CN212504657U - System for hydrogenation and extractive distillation of crude benzene - Google Patents
System for hydrogenation and extractive distillation of crude benzene Download PDFInfo
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Abstract
The utility model relates to a crude benzene hydrogenation and extractive distillation system, which comprises a prefractionating tower, a hydrogenation unit, a stabilizing tower and an extractive distillation unit; the pre-fractionating tower, the hydrogenation unit, the stabilizing tower and the extractive distillation unit are connected in sequence, or the hydrogenation unit, the stabilizing tower, the pre-fractionating tower and the extractive distillation unit are connected in sequence; the hydrogenation unit consists of a pre-evaporator, a sectional evaporator, a pre-reactor, a hydrogenation furnace, a main reactor and a high-pressure separator which are connected in sequence, and the hydrogenation unit is also provided with a circulating hydrogen pipeline; the extractive distillation unit consists of an extractive distillation tower and a solvent recovery tower. The utility model shortens the process flow, and realizes the purposes of improving the yield of pure benzene, improving economic benefit, saving energy and reducing consumption.
Description
Technical Field
The utility model relates to a crude benzene hydrofining technical field especially relates to a crude benzene hydrogenation and extractive distillation's system.
Background
The main components of crude benzene in the coking industry are benzene, toluene and xylene, and in addition, the crude benzene also contains 5-10% of unsaturated compounds which are cyclic hydrocarbon and straight-chain olefin with one or two double bonds, and are easy to generate polymerization reaction, and the boiling points of some unsaturated compounds, sulfides and nitrogen-containing compounds are similar to the boiling point temperature of corresponding benzene products, so that the unsaturated compounds, sulfides and nitrogen-containing compounds cannot be separated by a 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 separated and removed H after hydrogenation saturation2S、NH3And H2And O, the residual hydrogenated oil can be easily used for producing high-quality benzene, toluene and xylene by an extractive distillation mode.
The crude benzene hydrofining process has small production pollution and the product quality can be comparable to petroleum benzene, so the crude benzene refining in the coking industry at present is mainly low-pressure crude benzene hydrofining. The crude benzene hydrofining is divided into two basic modes of liquid-phase-gas-phase hydrogenation and two-stage gas-phase hydrogenation, and the two-stage gas-phase hydrogenation is mainly used.
The gas phase hydrogenation process system of crude benzene consists of a hydrogenation unit and an extractive distillation unit; the hydrogenation unit in the hydrogenation process system introduced from Germany is used for directly gasifying and hydrogenating crude benzene, i.e. the crude benzene as raw material is mixed with circulating hydrogen, passed through the processes of pre-evaporator, stage evaporator, removing heavy evaporation, pre-hydrogenation by pre-reactor and heating to defined temp. by hydrogenation furnaceRemoving the catalyst from the main reactor to carry out hydrogenation reaction; after the gas after reaction exchanges heat with the crude benzene raw material and is cooled, the obtained hydrogenated oil is sent into a high-pressure separator for gas-liquid separation; the circulating hydrogen is sent by a circulating fan to be mixed with the crude benzene raw material for recycling; the waste water and hydrogenated oil produced after hydrogenation are separated into oil and water due to the difference of specific gravity, the waste water is sent to an oil depot, the hydrogenated oil without circulating hydrogen and waste water is sent to a stabilizing tower, and H-containing water produced after hydrogenation is released2S、NH3The waste gas is sent to a gas pipeline, and the pure hydrogenated oil containing benzene, toluene and xylene is sent to an extractive distillation unit; the extraction process using N-formyl morpholine and the like as an extracting agent comprises two benzene extraction processes, namely, only benzene and toluene can be subjected to extractive distillation, hydrogenated oil is firstly sent to a pre-distillation tower for pre-distillation, the hydrogenated oil is separated into benzene, toluene fraction (namely BT fraction) and xylene fraction, the BT fraction is sent to an extractive distillation tower for non-aromatic hydrocarbon removal, non-aromatic hydrocarbon is extracted from the tower top, rich solvent (mixture of benzene, toluene and the extracting agent) is sent to a solvent recovery tower at the tower bottom, BT component is extracted from the tower top of the solvent recovery tower, poor solvent at the tower bottom is returned to the extractive distillation tower for recycling, the BT fraction is distilled and separated into pure benzene and toluene through the benzene-toluene tower, and the xylene fraction obtained from the pre-distillation tower is sent to a xylene distillation tower for distillation, so that xylene products are.
