Multifunctional alkylbenzene production system

Abstract

The invention provides a multifunctional alkylbenzene production system which is used for producing straight-chain alkylbenzene or polysubstituted alkylbenzene, and relates to the technical field of alkylbenzene production. The device comprises an alkylation reaction device, a hydraulic turbine, a debenzolization tower, a light component removal tower and a heavy component removal tower, materials obtained through reaction of the alkylation reaction device are connected into the hydraulic turbine, and an outlet of the hydraulic turbine is connected into the debenzolization tower or the light component removal tower. When straight-chain alkylbenzene is produced, an outlet of the hydraulic turbine is connected into the debenzolization tower, materials at the bottom of the debenzolization tower are connected into the light component removal tower, materials at the bottom of the light component removal tower are connected into the heavy component removal tower, and an alkylbenzene product is extracted from a side line of the heavy component removal tower; when polysubstituted alkylbenzene is produced, an outlet of the hydraulic turbine is connected into the light component removal tower, materials at the bottom of the light component removal tower are divided into two streams, one stream is connected into the benzene removal tower, the other stream is connected into the heavy component removal tower, and an alkylbenzene product is extracted from a side line of the heavy component removal tower. The method is designed according to the characteristics of an alkylbenzene synthesis process, and has the characteristics of short flow, continuous operation, comprehensive heat recycling, low energy consumption and diversified production.

Description

Technical Field

[0001] This application relates to the technical field of alkylbenzene production, and in particular to a multifunctional alkylbenzene production system. Background Art

[0002] Alkylbenzene is an organic compound, and its basic structure consists of an alkyl group and a benzene ring. Alkylbenzenes can generally be divided into linear alkylbenzenes (LAB) and branched alkylbenzenes (BAB). Linear alkylbenzenes usually refer to long straight-chain alkylbenzenes with a mixed carbon atom number of C10 - C14, which are mainly used to synthesize linear alkylbenzene sulfonates (LAS). Linear alkylbenzene sulfonates (LAS) have long been the most widely used and important synthetic surfactants in the world and are the main raw materials for synthetic detergents. Other linear alkylbenzenes with different carbon atom numbers are also important organic synthesis intermediates. For example, linear C16 - C18 alkylbenzenes are common surfactant intermediates such as oil displacement agents, and C20 - C24 alkylbenzenes are often used as lubricating oil dispersant intermediates. Compared with linear alkylbenzenes (LAB), branched alkylbenzene (BAB) detergent products have better washing performance, lower costs, and are more widely used. In addition, dialkylbenzene is the most typical alkylbenzene used as a lubricating base oil, which is used for blending engine oils, gear oils, and hydraulic oils and can be applied under low-temperature conditions below 0°C.

[0003] Currently, since different alkylbenzene products need to be produced using different catalysts and different reaction conditions are required for different alkylbenzene products, a production device can only produce one alkylbenzene product. Moreover, in the existing production process, the alkylation production process has a long flow, heavy pollution, high energy consumption, and the heat is not fully recovered and utilized; the feed raw materials are single and the product varieties produced are also single, and it is impossible to flexibly adjust production according to the changes in raw materials and product markets.

[0004] Therefore, the current alkylbenzene production devices can no longer meet the green chemistry concept of current green and low-carbon development. Summary of the Invention

[0005] In order to improve the problems of the current alkylbenzene production device, such as long process flow, high energy consumption, heavy pollution, and single raw materials and products in the production process, this application provides a multifunctional alkylbenzene production system.

[0006] This application provides a multifunctional alkylbenzene production system, adopting the following technical solutions: A multifunctional alkylbenzene production system for producing linear alkylbenzene or polysubstituted alkylbenzene, comprising an alkylation reaction unit, a hydraulic turbine, a debenzene tower, a light-removal tower, and a heavy-removal tower. The material obtained by the reaction in the alkylation reaction unit is connected to the hydraulic turbine for recovering the alkylation reaction pressure. The outlet of the hydraulic turbine can be connected to the debenzene tower or the light-removal tower. When producing linear alkylbenzene, the outlet of the hydraulic turbine is connected to the debenzene tower, the bottom material of the debenzene tower is connected to the light removal tower, the bottom material of the light removal tower is connected to the heavy removal tower, and the material taken out of the heavy removal tower side line is cooled to obtain a linear alkylbenzene product; When producing multi-substituted alkylbenzenes, the outlet of the hydraulic turbine is connected to the light removal tower, and the bottom material of the light removal tower is divided into two streams, one of which is connected to the debenzene tower and the other is connected to the heavy removal tower. The material is taken out from the side line of the heavy removal tower and cooled to obtain the dialkylbenzene product.

[0007] Optionally, an alkylation heat exchanger is further included, wherein the tube side inlet of the alkylation heat exchanger is connected to the raw materials to be reacted, the tube side outlet of the alkylation heat exchanger is connected to the inlet of the alkylation reaction unit, the outlet of the alkylation reaction unit is connected to the shell side inlet of the alkylation heat exchanger, and the shell side outlet of the alkylation heat exchanger is connected to the hydraulic turbine.

[0008] Optionally, a dehydration tower for dehydrating the raw materials to be reacted is further included, wherein the raw materials to be reacted include reaction raw material 1 and reaction raw material 2, the reaction raw material 1 is connected from the lower middle part of the dehydration tower, the top of the dehydration tower is connected to the inlet of the dehydration tower top condenser tube side, the outlet of the dehydration tower top condenser tube side is connected to the dehydration tower reflux pump, the outlet of the dehydration tower reflux pump is returned to the dehydration tower, the reaction raw material 2 is connected to the inlet of the benzene heater tube side, and the outlet of the benzene heater tube side is connected to the outlet pipeline of the dehydration tower reflux pump.

[0009] Optionally, the dehydration tower kettle is provided with a first reboiler, the tube side inlet of the first reboiler is connected to the shell side outlet of the alkylation heat exchanger, the tube side outlet of the first reboiler is connected to the hydraulic turbine, and the shell side is connected to the dehydration tower.

[0010] Optionally, the bottom of the dehydration tower is connected to the inlet of the dehydration tower bottom discharge heater tube side through the dehydration tower bottom output pump, the outlet of the dehydration tower bottom discharge heater tube side is connected to the alkylation reaction unit, the shell side outlet of the alkylation heat exchanger is connected to the inlet of the first reboiler tube side, and the outlet of the first reboiler tube side is connected to the hydraulic turbine.

[0011] Optionally, the alkylation reaction device includes a first alkylation reactor, a second alkylation reactor, a third alkylation reactor, and a fourth alkylation reactor connected in series. The operating mode of the four alkylbenzene reactors is three in operation and one in standby. And the first alkylation reactor or the second alkylation reactor serves as the alkylation reaction feed inlet, and the third alkylation reactor or the fourth alkylation reactor serves as the alkylation reaction product outlet.

[0012] Optionally, a first static mixer, a second static mixer, a third static mixer, and a fourth static mixer are respectively provided at the front ends of the inlets of the first alkylation reactor, the second alkylation reactor, the third alkylation reactor, and the fourth alkylation reactor. The alkylation heat exchanger is arranged between the first static mixer and the first alkylation reactor. The outlet of the tube side of the bottom discharge heater of the dehydration tower is divided into three streams of materials. One of them is mixed with recycled benzene, toluene, or alkylbenzene and then connected to the inlet of the tube side of the alkylation heat exchanger. The outlet of the tube side of the alkylation heat exchanger is connected to the inlet of the first alkylation reactor or the second alkylation reactor. The outlet of the first alkylation reactor is connected to the second static mixer, and after being mixed with a stream of material from the outlet of the tube side of the bottom discharge heater of the dehydration tower, it is connected to the inlet of the second alkylation reactor. The outlet of the second alkylation reactor is connected to the third static mixer, and after being mixed with a stream of material from the outlet of the tube side of the bottom discharge heater of the dehydration tower, it is connected to the inlet of the third alkylation reactor. The outlet of the third alkylation reactor is connected to the fourth static mixer, and after being mixed with a stream of material from the outlet of the tube side of the bottom discharge heater of the dehydration tower, it is connected to the inlet of the fourth alkylation reactor. The outlet of the third alkylation reactor or the fourth alkylation reactor is connected to the inlet of the shell side of the alkylation heat exchanger.

[0013] Optionally, it further includes a deoxygenation reactor for deoxygenating the first reaction raw material. The first reaction raw material is mixed with hydrogen and then connected to the inlet of the deoxygenation reactor. The outlet of the deoxygenation reactor is connected to the dehydration tower.

[0014] Optionally, it further includes a de-alcohol preheater, a de-alcohol heater, and a de-alcohol reactor. The outlet of the deoxygenation reactor is connected to the inlet of the tube side of the de-alcohol preheater. The outlet of the tube side of the de-alcohol preheater is connected to the tube side of the de-alcohol heater. The outlet of the tube side of the de-alcohol heater is connected to the de-alcohol reactor. The outlet of the de-alcohol reactor is connected to the shell side of the de-alcohol preheater for cooling. The outlet of the shell side of the de-alcohol preheater is connected to the dehydration tower.

[0015] Optionally, it further includes a circulating benzene booster pump and an alkane-benzene mixing tank. The material taken from the side line at the top of the benzene stripper is divided into multiple streams by the circulating benzene pump. One of the streams enters the alkane-benzene mixing tank, mixes with the heated alkane feed, and then enters the circulating benzene booster pump. The outlet of the circulating benzene booster pump is connected to the first static mixer.

