CN108558592A - A kind of alkane coalescence fractionation process - Google Patents
A kind of alkane coalescence fractionation process Download PDFInfo
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- CN108558592A CN108558592A CN201810574645.4A CN201810574645A CN108558592A CN 108558592 A CN108558592 A CN 108558592A CN 201810574645 A CN201810574645 A CN 201810574645A CN 108558592 A CN108558592 A CN 108558592A
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- Prior art keywords
- tower
- deisobutanizer
- passed
- fractionation process
- alkane
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
- C07C7/17—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound with acids or sulfur oxides
Abstract
The invention discloses a kind of alkane to coalesce fractionation process, including step 1, and alkylation reaction object is condensed；Condensed alkylation reaction object is passed through in settler by step 2；Hydrocarbon-type oil is mutually passed through caustic treater depickling by step 3；Step 4 enters deisobutanizer after oil phase substance is heated and detaches；Step 5, overhead are sent into air cooler condensation；The hydro carbons of tower bottom is entered de- normal butane tower by step 6 from force feed；Step 7, alkylate oil, which enters in separation equipment, to be detached；Technique isooctane and skellysolve E are discharged into deisobutanizer by step 8 again；Step 9, by after cooling technique isooctane and skellysolve E cool down.The technique uses reaction effluent to be mixed into pickling tank with acid, and effluent hydro carbons and acid are detached, and the sour Returning reactor recycling that mutually settles down, alkali mutually recycles；Overhead is used as recycle isobutane Returning reacting system through air cooler condensation rear portion lease making cooler cooling, reaches recycling effect of material.
Description
Technical field
The present invention relates to a kind of industrial fractionation process, specifically a kind of alkane coalesces fractionation process.
Background technology
Fractionation is a kind of method for the mixture for detaching several different boilings;A certain mixture is heated, for mixed
The different boiling for closing each ingredient in object carries out refrigerated separation into relatively pure single substance process.It is given birth in the process without novel substance
At only the starting substance is detached, belongs to physical change.Fractionation is actually repeatedly distillation, it is more suitable for separating-purifying
The liquid organic mixture that boiling point is not much different.Such as the fractionation of coal tar;The fractionation of oil.
At present often there is the waste of material, portion of secondary in existing alkane coalescence fractionation process during fractionation
Help substance that can not realize circulation and stress after utilization so that fractionation is of high cost, is unfavorable for large-scale industrialized production.
Invention content
The purpose of the present invention is to provide a kind of alkane to coalesce fractionation process, to solve mentioned above in the background art ask
Topic.
To achieve the above object, the present invention provides the following technical solutions：
A kind of alkane coalescence fractionation process, includes the following steps：
Step 1 cools down being passed through in condenser from the alkylation reaction object being discharged in reactor, in alkylation reaction object and condenser
Cryogen carry out heat exchange；
Condensed alkylation reaction object is passed through in settler by step 2, and hydro carbons and acid detach in reactant, will using drawing liquid pump
Sour phase substance after sedimentation pumps in reactor；
Step 3 is passed through alkali cleaning after mixing the hydro carbons of oil phase in step 2 with the sodium hydroxide solution that mass ratio is 10
The remaining a small amount of acid of tank removing, alkali mutually recycle, regular discharge system；
Step 4, oil phase substance are passed through liquid separation tank removing acid after Sour gas disposal, add through heat exchanger, feed heater
Enter deisobutanizer after heat to detach, oil phase substance is heated to 50-60 DEG C by feed heater；
Step 5 will enter return tank of top of the tower by overhead in step 4 after being sent into air cooler condensation, and distillate part is from tower
Top reflux is partly used as recycle isobutane Returning reacting system, extra iso-butane to send to iso-butane tank through cooler cooling；
The hydro carbons of tower bottom is entered de- normal butane tower by step 6 from force feed, and tower top separates normal butane, after condensed cooler heat exchange
Part overhead reflux partly sends to products pot group；
Step 7, bottom of tower be discharged alkylate oil, alkylate oil, which enters in separation equipment, to be detached, obtained after separation technique isooctane and
Skellysolve E；
Technique isooctane and skellysolve E are discharged into deisobutanizer and carry out heat exchange cooling by step 8 again；
Step 9 is discharged into technique isooctane and skellysolve E after carrying out heat exchange cooling in deisobutanizer and is cooled down, cold
But it is sent into products pot group afterwards.
