CN111939584A - Process and system for evaporating crude benzene in benzene hydrogenation reaction system - Google Patents
Process and system for evaporating crude benzene in benzene hydrogenation reaction system Download PDFInfo
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Abstract
The invention relates to a crude benzene evaporation process and a crude benzene evaporation 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 jet mixer, a raffinate evaporator, a pre-fractionating tower reflux tank, a pre-fractionating tower reflux pump and a pre-fractionating tower bottom pump; the sectional evaporator adopts light benzene reflux, and the light benzene for reflux adopts an outsourcing light benzene product or light benzene fractionated by crude benzene through a prefractionator. And a plurality of layers of tower trays are arranged in the raffinate evaporator, and a heater is arranged at the bottom of the tower. The invention can improve the de-heavy effect of crude benzene evaporation, reduce energy consumption, reduce the benzene content in the extracted crude benzene residual liquid and improve the yield of benzene.
Description
Technical Field
The invention relates to the technical field of benzene hydrofining, in particular to a process and a system for evaporating crude benzene in a low-pressure crude benzene two-stage gas-phase hydrogenation reaction system.
Background
The crude benzene of coking industry contains benzene, toluene and xylene as main components, and also contains 5-10% of unsaturated compoundsThe compounds are cyclic hydrocarbon and straight chain olefin with one or two double bonds, and are easy to polymerize, and the boiling points of some unsaturated compounds, sulfide and nitrogen-containing compounds are similar to the boiling point temperature of corresponding benzene products, so that they cannot be separated by rectification method. The hydrofining process has the function of completely removing various impurities mainly containing thiophene in the crude benzene by hydrogenation, wherein all sulfides are converted into H2S, conversion of nitrides to NH3Conversion of oxides to H2O, unsaturated hydrocarbon is hydrogenated to saturate, and H is separated and removed2S、NH3And H2The hydrogenated oil left after O can be easily used for producing high-quality benzene, toluene and xylene products by an extractive distillation mode.
The benzene hydrofining process has less production pollution and the product quality can be comparable to petroleum benzene, so that the crude benzene refining in the coking industry is mainly low-pressure crude benzene hydrofining at present. The crude benzene hydrofining is divided into two basic modes of liquid phase hydrogenation and gas phase hydrogenation, and two-stage gas phase hydrogenation mainly takes two-stage gas phase hydrogenation as the main mode.
The crude benzene hydrogenation or crude benzene gas phase hydrogenation refers to the reaction process of two-stage gas phase hydrogenation of crude benzene.
A gas-phase hydrogenation process for crude benzene, which is introduced from Germany at first, directly gasifies the crude benzene, hydrogenates the crude benzene after heavy removal and evaporation by a sectional evaporator, and later some domestic enterprises consider that the heavy removal degree is not enough in operation. But the pre-fractionation process of all the adopted crude benzene raw materials belongs to the excessive adjustment, the requirement of the benzene hydrogenation catalyst on crude benzene refining is not so high, the energy consumption of the process is too large, in addition, polymers generated by evaporation and heating at the bottom of a sectional evaporator in the process need to be removed, the effect of removing the weight of the sectional evaporator is not avoided, and crude benzene residual liquid needs to be removed; therefore, the defect of high benzene content in the crude benzene residual liquid at the bottom of the sectional evaporator is not fundamentally solved, the economical efficiency is not good, and the conventional process and places needing improvement are further explained.
In the conventional gas-phase hydrogenation and evaporation process of crude benzene, as shown in fig. 1, circulating hydrogen gas passes through a pre-evaporator jet mixer 106 at a high speed to form negative pressure, so that crude benzene liquid sent by a hydrogenation raw material pump 102 flows in a high-speed circulation manner in the pre-evaporator 103, the external crude benzene liquid is preheated and mostly gasified by the pre-evaporator 103 by using heat of crude benzene gas after hydrogenation reaction, the negative pressure formed by passing the crude benzene gas-liquid mixture through a segmented evaporator jet mixer 107 at a high speed is used as power, so that a closed cycle is formed between the bottom of a segmented evaporator 105 and a reboiler 104, heat is supplied by the reboiler 104 by using the heat of the crude benzene gas after hydrogenation reaction, and the crude benzene refluxed from the top of the segmented evaporator 105 is completely gasified in the segmented evaporator 105, that is, the gasification amount is controlled by keeping the liquid level at the bottom of the segmented evaporator constant.
