CN216192101U - Alkylation reaction system capable of achieving rapid start-up and shutdown - Google Patents
Alkylation reaction system capable of achieving rapid start-up and shutdown Download PDFInfo
- Publication number
- CN216192101U CN216192101U CN202122584847.7U CN202122584847U CN216192101U CN 216192101 U CN216192101 U CN 216192101U CN 202122584847 U CN202122584847 U CN 202122584847U CN 216192101 U CN216192101 U CN 216192101U
- Authority
- CN
- China
- Prior art keywords
- pipeline
- communicated
- acid
- tank
- shutdown
- 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.)
- Active
Links
- 238000005804 alkylation reaction Methods 0.000 title claims abstract description 18
- 239000002253 acid Substances 0.000 claims abstract description 55
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims abstract description 19
- 238000006243 chemical reaction Methods 0.000 claims abstract description 17
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 claims abstract description 16
- 238000005406 washing Methods 0.000 claims abstract description 14
- 230000001174 ascending effect Effects 0.000 claims abstract description 11
- 238000005554 pickling Methods 0.000 claims abstract description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000001282 iso-butane Substances 0.000 claims abstract description 8
- 238000007670 refining Methods 0.000 claims abstract description 7
- 238000005194 fractionation Methods 0.000 claims abstract description 5
- 239000003513 alkali Substances 0.000 claims abstract description 3
- 238000010992 reflux Methods 0.000 claims description 20
- 238000007599 discharging Methods 0.000 claims description 5
- 229930195733 hydrocarbon Natural products 0.000 description 7
- 150000002430 hydrocarbons Chemical class 0.000 description 7
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- 239000000463 material Substances 0.000 description 5
- 238000000034 method Methods 0.000 description 4
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 230000029936 alkylation Effects 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000839 emulsion Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses an alkylation reaction system capable of realizing rapid start-up and shutdown, which comprises: the reaction unit comprises a reactor body, an acid pouring pump and a settling tank; the refining unit comprises a pickling tank, an alkali washing tank and a water washing tank which are sequentially arranged and communicated, and the pickling tank is communicated with the reaction unit; the fractionation unit comprises a heat exchanger, an isobutane removing module and an n-butane removing module which are sequentially arranged and communicated, and the heat exchanger is communicated with the water washing tank; the acid removal device comprises a reactor body and is characterized in that an ascending pipeline and a descending pipeline are arranged on one side of the reactor body, the ascending pipeline and the descending pipeline are communicated with a settling tank, an acid discharge pipeline is arranged on the other side of the reactor body, and an acid pouring pump is arranged between the acid discharge pipeline and the descending pipeline. The utility model shortens the time of restarting after shutdown and saves acid.
Description
Technical Field
The utility model relates to the technical field of alkylation production, in particular to an alkylation reaction system capable of realizing rapid start-up and shutdown.
Background
The alkylation reaction is a reaction process for introducing alkyl into organic molecules by utilizing addition or replacement reaction, and the alkylation reaction is used as an important synthesis means and is widely applied to a plurality of chemical production processes.
At present, raw material olefin and isobutane in an alkylation device reactor generate alkylate oil in the presence of a sulfuric acid catalyst, acid-hydrocarbon emulsion which is completely reacted directly enters an acid settler through an ascending pipe, acid and hydrocarbon are settled and separated, a separated acid liquor descending pipe returns to the reactor for reuse reaction, and in a settlement system, acid circulation is naturally circulated by means of the difference of specific gravity of materials in the ascending pipe and the descending pipe.
However, when the reactor is stopped and then started, the acid in the reactor needs to be discharged, because the reactor is started when a large amount of acid exists in the reactor, the starting current of the reactor is too large, so that the reactor cannot be started, the normal treatment step is to close an acid liquor downcomer valve, settle the acid and the oil in the reactor for full separation, discharge all acid phases to a waste acid storage tank, fill the acid boundary position of the settling tank to a normal liquid level by injecting new acid, and finally start the reactor again. In the process, the sedimentation needs 0.5 hour, the acid discharge needs 1 hour, the acid supplement needs 0.5 hour, and the total time needs about 2 hours, so that the efficiency is low, and the waste of resources is caused because the acid in the reactor is discharged to a waste acid storage tank and part of hydrocarbons are carried outwards inevitably, which is not enough.
SUMMERY OF THE UTILITY MODEL
The present invention is directed to an alkylation reaction system with rapid start-up and shut-down to solve the above-mentioned problems.