In the benzene hydrogenation operation, some domestic enterprises consider that the removal degree of the sectional evaporator in the original process flow is not enough, which influences the service life of the hydrogenation catalyst, so the process is improved; before gas-phase hydrogenation, the crude benzene is passed through a prefractionator to remove the high-boiling fraction (heavy benzene) in the crude benzene by means of distillation so as to obtain light benzene, then the light benzene is undergone the process of gasification hydrogenation.
The crude benzene raw material contains about 78% of benzene, 11.4% of toluene and 1.8% of xylene, and the price of the benzene products in 2020 is approximately as follows: 4397 yuan/t crude benzene, 5654 yuan/t pure benzene, 4652 yuan/t toluene, 4714 yuan/t xylene, 4219 yuan/t non-aromatic hydrocarbon and 2900 yuan/t heavy benzene; it can be seen that the prices of toluene and xylene are much lower than pure benzene. In order to obtain a small amount of toluene and xylene products, the above process needs repeated distillation operation, and the operation cost is very high, thus seriously affecting the economic benefit of enterprises. At present, with the design and the operation of a heavy benzene hydrogenation system, fractions after toluene and xylene can be completely sold into the heavy benzene hydrogenation system, and only the benzene fractions are subjected to hydrogenation and extraction in the crude benzene hydrogenation process, so that the problem of heavy removal of a hydrogenation unit is solved, and the cost increase caused by frequent repeated distillation is avoided.
Disclosure of Invention
The utility model provides a crude benzene hydrogenation and extractive distillation's system, before hydrogenation earlier through the prefractionator to the whole excision of heavy ends behind the toluene, only carry out single benzene hydrogenation operation and single benzene extractive distillation to the benzene fraction in the crude benzene, perhaps after crude benzene hydrogenation operation, through the prefractionator to the whole excision of heavy ends behind the toluene outsourcing of heavy ends behind the toluene, only carry out single benzene extractive distillation to benzene hydrogenation oil; thereby shortening the process flow and realizing the purposes of improving the yield of pure benzene, improving economic benefit, saving energy and reducing consumption.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a system for hydrogenation and extractive distillation of crude benzene comprises a prefractionator, a hydrogenation unit, a stabilizer and an extractive distillation unit; the pre-fractionating tower, the hydrogenation unit, the stabilizing tower and the extractive distillation unit are connected in sequence, or the hydrogenation unit, the stabilizing tower, the pre-fractionating tower and the extractive distillation unit are connected in sequence; the hydrogenation unit consists of a pre-evaporator, a sectional evaporator, a pre-reactor, a hydrogenation furnace, a main reactor and a high-pressure separator which are connected in sequence, and the hydrogenation unit is also provided with a circulating hydrogen pipeline; the extractive distillation unit consists of an extractive distillation tower and a solvent recovery tower.
