CN213824746U - Novel plasma medium and high temperature coal tar combined oil refining device - Google Patents
Novel plasma medium and high temperature coal tar combined oil refining device Download PDFInfo
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- CN213824746U CN213824746U CN202022331429.2U CN202022331429U CN213824746U CN 213824746 U CN213824746 U CN 213824746U CN 202022331429 U CN202022331429 U CN 202022331429U CN 213824746 U CN213824746 U CN 213824746U
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Abstract
The utility model discloses a novel plasma medium-high temperature coal tar combined oil refining device, which comprises an emulsification tank, wherein the delivery outlet is communicated with an atmospheric pressure reactor through a low-pressure oil pump, an oil spray head I is arranged at the inner side of the reactor at the communication part, a heavy oil outlet at the lower part of the reactor is communicated with a pipeline mixer I, the delivery outlet is communicated with a plasma decompression reactor through the high-temperature low-pressure oil pump I, an oil spray head II is arranged at the inner side of the reactor at the communication part, a heavy oil outlet at the lower part of the reactor is communicated with a pipeline mixer II, the delivery outlet is communicated with a medium-high pressure reactor through a medium-high pressure oil pump I, an oil spray head III is arranged at the inner side of the reactor at the communication part, the heavy oil outlet at the lower part of the reactor is communicated with a heavy oil separator, the lower part outlet is a very small amount of residual oil of the device, and a mixed gas outlet above the medium-high pressure reactor is communicated with a fractionating system, the oil and gas products are fractionated, the device is very simple, the operation is easy, the cost is low, and the safety coefficient is high.
Description
The technical field is as follows:
the utility model relates to an oil refining equipment technical field specifically is a novel, among plasma, high temperature coal tar combination oil refining device.
Background art:
the coal tar hydrocracking process comprises the following steps: the yield of coal tar in China is 800-1000 million tons, coal tar is used as a raw material, and hydrocracking is converted into light fuel oil, so that the increasingly short crude oil resource can be effectively replaced, and the utilization value of low-temperature coal tar can be improved.
The hydrocracking process of the medium-high temperature coal tar comprises the following steps: according to the characteristics of high-aromatic narrow fraction of medium-high temperature coal tar, a new xsun combined hydrocracking process is developed by a medium-petrochemical smoothness research institute chensong and the like, the reaction pressure is 17.7-18.1 mpa, and the temperature is 360-380 ℃. And designs a CN series hydrocracking catalyst special for coal tar, and is matched with a flexible new combined hydrogenation technical operation scheme. Can process inferior high-temperature coal tar and realize the lightening of heavy fraction of the coal tar. But the mass fraction of nitrogen in the hydrogenation product oil is higher, still about 0.3 percent, and the requirement of environmental protection can not be met. M developed by using energy and chemical system of Shanghai east China university of eastern science and technology0o3—Nio/r— AI2O3A hydrocracking catalyst.The raw oil of the gas and the diesel oil with the grade and the gas oil and the diesel oil with the high grade are produced by the inferior coal tar through hydrocracking.
The hydrogen used for hydrocracking is stable under normal temperature and pressure conditions and is not easy to react with other elements. However, under the conditions of high temperature, high pressure and high hydrogen pressure, the catalyst is easy to react with a plurality of elements, and easily enters into crystal lattices of a plurality of metal structures, so that the hydrogen danger phenomenon occurs, the metal strength is reduced, and physical explosion and leakage explosion are caused, so that the high-pressure hydrogen equipment must use expensive Monel alloy steel, and the investment of the hydrogenation equipment is very high.
Hydrocracking is a gas phase reaction and a liquid phase reaction, and the operation pressure of equipment is high pressure or even ultrahigh pressure, so that the technical requirements on the strength of a reactor and equipment thereof, welding at joints, flanges and other joints for equipment manufacturing are high. So the construction investment is also increased.
Therefore, the medium and high temperature coal tar hydrocracking device has the defects of very high equipment investment cost, low safety factor, harsh operating conditions and the like.
In view of this prime, a novel plasma medium-high temperature coal tar combined oil refining device needs to be designed.
The utility model has the following contents:
an object of the utility model is to provide a novel, among plasma, high temperature coal tar combination oil refining device, it is very simple to possess the device, and the cost is low. Easy operation, high safety factor, high product yield, high product quality reaching the standard, freely controlled product processing direction and depth according to market demands and the like, and solves the problems in the background art.
In order to achieve the above object, the present invention provides the following technical solutions:
the utility model provides a novel, plasma medium and high temperature coal tar combination refining unit, includes the emulsification tank, the delivery outlet intercommunication of emulsification tank has the low-pressure oil pump, the delivery outlet intercommunication of low-pressure oil pump has ordinary pressure hydrocracking reactor, and is provided with nozzle I in junction ordinary pressure hydrocracking reactor inboard.
A fixed bed of refined catalyst is arranged in the upper part of the normal pressure hydrocracking reactor. The reactor comprises a reactor gas phase section I and a reactor liquid phase section I, wherein a gas phase direct current low-voltage electric heater is arranged in the normal pressure hydrocracking reactor gas phase section I, a liquid phase direct current low-voltage electric heater is arranged in the normal pressure hydrocracking reactor liquid phase section I, a gas heating furnace I is arranged below the normal pressure hydrocracking reactor, a blower I is communicated with the gas heating furnace I, a mixed gas outlet above the normal pressure hydrocracking reactor is communicated with a fractionation system, and a non-condensed mixed gas outlet above the fractionation system is communicated with a gas separator.
