CN107032943A - Cryogen phase propane extracts system out - Google Patents
Cryogen phase propane extracts system out Download PDFInfo
- Publication number
- CN107032943A CN107032943A CN201710308099.5A CN201710308099A CN107032943A CN 107032943 A CN107032943 A CN 107032943A CN 201710308099 A CN201710308099 A CN 201710308099A CN 107032943 A CN107032943 A CN 107032943A
- Authority
- CN
- China
- Prior art keywords
- cryogen
- tank
- pipeline
- propane
- air inlet
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 82
- 239000001294 propane Substances 0.000 title claims abstract description 41
- 239000000284 extract Substances 0.000 title claims abstract description 10
- 239000003518 caustics Substances 0.000 claims abstract description 15
- 239000012071 phase Substances 0.000 claims description 24
- 239000003513 alkali Substances 0.000 claims description 15
- 239000007791 liquid phase Substances 0.000 claims description 9
- 238000004140 cleaning Methods 0.000 claims description 8
- 239000002253 acid Substances 0.000 claims description 6
- 125000000217 alkyl group Chemical group 0.000 claims description 4
- 238000005057 refrigeration Methods 0.000 claims description 4
- 230000006835 compression Effects 0.000 claims description 2
- 238000007906 compression Methods 0.000 claims description 2
- 239000007788 liquid Substances 0.000 claims 1
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 abstract description 22
- 239000001282 iso-butane Substances 0.000 abstract description 11
- 235000013847 iso-butane Nutrition 0.000 abstract description 11
- 238000007670 refining Methods 0.000 abstract description 6
- 230000007613 environmental effect Effects 0.000 abstract description 3
- 239000000126 substance Substances 0.000 abstract description 2
- 239000002994 raw material Substances 0.000 description 9
- 238000005804 alkylation reaction Methods 0.000 description 8
- 230000029936 alkylation Effects 0.000 description 7
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 4
- BKOOMYPCSUNDGP-UHFFFAOYSA-N 2-methylbut-2-ene Chemical group CC=C(C)C BKOOMYPCSUNDGP-UHFFFAOYSA-N 0.000 description 3
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 3
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 3
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- -1 carbonium ion Chemical class 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
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 2
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- IAQRGUVFOMOMEM-ARJAWSKDSA-N cis-but-2-ene Chemical compound C\C=C/C IAQRGUVFOMOMEM-ARJAWSKDSA-N 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000006471 dimerization reaction Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- SYSQUGFVNFXIIT-UHFFFAOYSA-N n-[4-(1,3-benzoxazol-2-yl)phenyl]-4-nitrobenzenesulfonamide Chemical class C1=CC([N+](=O)[O-])=CC=C1S(=O)(=O)NC1=CC=C(C=2OC3=CC=CC=C3N=2)C=C1 SYSQUGFVNFXIIT-UHFFFAOYSA-N 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Classifications
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/11—Purification; Separation; Use of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Cryogen phase propane extracts system out, and the present invention relates to chemical producing system technical field；It includes cryogen tank；It also includes caustic treater, settling tank, compressor and cooler；The gas outlet of cryogen tank is connected by the air inlet of pipeline and caustic treater, the gas outlet of caustic treater is connected by the air inlet of pipeline and settling tank, the gas outlet of settling tank is connected by the air inlet of pipeline and compressor, and the air inlet of compressor is connected by pipeline with cooler.It can reduce the carrying amount of the iso-butane in propane, it is to avoid the high pressure caused by propane content superelevation, also avoid pressure height from setting fire refining losses that torch causes, and environmental protection, practicality is stronger.
Description
Technical field
The present invention relates to chemical producing system technical field, and in particular to cryogen phase propane extracts system out.
Background technology
Alkyl plant is the alkylation process for the purpose of producing motor petrol, aviation gasoline, uses two class raw materials,
One class raw material is isoparaffin, because alkylated reaction follows carbonium ion mechanism, it is desirable to which alkane has tertiary carbon atom, so only
It can be found in >=C4 alkane；Another kind of raw material is small-numerator olefin, including propylene, butylene and amylene.Butylene is best
Raw material for alkylation, preferably, acid consumption is also minimum for product quality, and the acid consumption of propylene and amylene is almost several times of butylene.In recent years by
Developed faster in producing high-octane rating blending component by propylene dimerization, therefore selection propylene raw material for alkylation is done
Method is fewer and fewer, as amylene itself can as automotive fuel component, almost no one it as raw material for alkylation, therefore
The raw material of alkylation olefin is most importantly butylene, and it includes 4 kinds of isomers：Isobutene, 1- butylene, cis-2-butene and trans- 2-
Butylene.A small amount of propane is carried in raw material for alkylation, long-term aggregated, propane content can be continuously increased, and propane content is too high to make
Into system pressure rise, system overpressure can influence safety in production.The extraction of propane liquid phase is designed with current production system, liquid phase is taken out
The shortcoming gone out is iso-butane too high levels in cryogen, iso-butane as raw material for alkylation, if when civil liquefied gas is used, its nothing
It is suspected to be a kind of loss, the torch if pressure height is set fire adds refining losses, the pollution of environment is caused again, it would be highly desirable to improve.