A system for hydrogenation and extractive distillation of crude benzene comprises a prefractionation tower, a hydrogenation unit, a stabilization tower and an extractive distillation unit which are connected in sequence; the top of the prefractionator is provided with a benzene fraction outlet which is connected with a circulating hydrogen pipeline at the upstream of a pre-evaporator in the hydrogenation unit through a benzene fraction pipeline; the middle part of the prefractionation tower is provided with a crude benzene liquid inlet, and the bottom of the prefractionation tower is provided with a crude benzene residual liquid outlet; the pre-evaporator is provided with a raw material inlet connected with one end of a circulating hydrogen pipeline, and the top of the high-pressure separator is provided with a circulating hydrogen outlet connected with the other end of the circulating hydrogen pipeline; the middle part of the high-pressure separator is provided with a hydrogenated oil outlet which is connected with a hydrogenated oil inlet of the stabilizing tower, and the bottom of the high-pressure separator is provided with a wastewater outlet; the top of the stabilizing tower is provided with a waste gas outlet, and the bottom of the stabilizing tower is provided with a hydrogenated oil outlet which is connected with a hydrogenated oil inlet of an extractive distillation tower in the extractive distillation unit; the top of the extractive distillation tower is provided with a non-aromatic hydrocarbon outlet, the upper part of the extractive distillation tower is provided with a solvent inlet, and the bottom of the extractive distillation tower is provided with a rich solvent outlet which is connected with a rich solvent inlet of the solvent recovery tower; the top of the solvent recovery tower is provided with a pure benzene outlet, and the bottom of the solvent recovery tower is provided with a poor solvent outlet which is connected with a solvent inlet of the extractive distillation tower.
A system for hydrogenation and extractive distillation of crude benzene comprises a hydrogenation unit, a stabilizing tower, a prefractionation tower and an extractive distillation unit which are connected in sequence; the pre-evaporator is provided with a raw material inlet which is connected with one end of a circulating hydrogen pipeline, and the circulating hydrogen pipeline close to the pre-evaporator is provided with a crude benzene liquid inlet; the top of the high-pressure separator is provided with a circulating hydrogen outlet which is connected with the other end of the circulating hydrogen pipeline; a heavy residual liquid outlet is arranged at the bottom of the sectional evaporator; the middle part of the high-pressure separator is provided with a hydrogenated oil outlet which is connected with a hydrogenated oil inlet of the stabilizing tower, and the bottom of the high-pressure separator is provided with a wastewater outlet; the top of the stabilizing tower is provided with a waste gas outlet, and the bottom of the stabilizing tower is provided with a hydrogenated oil outlet which is connected with a hydrogenated oil inlet in the middle of the prefractionating tower; the bottom of the prefractionator is provided with a hydrogenated oil residual liquid outlet, and the top is provided with a benzene hydrogenated oil outlet which is connected with a benzene hydrogenated oil inlet of an extractive distillation tower in the extractive distillation unit; the top of the extractive distillation tower is provided with a non-aromatic hydrocarbon outlet, the upper part of the extractive distillation tower is provided with a solvent inlet, and the bottom of the extractive distillation tower is provided with a rich solvent outlet which is connected with a rich solvent inlet of the solvent recovery tower; the top of the solvent recovery tower is provided with a pure benzene outlet, and the bottom of the solvent recovery tower is provided with a poor solvent outlet which is connected with a solvent inlet of the extractive distillation tower.
Compared with the prior art, the beneficial effects of the utility model are that:
1) before hydrogenation, heavy components after toluene are completely cut off through a prefractionator, and only benzene fraction in crude benzene is subjected to single benzene hydrogenation operation and single benzene extractive distillation, or after the crude benzene hydrogenation operation, the heavy components after toluene are completely cut off through the prefractionator and are sent out, and only benzene hydrogenated oil is subjected to single benzene extractive distillation; taking the heavy components after the toluene as raw materials and completely delivering the heavy benzene hydrofining system; compared with the conventional operation of repeatedly distilling to obtain a small amount of toluene and xylene products, the method greatly shortens the process flow, and achieves the purposes of improving the yield of pure benzene, improving economic benefits, saving energy and reducing consumption;
2) for the technical scheme that heavy components after toluene are completely cut off before hydrogenation, a sectional evaporator in a hydrogenation unit only plays a role in evaporation, and does not need to play a role in removing heavy components, so that the loss of benzene fractions is reduced, and the service life of a hydrogenation catalyst is prolonged;
3) compared with the conventional extractive distillation unit, the utility model saves a prefractionation tower, a toluene tower and a xylene tower, and reduces the equipment investment and the operation cost;
4) according to statistics, to the benzene hydrogenation system of same scale, adopt the utility model discloses the output of back pure benzene can improve more than 10%, and economic benefits is showing.