The sectional evaporator 105 has a plurality of trays, and a partition plate is arranged at the bottom of the sectional evaporator 105, so that the sectional evaporator 105 is divided into an upper part and a lower part; the gasified crude benzene gas-liquid mixed liquid from the segmented evaporator jet mixer 107 is subjected to gas-liquid separation at the lower part, the liquid falls into a bottom container, crude benzene vapor passes through a crude benzene gas outlet and forms negative pressure through a reflux liquid jet mixer 108 at high speed, so that the crude benzene reflux liquid falling from the top onto a separation plate is sucked and subjected to primary mixing mass transfer and heat transfer with the crude benzene vapor, enters the upper space of the segmented evaporator 105 for gas-liquid separation, the liquid returns to the upper part of the separation plate and flows into the lower container of the segmented evaporator 105 through a communicating pipe in a full flow mode, the gas flows upwards, is subjected to mass transfer and heat transfer with the crude benzene liquid flowing from the top through a plurality of layers of trays, and is sent to a hydrogenation pre-reactor through a mist catcher at the top; the crude benzene raffinate is continuously discharged from the bottom of the sectional evaporator 105, and is sent to a raffinate flash evaporation tank 109 for flash evaporation due to high benzene content, benzene steam is sent to a crude benzene buffer tank 101 for bubbling cooling to become a part of crude benzene raw materials, and the flash evaporation raffinate of the flash evaporated crude benzene is sent to a crude benzene raffinate tank.
The key equipment of the crude benzene evaporation process is a sectional evaporator 105, 90% of crude benzene is gasified by a pre-evaporator 103, 10% of crude benzene is used as reflux of the sectional evaporator 105, and about 5% of heavy components containing polymers, namely crude benzene residual liquid, can be continuously separated by refining the sectional evaporator 105 so as to improve the frequent occurrence of a reboiler 104 blockage phenomenon and the influence of the overweight of the gasified crude benzene steam components on a subsequent hydrogenation reaction catalyst.
There are two places where the above process and system need to be improved;
1. the sectional evaporator adopting crude benzene reflux is provided with a plurality of layers of tower trays, and has a certain gas-liquid separation effect while gasifying the crude benzene, which is a key technical point of the crude benzene evaporation process.
2. The crude benzene raffinate has low heavy components and high benzene content, the benzene content can not exceed 20 percent according to the specified requirement, and the benzene content is often over 30 percent or even higher. In the process, a small amount of benzene is recovered only by flash evaporation of the raffinate flash evaporation tank 109, the benzene content of the flashed crude benzene raffinate actually reaches more than 20%, and the annual loss of benzene is about 400 tons at the scale of 10 ten thousand tons per year of crude benzene hydrogenation, so that the raffinate flash evaporation tank 109 needs to be improved, and the benzene content of the flashed crude benzene raffinate is reduced.
Therefore, improvement of the existing crude benzene evaporation process and system is needed 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 process and a system for evaporating crude benzene in a benzene hydrogenation reaction system, which can reduce energy consumption, reduce the benzene content in extracted crude benzene residual liquid and improve the yield of benzene while improving the de-heavy effect of crude benzene evaporation.
In order to achieve the purpose, the invention adopts the following technical scheme:
a process for evaporating crude benzene in a benzene hydrogenation reaction system comprises a prefractionator and a sectional evaporator; the sectional evaporator adopts light benzene reflux, and the light benzene for reflux adopts an outsourcing light benzene product or light benzene fractionated by crude benzene through a prefractionator.
The crude benzene evaporation system further comprises a raffinate evaporator, wherein a plurality of layers of tower trays are arranged in the raffinate evaporator, and a heater is arranged at the bottom of the tower.