[0016] In summary, the present application includes at least one of the following beneficial effects: 1. The present invention is designed according to the characteristics of the alkylbenzene synthesis process, with the characteristics of short process flow, continuous operation, stable operation, comprehensive heat recovery and utilization, low energy consumption, low corrosion, low toxicity, large operation flexibility, and diversified production.

[0017] 2. The present invention can produce different varieties of alkylbenzene products using different raw materials in the same set of equipment, and can achieve diversified continuous production.

[0018] 3. All the reactors adopted in the present invention are fixed-bed reactors, and the reaction processes are all liquid-solid heterogeneous reactions. The reaction conditions are mild, the product yield is high, there are no by-products, the material separation is simple, the process flow is short, it can be continuously operated, the operation is stable, the energy consumption is low, the corrosion is small, and the toxicity is small.

[0019] 4. The operation mode of the alkylbenzene reactor adopted in the present invention is three in operation and one in standby, and each reactor can be switched to work, which is convenient for loading and replacing the catalyst; and the flow rates of the circulating benzene, circulating toluene, and circulating alkylbenzene are small, so the operation loads of the benzene stripper and the light ends stripper are small, and the energy consumption is low.

[0020] 5. The benzene stripper of the present invention adopts an integrated structure, with an internal condenser and a reboiler. It can be operated under positive pressure or negative pressure, without a reflux drum, the number of equipment is small, the equipment investment is reduced, and the floor area is small.

[0021] 6. The present invention uses a hydraulic turbine to recover the residual pressure of the alkylation reaction as one of the energy sources of the circulating benzene booster pump, recovering the energy, reducing both the energy consumption of the circulating benzene booster pump and the pressure rating of the subsequent pipeline, making the operation process stable, safe and energy-saving.

[0022] 7. The process of heating the circulating benzene in the present invention adopts the process of preheating the circulating benzene first and then boosting the pressure, and then recovering the heat at the top of the heavy ends stripper. This process will not cause safety risks such as pipeline vibration and pipeline leakage due to the formation of a gas-liquid two-phase flow after the circulating benzene is heated and vaporized, and is inherently safe, reliable and stable.

[0023] 8. The present invention uses the waste heat of the alkylation reaction as the heat source of the dehydrator reboiler, which not only makes the operation of the downstream benzene stripper stable, but also reduces the heat load requirement of the dehydrator reboiler and reduces the energy consumption.

[0024] 9. The present invention fully utilizes the reaction waste heat and the waste heat of the high-temperature rectification column for energy recovery, reduces the heat required for reaction heating, reduces the rectification cooling load and heating load, and by-produces heating hot water, achieving the maximum utilization of heat, with simple operation and low comprehensive energy consumption. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] Figure 1 is a schematic perspective view of a multifunctional alkylbenzene production system according to an embodiment of the present application.

[0026] BRIEF DESCRIPTION OF THE DRAWINGS: 1. Alkylbenzene cooler; 2. Deoxygenation preheater; 3. Fifth static mixer; 4. Deoxygenation reactor; 5. Dealcoholization reactor; 6. Dealcoholization preheater; 7. Dealcoholization heater; 8. Benzene heater; 9. Dehydration tower; 10. Dehydration tower top condenser; 11. Dehydration tower reflux liquid separation tank; 12. Dehydration tower reflux pump; 13. Second reboiler; 14. First reboiler; 15. Dehydration tower bottom output pump; 16. Dehydration tower bottom discharge heater; 17. First static mixer; 18. Second static mixer; 19. Third static mixer; 20. Fourth static mixer; 21. Alkylation heat exchanger; 22. First alkylation reactor; 23. Second alkylation reactor; 24. Third alkylation reactor; 25. Fourth alkylation reactor; 26. Circulating benzene booster pump; 27. Hydraulic turbine; 28. Alkane-benzene mixing tank; 29. Alkane heat exchanger; 30. Debenzylation tower; 31. Debenzylation tower built-in reboiler; 32. Debenzylation tower top cooler; 33. Circulating benzene pump; 34. Debenzylation tail gas condenser; 35. Debenzylation tower bottom transfer pump; 36. Light fraction removal tower; 37. Light fraction removal tower top partial condenser; 38. Light fraction removal tail gas condenser; 39. Light fraction removal tower top cooler; 40. Light fraction removal circulating pump; 41. Light fraction removal tower built-in reboiler; 42. Light fraction removal tower bottom transfer pump; 43. Light fraction removal tower middle post-heater; 44. Light fraction removal tower middle heater; 45. Heavy fraction removal tower; 46. Heavy fraction removal tower top cooler; 47. Alkylbenzene transfer pump; 48. Heavy fraction removal tower built-in reboiler; 49. Heavy alkylbenzene transfer pump; 50. Heavy fraction removal tail gas condenser; 51. Heavy alkylbenzene cooler; 101. First reaction raw material; 102. Hydrogen; 103. Second reaction raw material; 104. Dehydrated alkylation reaction feed; 105. One of the three dehydrated alkylation reaction feeds; 106. Alkylation reaction product; 107. Alkylation reaction product at the outlet of the hydraulic turbine; 108. Alkane feed; 109. Circulating alkylbenzene; 110. Circulating benzene or circulating toluene; 111. Alkylation product after debenzylation; 112. Dialkylbenzene; 113. Light fraction removal tower bottom discharge; 114. Alkylbenzene; 115. Heavy alkylbenzene; 116. Alkane discharge; 117. Cold water inlet; 118. Hot water for external supply. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0027] The following will be combined withFigure 1 A detailed description is given of the multifunctional alkylbenzene production system of the present application.

[0028] An embodiment of the present application provides a multifunctional alkylbenzene production system, which generally includes a deoxidation reactor 4, a dealcoholization reactor 5, a dehydration tower 9, an alkylation reaction device 22-25, a hydraulic turbine 27, a debenzene tower 30, a light fractionation tower 36, and a heavy fractionation tower 45.

[0029] Olefins or Fischer-Tropsch oil are fed into the tube-side inlet of the deoxidation preheater 2 as reaction raw material 101. The deoxidation preheater 2 preheats the reaction raw material 101 using the waste heat of the product alkylbenzene 114 or dialkylbenzene 112. The deoxidation preheater 2 is connected with a raw material olefin or Fischer-Tropsch oil pipe 101 and a dialkylbenzene line 112 or an alkylbenzene line 114. The tube-side outlet of the deoxidation preheater 2 is connected to the inlet of the fifth static mixer 3. The reaction raw material 101 is fully mixed with hydrogen 102 in the fifth static mixer 3. The outlet of the fifth static mixer 3 is connected to the fixed-bed deoxidation reactor 4. The outlet of the deoxidation reactor 4 can be connected to the tube-side inlet of the dealcoholization preheater 6 or the middle and lower part of the dehydration tower 9.

[0030] The deoxidation reactor 4 is filled with a solid catalyst. The outlet of the deoxidation reactor 4 is connected to the tube-side inlet of the dealcoholization preheater 6. The dealcoholization preheater 6 uses the waste heat of the dealcoholization reaction to heat the dealcoholization reaction feed. The tube-side outlet of the dealcoholization preheater 6 is connected to the tube-side of the dealcoholization heater 7. The dealcoholization heater 7 provides heat for vaporizing the dealcoholization reaction feed. The tube-side outlet of the dealcoholization heater 7 is connected to the fixed-bed dealcoholization reactor 5. The dealcoholization reactor 5 is filled with a solid catalyst. The outlet of the dealcoholization reactor 5 is connected to the shell-side of the dealcoholization preheater 6 for cooling.

[0031] The shell-side outlet of the dealcoholization preheater 6 is connected to the middle and lower part of the dehydration tower 9. The top of the dehydration tower 9 is connected to the tube-side inlet of the dehydration tower top condenser 10. The tube-side outlet of the dehydration tower top condenser 10 is connected to the dehydration tower reflux and liquid separation tank 11. Free water is separated from the bottom water collection package of the dehydration tower reflux and liquid separation tank 11. The tail gas separated from the top of the dehydration tower reflux and liquid separation tank 11 is connected to the tail gas treatment system. The outlet of the dehydration tower reflux and liquid separation tank 11 is connected to the dehydration tower reflux pump 12. The outlet of the dehydration tower reflux pump 12 returns to the top of the dehydration tower 9. Benzene, toluene, or alkylbenzene is fed into the tube-side inlet of the benzene heater 8 as reaction raw material 103. The tube-side outlet of the benzene heater 8 is connected to the outlet pipeline of the dehydration tower reflux pump 12. The benzene heater 8 is connected with a raw material benzene, toluene, or alkylbenzene line 103 and a dialkylbenzene line 112 or an alkylbenzene line 114.

[0032] The bottom of the dehydration tower 9 is provided with a first reboiler 14 and a second reboiler 13 to provide heat for vaporizing the liquid in the bottom of the dehydration tower 9. The tube side of the second reboiler 13 is connected to an external heat medium, and the shell side is connected to the dehydration tower 9; the first reboiler 14 uses the waste heat of the alkylation reaction to heat the liquid in the bottom, its tube side is connected to the outlet of the shell side of the alkylation heat exchanger 21, and the shell side is connected to the dehydration tower 9. The alkylation reaction product 106 is led out from the first reboiler 14. The bottom of the dehydration tower 9 is connected to the inlet of the bottom output pump 15 of the dehydration tower.