As a further solution of the present invention：Alkylation reaction object temperature is reduced to 25-30 DEG C in the step 1.
As further scheme of the invention：Drawing liquid pump rotary power is 180-200 kilowatt hours in the step 2.
As further scheme of the invention：Heat exchanger uses heat regenerator in the step 4.
As further scheme of the invention：Temperature after the condensed cooler heat exchange of the hydro carbons of tower bottom in the step 6
Degree is reduced to 30-37 DEG C.
As further scheme of the invention：Technique isooctane and skellysolve E are in deisobutanizer in the step 8
Interior heat exchange, temperature are down to 15-25 DEG C.
As further scheme of the invention：Cooling temperature is set as 5-8 DEG C in the step 9.
Compared with prior art, the beneficial effects of the invention are as follows：The technique is mixed into acid using reaction effluent with acid
Cleaning of evaporator detaches effluent hydro carbons and acid, the sour Returning reactor recycling that mutually settles down, while alkali mutually recycles；Tower
It pushes up distillate and is used as recycle isobutane Returning reacting system through air cooler condensation rear portion lease making cooler cooling, reach following for material
Ring uses effect, saves raw material and energy consumption, reduces production cost.
Specific implementation mode
It is clearly and completely described below in conjunction with the technical solution in the embodiment of the present invention, it is clear that described reality
It is only a part of the embodiment of the present invention to apply example, instead of all the embodiments.Based on the embodiments of the present invention, this field is general
The every other embodiment that logical technical staff is obtained without making creative work belongs to what the present invention protected
Range.
Embodiment one
In the embodiment of the present invention, a kind of alkane coalescence fractionation process includes the following steps：
Step 1 cools down being passed through in condenser from the alkylation reaction object being discharged in reactor, in alkylation reaction object and condenser
Cryogen carry out heat exchange；
Condensed alkylation reaction object is passed through in settler by step 2, and hydro carbons and acid detach in reactant, will using drawing liquid pump
Sour phase substance after sedimentation pumps in reactor, realizes that recycling for acid solution, drawing liquid pump rotary power are 180 kilowatt hours；
Step 3 is passed through alkali cleaning after mixing the hydro carbons of oil phase in step 2 with the sodium hydroxide solution that mass ratio is 10
The remaining a small amount of acid of tank removing, alkali mutually recycle, regular discharge system；
Step 4, oil phase substance are passed through liquid separation tank removing acid after Sour gas disposal, add through heat exchanger, feed heater
Enter deisobutanizer after heat to detach, heat exchanger uses heat regenerator, feed heater that oil phase substance is heated to 50 DEG C；
Step 5 will enter return tank of top of the tower by overhead in step 4 after being sent into air cooler condensation, and distillate part is from tower
Top reflux is partly used as recycle isobutane Returning reacting system, extra iso-butane to send to iso-butane tank through cooler cooling；
The hydro carbons of tower bottom is entered de- normal butane tower by step 6 from force feed, and tower top separates normal butane, after condensed cooler heat exchange
Part overhead reflux partly sends to products pot group；
Step 7, bottom of tower be discharged alkylate oil, alkylate oil, which enters in separation equipment, to be detached, obtained after separation technique isooctane and
Skellysolve E；
Technique isooctane and skellysolve E are discharged into deisobutanizer and carry out heat exchange cooling by step 8 again, and temperature is down to 25 DEG C；
Step 9 is discharged into technique isooctane and skellysolve E after carrying out heat exchange cooling in deisobutanizer and is cooled down, cold
But temperature is set as 5 DEG C, and products pot group is sent into after cooling.