The heavy oil outlet at the lower part of the normal-pressure hydrocracking reactor is communicated with a pipeline mixer I, the input port of the pipeline mixer I is communicated with steam and recycle oil I, the output port of the pipeline mixer I is communicated with a high-temperature low-pressure oil pump, the output port of the high-temperature low-pressure oil pump I is communicated with a plasma pressure reduction reactor, and the inner side of the plasma pressure reduction reactor at the communication position is provided with an oil spray head II.
The plasma vacuum reactor is characterized in that a cracking catalyst fixed bed I is arranged in the upper portion of the plasma vacuum reactor, a gas phase section II is arranged in the middle of the plasma vacuum reactor, a liquid phase section II is arranged in the lower portion of the plasma vacuum reactor, a gas phase plasma generator power supply I is arranged in the gas phase section II of the plasma vacuum reactor, a liquid phase plasma generator power supply II is arranged in the liquid phase section II of the plasma vacuum reactor, a gas heating furnace II is arranged below the plasma vacuum reactor, a blower II is communicated on the gas heating furnace II, a mixed gas outlet above the plasma vacuum reactor is communicated with a fractionating system, and a non-condensed mixed gas outlet above the fractionating system is communicated with a gas separator.
The lower part of the plasma decompression reactor is provided with an unvaporized heavy oil outlet which is communicated with a pipeline mixer II, an input port of the pipeline mixer II is communicated with steam and recycle oil II, an output port of the pipeline mixer II is communicated with a high-temperature medium-pressure oil pump I and a high-pressure oil pump I, an output port of the medium-pressure oil pump I and the high-pressure oil pump I is communicated with a plasma medium-pressure reactor and a plasma high-pressure reactor, and an oil spray head III is arranged on the inner side of the plasma medium-pressure reactor and the high-pressure reactor at the communicated position.
A cracking catalyst fixed bed II is arranged in the upper part of the plasma middle and high pressure reactor, a gas phase section III is arranged in the middle part of the plasma middle and high pressure reactor, a liquid phase section III is arranged in the lower part of the plasma middle and high pressure reactor, a gas phase plasma generator power supply II is arranged in the gas phase section III of the plasma middle and high pressure reactor, a liquid phase plasma generator power supply II is arranged in the liquid phase section III of the plasma middle and high pressure reactor, a gas heating furnace III is arranged below the plasma middle and high pressure reactor, a blower III is communicated above the gas heating furnace III, a mixed gas outlet above the plasma middle and high pressure reactor is communicated with a fractionating system, an uncondensed mixed gas outlet above the fractionating system is communicated with a gas separator, and an unvaporized heavy oil outlet below the plasma middle and high pressure reactor, the heavy oil separator is communicated with a heavy oil separator, a heaviest heavy oil and impurities discharge port is arranged below the heavy oil separator, a very small amount of residual oil is discharged regularly and quantitatively for the whole device, a heavier heavy oil outlet is arranged in the middle of the heavy oil separator, the heavy oil separator is communicated with a high-temperature medium-pressure oil pump II and a high-pressure oil pump II, an output port of the medium-pressure oil pump II and an output port of the high-pressure oil pump II are communicated with a return pipeline mixer II through a return oil pipeline II, and the heavier heavy oil returned to the plasma medium-pressure reactor and the high-pressure reactor for continuous reaction is return oil II.
The upper part of the heavy oil separator is provided with a light heavy oil outlet which is communicated with a high-temperature medium-pressure oil pump and a high-pressure oil pump III, and the light heavy oil which enters the plasma pressure reduction reactor for continuous reaction is recycled oil I, wherein the output port of the high-temperature medium-pressure oil pump and the output port of the high-temperature high-pressure oil pump III are communicated with a return pipeline mixer I through a recycled oil pipeline I.
Preferably, a pressure table I is fixed above the atmospheric hydrocracking reactor, and a pressure table II is fixed above the plasma vacuum reactor. And a pressure gauge III is fixed above the plasma medium and high pressure reactor.
Preferably, a gas-phase thermocouple I is fixed on the right side of the gas-phase section I of the normal-pressure hydrocracking reactor, and a liquid-phase thermocouple I is fixed on the right side of the liquid-phase section I of the normal-pressure hydrocracking reactor.
Preferably, a gas-phase thermocouple II is fixed on the right side of the gas-phase section II of the plasma decompression reactor, and a liquid-phase thermocouple II is fixed on the right side of the liquid-phase section II of the plasma decompression reactor.
Preferably, a gas-phase thermocouple III is fixed on the right side surface of the gas-phase section III of the plasma medium and high-pressure reactor, and a liquid-phase thermocouple III is fixed on the right side of the liquid-phase section III of the plasma medium and high-pressure reactor.
Preferably, a maintenance vent I is fixed on the front side surface of the gas phase section I of the normal pressure hydrocracking reactor, and a maintenance inlet manhole I is fixed on the front side surface of the liquid phase section I of the normal pressure hydrocracking reactor.
Preferably, a maintenance exhaust hole II is fixed on the front side surface of the gas phase section II of the plasma pressure reduction reactor, and a maintenance inlet manhole II is fixed on the front side surface of the liquid phase section II of the plasma pressure reduction reactor.
Preferably, a maintenance exhaust hole III is fixed on the front side surface of the gas phase section III of the plasma medium and high pressure reactor, and a maintenance inlet manhole III is fixed on the front side surface of the liquid phase section III of the plasma medium and high pressure reactor.
A liquid level meter I13 is fixed on the right side surface of the preferred normal pressure hydrocracking reactor, a liquid level meter II 14 is fixed on the right side surface of the preferred plasma vacuum reactor, and a liquid level meter III 15 is fixed on the right side surface of the preferred plasma medium and high pressure reactor, so that the liquid levels of the plasma medium and high pressure reactors can be monitored in real time conveniently.
