CN202246472U - Device for extracting n-hexane and isohexane from crude hexane - Google Patents
Device for extracting n-hexane and isohexane from crude hexane Download PDFInfo
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- CN202246472U CN202246472U CN2011203345195U CN201120334519U CN202246472U CN 202246472 U CN202246472 U CN 202246472U CN 2011203345195 U CN2011203345195 U CN 2011203345195U CN 201120334519 U CN201120334519 U CN 201120334519U CN 202246472 U CN202246472 U CN 202246472U
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- product
- tower
- isohexane
- discharge port
- feed
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- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 title claims abstract description 104
- AFABGHUZZDYHJO-UHFFFAOYSA-N 2-Methylpentane Chemical compound CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 title claims abstract description 80
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 13
- 238000005194 fractionation Methods 0.000 claims abstract description 10
- 238000010992 reflux Methods 0.000 claims abstract description 10
- 239000007788 liquid Substances 0.000 claims abstract description 9
- 239000002994 raw material Substances 0.000 claims abstract description 7
- 239000001257 hydrogen Substances 0.000 claims description 36
- 229910052739 hydrogen Inorganic materials 0.000 claims description 36
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 25
- 238000000605 extraction Methods 0.000 claims description 12
- 239000002131 composite material Substances 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 239000000047 product Substances 0.000 description 40
- 239000003921 oil Substances 0.000 description 29
- 235000019198 oils Nutrition 0.000 description 29
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 6
- 239000000470 constituent Substances 0.000 description 5
- 150000002431 hydrogen Chemical class 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 description 4
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 238000009835 boiling Methods 0.000 description 2
- 238000009795 derivation Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 238000013022 venting Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 239000000443 aerosol Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 239000008157 edible vegetable oil Substances 0.000 description 1
- 238000004508 fractional distillation Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- GDOPTJXRTPNYNR-UHFFFAOYSA-N methylcyclopentane Chemical class CC1CCCC1 GDOPTJXRTPNYNR-UHFFFAOYSA-N 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000049 pigment Substances 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model discloses a device for extracting normal hexane and isohexane from crude hexane, which consists of a hydrogenation device and a fractionation device, wherein a raw material discharge port of a feeding/product heat exchanger in the hydrogenation device is connected with a feed port of a feeding heater, a discharge port of the feeding heater is connected with a feed port of a hydrogenation reactor, a discharge port of the hydrogenation reactor is connected with a product feed port of the feeding/product heat exchanger, a product discharge port of the feeding/product heat exchanger is connected with a feed port of a product cooler, and a discharge port of the product cooler is connected with a feed port of a low knockout drum; a feed inlet of a light component removal tower in the fractionating device is connected with a discharge outlet of the low molecular tank, circulating pumps are connected among liquid outlets at the bottoms of the light component removal tower, the isohexane removal oil tower and the n-hexane removal oil tower, and the tops of the light component removal tower, the isohexane removal oil tower and the n-hexane removal oil tower are respectively connected with a cooler and a reflux tank. The utility model discloses equipment is simple, convenient operation, and the energy consumption is low, and product quality is reliable and stable.
Description
Technical field
The utility model belongs to petrochemical complex separation method technical field, especially relates to a kind of device 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 the utility model provides a kind of device by thick hexane extraction normal hexane, isohexane.
For realizing the foregoing invention purpose, the utility model adopts following technical scheme:
A kind of device by thick hexane extraction normal hexane, isohexane; It is made up of hydrogenation unit and fractionation plant; Said hydrogenation unit comprises charging/product interchanger, feed heater, hydrogenator, 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 is through pipe connection, and 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, takes off isohexane oil tower and takes 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 through pipe connection recycle pump is arranged, 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, and wherein a pipeline is connected with tower top outlet, and another pipeline is the product delivery line.
Described device by thick hexane extraction normal hexane, isohexane; Its low branch tank top venting port divides flow container, circulating hydrogen compressor, desulphurization of recycle hydrogen reactor drum to be connected with recycle hydrogen through pipeline successively, and the discharge port of desulphurization of recycle hydrogen reactor drum is connected with the material inlet of charging/product interchanger.
Described device by thick hexane extraction normal hexane, isohexane, 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.
