CN103242120A - Circulating device and refining method of extractant in normal hexane, isohexane and benzene separation process - Google Patents
Circulating device and refining method of extractant in normal hexane, isohexane and benzene separation process Download PDFInfo
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- CN103242120A CN103242120A CN201310152224XA CN201310152224A CN103242120A CN 103242120 A CN103242120 A CN 103242120A CN 201310152224X A CN201310152224X A CN 201310152224XA CN 201310152224 A CN201310152224 A CN 201310152224A CN 103242120 A CN103242120 A CN 103242120A
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Abstract
The invention relates to a circulating device and refining method of an extractant in a normal hexane, isohexane and benzene separation process. A refining tower comprises a normal hexane extracting and rectifying tower, a first solvent recovery tower, a benzene extracting and rectifying tower and a second solvent recovery tower. The extractant is respectively added into the normal hexane extracting and rectifying tower and the benzene extracting and rectifying tower, and two circulating loops are formed after the extractant is added, wherein one loop is formed between the normal hexane extracting and rectifying tower and the first solvent recovery tower, and the other loop is formed between the benzene extracting and rectifying tower and the second solvent recovery tower. Meanwhile, in order to prevent impurities from accumulating in the extractant, a small part of stream is introduced from an extractant stream, passes through a solvent regeneration evaporator, then returns to the normal hexane extracting and rectifying tower and the benzene extracting and rectifying tower and is subjected to de-weighting and impurity removal. According to the circulating device and the refining method, the high-concentration product can be obtained, the consumption amount of the extractant is greatly reduced, the production cost is reduced and the market competitiveness is improved.
Description
Technical field
The present invention relates to extraction agent treatment process in a kind of normal hexane, isohexane and the benzene sepn process, relate to circulation and the process for purification of extraction agent in normal hexane, isohexane and the benzene sepn process especially.
Background technology
The production normal hexane often adopts catalytic reforming generation oil, cracking hydrogenated gasoline or aromatic hydrocarbons to raffinate oil and makes raw material, and component complexity in the raw material comprise alkane, naphthenic hydrocarbon, aromatic hydrocarbons and small amounts of olefins etc., and the boiling point of different components is close.The normal separation method that adopts has conventional distillation method, molecular sieve adsorption and extraction fractional distillation.The conventional distillation method can not get high-pure normal hexane product; Molecular sieve adsorption is easily saturated, the regeneration difficulty; Extraction fractional distillation not only can obtain the product of higher degree, and simultaneously production cost is low relatively, is usually used in separating of aromatic hydrocarbons and non-aromatics.
Extraction agent commonly used comprises glycols, N-Methyl pyrrolidone, tetramethylene sulfone, dimethyl sulfoxide (DMSO), N-formyl morpholine etc.The mass ratio of extraction agent and raw material (solvent ratio) has material impact to the relative volatility that changes between feed composition.Solvent ratio is more big, and the effect of extracting and separating is more good, but with the increase of solvent ratio, the consumption of extraction agent can increase, and causes the increase of energy consumption and cost.Therefore, the treatment process of extraction agent has material impact to the process cost of device.
Summary of the invention
The object of the present invention is to provide circulation and the process for purification of extracting rectifying unit extraction agent in a kind of normal hexane, isohexane and the benzene sepn process.This technology can reduce the consumption of extraction agent in the production process when guaranteeing to obtain high purity product, reduce the cost of rectification cell significantly.
Technical scheme of the present invention is as follows:
Extraction agent circulation device in a kind of normal hexane, isohexane and the benzene sepn process comprises n-hexane extraction rectifying tower 108, first solvent recovery tower 113, benzene extractive distillation column 116 and second solvent recovery tower 118; The reboiler 107, the solvent cooler 115 of n-hexane extraction rectifying tower, the n-hexane extraction rectifying tower 108 that it is characterized in that first solvent recovery tower 113, isohexane purification tower are connected successively, and n-hexane extraction rectifying tower 108 is connected with first solvent recovery tower 113 and forms the loop; The feed preheater 103 of second solvent recovery tower 118, lightness-removing column, benzene extractive distillation column feed preheater 104, benzene extractive distillation column 116 are connected successively, and benzene extractive distillation column 116 is connected with second solvent recovery tower 118 and forms the loop; First solvent recovery tower 113 and second solvent recovery tower 118 are respectively equipped with the first regenerated solvent vaporizer 123 and the second regenerated solvent vaporizer 124.
The method of extraction agent circulation in normal hexane of the present invention, isohexane and the benzene sepn process, extraction agent adds in n-hexane extraction rectifying tower 108 and benzene extractive distillation column 116 respectively; Extraction agent is after n-hexane extraction rectifying tower 108 adds, flow to first solvent recovery tower 113 from n-hexane extraction rectifying tower 108 tower reactors, flow out from first solvent recovery tower, 113 tower reactors then, the solvent cooler 115 that the reboiler 107 of main stream stock-traders' know-how isohexane purification tower and normal hexane are got rectifying tower, after the still liquid of isohexane purification tower and recirculated water cooling, be back to n-hexane extraction rectifying tower 108 again, form a circulation, realized the repeated use of extraction agent; Extraction agent is after benzene extractive distillation column 116 adds, flow to second solvent recovery tower 118 from benzene extractive distillation column 116 tower reactors, flow out from second solvent recovery tower, 118 tower reactors then, feed preheater 103 and the benzene extractive distillation column feed preheater 104 of main stream stock-traders' know-how lightness-removing column, after the charging of lightness-removing column 101 and benzene extractive distillation column 116 cooling, be back to benzene extractive distillation column 116 again, form a circulation, realized the repeated use of extraction agent.