Compared with the prior art, the beneficial effects of the utility model are as follows:
a novel plasma medium-high temperature coal tar combined oil refining device is characterized in that crude oil is added with water, an activating agent or an emulsifying agent and a catalyst, the mixture is sprayed to a temperature higher than the gasification temperature of heavy oil fraction of product oil, the product oil is instantly and completely gasified into mixed gas in a normal-pressure hydrocracking reactor, the mixed gas continuously reacts through a refined catalyst fixed bed, and the mixed gas continuously flows into a fractionation system from a mixed gas outlet I to be fractionated.
The non-gasified heavy distillate oil is obtained by connecting a heavy oil outlet with a pipeline mixer I from the lower part of a normal pressure hydrocracking reactor, wherein an input port of the pipeline mixer I is communicated with steam and recycle oil I, after high-degree mixing is carried out in the pipeline mixer I, an output port of the pipeline mixer I is communicated with a high-temperature low-pressure oil pump, an output port of the high-temperature low-pressure oil pump is communicated with a plasma vacuum reactor, a reaction position of the communication position is provided with an oil spray head II, the oil spray head II supplies certain pressure to the oil spray head II through the high-temperature low-pressure oil pump, the oil spray head II sprays standard mixed liquid and steam into the plasma vacuum reactor, a plasma generator power supply I is arranged in the plasma vacuum reactor, and the generated plasma replaces the catalytic cracking action of a catalyst, and most of raw oil generates mixed gas after cracking reaction in various degrees under the high-temperature condition, then the reaction is continued through a cracking catalyst fixed bed, and a fractionating system is communicated with a mixed gas outlet II. The heavy distillate oil which is not gasified is communicated with a pipeline mixer II from a heavy oil outlet at the lower part of a plasma decompression reactor, the input port of the pipeline mixer II is communicated with steam and recycle oil II, after high mixing is carried out in the pipeline mixer II, the output port of the pipeline mixer II is communicated with a high-temperature medium-pressure oil pump and a high-pressure oil pump, the output port of the high-temperature medium-pressure oil pump and the high-pressure oil pump are communicated with a plasma medium-pressure reactor and a high-pressure reactor, the inner side of the plasma medium-pressure reactor and the high-pressure reactor at the communicated position is provided with an oil spray head III, the medium-pressure oil pump and the high-pressure oil pump I supply certain pressure to the oil spray the mixed liquid and the steam into the plasma medium-pressure reactor by the oil spray head III, and after cracking and polymerization reactions of various degrees of most raw oil are carried out under the action of high-temperature, medium-pressure and high-pressure conditions by a plasma generator power supply in the medium-pressure reactor instead of a catalyst, and the generated mixed gas continuously reacts through a cracking catalyst fixed bed II, continuously reacts and flows into a fractionation system from a mixed gas outlet III, and an uncondensed mixed gas outlet above the fractionation system is communicated with a gas separator. The front part of the fractionating system is small and simple, and the fractionating system has no liquid part flowing in, so that the great burden is reduced, the whole device is very simple, the operation is easy, Monel alloy steel is not used for manufacturing, the manufacturing cost is very low, the safety coefficient is high, the product yield is high, and the product processing direction and the processing depth can be freely controlled according to market demands.
Description of the drawings:
FIG. 1: the utility model discloses, whole structure picture.
FIG. 2: the utility model relates to a normal-pressure hydrocracking reactor.
FIG. 3: the utility model discloses, plasma decompression reactor.
FIG. 4: the utility model discloses, plasma medium and high pressure reactor.
Fig. 1 to 4: 1. an emulsifying tank. 2. A low pressure oil pump. 3. An atmospheric hydrocracking reactor. 4. Oil spout head I. 5. Pipeline mixer I. 6. A high-temperature low-pressure oil pump. 7. Plasma pressure reduction reactor. 8. And an oil spray head II. 9. And a pipeline mixer II. 10. High-temperature medium-pressure and high-pressure oil pumps I. 11. Plasma medium and high pressure reactor. 12. And an oil spray head III. 13. And a liquid level table I. 14. And a liquid level table II. 15. And a liquid level meter III. 16. Pressure gauge I. 17. And a pressure gauge II. 18. And a pressure gauge III. 19. A fractionation system. 20. A gas separator. 21. A heavy oil separator. 22. High-temperature medium-pressure oil pump III. 23. And a high-temperature medium-pressure oil pump II. 24. And a recycle oil pipeline I. 25. And a recycle oil pipeline II. 31. A fixed bed of the refined catalyst. 32. And a gas phase section I. 33. And a liquid phase section I. 34. Gas phase direct current low voltage electric heater. 35. Liquid phase direct current low voltage electric heater. 36. Gas heating furnace I. 37. And a blower I. 38. And a gas-phase thermocouple I. 39. And a liquid phase thermocouple I. 321. And maintaining the exhaust hole I. 331. And (5) repairing the manhole I. 71. Cracking catalyst fixed bed I. 72. And a gas phase section II. 73. And a liquid phase section II. 74. And a gas phase plasma generator power supply I. 75. And a liquid phase plasma generator power supply I. 76. And a gas heating furnace II. 77. And a blower II. 78. And a gas phase thermocouple II. 79. And a liquid phase thermocouple II. 721. And maintaining the exhaust hole II. 731. And (5) repairing the manhole II. 111. And a cracking catalyst fixed bed II. 112. And a gas phase section III. 113. And a liquid phase section III. 114. And a gas phase section III plasma generator power supply II. 115. And a liquid phase section III plasma generator power supply II. 116. And (3) a gas heating furnace III. 117. And a blower III. 118. And a gas phase thermocouple III. 119. And a liquid phase thermocouple III. 1121. And maintaining the exhaust hole III. 1131. And (5) repairing the manhole III.