In order to achieve the purpose, the utility model provides the following technical scheme: an alkylation reaction system with rapid start-up shutdown, comprising:
the reaction unit comprises a reactor body, an acid pouring pump and a settling tank;
the refining unit comprises a pickling tank, an alkali washing tank and a water washing tank which are sequentially arranged and communicated, and the pickling tank is communicated with the reaction unit;
the fractionation unit comprises a heat exchanger, an isobutane removing module and an n-butane removing module which are sequentially arranged and communicated, and the heat exchanger is communicated with the water washing tank;
the acid removal device comprises a reactor body and is characterized in that an ascending pipeline and a descending pipeline are arranged on one side of the reactor body, the ascending pipeline and the descending pipeline are communicated with a settling tank, an acid discharge pipeline is arranged on the other side of the reactor body, and an acid pouring pump is arranged between the acid discharge pipeline and the descending pipeline.
In a plurality of embodiments, an input pipeline and an output pipeline are arranged on two sides of the acid pouring pump, the input pipeline is communicated with the acid discharging pipeline, the output pipeline is communicated with the descending pipeline, and control valves are arranged on the input pipeline and the output pipeline.
In several embodiments, a downcomer valve is disposed on the downcomer conduit, the downcomer valve being disposed between the reactor body and the outlet conduit.
In several embodiments, a riser valve is also provided on the riser pipe.
In several embodiments, the deisobutanizer module includes a deisobutanizer, an air cooler, a first reflux drum, and a first electric pump, wherein the air cooler is communicated with a top outlet of the deisobutanizer, the first reflux drum is communicated with the air cooler, and the first electric pump is used for communicating the deisobutanizer with the first reflux drum.
In several embodiments, the n-butane removing module comprises a n-butane removing tower, a condensing heat exchanger, a second reflux tank and a second electric pump, wherein the condensing heat exchanger is communicated with a top outlet of the n-butane removing tower, the second reflux tank is communicated with the condensing heat exchanger, and the second electric pump is used for communicating the n-butane removing tower with the second reflux tank.
The utility model has the technical effects and advantages that:
the process of settling and separating acid when the settling tank is shut down and then started greatly shortens the time of restarting after shutdown, and reduces the time from the original 2 hours to 0.5 hour; and the separated acid can be reused in the reactor body again without being discharged, so that the consumption of the new acid is saved, and the utilization rate of resources is improved.
Drawings
FIG. 1 is a schematic view of a partially enlarged structure of a reaction unit in example 1 of the present invention;
fig. 2 is a schematic view of the overall structure in embodiment 1 of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
The utility model provides an alkylation reaction system with rapid start-up and shutdown as shown in fig. 1-2, which mainly comprises a reaction unit 100, a refining unit 200 and a fractionation unit 300 which are distributed in sequence, so as to carry out reaction and refining fractionation processes.
Specifically, the reaction unit 100 includes a reactor body 110, an acid pouring pump 120 and a settling tank 130, wherein an ascending pipe 140 and a descending pipe 150 are arranged on one side of the reactor body 110, the ascending pipe 140 and the descending pipe 150 are both communicated with the settling tank 130, an acid discharging pipe 160 is arranged on the other side of the reactor body 110, and the acid pouring pump 120 is arranged between the acid discharging pipe 160 and the descending pipe 150.
An input pipeline 121 and an output pipeline 122 are arranged on two sides of the acid pouring pump 120, the input pipeline 121 is communicated with an acid discharging pipeline 160, the output pipeline 122 is communicated with a descending pipeline 150, and control valves 123 are arranged on the input pipeline 121 and the output pipeline 122.
In view of the above, the downcomer valve 151 is disposed on the downcomer 150, the riser valve 141 is disposed on the riser 140, and the downcomer valve 151 is disposed between the reactor body 110 and the outlet 122.
When the reactor is stopped, the control valve 123 on the input pipeline 121 is opened, acid pouring is started, the acid hydrocarbon mixture in the reactor body is conveyed to the settling tank 130 through the descending pipeline 150 by the control valve 120, the descending pipe valve 151 on the descending pipeline 150 is closed, the acid is settled to the bottom of the settling tank 130 after the mixture reaches the settling tank 130, and the oil phase returns to the reactor body through the ascending pipeline 140, so that the acid in the reactor can be quickly transferred to the settling tank, and generally only 0.5 hour is needed.
The refining unit 200 comprises a pickling tank 210, an alkaline washing tank 220 and a water washing tank 230 which are sequentially arranged and communicated, wherein the pickling tank 210 is communicated with the reaction unit 100 to receive materials from the reaction unit 100.
The fractionating unit 300 comprises a heat exchanger 310, an isobutane removing module and an n-butane removing module which are sequentially arranged and communicated, wherein the heat exchanger 310 is communicated with the water washing tank 230.
The deisobutanizer module comprises an deisobutanizer 321, an air cooler 322, a first reflux tank 323 and a first electric pump 324, wherein the air cooler 322 is communicated with an outlet at the top of the deisobutanizer 321, the first reflux tank 323 is communicated with the air cooler 322, and the first electric pump 324 is used for communicating the deisobutanizer 321 with the first reflux tank 323.
