil is low (comprising various mixed oil components such as gasoline, diesel oil and the like), the collected oil is easy to oxidize and discolor, the production efficiency is low and the like; 3. molecular distillation method: the molecular distillation method can overcome the main problems of the chemical treatment method and the distillation method, but the equipment adopted in the three waste engine oil regeneration processes has the most complex structure, is difficult to manufacture and install, has huge investment and high operation cost, and cannot meet the requirement of large-scale waste lubricating oil regeneration processing.
The existing one set of distillation cracking catalytic system can only produce one set of distillation cracking products, waste oil is usually regenerated into diesel oil or base oil, if an enterprise needs to regenerate the waste oil into the diesel oil and also needs to regenerate the waste oil into the base oil, two sets of distillation cracking catalytic systems are needed, equipment purchase and investment cost are greatly improved, the requirement on site area is large, and the burden of the enterprise is increased. It is urgent to solve the above problems.
Disclosure of Invention
In order to solve the technical problems, the invention provides a waste oil distillation cracking catalytic system and a production process, which can produce two groups of distillation cracking products by switching.
In order to achieve the purpose, the technical scheme of the invention is as follows:
the utility model provides a waste oil distillation pyrolysis catalytic system, includes one-level distillation plant, second grade distillation plant and the catalytic cracking tower that communicates in proper order, its main points lie in: the first-stage distillation device is provided with a gaseous component collecting port I, the catalytic cracking tower is provided with a gaseous component collecting port II and a gaseous component collecting port III, and the catalytic cracking tower is connected with a negative pressure generator.
By adopting the structure, the waste oil is heated in the primary distillation device, part of the waste oil is distilled and gasified and then is discharged from the gaseous component collecting port I, the rest liquid waste oil enters the secondary distillation device, the waste oil is further heated in the secondary distillation device, the waste oil is distilled and gasified to obtain gaseous components and enters the catalytic cracking tower, and the gaseous components obtained by cracking are respectively discharged from the gaseous component collecting port II and the gaseous component collecting port III; collecting a light component with a lower boiling point from the gaseous component collecting port I, collecting a light component with a higher boiling point than the gaseous component collecting port I from the gaseous component collecting port II, and collecting a heavy component from the gaseous component collecting port III; when the negative pressure generator is closed, a group of distillation cracking products mainly comprising diesel oil can be obtained by controlling the temperature, and when the negative pressure generator is closed, another group of distillation cracking products mainly comprising base oil can be obtained by controlling the temperature; the structure is reliable, the manufacturing and the installation are easy, the equipment purchasing and investment cost are greatly reduced, the field area requirement is small, the burden of an enterprise is effectively reduced, and the economic and market values are high.
Preferably, the method comprises the following steps: the upper part of the catalytic cracking tower is divided into a low-temperature area and a high-temperature area, the low-temperature area is positioned above the high-temperature area, an atomizing device is arranged in the low-temperature area, the negative pressure generator and the gaseous component collecting port II are communicated with the low-temperature area, and the gaseous component collecting port III is communicated with the high-temperature area. By adopting the structure, the upper part of the catalytic cracking tower forms a low-temperature area and a high-temperature area through the control of the atomizing device, the efficiency is high, the reliability is good, and two different gaseous components are discharged from the gaseous component collecting port II and the gaseous component collecting port III.
Preferably, the method comprises the following steps: gaseous state component is collected mouthful II and is collected pipeline II and communicate with condensation tower I and collection tank II in proper order through the condensation, collection tank II passes through negative pressure pipeline and negative pressure generator intercommunication, and this collection tank II is through supplying liquid return circuit and atomizing device intercommunication. By adopting the structure, the condensation collection of the light components is realized, the light components can be utilized to directly supply liquid to the atomization device, and the additional liquid supply for the atomization device is not needed.
Preferably, the method comprises the following steps: gaseous state component is collected mouthful III and is collected pipeline III through the condensation and communicate with condensing tower II and collection tank III in proper order, and this collection tank III communicates with second grade distillation plant through air feed return circuit. By adopting the structure, the condensation and collection of the heavy components are realized, and the gaseous heavy components in the collection tank III can be conveyed to the secondary distillation device to be used as fuel of the secondary distillation device.