The specific implementation mode is as follows:
the technical solution in the embodiment of the present invention will be described clearly and completely with reference to the drawings in the embodiment of the present invention, and obviously, the described embodiment is only a part of the embodiments of the present invention, rather than all embodiments, based on the embodiments of the present invention, all other embodiments obtained by a person skilled in the art without creative labor fall into the protection scope of the present invention.
Referring to fig. 1 to 4, the present invention provides a technical solution:
a novel plasma medium and high temperature coal tar combined oil refining device comprises an emulsification tank 1. Raw oil is added with water and an activator or an emulsifier and a catalyst, and is highly mixed and emulsified into standard emulsified liquid through an emulsifying tank 1, and an output port of the emulsifying tank I is communicated with a low-pressure oil pump 2. The output port of the low-pressure oil pump 2 is communicated with the normal-pressure hydrocracking reactor 3. And the inner side of the normal pressure hydrocracking reactor 3 at the communication position is provided with an oil spray head I4, and the oil spray head I4 sprays standard atomized emulsion liquid into the normal pressure hydrocracking reactor 3 by the pressure of a low pressure oil pump.
The front side of the middle gas phase section I32 of the normal-pressure hydrocracking reactor 3 is fixedly provided with a maintenance vent I321, and the front side of the lower liquid phase section I33 of the normal-pressure hydrocracking reactor 3 is fixedly provided with a maintenance inlet manhole I331, so that later maintenance and repair are facilitated.
A pressure gauge I16 is fixed above the normal pressure hydrocracking reactor 3, which is convenient for monitoring the pressure of the normal pressure hydrocracking reactor 3, a refined catalyst fixed bed 31 is arranged in the upper part of the normal pressure hydrocracking reactor 3, the refining and partial cracking and cracking reactions are performed through the mixed gas of the refined catalyst fixed bed 31, the middle part of the normal pressure hydrocracking reactor 3 is a gas phase section I32, the lower part of the normal pressure hydrocracking reactor 3 is a liquid phase section I33, a gas phase direct current low voltage electric heater 34 is arranged in the gas phase section I32 of the normal pressure hydrocracking reactor 3, a liquid phase direct current low voltage electric heater 35 is arranged in the liquid phase section I33 of the normal pressure hydrocracking reactor 3, as long as the direct current low voltage electric heater is skillfully designed, a certain magnetic field range and direction can be generated, certain influence can be generated on the raw oil liquid and gas, and a good heat transfer synergistic effect is achieved, a gas-phase thermocouple I38 is fixed in the right side of the gas-phase section I32 of the normal-pressure hydrocracking reactor 3, and a liquid-phase thermocouple I39 is fixed in the right side of the liquid-phase section I33 of the normal-pressure hydrocracking reactor 3, so that the gas-phase and liquid-phase temperatures of the normal-pressure hydrocracking reactor 3 can be monitored in real time conveniently.
A gas heating furnace I36 is arranged below the normal pressure hydrocracking reactor 3, a blower I37 is communicated with the gas heating furnace I36, a mixed gas outlet at the upper part of the normal pressure hydrocracking reactor 3 is communicated with a fractionating system 19, when the gas heating furnace I36 heats the gas and the liquid phases of the normal pressure hydrocracking reactor 3 to a certain temperature, part of the light distillate oil is gasified and flows into the fractionating system 19, when the air does not exist in the normal pressure hydrocracking reactor 3, a gas phase direct current low voltage electric heater 34 and a liquid phase direct current low voltage electric heater 35 are used for adjusting the gas and liquid phase temperature of the normal pressure hydrocracking reactor 3, according to the gasification temperature of the highest distillate oil of the product oil, the gas phase temperature is increased by 5-10 ℃, at the moment, the standard emulsified liquid sprayed by a spray head I4 is instantly and completely gasified into mixed gas, and the gasification is accompanied with cracking and polymerization reactions, at this time, the molecules of the mixed gas are fully contacted and cracked, cracked and polymerized in the normal pressure hydrocracking reactor 3. The continuous reaction is carried out by the micro pressure generated by the normal pressure hydrocracking reactor 3, the reaction is carried out again through the refined catalyst fixed bed 31, the reaction is carried out continuously and flows into the fractionating system 19 from the mixed gas outlet I to produce the required product oil and gas, a gas separator is arranged above the fractionating system 19 to separate out trace hydrogen, a small amount of ozone tail gas and a large amount of byproduct refinery gas, the liquid heavy oil is communicated with the pipeline mixer I5 from the liquid heavy oil outlet at the lower part of the normal pressure hydrocracking reactor 3, the input port of the pipeline mixer I5 is communicated with water vapor and recycle oil I, after high mixing in the pipeline mixer I5, the output port of the pipeline mixer I5 is communicated with the high temperature and low pressure oil pump 6, the output port of the high temperature and low pressure oil pump 6 is communicated with the plasma vacuum reactor 7, and the inner side of the plasma vacuum reactor 7 at the communication position is provided with an oil spray head II, and the oil spray head II 8 sprays the mixed liquid and the steam into the plasma decompression reactor 7 by the pressure of the high-temperature low-pressure oil pump 6. A pressure gauge II 17 is fixed above the plasma decompression reactor 7 to facilitate real-time monitoring of the pressure of the plasma decompression reactor 7, a cracking catalyst fixed bed I71 is arranged in the upper portion of the plasma decompression reactor 7, a gas phase section II 72 is arranged in the middle of the plasma decompression reactor 7, a liquid phase section II 73 of the plasma decompression reactor 7 is arranged in the middle of the plasma decompression reactor 7, a gas phase plasma generator power supply I74 is arranged in the gas phase section II 72 of the plasma decompression reactor 7, a liquid phase plasma generator power supply I75 is arranged in the liquid phase section II 73 of the plasma decompression reactor 7, a gas phase thermocouple II 78 is fixed in the right side of the gas phase section II 72 of the plasma decompression reactor 7, a liquid phase thermocouple II 79 is fixed in the right side of the liquid phase section II 73, and therefore real-time monitoring of the temperature of the plasma decompression reactor 7 is facilitated.
