CN217854601U - Device for producing high-purity alkane by refining LPG through multi-tower coupling rectification - Google Patents
Device for producing high-purity alkane by refining LPG through multi-tower coupling rectification Download PDFInfo
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Abstract
The utility model provides a device for producing high-purity alkane by refining LPG through multi-tower coupling rectification, which belongs to the technical field of petrochemical industry, and comprises a mixed hydrocarbon storage tank for containing raw materials and propane preparation equipment, wherein the propane preparation equipment is connected with the mixed hydrocarbon storage tank and is used for preparing propane; the isobutane preparing equipment is connected with the output end of the propane preparing equipment and is used for preparing isobutane; the normal butane preparation equipment is connected with the isobutane preparation equipment and is used for preparing normal butane; and the refrigerating equipment is connected with the propane preparation equipment, the isobutane preparation equipment and the n-butane preparation equipment and is used for providing a cold source. The utility model separates the effective components in LPG raw material step by step through multi-tower coupling rectification to obtain various high-purity alkane products, and has simple and smooth process, high extraction rate, high product purity and stable operation; the whole physical production process is adopted, no new impurity is introduced, no pollution is caused, and the process safety coefficient is high.
Description
Technical Field
The utility model relates to a petrochemical technical field, concretely relates to adopt refined LPG of multitower coupling rectification to produce device of high-purity alkane.
Background
Liquefied Petroleum Gas (LPG) has main components of propane and butane and a small amount of olefin. LPG is stored in a storage tank in a liquid state under a suitable pressure and is often used as a cooking fuel, i.e. liquefied gas which we often use. LPG has been used as a fuel for light vehicles for many years and it can also be stored in tanks to fuel automobiles. The high-purity alkane is widely used as standard gas, correction gas, on-line instrument standard gas and prepared special mixed gas in the fields of industrial departments such as chemical industry, metallurgy, electronics, petroleum and the like, basic research, atmospheric pollution monitoring, aviation, atomic energy and the like, and has very high market value. The preparation of high-purity alkane usually adopts rectification separation, and the aim of separating mixed components is achieved through multiple condensation and evaporation processes according to different boiling points of substances. At present, a heat source of a reboiler of a rectification tower of petrochemical products generally adopts steam for heating to 80 ℃, circulating water is adopted for cooling to about 45 ℃ at the top of the rectification tower, and the tower pressure needs to be controlled to about 2.0MPa due to higher tower temperature. The relative separation degree of each component is greatly reduced under higher pressure, high-purity products are difficult to extract, the temperature of a tower kettle is high, steam heating is needed, fuel is additionally consumed to produce steam, and the production cost is increased. In addition, higher operating pressures also increase safety risks.
In order to overcome the defects, the device for producing high-purity alkane by refining LPG is safe, low in energy consumption, stable in production and easy to operate.
SUMMERY OF THE UTILITY MODEL
In view of this, the utility model provides an adopt refined LPG of multi-tower coupling rectification to produce high-purity alkane's device, simple structure, flow reasonable in design, easy and simple to handle, product yield height, energy saving and consumption reduction.
In order to achieve the technical effect, the utility model provides an adopt refined LPG of multicolumn coupling rectification to produce device of high-purity alkane adopts following technical scheme:
the device for producing high-purity alkane by refining LPG through multi-tower coupling rectification comprises a mixed hydrocarbon storage tank for containing raw materials, and is characterized by further comprising:
a propane production facility connected to the mixed hydrocarbon storage tank and configured to produce propane;
the isobutane preparation equipment is connected with the output end of the propane preparation equipment and is used for preparing isobutane;
the n-butane preparation equipment is connected with the isobutane preparation equipment and is used for preparing n-butane;
and the refrigerating equipment is connected with the propane preparation equipment, the isobutane preparation equipment and the normal butane preparation equipment and is used for providing a cold source.
Further, the propane preparation equipment comprises a deethanizer connected with the mixed hydrocarbon storage tank through a pipeline, a propane tower connected with a liquid outlet at the bottom of the deethanizer through a pipeline, a first gas-liquid separation mechanism connected with the top of the deethanizer through a pipeline and used for cooling the top steam of the deethanizer and performing gas-liquid separation, and a second gas-liquid separation mechanism connected with the top of the propane tower and used for cooling the top steam of the propane tower and performing gas-liquid separation;
reflux liquid separated by the vapor at the top of the deethanizer through the first gas-liquid separation mechanism flows back into the deethanizer, and reflux liquid separated by the vapor at the top of the propane tower through the second gas-liquid separation mechanism flows back into the propane tower;
the liquid taking port of the propane tower is connected with a propane intermediate storage tank through a pipeline, and the liquid outlet of the propane intermediate storage tank is connected with the propane storage tank through a 2# shielding pump.
Further, the first gas-liquid separation mechanism comprises a No. 1 top condenser connected with the top of the deethanizer through a pipeline, and a No. 1 separator connected with a liquid outlet of the No. 1 top condenser through a pipeline, wherein the liquid outlet of the No. 1 separator is connected with a reflux port of the deethanizer through a pipeline, gas discharged from the top of the deethanizer is liquefied by the No. 1 top condenser and then enters the No. 1 separator for gas-liquid separation, a liquid phase as reflux liquid enters the reflux port at the top of the deethanizer, and a gas phase is sent to a tail gas main pipe;
the second gas-liquid separation mechanism comprises a 2# top condenser connected with the top of the propane tower through a pipeline, and a 2# separator connected with a liquid discharge port of the 2# top condenser through a pipeline, wherein the liquid discharge port of the 2# top condenser is connected with a reflux port of the propane tower through a pipeline, and after the gas discharged from the top of the propane tower is liquefied through the 2# top condenser, a liquid phase enters the reflux port at the top of the propane tower as reflux liquid.