The crude benzene evaporation system comprises a prefractionator, a prefractionator reflux groove, a sectional evaporator, a raffinate evaporator and a crude benzene buffer groove; the crude benzene evaporation process specifically comprises the following steps:
1) the external crude benzene raw material enters a crude benzene evaporation system and then is divided into two paths, wherein most of the crude benzene raw material is sent to a crude benzene buffer tank, and the small part of the crude benzene raw material is sent to a pre-fractionating tower;
2) in a prefractionator, performing pre-separation of light components and heavy components on a crude benzene raw material, condensing and cooling tower top light benzene oil vapor by a tower top condenser, and then feeding the condensed and cooled tower top light benzene oil vapor into a prefractionator reflux groove; extracting light benzene in the reflux tank of the prefractionator by using a prefractionator reflux pump, sending one part of the light benzene back to the top of the prefractionator as reflux, and sending the other part of the light benzene back to a sectional evaporator as light benzene reflux;
3) heavy components at the bottom of the prefractionator are pumped out by a prefractionator bottom pump, and a part of the heavy components are circularly heated by a prefractionator reboiler and then return to the bottom of the prefractionator to provide heat required by prefractionation; the other part is taken as a heavy benzene product and sent out after being cooled;
4) circulating hydrogen passes through a jet mixer of the pre-evaporator at a high speed to form negative pressure, so that crude benzene liquid pumped by a hydrogenation raw material flows in the pre-evaporator at a high speed in a circulating manner, 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 passes through the jet mixer of the sectional evaporator at a high speed to form negative pressure as power, so that a closed cycle is formed between the bottom of the sectional evaporator and a reboiler, heat of the crude benzene gas after hydrogenation reaction is utilized, heat is supplied through the reboiler, light benzene flowing back from the top of the sectional evaporator is completely gasified in the sectional evaporator, and the gasification amount is controlled by keeping the liquid level at the bottom of the sectional evaporator balanced and stable;
6) a plurality of layers of tower trays are arranged in the segmented evaporator, and the inside of the segmented evaporator is partitioned into an upper space and a lower space by a partition plate arranged at the bottom; the sectional 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 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 at high speed, so that light benzene reflux liquid falling onto the isolation plate from the top of the sectional evaporator is sucked; after primary mixing mass transfer and heat transfer are carried out on the light benzene reflux liquid and the crude benzene steam, the light benzene reflux liquid enters the upper space of the sectional evaporator for gas-liquid separation, the separated liquid falls back to the isolation plate, flows into the lower space of the sectional evaporator fully through the communicating pipe and falls into a liquid storage tank at the bottom; the separated gas flows upwards, and is subjected to mass transfer and heat transfer with the light benzene liquid flowing from the top through a plurality of layers of tower trays, and finally is sent to a hydrogenation pre-reactor after fog drops are removed by a mist catcher at the top of the sectional evaporator;
7) sending the crude benzene residual liquid continuously discharged from the bottom of the sectional evaporator to a residual liquid evaporator for flash evaporation, sending the benzene steam after flash evaporation to a crude benzene buffer tank for bubbling cooling, and taking the benzene steam as a part of a crude benzene raw material; the liquid after flash evaporation falls on the tray on the uppermost layer and flows downwards as reflux liquid, and the crude benzene residual liquid flowing to the bottom of the residual liquid evaporator is evaporated under the heating action of a heater; the evaporated benzene vapor flows upwards, the reflux liquid is subjected to gas stripping refining, light components are sent to the crude benzene buffer tank along with crude benzene residual liquid vapor for bubbling cooling, and heavy components, namely crude benzene flash residual liquid, are continuously discharged from the bottom of the residual liquid evaporator.
70-90% of the external crude benzene raw materials are sent to a crude benzene buffer tank, and the other 10-30% of the crude benzene raw materials are sent to a pre-fractionating tower.
The pre-fractionating tower adopts decompression operation, the pressure at the top of the tower is 45-55 KPa, and the vacuum degree of the pre-fractionating tower is generated by a vacuum unit of the pre-fractionating tower; the reboiler of the pre-fractionating tower adopts heat conducting oil as a heat source.
The segmented evaporator is operated at high pressure, and the operating pressure is 2.5-3.5 MPa; the raffinate 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 raffinate evaporator, a pre-fractionating tower reflux tank, a pre-fractionating tower reflux pump and a pre-fractionating tower bottom pump; the pre-fractionating tower is internally provided with a plurality of layers of tower trays, the top of the pre-fractionating tower is provided with a light benzene oil vapor outlet, the upper part of the pre-fractionating tower is provided with a light benzene reflux liquid inlet, the middle part of the pre-fractionating tower is provided with a crude benzene liquid inlet, the lower part of the pre-fractionating tower is provided with a circulating liquid inlet, and the bottom of the; 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 prefractionation tower circulating pipeline, a prefractionation tower bottom pump, a heavy benzene liquid outlet and a prefractionation tower reboiler are sequentially arranged on the prefractionation tower circulating pipeline along the liquid flowing direction, and the heavy benzene liquid outlet is connected