Owing to adopt aforesaid technical scheme, the utlity model has following meliority:
Should be by the device of thick hexane extraction normal hexane, isohexane, thick hexane of its raw material and hydrogen remove the benzene in the thick hexane through in hydrogenator, carrying out hydrogenation reaction, through fractionation plant, normal hexane, isohexane fractionation are come out again; The thick hexane of raw material mixed before getting into charging/product interchanger with hydrogen, can improve the heat exchange effect of interchanger; Hydrogenation reaction system is provided with the desulphurization of recycle hydrogen reactor drum, 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; 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 structural representation of the utility model one embodiment;
Among the figure: the 1-hydrogenator; 2-desulphurization of recycle hydrogen reactor drum; 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 the technical scheme of the utility model is done further explain below.
As shown in Figure 1; Should be by the device of thick hexane extraction normal hexane, isohexane; 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 are through pipe connection, and the opening for feed of the discharge port of feed heater and hydrogenator 1 is through pipe connection, and 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, and low branch tank top venting port divides flow container 4, circulating hydrogen compressor 3, desulphurization of recycle hydrogen reactor drum 2 to be connected with recycle hydrogen through pipeline successively, and the discharge port of desulphurization of recycle hydrogen reactor drum 2 is connected with the material inlet of charging/product interchanger 25; Said fractionation plant comprises cut light tower 6, takes off isohexane oil tower 18 and takes 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, second recycle pump 19 respectively through pipeline; The top of cut light tower is all through pipe connection first water cooler 7 and first return tank 8, and the top of taking off isohexane oil tower is all through pipe connection second water cooler 9 and second return tank 10, and 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 corresponding with it return tank link to each other through pipeline; Return tank links to each other with reflux pump through pipeline, and the reflux pump outlet connects two pipelines, and 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, and taking off isohexane oil tower derivation product is isohexane 17, and taking off normal hexane oil tower derivation product is normal hexane 13; The bottom liquid outlet of taking off normal hexane oil tower links to each other with the 3rd recycle pump 16, interchanger 15 through pipeline successively, obtains the product heptane through pumping, after lowering the temperature.
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 drum 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 drum 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, a part of 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, a part of isohexane warp second water cooler, 9 condensations 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, a part of normal hexane warp the 3rd water cooler 11 condensations 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 (3)
1. device by thick hexane extraction normal hexane, isohexane; 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, 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 is through pipe connection, and 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), takes off isohexane oil tower (18) and takes 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, and return tank links to each other with reflux pump through pipeline, and the reflux pump outlet connects two pipelines; Wherein a pipeline is connected with tower top outlet, and another pipeline is the product delivery line.
2. the device by thick hexane extraction normal hexane, isohexane according to claim 1; 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 drum (2) to be connected with recycle hydrogen through pipeline successively, and the discharge port of desulphurization of recycle hydrogen reactor drum is connected with the material inlet of charging/product interchanger (25).
3. the device by thick hexane extraction normal hexane, isohexane according to claim 1 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.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011203345195U CN202246472U (en) | 2011-09-07 | 2011-09-07 | Device for extracting n-hexane and isohexane from crude hexane |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011203345195U CN202246472U (en) | 2011-09-07 | 2011-09-07 | Device for extracting n-hexane and isohexane from crude hexane |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202246472U true CN202246472U (en) | 2012-05-30 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011203345195U Expired - Lifetime CN202246472U (en) | 2011-09-07 | 2011-09-07 | Device for extracting n-hexane and isohexane from crude hexane |
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| CN (1) | CN202246472U (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103833499A (en) * | 2012-11-27 | 2014-06-04 | 中国石油天然气股份有限公司 | Preparation method of high-purity isohexane solvent oil |
| 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 |
| 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 |
| WO2023125044A1 (en) * | 2021-12-31 | 2023-07-06 | 中国石油天然气股份有限公司 | Method and system for producing solvent oil from raffinate oil |
-
2011
- 2011-09-07 CN CN2011203345195U patent/CN202246472U/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103833499A (en) * | 2012-11-27 | 2014-06-04 | 中国石油天然气股份有限公司 | Preparation method of high-purity isohexane solvent oil |
| CN103833499B (en) * | 2012-11-27 | 2016-03-09 | 中国石油天然气股份有限公司 | Preparation method of high-purity isohexane solvent oil |
| 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 |
| 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 |
| WO2023125044A1 (en) * | 2021-12-31 | 2023-07-06 | 中国石油天然气股份有限公司 | Method and system for producing solvent oil from raffinate oil |
| CN116408090A (en) * | 2021-12-31 | 2023-07-11 | 中国石油天然气股份有限公司 | Hydrogenation catalyst, preparation method thereof, method and system for producing solvent oil by reforming raffinate oil |
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| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20120530 |
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| CX01 | Expiry of patent term |