[0033] In some embodiments of the present invention, the outlet of the bottom output pump 15 of the dehydration tower is connected to the inlet of the tube side of the bottom discharge heater 16 of the dehydration tower. The bottom discharge heater 16 of the dehydration tower uses the waste heat of the product alkylbenzene 114 to heat the alkylation reaction feed 104 after dehydration. The bottom discharge heater 16 of the dehydration tower leads out one of the three feeds of the alkylation reaction after dehydration 105 and the di-alkylbenzene line 112 or the alkylbenzene line 114. The outlet of the tube side of the bottom discharge heater 16 of the dehydration tower is divided into three streams, which are respectively connected to three of the first static mixer 17, the second static mixer 18, the third static mixer 19 or the fourth static mixer 20.

[0034] In some embodiments of the present invention, the outlet of the bottom output pump 15 of the dehydration tower is directly divided into three streams, which are respectively connected to three of the first static mixer 17, the second static mixer 18, the third static mixer 19 or the fourth static mixer 20.

[0035] One of the three feeds for the alkylation reaction after dehydration, 105, is mixed with recycled benzene, toluene, or alkylbenzene in the first static mixer 17 and then enters the inlet of the tube side of the alkylation heat exchanger 21. The alkylation heat exchanger 21 uses the waste heat of the alkylation reaction to heat the feed. The outlet of the tube side of the alkylation heat exchanger 21 is connected to the inlet of the first alkylation reactor 22 or the inlet of the second alkylation reactor 23. The outlet of the first alkylation reactor 22 is connected to the second static mixer 18, where it is mixed with one of the three feeds for the alkylation reaction after dehydration, 105, and then enters the inlet of the second alkylation reactor 23; the outlet of the second alkylation reactor 23 is connected to the third static mixer 19, where it is mixed with one of the three feeds for the alkylation reaction after dehydration, 105, and then enters the inlet of the third alkylation reactor 24; the outlet of the third alkylation reactor 24 is connected to the fourth static mixer 20, where it is mixed with one of the three feeds for the alkylation reaction after dehydration, 105, and then enters the inlet of the fourth alkylation reactor 25. The first, second, third, and fourth alkylation reactors 22 - 25 are fixed-bed reactors, and solid acid alkylation reaction catalysts are installed in the alkylation reactors 22 - 25. The outlet of the third alkylation reactor 24 or the outlet of the fourth alkylation reactor 25 is connected to the inlet of the shell side of the alkylation heat exchanger 21; the outlet of the shell side of the alkylation heat exchanger 21 is connected to the inlet of the tube side of the first reboiler 14 of the dehydration tower 9. The outlet of the tube side of the first reboiler 14 is connected to the hydraulic turbine 27, and the hydraulic turbine 27 is used for the pressure recovery and utilization of the alkylation reaction and serves as one of the energy sources for the recycled benzene booster pump 26. The outlet of the hydraulic turbine 27 can be connected to the debenzene tower 30 or the light ends removal tower 36.

[0036] In some embodiments of the present invention, the debenzene tower 30 is connected from the outlet of the hydraulic turbine 27. An in-built condenser is provided at the top of the debenzene tower 30. The outlet of the in-built condenser at the top of the tower is connected to the inlet of the tube side of the debenzene off-gas condenser 34. The condensate from the tube side of the debenzene off-gas condenser 34 is connected to the underground waste oil collection tank, and the non-condensable gas from the tube side of the debenzene off-gas condenser 34 is connected to the off-gas treatment system. The top side line of the debenzene tower 30 is connected to the inlet of the recycled benzene pump 33; the outlet of the recycled benzene pump 33 is divided into three streams. One stream is connected to the inlet of the tube side of the debenzene tower top cooler 32, and the outlet of the tube side of the debenzene tower top cooler 32 is connected to the top of the in-built condenser; one stream is connected to the inlet of the tube side of the light ends removal tower top cooler 39, and the outlet of the tube side of the light ends removal tower top cooler 39 is connected to the inlet of the alkane-benzene mixing tank 28, where it is mixed with the alkane feed 108 coming from the outlet of the tube side of the alkane heat exchanger 29 and then enters the inlet of the recycled benzene booster pump 26. The outlet of the recycled benzene booster pump 26 is connected to the inlet of the tube side of the heavy ends removal tower top cooler 46, and the outlet of the tube side of the heavy ends removal tower top cooler 46 is connected to the first static mixer 17; the other stream returns and is connected to the debenzene tower 30. The debenzene tower 30 uses the in-built debenzene tower in-built reboiler 31. The bottom outlet of the debenzene tower 30 is connected to the inlet of the debenzene tower bottom transfer pump 35. The outlet of the debenzene tower bottom transfer pump 35 is connected to the middle of the light ends removal tower 36.

[0037] In some embodiments of the present invention, the benzene stripper 30 can also be connected at the outlet of the light ends column bottom transfer pump 42. An in-built condenser is provided at the top of the benzene stripper 30, and the outlet of the in-built condenser at the top of the benzene stripper is connected to the tube side of the benzene off-gas condenser 34. The condensate of the tube side of the benzene off-gas condenser 34 is connected to the underground waste oil collection tank, and the non-condensable gas of the tube side of the benzene off-gas condenser 34 is connected to the inlet of the vacuum pump. The outlet of the vacuum pump is connected to the tail gas treatment system. The top side line of the benzene stripper 30 is connected to the inlet of the circulating benzene pump 33; the outlet of the circulating benzene pump 33 is divided into three streams. One stream is connected to the inlet of the tube side of the benzene stripper top cooler 32, and the outlet of the tube side of the benzene stripper top cooler 32 is connected to the top of the in-built condenser. One stream is connected to the inlet of the shell side of the dewatering column bottom discharge heater 16, and the outlet of the shell side of the dewatering column bottom discharge heater 16 is connected to the inlet of the paraffin benzene mixing tank 28. The outlet of the paraffin benzene mixing tank 28 is connected to the inlet of the circulating benzene booster pump 26, and the outlet of the circulating benzene booster pump 26 is connected to the first static mixer 17; the other stream returns to the benzene stripper 30. The benzene stripper 30 uses an in-built benzene stripper in-built reboiler 31. The bottom outlet of the benzene stripper 30 is connected to the inlet of the benzene stripper bottom transfer pump 35. The outlet of the benzene stripper bottom transfer pump 35 is connected to the inlet of the shell side of the light ends column middle post-heater 43. The outlet of the shell side of the light ends column middle post-heater 43 is connected to the inlet of the shell side of the dewatering column bottom discharge heater 16. The outlet of the shell side of the dewatering column bottom discharge heater 16 is connected to the inlet of the shell side of the benzene heater 8. The outlet of the shell side of the benzene heater 8 is connected to the inlet of the shell side of the deoxidation preheater 2. The outlet of the shell side of the deoxidation preheater 2 is connected to the inlet of the shell side of the alkyl benzene cooler 1. The outlet of the shell side of the alkyl benzene cooler 1 is connected to the off-site piping system.

[0038] In some embodiments of the present invention, the light component removal column 36 is connected to the outlet of the benzol removal column bottom transfer pump 35. A top condenser 37 of the light component removal column 36 is provided at the top of the light component removal column 36. The outlet of the top condenser 37 of the light component removal column 36 is connected to the tube side of the light off-gas condenser 38. The condensate of the tube side of the light off-gas condenser 38 is connected to the underground waste oil collection tank. The non-condensable gas of the tube side of the light off-gas condenser 38 is connected to the inlet of the vacuum pump. The outlet of the vacuum pump is connected to the tail gas treatment system. The side stream extraction of the light component removal column 36 is connected to the inlet of the light component recycle pump 40. The outlet of the light component recycle pump 40 is divided into three streams. One stream is connected to the inlet of the shell side of the top cooler 39 of the light component removal column. The outlet of the shell side of the top cooler 39 of the light component removal column is connected to the light component removal column 36. One stream is connected to the inlet of the shell side of the alkane heat exchanger 29. The outlet of the shell side of the alkane heat exchanger 29 is connected to the off-site pipe system. Another stream is connected to the inlet of the tube side of the middle heater 44 of the light component removal column. The outlet of the tube side of the middle heater 44 of the light component removal column is connected to the inlet of the tube side of the post-middle heater 43 of the light component removal column. The outlet of the tube side of the post-middle heater 43 of the light component removal column is connected to the light component removal column 36. The middle heater 44 of the light component removal column uses the waste heat of the product alkylbenzene 114 to heat the circulating material of the light component removal column 36. The post-middle heater 43 of the light component removal column uses the waste heat of the product heavy alkylbenzene 115 to heat the circulating material of the light component removal column 36, so as to reduce the heating load required at the bottom of the light component removal column 36 and lower the temperatures of the product alkylbenzene 114 and heavy alkylbenzene 115, and comprehensively recover and utilize the heat of the system. The light component removal column 36 is equipped with an in-built reboiler 41. The bottom of the light component removal column 36 is connected to the inlet of the light component removal column bottom transfer pump 42. The outlet of the light component removal column bottom transfer pump 42 is connected to the heavy component removal column 45.