The small portion stream that also has that flows out from first solvent recovery tower, 113 tower reactors strand enters the first regenerated solvent vaporizer 123, after being heated by steam, by liquid phase flash to be back to after the gas phase first solvent recovery tower 113 take off reset assorted.
The small portion stream that also has that flows out from second solvent recovery tower, 118 tower reactors strand enters the second regenerated solvent vaporizer 124, after being heated by steam, by liquid phase flash to be back to after the gas phase second solvent recovery tower 118 take off reset assorted.
The present invention makes the extraction agent in normal hexane, isohexane and the benzene sepn process obtain effective utilization, has not only obtained highly purified normal hexane, isohexane and benzaldehyde product, has reduced the consumption of extraction agent simultaneously, has reduced production cost, has improved the market competitiveness.
Description of drawings
Fig. 1: the schematic flow sheet of extraction agent in normal hexane, isohexane and the benzene sepn process.
Embodiment
Below in conjunction with accompanying drawing several connections of the present invention are described in further detail.
The circulation of extraction agent and process for purification flow process are as shown in Figure 1 in normal hexane, isohexane and the benzene sepn process: n-hexane extraction rectifying tower 108, first solvent recovery tower 113, benzene extractive distillation column 116 and second solvent recovery tower 118 are formed.The reboiler 107 of first solvent recovery tower 113, isohexane purification tower, the solvent cooler 115 of n-hexane extraction rectifying tower, n-hexane extraction rectifying tower 108 are connected successively, and n-hexane extraction rectifying tower 108 is connected with first solvent recovery tower 113 and forms the loop; The feed preheater 103 of second solvent recovery tower 118, lightness-removing column, benzene extractive distillation column feed preheater 104, benzene extractive distillation column 116 are connected successively, and benzene extractive distillation column 116 is connected with second solvent recovery tower 118 and forms the loop; First solvent recovery tower 113 and second solvent recovery tower 118 are respectively equipped with the first regenerated solvent vaporizer 123 and the second regenerated solvent vaporizer 124.
According to the present invention, normal hexane, isohexane and benzene separation processes are as follows: from the total hydrocarbon feed outside the battery limit (BL) after feed preheater 103 preheatings, from lightness-removing column 101 top chargings, overhead vapours is after condenser condenses, lime set enters a return tank part and refluxes, another part as the light constituent product from the return tank extraction; Remove than 2-methylpentane behind the low-boiling impurity composition through lightness-removing column 101, send into isohexane tower 105 and remove the low-boiling cut of isohexane geometric ratio normal hexane, cat head extraction stream thigh is sent into basin as the isohexane product; Isohexane tower 105 tower reactor extraction materials are sent into n-hexane extraction rectifying tower 108 and are separated, and extraction agent is added by the feed plate top, obtain normal hexane product after the normal hexane stream stock-traders' know-how carclazyte adsorption bed 111 of cat head extraction is handled and send into basin; The mixture of tower reactor extraction is sent into first solvent recovery tower 113 and is separated, and tower reactor obtains reclaiming solvent, and most of normal hexane that returns after cooling is got rectifying tower 108 and used repeatedly, and small part is sent the solvent reclamation unit to take off to reset and mixed; Cat head obtains the mixture of benzene and non-aromatics impurity; First solvent recovery tower, 113 overhead streams thighs are sent into benzene extractive distillation column 116 and are separated, and extraction agent is added by feed plate top, from removed overhead non-aromatics impurity, and send into basin as the solvent oil product; Tower reactor is the mixed flow thigh of benzene and extraction agent, send second solvent recovery tower 118 to separate; The second solvent recuperation tower reactor obtains reclaiming solvent, and major part is returned benzene extractive distillation column 116 and used repeatedly after cooling, and small part is sent the solvent reclamation unit to take off rearrangement and mixed; After the benzene stream stock-traders' know-how carclazyte adsorption bed 121 of cat head extraction is handled, obtain benzaldehyde product.In order to obtain highly purified normal hexane product and benzaldehyde product, the consumption of extraction agent is 3～5 times of raw material inlet amount.
Described extraction agent is after n-hexane extraction rectifying tower 108 adds, flow to first solvent recovery tower 113 from n-hexane extraction rectifying tower 108 tower reactors, flow out from first solvent recovery tower, 113 tower reactors then, the reboiler 107 of main stream stock-traders' know-how isohexane purification tower and the solvent cooler 115 of n-hexane extraction rectifying tower, after the still liquid of isohexane purification tower and recirculated water cooling, be back to n-hexane extraction rectifying tower 108 again, form a circulation, thereby realized the repeated use of extraction agent, greatly reduced the consumption of extraction agent.The small portion stream thigh that also has that flows out from first solvent recovery tower, 113 tower reactors enters the first regenerated solvent vaporizer 123, after being heated by steam, flashed to by liquid phase and to be back to first solvent recovery tower 113 after the gas phase and to take off and reset assortedly, accumulate in extraction agent to prevent impurity.