The content of the invention
It is reasonable in design, make in view of the defects and deficiencies of the prior art, the present invention intends to provide one kind is simple in construction
System is extracted out with convenient cryogen phase propane, and it can reduce the carrying amount of the iso-butane in propane, it is to avoid because of propane content
High pressure caused by superelevation, also avoid pressure height from setting fire refining losses that torch causes, environmental protection, practicality is stronger.
To achieve the above object, the technical solution adopted by the present invention is：It includes cryogen tank；It also includes caustic treater, sunk
Tank, compressor and cooler drop；The gas outlet of cryogen tank is connected by the air inlet of pipeline and caustic treater, the gas outlet of caustic treater
Connected by the air inlet of pipeline and settling tank, the gas outlet of settling tank is connected by the air inlet of pipeline and compressor, compression
The air inlet of machine is connected by pipeline with cooler.
Further, it is connected with pressure gauge on described cryogen tank.
Further, it is equipped with control valve on the connecting pipe in the present invention between all parts.
The workflow of the present invention is as follows：
First, the circulation cryogen of alkyl plant shows after refrigeration compressor is extracted out in faintly acid, and feeding cryogen tank；
2nd, sent into by cryogen tank in caustic treater, phase propane is subjected to alkali cleaning；
3rd, the phase propane after alkali cleaning, is settled by settling tank, a small amount of alkali lye in abjection phase propane, it is to avoid by alkali lye
Take tank field to；
4th, the phase propane after settling is extracted out by compressor to be pressurized, and is changed into liquid phase after being cooled down through cooler, is sent into tank field.
After said structure, the present invention has the beneficial effect that：
1st, cryogen phase propane, which is extracted out, reduces the loss of iso-butane, it is to avoid refining losses caused by pressure height sets fire torch,
Protect environment；
2nd, the propane fixed gas faintly acid in cryogen, by alkali cleaning, then by settling tank sedimentation, it is to avoid alkali lye takes liquefaction balloon to
Tank, is extracted out through compressor, is cooled down through cooler, by liquid phase propane tank sending area, reduces the pressure of compressor refrigeration system；
3rd, cryogen phase propane is extracted out after system comes into operation, and has been prevented because cryogen tank D204 pressure height is set fire torch phenomenon, alkylation fire
Torch extinguishes, and is extracted out compared to liquid phase, and iso-butane carrying amount reduces 20% in propane, reduces refining losses, reduces iso-butane
Loss.
Brief description of the drawings
In order to illustrate more clearly about the embodiment of the present invention or technical scheme of the prior art, below will be to embodiment or existing
There is the accompanying drawing used required in technology description to be briefly described, it should be apparent that, drawings in the following description are only this
Some embodiments of invention, for those of ordinary skill in the art, without having to pay creative labor, may be used also
To obtain other accompanying drawings according to these accompanying drawings.
Fig. 1 is the process chart of the present invention.
Description of reference numerals：
Cryogen tank 1, caustic treater 2, settling tank 3, compressor 4, cooler 5.
Embodiment
The present invention is further illustrated below in conjunction with the accompanying drawings.
Referring to as shown in figure 1, the technical scheme that present embodiment is used is：It includes cryogen tank 1；It also includes alkali
Cleaning of evaporator 2, settling tank 3, compressor 4 and cooler 5；The gas outlet of cryogen tank 1 is connected by pipeline with the air inlet of caustic treater 2,
The gas outlet of caustic treater 2 is connected by the air inlet of pipeline and settling tank, and the gas outlet of settling tank 3 passes through pipeline and compressor 4
Air inlet connection, the air inlet of compressor is connected by pipeline with cooler 5.
Further, the model D204 of described cryogen tank 1, and be connected with pressure gauge thereon.
Further, control valve is equipped with the connecting pipe in present embodiment between all parts, for controlling
The conveying of material in system processed.
The workflow of present embodiment is as follows：
First, the circulation cryogen of alkyl plant shows after refrigeration compressor is extracted out in faintly acid, and feeding cryogen tank 1；
2nd, sent into by cryogen tank 1 in caustic treater 2, phase propane is subjected to alkali cleaning；
3rd, the phase propane after alkali cleaning, is settled by settling tank 3, a small amount of alkali lye in abjection phase propane, it is to avoid by alkali lye
Take tank field to；
4th, the phase propane after settling is extracted out by compressor 4 to be pressurized, and is changed into liquid phase after being cooled down through cooler 5, is sent into tank field.