Embodiment two
In the embodiment of the present invention, a kind of alkane coalescence fractionation process includes the following steps：
Step 1 cools down being passed through in condenser from the alkylation reaction object being discharged in reactor, in alkylation reaction object and condenser
Cryogen carry out heat exchange, alkylation reaction object temperature is reduced to 25 DEG C；
Condensed alkylation reaction object is passed through in settler by step 2, and hydro carbons and acid detach in reactant, will using drawing liquid pump
Sour phase substance after sedimentation pumps in reactor, realizes that recycling for acid solution, drawing liquid pump rotary power are 200 kilowatt hours；
Step 3 is passed through alkali cleaning after mixing the hydro carbons of oil phase in step 2 with the sodium hydroxide solution that mass ratio is 10
The remaining a small amount of acid of tank removing, alkali mutually recycle, regular discharge system；
Step 4, oil phase substance are passed through liquid separation tank removing acid after Sour gas disposal, add through heat exchanger, feed heater
Enter deisobutanizer after heat to detach；
Step 5 will enter return tank of top of the tower by overhead in step 4 after being sent into air cooler condensation, and distillate part is from tower
Top reflux is partly used as recycle isobutane Returning reacting system, extra iso-butane to send to iso-butane tank through cooler cooling；
The hydro carbons of tower bottom is entered de- normal butane tower by step 6 from force feed, and tower top separates normal butane, after condensed cooler heat exchange
Temperature is reduced to 37 DEG C of part overhead refluxes, partly sends to products pot group；
Step 7, bottom of tower be discharged alkylate oil, alkylate oil, which enters in separation equipment, to be detached, obtained after separation technique isooctane and
Skellysolve E；
Technique isooctane and skellysolve E are discharged into deisobutanizer and carry out heat exchange cooling by step 8 again, and temperature is down to 15 DEG C；
Step 9 is discharged into technique isooctane and skellysolve E after carrying out heat exchange cooling in deisobutanizer and is cooled down, cold
But it is sent into products pot group afterwards.
Embodiment three
In the embodiment of the present invention, a kind of alkane coalescence fractionation process includes the following steps：
Step 1 cools down being passed through in condenser from the alkylation reaction object being discharged in reactor, in alkylation reaction object and condenser
Cryogen carry out heat exchange, alkylation reaction object temperature is reduced to 30 DEG C；
Condensed alkylation reaction object is passed through in settler by step 2, and hydro carbons and acid detach in reactant, will using drawing liquid pump
Sour phase substance after sedimentation pumps in reactor, and drawing liquid pump rotary power is 200 kilowatt hours；
Step 3 is passed through alkali cleaning after mixing the hydro carbons of oil phase in step 2 with the sodium hydroxide solution that mass ratio is 10
The remaining a small amount of acid of tank removing, alkali mutually recycle, regular discharge system；
Step 4, oil phase substance are passed through liquid separation tank removing acid after Sour gas disposal, add through heat exchanger, feed heater
Enter deisobutanizer after heat to detach, heat exchanger uses heat regenerator, feed heater that oil phase substance is heated to 60 DEG C；
Step 5 will enter return tank of top of the tower by overhead in step 4 after being sent into air cooler condensation, and distillate part is from tower
Top reflux is partly used as recycle isobutane Returning reacting system, extra iso-butane to send to iso-butane tank through cooler cooling；
The hydro carbons of tower bottom is entered de- normal butane tower by step 6 from force feed, and tower top separates normal butane, after condensed cooler heat exchange
Temperature is reduced to 30 DEG C of part overhead refluxes, partly sends to products pot group；
Step 7, bottom of tower be discharged alkylate oil, alkylate oil, which enters in separation equipment, to be detached, obtained after separation technique isooctane and
Skellysolve E；
Technique isooctane and skellysolve E are discharged into deisobutanizer and carry out heat exchange cooling by step 8 again；
Step 9 is discharged into technique isooctane and skellysolve E after carrying out heat exchange cooling in deisobutanizer and is cooled down, cold
But temperature is set as 8 DEG C, and products pot group is sent into after cooling.
It is obvious to a person skilled in the art that invention is not limited to the details of the above exemplary embodiments, Er Qie
In the case of without departing substantially from spirit or essential attributes of the invention, the present invention can be realized in other specific forms.Therefore, no matter
From the point of view of which point, the present embodiments are to be considered as illustrative and not restrictive, and the scope of the present invention is by appended power
Profit requires rather than above description limits, it is intended that all by what is fallen within the meaning and scope of the equivalent requirements of the claims
Variation is included within the present invention.
