CN111939584B - Crude benzene evaporation process and system in benzene hydrogenation reaction system - Google Patents
Crude benzene evaporation process and system in benzene hydrogenation reaction system Download PDFInfo
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Abstract
The invention relates to a crude benzene evaporation process and a system in a benzene hydrogenation reaction system, wherein the crude benzene evaporation system comprises a crude benzene buffer tank, a hydrogenation raw material pump, a pre-evaporator, a sectional evaporator, a pre-evaporator jet mixer, a sectional evaporator jet mixer, a reflux liquid jet mixer, a raffinate evaporator, a prefractionator reflux tank, a prefractionator reflux pump and a prefractionator bottom pump; the sectional evaporator adopts light benzene for reflux, and the light benzene for the reflux adopts outsourced light benzene products or adopts light benzene distilled from crude benzene by a prefractionator. The residual liquid evaporator is internally provided with a plurality of layers of trays, and the bottom of the tower is provided with a heater. The invention can improve the heavy removal effect of crude benzene evaporation, reduce energy consumption, reduce the benzene content in the residual liquid of the extracted crude benzene and improve the benzene yield.
Description
Technical Field
The invention relates to the technical field of benzene hydrofining, in particular to a crude benzene evaporation process and a system in a low-pressure crude benzene two-stage gas-phase hydrogenation reaction system.
Background
Crude benzene in the coking industry contains benzene, toluene and xylene as main components and 5-10% of unsaturated compounds, which are cyclic hydrocarbons and linear olefins with one or two double bonds, and are easy to polymerize, and the boiling points of some unsaturated compounds, sulfides and nitrogen-containing compounds are similar to the boiling point temperatures of corresponding benzene products, so that the unsaturated compounds, sulfides and nitrogen-containing compounds cannot be separated by a rectification method. The hydrofining process is to remove all impurities including thiophene in crude benzene by hydrogenation, wherein sulfide is converted into H 2 S, conversion of nitride to NH 3 Conversion of oxides to H 2 O, unsaturated hydrocarbon is hydrogenated and saturated, and H is removed by separation 2 S、NH 3 And H 2 The hydrogenated oil left after O can easily produce high-quality benzene, toluene and xylene products by means of extractive distillation.
The benzene hydrofining process has small production pollution and product quality comparable to petroleum benzene, so the crude benzene refining in the coking industry is mainly performed by low-pressure crude benzene hydrofining. The crude benzene hydrorefining is divided into two basic modes of liquid phase hydrogenation and then gas phase hydrogenation, and mainly comprises two stages of gas phase hydrogenation.
The crude benzene hydrogenation or crude benzene gas phase hydrogenation refers to a reaction process of two-stage gas phase hydrogenation of crude benzene.
The gas-phase hydrogenation process of crude benzene is characterized in that crude benzene is gasified directly when introduced from Germany, is subjected to heavy evaporation through a sectional evaporator and is hydrogenated, and then some domestic enterprises consider that the heavy removal degree is insufficient in operation, the process is modified, high-boiling-point fractions in the crude benzene are removed through a prefractionator by distillation before the crude benzene is subjected to gas-phase hydrogenation, so that light benzene is obtained, and then the light benzene is gasified and hydrogenated. However, the prefractionation technology of the crude benzene raw material adopted by the technology is not excessively high, the requirement of the benzene hydrogenation catalyst on crude benzene refining is not so high, the energy consumption of the technology is too large, in addition, the polymer generated by evaporation heating at the bottom of the sectional evaporator in the technology needs to be removed, the heavy removal effect of the sectional evaporator is not avoided, and the crude benzene residual liquid needs to be removed; therefore, the defect of high benzene content in the crude benzene raffinate at the bottom of the sectional evaporator is not fundamentally solved, the economy is poor, and the conventional process and the places needing improvement are further described below.
In the conventional gas-phase hydrogenation evaporation process of crude benzene, as shown in fig. 1, circulating hydrogen gas forms negative pressure at a high speed through a pre-evaporator jet mixer 106, crude benzene liquid sent by a hydrogenation raw material pump 102 flows circularly at a high speed in a pre-evaporator 103, external crude benzene liquid is preheated and mostly gasified through the pre-evaporator 103 by utilizing heat of the crude benzene gas after hydrogenation reaction, the negative pressure formed by the crude benzene gas-liquid mixture at a high speed through a staged evaporator jet mixer 107 is used as power, so that a closed cycle is formed between the bottom of a staged evaporator 105 and a reboiler 104, heat of the crude benzene gas after hydrogenation reaction is supplied by the reboiler 104, and crude benzene flowing back from the top of the staged evaporator 105 is gasified in the staged evaporator 105 completely, namely, the gasification amount is controlled by keeping the liquid level balance at the bottom of the staged evaporator 105 unchanged.