Preferably, the method comprises the following steps: a preheating oil supply pipeline, a heat supply pipeline and a distillation oil supply pipeline are arranged between the primary distillation device and the secondary distillation device, and the secondary distillation device is communicated with the catalytic cracking tower through a gas conveying pipeline; when the waste oil enters the primary distillation device, gaseous components obtained by distillation are discharged from the gaseous component collecting port I, the residual waste oil enters the secondary distillation device for heating through the preheating oil supply pipeline, the heated waste oil flows back to the primary distillation device through the heat supply pipeline to be used as a heat source of the primary distillation device, the waste oil flowing back to the primary distillation device returns to the secondary distillation device again through the distillation oil supply pipeline, and the gaseous components obtained by distillation enter the catalytic cracking tower through the gas conveying pipeline. By adopting the structure, the internal structures of the primary distillation device and the secondary distillation device are limited through the inlet and the outlet, so that the primary distillation device and the secondary distillation device, together with the preheating oil supply pipeline, the heat supply pipeline and the distillation oil supply pipeline, form a waste oil secondary molecular distillation passage with clear and definite circuits, and the specific structural design and the manufacture of the primary distillation device and the secondary distillation device are facilitated.
Preferably, the method comprises the following steps: the inside of the primary distillation device comprises a primary distillation cavity and a reflux heat supply cavity for heating the primary distillation cavity; the secondary distillation device comprises an outer cylinder and a heating cylinder arranged in the outer cylinder, a heat source cavity is arranged in the heating cylinder, and a secondary distillation cavity is formed between the outer cylinder and the heating cylinder; the primary distillation cavity is communicated with the heat source cavity through a preheating oil supply pipeline, the heat source cavity is communicated with the reflux heat supply cavity through a heat supply pipeline, and the reflux heat supply cavity is communicated with the secondary distillation cavity through a distillation oil supply pipeline. By adopting the structure, the waste oil is heated in the primary distillation cavity, part of the waste oil is distilled and gasified and then is discharged from the gas component collecting port I, the rest liquid waste oil flows into the heat source cavity, the waste oil is heated in the heat source cavity and then flows into the reflux heat supply cavity, the waste oil in the reflux heat supply cavity supplies heat to the primary distillation cavity and is the only heat source of the primary distillation cavity, the waste oil in the reflux heat supply cavity flows into the secondary distillation cavity, is heated by the heating cylinder in the secondary distillation cavity, is distilled and gasified to obtain gas components, and is introduced into the catalytic cracking tower from the gas conveying pipeline; the primary distillation device and the secondary distillation device can share one heat source in the heating cylinder, so that the energy utilization rate is greatly improved, the energy consumption is reduced, and the production and operation cost is effectively reduced; the primary distillation device and the secondary distillation device have novel structures, are simple and reliable, are easy to manufacture and have low cost.
Preferably, the method comprises the following steps: an oil-liquid distributor is sleeved outside the heating cylinder, and a gap is reserved between the oil-liquid distributor and the cylinder wall of the heating cylinder; when the waste oil on the upper end surface of the heating cylinder flows through the gap, a film-shaped oil layer is formed on the cylinder wall of the heating cylinder. Structure more than adopting, through the design of oil liquid distributor, after making waste oil flow through the clearance between the oil liquid distributor heating cylinder section of thick bamboo wall, can be the film form attached to the section of thick bamboo wall of heating cylinder, and thickness is even to improved the efficiency of used oil molecular distillation by a wide margin, can satisfy large-scale waste oil regeneration processing demand, reduced the consumption of the energy, reduction production running cost.
Preferably, the method comprises the following steps: an oil liquid pre-distributor is arranged above the heating cylinder, and a circle of annular liquid outlet is formed in the lower portion of the oil liquid pre-distributor. Structure more than adopting, through fluid pre-distributor can avoid waste oil to gush the up end to the heating cylinder, but is on the up end of heating cylinder with spilling waterfall form to cooperation oil distributor has effectively improved the shaping efficiency that forms the film oil reservoir on the heating cylinder section of thick bamboo wall, prevents simultaneously that waste oil from outwards gushing out the condition of oil distributor and taking place.