Further, the isobutane preparing equipment comprises a depropanizing tower connected with the propane preparing equipment through a pipeline, an isobutane tower connected with a liquid outlet at the bottom of the depropanizing tower through a # 8 shielding pump, an isobutane intermediate storage tank connected with a liquid taking port of the isobutane tower through a pipeline, and an isobutane storage tank connected with the isobutane intermediate storage tank through a # 4 shielding pump;
the top of depropanizing tower is passed through the pipeline and is connected with 2# top condenser, the leakage fluid dram of 2# separator passes through the pipe connection with the backward flow mouth of depropanizing tower, the gas that gets into 2# separator after 2# top condenser liquefaction from depropanizing tower top gas carries out gas-liquid separation, the liquid phase gets into the backward flow mouth at depropanizing tower top as the reflux, gaseous phase is sent into the tail gas house steward, the top gas of isobutane tower is through the liquefaction of 3# top condenser after, the liquid phase flows back to the backward flow mouth of isobutane tower as the reflux.
Further, a liquid outlet at the bottom of the isobutane tower is respectively connected with a pentane-rich storage tank and n-butane preparation equipment through pipelines.
Further, the n-butane is prepared equipment and is included and prepare the deisobutanizer that equipment passes through the pipe connection with the isobutane, the n-butane tower of being connected through 7# canned motor pump with the leakage fluid dram of deisobutanizer bottom, the n-butane intermediate storage tank of being connected through the pipe connection with the liquid mouth of getting of n-butane tower, the n-butane storage tank of being connected through 6# canned motor pump with the n-butane intermediate storage tank, the third gas-liquid separation mechanism of being connected through the pipe connection with the top of deisobutanizer and the top of n-butane tower, the reflux that separates through third gas-liquid separation mechanism flows back respectively to the reflux mouth of deisobutanizer and the reflux mouth of n-butane tower, the bottom of n-butane tower is passed through 5# canned motor pump and is connected with LPG raffinate storage tank.
Further, the third gas-liquid separation mechanism comprises a 4# top condenser, a 3# separator connected with a liquid outlet of the 4# top condenser through a pipeline, the liquid outlet of the 3# separator is connected with a top reflux port of the deisobutanizer through a pipeline, the liquid outlet of the 4# top condenser is connected with a reflux port of the n-butane tower through a pipeline, gas discharged from the top of the deisobutanizer is liquefied through the 4# top condenser and then enters the 3# separator for gas-liquid separation, a liquid phase enters the reflux port at the top of the deisobutanizer as reflux liquid, and a gas phase is sent to the tail gas main pipe.
Further, the refrigeration equipment comprises a circulating ice machine, an evaporative condenser connected with the circulating ice machine through a pipeline, and a refrigerant storage tank connected with an outlet of the evaporative condenser;
the refrigerant storage tank uses the cooled condensing agent for refrigeration of propane preparation equipment, isobutane preparation equipment and normal butane preparation equipment, and the refrigerant refrigerated by the propane preparation equipment, the isobutane preparation equipment and the normal butane preparation equipment enters a circulating ice machine and an evaporative condenser for cooling treatment.
The above technical scheme of the utility model at least including following beneficial effect:
1. through multi-tower coupling rectification, effective components in the LPG raw material are separated step by step, various high-purity alkane products are obtained, the process is simple and smooth, the extraction rate is high, the product purity is high, and the operation is stable;
2. the whole physical production process is adopted, no new impurity is introduced, no pollution is caused, and the process safety coefficient is high;
3. the structured packing with large specific surface area is adopted, so that the effects of reduced resistance, high separation efficiency and large operation elastic range are achieved;
4. according to the physicochemical characteristics of C3-C5, the evaporation of the refrigerant is selected as a cold source for reflux at the top of the tower, the temperature of-20 ℃ or even lower can be obtained, the tower pressure is reduced to 0.3MPa or micro-positive pressure, so that the separation degree of each component is increased, the product purity is favorably improved, the temperature at the bottom of the tower can be reduced to normal temperature, the liquefied heat release potential of the compressed refrigerant gas replaces steam to be used as a heat source of a reboiler, the liquefied refrigerant is evaporated at the top of the tower to be used as a cold source for reflux, the refrigeration and heating cycle of the heat pump rectification principle is formed, the production cost is reduced, and the safety and the reliability of the device are greatly improved due to the lower operating pressure;
5. the technological process is continuous rectification, and the long-period safe and stable operation of the device can be realized.
Drawings
FIG. 1 is a flow chart of the process in the embodiment of the present invention;
in the figure:
1. a mixed hydrocarbon storage tank; 2. a deethanizer; 3. 1# Top condenser; 4. 1# separator; 5. a propane column; 6. 2# overhead condenser; 7. a # 2 separator; 8. a depropanizer; 9. 8# canned motor pump; 10. 5# canned motor pump; 11. an isobutane tower; 12. a # 3 top condenser; 13. 1# canned motor pump; 14. a propane intermediate storage tank; 15. 2# canned motor pump; 16. 3# canned motor pump; 17. an isobutane intermediate storage tank; 18. 4# canned motor pump; 19. an isobutane removal tower; 20. 7# canned motor pump; 21. a n-butane tower; 22. 4# Top condenser; 23. a 3# separator; 24. a refrigerant gas-liquid separator; 25. a n-butane intermediate storage tank; 26. 6# canned motor pump; 27. 4# separator; 28. an evaporative condenser; 29. a refrigerant storage tank; 30. a circulating ice machine; 31. an oil separator.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the following description will be made with reference to fig. 1 of the embodiments of the present invention to clearly and completely describe the technical solutions of the embodiments of the present invention. It is to be understood that the embodiments described are some, not all embodiments of the invention. All other embodiments, which can be derived from the description of the embodiments of the present invention by a person skilled in the art, are within the scope of the present invention.
