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    • 专利摘要:
    1 solvent from the raffinate solution and in the implementation of heavy non-aromatic carbon dioxide and extraction of aromatic carbon light hydrocarbons from a stream of light hydrocarbons to produce light extract and light raffinate solutions with solvent recovery from a light, raffinate solution, characterized in that, in order to improve the degree of separation, the heavy extract solution is fed to the extraction of aromatic hydrocarbons from a stream of light hydrocarbons, followed by separation from the obtained light raffinate solution of a selective solvent and a mixture of heavy aromatic and light non-aromatic hydrocarbons, the light extract extract The reservoir is subjected to extractive distillation, and the residual fraction thus obtained is subjected to distillation with the production of light aromatic hydrocarbons and a selective solvent; 2. A method according to claim 1, characterized in that sulpholane is used as a solvent in the extraction step from a heavy hydrocarbon stream. 3. Method according to paragraphs. 1 and 2, I differ by the fact that light hydrocarbon hydrocarbons have a boiling point of 50–170 ° C. 4. Method according to paragraphs. 1-3, about tl and the fact that heavy hydrocarbons have boiling temperature of 150-350 ° C. 5. Method according to paragraphs. 1-4, characterized in that the selective solvent is removed from raffinate solutions by washing with water.
    公开号:SU1122217A3
    申请号:SU813343295
    申请日:1981-10-14
    公开日:1984-10-30
    发明作者:Корнелис Джерард Костерз Уолтер
    申请人:Шелл Интернэшнл Рисерч Маатсхаппий,Б.В.(Фирма)；
    IPC主号:
    专利说明:

    This invention relates to a process for the simultaneous separation into heavy and light hydrocarbons of aromatic and non-aromatic hydrocarbons. Separation of aromatic and non-aromatic compounds present in a hydrocarbon stream is known by extracting aromatic compounds with a selective solvent, followed by separating the resulting extract phase into aromatic compounds and solvent by distillation. This method is very convenient for hydrocarbon streams that have lower boiling points than those of the selective solvent, since the difference in boiling points between the aromatic compounds and the sepative solvent results in a good separation by distilling 1. It is more difficult to separate the hydrocarbon streams having boiling temperatures close to or comparable to the boiling point of the selective solvent, since distillation separation of aromatics extracted from tako1: about the hydrocarbon stream and the selective solvent is impossible and more complicated methods are required to effect separation. . A known method for simultaneously separating heavy and light hydrocarbon streams into aromatic and non-aromatic hydrocarbons is that the heavy fraction stream is mixed with a selective solvent that has a boiling point in the boiling point of a light kg hydrocarbon stream, such as sulfolane, to produce heavy pc1 and pineapple extract solutions. The stream of light hydrocarbons is also mixed with a selective solvent and light extract and raffinate solutions are obtained. The raffinate solutions from each extraction stage are fed to solvent regeneration. The extract solutions from both stages are co-distilled to obtain light non-aromatic hydrocarbons, which are sent to the light hydrocarbon stage extraction stage, and heavy non-aromatic hydrocarbons, which are sent to stage extracting a stream of heavy hydrocarbons, as well as a residue that is distilled to obtain a solvent and aromatic hydrocarbons. The solvent is returned to the stage of extraction G2. However, in the known method, a clear separation of aromatic hydrocarbons into light and heavy ones is not achieved and such separation becomes impossible simply by distillation if the boiling point of heavy aromatic hydrocarbons overlaps with the solvent. The purpose of the invention is to improve the degree of separation. The goal is achieved by agreeing on the method of simultaneous separation of heavy and light hydrocarbon streams into aromatic and non-aromatic hydrocarbons by separate extraction of aromatic hydrocarbons from the heavy hydrocarbon stream with a solvent that has a boiling point above the boiling point of a light hydrocarbon stream, to obtain a heavy extract and raffinate solutions with solvent recovery from the raffinate solution and isolation of heavy non-aromatic hydrocarbons and Arranging the aromatic hydrocarbons to produce light extract and light raffinate solutions with solvent regeneration from a light raffinate solution, a heavy extract solution is fed to the extraction of aromatic hydrocarbons from a light hydrocarbons stream, followed by extracting a selective solvent from the light raffinate solution and a mixture of heavy aromatic and light nonaromatics hydrocarbon, the light extract solution is subjected to extractive distillation and the resulting The base fraction is distilled to give off light aromatic hydrocarbons and a selective solvent, which is recycled to the extraction stage of the heavy hydrocarbon stream. Sulfolane is used as a solvent at the extraction stage from a stream of heavy hydrocarbons. Light hydrocarbons have a boiling point of 50-170 ° C. T-hydrocarbons have a boiling point of 150-350 0. 