Preferably, the method comprises the following steps: an inner tank is arranged in the primary distillation device, the reflux heat supply cavity is formed between the inner tank and the primary distillation device, the inner cavity of the inner tank is the primary distillation cavity, and a stirrer is arranged in the primary distillation device; after the waste oil enters the primary distillation cavity, a film-shaped oil layer is formed on the inner wall of the inner tank through the stirrer. Structure more than adopting, simple structure is reliable, easily makes, low cost, and waste oil preheats efficiently, through the agitator, can form film form oil reservoir on the inner wall of inner tank fast to improved the efficiency that used oil preheats and molecular distillation by a wide margin, satisfied large-scale waste oil regeneration processing demand, reduce the consumption of the energy, reduction production running cost.
The production process of distillation cracking catalysis of waste oil includes the following steps:
the method a, closing the negative pressure generator, controlling the temperature of the gaseous component collecting port I to be 100-150 ℃, controlling the temperature of the gaseous component collecting port II to be 150-260 ℃, and controlling the temperature of the gaseous component collecting port III to be 380-420 ℃ to obtain a first group of distillation cracking products;
and b, opening the negative pressure generator, controlling the temperature of the gaseous component collecting port I to be 100-180 ℃, the temperature of the gaseous component collecting port II to be 150-200 ℃, and the temperature of the gaseous component collecting port III to be 220-320 ℃ so as to obtain a second group of distillation cracking products.
By adopting the method, two groups of different distillation cracking products can be obtained by controlling the opening and closing of the negative pressure generator and the temperatures of the gaseous component collecting port I, the gaseous component collecting port II and the gaseous component collecting port III; by the method a, water and gasoline can be collected from the gaseous component collecting port I, light diesel oil is collected from the gaseous component collecting port II, heavy diesel oil is collected from the gaseous component collecting port III, and the light diesel oil and the heavy diesel oil account for 85% -92% of the refined product; by the method b, water, gasoline and diesel oil can be collected from the gaseous component collecting port I, the diesel oil is collected from the gaseous component collecting port II, and the base oil is collected from the gaseous component collecting port III, wherein the base oil accounts for 75-80% of the refined product, and the light components mainly comprising the gasoline and the diesel oil account for 8-12% of the refined product; therefore, the waste oil distillation cracking catalytic system can be utilized to regenerate the waste oil into diesel oil and also regenerate the waste oil into base oil.
Compared with the prior art, the invention has the beneficial effects that:
the waste oil distillation cracking catalytic system and the production process provided by the invention have the advantages of novel structure, easiness in realization and high reliability, and by utilizing one set of waste oil distillation cracking catalytic system, the waste oil can be regenerated into diesel oil and base oil, so that the equipment purchase and investment cost is greatly reduced, the site area demand is small, the burden of enterprises is effectively reduced, and the economic and market values are extremely high.
Drawings
FIG. 1 is a schematic view of the present invention;
FIG. 2 is a schematic view of the external structure of a two-stage distillation apparatus;
FIG. 3 is a schematic view of the internal structure of a two-stage distillation apparatus;
FIG. 4 is an enlarged view taken at A in FIG. 3;
FIG. 5 is a schematic view of an oil pre-distributor;
FIG. 6 is a schematic view of the structure of a primary distillation apparatus;
fig. 7 is a schematic structural view of a catalytic cracking tower.
Detailed Description
The present invention will be further described with reference to the following examples and the accompanying drawings.
Referring to fig. 1, a waste oil distillation cracking catalytic system comprises a primary distillation device 2, a secondary distillation device 1 and a catalytic cracking tower 3 which are sequentially communicated, wherein the primary distillation device 2 is provided with a gaseous component collecting port i 23, the catalytic cracking tower 3 is provided with a gaseous component collecting port ii 31 and a gaseous component collecting port iii 32, and the catalytic cracking tower 3 is connected with a negative pressure generator 33.
It should be emphasized that the primary distillation unit 2 may be disposed inside the catalytic cracking tower 3 and combined with the catalytic cracking tower 3 into one unit, and the primary distillation unit 2 may be separated from the catalytic cracking tower 3, so that the primary distillation unit 2 and the catalytic cracking tower 3 are two independent units. Such a design greatly improves the flexibility of installation and sale of the device.