[0039] In some embodiments of the present invention, the light component removal column 36 is connected to the outlet of the hydraulic turbine 27. A top condenser 37 of the light component removal column 36 is provided at the top of the light component removal column 36. The outlet of the top condenser 37 of the light component removal column 36 is connected to the tube side of the light off-gas condenser 38. The condensate of the tube side of the light off-gas condenser 38 is connected to the underground waste oil collection tank. The non-condensable gas of the tube side of the light off-gas condenser 38 is connected to the inlet of the vacuum pump. The outlet of the vacuum pump is connected to the tail gas treatment system. The side stream extraction of the light component removal column 36 is connected to the inlet of the light component recycle pump 40. The outlet of the light component recycle pump 40 is divided into two streams. One stream is connected to the inlet of the shell side of the alkane heat exchanger 29. The outlet of the shell side of the alkane heat exchanger 29 is connected to the off-site pipe system. Another stream is connected to the inlet of the tube side of the post-middle heater 43 of the light component removal column. The outlet of the tube side of the post-middle heater 43 of the light component removal column is connected to the light component removal column 36. The post-middle heater 43 of the light component removal column uses the waste heat of the product dialkylbenzene 112 to heat the circulating material of the light component removal column 36, so as to reduce the heating load required at the bottom of the light component removal column 36 and lower the temperature of the product dialkylbenzene, and comprehensively recover and utilize the heat of the system. The light component removal column 36 is equipped with an in-built reboiler 41. The bottom of the light component removal column 36 is connected to the inlet of the light component removal column bottom transfer pump 42. The outlet of the light component removal column bottom transfer pump 42 is divided into two streams. One stream is connected to the inlet of the benzol removal column 3, and one stream is connected to the inlet of the heavy component removal column 45.

[0040] In some embodiments of the present invention, the outlet of the light - end tower bottom transfer pump 42 is connected to the middle part of the heavy - end tower 45. An in - built condenser is provided at the top of the heavy - end tower 45. The outlet of the in - built condenser at the top of the tower is connected to the tube side of the heavy - end tail gas condenser 50. The condensate of the tube side of the heavy - end tail gas condenser 50 is connected to the underground dirty oil collection tank, and the non - condensable gas of the tube side of the heavy - end tail gas condenser 50 is connected to the inlet of the vacuum pump. The outlet of the vacuum pump is connected to the tail gas treatment system. The top side line of the heavy - end tower 45 is connected to the inlet of the alkylbenzene transfer pump 47; the outlet of the alkylbenzene transfer pump 47 is divided into three streams. One stream is connected to the inlet of the shell side of the heavy - end tower top cooler 46, and the outlet of the shell side of the heavy - end tower top cooler 46 is connected to the top of the in - built condenser; one stream is connected to the inlet of the shell side of the middle heater 44 of the light - end tower, the outlet of the shell side of the middle heater 44 of the light - end tower is connected to the inlet of the shell side of the bottom discharge heater 16 of the dehydration tower, the outlet of the shell side of the bottom discharge heater 16 of the dehydration tower is connected to the inlet of the shell side of the benzene heater 8, the outlet of the shell side of the benzene heater 8 is connected to the inlet of the shell side of the deoxidation pre - heater 2, the outlet of the shell side of the deoxidation pre - heater 2 is connected to the inlet of the shell side of the alkylbenzene cooler 1, and the outlet of the shell side of the alkylbenzene cooler 1 is connected to the off - site pipe system; the other stream is returned and connected to the heavy - end tower 45. The heavy - end tower 45 adopts an in - built heavy - end tower in - built reboiler 48. The bottom of the heavy - end tower 45 is connected to the inlet of the heavy alkylbenzene transfer pump 49, the outlet of the heavy alkylbenzene transfer pump 49 is connected to the inlet of the shell side of the middle post - heater 43 of the light - end tower, the outlet of the shell side of the middle post - heater 43 of the light - end tower is connected to the inlet of the shell side of the heavy alkylbenzene cooler 51, and the outlet of the shell side of the heavy alkylbenzene cooler 51 is connected to the off - site pipe system.

[0041] In some embodiments of the present invention, the outlet of the light - component removal tower bottom transfer pump 42 is connected to the middle part of the heavy - component removal tower 45. An in - built condenser is provided at the top of the heavy - component removal tower 45. The outlet of the in - built condenser at the top of the tower is connected to the tube side of the heavy - component removal tail gas condenser 50. The condensate of the tube side of the heavy - component removal tail gas condenser 50 is connected to the underground dirty oil collection tank. The non - condensable gas at the bottom of the tube side of the heavy - component removal tail gas condenser 50 is connected to the inlet of the vacuum pump, and the outlet of the vacuum pump is connected to the tail gas treatment system. The top side line of the heavy - component removal tower 45 is connected to the inlet of the alkylbenzene transfer pump 47; the outlet of the alkylbenzene transfer pump 47 is divided into three streams. One stream is connected to the inlet of the shell side of the heavy - component removal tower top cooler 46, and the outlet of the shell side of the heavy - component removal tower top cooler 46 is connected to the top of the in - built condenser; one stream is connected to the inlet of the shell side of the dehydration tower bottom discharge heater 16, the outlet of the shell side of the dehydration tower bottom discharge heater 16 is connected to the inlet of the alkane - benzene mixing tank 28, the outlet of the alkane - benzene mixing tank 28 is connected to the inlet of the circulating benzene booster pump 26, and the outlet of the circulating benzene booster pump 26 is connected to the first static mixer 17; one stream returns to the heavy - component removal tower 45. The heavy - component removal tower 45 uses an in - built heavy - component removal tower in - built reboiler 48. The bottom outlet of the heavy - component removal tower 45 is connected to the inlet of the heavy alkylbenzene transfer pump 49. The outlet of the heavy alkylbenzene transfer pump 49 is connected to the inlet of the shell side of the after - heater 43 in the middle of the light - component removal tower. The outlet of the shell side of the after - heater 43 in the middle of the light - component removal tower is connected to the inlet of the tube side of the dehydration tower bottom discharge heater 16. The outlet of the tube side of the dehydration tower bottom discharge heater 16 is connected to the inlet of the shell side of the benzene heater 8. The outlet of the shell side of the benzene heater 8 is connected to the inlet of the shell side of the deoxidation pre - heater 2. The outlet of the shell side of the deoxidation pre - heater 2 is connected to the inlet of the shell side of the alkylbenzene cooler 1. The outlet of the shell side of the alkylbenzene cooler 1 is connected to the off - site piping system.

[0042] In some embodiments of the present invention, the cold water inlet 117 is connected to the inlet of the tube side of the alkylbenzene cooler 1. The outlet of the tube side of the alkylbenzene cooler 1 is connected to the inlet of the tube side of the heavy alkylbenzene cooler 51. The outlet of the tube side of the heavy alkylbenzene cooler 51 is connected to the inlet of the shell side of the light - component removal tower top partial condenser 37. The outlet of the shell side of the light - component removal tower top partial condenser 37 is connected to the piping system of the hot water supply 118.

[0043] In some embodiments of the present invention, the cold water inlet 117 is connected to the inlet of the tube side of the alkylbenzene cooler 1. The outlet of the tube side of the alkylbenzene cooler 1 is connected to the inlet of the shell side of the light - component removal tower top partial condenser 37. The outlet of the shell side of the light - component removal tower top partial condenser 37 is connected to the inlet of the tube side of the heavy - component removal tower top cooler 46. The outlet of the tube side of the heavy - component removal tower top cooler 46 is connected to the piping system of the hot water supply 118.

[0044] The present invention will be further described below in conjunction with specific embodiments.

[0045] Example 1 See Figure 1This embodiment provides a multifunctional alkylbenzene production system using a solid acid catalyst, comprising a deoxygenation reactor 4, a dealcoholization reactor 5, a dehydration tower 9, alkylation reactors 22-25, a hydraulic turbine 27, a debenzenization tower 30, a light-removal tower 36, and a heavy-removal tower 45. Taking 25,000 tons / year of C12 alkylbenzene production as an example, the specific solution is as follows: C12 normal or isoolefin feedstock 101, at room temperature, 0.8 MPa pressure, and a flow rate of 2218 kg / h, is preheated to 75-85°C in deoxygenation preheater 2. It is then thoroughly mixed with hydrogen 102 at room temperature, 0.8 MPa pressure, and a flow rate of 0.8 kg / h in a fifth static mixer 3 before entering deoxygenation reactor 4. The material at the outlet of deoxygenation reactor 4 enters dehydration tower 9. Benzene feedstock 103, at room temperature, 0.3 MPa pressure, and a flow rate of 1041 kg / h, is heated to 75-85°C in benzene heater 8 and then fed into the outlet pipeline of dehydration tower reflux pump 12, where it enters dehydration tower 9. The dehydration tower 9 operates at atmospheric pressure. The overhead vapor enters the dehydration tower overhead condenser 10, where it is condensed and cooled to 40-55°C before entering the dehydration tower reflux separator 11. Free water is separated and removed in a water collection drum. The tail gas is transported from the tank overhead to the tail gas treatment facility, and the reflux liquid is returned to the dehydration tower 9 via the dehydration tower reflux pump 12. The second reboiler 13 of the dehydration tower 9 is heated by an external heat source, while the first reboiler 14 of the dehydration tower 9 is heated by the waste heat of the alkylation product. After dehydration, the alkylation reaction feed 104 is pressurized to 3.9-4.5 MPa by the dehydration tower bottom outlet pump 15, then heated to 130-150°C by the dehydration tower bottom outlet heater 16. The feed is then divided into three streams and enters the first static mixer 17, the second inlet static mixer 18, the third static mixer 19, or the fourth static mixer 20, respectively.