31 The selective solvent is removed from raffinate solutions by washing with water. The use of sulfolane as a selective solvent is particularly preferred. However, other well-known selective solvents can be used, ngn1l1mer Furfural, phenol, sulfoxide, fatty acid alkylamides. Glycol, morpholine, and / or pyrrolidine-piperidine, lower polyapcylene glycols (such as dithylene-, triethchen-, tetraethylene-, and dipropylene glycol) can also be used. If necessary, the selective solvent may contain some amount of water, which has a favorable effect on the selectivity and solubility of the solvent. The stream of light carbohydrates according to the invention is a stream of hydrocarbons that have boiling temperatures lower than the boiling point (or boiling points of temperature) of the selective solvent used. A heavy hydrocarbons stream is a stream of hydrocarbons that have boiling points more than higher than the flow of light hydrocarbons. There may be some overlap in the temperature limits of the boiling streams of light and heavy hydrocarbons, however, it is desirable that there is no such overlap. The temperature limits of the boiling stream of heavy hydrocarbons can be lower or higher or comparable to the boiling point (or temperature range of the boiling point) of the selective solvent used. Preferred are light hydrocarbon streams that boil in a temperature range of 50 - i, such as gasoline fractions that can be directly distilled or obtained in the conversion process, in particular during catalytic reforming or in the pyrolysis process. Suitable heavy carbon and hydrocarbon streams are flows boiling within ISO-SSO C temperatures, such as kerosene, gas oils, which can be obtained as fractions by direct distillation or by 74 catalytic and non-catalytic processes, such as thermal cracking. , catalytic cracking and / or hydrocracking. Extraction from the streams is preferably multistage, any suitable equipment can be used. Extraction can, for example, be carried out using a series of mixing and asserting steps. The raffinate solutions from the extraction stages contain a small amount of a selective solvent that must be removed. It is preferable to rinse these solutions with water to remove the selective solvent. A heavy extract solution is used as an extraction solution for a stream of light hydrocarbons. As a result of this extraction, a raffinate solution is obtained, which includes all or most of the heavy aromatics and non-aromatics from the stream of light hydrocarbons (also called light non-aromatics) along with a small amount of selective solvent, and the extract phase contains all or most of the aromatic compounds from a stream of light hydrocarbons (also called light aromatics). The raffinate solution (after water injection) can, if necessary, be easily divided into light non-aromatic compounds and heavy aromatic compounds by distillation due to the difference in temperature limits between these fractions. The extract phase from the light hydrocarbon stream contains light aromatics and part of the light non-aromatics. It is subjected to extractive distillation to remove light non-aromatic compounds. In extractive distillation, hydrocarbons, at least partially in the vapor phase, are contacted with a liquid selective solvent, as a result of which the aromatic compounds are separated from non-aromatic compounds, the latter being removed as vapor. The extractive distillation fraction, which contains light non-aromatic compounds and a small amount of light aromatics, is removed from the top very easily condenses, water (if any) is removed, and the hydrocarbon is recycled to the extraction stage FROM light hydrocarbons .. Most light aromatic compounds remain in the residual fraction during extractive distillation. Light aromatic compounds are separated from the selective solvent by distilling the residual fraction obtained during the extractive distillation process. Distillation is very conveniently carried out in a separation column under reduced