Referring to fig. 1 and 7, the upper portion of the catalytic cracking tower 3 is divided into a low temperature region 35 and a high temperature region 36, the low temperature region 35 is located above the high temperature region 36, an atomizing device 34 is disposed in the low temperature region 35, the negative pressure generator 33 and the gaseous component collecting port ii 31 are both communicated with the low temperature region 35, and the gaseous component collecting port iii 32 is communicated with the high temperature region 36.
Specifically, the gaseous component collection port II 31 is sequentially communicated with the condensation tower I42 and the collection tank II 52 through a condensation collection pipeline II 808, and the gaseous light component is condensed into a liquid state on the condensation tower I42 and then collected by the collection tank II 52.
Furthermore, the collection tank II 52 is communicated with the atomizing device 34 through the liquid supply loop 811, and the light components are used for directly supplying liquid to the atomizing device 34 without additionally providing liquid supply for the atomizing device 34. The liquid supply circuit 811 is provided with a booster oil pump i 61 for boosting pressure.
Further, the collection tank II 52 is communicated with the negative pressure generator 33 through a negative pressure pipeline 810, and the negative pressure generator 33 preferably adopts a vacuum pump, so that the stability and reliability are realized, and the cost is low. And, at least one buffer tank 54 is provided on the negative pressure pipeline 810 to ensure stability of the negative pressure state.
Referring to fig. 1, the gaseous component collecting port iii 32 is sequentially communicated with the condensing tower ii 43 and the collecting tank iii 53 through a condensing collecting line iii 809, and the gaseous heavy component is condensed to a liquid state on the condensing tower ii 43 and then collected by the collecting tank iii 53.
Further, the collecting tank III 53 is communicated with the secondary distillation device 1 through the air supply loop 812, and the gaseous heavy components in the collecting tank III 53 can be conveyed to the secondary distillation device 1 to be used as fuel of the secondary distillation device 1. It should be noted that the water seal 71 and the flame arrester 72 are arranged on the air supply loop 812, so that the safety of air supply is greatly improved.
Further, the catalytic cracking tower 3 is communicated with the preheating oil supply pipeline 801 through the oil liquid loop 813, uncracked components are circulated to the preheating oil supply pipeline 801, and molecular distillation is carried out through the primary distillation device 2 and the secondary distillation device 1 again, so that the conversion rate of waste oil recycling is greatly improved. Moreover, a cooling device 77 is arranged on the oil liquid loop 813, so that the liquid components which circulate back to the preheating oil supply pipeline 801 are liquid components, and the normal operation of the whole system is ensured.
Referring to fig. 1 to 6, the primary distillation apparatus 2 includes a primary distillation chamber 21 and a reflux heat supply chamber 22, the reflux heat supply chamber 22 may be covered outside the primary distillation chamber 21, may also be located inside the primary distillation chamber 21, and may also be of other structures as long as the reflux heat supply chamber 22 can provide heat for the primary distillation chamber 21. The primary distillation device 2 is provided with a gaseous component collecting port I23 communicated with the primary distillation cavity 21. The secondary distillation device 1 comprises an outer cylinder 11 and a heating cylinder 12 arranged inside the outer cylinder 11, a secondary distillation cavity 13 is formed between the outer cylinder 11 and the heating cylinder 12, a gas outlet 113 communicated with the secondary distillation cavity 13 is arranged on the outer cylinder 11, and the gas outlet 113 is communicated with the catalytic cracking tower 3 through a gas conveying pipeline 806. The heating cartridge 12 has a heat source chamber 121 inside. The primary distillation cavity 21, the heat source cavity 121, the backflow heat supply cavity 22 and the secondary distillation cavity 13 are sequentially communicated through pipelines, and after waste oil sequentially flows through the primary distillation cavity 21, the heat source cavity 121, the backflow heat supply cavity 22 and the secondary distillation cavity 13, gaseous components obtained through distillation are discharged through the gaseous component collecting port I23 and the gas outlet 113.
Specifically, the waste oil is heated in the primary distillation chamber 21, at this time, the waste oil is partially distilled and gasified and then discharged from the gaseous component collecting port i 23, the remaining liquid waste oil flows into the heat source chamber 121, the waste oil is heated in the heat source chamber 121 and then flows into the reflux heat supply chamber 22, the hotter waste oil in the reflux heat supply chamber 22 supplies heat to the primary distillation chamber 21 and is the only heat source of the primary distillation chamber 21, the waste oil in the reflux heat supply chamber 22 flows into the secondary distillation chamber 13 and is heated by the heating cylinder 12 in the secondary distillation chamber 13, the gaseous component is obtained through distillation and gasification, the waste oil is discharged from the gas outlet 113 and is introduced into the catalytic cracking tower 3 through the gas conveying pipeline 806.