The segmented evaporator 105 has a plurality of trays with a separator at the bottom such that the segmented evaporator 105 is separated into upper and lower sections; the gasified crude benzene gas-liquid mixture from the sectional evaporator jet mixer 107 is separated in the lower part, the liquid falls into the bottom container, crude benzene vapor passes through the crude benzene gas outlet, negative pressure is formed by the reflux liquid jet mixer 108 at high speed, so that the crude benzene reflux liquid falling onto the partition plate from the top is sucked and carries out primary mixed mass transfer with the crude benzene vapor, the crude benzene reflux liquid enters the upper space of the sectional evaporator 105 for gas-liquid separation, the liquid returns to the upper part of the partition plate, fully flows into the lower container of the sectional evaporator 105 through the communicating pipe, the gas is upward, carries out mass transfer and heat transfer with the crude benzene liquid flowing back from the top through the multilayer tray, and is sent to the hydrogenation pre-reactor through the mist catcher at the top; the crude benzene raffinate is continuously discharged from the bottom of the staged evaporator 105, and is sent to a raffinate flash tank 109 for flash evaporation due to high benzene content, and the benzene vapor is sent to a crude benzene buffer tank 101 for bubbling cooling, and becomes a part of crude benzene raw material, and the flashed crude benzene flash raffinate is sent to a crude benzene raffinate tank.
The core equipment of the crude benzene evaporation process is a staged evaporator 105, 90% of crude benzene is gasified by a pre-evaporator 103, 10% is used as reflux of the staged evaporator 105, and about 5% of heavy components containing polymers, namely crude benzene residual liquid, can be continuously separated by refining of the staged evaporator 105 so as to improve the frequent occurrence of the phenomenon of blocking a reboiler 104 and the influence of excessive weight of gasified crude benzene vapor components on a subsequent hydrogenation reaction catalyst.
There are two places where the above process and system need improvement;
1. the method adopts a sectional evaporator for crude benzene reflux, is provided with a plurality of layers of trays, and plays a certain role in gas-liquid separation while gasifying the crude benzene, which is a key technical point of the crude benzene evaporation process, and has the defects that because reflux liquid is crude benzene, components are too heavy, and heavy components in gasified crude benzene vapor are not thoroughly removed.
2. The heavy component of the crude benzene raffinate is low, the benzene content is high, and the benzene content can not exceed 20 percent according to the specified requirement, but the benzene content is often more than 30 percent or even higher. The process only recovers a small amount of benzene through flash evaporation of the residual liquid flash evaporation tank 109, the benzene content of the crude benzene residual liquid after flash evaporation practically reaches more than 20%, and the benzene content of the crude benzene residual liquid after flash evaporation is reduced by about 400 tons of lost benzene in a scale of 10 ten thousand tons/year crude benzene hydrogenation.
Therefore, the prior crude benzene evaporation process and system are required to be improved so as to reduce the heavy component content of the gasified crude benzene, reduce the benzene content of the crude benzene residual liquid and improve the economic benefit.
Disclosure of Invention
The invention provides a crude benzene evaporation process and a system in a benzene hydrogenation reaction system, which can improve the heavy removal effect of crude benzene evaporation, reduce energy consumption, reduce the benzene content in the residual liquid of the extracted crude benzene and improve the benzene yield.
In order to achieve the above purpose, the invention is realized by adopting the following technical scheme:
the crude benzene evaporation process in the benzene hydrogenation reaction system comprises a prefractionator and a sectional evaporator; the sectional evaporator adopts light benzene for reflux, and the light benzene for the reflux adopts outsourced light benzene products or adopts light benzene distilled from crude benzene by a prefractionator.
The crude benzene evaporation system further comprises a residual liquid evaporator, wherein a plurality of layers of trays are arranged in the residual liquid evaporator, and a heater is arranged at the bottom of the residual liquid evaporator.
The crude benzene evaporation system comprises a prefractionator, a prefractionator reflux tank, a sectional evaporator, a raffinate evaporator and a crude benzene buffer tank; the crude benzene evaporation process specifically comprises the following steps:
1) The external raw benzene enters a raw benzene evaporation system and is divided into two paths, most raw benzene raw materials are removed to a raw benzene buffer tank, and the other small raw benzene raw materials are removed to a prefractionator;
2) In the prefractionator, the crude benzene raw material is subjected to prefractionation of light components and heavy components, and the tower top light benzene oil steam enters a prefractionator reflux tank after being condensed and cooled by a tower top condenser; pumping light benzene in a reflux tank of the prefractionator by a reflux pump of the prefractionator, wherein one part of the light benzene is returned to the top of the prefractionator as reflux, and the other part of the light benzene is returned as light benzene reflux liquid to the segment evaporator;
3) The heavy components at the bottom of the prefractionation tower are pumped out by a pump at the bottom of the prefractionation tower, and one part of the heavy components is circularly heated by a reboiler of the prefractionation tower and then returns to the bottom of the prefractionation tower so as to provide heat required by prefractionation; the other part is taken as a heavy benzene product to be sent out after being cooled;
