CN102351627A - Process method for extracting normal hexane and isohexane from crude hexane - Google Patents
Process method for extracting normal hexane and isohexane from crude hexane Download PDFInfo
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Abstract
The invention discloses a process method for extracting normal hexane and isohexane from crude hexane. The process method comprises the following steps of: (1) mixing and heating raw material crude hexane and hydrogen gas and feeding into a hydrogenation reactor, and performing hydrodearomatization reaction under the action of a catalyst; (2) cooling a hydrogenation reaction product and then feeding in a low-pressure separation tank to perform gas-liquid separation, wherein gas phase is discharged from the top of the low-pressure separation tank, and oil phase at the bottom of the low-pressure separation tank is conveyed to a fractionation device to perform precise fractionation; (3) preheating the oil phase and feeding into a light component removal tower of the fractionation device to remove light components with fraction of less than 59 DEG C; (4) introducing remaining fractions of light component removal into an isohexane removal oil tower of the fractionation device to obtain high-purity isohexane; and (5) introducing the remaining fraction of isohexane removal into a normal hexane removal oil tower of the fractionation device to obtain the normal hexane. The process method has the advantages of simple and practical process, simple equipment, convenience in operation and stable and reliable product quality.
Description
Technical field
The invention belongs to petrochemical complex separation method technical field, especially relate to a kind of processing method by thick hexane extraction normal hexane, isohexane.
Background technology
Normal hexane is that one of varsol the most widely go up is used in industry now, the solvent when being mainly used in olefinic polymerization such as propylene, the solvent of extraction agent, rubber and the coating of edible vegetable oil and the thinner of pigment.At present in the industry mainly from platformate raffinate rectifying separation to obtain purity be 60% ~ 80% (wt) technical grade normal hexane product.Because C
6Cut boiling point very close (like 69 ℃ of normal hexanes, 71.8 ℃ of methylcyclopentanes), conventional distillation are difficult to its separation, and employing precise distillation energy consumption is high, production cost is high, yield is lower, and is difficult to obtain Zheng Jiwan>99% (wt) high purity product; Use the special extract rectification method, cost is higher, and process is complicated, and this has also caused the most of dependence on import of China's high purity normal hexane.
The isohexane boiling point is low, be easy to, security is good, energy cost is low; As substituting little, the safer aerosol products of normal hexane production toxicity and in field of precision instruments very wide prospect being arranged, the technology of preparing of isohexane has become the focus that the researchist pays close attention to.
Summary of the invention
For addressing the above problem, the purpose of this invention is to provide a kind of processing method by thick hexane extraction normal hexane, isohexane.
For realizing the foregoing invention purpose, the present invention adopts following technical scheme:
A kind of processing method by thick hexane extraction normal hexane, isohexane, it may further comprise the steps:
(1), the thick hexane of raw material mixes with hydrogen through charging/product interchanger, feed heater and is heated to 130～170 ℃, gets into hydrogenator, under the effect of catalyzer, carries out the hydrogenation dearomatization hydrocarbon reaction, removes the benzene in the thick hexane;
(2), the hydrogenation reaction product that obtains through step 1 is cooled to 30～40 ℃ through charging/product interchanger, product water cooler; Get into the low jar that divides and carry out gas-liquid separation; Gas phase is discharged by the low tank top of dividing, and the oil phase of low branch pot bottom is delivered to fractionation plant and carried out precision fractional distillation;
(3), through oil phase that step 2 obtains after preheater is preheated to 80～85 ℃; Get into the cut light tower of fractionation plant, tower top temperature is controlled at 50～80 ℃, tower top pressure and is controlled at the light constituent that 0.05～0.11MPa, column bottom temperature are controlled at 90～100 ℃, removed overhead cut＜59 ℃;
(4), will take off isohexane oil tower through what step 3 took off that light remaining cut (＞59 ℃ of distillates) introduces fractionation plant; Tower top temperature is controlled at 75～85 ℃, tower top pressure and is controlled at 0.05～0.11MPa, column bottom temperature and is controlled at 103～113 ℃, cat head and cuts 59～63 ℃ of cuts, obtains the high purity isohexane of content >=99.5%;
(5), will take off normal hexane oil tower through what step 4 removed that the remaining cut of isohexane introduces fractionation plant; Tower top temperature is controlled at 83～93 ℃, tower top pressure and is controlled at 0.05～0.11MPa, column bottom temperature and is controlled at 110 ℃～120 ℃, cat head and cuts 65～70 ℃ of cuts; Obtain content and be respectively 60%, 70%, 80%, 90% normal hexane, the residue double distilled is divided into heptane at the bottom of the tower.