pressure. Preliminary separation vapor is introduced dp. Separation improvement taken from the top, which contains steam and light aromatic compounds, is cooled, water is separated, and light aromatic compounds (which can be recycled in the distillation column) are removed. The selective solvent, obtained after the removal of light aromatic compounds, is recycled to the stage of extraction of heavy hydrocarbons. Part of it can be recycled to the stage of extraction of aromatic hydrocarbons from a stream of light hydrocarbons and can be introduced into it along with the extract phase from the stage of extraction of heavy hydrocarbons and / or at the point closest to the entrance of the stream of light hydrocarbons to the second extractor (at the stage of extraction light hydrocarbons). selective solvent can also be introduced into the extractive distillation column. The drawing shows the implementation scheme of the proposed method. A stream of heavy hydrocarbons is introduced via line 1 into the first extractor 2, and the selective solvent is introduced into the first extractor via line 3. The raffinate phase is removed from the extractor by 4 and washed with water (not shown). The extract phase is removed via line 5 and introduced into the second extractor 6. A stream of light hydrocarbons is introduced into extractor 6 via line 7. The selective solvent is introduced into extractor 6 through line 8. The refined phase is removed from the extractor through line 9, washed with water (not shown) and distilled (not shown) to obtain heavy aromatic compounds and light non-aromatic compounds. The extract phase is withdrawn from the extractor via line 10 and sent through a heat exchanger 11 to the extractive distillation column 12. From there, the light fraction is sent to the separation tank via line 13. From this tank, the hydrocarbon is recycled to extractor b via line 14, and water is removed by line 15, the residue from the extractive distillation column 12 is directed along line 12 to distillation column 17 .. Steam is introduced into this column through line 18. The light fraction is sent through line 19 to the separation tank 20. From this tank d (light aromatics) is partially recycled to distillation column 17 through line 21 and partially removed through line 22, and water is removed through line 23. The regenerated selective solvent obtained as residue in distillation column 17 is removed from there by 24 and sent through heat exchangers 25 and 11 partially to extractor 2 and partially to extractor 6. Example 1.61 tons / day of a kerosene fraction with a boiling temperature range of 190-240 ° C, which contains 20% by weight of aromatic compounds, is introduced into extractor 2. Extractor p edstavl is a pin apparatus with a rotating disc. Extraction was carried out at C with a sul lolan introduced with poly3 in an amount of 555 tons / day. The raffinate phase is washed with water, giving 37 tons / day of heavy non-aromatic compounds (the content of aromatic compounds is below 1% by weight). Extractor 6 (which is also a rotary disk contact apparatus) is fed along three lines of 7,122 tons / day to lightly obtained by direct distillation of a hydrocarbon fraction with a boiling temperature range of 55-85 ° C, which contains 5% by weight of benzene. The extract phase from extractor 2 (579 tons / day) is introduced into extractor 6. The temperature in extractor 6 is 90 ° C. By line 8, 430 t / day of sulfolane is also introduced into extractor 6, the refined phase from extractor 6 is washed with water. receiving 134 tons / day of raffinate. The extract phase from extractor 6 (1025 tons / day) is introduced through the heat exchanger 11 into the extractive distillation column 12 via line 10. Extractive distillation in column 12 is carried out at a pressure of 0.2 at and a residue temperature of 175 ° C. Taken from the top, the runway is directed along line 13 to the separator and is divided into water and hydrocarbon; Hydrogen recycle to extractor 6 through line 14. The residue from column 12 is withdrawn through line t6 to the distillation column not 17, which is heated by steam from line 18. The product taken from the top directs line 19 to the separator 20, and the hydrocarbon (light aromatics), obtained there, is partially recycled to the distillation column through line 21 and partially removed through line 22 at 12 tons / day. The raffinate phase, exiting via line 9 from extractor 6 (which contains less than 100 pp m of benzene), is washed with water and distilled to give 24 tons / day of heavy aromatics and 110 tons / day of edible hexane. Example 2. A 61 ton / day bark fraction of 190–240 ° C, which contains 20% by weight of aromatic hydrocarbons, is fed to extractor 2. The extractor is a rotary disk contactor of this type. Extraction is carried out at, feeding sulfolane via line 3 in an amount of 540 tons / day. The raffinate phase from the extractor is washed with water and get 39 tons / day of heavy aromatic hydrocarbons (the content of aromatic products is below 1 wt.