4) Circulating hydrogen is sprayed into a mixer through a pre-evaporator to form negative pressure at a high speed, crude benzene liquid pumped by a hydrogenation raw material flows circularly in the pre-evaporator at a high speed, and the crude benzene liquid is preheated and mostly gasified through the pre-evaporator by utilizing the heat of crude benzene gas after hydrogenation reaction to form a crude benzene gas-liquid mixture;
5) The crude benzene gas-liquid mixture is sprayed by a sectional evaporator to form negative pressure as power through a mixer, so that the bottom of the sectional evaporator and a reboiler form a closed cycle, the heat of crude benzene gas after hydrogenation reaction is utilized, heat is supplied by the reboiler, light benzene flowing back from the top of the sectional evaporator is gasified in the sectional evaporator, and the gasification amount is controlled stably by keeping the liquid level balance at the bottom of the tower;
6) The inside of the sectional evaporator is provided with a plurality of layers of trays, and the bottom of the sectional evaporator is provided with a partition plate to partition the inside of the sectional evaporator into an upper space and a lower space; the section evaporator sprays the gasified crude benzene gas-liquid mixture from the mixer, gas-liquid separation is carried out in the lower space, and the separated liquid falls into the bottom liquid storage tank; the separated crude benzene vapor is led out through a crude benzene gas outlet and forms negative pressure through a reflux liquid jet mixer at high speed, so that light benzene reflux liquid falling onto a separation plate from the top of the segmented evaporator is sucked; after carrying out primary mixed mass transfer and heat transfer on the light benzene reflux liquid and the crude benzene vapor, the light benzene reflux liquid enters an upper space of the sectional evaporator to carry out gas-liquid separation, and the separated liquid falls back onto the isolation plate, fully flows into a lower space of the sectional evaporator through the communicating pipe and falls into the bottom liquid storage tank; the separated gas flows upwards, and is subjected to mass transfer and heat transfer with light benzene liquid flowing back from the top through a multi-layer tray, and finally fog drops are removed through a fog catcher at the top of the sectional evaporator and then sent to a hydrogenation pre-reactor;
7) Feeding the crude benzene residual liquid continuously discharged from the bottom of the staged evaporator into a residual liquid evaporator for flash evaporation, and feeding the benzene vapor subjected to flash evaporation into a crude benzene buffer tank for bubbling cooling to serve as a part of crude benzene raw material; the liquid after flash evaporation falls onto the tray at the uppermost layer, flows downwards as reflux liquid, flows to the crude benzene raffinate at the bottom of the raffinate evaporator, and is evaporated under the heating effect of a heater; the vaporized benzene vapor flows upwards, the reflux liquid is subjected to gas stripping refining, the light component is sent to a crude benzene buffer tank along with crude benzene residual liquid vapor for bubbling cooling, and the heavy component, namely crude benzene flash evaporation residual liquid, is continuously discharged from the bottom of a residual liquid evaporator.
In the external crude benzene raw materials, 70-90% of the crude benzene raw materials are removed to a crude benzene buffer tank, and 10-30% of the crude benzene raw materials are removed to a prefractionator.
The prefractionation tower adopts decompression operation, the tower top pressure is 45-55 KPa, and the vacuum degree is generated by a prefractionation tower vacuum unit; the prefractionator reboiler uses heat transfer oil as a heat source.
The sectional evaporator is operated at high pressure, and the operating pressure is 2.5-3.5 MPa; the residual liquid evaporator is operated at low pressure, and the operating pressure is 0.1-0.3 MPa.
The crude benzene evaporation system in the benzene hydrogenation reaction system for realizing the process comprises a crude benzene buffer tank, a hydrogenation raw material pump, a pre-evaporator, a sectional evaporator, a pre-evaporator jet mixer, a sectional evaporator jet mixer, a reflux liquid jet mixer, a residual liquid evaporator, a prefractionator reflux tank, a prefractionator reflux pump and a prefractionator bottom pump; the prefractionator is internally provided with a plurality of layers of trays, the top of the prefractionator is provided with a light benzene oil vapor outlet, the upper part of the prefractionator is provided with a light benzene reflux liquid inlet, the middle part of the prefractionator is provided with a crude benzene liquid inlet, the lower part of the prefractionator is provided with a circulating liquid inlet, and the bottom of the prefractionator is provided with a heavy benzene outlet; the crude benzene liquid inlet is connected with a crude benzene raw material conveying pipeline; the circulating liquid inlet is connected with the heavy benzene outlet through a prefractionator circulating pipeline, a prefractionator bottom pump, a heavy benzene liquid delivery outlet and a prefractionator reboiler are sequentially arranged on the prefractionator circulating pipeline along the liquid flow direction, and the heavy benzene liquid delivery outlet is connected with a heavy benzene product pipeline; the prefractionator is provided with a tower top cooler, and the light benzene oil gas outlet is connected with a light benzene oil gas condensate inlet on a reflux tank of the prefractionator through the tower top cooler; the top of the prefractionator reflux tank is provided with a tail gas outlet, the bottom of the prefractionator reflux tank is provided with a light benzene outlet, the tail gas outlet is connected with a vacuum unit through a tail gas pipeline, the light benzene outlet is respectively connected with a light benzene reflux inlet of the prefractionator and a light benzene reflux inlet of the segment evaporator through a light