In the above-mentioned processing method by thick hexane extraction normal hexane, isohexane, described hydrogenation aromatics-removing operation condition is: reaction pressure 1.5～1.9MPa, reactor inlet hydrogen to oil volume ratio 300～350, volume space velocity 1.2～1.8hr
-1, 130～170 ℃ of temperature of reaction.
In the above-mentioned processing method by thick hexane extraction normal hexane, isohexane, described hydrogenation aromatics-removing catalysts is the reactive metal nickel catalyst, and outward appearance is spherical, and diameter is 2.5 ~ 4.5mm, and tap density is 0.6 ± 0.02 g/cm
3, specific surface area is not less than 100m
2/ g, radially compressive strength is not more than the 40N/ grain.
In the above-mentioned processing method by thick hexane extraction normal hexane, isohexane; The gas phase of tank top discharge in described low minute gets into recycle hydrogen as recycle hydrogen and divides in the flow container; Getting into circulating hydrogen compressor behind the separatory boosts; Be mixed together with fresh hydrogen then and get into the desulphurization of recycle hydrogen reactor, the mixing hydrogen and the thick hexane of raw material that remove hydrogen sulfide get in the hydrogenator.
A kind of realization is described by thick hexane extraction normal hexane; The equipment of the processing method of isohexane; It is made up of hydrogenation unit and fractionation plant; Said hydrogenation unit comprises charging/product interchanger; Feed heater; Hydrogenator; The product water cooler; Low jar and the pipeline of dividing; The raw material discharge port of charging/product interchanger and the opening for feed of feed heater pass through pipe connection; The discharge port of feed heater and the opening for feed of hydrogenator pass through pipe connection; The product opening for feed of the discharge port of hydrogenator and charging/product interchanger passes through pipe connection; The product discharge port of charging/product interchanger links to each other with the opening for feed of product water cooler through pipeline, and the discharge port of product water cooler links to each other with the low opening for feed of jar that divides; Said fractionation plant comprises cut light tower; Take off isohexane oil tower and take off normal hexane oil tower; The opening for feed of cut light tower links to each other through pipeline with the low discharge port of jar that divides; Cut light tower; Take off isohexane oil tower and take off between the bottom liquid outlet of normal hexane oil tower and all recycle pump is arranged through pipe connection; Cut light tower; Take off isohexane oil tower and all be connected water cooler and return tank respectively through pipeline with the top of taking off normal hexane oil tower; Water cooler links to each other with return tank through pipeline; Return tank links to each other with reflux pump through pipeline; The reflux pump outlet connects two pipelines; Wherein a pipeline is connected with tower top outlet, and another pipeline is the product delivery line.
Further, low branch tank top venting port divides flow container, circulating hydrogen compressor, desulphurization of recycle hydrogen reactor to be connected with recycle hydrogen through pipeline successively, and the discharge port of desulphurization of recycle hydrogen reactor is connected with the material inlet of charging/product interchanger.
Further, cut light tower, take off isohexane oil tower, the column plate that takes off normal hexane oil tower all adopts composite holes miniature valve high capacity tray.