More specifically, the primary distillation device 2 is provided with an oil outlet 27, a reflux heat supply inlet 221, a reflux heat supply outlet 222 and a gaseous component collection port I23, and the secondary distillation device 1 is provided with a preheating inlet 124, a preheating outlet 125, a distillation inlet 112 and a gas outlet 113.
A preheating oil supply pipeline 801 is connected between the oil outlet 27 and the preheating inlet 124, a heat supply pipeline 802 is connected between the preheating outlet 125 and the backflow heat supply inlet 221, and a distillation oil supply pipeline 803 is connected between the backflow heat supply outlet 222 and the distillation inlet 112.
When the waste oil enters the primary distillation device 2, the gaseous components obtained by distillation are discharged from a gaseous component collecting port I23, the rest waste oil enters the secondary distillation device 1 for heating through a preheating oil supply pipeline 801, the heated waste oil flows back to the primary distillation device 2 through a heat supply pipeline 802 to be used as a heat source of the primary distillation device 2, the waste oil flowing back to the primary distillation device 2 returns to the secondary distillation device 1 again through a distillation oil supply pipeline 803, the gaseous components obtained by distillation are discharged from a gas outlet 113 and are introduced into a catalytic cracking tower 3 through a gas conveying pipeline 806.
As shown in fig. 2 to 5, the specific structure of the secondary distillation apparatus 1 is as follows:
referring to fig. 2 and 3, the secondary distillation apparatus 1 includes an outer tube 11 and a heating tube 12 disposed inside the outer tube 11, the heating tube 12 has a heat source chamber 121 inside, a secondary distillation chamber 13 is formed between the outer tube 11 and the heating tube 12, the preheating inlet 124 and the preheating outlet 125 are communicated with the heat source chamber 121, and the distillation inlet 112 and the gaseous component collecting port ii 113 are communicated with the heat source chamber 121.
Referring to fig. 3, the heating cylinder 12 is a cylindrical tank structure, the heat source cavity 121 is formed inside the heating cylinder 12, the lower end of the heating cylinder 12 penetrates through the outer cylinder 11, a heat source inlet 123 and a flue gas discharge pipe 122 communicated with the heat source cavity 121 are arranged on the heating cylinder 12, wherein the heat source inlet 123 is located at the lower end of the heating cylinder 12, the heat source inlet 123 is connected with the burner 73, and it should be noted that the outlet of the air supply loop 812 is located near the heat source inlet 123, and is located reasonably and sufficiently to burn. The flue gas outlet pipe 122 is located at the upper end of the heating cylinder 12, and the burner 73 provides hot gas into the heating cylinder 12, and the hot gas is finally discharged from the flue gas outlet pipe 122. Therefore, the design that the heat is spread from bottom to top can improve the heating efficiency of the heating tube 12 tube wall and the preheating tube 16 by the heat source, and the utilization efficiency of energy is improved. The gas inlet end of the flue gas discharge pipe 122 is installed on the upper end face of the heating cylinder 12 and is communicated with the heat source cavity 121, the flue gas discharge pipe 122 extends upwards, then is bent outwards to form an L shape, and finally penetrates out of the outer cylinder 11, and the design of the flue gas discharge pipe 122 is convenient for installing the oil pre-distributor 14.
A preheating pipe 16 is provided in the heating cylinder 12, a preheating pipe 16 distributed in a spiral manner is provided in the heat source chamber 121, one end of the preheating pipe 16 is communicated with the primary distillation chamber 21 through a preheating oil supply line 801, and the other end is communicated with the reflux heat supply chamber 22 through a heat supply line 802. It should be noted that the inlet end of the preheating pipe 16 is located below the outlet end, and this design can further improve the efficiency of preheating the used oil. Therefore, the preheating oil supply line 801 is inserted into the heating cylinder 12 through the outer cylinder 11 to communicate with the inlet end of the preheating pipe 16; the heat supply pipe 802 is inserted into the heating cylinder 12 through the outer cylinder 11 and communicates with the outlet end of the preheating pipe 16.