The right side surface of the normal pressure hydrocracking reactor 3 is fixed with a liquid level indicator I13, the right side surface of the plasma vacuum reactor 7 is fixed with a liquid level indicator II 14, and the right side surface of the plasma middle and high pressure reactor 11 is fixed with a liquid level indicator III 15.
A gas heating furnace II 76 is arranged below the plasma decompression reactor 7, a blower II 77 is communicated with the gas heating furnace II 76, a mixed gas outlet above the plasma decompression reactor 7 is communicated with a fractionating system 19, a gas separator 20 is arranged above the fractionating system 19, and hydrogen with a small quantity, a small quantity of ozone tail gas and a large quantity of byproduct refinery gas are fractionated.
A maintenance exhaust hole II 721 is fixed on the front side surface of the middle gas phase section II 72 of the plasma pressure reduction reactor 7, and a maintenance inlet manhole II 731 is fixed on the front side surface of the lower liquid phase section II 73 of the plasma pressure reduction reactor 7, so that later maintenance and repair are facilitated.
When the gas-liquid phase temperature of the plasma decompression reactor 7 is heated to a certain temperature by the gas heating furnace II 76, the mixed liquid and the water vapor which are mixed by the oil sprayer II 8 are sprayed and comprise raw oil prestored in the liquid phase section of the plasma decompression reactor 7, so that part of light distillate oil is gasified and flows into the fractionating system 19, and when air is not stored in the plasma decompression reactor 7, the gas-liquid phase temperature of the plasma decompression reactor 7 is adjusted by using the power supplies I74 and I75 of the gas-liquid phase plasma generator. According to the gasification temperature of the highest fraction oil of the product oil, the gas phase temperature is increased by 10-15 ℃, at the moment, the standard mixed liquid and the steam sprayed by the oil spray head II 8 are completely gasified instantly, and sufficient plasma is generated in a power supply of a plasma generator, so that the heat transfer and heat coordination effects are good. [ Shanghai China east Arganister university's old professor Zhouxiamnu: (the plasma is classified into high-temperature plasma and medium-low temperature plasma according to temperature, the high-temperature plasma technology is generally used for nuclear fusion and laser devices; the medium-low temperature plasma front-edge technology is being used for coal gasification and petroleum heavy oil catalytic modification, in the chemical industry, a series of chemical reactions can be realized by using the plasma. for example, CN108998080A, a discharge plasma heavy oil hydrogenation multistage treatment device and process of the institute of Electrical engineering, China petrochemical industry, Inc., 2019-08-16CN110124471A, a high-flux low-temperature plasma system for decomposing hydrogen sulfide and a method for decomposing hydrogen sulfide of the Qingdao safety engineering institute of China petrochemical industry, etc., the reduced pressure distillation process is a mature process in the chemical industry, such as petrochemical industry, coal industry, etc.) (note: the second plasma reaction generator therein is provided by the domestic famous low-temperature plasma research center, Nanjing Suman plasma technology, etc.). Gas phase plasma generation methods include gas discharge (direct current discharge, low frequency discharge, high frequency discharge, microwave discharge, inductive discharge), thermal ionization (combustion), photoionization (laser, ultraviolet), and ray ionization (isotope, X-ray, accelerator), and have been expanded to many research fields. The liquid phase plasma is generated by the above-mentioned gas phase plasma generation methods selectively in the liquid phase (water phase), and a "liquid electric effect" is generated, which can instantaneously form a plasma channel in the liquid phase (refer to the article of grandson ice et al: the generation method and formation mechanism of microwave liquid phase discharge plasma). Note: the technical parameters of the reverse phase section and the liquid phase section of the medium-low temperature plasma reactor are provided by the famous low-temperature plasma research center in China and the assistance of Nanjing Suman plasma technology Co., Ltd.) (when professor carries out regular experiments, the power and various data of the plasma generator can be made according to the size, the processing direction and the depth of the experimental reactor), and the following are laboratory small experimental data:
intermediate temperature, electron temperature Te＝104～106K
Ion temperature Ti＝3X103～3X104K (for example arc plasma)
Low temperature Te＞104K、TiRoom temperature (e.g. glow discharge plasma)
The electrical parameters of the plasma of the invention controlled by a computer are as follows: a radio frequency power supply: 13.56MHZ, plasma power of 0-1000W, discharge pressure of 0.1-50Pa, plasma volume of 5L-10L, gas flow control of 1-80sccm, and generated plasma gas which is one or more of hydrogen, oxygen and nitrogen; the single pass of the treatment process is 10s, and the process is continuous. For thermally balanced plasma (high temperature plasma), temperature is an average measure of the thermal motion of various particles; for non-thermal equilibrium plasma (low temperature plasma), the electron and ion temperatures are different, and T is generally usediDenotes the ion temperature, TeIndicating the electron temperature. (Note: technical parameters of the reverse phase section and the liquid phase section of the medium-low temperature plasma reactor, and the new process relates to parameters of energy conservation, momentum conservation and mass conservation, which are provided by the famous low-temperature plasma research center in China and Suman plasma technology Co., Ltd., Nanjing). The function of a cracking catalyst is replaced, at the moment, all molecules of mixed gas in the plasma reduced pressure reactor 7 are fully contacted, cracking and polymerization reaction are continuously carried out, the mixed gas passes through the cracking catalyst fixed bed 71 to continuously react under a certain pressure generated by the plasma reduced pressure reactor 7, the mixed gas flows into the fractionating system 19 from a mixed gas outlet, the required product oil, gas oil, kerosene, diesel oil, heavy oil or naphthalene oil is fractionated, the upper part of the fractionating system is communicated with the gas separator 20, and a small amount of