Because adopt aforesaid technical scheme, the present invention has following superiority:
Should be by the processing method of thick hexane extraction normal hexane, isohexane, the thick hexane of its raw material gets into charging/product interchanger with hydrogen to be mixed before, can improve the heat exchange effect of interchanger; The nickel catalyst operational condition that the hydrogenation dearomatization hydrocarbon reaction adopts is gentle relatively, and it is remarkable to take off the benzene effect; Hydrogenation reaction system is provided with the desulphurization of recycle hydrogen reactor, can be with by the discharge of low branchs tank top, divide the recycle hydrogen that flow container separatory and circulating hydrogen compressor boost and install the H that contains in the external fresh hydrogen through recycle hydrogen
2The S gas removal guarantees the long-time running of the catalyzer in the hydrogenator; Production technique is simple, practical, and equipment is simple, and is easy to operate, and energy consumption is low, stable and reliable product quality, and economical efficiency is high.
Description of drawings
Fig. 1 is the present invention by the process flow sheet of one of embodiment of the processing method of thick hexane extraction normal hexane, isohexane;
Fig. 2 is the present invention by two the process flow sheet of the embodiment of the processing method of thick hexane extraction normal hexane, isohexane;
Fig. 3 is a structural representation of realizing the equipment of the said processing method of Fig. 2;
Among the figure: the 1-hydrogenator; 2-desulphurization of recycle hydrogen reactor; The 3-circulating hydrogen compressor; The 4-recycle hydrogen divides flow container; The 5-preheater; The 6-cut light tower; 7-first water cooler; 8-first return tank; 9-second water cooler; 10-second return tank; 11-the 3rd water cooler; 12-the 3rd return tank; The 13-normal hexane; 14-takes off normal hexane oil tower; The 15-interchanger; 16-the 3rd recycle pump; The 17-isohexane; 18-takes off isohexane oil tower; 19-second recycle pump; The 20-light constituent; 21-first recycle pump; The 22-fresh hydrogen; The low jar that divides of 23-; 24-product water cooler; 25-charging/product interchanger; The thick hexane of 26-; The 27-feed heater.
Embodiment
Through accompanying drawing and embodiment technical scheme of the present invention is done further explain below, still, the present invention is not limited to these embodiment.
As shown in Figure 1, the present invention is by the processing method of thick hexane extraction normal hexane, isohexane, and its concrete processing step is:
(1), the catalyzer that loads in the hydrogenator is the reactive metal nickel catalyst, outward appearance is spherical, diameter is 2.5 ~ 4.5mm, tap density is 0.6 ± 0.02 g/cm
3, specific surface area is not less than 100m
2/ g, radially compressive strength is not more than the 40N/ grain; The thick hexane of raw material mixes with hydrogen through charging/product interchanger, feed heater and is heated to 130～170 ℃; Get into hydrogenator; Under the effect of catalyzer, carry out the hydrogenation dearomatization hydrocarbon reaction; The hydrogenation reaction operational condition is: reaction pressure 1.5～1.9MPa; Reactor inlet hydrogen to oil volume ratio 300～350, volume space velocity 1.2～1.8hr
-1, 130～170 ℃ of temperature of reaction remove the benzene in the thick hexane;
(2), the hydrogenation reaction product that obtains through step 1 is cooled to 30～40 ℃ through charging/product interchanger, product water cooler; Get into the low jar that divides and carry out gas-liquid separation; Gas phase is discharged by the low tank top of dividing, and the oil phase of low branch pot bottom is delivered to fractionation plant and carried out precision fractional distillation;
(3), through oil phase that step 2 obtains after preheater is preheated to 80～85 ℃; Get into the cut light tower of fractionation plant, tower top temperature is controlled at 50～80 ℃, tower top pressure and is controlled at the light constituent that 0.05～0.11MPa, column bottom temperature are controlled at 90～100 ℃, removed overhead cut＜59 ℃;
(4), will take off isohexane oil tower through what step 3 took off that light remaining cut (＞59 ℃ of distillates) introduces fractionation plant; Tower top temperature is controlled at 75～85 ℃, tower top pressure and is controlled at 0.05～0.11MPa, column bottom temperature and is controlled at 103～113 ℃, cat head and cuts 59～63 ℃ of cuts, obtains the high purity isohexane of content >=99.5%;
(5), will take off normal hexane oil tower through what step 4 removed that the remaining cut of isohexane introduces fractionation plant; Tower top temperature is controlled at 83～93 ℃, tower top pressure and is controlled at 0.05～0.11MPa, column bottom temperature and is controlled at 110 ℃～120 ℃, cat head and cuts 65～70 ℃ of cuts; Obtain content and be respectively 60%, 70%, 80%, 90% normal hexane, the residue double distilled is divided into heptane at the bottom of the tower.