[0046] After dehydration, one of the three feed streams 105 of the alkylation reaction is thoroughly mixed with the recycle benzene 110 from the recycle benzene booster pump 26 in the first static mixer 17. The feed then enters the alkylation heat exchanger 21, where it is heated to 180-240°C. It then enters the first alkylation reactor 22 or the second alkylation reactor 23. After the three-stage series alkylation reaction, the alkylation reaction product 106 exiting the third alkylation reactor 24 or the fourth alkylation reactor 25 is cooled to 175-190°C via the alkylation heat exchanger 21. The product enters the first reboiler 14 of the dehydration tower 9, where it continues to cool to 155-175°C. The product is then depressurized to 0.7-0.5 MPa in the hydraulic turbine 27 to obtain the hydraulic turbine outlet alkylation product 107, which then enters the debenzene tower 30.

[0047] The debenzolization column 30 operates at atmospheric pressure. The material taken out from the side line at the top of the column is divided into three streams by the circulating benzene pump 33. One stream is cooled to 40 - 55°C by the cooler 32 at the top of the debenzolization column and then returns to the top of the in-column condenser of the debenzolization column 30. The tail gas at the top of the debenzolization column 30 is condensed and cooled by the debenzolization tail gas condenser 34 and then enters the tail gas treatment facility. One stream of circulating benzene 110 is heated to 85 - 95°C by the cooler 39 at the top of the light component removal column and then enters the paraffin-benzene mixing tank 28, where it is mixed with the paraffin feed 108 with a temperature of about 95 - 110°C and a flow rate of 1000 kg / h after heat exchange. Then, they enter the circulating benzene booster pump 26 together, are pressurized to 3.9 - 4.5 MPa, enter the cooler 46 at the top of the heavy component removal column, are heated to 140 - 160°C, and then enter the first static mixer 17, where they converge with one of the three feeds of the alkylation reaction after dehydration, 105, in the first static mixer 17. One stream returns to the debenzolization column 30. The in-column reboiler 31 of the debenzolization column is heated by an external heat source. The alkylated product 111 after debenzolization is transported to the middle of the light component removal column 36 by the transfer pump 35 at the bottom of the debenzolization column.

[0048] The light component removal column 36 operates under negative pressure with an operating pressure of 5 - 9 kPa. The side line draw of the light component removal column 36 is divided into three streams by the light component recycle pump 40. One stream is cooled to 90 - 100°C by the cooler 39 at the top of the light component removal column and then enters below the top partial condenser 37 of the light component removal column. One stream of paraffin product 116 with a flow rate of 1000 kg / h is cooled by the paraffin heat exchanger 29 and then transported to other unit areas. One stream is heated to 125 - 140°C by the middle heater 44 and the post-middle heater 43 of the light component removal column and then enters the light component removal column 36. The cold water inlet 117 is heated to 30 - 40°C by the alkylbenzene cooler 1, then continues to exchange heat in the heavy alkylbenzene cooler 51, enters the top partial condenser 37 of the light component removal column, is heated to 90 - 95°C, and then the hot water is supplied externally 118. The tail gas at the outlet of the top partial condenser 37 of the light component removal column is condensed and cooled by the light component tail gas condenser 38 and then enters the vacuum pump. The air discharged from the vacuum pump goes to the tail gas treatment system. The in-column reboiler 41 of the light component removal column is heated by an external heat source. The bottom draw 113 of the light component removal column is transported to the middle of the heavy component removal column 45 by the transfer pump 42 at the bottom of the light component removal column.

[0049] The de-weighting tower 45 operates under negative pressure, with an operating pressure of 1-3 kPa. The side stream from the de-weighting tower 45 is divided into three streams via an alkylbenzene transfer pump 47. One stream is cooled to 90-115°C via a de-weighting tower overhead cooler 46 and returned to the top of the de-weighting tower 45. The exhaust gas from the de-weighting tower 45 is condensed and cooled in a de-weighting tower exhaust condenser 50 before entering a vacuum pump and entering the exhaust gas treatment system. One stream returns to the de-weighting tower 45. The other stream, alkylbenzene 114, passes through a light de-weighting tower mid-heater 44, a dehydration tower bottom discharge heater 16, a benzene heater 8, a deoxidation preheater 2, and an alkylbenzene cooler 1, where it is cooled to 50°C, producing 3183 kg / h of product. The de-weighting tower's internal reboiler 48 is heated by an external heat source. Heavy alkylbenzene 115 is transferred via a heavy alkylbenzene transfer pump 49 to a light de-weighting tower mid-postheater 43 and a heavy alkylbenzene cooler 51, where it is cooled to 80°C, producing 70 kg / h of heavy alkylbenzene product.

[0050] Example 2 See also Figure 1 This embodiment provides a multifunctional alkylbenzene production system using a solid acid catalyst, comprising a deoxygenation reactor 4, a dealcoholization reactor 5, a dehydration tower 9, alkylation reactors 22-25, a hydraulic turbine 27, a debenzenization tower 30, a light-removal tower 36, and a heavy-removal tower 45. Taking 25,000 tons / year of C16 alkylbenzene production as an example, the specific solution is as follows: C16 normal or isoolefin feedstock 101, at room temperature, 0.8 MPa pressure, and a flow rate of 2261 kg / h, is preheated to 75-85°C in deoxygenation preheater 2. It is then thoroughly mixed with hydrogen 102 at room temperature, 0.8 MPa pressure, and a flow rate of 0.9 kg / h in a fifth static mixer 3 before entering deoxygenation reactor 4. The outlet of deoxygenation reactor 4 enters dehydration tower 9. Toluene feedstock 103, at room temperature, 0.3 MPa pressure, and a flow rate of 933 kg / h, is heated to 85-100°C in benzene heater 8 and then fed into the outlet pipeline of dehydration tower reflux pump 12, where it enters dehydration tower 9. The dehydration tower 9 operates at atmospheric pressure. The overhead vapor enters the dehydration tower overhead condenser 10, where it is condensed and cooled to 40-55°C before entering the dehydration tower reflux separator 11. Free water is separated and removed in a water collection drum. The tail gas is transported from the tank overhead to the tail gas treatment facility, and the reflux liquid is returned to the dehydration tower 9 via the dehydration tower reflux pump 12. The second reboiler 13 of the dehydration tower 9 is heated by an external heat source, while the first reboiler 14 of the dehydration tower 9 is heated by the waste heat of the alkylation product. After dehydration, the alkylation reaction feed 104 is pressurized to 3.9-4.5 MPa by the dehydration tower bottom discharge pump 15, then heated to 165-190°C by the dehydration tower bottom discharge heater 16. The feed is then divided into three streams and enters the first static mixer 17, the second static mixer 18, the third static mixer 19, or the fourth static mixer 20, respectively.

[0051] One of the three feeds of the alkylation reaction after dehydration, 105, is fully mixed with the recycled toluene 110 from the recycled benzene booster pump 26 in the first static mixer 17, and then enters the alkylation heat exchanger 21 to be heated to 210 - 240 °C, and then enters the first alkylation reactor 22 or the second alkylation reactor 23. After three-stage series alkylation reaction, the alkylation reaction product 106 coming out from the third alkylation reactor 24 or the fourth alkylation reactor 25 is cooled to 195 - 215 °C by heat exchange in the alkylation heat exchanger 21 and enters the first reboiler 14 of the dehydration tower 9, and is further cooled to 180 - 195 °C, and then is depressurized to 0.7 - 0.5 Mpa by the hydraulic turbine 27 to obtain the alkylation reaction product 107 at the outlet of the hydraulic turbine and then enters the debenzene tower 30.

[0052] The debenzene tower 30 operates at atmospheric pressure. The material taken from the top side line of the tower is divided into three streams by the recycled benzene pump 33. One stream is cooled to 40 - 55 °C by the debenzene tower top cooler 32 and returns to the top of the built-in condenser of the debenzene tower 30. The tail gas at the top of the debenzene tower 30 is condensed and cooled by the debenzene tail gas condenser 34 and then enters the tail gas treatment facility; one stream of recycled toluene 110 is heated to 115 - 125 °C by the de-light tower top cooler 39 and then enters the alkane-benzene mixing tank 28, where it is mixed with the alkane feed 108 with a temperature of about 95 - 110 °C and a flow rate of 1000 kg / h after heat exchange, and then enters the recycled benzene booster pump 26 together, is pressurized to 3.9 - 4.5 MPa, and then enters the de-heavy tower top cooler 46, where it is heated to 165 - 175 °C, and then enters the first mixer 17 to converge with one of the three feeds of the alkylation reaction after dehydration, 105, in the static mixer 17; one stream returns to the debenzene tower 30. The built-in reboiler 31 of the debenzene tower is heated by an external heat source. The alkylation product 111 after debenzene is transported to the middle of the de-light tower 36 by the debenzene tower bottom transfer pump 35.

[0053] The de-light tower 36 operates under negative pressure, and the operating pressure is 5 - 9 kPa. The side line draw of the de-light tower 36 is divided into three streams by the de-light recycle pump 40. One stream is cooled to 100 - 120 °C by the de-light tower top cooler 39 and then enters below the de-light tower top partial condenser 37; one stream of alkane discharge 116 with a flow rate of 1000 kg / h is cooled by the alkane heat exchanger 29 and then transported to other unit areas; one stream is heated to 130 - 145 °C by the de-light tower middle heater 44 and the de-light tower middle after-heater 43 and then enters the de-light tower 36. The cold water inlet 117 is heated to 30 - 40 °C by the alkylbenzene cooler 1, then enters the heavy alkylbenzene cooler 51 for further heat exchange, and then enters the de-light tower top partial condenser 37 and is heated to 90 - 95 °C and then the hot water is supplied externally 118. The tail gas at the outlet of the de-light tower top partial condenser 37 is condensed and cooled by the de-light tail gas condenser 38 and then enters the vacuum pump, and the air discharged from the vacuum pump goes to the tail gas treatment system. The built-in reboiler 41 of the de-light tower is heated by an external heat source. The bottom discharge 113 of the de-light tower is transported to the middle of the de-heavy tower 45 by the de-light tower bottom transfer pump 42.