with a heavy benzene product pipeline; the prefractionator is provided with a tower top cooler, and a light benzene oil vapor outlet is connected with a light benzene oil vapor condensate inlet on a prefractionator reflux groove through the tower top cooler; the top of the reflux tank of the prefractionating tower is provided with a tail gas outlet, the bottom of the reflux tank of the prefractionating tower 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 prefractionating tower and a light benzene reflux inlet of the sectional evaporator through light benzene reflux pipelines, and the light benzene reflux pipeline is provided with a prefractionating tower reflux pump; the sectional evaporator is internally provided with a demister, a plurality of layers of tower trays and a partition plate in sequence from top to bottom, wherein the partition plate is arranged at the lower part of the sectional evaporator and partitions the internal space of the sectional evaporator 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 partition plate; the top of the sectional evaporator is provided with a crude benzene gas outlet, one side of the sectional evaporator above the tray on the uppermost layer is provided with a light benzene reflux inlet, one side of the sectional evaporator between the tray on the lowermost layer and the partition plate is provided with a gas-liquid mixture inlet and a light benzene reflux outlet, the same side of the sectional evaporator below the partition plate is provided with a crude benzene gas outlet, and the gas-liquid mixture inlet, the light benzene reflux outlet and the crude benzene gas outlet are respectively connected with a reflux liquid jet mixer; the other side of the segmented evaporator below the partition plate is provided with a circulating liquid inlet, the bottom of the segmented evaporator is provided with a crude benzene raffinate outlet and a circulating liquid outlet, and the crude benzene raffinate outlet is connected with a crude benzene raffinate inlet at the upper part of the raffinate evaporator through a crude benzene raffinate pipeline; the circulating liquid outlet is connected with the circulating liquid inlet through a circulating liquid pipeline, and a reboiler and a segmented evaporator jet mixer are sequentially arranged on the circulating liquid pipeline along the liquid flowing direction; the pre-evaporator is respectively connected with the jet mixer of the sectional evaporator, the reboiler and the jet mixer of the pre-evaporator, and the jet mixer of the pre-evaporator is provided with a circulating hydrogen inlet and a hydrogenated crude benzene gas-liquid mixture outlet; a crude benzene raffinate steam outlet is arranged at the top of the raffinate evaporator and connected with a crude benzene raffinate steam inlet on the crude benzene buffer tank, a multilayer tower tray is arranged in the raffinate evaporator, a heater is arranged at the lower part of the raffinate evaporator, and a crude benzene flash raffinate outlet arranged at the bottom of the raffinate evaporator is connected with a crude benzene flash raffinate output pipeline; crude benzene raw materials entry linkage crude benzene raw materials pipeline is established at crude benzene dashpot top, and the bottom is established the crude benzene export and is passed through crude benzene pipeline and connect the pre-evaporator, establishes hydrogenation raw materials pump on the crude benzene pipeline.
The raffinate evaporimeter is vertical evaporimeter, is equipped with 3 ~ 5 layers of tower tray wherein.
Compared with the prior art, the invention has the beneficial effects that:
1) the conventional crude benzene reflux is changed into light benzene reflux in the sectional evaporator, and the existing stripping distillation is changed into refining distillation in the sectional evaporator, so that the refining effect of the sectional evaporator is greatly improved, and the heavy removal effect of crude benzene evaporation is improved;
2) the reflux amount of the light benzene only accounts for 10-30% of the total evaporation amount of the crude benzene raw material, and compared with the conventional mode of pre-distilling the crude benzene to obtain the light benzene and then evaporating, the energy consumption is obviously reduced;
3) the conventional raffinate flash evaporation tank (empty tank) is changed into a raffinate evaporator with a heater and a tower tray, and the ordinary flash evaporation of the crude benzene raffinate is changed into gas stripping rectification, so that the benzene content of the crude benzene flash evaporation raffinate after the flash evaporation of the crude benzene raffinate is reduced to the greatest extent, and the benzene yield is improved.
Drawings
FIG. 1 is a schematic view of a conventional crude benzene vaporization system.
FIG. 2 is a schematic diagram of the structure of the crude benzene evaporation process and system according to the present invention.
In fig. 1: 101. crude benzene buffer tank 102, hydrogenation feedstock 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 drum
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 injection mixer 7, sectional evaporator injection mixer 8, reflux injection mixer 9, raffinate evaporator 10, heater 11, prefractionator 12, overhead condenser 13, prefractionator reflux tank 14, prefractionator reflux pump 15, prefractionator bottom pump 16, prefractionator reboiler 17, lowermost tray 18, uppermost tray 18
Detailed Description
The following further describes embodiments of the present invention with reference to the accompanying drawings:
as shown in fig. 2, the crude benzene evaporation process in the benzene hydrogenation reaction system according to the present invention includes a prefractionation tower 11 and a sectional evaporator 5, wherein the sectional evaporator 5 adopts light benzene reflux, and light benzene for reflux adopts purchased light benzene products, or adopts light benzene obtained by fractionating crude benzene through the prefractionation tower.
The crude benzene evaporation system also comprises a raffinate evaporator 9, wherein a plurality of layers of tower trays are arranged in the raffinate evaporator 9, and a heater 10 is arranged at the bottom of the tower.