Present embodiment is extracted the iso-butane carrying amount in system, its phase propane out compared to former design liquid phase propane and subtracted
Lack 20%, 6 tons of calculating are extracted out according to daily, can reduce 1.2 tons of isobutane losses daily, iso-butane and civil liquefied gas
2000 yuan of price difference, every year can 87.6 ten thousand yuan of synergy, if extracting system out using liquid phase propane, daily torch can burn up 6 tons of liquefaction
Gas, 3600 yuan of liquefied gas per ton, 2.16 ten thousand yuan of daily loss loses 7,880,000 yuan year.Phase propane extracts the nothing that comes into operation of system out
Torch need to be used, environment is protected.
After said structure, present embodiment has the beneficial effect that：Present embodiment provides a kind of structure letter
Single, cryogen phase propane reasonable in design, easy to use extracts system out, and it can reduce the carrying amount of the iso-butane in propane,
The high pressure caused by propane content superelevation is avoided, also avoid pressure height from setting fire refining losses that torch causes, environmental protection is practical
Property is stronger.
It is described above, it is merely illustrative of the technical solution of the present invention and unrestricted, those of ordinary skill in the art are to this hair
Other modifications or equivalent substitution that bright technical scheme is made, without departing from the spirit and scope of technical solution of the present invention,
It all should cover among scope of the presently claimed invention.
Claims (4)
1. cryogen phase propane extracts system out, it includes cryogen tank；It is characterized in that：It also includes caustic treater, settling tank, compression
Machine and cooler；The gas outlet of cryogen tank is connected by the air inlet of pipeline and caustic treater, and the gas outlet of caustic treater passes through pipeline
It is connected with the air inlet of settling tank, the gas outlet of settling tank is connected by the air inlet of pipeline and compressor, the air inlet of compressor
Mouth is connected by pipeline with cooler.
2. cryogen phase propane according to claim 1 extracts system out, it is characterised in that：Connecting tube between all parts
Control valve is equipped with road.
3. cryogen phase propane according to claim 1 extracts system out, it is characterised in that：It is connected with described cryogen tank
Pressure gauge.
4. cryogen phase propane extracts system out, it is characterised in that：Its workflow is as follows：
(1), the circulation cryogen of alkyl plant shows after refrigeration compressor is extracted out in faintly acid, and feeding cryogen tank；
(2), sent into by cryogen tank in caustic treater, phase propane is subjected to alkali cleaning；
(3), the phase propane after alkali cleaning, is settled by settling tank, a small amount of alkali lye in abjection phase propane, it is to avoid by alkali
Liquid band is to tank field；
(4) phase propane after, settling is extracted out by compressor to be pressurized, and is changed into liquid phase after being cooled down through cooler, is sent into tank field.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710308099.5A CN107032943A (en) | 2017-05-04 | 2017-05-04 | Cryogen phase propane extracts system out |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710308099.5A CN107032943A (en) | 2017-05-04 | 2017-05-04 | Cryogen phase propane extracts system out |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107032943A true CN107032943A (en) | 2017-08-11 |
Family
ID=59537728
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710308099.5A Pending CN107032943A (en) | 2017-05-04 | 2017-05-04 | Cryogen phase propane extracts system out |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107032943A (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2001034726A2 (en) * | 1999-10-21 | 2001-05-17 | Fluor Corporation | Methods and apparatus for high propane recovery |
| WO2004057253A2 (en) * | 2002-12-19 | 2004-07-08 | Abb Lummus Global Inc. | Lean reflux-high hydrocarbon recovery process |
| CN104151119B (en) * | 2014-08-08 | 2016-01-13 | 山东利丰达生物科技有限公司 | The method of octane-iso is prepared in the deep processing of a kind of carbon four |
| CN205435452U (en) * | 2016-04-01 | 2016-08-10 | 临沂金誉石化有限公司 | A settling cask for producing propane |
| CN205586791U (en) * | 2016-04-26 | 2016-09-21 | 山西页岩气有限公司 | Acidity recovery system that drops a hint in sulfuric acid process alkanisation technology |
-
2017
- 2017-05-04 CN CN201710308099.5A patent/CN107032943A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2001034726A2 (en) * | 1999-10-21 | 2001-05-17 | Fluor Corporation | Methods and apparatus for high propane recovery |
| WO2004057253A2 (en) * | 2002-12-19 | 2004-07-08 | Abb Lummus Global Inc. | Lean reflux-high hydrocarbon recovery process |
| CN104151119B (en) * | 2014-08-08 | 2016-01-13 | 山东利丰达生物科技有限公司 | The method of octane-iso is prepared in the deep processing of a kind of carbon four |
| CN205435452U (en) * | 2016-04-01 | 2016-08-10 | 临沂金誉石化有限公司 | A settling cask for producing propane |
| CN205586791U (en) * | 2016-04-26 | 2016-09-21 | 山西页岩气有限公司 | Acidity recovery system that drops a hint in sulfuric acid process alkanisation technology |
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| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20170811 |