Example 1
As shown in fig. 1: a device for producing high-purity alkane by refining LPG through multi-tower coupling rectification comprises a mixed hydrocarbon storage tank 1 for containing raw materials and propane preparation equipment, wherein the propane preparation equipment is connected with the mixed hydrocarbon storage tank 1 and is used for preparing propane;
the isobutane preparation equipment is connected with the output end of the propane preparation equipment and is used for preparing isobutane;
the normal butane preparation equipment is connected with the isobutane preparation equipment and is used for preparing normal butane;
and the refrigerating equipment is connected with the propane preparation equipment, the isobutane preparation equipment and the normal butane preparation equipment and is used for providing a cold source.
The propane preparation equipment comprises a deethanizer 2 connected with a mixed hydrocarbon storage tank 1 through a pipeline, a propane tower 5 connected with a liquid outlet at the bottom of the deethanizer 2 through a pipeline, a first gas-liquid separation mechanism connected with the top of the deethanizer 2 through a pipeline and used for cooling and gas-liquid separating the top steam of the deethanizer 2, and a second gas-liquid separation mechanism connected with the top of the propane tower 5 and used for cooling and gas-liquid separating the top steam of the propane tower 5, wherein reflux liquid separated by the first gas-liquid separation mechanism from the top steam of the deethanizer 2 flows back into the deethanizer 2, and reflux liquid separated by the second gas-liquid separation mechanism from the top steam of the propane tower 5 flows back into the propane tower 5; the liquid taking port of the propane tower 5 is connected with a propane intermediate storage tank 14 through a pipeline, and the liquid discharging port of the propane intermediate storage tank 14 is connected with the propane storage tank through a 2# shield pump 15. The first gas-liquid separation mechanism comprises a 1# top condenser 3 connected with the top of a deethanizer 2 through a pipeline, a 1# separator 4 connected with a liquid outlet of the 1# top condenser 3 through a pipeline, a liquid outlet of the 1# separator 4 is connected with a reflux outlet of the deethanizer 2 through a pipeline, gas discharged from the top of the deethanizer 2 is liquefied through the 1# top condenser 3 and then enters the 1# separator 4 for gas-liquid separation, a liquid phase enters a reflux outlet at the top of the deethanizer 2 as reflux liquid, a gas phase is sent to a tail gas main pipe, the second gas-liquid separation mechanism comprises a 2# top condenser 6 connected with the top of a propane tower 5 through a pipeline, a 2# separator 7 connected with a liquid outlet of the 2# top condenser 6 through a pipeline, a liquid outlet of the 2# top condenser 6 is connected with a reflux outlet of a propane tower 5 through a pipeline, and a liquid phase enters a top reflux outlet of the propane tower 5 as reflux liquid after the liquid discharged from the top of the propane tower 5 is liquefied through the 2# top condenser 6.
The specific flow of the propane preparation equipment for preparing propane is as follows: LPG raw material comes from a mixed hydrocarbon storage tank 1 and is connected with an inlet at the middle upper part of a deethanizer 2 through a pipeline, the raw material enters the deethanizer 2 and then has mass transfer and heat transfer with reflux liquid at the top of the deethanizer 2, the temperature range of the reflux liquid is minus 5 ℃ to minus 1 ℃, after the mass transfer and heat transfer, the temperature range of heavy components is 5 ℃ to 13 ℃, the heavy components are continuously accumulated at the bottom of the deethanizer 2, the light components are heated and evaporated by a reboiler at the bottom of the deethanizer 2, the temperature range heated by the reboiler is 5 ℃ to 13 ℃, the heavy components are discharged from the top of the deethanizer 2, the heavy components enter a top condenser 3# 1 through a pipeline to exchange heat with refrigerant of the top condenser 3# 1, most of the LPG raw material is liquefied and then enters a separator 4# 1 through a pipeline to be subjected to gas-liquid separation, the liquid phase is taken as the reflux liquid to enter a top reflux port of the deethanizer 2, the gas phase is sent to a tail gas-gas main pipe, and the liquid component at the bottom of the deethanizer 2 is C 3 H 8 67%，C 2 H 6 0.5ppm，C 4 H 10-1 15%，C 4 H 10-2 13% and the balance being trace C 5 And the components are mixed, the temperature is 5 to 13 ℃, the pressure is 4 to 5bar, and most of ethane in the raw materials is removed; the liquid phase discharged from the bottom of the deethanizer 2 is connected with the middle inlet of the propane tower 5 through a pipeline, the liquid phase discharged from the bottom of the deethanizer 2 and the reflux liquid at the top of the propane tower 5 are subjected to mass transfer and heat transfer, the temperature range of the reflux liquid is-13 ℃ to-3 ℃, after the mass transfer and heat transfer, the temperature range of the heavy component is 30 ℃ to 40 ℃, the heavy component is continuously accumulated at the bottom of the propane tower 5, the light component is heated and evaporated by a reboiler at the bottom of the propane tower 5, the temperature range heated by the reboiler is 30 ℃ to 40 ℃, the heavy component is discharged from the top of the propane tower 5, enters a 2# top condenser 6 through a pipeline, and is cooled with the 2# topThe refrigerant of the condenser 6 exchanges heat, most of the liquefied refrigerant enters a propane tower reflux port through a pipeline after being liquefied, the temperature of the liquefied reflux liquid is minus 13 ℃ to minus 3 ℃, the pressure is 3 to 4.5bar, an overflow weir is arranged at the upper part of the propane tower 5, the reflux liquid firstly enters the overflow weir, when the liquid level is higher than a baffle plate of the overflow weir, the reflux liquid overflows from the top of the propane tower 5 to the bottom of the propane tower 5, a liquid taking port is arranged at the lower part of the overflow weir, a propane product is obtained through control of an adjusting valve, the propane taking port is connected with a propane intermediate storage tank 14 through a pipeline, a liquid phase is sent into a propane storage tank through a 2# shielding pump 15, the purity of the propane product is more than 99.995%, the temperature is minus 5 ℃ to minus 10 ℃, the pressure is 3.2 to 4bar, the extraction rate of propane can reach more than 97%, and a gas phase returns to the top of the propane tower 5 to be continuously condensed and separated, so that the extraction rate of the product is improved.