In the processing method by thick hexane extraction normal hexane, isohexane shown in Figure 2, the difference of its technical process and technical process shown in Figure 1 only is: to the processing of the gaseous component of low branchs tank top discharge.Can know by Fig. 2; The gaseous component that discharge low branch tank top gets into recycle hydrogen as recycle hydrogen and divides in the flow container; Getting into circulating hydrogen compressor behind the separatory boosts; Be mixed together with fresh hydrogen then and get into the desulphurization of recycle hydrogen reactor; To remove the hydrogen sulfide that mixes in the hydrogen, mix hydrogen then and after charging/product interchanger, feed heater heating, get in the hydrogenator.
As shown in Figure 3; Realize the equipment of the said processing method of Fig. 2; It is made up of hydrogenation unit and fractionation plant; Said hydrogenation unit comprises charging/product interchanger 25; Feed heater 27; Hydrogenator 1; Product water cooler 24; Low jar 23 and the pipeline of dividing; The raw material discharge port of charging/product interchanger 25 and the opening for feed of feed heater 27 pass through pipe connection; The opening for feed of the discharge port of feed heater and hydrogenator 1 passes through pipe connection; The product opening for feed of the discharge port of hydrogenator and charging/product interchanger 25 passes through pipe connection; The product discharge port of charging/product interchanger links to each other with the opening for feed of product water cooler 24 through pipeline; The discharge port of product water cooler links to each other with the low opening for feed of jar 23 that divides; Low branch tank top venting port divides flow container 4 with recycle hydrogen successively through pipeline; Circulating hydrogen compressor 3; Desulphurization of recycle hydrogen reactor 2 connects, and the discharge port of desulphurization of recycle hydrogen reactor 2 is connected with the material inlet of charging/product interchanger 25; Said fractionation plant comprises cut light tower 6; Take off isohexane oil tower 18 and take off normal hexane oil tower 14; The opening for feed of cut light tower 6 links to each other through pipeline with the low discharge port of jar 23 that divides; Cut light tower; Take off isohexane oil tower and take off between the bottom liquid outlet of normal hexane oil tower and be connected with first recycle pump 21 respectively through pipeline; Second recycle pump 19; The top of cut light tower is all through pipe connection first water cooler 7 and first return tank 8; The top of taking off isohexane oil tower is all through pipe connection second water cooler 9 and second return tank 10; The top of taking off normal hexane oil tower is through pipe connection the 3rd water cooler 11 and the 3rd return tank 12; Each above-mentioned water cooler; And return tank correspondingly links to each other through pipeline; Return tank links to each other with reflux pump through pipeline; The reflux pump outlet connects two pipelines; Wherein a pipeline is connected with tower top outlet; Another pipeline is the product delivery line; It is light constituent 20 that cut light tower derives product; Taking off isohexane oil tower derivation product is isohexane 17; Taking off normal hexane oil tower derivation product is normal hexane 13; The bottom liquid outlet of taking off normal hexane oil tower is through pipeline and the 3rd recycle pump 16; Interchanger 15 links to each other successively, through pumping; Obtain the product heptane after the cooling.
Above-mentioned cut light tower 6, take off isohexane oil tower 18, the column plate that takes off normal hexane oil tower 14 all adopts composite holes miniature valve high capacity tray, can improve fractionating effect, reduces the separation column height.