Drawings
FIG. 1 is a schematic structural diagram of a system for hydrogenation and extractive distillation of crude benzene according to the present invention.
FIG. 2 is a schematic structural diagram II of a system for hydrogenation and extractive distillation of crude benzene according to the present invention.
In the figure: 1. prefractionation tower 2, pre-evaporator 3, sectional evaporator 4, pre-reactor 5, hydrogenation furnace 6, main reactor 7, high-pressure separator 8, stabilizing tower 9, extractive distillation tower 10 and solvent recovery tower
Detailed Description
The following description of the embodiments of the present invention will be made with reference to the accompanying drawings:
the utility model relates to a crude benzene hydrogenation and extractive distillation system, which comprises a prefractionation tower 1, a hydrogenation unit, a stabilization tower 8 and an extractive distillation unit; the pre-fractionating tower 1, the hydrogenation unit, the stabilizing tower 8 and the extractive distillation unit are connected in sequence, or the hydrogenation unit, the stabilizing tower 8, the pre-fractionating tower 1 and the extractive distillation unit are connected in sequence; the hydrogenation unit consists of a pre-evaporator 2, a sectional evaporator 3, a pre-reactor 4, a hydrogenation furnace 5, a main reactor 6 and a high-pressure separator 7 which are connected in sequence, and the hydrogenation unit is also provided with a circulating hydrogen pipeline; the extractive distillation unit is composed of an extractive distillation column 9 and a solvent recovery column 10.
As shown in fig. 1, the system for hydrogenation and extractive distillation of crude benzene of the present invention comprises a prefractionator 1, a hydrogenation unit, a stabilizer 8 and an extractive distillation unit which are connected in sequence; the hydrogenation unit consists of a pre-evaporator 2, a sectional evaporator 3, a pre-reactor 4, a hydrogenation furnace 5, a main reactor 6 and a high-pressure separator 7 which are connected in sequence, and the hydrogenation unit is also provided with a circulating hydrogen pipeline; the extractive distillation unit consists of an extractive distillation tower 9 and a solvent recovery tower 10; the top of the prefractionator 1 is provided with a benzene fraction outlet which is connected with a circulating hydrogen pipeline at the upstream of a pre-evaporator 2 in a hydrogenation unit through a benzene fraction pipeline; the middle part of the prefractionator 1 is provided with a crude benzene liquid inlet, and the bottom is provided with a crude benzene raffinate outlet; the pre-evaporator 2 is provided with a raw material inlet connected with one end of a circulating hydrogen pipeline, and the top of the high-pressure separator 7 is provided with a circulating hydrogen outlet connected with the other end of the circulating hydrogen pipeline; the middle part of the high-pressure separator 7 is provided with a hydrogenated oil outlet which is connected with a hydrogenated oil inlet of the stabilizing tower 8, and the bottom part is provided with a wastewater outlet; the top of the stabilizing tower 8 is provided with a waste gas outlet, and the bottom of the stabilizing tower 8 is provided with a hydrogenated oil outlet which is connected with a hydrogenated oil inlet of an extractive distillation tower 9 in the extractive distillation unit; the top of the extractive distillation tower 9 is provided with a non-aromatic hydrocarbon outlet, the upper part is provided with a solvent inlet, and the bottom is provided with a rich solvent outlet which is connected with a rich solvent inlet of the solvent recovery tower 10; the top of the solvent recovery tower 10 is provided with a pure benzene outlet, and the bottom is provided with a poor solvent outlet which is connected with a solvent inlet of the extractive distillation tower 9.