The isobutane preparation equipment comprises a depropanizing tower 8, an isobutane tower 11, an isobutane intermediate storage tank 17 and an isobutane intermediate storage tank 17, wherein the depropanizing tower 8 is connected with the bottom of a propane tower 5 through a # 1 shielding pump 13 and a pipeline, a liquid outlet at the bottom of the depropanizing tower 8 is connected with an isobutane taking port of the isobutane tower 11 through a pipeline, the isobutane intermediate storage tank 17 is connected with an isobutane storage tank through a # 4 shielding pump 18, the top of the depropanizing tower 8 is connected with a # 2 top condenser 6 through a pipeline, a liquid outlet of a # 2 separator 7 is connected with a reflux port of the depropanizing tower 8 through a pipeline, gas discharged from the top of the depropanizing tower 8 is liquefied through the # 2 top condenser 6 and then enters the # 2 separator 7 for gas-liquid separation, a liquid phase is taken as reflux liquid and enters a reflux port at the top of the depropanizing tower 5, a gas phase is sent to a main pipe, and the liquid phase is taken as the reflux liquid and then reflows to the reflux port of the isobutane tower 11 after the top gas of the isobutane tower 12 is liquefied through the # 3 top condenser. And a liquid outlet at the bottom of the isobutane tower 11 is respectively connected with a pentane-rich storage tank and n-butane preparation equipment through pipelines.
The specific process for preparing isobutane by isobutane preparing equipment comprises the following steps: liquid discharged from the bottom of the propane tower 5 is sent into the depropanizing tower 8 through a No. 1 shielding pump 13, enters from the middle part of the depropanizing tower 8, and has mass and heat transfer with reflux liquid at the top of the depropanizing tower 8, the temperature range of the reflux liquid is-11 ℃ to-1 ℃, after the mass and heat transfer, the temperature range of heavy components is 22 ℃ to 32 ℃, and the heavy components are continuously accumulated at the bottom of the depropanizing tower 8The light component is heated and evaporated by a reboiler at the bottom of the depropanizing tower 8, the temperature range of the reboiler is 22-32 ℃, the light component is discharged from the top of the depropanizing tower 8, the light component enters the 2# top condenser 6 through a pipeline, the light component exchanges heat with refrigerant of the 2# top condenser 6, most of the light component is liquefied and then enters the 2# separator 7 through a pipeline to be subjected to gas-liquid separation, the liquid phase enters a reflux port at the top of the depropanizing tower 8 as reflux liquid, the gas phase is sent into a tail gas main pipe, the bottom liquid component of the depropanizing tower 8 is C 3 H 8 1ppm，C 4 H 10-1 48%，C 4 H 10-2 39% and the rest is trace C 5 And the components are mixed, the temperature is 22-32 ℃, the pressure is 2.2-3.2bar, and most of propane in the raw materials is removed; liquid discharged from the bottom of the depropanization 8 tower is sent into an isobutane tower 11 through a # 8 shielding pump 8, enters from the middle lower part of the isobutane tower 11, and is subjected to mass and heat transfer with a top reflux liquid of the isobutane tower 11, the temperature range of the reflux liquid is-13 ℃ to-3 ℃, after the mass and heat transfer, the temperature range of a heavy component is 2 ℃ to 12 ℃, the heavy component is continuously accumulated at the bottom of the isobutane tower 11, a light component is heated and evaporated through a bottom reboiler of the isobutane tower 11 at the bottom of the isobutane tower, the temperature range heated by the reboiler is 2 ℃ to 12 ℃, the liquid is discharged from the top of the isobutane tower 11, enters a # 3 top condenser 12 through a pipeline, is subjected to heat exchange with a refrigerant of the # 3 top condenser 12, most of the liquid is liquefied and then enters a reflux port of the isobutane tower 11 through the pipeline, the temperature of the liquefied reflux liquid is-13 ℃ to-3 ℃, the pressure is 1 to 1.3bar, an overflow weir is arranged at the upper part of the isobutane tower 11, the reflux liquid firstly enters the overflow weir, when the liquid level is higher than a baffle plate of the overflow weir, the reflux liquid overflows from the top of the isobutane tower 11 to the bottom of the isobutane tower 11, a liquid taking port is arranged at the lower part of the overflow weir, an isobutane product is obtained under the control of an adjusting valve, the isobutane taking port is connected with an isobutane intermediate storage tank 17 through a pipeline, the liquid phase is sent into the isobutane storage tank through a 4# shielding pump 16, the purity of the isobutane product is more than 99.995%, the temperature is-4 ℃ to-11 ℃, the pressure is 1.02 to 1.5bar, the extraction rate of isobutane can reach more than 90, and the gas phase returns to the top of the isobutane tower 11 to be continuously condensed and separated, so that the extraction rate of the product is improved.