Referring to fig. 2 and 3, the outer tube 11 is a cylindrical tank structure, the bottom wall 111 of the outer tube 11 extends obliquely upward from the side wall of the outer tube 11 to the wall of the heating tube 12 to form a conical structure with a small top and a large bottom, and the lower end of the side wall of the outer tube 11 is provided with a slag outlet 115, so that impurities such as heavy oil, asphalt and the like remaining in the secondary distillation chamber 13 can be discharged even when the whole equipment is not shut down, thereby maintaining the cleanliness of the secondary distillation chamber 13 and improving the efficiency of molecular distillation of the waste oil. The slag outlet 115 is connected to a slag collection box 74 via a slag line 805, so that impurities such as heavy oil and asphalt can be collected and treated.
The outer barrel 11 is provided with a gaseous component collecting port II 113, and the gaseous component collecting port II 113 is positioned at the upper end of the outer barrel 11 so as to be beneficial to discharge of gaseous components. The distillation oil supply pipeline 803 is inserted into the secondary distillation cavity 13 through the distillation inlet 112 of the outer cylinder 11, and the oil outlet of the distillation oil supply pipeline 803 is positioned above the upper end surface of the heating cylinder 12, so that waste oil can be led to the upper end surface of the heating cylinder 12, and a film-shaped oil layer can be formed on the cylinder wall of the heating cylinder 12. Furthermore, an oil return port 114 is disposed at the lower portion of the outer cylinder 11, and the position of the oil return port 114 is lower than the upper end surface of the heating cylinder 12 and higher than the position of the slag outlet 115, it should be noted that the position of the oil return port 114 should not be too high so as to avoid affecting the area of the film-like oil layer formed on the cylinder wall of the heating cylinder 12, thereby ensuring the efficiency of molecular distillation. In addition, the oil return port 114 is communicated with the distillation oil supply pipeline 803 through an oil return pipeline 804, so that the circulation and supplement of the waste oil are realized. Oil storage tank 75 is arranged on oil return pipeline 804, level gauge 76 is installed on oil storage tank 75, and supply regulation of oil can be realized through oil storage tank 75, and it is too much to further prevent the oil that second grade distillation chamber 13 bottom is gathered, simultaneously, can accurately learn the oil mass in oil storage tank 75 through level gauge 76 to the control should open oil storage tank 75 and supply oil to distillation oil supply pipeline 803, still open backward flow heat supply chamber 22 and supply oil to distillation oil supply pipeline 803.
Referring to fig. 3 and 4, an oil-liquid distributor 15 is installed at an upper end portion of the heating cylinder 12, and a gap 17 is formed between the oil-liquid distributor 15 and a cylinder wall of the heating cylinder 12, so that waste oil introduced from a distillation oil supply line 803 to an upper end surface of the heating cylinder 12 flows through the gap 17 to form a film-like oil layer on the cylinder wall of the heating cylinder 12. Specifically, the oil-liquid distributor 15 is annular and is fitted over the heating cylinder 12, the gap 17 is formed between the inner wall of the oil-liquid distributor 15 and the cylinder wall of the heating cylinder 12, and the upper edge of the oil-liquid distributor 15 is higher than the upper end surface of the heating cylinder 12 and the lower edge thereof is lower than the upper end surface of the heating cylinder 12, so that the waste oil on the upper end surface of the heating cylinder 12 can be effectively prevented from being discharged outward, and the waste oil can continuously and efficiently form a film-shaped oil-liquid layer on the cylinder wall of the heating cylinder 12. In addition, the lower edge of the oil-liquid distributor 15 is narrowed inward, so that the thickness of the film-shaped oil layer formed on the cylinder wall of the heating cylinder 12 is thinner, and the molecular distillation efficiency of the waste oil is further improved.
Referring to fig. 3 and 5, an oil pre-distributor 14 is disposed above the heating cylinder 12, a ring-shaped liquid outlet 141 is formed at a lower portion of the oil pre-distributor 14, and an oil outlet of the distillation oil feed line 803 is located inside the oil pre-distributor 14. Specifically, the oil predistributor 14 includes a disc-shaped mounting portion 142 and a ring-shaped collecting portion 143, the mounting portion 142 and the collecting portion 143 form a cylindrical structure with an open upper portion, and the liquid outlet 141 is formed between the lower edge of the collecting portion 143 and the outer edge of the mounting portion 142. And, the installation department 142 cover is established on flue gas discharge pipe 122, and the installation is easy, reliable and stable. The distillation oil supply line 803 is inserted from the opening of the oil predistributor 14.