As shown in fig. 2, the system for crude benzene hydrogenation and extractive distillation of the present invention comprises a hydrogenation unit, a stabilizer 8, a prefractionation column 1 and an extractive distillation unit which are connected in sequence; the hydrogenation unit consists of a pre-evaporator 2, a sectional evaporator 3, a pre-reactor 4, a hydrogenation furnace 5, a main reactor 6 and a high-pressure separator 7 which are connected in sequence, and the hydrogenation unit is also provided with a circulating hydrogen pipeline; the extractive distillation unit consists of an extractive distillation tower 9 and a solvent recovery tower 10; the pre-evaporator 2 is provided with a raw material inlet which is connected with one end of a circulating hydrogen pipeline, and the circulating hydrogen pipeline close to the pre-evaporator 2 is provided with a crude benzene liquid inlet; the top of the high-pressure separator 7 is provided with a circulating hydrogen outlet which is connected with the other end of the circulating hydrogen pipeline; the bottom of the sectional evaporator 3 is provided with a heavy residual liquid outlet; the middle part of the high-pressure separator 7 is provided with a hydrogenated oil outlet which is connected with a hydrogenated oil inlet of the stabilizing tower 8, and the bottom part is provided with a wastewater outlet; the top of the stabilizing tower 8 is provided with a waste gas outlet, and the bottom of the stabilizing tower 8 is provided with a hydrogenated oil outlet which is connected with a hydrogenated oil inlet in the middle of the prefractionator 1; the bottom of the prefractionator 1 is provided with a hydrogenated oil residual liquid outlet, and the top is provided with a benzene hydrogenated oil outlet which is connected with a benzene hydrogenated oil inlet of an extractive distillation tower 9 in an extractive distillation unit; the top of the extractive distillation tower 9 is provided with a non-aromatic hydrocarbon outlet, the upper part is provided with a solvent inlet, and the bottom is provided with a rich solvent outlet which is connected with a rich solvent inlet of the solvent recovery tower 10; the top of the solvent recovery tower 10 is provided with a pure benzene outlet, and the bottom is provided with a poor solvent outlet which is connected with a solvent inlet of the extractive distillation tower 9.
The working principle of the crude benzene hydrogenation and extractive distillation system is as follows: before hydrogenation, heavy components after toluene are completely cut off and sent out through a prefractionator 1, and only benzene fraction in crude benzene is subjected to single benzene hydrogenation and single benzene extractive distillation; or after the hydrogenation operation of the crude benzene, all heavy components after toluene are cut off and sent out through the prefractionator 1, and only the benzene hydrogenation oil is subjected to single benzene extractive distillation.
The technical process of the crude benzene hydrogenation and extractive distillation system is as follows:
1) before hydrogenation, the crude benzene raw material is sent to a prefractionator 1 for prefractionation, crude benzene residual liquid discharged from the bottom of the prefractionator 1 contains heavy components after toluene, and benzene fraction is obtained at the top of the tower;
2) the benzene fraction is sent to a hydrogenation unit to be mixed with circulating hydrogen, then is evaporated by a pre-evaporator 2 and a sectional evaporator 3, is pre-hydrogenated by a pre-reactor 4, is heated to a set temperature by a hydrogenation furnace 5, and then is sent to a main reactor 6 for hydrogenation reaction; exchanging heat between the gas generated after the reaction and the benzene fraction in the pre-evaporator 2 and the sectional evaporator 3, and cooling to obtain benzene hydrogenated oil;
3) sending the benzene hydrogenated oil into a high-pressure separator 7 for gas-liquid separation, and sending circulating hydrogen by a circulating fan to be mixed with the benzene fraction subjected to pre-fractionation for recycling; meanwhile, the waste water generated after hydrogenation and the benzene hydrogenated oil are subjected to oil-water separation, and the waste water is sent out; the benzene hydrogenated oil from which the circulating hydrogen and the wastewater are removed is sent to a stabilization tower 8;
4) in the stabilizer column 8, the benzene hydrogenated oil releases H-containing oil produced by hydrogenation2S、NH3The obtained pure hydrogenated oil is sent to an extractive distillation unit;
5) in the extractive distillation unit, adopting an extractive distillation tower 9 to extract benzene hydrogenated oil by an extractant; non-aromatic hydrocarbons are extracted from the tower top, and rich solvent, namely the mixture of benzene and the extractant, at the tower bottom is sent to a solvent recovery tower 10; pure benzene products are extracted from the top of the solvent recovery tower 10, and the poor solvent at the bottom of the tower returns to the extractive distillation tower 9 for recycling.