Described extraction agent is after benzene extractive distillation column 116 adds, flow to second solvent recovery tower 118 from benzene extractive distillation column 116 tower reactors, flow out from second solvent recovery tower, 118 tower reactors then, feed preheater 103 and the benzene extractive distillation column feed preheater 104 of main stream stock-traders' know-how lightness-removing column, after the charging of lightness-removing column 101 and benzene extractive distillation column 116 cooling, be back to benzene extractive distillation column 116 again, form a circulation, thereby realized the repeated use of extraction agent, greatly reduced the consumption of extraction agent.The small portion stream thigh that also has that flows out from second solvent recovery tower, 118 tower reactors enters the second regenerated solvent vaporizer 124, after being heated by steam, flashed to by liquid phase and to be back to second solvent recovery tower 118 after the gas phase and to take off and reset assortedly, accumulate in extraction agent to prevent impurity.
Adopt extraction agent circulation and refining method between the equipment different units that the present invention connects, purpose is to change the relative volatility of normal hexane and benzene, obtains highly purified normal hexane product (concentration〉99wt%).Change benzene and methylcyclopentane, 2, the relative volatility of 2-dimethylpentane etc., acquisition high-purity benzene product (concentration〉95wt%).
Claims (4)
1. extraction agent circulation device in a normal hexane, isohexane and the benzene sepn process comprises n-hexane extraction rectifying tower (108), first solvent recovery tower (113), benzene extractive distillation column (116) and second solvent recovery tower (118); The reboiler (107), the solvent cooler (115) of n-hexane extraction rectifying tower, the n-hexane extraction rectifying tower (108) that it is characterized in that first solvent recovery tower (113), isohexane purification tower are connected successively, and n-hexane extraction rectifying tower (108) is connected with first solvent recovery tower (113) and forms the loop; The feed preheater (103) of second solvent recovery tower (118), lightness-removing column, benzene extractive distillation column feed preheater (104), benzene extractive distillation column (116) are connected successively, and benzene extractive distillation column (116) is connected with second solvent recovery tower (118) and forms the loop; First solvent recovery tower (113) and second solvent recovery tower (118) are respectively equipped with the first regenerated solvent vaporizer (123) and the second regenerated solvent vaporizer (124).
2. the method for extraction agent circulation in normal hexane as claimed in claim 1, isohexane and the benzene sepn process is characterized in that extraction agent adds respectively in n-hexane extraction rectifying tower (108) and benzene extractive distillation column (116); Extraction agent is after n-hexane extraction rectifying tower (108) adds, flow to first solvent recovery tower (113) from n-hexane extraction rectifying tower (108) tower reactor, flow out from first solvent recovery tower (113) tower reactor then, the reboiler (107) of main stream stock-traders' know-how isohexane purification tower and the solvent cooler (115) of n-hexane extraction rectifying tower, after the still liquid of isohexane purification tower and recirculated water cooling, be back to n-hexane extraction rectifying tower (108) again, form a circulation, realized the repeated use of extraction agent; Extraction agent is after benzene extractive distillation column (116) adds, flow to second solvent recovery tower (118) from benzene extractive distillation column (116) tower reactor, flow out from second solvent recovery tower (118) tower reactor then, feed preheater (103) and the benzene extractive distillation column feed preheater (104) of main stream stock-traders' know-how lightness-removing column, after the charging of lightness-removing column (101) and benzene extractive distillation column (116) cooling, be back to benzene extractive distillation column (116) again, form a circulation, realized the repeated use of extraction agent.
3. method as claimed in claim 2, it is characterized in that entering the first regenerated solvent vaporizer (123) from the small portion stream thigh that also has that first solvent recovery tower (113) tower reactor flows out, after being heated by steam, by liquid phase flash to be back to after the gas phase first solvent recovery tower (113) take off reset assorted.
4. method as claimed in claim 2, it is characterized in that entering the second regenerated solvent vaporizer (124) from the small portion stream thigh that also has that second solvent recovery tower (118) tower reactor flows out, after being heated by steam, by liquid phase flash to be back to after the gas phase second solvent recovery tower (118) take off reset assorted.
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| CN105906479A (en) * | 2016-05-24 | 2016-08-31 | 济南大学 | Method for separating butanol-butyronitrile mixture |
| CN106008159A (en) * | 2016-05-24 | 2016-10-12 | 济南大学 | Method for separating isopropyl alcohol-propionitrile mixture |
| CN106518598A (en) * | 2016-10-09 | 2017-03-22 | 大连理工大学 | Device and method for purifying n-hexane with N,N-dimethylacetamide solvent |
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| CN106008159A (en) * | 2016-05-24 | 2016-10-12 | 济南大学 | Method for separating isopropyl alcohol-propionitrile mixture |
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