hydrogen, a small amount of ozone tail gas and a large amount of byproduct refinery gas are separated. (adapted according to the reactorThe size of the mixed gas outlet is adjusted by pressure, the pressure of the reactor is controlled below 0.02-0.1 generally in laboratory experiments, after the institute (college) is established, the pressure generated by the reactor can be increased according to the production requirement in the formal experiments of the university students), the non-gasified heavy distillate oil liquid at the lower part of the plasma decompression reactor 7 is communicated with a pipeline mixer II 9 through an outlet, the input port of the pipeline mixer II 9 is communicated with water vapor and recycle oil II, after high mixing in the pipeline mixer, the output port of the pipeline mixer II 9 is communicated with a high-temperature medium and high-pressure oil pump 10, the output port of the high-temperature medium and high-pressure oil pump 10 is communicated with a plasma medium and high-pressure reactor 11, an oil spray head III 12 is arranged in the plasma at the connection part and inside the high-pressure reactor 11, the oil spray head III 12 is close to the pressure of the high-temperature medium and high-pressure oil pump I10, spraying highly mixed liquid and vapor into a plasma high-pressure reactor 11, wherein a pressure gauge III 18 is fixed above the plasma high-pressure reactor 11 to facilitate real-time detection of the pressure in the plasma high-pressure reactor 11, a cracking catalyst fixed bed II 111 is arranged in the upper part of the plasma high-pressure reactor 11, a gas phase section III 112 is arranged in the middle part of the plasma high-pressure reactor 11, a liquid phase section III 113 is arranged in the lower part of the plasma high-pressure reactor 11, a gas phase section plasma generator power supply II 114 is arranged in the gas phase section III 112 of the plasma high-pressure reactor 11, a liquid phase section plasma generator power supply II 115 is arranged in the liquid phase section III 113 of the plasma high-pressure reactor 11, a gas phase thermocouple III 118 is fixed on the right side of the gas phase section III 112 of the plasma high-pressure reactor 11, and a gas phase thermocouple III 118 is fixed in the plasma, And a liquid-phase thermocouple III 119 is fixed on the right side of the liquid-phase section III 113 of the high-pressure reactor 11, so that the gas-phase and liquid-phase temperatures of the plasma and the high-pressure reactor 11 can be monitored in real time.
A gas heating furnace III 116 is arranged below the plasma medium and high pressure reactor 11, a blower III 117 is communicated above the gas heating furnace III 116, a mixed gas outlet above the plasma medium and high pressure reactor 11 is communicated with a fractionating system 19, a mixed gas outlet which is not condensed above the fractionating system is communicated with a gas separator 20, and a small amount of hydrogen, a small amount of ozone tail gas and a large amount of byproduct oil refinery gas are separated.
A maintenance exhaust hole III 1121 is fixed on the front side surface of the middle gas phase section III 112 of the plasma medium and high pressure reactor 11, and a maintenance inlet manhole III 1131 is fixed on the front side surface of the lower liquid phase section III 113, so that later maintenance and repair are facilitated.
When the gas heating furnace III 116 heats the gas phase and liquid phase temperature of the plasma middle and high pressure reactor 11 to a certain temperature, the oil spray head III 12 starts to spray mixed liquid and vapor to the plasma middle and high pressure reactor 11, including raw oil pre-stored in the plasma middle and high pressure reactor 11, to gasify part of the light fraction oil, and then flows into the fractionating system 19, when air is not present in the plasma middle and high pressure reactor 11, the gas phase and liquid phase plasma generator power sources III 114 and III 115 are used to adjust the gas phase and liquid phase temperature of the plasma middle and high pressure reactor 11, according to the highest fraction oil gasification temperature of the product oil, the gas phase temperature is increased by 10-15 ℃, at this time, the standard mixed liquid sprayed by the oil spray head III 12 instantly gasifies all the product oil distillate, the gas phase section and liquid phase section plasma generator power sources III and III 115 of the plasma middle and high pressure reactor 11 in the plasma, sufficient plasma is generated, [ schanpinny old professor, shanghai east university of eastern science: [ (the main advantages of the plasma power supply used in this patent are that it can crack petroleum heavy oil/coal tar fast to remove organic sulfur and heavy metal in oil gas, the highest efficiency can reach 99%, the technical parameters of "plasma power supply of Chengdu-jin founding science and technology limited company" purchased in energy utilization can be inquired, and it is the purchasing part in the patent, and it is not necessary to explain the distribution of plasma power supply cracking in detail, and at the same time, it makes the utility model's operation more reliable ' < it is not possible for any factory or research unit to research plasma power supply ' < ' > it can replace catalyst to crack petroleum heavy oil/coal tar fast ' ] (in the research and development experiment of the university, a zeolite catalyst is arranged in the plasma, the lower part of the gas phase section of the high pressure reactor 11, and the upper part of the liquid phase section, that is in the plasma, and in the plasma area of the high pressure reactor 11), in the research of treating thick oil by Zhao Ming of China Petroleum university (mainly due to oxidation reaction, argon plasma generates gas after treating thick oil, and the gas generates product components including hydrogen, low molecular alkane and a small amount of thin hydrocarbon). (in the dielectric barrier discharge plasma, in the high pressure reactor 11, introducing zeolite catalyst, on methane and carbon dioxide conversion to prepare higher hydrocarbon research, in the product detected in the alkane, dilute hydrocarbon, oxide and synthesis gas, product distribution conditions by input power, gas flow, material ratio, pressure and catalyst type, plasma area introduction of zeolite catalyst, methane and carbon dioxide conversion rate decreased, but hydrocarbon product selectivity increased, carbon formation also inhibited). (under the action of the pulse corona plasma, the catalyst activity is very different, and has certain regulating