benzene reflux pipeline, and the light benzene reflux pipeline is provided with a prefractionator reflux pump; the inside of the sectional evaporator is sequentially provided with a demister, a multilayer tray and a separation plate from top to bottom, wherein the separation plate is arranged at the lower part of the sectional evaporator, the internal space of the sectional evaporator is separated into an upper space and a lower space, and the upper space and the lower space are communicated through a communicating pipe arranged on the separation plate; the top of the sectional evaporator is provided with a crude benzene gas outlet, one side of the sectional evaporator above the uppermost tray is provided with a light benzene reflux liquid inlet, one side of the sectional evaporator between the lowermost tray and the isolation plate is provided with a gas-liquid mixture inlet and a light benzene reflux liquid outlet, the same side of the sectional evaporator below the isolation plate is provided with a crude benzene gas outlet, and the gas-liquid mixture inlet, the light benzene reflux liquid outlet and the crude benzene gas outlet are respectively connected with a reflux liquid jet mixer; the other side of the sectional evaporator below the isolation plate is provided with a circulating liquid inlet, the bottom of the sectional evaporator is provided with a crude benzene residual liquid outlet and a circulating liquid outlet, and the crude benzene residual liquid outlet is connected with the crude benzene residual liquid inlet at the upper part of the residual liquid evaporator through a crude benzene residual liquid pipeline; the circulating liquid outlet is connected with the circulating liquid inlet through a circulating liquid pipeline, and a reboiler and a sectional evaporator jet mixer are sequentially arranged on the circulating liquid pipeline along the liquid flowing direction; the pre-evaporator is respectively connected with a sectional evaporator jet mixer, a reboiler and a pre-evaporator jet mixer, and the pre-evaporator jet mixer is provided with a circulating hydrogen inlet and a hydrogenated crude benzene gas-liquid mixture outlet; the top of the residual liquid evaporator is provided with a crude benzene residual liquid vapor outlet which is connected with a crude benzene residual liquid vapor inlet on a crude benzene buffer tank, a plurality of layers of trays are arranged in the residual liquid evaporator, the lower part of the residual liquid evaporator is provided with a heater, and the bottom of the residual liquid evaporator is provided with a crude benzene flash evaporation residual liquid outlet which is connected with a crude benzene flash evaporation residual liquid output pipeline; the top of the crude benzene buffer tank is provided with a crude benzene raw material inlet connected with a crude benzene raw material conveying pipeline, the bottom of the crude benzene buffer tank is provided with a crude benzene outlet connected with a pre-evaporator through the crude benzene conveying pipeline, and the crude benzene conveying pipeline is provided with a hydrogenation raw material pump.
The residual liquid evaporator is a vertical evaporator, wherein 3-5 layers of trays are arranged.
Compared with the prior art, the invention has the beneficial effects that:
1) The sectional evaporator is changed from conventional crude benzene reflux to light benzene reflux, and the current stripping distillation in the sectional evaporator is changed into refined distillation, so that the refining effect of the sectional evaporator is greatly improved, and the weight removing effect of crude benzene evaporation is improved;
2) The light benzene reflux quantity only accounts for 10% -30% of the total evaporation capacity of the crude benzene raw material, and compared with the conventional mode that the crude benzene is completely pre-fractionated to obtain light benzene and then evaporated, the energy consumption is obviously reduced;
3) The conventional raffinate flash tank (empty tank) is changed into a raffinate evaporator with a heater and a tray, and the common flash evaporation is changed into gas stripping rectification for the crude benzene raffinate, so that the benzene content of the crude benzene flash evaporation raffinate after the crude benzene raffinate is flashed is reduced to the greatest extent, and the benzene yield is improved.
Drawings
Fig. 1 is a schematic diagram of the structure of a conventional crude benzene evaporation system.
Fig. 2 is a schematic diagram of the crude benzene evaporation process and system according to the present invention.
In fig. 1: 101. crude benzene buffer tank 102, hydrogenation feed pump 103, pre-evaporator 104, reboiler 105, staged evaporator 106, pre-evaporator jet mixer 107, staged evaporator jet mixer 108, reflux jet mixer 109, raffinate flash tank
In fig. 2: 1. crude benzene buffer tank 2, hydrogenation raw material pump 3, pre-evaporator 4, reboiler 5, sectional evaporator 51, demister 52, partition plate 53, communicating pipe 6, pre-evaporator jet mixer 7, sectional evaporator jet mixer 8, reflux jet mixer 9, raffinate evaporator 10, heater 11, prefractionation column 12, overhead condenser 13, prefractionation column reflux tank 14, prefractionation column reflux pump 15, prefractionation column bottom pump 16, prefractionation column reboiler 17, lowest tray 18, uppermost tray
Detailed Description
The following is a further description of embodiments of the invention, taken in conjunction with the accompanying drawings:
as shown in FIG. 2, the crude benzene evaporation process in the benzene hydrogenation reaction system comprises a prefractionator 11 and a segment evaporator 5, wherein the segment evaporator 5 adopts light benzene for reflux, and the light benzene for reflux adopts outsourced light benzene products or adopts light benzene distilled from the crude benzene through the prefractionator.
The crude benzene evaporation system further comprises a raffinate evaporator 9, wherein a plurality of layers of trays are arranged in the raffinate evaporator 9, and a heater 10 is arranged at the bottom of the raffinate evaporator.