[0054] The de-weighting tower 45 operates under negative pressure, with an operating pressure of 1-3 kPa. The side stream from the de-weighting tower 45 is divided into three streams via an alkylbenzene transfer pump 47. One stream is cooled to 155-170°C via the de-weighting tower overhead cooler 46 and returned to the top of the de-weighting tower 45. The overhead off-gas from the de-weighting tower 45 is condensed and cooled in the heavy off-gas condenser 50 before entering a vacuum pump and then the off-gas treatment system. Another stream returns to the de-weighting tower 45. Alkylbenzene 114 is cooled to 50°C via the de-lighting tower mid-heater 44, the dehydration tower bottom discharge heater 16, the benzene heater 8, the deoxidation preheater 2, and the alkylbenzene cooler 1, producing 3125 kg / h of product. The de-weighting tower's internal reboiler 48 is heated by an external heat source. Heavy alkylbenzene 115 is transferred via a heavy alkylbenzene transfer pump 49 to the de-lighting tower mid-post-heater 43 and heavy alkylbenzene cooler 51, where it is cooled to 80°C, producing 64 kg / h of heavy alkylbenzene product.

[0055] Example 3 See also Figure 1 This embodiment provides a multifunctional alkylbenzene production system using a solid acid catalyst, comprising a deoxygenation reactor 4, a dealcoholization reactor 5, a dehydration tower 9, alkylation reactors 22-25, a hydraulic turbine 27, a debenzenization tower 30, a light-removal tower 36, and a heavy-removal tower 45. Taking 25,000 tons / year of C20-C24 alkylbenzene production as an example, the specific solution is as follows: C20-C24 normal or isoolefin feedstock 101, at room temperature, 0.8 MPa pressure, and a flow rate of 2512 kg / h, is preheated to 75-85°C in deoxygenation preheater 2. It is then thoroughly mixed with hydrogen 102 at room temperature, 0.8 MPa pressure, and a flow rate of 1 kg / h in a fifth static mixer 3 before entering deoxygenation reactor 4. The material at the outlet of deoxygenation reactor 4 enters dehydration tower 9. Benzene feedstock 103, at room temperature, 0.3 MPa pressure, and a flow rate of 691 kg / h, is heated to 75-95°C in benzene heater 8 and then fed into the outlet pipeline of dehydration tower reflux pump 12, where it enters dehydration tower 9. The dehydration tower 9 operates at atmospheric pressure. The overhead vapor enters the dehydration tower overhead condenser 10, where it is condensed and cooled to 40-55°C. It then enters the dehydration tower reflux separator 11. Free water is separated and removed in a water collection drum. The tail gas is transported from the tank overhead to the tail gas treatment facility, and the reflux liquid is returned to the dehydration tower 9 via the dehydration tower reflux pump 12. The second reboiler 13 of the dehydration tower 9 is heated by an external heat source, while the first reboiler 14 of the dehydration tower 9 is heated by the waste heat of the alkylation product. After dehydration, the alkylation reaction feed 104 is pressurized to 3.9-4.5 MPa by the dehydration tower bottom discharge pump 15, then heated to 170-190°C by the dehydration tower bottom discharge heater 16. It is then divided into three streams and enters the first static mixer 17, the second static mixer 18, the third static mixer 19, or the fourth static mixer 20, respectively.

[0056] One of the three feeds of the alkylation reaction after dehydration, 105, is fully mixed with the recycled benzene 110 from the recycled benzene booster pump 26 in the first static mixer 17, then enters the alkylation heat exchanger 21 and is heated to 180 - 240 °C, and then enters the first alkylation reactor 22 or the second alkylation reactor 23. After three - stage series alkylation reaction, the alkylation reaction product 106 coming out from the third alkylation reactor 24 or the fourth alkylation reactor 25 is cooled to 195 - 220 °C by heat exchange in the alkylation heat exchanger 21 and enters the first reboiler 14 of the dehydration tower 9, and is further cooled to 160 - 175 °C, and then is depressurized to 0.7 - 0.5 Mpa by the hydraulic turbine 27 to obtain the alkylation reaction product 107 at the outlet of the hydraulic turbine and then enters the debenzene tower 30.

[0057] The debenzene tower 30 operates at atmospheric pressure. The material taken from the top side line of the tower is divided into three streams by the recycled benzene pump 33. One stream is cooled to 40 - 55 °C by the debenzene tower top cooler 32 and returns to the top of the in - tower condenser of the debenzene tower 30. The tail gas at the top of the debenzene tower 30 is condensed and cooled by the debenzene tail gas condenser 34 and then enters the tail gas treatment facility; one stream of recycled benzene 110 is heated to 90 - 100 °C by the de - light tower top cooler 39 and then enters the alkane - benzene mixing tank 28, where it is mixed with the alkane feed 108 with a temperature of about 95 - 110 °C and a flow rate of 1000 kg / h after heat exchange. Then they enter the recycled benzene booster pump 26 together, are pressurized to 3.9 - 4.5 MPa, enter the de - heavy tower top cooler 46, are heated to 190 - 205 °C, and then enter the first static mixer 17, where it converges with one of the three feeds of the alkylation reaction after dehydration, 105, in the first static mixer 17; one stream returns to the debenzene tower 30. The in - tower reboiler 31 of the debenzene tower is heated by an external heat source. The alkylation product 111 after debenzene is transported to the middle of the de - light tower 36 by the debenzene tower bottom transfer pump 35.

[0058] The de - light tower 36 operates under negative pressure, with an operating pressure of 5 - 9 kPa. The side - line product of the de - light tower 36 is divided into three streams by the de - light recycle pump 40. One stream is cooled to 90 - 105 °C by the de - light tower top cooler 39 and then enters below the de - light tower top partial condenser 37; one stream of alkane product 116 with a flow rate of 1000 kg / h is cooled by the alkane heat exchanger 29 and then transported to other plant areas; one stream is heated to 130 - 145 °C by the de - light tower middle heater 44 and the de - light tower middle post - heater 43 and then enters the de - light tower 36. The cold water inlet 117 is heated to 30 - 40 °C by the alkylbenzene cooler 1, then enters the heavy alkylbenzene cooler 51 for further heat exchange, and then enters the de - light tower top partial condenser 37 and is heated to 90 - 95 °C, and then the hot water is supplied externally 118. The tail gas at the outlet of the de - light tower top partial condenser 37 is condensed and cooled by the de - light tail gas condenser 38 and then enters the vacuum pump, and the air discharged from the vacuum pump goes to the tail gas treatment system. The in - tower reboiler 41 of the de - light tower is heated by an external heat source. The bottom material of the tower is transported to the middle of the de - heavy tower 45 by the de - light tower bottom transfer pump 42.

[0059] The de-weighting tower 45 operates under negative pressure, with an operating pressure of 1-3 kPa. The side stream from the de-weighting tower 45 is split into three streams via an alkylbenzene transfer pump 47. One stream is cooled to 150-170°C via a de-weighting tower overhead cooler 46 and then returned to the top of the de-weighting tower 45. The exhaust gas from the de-weighting tower 45 is condensed and cooled in a de-weighting tower exhaust condenser 50 before entering a vacuum pump and entering the exhaust gas treatment system. Another stream returns to the de-weighting tower 45. Alkylbenzene 114 is cooled to 50°C via a de-lighting tower mid-heater 44, a dehydration tower bottom discharge heater 16, a benzene heater 8, a deoxidation preheater 2, and an alkylbenzene cooler 1, producing 3130 kg / h of product. The de-weighting tower's internal reboiler 48 is heated by an external heat source. Heavy alkylbenzene 115 is transferred via a heavy alkylbenzene transfer pump 49 to a de-lighting tower mid-heater 43 and a heavy alkylbenzene cooler 51, where it is cooled to 80°C, producing 57 kg / h of heavy alkylbenzene product.