%). To extractor 6 (also a rotating disk contactor), via line 7, are fed 122 tonnes / day of light hydrocarbon fractions obtained by direct distillation, having a boiling point of 55-85 ° C and containing 5 wt. % benzene. The extract solution from extractor 2 (572 tons / day) is fed to the extractor 6. The temperature in the extractor 6 is equal. The extract solution from the extractor 6 (572 tons / day) is fed through the heat exchanger 11 to the column 12 for extractive distillation through line 10. The extraction distillation in column 12 is carried out at a pressure of 0.2 at and a lower temperature of 175 ° C. The distillate is passed through conduit 13 to a separator and separated into aqueous and hydrocarbon phases; the hydrocarbon phase is recycled to extractor 6 via line 14. The remaining product from column 12 is fed via line 16 to a distillation column 17, which is heated with steam coming through line 18. Light fractions are led through line 19 to separator 20, the hydrocarbon phase obtained therein (light aromatic hydrocarbons) are partially recycled to the distillation column via conduit 21, and partially removed via conduit 22 at 9 tonnes / day. The raffinate solution obtained from extractor 6 (containing 136 pp, Yi of benzene) was washed with water and distilled to give 24 tons / day of heavy aromatic hydrocarbons and 110 tons / day of food hexane. The proposed method is simpler than the prototype, in which a mixture of light aromatic hydrocarbons and heavy aromatic hydrocarbons and a selective solvent are separated by distillation. This separation by distillation is difficult if the mixture of aromatic hydrocarbons from the heavy hydrocarbon stream has a boiling point close to the boiling point of the selective solvent, and it is not possible if this boiling point range includes the boiling point of the solvent. In accordance with isoghetemia, heavy aromatic hydrocarbons are contained in the raffinate in the second extractor, and light aromatic hydrocarbons in the extract in the second extractor. By distillation, this extract solution can be easily divided into light aromatic hydrocarbons and a selective solvent, the boiling point of the solvent being above the boiling range of the mixture of light aromatic hydrocarbons. Thus, heavy aromatic hydrocarbons and solvent are prepared separately.
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    权利要求:
    Claims (5)
    [1]
    1. METHOD FOR SIMULTANEOUS SEPARATION OF HEAVY AND LIGHT HYDROCARBON FLOWS FOR AROMATIC AND NON-AROMATIC HYDROCARBONS by separate extraction of aromatic hydrocarbons from a heavy hydrocarbon stream with a selective solvent having a boiling point above the boiling point of a heavy solvent and a heavy solvent solution and the release of heavy non-aromatic hydrocarbons and extraction of aromatic hydrocarbons water from a stream of light hydrocarbons to obtain a light extract and light raffinate solutions with solvent regeneration from. a light raffinate solution, characterized in that, in order to improve the degree of separation, the heavy extract solution is fed to the extraction of aromatic hydrocarbons from a stream of light hydrocarbons, followed by separation from the obtained light raffinate solution of a selective solvent and a mixture of heavy aromatic and light non-aromatic hydrocarbons, a light extract the solution is subjected to extractive distillation and the resulting residual fraction is subjected to distillation with the release of light aromatic carbon hydrogens and a selective solvent, which is recycled to the stage of extraction from the stream of heavy hydrocarbons.
    [2]
    2. The method according to p. ^ Characterized in that sulfolane is used as a solvent in the extraction stage from the heavy hydrocarbon stream.
    [3]
    3. The method according to PP. 1 and 2, which is characterized in that light hydrocarbons have a boiling point of 50-170 ° C.
    [4]
    4. The method according to PP. 1-3, starting from the fact that heavy hydrocarbons have a boiling point of 150-350 ° C.
    [5]
    5. The method according to PP. 1-4, characterized in that the selective solvent is removed from the raffinate solutions by washing with water.
    SU, 1122217 th
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