The crude benzene evaporation system comprises a prefractionator 11, a prefractionator reflux tank 13, a segmented evaporator 5, a raffinate evaporator 9 and a crude benzene buffer tank 1; the crude benzene evaporation process specifically comprises the following steps:
1) The external raw benzene enters a raw benzene evaporation system and is divided into two paths, most raw benzene raw materials are removed to a raw benzene buffer tank 1, and the other small raw benzene raw materials are removed to a prefractionator 11;
2) In the prefractionator 11, the crude benzene raw material is subjected to prefractionation of light components and heavy components, and the light benzene oil gas at the top of the tower enters a prefractionator reflux tank 13 after being condensed and cooled by a tower top condenser 12; the light benzene in the prefractionator reflux tank 13 is pumped by a prefractionator reflux pump 14, one part is sent back to the top of the prefractionator 11 as reflux, and the other part is sent to the segment evaporator 5 as light benzene reflux;
3) The heavy components at the bottom of the prefractionator 11 are pumped by a prefractionator bottom pump 15, and a part of the heavy components is circularly heated by a prefractionator reboiler 16 and then returns to the bottom of the prefractionator 11 so as to provide heat required by prefractionation; the other part is taken as a heavy benzene product to be sent out after being cooled;
4) Circulating hydrogen is high-speed formed into negative pressure through a pre-evaporator jet mixer 6, so that crude benzene liquid sent by a hydrogenation raw material pump 2 circularly flows in the pre-evaporator 3 at high speed, and the crude benzene liquid is preheated and mostly gasified through the pre-evaporator 3 by utilizing the heat of crude benzene gas after hydrogenation reaction to form a crude benzene gas-liquid mixture;
5) The crude benzene gas-liquid mixture is sprayed by a sectional evaporator jet mixer 7 at high speed to form negative pressure as power, so that the bottom of the sectional evaporator 5 and the reboiler 4 form a closed cycle, heat of the crude benzene gas after hydrogenation reaction is utilized, heat is supplied by the reboiler 4, light benzene flowing back from the top of the sectional evaporator 5 is gasified in the sectional evaporator 5, and the gasification amount is controlled stably by keeping the liquid level balance at the bottom of the tower;
6) The inside of the segmented evaporator 5 is provided with a plurality of trays, and the bottom of the segmented evaporator is provided with a separation plate 52 for separating the inside of the segmented evaporator into an upper space and a lower space; the gas-liquid separation is carried out in the lower space on the gasified crude benzene gas-liquid mixture from the sectional evaporator jet mixer 7, and the separated liquid falls into a liquid storage tank at the bottom; the separated crude benzene vapor is led out through a crude benzene gas outlet and forms negative pressure through a reflux liquid jet mixer 8 at high speed, so that light benzene reflux liquid falling onto a separation plate 52 from the top of the staged evaporator 5 is sucked; after the light benzene reflux liquid and the crude benzene vapor perform primary mixed mass transfer and heat transfer, the light benzene reflux liquid enters the upper space of the segment evaporator 5 to perform gas-liquid separation, the separated liquid falls back onto the isolation plate 52, flows into the lower space of the segment evaporator 5 through the communicating pipe 53 fully, and falls into the bottom liquid storage tank; the separated gas flows upwards, and is subjected to mass transfer and heat transfer with light benzene liquid flowing back from the top through a multi-layer tray, and finally, fog drops are removed through a fog catcher 51 at the top of the staged evaporator 5 and then sent to a hydrogenation pre-reactor;
7) The crude benzene residual liquid continuously discharged from the bottom of the staged evaporator 5 is sent to a residual liquid evaporator 9 for flash evaporation, and the benzene vapor after flash evaporation is sent to a crude benzene buffer tank 1 for bubbling cooling and is used as a part of crude benzene raw material; the liquid after flash evaporation falls on the tray at the uppermost layer, flows downwards as reflux liquid, and flows to the crude benzene raffinate at the bottom of the raffinate evaporator 9 to be evaporated under the heating effect of the heater 10; the vaporized benzene vapor flows upwards, the reflux liquid is subjected to gas stripping refining, the light component is sent to the crude benzene buffer tank 1 along with the crude benzene residual liquid vapor to be bubbling cooled, and the heavy component, namely the crude benzene flash residual liquid is continuously discharged from the bottom of the residual liquid evaporator 9.
Of the external raw benzene materials, 70% -90% of the raw benzene materials are removed to the raw benzene buffer tank 1, and the other 10% -30% of the raw benzene materials are removed to the prefractionator 11.
The prefractionator 11 is operated under reduced pressure, the pressure at the top of the prefractionator is 45-55 KPa, and the vacuum degree is generated by a prefractionator vacuum unit; prefractionator reboiler 16 uses heat transfer oil as a heat source.
The sectional evaporator 5 is operated at high pressure, and the operating pressure is 2.5-3.5 MPa; the residual liquid evaporator 9 is operated at low pressure, and the operating pressure is 0.1-0.3 MPa.