The thick hexane 26 of raw material mixes with the hydrogen that mixes that obtains through desulphurization of recycle hydrogen reactor 2; Mixing hydrogen comprises by the discharge of low branchs tank top, divides the recycle hydrogen that flow container 4 separatory and circulating hydrogen compressor 3 boost and install external fresh hydrogen 22 through recycle hydrogen; Be heated to 130～170 ℃ through charging/product interchanger 25, feed heater 27; Get into hydrogenator 1; Under the effect of catalyzer, carry out the hydrogenation dearomatization hydrocarbon reaction, remove the benzene in the thick hexane; The reaction product of hydrogenator is cooled to 30～40 ℃ through charging/product interchanger 25, product water cooler 24, gets into the low jar 23 that divides and carries out gas-liquid separation, and gas phase is discharged by the low tank top of dividing, and the oil phase of low branch pot bottom is delivered to fractionation plant and carried out precision fractional distillation; Low gas phase of dividing jar 23 tops to discharge gets into recycle hydrogen as the recycle hydrogen of recycling divides in the flow container 4, gets into circulating hydrogen compressor 3 behind the separatory and boosts, and is mixed together with fresh hydrogen 22 then and gets into desulphurization of recycle hydrogen reactor 2, to remove the hydrogen sulfide in the recycle hydrogen; The low oil phase that divides jar 23 bottoms is after preheater 5 is preheated to 80～85 ℃; Get into cut light tower 6; The light constituent of removed overhead cut＜59 ℃; According to reflux ratio; Part light constituent passes back in the cut light tower through 7 condensations of first water cooler and first return tank 8, and another part light constituent 20 is derived through the product delivery line; The outlet of the bottom liquid of cut light tower is discharged takes off light remaining cut (＞59 ℃ of distillates) and sends into through first recycle pump 21 and take off in the isohexane oil tower 18; Cat head cuts 59～63 ℃ of cuts; Obtain the high purity isohexane of content >=99.5%; According to reflux ratio; Warp second water cooler, 9 condensations of part isohexane and second return tank 10 pass back into and take off in the isohexane oil tower, and another part isohexane 17 is derived through the product delivery line; The remaining cut of isohexane that removes that takes off that the bottom liquid outlet of isohexane oil tower discharges is sent into through second recycle pump 19 and is taken off in the normal hexane oil tower 14; Cat head cuts 65～70 ℃ of cuts; Obtain content and be respectively 60%, 70%, 80%, 90% normal hexane; According to reflux ratio; Warp the 3rd water cooler 11 condensations of part normal hexane and the 3rd return tank 12 pass back into and take off in the normal hexane oil tower, and another part normal hexane 13 is derived through the product delivery line; The residue last running of taking off the bottom liquid outlet discharge of normal hexane oil tower 14 obtains the product heptane via 16 conveyings of the 3rd recycle pump, interchanger 15 after lowering the temperature.