In addition, it should be understood that although this specification is described in terms of embodiments, but not each embodiment is only wrapped
Containing an independent technical solution, this description of the specification is merely for the sake of clarity, and those skilled in the art should
It considers the specification as a whole, the technical solutions in the various embodiments may also be suitably combined, forms those skilled in the art
The other embodiment being appreciated that.
Claims (7)
1. a kind of alkane coalesces fractionation process, which is characterized in that include the following steps：
Step 1 cools down being passed through in cryogen condenser from the alkylation reaction object being discharged in reactor, alkylation reaction object and condensation
Cryogen in device carries out heat exchange；
Condensed alkylation reaction object is passed through in settler by step 2, and hydro carbons and acid detach in reactant, will using drawing liquid pump
Sour phase substance after sedimentation pumps in reactor；
Step 3 is passed through the remaining a small amount of acid of caustic treater removing after mixing hydro carbons oil phase in step 2 with 10%NaOH,
Alkali mutually recycles, regular discharge system；
Step 4, oil phase substance are passed through liquid separation tank removing acid after Sour gas disposal, add through heat exchanger, feed heater
Enter deisobutanizer after heat to detach, oil phase substance is heated to 50-60 °C by feed heater；
Step 4 kind gains are passed through deisobutanizer separation by step 5, and overhead enters after being sent into air cooler condensation
Return tank of top of the tower, distillate part is partly used as recycle isobutane Returning reacting system from overhead reflux through cooler cooling, more
Remaining iso-butane sends to iso-butane tank；
The hydro carbons of tower bottom is entered de- normal butane tower by step 6 from force feed, and tower top separates normal butane, after condensed cooler heat exchange
Part overhead reflux partly sends to products pot group；
Step 7, bottom of tower be discharged alkylate oil, alkylate oil, which enters in separation equipment, to be detached, obtained after separation technique isooctane and
Skellysolve E；
Technique isooctane and skellysolve E are discharged into deisobutanizer and carry out heat exchange cooling by step 8 again；
Step 9 is discharged into technique isooctane and skellysolve E after carrying out heat exchange cooling in deisobutanizer and is cooled down, cold
But it is sent into products pot group afterwards.
2. a kind of alkane according to claim 1 coalesces fractionation process, which is characterized in that in the step 1 that alkyl is anti-
Object temperature is answered to be reduced to 25-30 °C.
3. a kind of alkane according to claim 1 coalesces fractionation process, which is characterized in that drawing liquid pump revolves in the step 2
It is 180-200 kilowatt hours to turn power.
4. a kind of alkane according to claim 1 coalesces fractionation process, which is characterized in that heat exchanger is adopted in the step 4
Use heat regenerator.
5. a kind of alkane according to claim 1 coalesces fractionation process, which is characterized in that tower bottom in the step 6
Temperature is reduced to 30-37 °C after the condensed cooler heat exchange of hydro carbons.
6. a kind of alkane according to claim 1 coalesces fractionation process, which is characterized in that technique is different pungent in the step 8
Alkane and skellysolve E exchange heat in deisobutanizer, and temperature is down to 15-25 °C.
7. a kind of alkane according to claim 1 coalesces fractionation process, which is characterized in that cooling temperature in the step 9
It is set as 5-8 °C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810574645.4A CN108558592A (en) | 2018-06-06 | 2018-06-06 | A kind of alkane coalescence fractionation process |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201810574645.4A CN108558592A (en) | 2018-06-06 | 2018-06-06 | A kind of alkane coalescence fractionation process |
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| CN108558592A true CN108558592A (en) | 2018-09-21 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110129092A (en) * | 2019-04-28 | 2019-08-16 | 东营市科德化工有限公司 | A kind of super oil and preparation method thereof for aviation gasoline |
-
2018
- 2018-06-06 CN CN201810574645.4A patent/CN108558592A/en not_active Withdrawn
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110129092A (en) * | 2019-04-28 | 2019-08-16 | 东营市科德化工有限公司 | A kind of super oil and preparation method thereof for aviation gasoline |
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Application publication date: 20180921 |