The crude benzene evaporation system in the benzene hydrogenation reaction system for realizing the process comprises a crude benzene buffer tank 1, a hydrogenation raw material pump 2, a pre-evaporator 3, a sectional evaporator 5, a pre-evaporator jet mixer 6, a sectional evaporator jet mixer 7, a reflux liquid jet mixer 8, a raffinate evaporator 9, a prefractionation tower 11, a prefractionation tower reflux tank 13, a prefractionation tower reflux pump 14 and a prefractionation tower bottom pump 15; the prefractionator 11 is internally provided with a plurality of layers of trays, the top is provided with a light benzene oil vapor outlet, the upper part is provided with a light benzene reflux liquid inlet, the middle part is provided with a crude benzene liquid inlet, the lower part is provided with a circulating liquid inlet, and the bottom is provided with a heavy benzene outlet; the crude benzene liquid inlet is connected with a crude benzene raw material conveying pipeline; the circulating liquid inlet is connected with the heavy benzene outlet through a prefractionator circulating pipeline, a prefractionator bottom pump 15, a heavy benzene liquid delivery outlet and a prefractionator reboiler 16 are sequentially arranged on the prefractionator circulating pipeline along the liquid flow direction, and the heavy benzene liquid delivery outlet is connected with a heavy benzene product pipeline; the prefractionator 11 is provided with a tower top cooler 12, and a light benzene oil gas outlet is connected with a light benzene oil gas condensate inlet on a prefractionator reflux tank 13 through the tower top cooler 12; the top of the prefractionator reflux tank 13 is provided with a tail gas outlet, the bottom is provided with a light benzene outlet, the tail gas outlet is connected with a vacuum unit through a tail gas pipeline, the light benzene outlet is respectively connected with a light benzene reflux inlet of the prefractionator 11 and a light benzene reflux inlet of the segment evaporator 5 through a light benzene reflux pipeline, and the light benzene reflux pipeline is provided with a prefractionator reflux pump 14; a demister 51, a multi-layer tray and a separation plate 52 are sequentially arranged in the segmented evaporator 5 from top to bottom, wherein the separation plate 52 is arranged at the lower part of the segmented evaporator 5, the internal space of the segmented evaporator 5 is partitioned into an upper space and a lower space, and the upper space and the lower space are communicated through a communicating pipe 53 arranged on the separation plate 52; the top of the segment evaporator 5 is provided with a crude benzene gas outlet, one side of the segment evaporator 5 above the uppermost tray 18 is provided with a light benzene reflux liquid inlet, one side of the segment evaporator 5 between the lowermost tray 17 and the isolation plate 52 is provided with a gas-liquid mixture inlet and a light benzene reflux liquid outlet, the same side of the segment evaporator 5 below the isolation plate 52 is provided with a crude benzene gas outlet, and the gas-liquid mixture inlet, the light benzene reflux liquid outlet and the crude benzene gas outlet are respectively connected with a reflux liquid jet mixer 8; the other side of the segment evaporator 5 below the isolation plate 52 is provided with a circulating liquid inlet, the bottom of the segment evaporator 5 is provided with a crude benzene residual liquid outlet and a circulating liquid outlet, and the crude benzene residual liquid outlet is connected with a crude benzene residual liquid inlet at the upper part of the residual liquid evaporator 9 through a crude benzene residual liquid pipeline; the circulating liquid outlet is connected with a circulating liquid inlet through a circulating liquid pipeline, and a reboiler 4 and a sectional evaporator jet mixer 7 are sequentially arranged on the circulating liquid pipeline along the liquid flowing direction; the pre-evaporator 3 is respectively connected with a sectional evaporator jet mixer 7, a reboiler 4 and a pre-evaporator jet mixer 6, and the pre-evaporator jet mixer 6 is provided with a circulating hydrogen inlet and a hydrogenated crude benzene gas-liquid mixture outlet; the top of the residual liquid evaporator 9 is provided with a crude benzene residual liquid vapor outlet which is connected with a crude benzene residual liquid vapor inlet on the crude benzene buffer tank 1, a plurality of layers of trays are arranged in the residual liquid evaporator 9, the lower part of the residual liquid evaporator is provided with a heater 10, and the bottom of the residual liquid evaporator is provided with a crude benzene flash evaporation residual liquid outlet which is connected with a crude benzene flash evaporation residual liquid output pipeline; the top of the crude benzene buffer tank 1 is provided with a crude benzene raw material inlet connected with a crude benzene raw material conveying pipeline, the bottom of the crude benzene buffer tank is provided with a crude benzene outlet connected with a pre-evaporator 3 through the crude benzene conveying pipeline, and the crude benzene conveying pipeline is provided with a hydrogenation raw material pump 2.
The residual liquid evaporator 9 is a vertical evaporator, and 3-5 layers of trays are arranged in the vertical evaporator.
The invention relates to a crude benzene evaporation process and a design principle of the system in a benzene hydrogenation reaction system, wherein the design principle is as follows: in order to improve the heavy removal effect of crude benzene evaporation and reduce energy consumption, the fractional evaporator 5 in the crude benzene evaporation system is changed from crude benzene reflux to light benzene reflux, and the working mode is changed from stripping distillation to refining distillation, so that the refining effect of the fractional evaporator 5 is greatly improved. When the light benzene is obtained by adopting a crude benzene prefractionation mode, the reflux quantity of the light benzene only accounts for 10% -30% of the total evaporation capacity of the crude benzene raw material, and compared with the mode that the light benzene is obtained by the whole prefractionation of the crude benzene in the conventional crude benzene evaporation process and then evaporated, the energy consumption is obviously reduced. In order to minimize the benzene content in the crude benzene flash residue after the crude benzene residue is flashed, the empty tank of the residue flash tank is changed into a residue evaporator 9 with a heater 10 and a plurality of layers of trays, and the crude benzene residue is changed into stripping rectification from the existing flash mode.
The crude benzene evaporation system is obtained by a crude benzene prefractionation mode based on light benzene, and if an outsourced light benzene product is adopted, the operation of the prefractionation tower 11 can be directly omitted.