The crude benzene evaporation system comprises a prefractionator 11, a prefractionator reflux groove 13, a sectional evaporator 5, a raffinate evaporator 9 and a crude benzene buffer groove 1; the crude benzene evaporation process specifically comprises the following steps:
1) the external crude benzene raw material enters a crude benzene evaporation system and then is divided into two paths, wherein most of the crude benzene raw material enters a crude benzene buffer tank 1, and the small part of the crude benzene raw material enters a pre-fractionating tower 11;
2) in a prefractionator 11, a crude benzene raw material is subjected to pre-separation of light components and heavy components, and light benzene oil vapor at the top of the tower is condensed and cooled by a tower top condenser 12 and then enters a prefractionator reflux groove 13; light benzene in the reflux tank 13 of the prefractionator is pumped out by a prefractionator reflux pump 14, one part of the light benzene is sent back to the top of the prefractionator 11 as reflux, and the other part of the light benzene is sent to the sectional evaporator 5 as light benzene reflux;
3) heavy components at the bottom of the prefractionation tower 11 are pumped out by a prefractionation tower bottom pump 15, and a part of the heavy components are circularly heated by a prefractionation tower reboiler 16 and then return to the bottom of the prefractionation tower 11 to provide heat required by prefractionation; the other part is taken as a heavy benzene product and sent out after being cooled;
4) circulating hydrogen passes through the jet mixer 6 of the pre-evaporator at a high speed to form negative pressure, so that the crude benzene liquid sent by the hydrogenation raw material pump 2 flows in the pre-evaporator 3 at a high speed in a circulating manner, and the crude benzene liquid is preheated and mostly gasified through the pre-evaporator 3 by utilizing the heat of the crude benzene gas after hydrogenation reaction to form a crude benzene gas-liquid mixture;
5) the crude benzene gas-liquid mixture forms negative pressure as power through a sectional evaporator jet mixer 7 at high speed, so that a closed cycle is formed between the tower bottom of a sectional evaporator 5 and a reboiler 4, heat of crude benzene gas after hydrogenation reaction is utilized, heat is supplied through the reboiler 4, light benzene flowing back from the top of the sectional evaporator 5 is completely gasified in the sectional evaporator 5, and the gasification amount is controlled by keeping the liquid level at the tower bottom balanced and stable;
6) a plurality of layers of tower trays are arranged in the segmented evaporator 5, and the inside of the segmented evaporator is divided into an upper space and a lower space by a partition plate 52 arranged at the bottom; the gasified crude benzene gas-liquid mixture from the segmented evaporator injection mixer 7 is subjected to gas-liquid separation in the lower space, 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 passes through the reflux liquid jet mixer 8 at a high speed to form negative pressure, so that the light benzene reflux liquid falling from the top of the sectional evaporator 5 onto the isolation plate 52 is sucked; after primary mixing mass transfer and heat transfer are carried out on the light benzene reflux liquid and the crude benzene steam, the light benzene reflux liquid enters the upper space of the sectional evaporator 5 for gas-liquid separation, the separated liquid falls back onto the isolation plate 52, flows into the lower space of the sectional evaporator 5 fully through the communicating pipe 53 and falls into a liquid storage tank at the bottom; the separated gas flows upwards, and is subjected to mass transfer and heat transfer with the light benzene liquid flowing from the top through a plurality of layers of tower trays, and finally is sent to a hydrogenation pre-reactor after fog drops are removed by a mist catcher 51 at the top of the sectional evaporator 5;
7) sending the crude benzene residual liquid continuously discharged from the bottom of the sectional evaporator 5 to a residual liquid evaporator 9 for flash evaporation, sending the benzene steam after flash evaporation to a crude benzene buffer tank 1 for bubbling cooling, and taking the benzene steam as a part of a crude benzene raw material; the liquid after flash evaporation falls on the tray on the uppermost layer and flows downwards as reflux liquid, and the crude benzene raffinate flowing to the bottom of the raffinate evaporator 9 is evaporated under the heating action of a heater 10; the evaporated benzene vapor flows upwards, the reflux liquid is subjected to gas stripping refining, light components are sent to the crude benzene buffer tank 1 along with crude benzene residual liquid vapor for bubbling cooling, and heavy components, namely crude benzene flash residual liquid, are continuously discharged from the bottom of the residual liquid evaporator 9.
70-90% of the external crude benzene raw materials are sent to a crude benzene buffer tank 1, and the other 10-30% of the crude benzene raw materials are sent to a pre-fractionating tower 11.
The pre-fractionation tower 11 adopts decompression operation, the pressure at the top of the tower is 45-55 KPa, and the vacuum degree of the pre-fractionation tower is generated by a pre-fractionation tower vacuum unit; the pre-fractionation tower reboiler 16 uses heat transfer oil as a heat source.