[0060] Example 4 See also Figure 1 This embodiment provides a multifunctional alkylbenzene production system using a solid acid catalyst, comprising a deoxygenation reactor 4, a dealcoholization reactor 5, a dehydration tower 9, alkylation reactors 22-25, a hydraulic turbine 27, a debenzenization tower 30, a light-removal tower 36, and a heavy-removal tower 45. Taking 20,000 tons / year of C14-C18 alkylbenzene production as an example, the specific solution is as follows: The raw material Fischer-Tropsch oil 101 at room temperature, pressure of 0.8 MPa, and flow rate of 3023 kg / h is preheated to 75-85°C in the deoxygenation preheater 2, then fully mixed with hydrogen 102 at room temperature, pressure of 0.8 MPa, and flow rate of 1 kg / h in the fifth static mixer 3 before entering the deoxygenation reactor 4. The material at the outlet of the deoxygenation reactor 4 enters the dealcoholization preheater 6 and is heated to 270-305°C. It then enters the dealcoholization heater 7 and is heated to 320-350°C before entering the dealcoholization reactor 5. The dealcoholized material is cooled to 165-175°C in the dealcoholization preheater 6 and enters the dehydration tower 9. The raw material benzene 103 at room temperature, pressure of 0.3 MPa, and flow rate of 695 kg / h is heated to 80-95°C in the benzene heater 8 and is then connected to the outlet pipeline of the dehydration tower reflux pump 12 and enters the dehydration tower 9. The dehydration tower 9 operates at atmospheric pressure. The overhead vapor enters the dehydration tower overhead condenser 10, where it is condensed and cooled to 40-55°C before entering the dehydration tower reflux separator 11. Free water is separated and removed in a water collection drum. The tail gas is transported from the tank overhead to the tail gas treatment facility, and the reflux liquid is returned to the dehydration tower 9 via the dehydration tower reflux pump 12. The second reboiler 13 of the dehydration tower 9 is heated by an external heat source, while the first reboiler 14 of the dehydration tower 9 is heated by the waste heat of the alkylation product. After dehydration, the alkylation reaction feed 104 is pressurized to 3.9-4.5 MPa by the dehydration tower bottom discharge pump 15, then heated to 175-190°C by the dehydration tower bottom discharge heater 16. The feed is then divided into three streams and enters the first static mixer 17, the second static mixer 18, the third static mixer 19, or the fourth static mixer 20, respectively.

[0061] One of the three feeds of the alkylation reaction after dehydration, 105, is fully mixed with the recycled benzene 110 from the recycled benzene booster pump 26 in the first static mixer 17, and then enters the alkylation heat exchanger 21 to be heated to 190 - 240 °C, and then enters the first alkylation reactor 22 or the second alkylation reactor 23. After three-stage series alkylation reaction, the alkylation reaction product 106 coming out of the third alkylation reactor 24 or the fourth alkylation reactor 25 is cooled to 175 - 210 °C by heat exchange in the alkylation heat exchanger 21 and enters the first reboiler 14, and continues to be cooled to 140 - 160 °C, and then is depressurized to 0.7 - 0.5 Mpa by the hydraulic turbine 27 to obtain the alkylation reaction product 107 at the outlet of the hydraulic turbine and then enters the debenzene column 30.

[0062] The debenzene column 30 operates at atmospheric pressure. The material drawn from the top side line of the column is divided into three streams by the recycled benzene pump 33. One stream is cooled to 40 - 55 °C by the debenzene column top cooler 32 and returns to the top of the in-column condenser of the debenzene column 30. The tail gas at the top of the debenzene column 30 is condensed and cooled by the debenzene tail gas condenser 34 and then enters the tail gas treatment facility; one stream of recycled benzene 110 is heated to 95 - 120 °C by the light ends column top cooler 39, then enters the paraffin-benzene mixing tank 28, and after being pressurized to 3.9 - 4.5 MPa by the recycled benzene booster pump 26, enters the heavy ends column top cooler 46, and is heated to 160 - 170 °C, and then enters the first static mixer 17, where it converges with one of the three feeds of the alkylation reaction after dehydration, 105, in the first static mixer 17; one stream returns to the debenzene column 30. The in-column reboiler 31 of the debenzene column is heated by an external heat source. The alkylation product 111 after debenzene is transported to the middle of the light ends column 36 by the debenzene column bottom transfer pump 35.

[0063] The light ends column 36 operates under negative pressure, with an operating pressure of 5 - 9 kPa. The side stream drawn from the light ends column 36 is divided into three streams by the light ends recycle pump 40. One stream is cooled to 90 - 100 °C by the light ends column top cooler 39 and then enters below the top partial condenser 37 of the light ends column; one stream of paraffin discharge 116 with a flow rate of 1205 kg / h is transported to the dehydrogenation unit area outside the plant; one stream is heated to 125 - 140 °C by the middle heater 44 and the post-middle heater 43 of the light ends column and then enters the light ends column 36. The cold water inlet 117 is heated to 30 - 40 °C by the alkylbenzene cooler 1, then enters the heavy alkylbenzene cooler 51 for further heat exchange, and then enters the top partial condenser 37 of the light ends column and is heated to 90 - 95 °C, and then the hot water is supplied externally 118. The tail gas at the outlet of the top partial condenser 37 of the light ends column is condensed and cooled by the light ends tail gas condenser 38 and then enters the vacuum pump, and the air discharged from the vacuum pump goes to the tail gas treatment system. The in-column reboiler 41 of the light ends column is heated by an external heat source. The bottom material of the column is transported to the middle of the heavy ends column 45 by the light ends column bottom transfer pump 42.

[0064] The de-weighting tower 45 operates under negative pressure, with an operating pressure of 1-3 kPa. The side stream from the de-weighting tower 45 is divided into three streams via an alkylbenzene transfer pump 47. One stream is cooled to 145-170°C via the de-weighting tower overhead cooler 46 and returned to the top of the de-weighting tower 45. The exhaust gas from the de-weighting tower 45 is condensed and cooled in the de-weighting tower exhaust condenser 50 before entering a vacuum pump and entering the exhaust gas treatment system. Another stream returns to the de-weighting tower 45. Alkylbenzene 114 is cooled to 50°C via the de-lighting tower mid-heater 44, the dehydration tower bottom discharge heater 16, the benzene heater 8, the deoxidation preheater 2, and the alkylbenzene cooler 1, producing 2385 kg / h of product. The de-weighting tower's internal reboiler 48 is heated by an external heat source. Heavy alkylbenzene 115 is transferred via a heavy alkylbenzene transfer pump 49 to the de-lighting tower mid-post-heater 43 and heavy alkylbenzene cooler 51, where it is cooled to 80°C, producing 124 kg / h of heavy alkylbenzene product.

[0065] Example 5 See also Figure 1 This embodiment provides a multifunctional alkylbenzene production system using a solid acid catalyst, comprising a deoxygenation reactor 4, a dealcoholization reactor 5, a dehydration tower 9, alkylation reactors 22-25, a hydraulic turbine 27, a debenzenization tower 30, a light-removal tower 36, and a heavy-removal tower 45. Taking 18,000 tons / year of dialkylbenzene production as an example, the specific solution is as follows: The raw material C12 normal or isoolefin 101 at room temperature, pressure of 0.8 MPa and flow rate of 300 kg / h is preheated to 75~85°C in the deoxygenation preheater 2, and then fully mixed with hydrogen 102 at room temperature, pressure of 0.8 MPa and flow rate of 0.08 kg / h in the fifth static mixer 3, and then enters the deoxygenation reactor 4. The outlet material of the deoxygenation reactor 4 enters the dehydration tower 9.

[0066] Alkylbenzene feedstock 103, at room temperature and a pressure of 0.3 MPa at a flow rate of 435 kg / h, is heated to 125-135°C by benzene heater 8 and then fed into the outlet pipeline of dehydration tower reflux pump 12, which then enters dehydration tower 9. Dehydration tower 9 operates at atmospheric pressure. The overhead vapor enters dehydration tower overhead condenser 10, condenses and cools to 40-55°C, and enters dehydration tower reflux separator 11. Free water is separated and removed in a water collection drum. The tail gas is transported from the tank top to the tail gas treatment facility, and the reflux liquid is returned to dehydration tower 9 via dehydration tower reflux pump 12. The second reboiler 13 of dehydration tower 9 is heated by an external heat source. After dehydration, the alkylation reaction feed 104 is pressurized to 3.9-4.5 MPa by dehydration tower bottom outlet pump 15 and then divided into three streams, entering the first static mixer 17, the second static mixer 18, the third static mixer 19, or the fourth static mixer 20, respectively.

[0067] One of the three feeds for the alkylation reaction after dehydration, stream 105, is fully mixed with the recycled alkylbenzene 109 from the recycled benzene booster pump 26 in the first static mixer 17, and then enters the alkylation heat exchanger 21 to be heated to 195 - 240 °C. After that, it enters the first alkylation reactor 22 or the second alkylation reactor 23. The alkylation reaction product 106 exiting from the third alkylation reactor 24 or the fourth alkylation reactor 25 after three-stage series alkylation reaction is cooled to 220 - 230 °C through heat exchange in the alkylation heat exchanger 21 and then depressurized to 0.7 - 0.5 Mpa by the hydraulic turbine 27 to obtain the alkylation reaction product 107 at the outlet of the hydraulic turbine, and then enters the light ends removal column 36.

[0068] The light ends removal column 36 operates under negative pressure with an operating pressure of 5 - 9 kPa. The side stream of the light ends removal column 36 is divided into three streams by the light ends recycle pump 40. One stream is the alkane product 116 with a flow rate of 300 kg / h, which is cooled by the alkane heat exchanger 29 and then transported to other plant areas; one stream is heated to 125 - 135 °C by the middle heater 44 and the post-middle heater 43 of the light ends removal column and then returned to the light ends removal column 36. The cold water feed 117 is heated to 30 - 35 °C by the alkylbenzene cooler 1, then enters the top partial condenser 37 of the light ends removal column and is heated to 75 - 80 °C, and then enters the top cooler 46 of the heavy ends removal column and is heated to 92 - 97 °C for external supply of hot water 118. The tail gas at the outlet of the top partial condenser 37 of the light ends removal column is condensed and cooled by the light ends tail gas condenser 38 and then enters the vacuum pump. The air discharged from the vacuum pump goes to the tail gas treatment system. The in-built reboiler 41 of the light ends removal column is heated by an external heat source. The bottom material of the column is divided into two streams by the bottom transfer pump 42 of the light ends removal column. One stream is transported to the middle of the benzene removal column 30, and one stream is transported to the middle of the heavy ends removal column 45.