The n-butane preparation equipment comprises an deisobutanizer 19 connected with an isobutane tower 11 through a 3# shielding pump 15 and a pipeline, an n-butane tower 21 connected with a liquid outlet at the bottom of the deisobutanizer 19 through a 7# shielding pump 20, an n-butane intermediate storage tank 25 connected with a liquid taking port of the n-butane tower 21 through a pipeline, an n-butane storage tank connected with the n-butane intermediate storage tank 25 through a 6# shielding pump 26, and a third gas-liquid separation mechanism connected with the top of the deisobutanizer 19 and the top of the n-butane tower 21 through pipelines, wherein reflux liquid separated by the third gas-liquid separation mechanism respectively reflows to a reflux port of the deisobutanizer 19 and a reflux port of the n-butane tower 21, and the bottom of the n-butane tower 21 is connected with LPG through a 5# shielding pump 10. The third gas-liquid separation mechanism comprises a 4# top condenser 22 and a 3# separator 23 connected with a liquid discharge port of the 4# top condenser 22 through a pipeline, the liquid discharge port of the 3# separator 23 is connected with a top reflux port of the deisobutanizer 19 through a pipeline, the liquid discharge port of the 4# top condenser 22 is connected with a reflux port of the n-butane tower 21 through a pipeline, gas discharged from the top of the deisobutanizer 19 is liquefied through the 4# top condenser 22 and then enters the 3# separator for gas-liquid separation, a liquid phase is taken as reflux liquid to enter the reflux port at the top of the deisobutanizer 19, and a gas phase is sent to a tail gas main pipe.
The specific flow of the n-butane preparation equipment for preparing n-butane is as follows: the method comprises the steps that liquid discharged from the bottom of an isobutane tower 11 is pressurized through a 3# shielding pump 16 and then divided into two paths, one path is connected with a pentane-rich storage tank, the other path is sent into an isobutane removing tower 19 and enters from the middle upper portion of the isobutane removing tower 19 to perform mass and heat transfer with overhead reflux liquid of the isobutane removing tower 19, the temperature range of the reflux liquid is 10-18 ℃, after mass and heat transfer, the temperature range of heavy components is 22-32 ℃, the heavy components are continuously accumulated at the bottom of the isobutane removing tower 19, the light components are heated and evaporated through a tower bottom reboiler of the isobutane removing tower 19, the temperature range heated by the reboiler is 22-32 ℃, the liquid components are discharged from the top of the isobutane removing tower 19, enter a 4# top condenser 22 through a pipeline to perform heat exchange with refrigerant of the 4# top condenser 22, most of the liquid components are liquefied and then enter a 3# separator 23 through a pipeline to perform separation, liquid phase serving as gas-liquid reflux liquid at the top of the isobutane removing tower 19, the gas phase is sent to a tail gas-phase main pipe, and liquid component of the isobutane removing tower 19 is C 4 H 10-1 75%，C 5 H 12-2 14%，C 4 H 10-2 0.2% and trace C 5 And the components are mixed, the temperature is 22-32 ℃, the pressure is 1.7-2.6 bar, and most of isobutane in the raw material is removed; liquid discharged from the bottom of the deisobutanizer 19 is sent into a normal butane tower 21 through a 7# shielding pump, enters from the middle lower part of the normal butane tower 21, and has mass and heat transfer with the top reflux of the normal butane tower 21, the temperature range of the reflux is 11-21 ℃, after the mass and heat transfer, the temperature range of heavy components is 30-40 ℃, the heavy components are continuously accumulated at the bottom of the normal butane tower 21, the light components are heated and evaporated through a tower bottom reboiler of the normal butane tower 21, the temperature range heated by the reboiler is 30-40 ℃, the liquid is discharged from the top of the normal butane tower 21, enters a 4# top condenser 22 through a pipeline, exchanges heat with refrigerant of the 4# top condenser 22, most of the liquid is liquefied and enters a reflux opening of the normal butane tower 21 through a pipeline, the temperature of the liquefied reflux liquid is 11-21 ℃, the pressure is 1.2-2.3 bar, an overflow weir is arranged at the upper part of a normal butane tower 21, the reflux liquid firstly enters the overflow weir, when the liquid level exceeds a baffle plate of the overflow weir, the reflux liquid overflows from the top of the normal butane tower 21 to the bottom of the normal butane tower 21, a liquid taking port is arranged at the lower part of the overflow weir, a normal butane product is obtained under the control of an adjusting valve, the liquid taking port of the normal butane is connected with a normal butane intermediate storage tank through a pipeline, the liquid phase is sent into the normal butane storage tank through a No. 6 shielding pump, the purity of the normal butane product is more than 99%, the temperature is 10-20 ℃, the pressure is 1.2-2.5 bar, the extraction rate of the normal butane can reach more than 85%, the gas phase returns to the top of the normal butane tower 21 and is continuously condensed and separated, and the product extraction rate is improved.
The refrigeration equipment comprises a circulating ice machine 30, an evaporative condenser 28 connected with the circulating ice machine 30 through a pipeline, and a refrigerant storage tank 29 connected with an outlet of the evaporative condenser 28, wherein the refrigerant storage tank 29 is used for refrigerating cooled condensing agents for propane preparation equipment, isobutane preparation equipment and n-butane preparation equipment, the refrigerant refrigerated by the propane preparation equipment, the isobutane preparation equipment and the n-butane preparation equipment enters the circulating ice machine and the evaporative condenser 28 for cooling treatment, the refrigeration equipment further comprises a refrigerant gas-liquid separator 24 for performing gas-liquid separation on the refrigerant, a liquid outlet of the refrigerant gas-liquid separator 24 is connected with a refrigerant inlet of the circulating ice machine, a refrigerant inlet of the 4# top condenser 22, a refrigerant inlet of the 3# top condenser 12, a refrigerant inlet of the 1# top condenser 3 and a refrigerant inlet of the 4# separator 27 through pipelines, an inlet of the refrigerant gas-liquid separator 24 is connected with an inlet of the refrigerant gas-liquid separator 29 through a pipeline, a refrigerant outlet of the 4# top condenser 22 is connected with an inlet of the refrigerant gas-liquid separator 24 through a pipeline, and a refrigerant outlet of the 4# separator 27 is connected with the circulating ice machine 30 through a pipeline for cooling.