The heater 10 of the raffinate evaporator 9 can adopt heat conduction oil as a heating medium, and can also adopt other media meeting the conditions for heating.
The foregoing is only a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art, who is within the scope of the present invention, should make equivalent substitutions or modifications according to the technical scheme of the present invention and the inventive concept thereof, and should be covered by the scope of the present invention.
Claims (6)
1. The crude benzene evaporation process in the benzene hydrogenation reaction system comprises a prefractionator and a sectional evaporator; the method is characterized in that the sectional evaporator adopts light benzene for reflux, and the light benzene for the reflux adopts outsourced light benzene products or adopts light benzene distilled from crude benzene through a prefractionator; the crude benzene evaporation system further comprises a residual liquid evaporator, wherein a plurality of layers of trays are arranged in the residual liquid evaporator, and a heater is arranged at the bottom of the residual liquid evaporator; the crude benzene evaporation system comprises a prefractionator, a prefractionator reflux tank, a sectional evaporator, a raffinate evaporator and a crude benzene buffer tank; the crude benzene evaporation process specifically comprises the following steps:
1) The external raw benzene enters a raw benzene evaporation system and is divided into two paths, most raw benzene raw materials are removed to a raw benzene buffer tank, and the other small raw benzene raw materials are removed to a prefractionator;
2) In the prefractionator, the crude benzene raw material is subjected to prefractionation of light components and heavy components, and the tower top light benzene oil steam enters a prefractionator reflux tank after being condensed and cooled by a tower top condenser; pumping light benzene in a reflux tank of the prefractionator by a reflux pump of the prefractionator, wherein one part of the light benzene is returned to the top of the prefractionator as reflux, and the other part of the light benzene is returned as light benzene reflux liquid to the segment evaporator;
3) The heavy components at the bottom of the prefractionation tower are pumped out by a pump at the bottom of the prefractionation tower, and one part of the heavy components is circularly heated by a reboiler of the prefractionation tower and then returns to the bottom of the prefractionation tower so as to provide heat required by prefractionation; the other part is taken as a heavy benzene product to be sent out after being cooled;
4) Circulating hydrogen is sprayed into a mixer through a pre-evaporator to form negative pressure at a high speed, crude benzene liquid pumped by a hydrogenation raw material flows circularly in the pre-evaporator at a high speed, and the crude benzene liquid is preheated and mostly gasified through the pre-evaporator by utilizing the heat of crude benzene gas after hydrogenation reaction to form a crude benzene gas-liquid mixture;
5) The crude benzene gas-liquid mixture is sprayed by a sectional evaporator to form negative pressure as power through a mixer, so that the bottom of the sectional evaporator and a reboiler form a closed cycle, the heat of crude benzene gas after hydrogenation reaction is utilized, heat is supplied by the reboiler, light benzene flowing back from the top of the sectional evaporator is gasified in the sectional evaporator, and the gasification amount is controlled stably by keeping the liquid level balance at the bottom of the tower;
6) The inside of the sectional evaporator is provided with a plurality of layers of trays, and the bottom of the sectional evaporator is provided with a partition plate to partition the inside of the sectional evaporator into an upper space and a lower space; the section evaporator sprays the gasified crude benzene gas-liquid mixture from the mixer, gas-liquid separation is carried out in the lower space, and the separated liquid falls into the bottom liquid storage tank; the separated crude benzene vapor is led out through a crude benzene gas outlet and forms negative pressure through a reflux liquid jet mixer at high speed, so that light benzene reflux liquid falling onto a separation plate from the top of the segmented evaporator is sucked; after carrying out primary mixed mass transfer and heat transfer on the light benzene reflux liquid and the crude benzene vapor, the light benzene reflux liquid enters an upper space of the sectional evaporator to carry out gas-liquid separation, and the separated liquid falls back onto the isolation plate, fully flows into a lower space of the sectional evaporator through the communicating pipe and falls into the bottom liquid storage tank; the separated gas flows upwards, and is subjected to mass transfer and heat transfer with light benzene liquid flowing back from the top through a multi-layer tray, and finally fog drops are removed through a fog catcher at the top of the sectional evaporator and then sent to a hydrogenation pre-reactor;
7) Feeding the crude benzene residual liquid continuously discharged from the bottom of the staged evaporator into a residual liquid evaporator for flash evaporation, and feeding the benzene vapor subjected to flash evaporation into a crude benzene buffer tank for bubbling cooling to serve as a part of crude benzene raw material; the liquid after flash evaporation falls onto the tray at the uppermost layer, flows downwards as reflux liquid, flows to the crude benzene raffinate at the bottom of the raffinate evaporator, and is evaporated under the heating effect of a heater; the vaporized benzene vapor flows upwards, the reflux liquid is subjected to gas stripping refining, the light component is sent to a crude benzene buffer tank along with crude benzene residual liquid vapor for bubbling cooling, and the heavy component, namely crude benzene flash evaporation residual liquid, is continuously discharged from the bottom of a residual liquid evaporator.
2. The process for evaporating crude benzene in a benzene hydrogenation reaction system according to claim 1, wherein 70% -90% of the external crude benzene raw materials are removed from the crude benzene buffer tank, and 10% -30% of the external crude benzene raw materials are removed from the prefractionator.