The segmented evaporator 5 is operated at high pressure, and the operating pressure is 2.5-3.5 MPa; the raffinate 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 jet mixer 8, a raffinate evaporator 9, a prefractionator 11, a prefractionator reflux tank 13, a prefractionator reflux pump 14 and a prefractionator bottom pump 15; the prefractionator 11 is internally provided with a plurality 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 prefractionat; 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 prefractionation tower circulating pipeline, a prefractionation tower bottom pump 15, a heavy benzene liquid outlet and a prefractionation tower reboiler 16 are sequentially arranged on the prefractionation tower circulating pipeline along the liquid flowing direction, and the heavy benzene liquid 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 vapor outlet is connected with a light benzene oil vapor condensate inlet on a prefractionator reflux groove 13 through the tower top cooler 12; a tail gas outlet is arranged at the top of the prefractionation tower reflux groove 13, a light benzene outlet is arranged at the bottom of the prefractionation tower reflux groove, 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 prefractionation tower 11 and a light benzene reflux inlet of the sectional evaporator 5 through a light benzene reflux pipeline, and a prefractionation tower reflux pump 14 is arranged on the light benzene reflux pipeline; a demister 51, a plurality of layers of tower trays and a partition plate 52 are sequentially arranged in the segmented evaporator 5 from top to bottom, wherein the partition plate 52 is arranged at the lower part of the segmented evaporator 5 and partitions the internal space of the segmented evaporator 5 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 partition plate 52; the top of the segmented evaporator 5 is provided with a crude benzene gas outlet, one side of the segmented evaporator 5 above the tray 18 at the uppermost layer is provided with a light benzene reflux inlet, one side of the segmented evaporator 5 between the tray 17 at the lowermost layer and the partition plate 52 is provided with a gas-liquid mixture inlet and a light benzene reflux outlet, the same side of the segmented evaporator 5 below the partition plate 52 is provided with a crude benzene gas outlet, and the gas-liquid mixture inlet, the light benzene reflux outlet and the crude benzene gas outlet are respectively connected with the reflux injection mixer 8; the other side of the segmented evaporator 5 below the isolation plate 52 is provided with a circulating liquid inlet, the bottom of the segmented evaporator 5 is provided with a crude benzene raffinate outlet and a circulating liquid outlet, and the crude benzene raffinate outlet is connected with a crude benzene raffinate inlet at the upper part of the raffinate evaporator 9 through a crude benzene raffinate pipeline; the circulating liquid outlet is connected with the circulating liquid inlet through a circulating liquid pipeline, and a reboiler 4 and a segmented 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; a crude benzene raffinate steam outlet is arranged at the top of the raffinate evaporator 9 and connected with a crude benzene raffinate steam inlet on the crude benzene buffer tank 1, a plurality of layers of tower trays are arranged in the raffinate evaporator 9, a heater 10 is arranged at the lower part of the raffinate evaporator, and a crude benzene flash raffinate outlet arranged at the bottom of the raffinate evaporator is connected with a crude benzene flash raffinate output pipeline; crude benzene raw materials entry linkage crude benzene raw materials pipeline is established at 1 top of crude benzene buffer slot, and the bottom is established the crude benzene export and is passed through crude benzene pipeline and connect pre-evaporator 3, establishes hydrogenation raw materials pump 2 on the crude benzene pipeline.
The raffinate evaporator 9 is a vertical evaporator, wherein 3-5 layers of tower trays are arranged.
The design principle of the crude benzene evaporation process and system in the benzene hydrogenation reaction system is as follows: in order to improve the heavy removal effect of crude benzene evaporation and reduce energy consumption, the working mode of the sectional 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 sectional evaporator 5 is greatly improved. When the light benzene is obtained by adopting a crude benzene pre-fractionation mode, the reflux amount of the light benzene only accounts for 10-30% of the total evaporation amount of the crude benzene raw material, and compared with the mode of obtaining the light benzene by pre-fractionating the crude benzene in the conventional crude benzene evaporation process and then evaporating, the energy consumption is obviously reduced. In order to reduce the benzene content in the crude benzene flash evaporation residual liquid after the flash evaporation of the crude benzene residual liquid to the maximum extent, the empty tank of the residual liquid flash evaporation tank is changed into a residual liquid evaporator 9 with a heater 10 and a plurality of trays, and the crude benzene residual liquid is changed into gas stripping rectification from the existing flash evaporation mode.
The crude benzene evaporation system is obtained by a crude benzene pre-fractionation mode based on light benzene, and if an outsourcing light benzene product is adopted, the operation of the pre-fractionation tower 11 can be directly omitted.