Claims (7)
1. processing method by thick hexane extraction normal hexane, isohexane, it is characterized in that: it may further comprise the steps:
(1), the thick hexane of raw material mixes with hydrogen through charging/product interchanger, feed heater and is heated to 130～170 ℃, gets into hydrogenator, under the effect of catalyzer, carries out the hydrogenation dearomatization hydrocarbon reaction, removes the benzene in the thick hexane;
(2), the hydrogenation reaction product that obtains through step 1 is cooled to 30～40 ℃ through charging/product interchanger, product water cooler; Get into the low jar that divides and carry out gas-liquid separation; Gas phase is discharged by the low tank top of dividing, and the oil phase of low branch pot bottom is delivered to fractionation plant and carried out precision fractional distillation;
(3), through oil phase that step 2 obtains after preheater is preheated to 80～85 ℃; Get into the cut light tower of fractionation plant, tower top temperature is controlled at 50～80 ℃, tower top pressure and is controlled at the light constituent that 0.05～0.11MPa, column bottom temperature are controlled at 90～100 ℃, removed overhead cut＜59 ℃;
(4), will take off isohexane oil tower through what step 3 took off that light remaining cut introduces fractionation plant; Tower top temperature is controlled at 75～85 ℃, tower top pressure and is controlled at 0.05～0.11MPa, column bottom temperature and is controlled at 103～113 ℃, cat head and cuts 59～63 ℃ of cuts, obtains the high purity isohexane of content >=99.5%;
(5), will take off normal hexane oil tower through what step 4 removed that the remaining cut of isohexane introduces fractionation plant; Tower top temperature is controlled at 83～93 ℃, tower top pressure and is controlled at 0.05～0.11MPa, column bottom temperature and is controlled at 110 ℃～120 ℃, cat head and cuts 65～70 ℃ of cuts; Obtain content and be respectively 60%, 70%, 80%, 90% normal hexane, the residue double distilled is divided into heptane at the bottom of the tower.
2. processing method according to claim 1 is characterized in that: its hydrogenation aromatics-removing operation condition is: reaction pressure 1.5～1.9MPa, reactor inlet hydrogen to oil volume ratio 300～350, volume space velocity 1.2～1.8hr
-1, 130～170 ℃ of temperature of reaction.
3. processing method according to claim 1 is characterized in that: its hydrogenation aromatics-removing catalysts is the reactive metal nickel catalyst, and outward appearance is spherical, and diameter is 2.5 ~ 4.5mm, and tap density is 0.6 ± 0.02 g/cm
3, specific surface area is not less than 100m
2/ g, radially compressive strength is not more than the 40N/ grain.
4. processing method according to claim 1; It is characterized in that: the gas phase that discharge its low branch tank top gets into recycle hydrogen as recycle hydrogen and divides in the flow container; Getting into circulating hydrogen compressor behind the separatory boosts; Be mixed together with fresh hydrogen then and get into the desulphurization of recycle hydrogen reactor, the mixing hydrogen and the thick hexane of raw material that remove hydrogen sulfide get in the hydrogenator.
5. equipment of realizing claim 1 or 4 said processing methodes; It is characterized in that: it is made up of hydrogenation unit and fractionation plant; Said hydrogenation unit comprises charging/product interchanger; Feed heater; Hydrogenator; The product water cooler; Low jar and the pipeline of dividing; The raw material discharge port of charging/product interchanger (25) and the opening for feed of feed heater (27) pass through pipe connection; The opening for feed of the discharge port of feed heater and hydrogenator (1) passes through pipe connection; The product opening for feed of the discharge port of hydrogenator and charging/product interchanger passes through pipe connection; The product discharge port of charging/product interchanger links to each other with the opening for feed of product water cooler (24) through pipeline, and the discharge port of product water cooler links to each other with the low opening for feed of jar (23) that divides; Said fractionation plant comprises cut light tower (6); Take off isohexane oil tower (18) and take off normal hexane oil tower (14); The opening for feed of cut light tower links to each other through pipeline with the low discharge port of jar that divides; Cut light tower; Take off isohexane oil tower and take off between the bottom liquid outlet of normal hexane oil tower and all recycle pump is arranged through pipe connection; Cut light tower; Take off isohexane oil tower and all be connected water cooler and return tank respectively through pipeline with the top of taking off normal hexane oil tower; Water cooler links to each other with return tank through pipeline; Return tank links to each other with reflux pump through pipeline; The reflux pump outlet connects two pipelines; Wherein a pipeline is connected with tower top outlet, and another pipeline is the product delivery line.
6. equipment according to claim 5; It is characterized in that: its low jar (23) top vent of dividing divides flow container (4), circulating hydrogen compressor (3), desulphurization of recycle hydrogen reactor (2) to be connected with recycle hydrogen through pipeline successively, and the discharge port of desulphurization of recycle hydrogen reactor is connected with the material inlet of charging/product interchanger (25).