[0069] Both the debenzene tower 30 and the de-weighting tower 45 operate at negative pressure, with operating pressures of 1-3 kPa. The material drawn from the overhead sidestream is separated into three streams by an alkylbenzene delivery pump 47. One stream is cooled to 80-95°C in the de-weighting tower overhead cooler 46 and returned to the top of the built-in condenser in the de-weighting tower 45. The tail gas from the top of the de-weighting tower 45 is condensed and cooled in the de-weighting tail gas condenser 50 before entering a vacuum pump. The tail gas from the vacuum pump is then discharged into the tail gas treatment facility. A stream of circulating alkylbenzene 109 is cooled in the middle heater 44 of the de-weighting tower and then fed into the circulating benzene pump 33. It is then heated to 175-190°C by the dehydration tower bottom outlet heater 16 before entering the alkane-benzene mixing tank 28. After mixing with the alkane feed 108 (which has a temperature of approximately 95-110°C and a flow rate of 300 kg / h after heat exchange), it enters the circulating benzene booster pump 26, where it is pressurized to 3.9-4.5 MPa. The stream then enters the first static mixer 17 along with one of the three feeds for the post-dehydration alkylation reaction, 105. A stream of circulating alkylbenzene returns to the de-weighting tower 45. The reboiler 48 in the de-weighting tower is heated by an external heat source. The product dialkylbenzene 112 is transported by the heavy alkylbenzene delivery pump 49 to the middle post-heater 43 of the dehydration tower, the bottom discharge heater 16 of the dehydration tower, the benzene heater 8, the deoxidation preheater 2, and the alkylbenzene cooler 1 to be cooled to 50°C and then output from the boundary area.

[0070] The above are all preferred embodiments of the present application, and are not intended to limit the scope of protection of the present application. Therefore, any equivalent changes made based on the structure, shape, and principle of the present application should be included in the scope of protection of the present application.

Claims

1. A multifunctional alkylbenzene production system, characterized in that, For producing linear alkylbenzene or polysubstituted alkylbenzene, it includes an alkylation reaction device (22, 23, 24, 25), a hydraulic turbine (27), a debenzene tower (30), a light component removal tower (36) and a heavy component removal tower (45). The material obtained from the reaction in the alkylation reaction device (22, 23, 24, 25) is connected to the hydraulic turbine (27) to recover the alkylation reaction pressure. The outlet of the hydraulic turbine (27) can be connected to the debenzene tower (30) or the light component removal tower (36). When producing linear alkylbenzene, the outlet of the hydraulic turbine (27) is connected to the debenzene tower (30). The bottom material of the debenzene tower (30) is connected to the light component removal tower (36). The bottom material of the light component removal tower (36) is connected to the heavy component removal tower (45). After the side stream of the heavy component removal tower (45) is taken out and cooled, a linear alkylbenzene product is obtained. When producing polysubstituted alkylbenzene, the outlet of the hydraulic turbine (27) is connected to the light component removal tower (36). The bottom material of the light component removal tower (36) is divided into two streams. One stream is connected to the debenzene tower (30), and the other stream is connected to the heavy component removal tower (45). After the side stream of the heavy component removal tower (45) is taken out and cooled, a dialkylbenzene product is obtained.

2. The multifunctional alkylbenzene production system according to claim 1, wherein It also includes an alkylation heat exchanger (21). The inlet of the tube side of the alkylation heat exchanger (21) is connected to the raw material to be reacted. The outlet of the tube side of the alkylation heat exchanger (21) is connected to the inlet of the alkylation reaction device (22, 23, 24, 25). The outlet of the alkylation reaction device (22, 23, 24, 25) is connected to the inlet of the shell side of the alkylation heat exchanger (21). The outlet of the shell side of the alkylation heat exchanger (21) is connected to the hydraulic turbine (27).

3. The multifunctional alkylbenzene production system according to claim 2, characterized in that, It also includes a dehydration tower (9) for dehydrating the raw material to be reacted. The raw material to be reacted includes reaction raw material one and reaction raw material two. Reaction raw material one is introduced into the middle and lower part of the dehydration tower (9). The top of the dehydration tower (9) is connected to the inlet of the tube side of the overhead condenser of the dehydration tower (10). The outlet of the tube side of the overhead condenser of the dehydration tower (10) is connected to the reflux pump of the dehydration tower (12). The outlet of the reflux pump of the dehydration tower (12) is returned to the dehydration tower (9). Reaction raw material two is introduced into the inlet of the tube side of the benzene heater (8). The outlet of the tube side of the benzene heater (8) is connected to the outlet pipeline of the reflux pump of the dehydration tower (12).

4. The multifunctional alkylbenzene production system according to claim 3, characterized in that, A first reboiler (14) is provided at the bottom of the dehydration tower (9). The inlet of the tube side of the first reboiler (14) is connected to the outlet of the shell side of the alkylation heat exchanger (21). The outlet of the tube side of the first reboiler (14) is connected to the hydraulic turbine (27), and the shell side is connected to the dehydration tower (9).

5. The multifunctional alkylbenzene production system according to claim 4, characterized in that, The bottom of the dehydration tower (9) is connected to the inlet of the tube side of the bottom discharge heater of the dehydration tower (16) through the bottom discharge pump of the dehydration tower (15). The outlet of the tube side of the bottom discharge heater of the dehydration tower (16) is connected to the alkylation reaction device (22, 23, 24, 25). The outlet of the shell side of the alkylation heat exchanger (21) is connected to the inlet of the tube side of the first reboiler (14). The outlet of the tube side of the first reboiler (14) is connected to the hydraulic turbine (27).

6. The multifunctional alkylbenzene production system according to claim 5, characterized in that, The alkylation reaction apparatuses (22, 23, 24, 25) include a first alkylation reactor (22), a second alkylation reactor (23), a third alkylation reactor (24), and a fourth alkylation reactor (25) connected in series. The operating mode of the four alkylbenzene reactors is three in operation and one in standby. And the first alkylation reactor (22) or the second alkylation reactor (23) serves as the alkylation reaction feed inlet, and the third alkylation reactor (24) or the fourth alkylation reactor (25) serves as the alkylation reaction product outlet.

7. The multifunctional alkylbenzene production system according to claim 6, wherein, A first static mixer (17), a second static mixer (18), a third static mixer (19), and a fourth static mixer (20) are respectively provided at the front ends of the inlets of the first alkylation reactor (22), the second alkylation reactor (23), the third alkylation reactor (24), and the fourth alkylation reactor (25). The alkylation heat exchanger (21) is arranged between the first static mixer (17) and the first alkylation reactor (22). The outlet of the tube side of the bottom discharge heater (16) of the dehydration tower is divided into three streams of materials. One of them is mixed with recycled benzene, toluene, or alkylbenzene and then connected to the inlet of the tube side of the alkylation heat exchanger (21). The outlet of the tube side of the alkylation heat exchanger (21) is connected to the inlet of the first alkylation reactor (22) or the second alkylation reactor (23). The outlet of the first alkylation reactor (22) is connected to the second static mixer (18), and after being mixed with a stream of material from the outlet of the tube side of the bottom discharge heater (16) of the dehydration tower, it is connected to the inlet of the second alkyl reactor (23). The outlet of the second alkyl reactor (23) is connected to the third static mixer (19), and after being mixed with a stream of material from the outlet of the tube side of the bottom discharge heater (16) of the dehydration tower, it is connected to the inlet of the third alkyl reactor (24). The outlet of the third alkyl reactor (24) is connected to the fourth static mixer (20), and after being mixed with a stream of material from the outlet of the tube side of the bottom discharge heater (16) of the dehydration tower, it is connected to the inlet of the fourth alkyl reactor (25). The outlet of the third alkylation reactor (24) or the fourth alkyl reactor (25) is connected to the inlet of the shell side of the alkylation heat exchanger (21).

8. The multifunctional alkylbenzene production system according to any one of claims 3-7, characterized in that, It further includes a deoxidation reactor (4) for deoxidizing the first reaction raw material. The first reaction raw material is mixed with hydrogen and then connected to the inlet of the deoxidation reactor (4). The outlet of the deoxidation reactor (4) is connected to the dehydration tower (9).

9. The multifunctional alkylbenzene production system according to claim 8, wherein It further includes a de-alcohol preheater (6), a de-alcohol heater (7), and a de-alcohol reactor (5). The outlet of the deoxidation reactor (4) is connected to the inlet of the tube side of the de-alcohol preheater (6). The outlet of the tube side of the de-alcohol preheater (6) is connected to the tube side of the de-alcohol heater (7). The outlet of the tube side of the de-alcohol heater (7) is connected to the de-alcohol reactor (5). The outlet of the de-alcohol reactor (5) is connected to the shell side of the de-alcohol preheater (6) for cooling. The outlet of the shell side of the de-alcohol preheater (6) is connected to the dehydration tower (9).

10. The multifunctional alkylbenzene production system according to claim 7, wherein, It further includes a circulating benzene booster pump (26) and an alkane-benzene mixing tank (28). The material extracted from the side line at the top of the benzene stripper (30) is divided into multiple streams by a circulating benzene pump (33). One of the streams enters the alkane-benzene mixing tank (28) and is mixed with the heated alkane feed (108), and then enters the circulating benzene booster pump (26). The outlet of the circulating benzene booster pump (26) is connected to the first static mixer (17).

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