The technical process of the other crude benzene hydrogenation and extractive distillation system is as follows:
1) mixing raw material crude benzene and circulating hydrogen, removing heavy evaporation through a pre-evaporator 2 and a sectional evaporator 3, pre-hydrogenating through a pre-reactor 4, heating to a set temperature through a hydrogenation furnace 5, and then performing hydrogenation reaction in a main reactor 6; exchanging heat between the gas generated after the reaction and the crude benzene raw material in a pre-evaporator 2 and a sectional evaporator 3, and cooling to obtain hydrogenated oil;
2) the hydrogenated oil is sent into a high-pressure separator 7 for gas-liquid separation, and the circulating hydrogen is sent by a circulating fan to be mixed with the raw material crude benzene for recycling; meanwhile, the waste water generated after hydrogenation is separated from the hydrogenated oil in oil-water mode, and the waste water is sent out; the hydrogenated oil from which the circulating hydrogen and the wastewater are removed is sent to a stabilization tower 8;
3) in the stabilizer column 8, the hydrogenated oil releases H-containing gas produced by the hydrogenation2S、NH3The obtained pure hydrogenated oil containing benzene, toluene and xylene;
4) the pure hydrogenated oil enters a prefractionator 1 for prefractionation, the hydrogenated oil residual liquid at the bottom of the tower contains heavy components after toluene, benzene hydrogenated oil only containing benzene is obtained at the top of the tower and is sent to an extractive distillation unit;
5) in the extractive distillation unit, adopting an extractive distillation tower 9 to extract benzene hydrogenated oil by an extractant; non-aromatic hydrocarbons are extracted from the tower top, and rich solvent, namely the mixture of benzene and the extractant, at the tower bottom is sent to a solvent recovery tower 10; pure benzene products are extracted from the top of the solvent recovery tower 10, and the poor solvent at the bottom of the tower returns to the extractive distillation tower 9 to be used as an extracting agent for recycling.
The extracting agent is N-formyl morpholine, sulfolane or a composite extracting agent containing N-formyl morpholine and sulfolane.
And the crude benzene raffinate containing heavy components after toluene is used as a raw material and sent to a heavy benzene hydrofining system.
And the hydrogenated oil residual liquid containing the heavy components after the toluene is used as a raw material and is sent to a heavy benzene hydrofining system.
The above, only be the concrete implementation of the preferred embodiment of the present invention, but the protection scope of the present invention is not limited thereto, and any person skilled in the art is in the technical scope of the present invention, according to the technical solution of the present invention and the utility model, the concept of which is equivalent to replace or change, should be covered within the protection scope of the present invention.
Claims (3)
1. A system for hydrogenation and extractive distillation of crude benzene is characterized by comprising a prefractionator, a hydrogenation unit, a stabilizer and an extractive distillation unit; the pre-fractionating tower, the hydrogenation unit, the stabilizing tower and the extractive distillation unit are connected in sequence, or the hydrogenation unit, the stabilizing tower, the pre-fractionating tower and the extractive distillation unit are connected in sequence; the hydrogenation unit consists of a pre-evaporator, a sectional evaporator, a pre-reactor, a hydrogenation furnace, a main reactor and a high-pressure separator which are connected in sequence, and the hydrogenation unit is also provided with a circulating hydrogen pipeline; the extractive distillation unit consists of an extractive distillation tower and a solvent recovery tower.