Referring to fig. 1 and 6, the primary distillation apparatus 2 has the following specific structure:
an inner tank 24 is arranged in the primary distillation device 2, the reflux heat supply cavity 22 is formed between the inner tank 24 and the inner wall of the primary distillation device 2, and the inner cavity of the inner tank 24 is the primary distillation cavity 21. Be provided with agitator 25 in the inside of one-level distillation plant 2, this agitator 25 inserts in one-level distillation chamber 21, and after waste oil got into one-level distillation chamber 21, through agitator 25 formation film form the oil reservoir on the inner wall of inner tank 24, improved waste oil preheating and light component distillation gasification's efficiency by a wide margin.
Further, referring to fig. 1, the gaseous component collecting port i 23 is sequentially communicated with the heat exchanger 41 and the collecting tank i 51 through a condensation collecting pipeline i 807, and the gaseous light component is condensed into a liquid state on the heat exchanger 41 and then collected by the collecting tank i 51.
Referring to fig. 6, the back-flow heat-supplying chamber 22 has a back-flow heat-supplying inlet 221 at the bottom and a back-flow heat-supplying outlet 222 at the top, the back-flow heat-supplying inlet 221 is communicated with the outlet end of the preheating pipe 16 through a heat-supplying pipe 802, and the back-flow heat-supplying outlet 222 is connected with a distillation oil-supplying pipe 803.
The primary distillation device 2 is provided with an oil inlet 26 and an oil outlet 27, the oil inlet 26 is located at the upper end of the primary distillation device 2, the oil outlet 27 is located at the lower end of the primary distillation device 2, and the oil outlet 27 is communicated with the inlet end of the preheating pipe 16 through a pipeline.
Referring to fig. 6, a pressurizing oil pump ii 62 for pressurizing is disposed on the preheating oil supply line 801, and a pressurizing oil pump iii 63 for pressurizing is disposed on the oil return line 804 to provide pressure for flowing the oil.
Further, all install the check valve on each pipeline to prevent the backward flow, be convenient for control pipeline's switching simultaneously.
A production process for distillation cracking catalysis of waste oil is characterized by comprising the following steps:
the method a comprises the steps of closing the negative pressure generator 33, controlling the temperature of the gaseous component collecting port I23 to be 100-150 ℃, controlling the temperature of the gaseous component collecting port II 31 to be 150-260 ℃, and controlling the temperature of the gaseous component collecting port III 32 to be 380-420 ℃ to obtain a first group of distillation cracking products.
By the method a, the light components collected from the gaseous component collecting port I mainly comprise water and gasoline, the light diesel oil is collected from the gaseous component collecting port II, and the heavy diesel oil is collected from the gaseous component collecting port III, wherein the light diesel oil and the heavy diesel oil account for 85-92% of the refined product, and the residue accounts for 8-12%.
And b, opening the negative pressure generator 33, controlling the temperature of the gaseous component collecting port I23 to be 100-180 ℃, controlling the temperature of the gaseous component collecting port II 31 to be 150-200 ℃, and controlling the temperature of the gaseous component collecting port III 32 to be 220-320 ℃ to obtain a second group of distillation cracking products.
By the method b, the light components collected from the gaseous component collecting port I mainly comprise water, gasoline, diesel oil and the like, the diesel oil is collected from the gaseous component collecting port II, the base oil accounts for 75-80% of the refined product and the light components mainly comprising the gasoline and the diesel oil account for 8-12% of the refined product and the residues account for 5-8% of the refined product.
Finally, it should be noted that the above-mentioned description is only a preferred embodiment of the present invention, and that those skilled in the art can make various similar representations without departing from the spirit and scope of the present invention.