Example 2
A process for producing high-purity alkane by refining LPG through multi-tower coupling rectification comprises the following steps:
step 1, adding the raw materials into propane preparation equipment to obtain propane and a first mixed raw material; the method comprises the following specific steps: LPG raw material comes from a mixed hydrocarbon storage tank 1 and is connected with an inlet at the middle upper part of a deethanizer 2 through a pipeline, the raw material enters the deethanizer 2 and then undergoes mass and heat transfer with reflux liquid at the top of the deethanizer 2, the temperature range of the reflux liquid is-5 ℃ to-1 ℃, after the mass and heat transfer, the temperature range of heavy components is 5 ℃ to 13 ℃, the heavy components are continuously accumulated at the bottom of the deethanizer 2, the light components are heated and evaporated by a reboiler at the bottom of the deethanizer 2, the temperature range heated by the reboiler is 5 ℃ to 13 ℃, the heavy components are discharged from the top of the deethanizer 2, the heavy components enter a No. 1 top condenser 3 through a pipeline to exchange heat with refrigerant of the No. 1 top condenser 3, most of the LPG raw material is liquefied and then enters a No. 1 separator 4 through a pipeline to be subjected to gas-liquid separation, the liquid phase serving as the reflux liquid enters a top reflux port of the deethanizer 2, the gas phase is sent to a tail gas main pipe, and the liquid component at the bottom of the deethanizer 2 is C 3 H 8 67%，C 2 H 6 0.5ppm，C 4 H 10-1 15%，C 4 H 10-2 13% and the balance being trace C 5 And the components are mixed, the temperature is 5 to 13 ℃, the pressure is 4 to 5bar, and most of ethane in the raw materials is removed; the liquid phase discharged from the bottom of the deethanizer 2 is connected with the middle inlet of the propane tower 5 through a pipeline, the liquid phase discharged from the bottom of the deethanizer 2 and the reflux liquid at the top of the propane tower 5 carry out mass and heat transfer, the temperature range of the reflux liquid is-13 ℃ to-3 ℃, after the mass and heat transfer, the temperature range of the heavy component is 30 ℃ to 40 ℃,heavy components are continuously accumulated at the bottom of a propane tower 5, light components are heated and evaporated by a reboiler at the bottom of the propane tower 5, the heating temperature range of the reboiler is 30-40 ℃, the light components are discharged from the top of the propane tower 5, the light components enter a 2# top condenser 6 through a pipeline to exchange heat with refrigerant of the 2# top condenser 6, most of the light components are liquefied and then enter a return opening of the propane tower 5 through a pipeline, the temperature of the return liquid is-13 ℃ to-3 ℃, the pressure of the return liquid is 3 to 4.5bar, an overflow weir is arranged at the upper part of the propane tower 5, the return liquid firstly enters the overflow weir, when the liquid level is higher than a baffle of the overflow weir, the return liquid overflows from the top of the propane tower 5 to the bottom of the propane tower 5, a liquid taking opening is arranged at the lower part of the overflow weir and is controlled by a regulating valve to obtain a propane product, the liquid taking opening is connected with a propane intermediate storage tank 14 through a pipeline, the liquid phase is sent into a propane storage tank through a 2# shielding pump 15, the purity of the propane product is over 99.995%, the temperature is-5 ℃ to-10 ℃, the pressure of the propane product is over 97%, the extraction rate of the propane tower, and the gas phase is continuously condensed and the propane separation tower, and the gas phase is increased.
Step 2, adding the first mixed raw material obtained in the step 1 into isobutane preparation equipment to obtain isobutane and pentane-rich gas, and meanwhile, obtaining a second mixed raw material; the method comprises the following specific steps: liquid discharged from the bottom of a propane tower 5 is sent into a depropanizing tower 8 through a No. 1 shielding pump 13, enters from the middle of the depropanizing tower 8, has a mass and heat transfer reflux liquid temperature range of-11 ℃ to-1 ℃ with the top reflux liquid of the depropanizing tower 8, after mass and heat transfer, has a heavy component temperature range of 22 ℃ to 32 ℃, continuously accumulates at the bottom of the depropanizing tower 8, a light component is heated and evaporated through a reboiler at the bottom of the depropanizing tower 8, has a heating temperature range of 22 ℃ to 32 ℃, is discharged from the top of the depropanizing tower 8, enters a No. 2 top condenser 6 through a pipeline to exchange heat with refrigerant of the No. 2 top condenser 6, most of the liquid is liquefied and then enters a No. 2 separator 7 to be subjected to gas-liquid separation through a pipeline, a liquid phase is taken as a reflux liquid to enter a reflux port at the top of the depropanizing tower 8, a gas phase is sent to a tail gas-phase main pipe, and a liquid component at the bottom of the depropanizing tower 8 is C 3 H 8 1ppm，C 4 H 10-1 48%，C 4 H 10-2 39% and the balance being trace C 5 And the components are mixed at the temperature of 22-32 ℃ and the pressure2.2 to 3.2bar, and removing most of propane in the raw materials; liquid discharged from the bottom of the depropanization 8 tower is sent into an isobutane tower 11 through a # 8 shielding pump 8, enters from the middle lower part of the isobutane tower 11, and is subjected to mass and heat transfer with a top reflux liquid of the isobutane tower 11, the temperature range of the reflux liquid is-13 ℃ to-3 ℃, after the mass and heat transfer, the temperature range of a heavy component is 2 ℃ to 12 ℃, the heavy component is continuously accumulated at the bottom of the isobutane tower 11, a light component is heated and evaporated through a bottom reboiler of the isobutane tower 11 at the bottom of the isobutane tower, the temperature range heated by the reboiler is 2 ℃ to 12 ℃, the liquid is discharged from the top of the isobutane tower 11, enters a # 3 top condenser 12 through a pipeline, is subjected to heat exchange with a refrigerant of the # 3 top condenser 12, most of the liquid is liquefied and then enters a reflux port of the isobutane tower 11 through the pipeline, the temperature of the liquefied reflux liquid is-13 ℃ to-3 ℃, the pressure is 1 to 1.3bar, an overflow weir is arranged at the upper part of the isobutane tower 11, the reflux liquid firstly enters the overflow weir, when the liquid level is higher than a baffle plate of the overflow weir, the reflux liquid overflows from the top of the isobutane tower 11 to the bottom of the isobutane tower 11, a liquid taking port is arranged at the lower part of the overflow weir, an isobutane product is obtained under the control of an adjusting valve, the isobutane taking port is connected with an isobutane intermediate storage tank 17 through a pipeline, the liquid phase is sent into the isobutane storage tank through a 4# shielding pump 16, the purity of the isobutane product is more than 99.995%, the temperature is-4 ℃ to-11 ℃, the pressure is 1.02 to 1.5bar, the extraction rate of isobutane can reach more than 90, and the gas phase returns to the top of the isobutane tower 11 to be continuously condensed and separated, so that the extraction rate of the product is improved.