3. The process for evaporating crude benzene in a benzene hydrogenation reaction system according to claim 1, wherein the prefractionator is operated under reduced pressure, the pressure at the top of the prefractionator is 45-55 KPa, and the vacuum degree is generated by a prefractionator vacuum unit; the prefractionator reboiler uses heat transfer oil as a heat source.
4. The process for evaporating crude benzene in a benzene hydrogenation reaction system according to claim 1, wherein the staged evaporator is operated at a high pressure, and the operating pressure is 2.5-3.5 MPa; the residual liquid evaporator is operated at low pressure, and the operating pressure is 0.1-0.3 MPa.
5. A crude benzene evaporation device used in a benzene hydrogenation reaction system for realizing the process according to any one of claims 1 to 4, which is characterized by comprising a crude benzene buffer tank, a hydrogenation raw material pump, a pre-evaporator, a sectional evaporator, a pre-evaporator jet mixer, a sectional evaporator jet mixer, a reflux liquid jet mixer, a raffinate evaporator, a prefractionation column reflux tank, a prefractionation column reflux pump and a prefractionation column bottom pump; the prefractionator is internally provided with a plurality of layers of trays, the top of the prefractionator is provided with a light benzene oil vapor outlet, the upper part of the prefractionator is provided with a light benzene reflux liquid inlet, the middle part of the prefractionator is provided with a crude benzene liquid inlet, the lower part of the prefractionator is provided with a circulating liquid inlet, and the bottom of the prefractionator is provided with a heavy benzene outlet; the crude benzene liquid inlet is connected with a crude benzene raw material conveying pipeline; the circulating liquid inlet is connected with the heavy benzene outlet through a prefractionator circulating pipeline, a prefractionator bottom pump, a heavy benzene liquid delivery outlet and a prefractionator reboiler are sequentially arranged on the prefractionator circulating pipeline along the liquid flow direction, and the heavy benzene liquid delivery outlet is connected with a heavy benzene product pipeline; the prefractionator is provided with a tower top cooler, and the light benzene oil gas outlet is connected with a light benzene oil gas condensate inlet on a reflux tank of the prefractionator through the tower top cooler; the top of the prefractionator reflux tank is provided with a tail gas outlet, the bottom of the prefractionator reflux tank is provided with a light benzene outlet, the tail gas outlet is connected with a vacuum unit through a tail gas pipeline, the light benzene outlet is respectively connected with a light benzene reflux inlet of the prefractionator and a light benzene reflux inlet of the segment evaporator through a light benzene reflux pipeline, and the light benzene reflux pipeline is provided with a prefractionator reflux pump; the inside of the sectional evaporator is sequentially provided with a demister, a multilayer tray and a separation plate from top to bottom, wherein the separation plate is arranged at the lower part of the sectional evaporator, the internal space of the sectional evaporator is separated into an upper space and a lower space, and the upper space and the lower space are communicated through a communicating pipe arranged on the separation plate; the top of the sectional evaporator is provided with a crude benzene gas outlet, one side of the sectional evaporator above the uppermost tray is provided with a light benzene reflux liquid inlet, one side of the sectional evaporator between the lowermost tray and the isolation plate is provided with a gas-liquid mixture inlet and a light benzene reflux liquid outlet, the same side of the sectional evaporator below the isolation plate is provided with a crude benzene gas outlet, and the gas-liquid mixture inlet, the light benzene reflux liquid outlet and the crude benzene gas outlet are respectively connected with a reflux liquid jet mixer; the other side of the sectional evaporator below the isolation plate is provided with a circulating liquid inlet, the bottom of the sectional evaporator is provided with a crude benzene residual liquid outlet and a circulating liquid outlet, and the crude benzene residual liquid outlet is connected with the crude benzene residual liquid inlet at the upper part of the residual liquid evaporator through a crude benzene residual liquid pipeline; the circulating liquid outlet is connected with the circulating liquid inlet through a circulating liquid pipeline, and a reboiler and a sectional evaporator jet mixer are sequentially arranged on the circulating liquid pipeline along the liquid flowing direction; the pre-evaporator is respectively connected with the sectional evaporator jet mixer, the reboiler and the pre-evaporator jet mixer, and the pre-evaporator jet mixer is provided with a circulating hydrogen inlet and a hydrogenated crude benzene gas-liquid mixture outlet; the top of the residual liquid evaporator is provided with a crude benzene residual liquid vapor outlet which is connected with a crude benzene residual liquid vapor inlet on a crude benzene buffer tank, a plurality of layers of trays are arranged in the residual liquid evaporator, the lower part of the residual liquid evaporator is provided with a heater, and the bottom of the residual liquid evaporator is provided with a crude benzene flash evaporation residual liquid outlet which is connected with a crude benzene flash evaporation residual liquid output pipeline; the top of the crude benzene buffer tank is provided with a crude benzene raw material inlet connected with a crude benzene raw material conveying pipeline, the bottom of the crude benzene buffer tank is provided with a crude benzene outlet connected with a pre-evaporator through the crude benzene conveying pipeline, and the crude benzene conveying pipeline is provided with a hydrogenation raw material pump.
6. The apparatus for vaporizing crude benzene in a benzene hydrogenation reaction system according to claim 5, wherein said raffinate vaporizer is a vertical vaporizer having 3 to 5 trays.
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