Claims (5)
1. The utility model provides a waste oil distillation schizolysis catalytic system, includes one-level distillation plant (2), second grade distillation plant (1) and catalytic cracking tower (3) that communicate in proper order, its characterized in that: the primary distillation device (2) is provided with a gaseous component collecting port I (23), the catalytic cracking tower (3) is provided with a gaseous component collecting port II (31) and a gaseous component collecting port III (32), and the catalytic cracking tower (3) is connected with a negative pressure generator (33);
a preheating oil supply pipeline (801), a heat supply pipeline (802) and a distillation oil supply pipeline (803) are arranged between the primary distillation device (2) and the secondary distillation device (1), and the secondary distillation device (1) is communicated with the catalytic cracking tower (3) through a gas conveying pipeline (806);
when waste oil enters a primary distillation device (2), gaseous components obtained by distillation are discharged from a gaseous component collecting port I (23), the residual waste oil enters a secondary distillation device (1) for heating through a preheating oil supply pipeline (801), the heated waste oil flows back to the primary distillation device (2) through a heat supply pipeline (802) to be used as a heat source of the primary distillation device (2), the waste oil flowing back to the primary distillation device (2) returns to the secondary distillation device (1) again through a distillation oil supply pipeline (803), and the gaseous components obtained by distillation enter a catalytic cracking tower (3) through a gas conveying pipeline (806);
the primary distillation device (2) comprises a primary distillation cavity (21) and a reflux heat supply cavity (22) for heating the primary distillation cavity (21);
the secondary distillation device (1) comprises an outer cylinder (11) and a heating cylinder (12) arranged inside the outer cylinder (11), a heat source cavity (121) is arranged inside the heating cylinder (12), and a secondary distillation cavity (13) is formed between the outer cylinder (11) and the heating cylinder (12);
the primary distillation cavity (21) is communicated with the heat source cavity (121) through a preheating oil supply pipeline (801), the heat source cavity (121) is communicated with the reflux heat supply cavity (22) through a heat supply pipeline (802), and the reflux heat supply cavity (22) is communicated with the secondary distillation cavity (13) through a distillation oil supply pipeline (803);
an oil-liquid distributor (15) is sleeved outside the heating cylinder (12), and a gap (17) is reserved between the oil-liquid distributor (15) and the cylinder wall of the heating cylinder (12);
after the waste oil on the upper end surface of the heating cylinder (12) flows through the gap (17), a film-shaped oil layer is formed on the cylinder wall of the heating cylinder (12);
an oil liquid pre-distributor (14) is arranged above the heating cylinder (12), and a ring of annular liquid outlet (141) is formed in the lower portion of the oil liquid pre-distributor (14).
2. The used oil distillative cracking catalytic system of claim 1, wherein: the upper part of the catalytic cracking tower (3) is divided into a low-temperature area (35) and a high-temperature area (36), the low-temperature area (35) is positioned above the high-temperature area (36), an atomizing device (34) is arranged in the low-temperature area (35), the negative pressure generator (33) and the gaseous component collecting port II (31) are communicated with the low-temperature area (35), and the gaseous component collecting port III (32) is communicated with the high-temperature area (36).
3. The used oil distillative cracking catalytic system of claim 2, wherein: the gas component collecting port II (31) is sequentially communicated with the condensing tower I (42) and the collecting tank II (52) through a condensing collecting pipeline II (808), the collecting tank II (52) is communicated with the negative pressure generator (33) through a negative pressure pipeline (810), and the collecting tank II (52) is communicated with the atomizing device (34) through a liquid supply loop (811).
4. The used oil distillative cracking catalytic system of claim 2, wherein: the gaseous component collecting port III (32) is sequentially communicated with a condensing tower II (43) and a collecting tank III (53) through a condensing collecting pipeline III (809), and the collecting tank III (53) is communicated with the secondary distillation device (1) through an air supply loop (812).
5. The used oil distillation cracking catalytic system according to any one of claims 1 to 4, wherein: an inner tank (24) is arranged in the primary distillation device (2), a reflux heat supply cavity (22) is formed between the inner tank (24) and the primary distillation device (2), the inner cavity of the inner tank (24) is the primary distillation cavity (21), and a stirrer (25) is arranged in the primary distillation device (2);
after the waste oil enters the primary distillation chamber (21), a film-shaped oil layer is formed on the inner wall of the inner tank (24) through the stirrer (25).
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| CN116426314A (en) * | 2023-05-16 | 2023-07-14 | 重庆工商大学 | Method for catalytically thermally cracking industrial waste oil by microwaves |
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