effect on the distribution of products, the hydrocarbon yield of the Y row-one catalyst is improved by nearly times compared with that of a blank carrier, the hydrocarbon selectivity is improved by more than times, and the energy efficiency can be improved by more than times by combining the catalyst with the pulse corona plasma). (researches show that after a row of catalyst is introduced into the pulsed corona discharge plasma, the yield of hydrocarbon preparation from mixed gas is greatly improved, the synergistic effect of the catalyst and the plasma obviously improves the yield of ethylene, the product distribution is changed, and the zeolite catalyst and the plasma have the optimal plasma-catalysis synergistic effect). (an important research direction of the plasma is application in the field of catalysts, and the plasma is used as an emerging technical means and is more and more closely related to the field of catalysts). The function of the cracking catalyst is replaced, at the moment, the molecules of the mixed gas in the plasma and in the high-pressure reactor 11 are fully contacted, cracking reaction and polymerization reaction are generated, the mixed gas passes through the cracking catalyst fixed bed II 111 to continue the reaction by the pressure generated by the plasma and in the high-pressure reactor 11, the reaction is continued, and a fractionating system 19 is communicated with a mixed gas outlet III. Wherein, the pressure is supplied by the high pressure oil pump in the oil spraying head support, the oil spraying to the plasma medium and high pressure reactor 11 is the third oil refining method and the innovation key point of the device, the gas phase temperature of the plasma medium and high pressure reactor 11 exceeds the gasification temperature (boiling point) of the highest fraction of the heavy product oil, the product oil is instantly and completely gasified into mixed gas (this is also the key point of the third oil refining method and the new condition of the chemical reaction of the device, and each molecule of the product oil is sprayed into the reactor from the normal temperature condition, the temperature of the normal pressure hydrocracking reactor is controlled below 365 ℃ instantly when the normal experiment is carried out by the university research, the temperature of the plasma vacuum reactor is controlled below 540 ℃, the temperature of the high temperature reactor in the plasma is controlled below 390 ℃, and the pressure is controlled below 13.4-18.1 mpa), under the condition of temperature fusion, the power supply of the plasma generator generates enough plasma, the plasma generator becomes an important new condition for cracking reaction under the condition of good heat transfer and synergistic heating action and under the action of replacing a catalyst, all molecules of product oil are instantly and completely gasified, the violent expansion coefficient is 3160 times (calculated by the company) under the conditions of instant gasification and instant sudden change of temperature, and all molecules can be cracked, cracked and polymerized under the conditions of mutual extrusion and collision of all molecules and high temperature and under the action of replacing the cracking catalyst by the plasma generated by the plasma reaction. Mainly, the steam also has cracking reaction, so that dehydrogenation reaction of water molecule cracking is carried out, the produced hydrogen atoms and a small amount of hydrogen atoms of oil molecules are thermal hydrogen, hydrofining and hydrocracking reaction are carried out under the hydrogen-contacting condition, most of the thermal hydrogen and unsaturated oil molecules, olefin molecules and molecular fragments (according to the principle that like-polarity repulsion and opposite-polarity attraction of chemical reaction are adopted, the valence of the thermal hydrogen (hydrogen atom) -1 carbon atom valence of the oil molecules + 4) have chemical reaction and polymerization reaction, and saturated alkane molecules and a small amount of diluted hydrocarbon molecules are generated.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (9)
1. A novel plasma medium-high temperature coal tar combined oil refining device comprises an emulsification tank (1), and is characterized in that an output port of the emulsification tank (1) is communicated with a low-pressure oil pump (2), and an output port of the low-pressure oil pump (2) is communicated with a normal-pressure hydrocracking reactor (3) and is positioned at the communication position; an oil spray head I (4) is arranged on the inner side of the normal-pressure hydrocracking reactor (3);
a refined catalyst fixed bed (31) is arranged in the upper part of the normal pressure hydrocracking reactor (3), the middle part of the normal pressure hydrocracking reactor is a gas phase section I (32), the lower part of the normal pressure hydrocracking reactor is a liquid phase section I (33), a gas phase direct current low-voltage electric heater (34) is arranged in the gas phase section I (32) of the normal pressure hydrocracking reactor, a liquid phase direct current low-voltage electric heater (35) is arranged in the liquid phase section I (33) of the reactor, a gas heating furnace I (36) is arranged below the normal pressure hydrocracking reactor (3), a blower I (37) is communicated with the gas heating furnace I (36), and a mixed gas outlet above the normal pressure hydrocracking reactor (3) is communicated with a fractionation system (19); the outlet of the uncondensed mixed gas above the fractionation system (19) is communicated with a gas separator (20);
a liquid heavy oil outlet below the normal-pressure hydrocracking reactor (3) is communicated with a pipeline mixer I (5), an input port of the pipeline mixer I (5) is communicated with steam, an output port of the pipeline mixer I (5) is communicated with a high-temperature low-pressure oil pump I (6), an output port of the high-temperature low-pressure oil pump I (6) is communicated with a plasma reduced pressure reactor (7), and an oil spray head II (8) is arranged on the inner side of the plasma reduced pressure reactor (7) at the communicated position;