The heater 10 of the raffinate evaporator 9 can adopt heat conducting oil as a heating medium, and can also adopt other media meeting the conditions for heating.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention.
Claims (8)
1. A process for evaporating crude benzene in a benzene hydrogenation reaction system comprises a prefractionator and a sectional evaporator; the method is characterized in that the sectional evaporator adopts light benzene reflux, and the light benzene for reflux adopts an outsourcing light benzene product or light benzene fractionated by crude benzene through a prefractionating tower.
2. The process of claim 1, wherein the crude benzene evaporation system further comprises a raffinate evaporator, wherein the raffinate evaporator is provided with a plurality of trays, and the bottom of the raffinate evaporator is provided with a heater.
3. The process of claim 1 or 2, wherein the crude benzene evaporation system comprises a prefractionator, a prefractionator reflux drum, a staged evaporator, a raffinate evaporator, a crude benzene buffer drum; the crude benzene evaporation process specifically comprises the following steps:
1) the external crude benzene raw material enters a crude benzene evaporation system and then is divided into two paths, wherein most of the crude benzene raw material is sent to a crude benzene buffer tank, and the small part of the crude benzene raw material is sent to a pre-fractionating tower;
2) in a prefractionator, performing pre-separation of light components and heavy components on a crude benzene raw material, condensing and cooling tower top light benzene oil vapor by a tower top condenser, and then feeding the condensed and cooled tower top light benzene oil vapor into a prefractionator reflux groove; extracting light benzene in the reflux tank of the prefractionator by using a prefractionator reflux pump, sending one part of the light benzene back to the top of the prefractionator as reflux, and sending the other part of the light benzene back to a sectional evaporator as light benzene reflux;
3) heavy components at the bottom of the prefractionator are pumped out by a prefractionator bottom pump, and a part of the heavy components are circularly heated by a prefractionator reboiler and then return to the bottom of the prefractionator to provide heat required by prefractionation; the other part is taken as a heavy benzene product and sent out after being cooled;
4) circulating hydrogen passes through a jet mixer of the pre-evaporator at a high speed to form negative pressure, so that crude benzene liquid pumped by a hydrogenation raw material flows in the pre-evaporator at a high speed in a circulating manner, 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 passes through the jet mixer of the sectional evaporator at a high speed to form negative pressure as power, so that a closed cycle is formed between the bottom of the sectional evaporator and a reboiler, heat of the crude benzene gas after hydrogenation reaction is utilized, heat is supplied through the reboiler, light benzene flowing back from the top of the sectional evaporator is completely gasified in the sectional evaporator, and the gasification amount is controlled by keeping the liquid level at the bottom of the sectional evaporator balanced and stable;
6) a plurality of layers of tower trays are arranged in the segmented evaporator, and the inside of the segmented evaporator is partitioned into an upper space and a lower space by a partition plate arranged at the bottom; the sectional 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 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 at high speed, so that light benzene reflux liquid falling onto the isolation plate from the top of the sectional evaporator is sucked; after primary mixing mass transfer and heat transfer are carried out on the light benzene reflux liquid and the crude benzene steam, the light benzene reflux liquid enters the upper space of the sectional evaporator for gas-liquid separation, the separated liquid falls back to the isolation plate, flows into the lower space of the sectional evaporator fully through the communicating pipe and falls into a liquid storage tank at the bottom; the separated gas flows upwards, and is subjected to mass transfer and heat transfer with the light benzene liquid flowing from the top through a plurality of layers of tower trays, and finally is sent to a hydrogenation pre-reactor after fog drops are removed by a mist catcher at the top of the sectional evaporator;
7) sending the crude benzene residual liquid continuously discharged from the bottom of the sectional evaporator to a residual liquid evaporator for flash evaporation, sending the benzene steam after flash evaporation to a crude benzene buffer tank for bubbling cooling, and taking the benzene steam as a part of a crude benzene raw material; the liquid after flash evaporation falls on the tray on the uppermost layer and flows downwards as reflux liquid, and the crude benzene residual liquid flowing to the bottom of the residual liquid evaporator is evaporated under the heating action of a heater; the evaporated benzene vapor flows upwards, the reflux liquid is subjected to gas stripping refining, light components are sent to the crude benzene buffer tank along with crude benzene residual liquid vapor for bubbling cooling, and heavy components, namely crude benzene flash residual liquid, are continuously discharged from the bottom of the residual liquid evaporator.
4. The process of claim 3, wherein 70-90% of the crude benzene raw material is fed to the crude benzene buffer tank, and the other 10-30% of the crude benzene raw material is fed to the pre-fractionation tower.