2. The system for hydrogenation and extractive distillation of crude benzene according to claim 1, comprising a prefractionating column, a hydrogenation unit, a stabilization column and an extractive distillation unit which are connected in sequence; the top of the prefractionator is provided with a benzene fraction outlet which is connected with a circulating hydrogen pipeline at the upstream of a pre-evaporator in the hydrogenation unit through a benzene fraction pipeline; the middle part of the prefractionation tower is provided with a crude benzene liquid inlet, and the bottom of the prefractionation tower is provided with a crude benzene residual liquid outlet; the pre-evaporator is provided with a raw material inlet connected with one end of a circulating hydrogen pipeline, and the top of the high-pressure separator is provided with a circulating hydrogen outlet connected with the other end of the circulating hydrogen pipeline; the middle part of the high-pressure separator is provided with a hydrogenated oil outlet which is connected with a hydrogenated oil inlet of the stabilizing tower, and the bottom of the high-pressure separator is provided with a wastewater outlet; the top of the stabilizing tower is provided with a waste gas outlet, and the bottom of the stabilizing tower is provided with a hydrogenated oil outlet which is connected with a hydrogenated oil inlet of an extractive distillation tower in the extractive distillation unit; the top of the extractive distillation tower is provided with a non-aromatic hydrocarbon outlet, the upper part of the extractive distillation tower is provided with a solvent inlet, and the bottom of the extractive distillation tower is provided with a rich solvent outlet which is connected with a rich solvent inlet of the solvent recovery tower; the top of the solvent recovery tower is provided with a pure benzene outlet, and the bottom of the solvent recovery tower is provided with a poor solvent outlet which is connected with a solvent inlet of the extractive distillation tower.
3. The system for hydrogenation and extractive distillation of crude benzene according to claim 1, comprising a hydrogenation unit, a stabilization column, a prefractionation column and an extractive distillation unit which are connected in sequence; the pre-evaporator is provided with a raw material inlet which is connected with one end of a circulating hydrogen pipeline, and the circulating hydrogen pipeline close to the pre-evaporator is provided with a crude benzene liquid inlet; the top of the high-pressure separator is provided with a circulating hydrogen outlet which is connected with the other end of the circulating hydrogen pipeline; a heavy residual liquid outlet is arranged at the bottom of the sectional evaporator; the middle part of the high-pressure separator is provided with a hydrogenated oil outlet which is connected with a hydrogenated oil inlet of the stabilizing tower, and the bottom of the high-pressure separator is provided with a wastewater outlet; the top of the stabilizing tower is provided with a waste gas outlet, and the bottom of the stabilizing tower is provided with a hydrogenated oil outlet which is connected with a hydrogenated oil inlet in the middle of the prefractionating tower; the bottom of the prefractionator is provided with a hydrogenated oil residual liquid outlet, and the top is provided with a benzene hydrogenated oil outlet which is connected with a benzene hydrogenated oil inlet of an extractive distillation tower in the extractive distillation unit; the top of the extractive distillation tower is provided with a non-aromatic hydrocarbon outlet, the upper part of the extractive distillation tower is provided with a solvent inlet, and the bottom of the extractive distillation tower is provided with a rich solvent outlet which is connected with a rich solvent inlet of the solvent recovery tower; the top of the solvent recovery tower is provided with a pure benzene outlet, and the bottom of the solvent recovery tower is provided with a poor solvent outlet which is connected with a solvent inlet of the extractive distillation tower.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115193082A (en) * | 2022-09-16 | 2022-10-18 | 旭阳工程有限公司 | Novel crude benzene hydrofining separation system and process |
| CN115193082B (en) * | 2022-09-16 | 2022-12-30 | 旭阳工程有限公司 | Crude benzene hydrofining separation process |
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