a cracking catalyst fixed bed I (71) is arranged in the upper part of the plasma reduced-pressure reactor (7), a gas phase section II (72) is arranged in the middle of the plasma reduced-pressure reactor (7), a liquid phase section II (73) is arranged in the lower part of the plasma reduced-pressure reactor (7), a gas phase plasma generator power supply I (74) is arranged in the gas phase section II (72) of the plasma reduced-pressure reactor (7), a liquid phase plasma generator power supply I (75) is arranged in the liquid phase section II (73) of the plasma reduced-pressure reactor (7), a gas heating furnace II (76) is arranged below the plasma reduced-pressure reactor (7), a blower II (77) is communicated with the gas heating furnace II (76), and a mixed gas outlet above the plasma reduced-pressure reactor (7) is communicated with a fractionation system (19); the outlet of the uncondensed mixed gas on the fractionation system is communicated with a gas separator (20);
the heavy oil outlet at the lower part of the plasma decompression reactor (7) is communicated with a pipeline mixer II (9), the input port of the pipeline mixer II (9) is communicated with steam and recycled oil, the output port of the pipeline mixer II (9) is communicated with a high-temperature medium-pressure oil pump I (10), the output port of the high-temperature medium-pressure oil pump I (10) is communicated with a plasma medium-pressure high-pressure reactor (11), a cracking catalyst fixed bed II (111) is arranged above the plasma medium-pressure high-pressure reactor (11), the middle part of the plasma medium-pressure high-pressure reactor (11) is a gas phase section III (112), the lower part of the plasma medium-pressure high-pressure reactor (11) is a liquid phase section III (113), a gas phase section plasma generator power supply II (114) is arranged in the middle part of the plasma medium-pressure high-pressure reactor (11) and in the liquid phase section III (113), and a liquid phase section plasma generator power supply II (115) is arranged in the liquid phase section III (113) of the plasma medium-pressure high-pressure reactor (11) ) A mixed gas outlet at the upper part of the plasma medium and high pressure reactor (11) is communicated with a fractionation system (19); the outlet of the uncondensed mixed gas above the fractionation system is communicated with a gas separator (20);
an unvaporized heavy oil outlet arranged below the plasma medium and high pressure reactor (11) is communicated with a heavy oil separator (21), the heaviest heavy oil product and impurities such as organic impurities are arranged below the separator (21), and part of oil products discharged in fixed time and quantity are extremely small amount of residual oil generated by the whole device; a lighter heavy oil outlet is arranged above the heavy oil separator and is communicated with a high-temperature medium-pressure oil pump and a high-pressure oil pump III, the output ports of the high-temperature medium-pressure oil pump and the high-pressure oil pump III are communicated with a return pipeline mixer I (5) through a return oil pipeline I, and the return oil is returned to a plasma pressure reduction reactor (7) to continue to react into return oil I; the heavy oil separator is characterized in that a heavy oil product outlet is formed in the middle of the heavy oil separator and communicated with a high-temperature medium-pressure oil pump and a high-pressure oil pump II, and the heavy oil outlet of the high-temperature medium-pressure oil pump and the high-pressure oil pump II is communicated with a return pipeline mixer II (9) through a return oil pipeline II to enter a plasma medium-pressure and high-pressure reactor (11) to continue to react to form return oil II.
2. The novel plasma medium-high temperature coal tar combined oil refining device according to claim 1, wherein a pressure gauge I (16) is fixed above the atmospheric hydrocracking reactor (3), a pressure gauge II (17) is fixed above the plasma vacuum reactor (7), and a pressure gauge III (18) is fixed above the plasma medium-high temperature reactor (11).
3. The novel plasma medium-high temperature coal tar combined oil refining device according to claim 1, wherein a gas phase thermocouple i (38) is fixed on the right side surface of the gas phase section i (32) of the atmospheric hydrocracking reactor (3), and a liquid phase thermocouple i (39) is fixed on the right side surface of the liquid phase section i (33) of the atmospheric hydrocracking reactor (3).
4. The novel plasma medium-temperature and high-temperature coal tar combined oil refining device according to claim 1, wherein a gas-phase thermocouple II (78) is fixed on the right side surface of the gas-phase section II (72) of the plasma pressure reduction reactor (7), and a liquid-phase thermocouple II (79) is fixed on the right side surface of the liquid-phase section II (73) of the plasma pressure reduction reactor (7).
5. The novel, medium-and high-temperature coal tar combination refining unit according to claim 1, characterized in that a gas-phase thermocouple iii (118) is fixed on the right side surface of the gas-phase section iii (112) of the medium-and high-pressure plasma reactor (11), and a liquid-phase thermocouple iii (119) is fixed on the right side surface of the liquid-phase section iii (113) of the medium-and high-pressure plasma reactor (11).
6. The novel plasma medium-high temperature coal tar combined oil refining device according to claim 1, wherein a maintenance vent hole I (321) is fixed on the front side surface of the gas phase section I (32) of the atmospheric hydrocracking reactor (3), and a maintenance inlet manhole I (331) is fixed on the front side surface of the liquid phase section I (33) of the atmospheric hydrocracking reactor (3).
7. A novel, medium-and high-temperature coal tar combination oil refining plant as claimed in claim 1, characterized in that the front side of the gas phase section II (72) of the plasma pressure reduction reactor (7) is fixed with a maintenance vent hole II (721), and the front side of the liquid phase section II (73) of the plasma pressure reduction reactor (7) is fixed with a maintenance manhole II (731).
8. The novel plasma medium-high temperature coal tar combination oil refining device according to claim 1, wherein a maintenance exhaust hole III (1121) is fixed on the front side surface of the gas phase section III (112) of the plasma medium-high pressure reactor (11), and a maintenance inlet manhole III (1131) is fixed on the front side surface of the liquid phase section III (113) of the plasma medium-high pressure reactor.
9. The novel plasma medium-high temperature coal tar combined oil refining device according to claim 1, wherein a liquid level gauge I (13) is fixed on the right side surface of the atmospheric hydrocracking reactor (3), a liquid level gauge II (14) is fixed on the right side surface of the plasma reduced pressure reactor (7), and a liquid level gauge III (15) is fixed on the right side surface of the plasma medium-high pressure reactor (11).
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