And 3, adding the second mixed raw material obtained in the step 2 into n-butane preparation equipment to obtain n-butane and LPG raffinate, wherein the specific steps are as follows: the method comprises the steps that the pressure of liquid discharged from the bottom of an isobutane tower 11 is increased through a 3# shielding pump 16, the liquid is divided into two paths, one path is connected with a pentane-rich storage tank, the other path is sent into an isobutane removing tower 19, the liquid enters from the middle upper portion of the isobutane removing tower 19 and conducts mass transfer and heat transfer with top reflux liquid of the isobutane removing tower 19, the temperature range of the reflux liquid is 10-18 ℃, after mass transfer and heat transfer, the temperature range of heavy components is 22-32 ℃, the heavy components are continuously accumulated at the bottom of the isobutane removing tower 19, the light components are heated and evaporated through a bottom reboiler of the isobutane removing tower 19, the heating temperature range of the reboiler is 22-32 ℃, and the liquid is discharged from the top of the isobutane removing tower 19And the liquid phase enters a top reflux port of the deisobutanizer 19 as reflux liquid, the gas phase is sent to a tail gas main pipe, and the liquid component at the bottom of the deisobutanizer 19 is C 4 H 10-1 75%，C 5 H 12-2 14%，C 4 H 10-2 0.2% and trace C 5 And the components are mixed, the temperature is 22-32 ℃, the pressure is 1.7-2.6 bar, and most of isobutane in the raw materials is removed; liquid discharged from the bottom of the deisobutanizer 19 is sent into a normal butane tower 21 through a 7# shielding pump, enters from the middle lower part of the normal butane tower 21, and has mass and heat transfer with the top reflux of the normal butane tower 21, the temperature range of the reflux is 11-21 ℃, after the mass and heat transfer, the temperature range of heavy components is 30-40 ℃, the heavy components are continuously accumulated at the bottom of the normal butane tower 21, the light components are heated and evaporated through a tower bottom reboiler of the normal butane tower 21, the temperature range heated by the reboiler is 30-40 ℃, the liquid is discharged from the top of the normal butane tower 21, enters a 4# top condenser 22 through a pipeline, exchanges heat with refrigerant of the 4# top condenser 22, most of the liquid is liquefied and enters a reflux opening of the normal butane tower 21 through a pipeline, the temperature of the liquefied reflux liquid is 11-21 ℃, the pressure is 1.2-2.3 bar, an overflow weir is arranged at the upper part of a normal butane tower 21, the reflux liquid firstly enters the overflow weir, when the liquid level exceeds a baffle plate of the overflow weir, the reflux liquid overflows from the top of the normal butane tower 21 to the bottom of the normal butane tower 21, a liquid taking port is arranged at the lower part of the overflow weir, a normal butane product is obtained under the control of an adjusting valve, the liquid taking port of the normal butane is connected with a normal butane intermediate storage tank through a pipeline, the liquid phase is sent into the normal butane storage tank through a No. 6 shielding pump, the purity of the normal butane product is more than 99%, the temperature is 10-20 ℃, the pressure is 1.2-2.5 bar, the extraction rate of the normal butane can reach more than 85%, the gas phase returns to the top of the normal butane tower 21 and is continuously condensed and separated, and the product extraction rate is improved.
In the present invention, unless otherwise explicitly specified or limited, for example, it may be fixedly connected, detachably connected, or integrated; can be mechanically or electrically connected; they may be directly connected or indirectly connected through an intermediate medium, and may be connected through the inside of two elements or in an interaction relationship between two elements, unless otherwise specifically defined, and the specific meaning of the above terms in the present invention will be understood by those skilled in the art according to specific situations.
The foregoing is a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, a plurality of improvements and decorations can be made without departing from the principle of the present invention, and these improvements and decorations should be regarded as the protection scope of the present invention.
Claims (8)
1. An apparatus for producing high purity alkane by refining LPG through multi-tower coupling rectification comprises a mixed hydrocarbon storage tank for containing raw materials, and is characterized by also comprising:
a propane production facility connected to the mixed hydrocarbon storage tank and configured to produce propane;
the isobutane preparation equipment is connected with the output end of the propane preparation equipment and is used for preparing isobutane;
the n-butane preparation equipment is connected with the isobutane preparation equipment and is used for preparing n-butane;
and the refrigeration equipment is connected with the propane preparation equipment, the isobutane preparation equipment and the normal butane preparation equipment and is used for providing a cold source.