5. The process for evaporating the crude benzene in the benzene hydrogenation reaction system according to claim 3, wherein the pre-fractionation tower is operated under reduced pressure, the pressure at the top of the tower is 45-55 KPa, and the vacuum degree of the pre-fractionation tower is generated by a pre-fractionation tower vacuum unit; the reboiler of the pre-fractionating tower adopts heat conducting oil as a heat source.
6. The process for evaporating crude benzene in the benzene hydrogenation reaction system according to claim 3, wherein the staged evaporator is operated at high pressure, and the operating pressure is 2.5-3.5 MPa; the raffinate evaporator is operated at low pressure, and the operating pressure is 0.1-0.3 MPa.
7. The crude benzene evaporation system in the benzene hydrogenation reaction system for realizing any one of the processes of claims 1-6, 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 pre-fractionating tower reflux tank, a pre-fractionating tower reflux pump and a pre-fractionating tower bottom pump; the pre-fractionating tower is internally provided with a plurality of layers of tower trays, the top of the pre-fractionating tower is provided with a light benzene oil vapor outlet, the upper part of the pre-fractionating tower is provided with a light benzene reflux liquid inlet, the middle part of the pre-fractionating tower is provided with a crude benzene liquid inlet, the lower part of the pre-fractionating tower is provided with a circulating liquid inlet, and the bottom of the; 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 prefractionation tower circulating pipeline, a prefractionation tower bottom pump, a heavy benzene liquid outlet and a prefractionation tower reboiler are sequentially arranged on the prefractionation tower circulating pipeline along the liquid flowing direction, and the heavy benzene liquid outlet is connected with a heavy benzene product pipeline; the prefractionator is provided with a tower top cooler, and a light benzene oil vapor outlet is connected with a light benzene oil vapor condensate inlet on a prefractionator reflux groove through the tower top cooler; the top of the reflux tank of the prefractionating tower is provided with a tail gas outlet, the bottom of the reflux tank of the prefractionating tower 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 prefractionating tower and a light benzene reflux inlet of the sectional evaporator through light benzene reflux pipelines, and the light benzene reflux pipeline is provided with a prefractionating tower reflux pump; the sectional evaporator is internally provided with a demister, a plurality of layers of tower trays and a partition plate in sequence from top to bottom, wherein the partition plate is arranged at the lower part of the sectional evaporator and partitions the internal space of the sectional evaporator 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 partition plate; the top of the sectional evaporator is provided with a crude benzene gas outlet, one side of the sectional evaporator above the tray on the uppermost layer is provided with a light benzene reflux inlet, one side of the sectional evaporator between the tray on the lowermost layer and the partition plate is provided with a gas-liquid mixture inlet and a light benzene reflux outlet, the same side of the sectional evaporator below the partition plate is provided with a crude benzene gas outlet, and the gas-liquid mixture inlet, the light benzene reflux outlet and the crude benzene gas outlet are respectively connected with a reflux liquid jet mixer; the other side of the segmented evaporator below the partition plate is provided with a circulating liquid inlet, the bottom of the segmented evaporator is provided with a crude benzene raffinate outlet and a circulating liquid outlet, and the crude benzene raffinate outlet is connected with a crude benzene raffinate inlet at the upper part of the raffinate evaporator through a crude benzene raffinate pipeline; the circulating liquid outlet is connected with the circulating liquid inlet through a circulating liquid pipeline, and a reboiler and a segmented evaporator jet mixer are sequentially arranged on the circulating liquid pipeline along the liquid flowing direction; the pre-evaporator is respectively connected with the jet mixer of the sectional evaporator, the reboiler and the jet mixer of the pre-evaporator, and the jet mixer of the pre-evaporator is provided with a circulating hydrogen inlet and a hydrogenated crude benzene gas-liquid mixture outlet; a crude benzene raffinate steam outlet is arranged at the top of the raffinate evaporator and connected with a crude benzene raffinate steam inlet on the crude benzene buffer tank, a multilayer tower tray is arranged in the raffinate evaporator, a heater is arranged at the lower part of the raffinate evaporator, and a crude benzene flash raffinate outlet arranged at the bottom of the raffinate evaporator is connected with a crude benzene flash raffinate output pipeline; crude benzene raw materials entry linkage crude benzene raw materials pipeline is established at crude benzene dashpot top, and the bottom is established the crude benzene export and is passed through crude benzene pipeline and connect the pre-evaporator, establishes hydrogenation raw materials pump on the crude benzene pipeline.
8. The system for evaporating crude benzene in a benzene hydrogenation reaction system according to claim 7, wherein the raffinate evaporator is a vertical evaporator provided with 3-5 trays.
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