7. equipment according to claim 5 is characterized in that: its cut light tower, take off isohexane oil tower, the column plate that takes off normal hexane oil tower all adopts composite holes miniature valve high capacity tray.
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| CN103073383A (en) * | 2013-02-07 | 2013-05-01 | 天津大学 | Method and device for separating isohexane, n-hexane and benzene |
| CN103086823A (en) * | 2013-02-07 | 2013-05-08 | 天津大学 | Method and device for separating n-hexane, isohexane and benzene |
| CN103113179A (en) * | 2013-02-07 | 2013-05-22 | 天津大学 | Thermal coupling system and method for extractive distillation of normal hexane, isohexane and benzene |
| CN103833499A (en) * | 2012-11-27 | 2014-06-04 | 中国石油天然气股份有限公司 | Method for preparing high-purity isohexane solvent oil |
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| CN102675023B (en) * | 2012-05-19 | 2014-08-27 | 淄博汇佳橡胶新型材料有限公司 | Preparation method of narrow-fraction high-purity isohexane |
| CN102675023A (en) * | 2012-05-19 | 2012-09-19 | 淄博汇佳橡胶新型材料有限公司 | Preparation method of narrow-fraction high-purity isohexane |
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| CN103833499A (en) * | 2012-11-27 | 2014-06-04 | 中国石油天然气股份有限公司 | Method for preparing high-purity isohexane solvent oil |
| CN103073383A (en) * | 2013-02-07 | 2013-05-01 | 天津大学 | Method and device for separating isohexane, n-hexane and benzene |
| CN103086823A (en) * | 2013-02-07 | 2013-05-08 | 天津大学 | Method and device for separating n-hexane, isohexane and benzene |
| CN103113179A (en) * | 2013-02-07 | 2013-05-22 | 天津大学 | Thermal coupling system and method for extractive distillation of normal hexane, isohexane and benzene |
| CN103113179B (en) * | 2013-02-07 | 2015-03-25 | 天津大学 | Thermal coupling system and method for extractive distillation of normal hexane, isohexane and benzene |
| CN103086823B (en) * | 2013-02-07 | 2015-07-01 | 天津大学 | Method and device for separating n-hexane, isohexane and benzene |
| CN104045500B (en) * | 2013-03-15 | 2016-04-13 | 中石化广州工程有限公司 | A kind of production method of high purity polymerization-grade normal hexane |
| CN104045500A (en) * | 2013-03-15 | 2014-09-17 | 中石化广州工程有限公司 | Highly pure polymer-grade n-hexane production method |
| CN107365599A (en) * | 2017-07-28 | 2017-11-21 | 大庆亿鑫化工股份有限公司 | A kind of food-grade normal hexane low-voltage hydrogenation production technology |
| CN111057581A (en) * | 2018-10-17 | 2020-04-24 | 内蒙古伊泰煤基新材料研究院有限公司 | Method for removing aromatic hydrocarbon from industrial grade light hydrocarbon |
| CN110256190A (en) * | 2019-06-20 | 2019-09-20 | 山东京博石油化工有限公司 | A kind of production method of food-grade n-hexane |
| CN110511107A (en) * | 2019-09-19 | 2019-11-29 | 山东京博石油化工有限公司 | A method of polytypic n-hexane is produced using C5 oil is reformed |
| CN112403013A (en) * | 2020-10-28 | 2021-02-26 | 洛阳金达石化有限责任公司 | Fine processing method of crude hexane |
| CN112225633A (en) * | 2020-10-29 | 2021-01-15 | 洛阳金达石化有限责任公司 | Production method of normal hexane containing heptane raw material |
| CN112341308A (en) * | 2020-10-29 | 2021-02-09 | 洛阳金达石化有限责任公司 | Production method of n-hexane and isohexane |
| CN113150825A (en) * | 2021-04-25 | 2021-07-23 | 中国石油化工股份有限公司 | Gasoline light fraction deep processing technology |
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