2. The apparatus for producing high purity paraffin according to claim 1, wherein the propane producing means comprises a deethanizer connected to the mixed hydrocarbon storage tank through a pipe, a propane column connected to a liquid outlet at the bottom of the deethanizer through a pipe, a first gas-liquid separating means connected to the top of the deethanizer through a pipe for cooling and separating the vapor at the top of the deethanizer, and a second gas-liquid separating means connected to the top of the propane column for cooling and separating the vapor at the top of the propane column;
reflux liquid separated by the vapor at the top of the deethanizer through the first gas-liquid separation mechanism flows back into the deethanizer, and reflux liquid separated by the vapor at the top of the propane tower through the second gas-liquid separation mechanism flows back into the propane tower;
the liquid taking port of the propane tower is connected with a propane intermediate storage tank through a pipeline, and the liquid discharging port of the propane intermediate storage tank is connected with the propane storage tank through a 2# shielding pump.
3. The apparatus for producing high purity paraffin hydrocarbon from LPG through multi-tower coupled rectification refining as claimed in claim 2, wherein the first gas-liquid separation means comprises a # 1 top condenser connected to the top of the deethanizer through a pipeline, and a # 1 separator connected to the liquid outlet of the # 1 top condenser through a pipeline, the liquid outlet of the # 1 separator is connected to the reflux outlet of the deethanizer through a pipeline, the gas discharged from the top of the deethanizer is liquefied by the # 1 top condenser and then enters the # 1 separator for gas-liquid separation, the liquid phase enters the reflux outlet of the top of the deethanizer as reflux liquid, and the gas phase is sent to the tail gas main;
the second gas-liquid separation mechanism comprises a 2# top condenser connected with the top of the propane tower through a pipeline, and a 2# separator connected with a liquid discharge port of the 2# top condenser through a pipeline, wherein the liquid discharge port of the 2# top condenser is connected with a reflux port of the propane tower through a pipeline, and after the gas discharged from the top of the propane tower is liquefied through the 2# top condenser, a liquid phase enters the reflux port at the top of the propane tower as reflux liquid.
4. The apparatus for producing high purity alkane from LPG through multi-tower coupling rectification refining as claimed in claim 1, wherein said isobutane making equipment includes a depropanizer connected with propane making equipment through a pipeline, an isobutane tower connected with a liquid outlet at the bottom of the depropanizer through a # 8 shield pump, an isobutane intermediate storage tank connected with a liquid outlet of the isobutane tower through a pipeline, and an isobutane storage tank connected with the isobutane intermediate storage tank through a # 4 shield pump;
the top of depropanizing tower is passed through the pipeline and is connected with 2# top condenser, the leakage fluid dram of 2# separator passes through the pipe connection with the backward flow mouth of depropanizing tower, the gas that gets into 2# separator after 2# top condenser liquefaction from depropanizing tower top gas carries out gas-liquid separation, the liquid phase gets into the backward flow mouth at depropanizing tower top as the reflux, gaseous phase is sent into the tail gas house steward, the top gas of isobutane tower is through the liquefaction of 3# top condenser after, the liquid phase flows back to the backward flow mouth of isobutane tower as the reflux.
5. The apparatus for producing high purity alkane from LPG through coupled rectification of multiple towers according to claim 4, wherein the liquid outlet at the bottom of the isobutane tower is connected with a pentane-rich storage tank and n-butane production equipment through pipelines.
6. The apparatus according to claim 1, wherein the n-butane production device comprises an isobutane removal tower connected to the isobutane production device through a pipeline, an n-butane tower connected to a liquid outlet at the bottom of the isobutane removal tower through a 7# shielding pump, an n-butane intermediate storage tank connected to a liquid outlet of the n-butane tower through a pipeline, an n-butane storage tank connected to the n-butane intermediate storage tank through a 6# shielding pump, and a third gas-liquid separation mechanism connected to the top of the isobutane removal tower and the top of the n-butane tower through a pipeline, wherein the reflux liquid separated by the third gas-liquid separation mechanism respectively flows back to the reflux outlet of the isobutane removal tower and the reflux outlet of the n-butane tower, and the bottom of the n-butane tower is connected to the LPG raffinate storage tank through a 5# shielding pump.
7. The device for producing high-purity alkane by refining LPG through multi-tower coupled rectification according to claim 6, wherein the third gas-liquid separation mechanism comprises a No. 4 top condenser and a No. 3 separator connected with a liquid outlet of the No. 4 top condenser through a pipeline, the liquid outlet of the No. 3 separator is connected with a top reflux port of the deisobutanizer through a pipeline, the liquid outlet of the No. 4 top condenser is connected with a reflux port of the n-butane tower through a pipeline, gas discharged from the top of the deisobutanizer is liquefied through the No. 4 top condenser and then enters the No. 3 separator for gas-liquid separation, a liquid phase is taken as reflux liquid and enters the reflux port at the top of the deisobutanizer, and a gas phase is sent to a tail gas main pipe.
8. The apparatus for producing high purity paraffin hydrocarbon from LPG using multi-tower coupled rectification for refining according to claim 6, wherein the refrigeration equipment comprises a circulating ice maker, an evaporative condenser connected to the circulating ice maker via a pipe, and a refrigerant storage tank connected to an outlet of the evaporative condenser;
the refrigerant storage tank uses the cooled condensing agent for refrigeration of propane preparation equipment, isobutane preparation equipment and normal butane preparation equipment, and the refrigerant refrigerated by the propane preparation equipment, the isobutane preparation equipment and the normal butane preparation equipment enters a circulating ice machine and an evaporative condenser for cooling treatment.
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