Correspondingly, the n-butane removing module comprises a n-butane removing tower 331, a condensation heat exchanger 332, a second reflux tank 333 and a second electric pump 334, wherein the condensation heat exchanger 332 is communicated with the top outlet of the n-butane removing tower 331, the second reflux tank 333 is communicated with the condensation heat exchanger 332, and the second electric pump 334 is used for communicating the n-butane removing tower 331 with the second reflux tank 333.
During operation, materials enter the alkylation reactor body 110 to react under the action of a sulfuric acid catalyst, a mixture of a reaction product and sulfuric acid enters the settling tank 130, most of separated acid liquor returns to the reactor to be recycled, and a small part of 90% of acid is discharged to the 90% acid tank to be stored; partial material flow discharged from the upper part of the settling tank is partially vaporized by the hot side of the reactor body and enters a flash tank, and partial material flow is subjected to heat exchange and temperature rise and then enters a refining system for treatment; the reaction effluent is mixed with acid after heat exchange and enters a pickling tank 210 for pickling, an acid phase in the pickling tank 210 is settled and returns to the reactor for recycling, an oil phase is mixed with 10% NaOH and then enters an alkaline washing tank 220 for removing acid substances, an alkaline phase is recycled and is periodically discharged out of the system; the oil phase is washed by water in the water washing tank 230 to remove salt substances, the oil phase is heated by the heat exchanger 310 after being washed by water and then enters the deisobutanizer 321 to separate isobutane, distillate at the top of the tower is condensed by the air cooler 322 and then enters the first reflux tank 323 at the top of the tower, part of the distillate flows back to the deisobutanizer 321 through the first electric pump 324, part of the distillate is cooled by the cooler and returns to the reaction system as circulating isobutane, and redundant isobutane is sent to the deisobutanizer; then the hydrocarbons at the bottom of the deisobutanizer 321 are sent to a n-butane removal tower 331 under self pressure, n-butane is separated from the tower top, the hydrocarbons enter a second reflux tank 333 at the top side of the tower after heat exchange of a condensing heat exchanger 332, part of the hydrocarbons flow back to the n-butane removal tower 331 through a second electric pump 334, and part of the hydrocarbons flow back to a product tank group; and the product at the bottom of the tower is alkylate oil, and the alkylate oil exchanges heat with the feed of the deisobutanizer firstly to reduce the temperature and then is sent to a product tank group after being cooled.
Finally, it should be noted that: although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments or portions thereof without departing from the spirit and scope of the utility model.
Claims (6)
1. An alkylation reaction system with rapid start-up and shut-down, comprising:
the reaction unit comprises a reactor body, an acid pouring pump and a settling tank;
the refining unit comprises a pickling tank, an alkali washing tank and a water washing tank which are sequentially arranged and communicated, and the pickling tank is communicated with the reaction unit;
the fractionation unit comprises a heat exchanger, an isobutane removing module and an n-butane removing module which are sequentially arranged and communicated, and the heat exchanger is communicated with the water washing tank;
the acid removal device comprises a reactor body and is characterized in that an ascending pipeline and a descending pipeline are arranged on one side of the reactor body, the ascending pipeline and the descending pipeline are communicated with a settling tank, an acid discharge pipeline is arranged on the other side of the reactor body, and an acid pouring pump is arranged between the acid discharge pipeline and the descending pipeline.
2. The alkylation reaction system with rapid start-up and shutdown as claimed in claim 1, wherein an input pipeline and an output pipeline are arranged on two sides of the acid pouring pump, the input pipeline is communicated with the acid discharging pipeline, the output pipeline is communicated with the descending pipeline, and control valves are arranged on the input pipeline and the output pipeline.
3. The rapid start-up shutdown alkylation reaction system according to claim 2, wherein the downcomer valve is disposed on the downcomer conduit and is disposed between the reactor body and the outlet conduit.
4. The rapid start-up shutdown alkylation reaction system according to claim 2, wherein the riser pipe is provided with a riser valve.
5. The alkylation reaction system with rapid start-up and shutdown as claimed in claim 1, wherein the deisobutanizer module comprises a deisobutanizer, an air cooler, a first reflux tank and a first electric pump, the air cooler is communicated with a top outlet of the deisobutanizer, the first reflux tank is communicated with the air cooler, and the first electric pump is used for communicating the deisobutanizer with the first reflux tank.
6. The alkylation reaction system with rapid start-up and shutdown as claimed in claim 1, wherein the n-butane removal module comprises an n-butane removal tower, a condensing heat exchanger, a second reflux tank and a second electric pump, the condensing heat exchanger is communicated with a top outlet of the n-butane removal tower, the second reflux tank is communicated with the condensing heat exchanger, and the second electric pump is used for communicating the n-butane removal tower with the second reflux tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122584847.7U CN216192101U (en) | 2021-10-26 | 2021-10-26 | Alkylation reaction system capable of achieving rapid start-up and shutdown |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122584847.7U CN216192101U (en) | 2021-10-26 | 2021-10-26 | Alkylation reaction system capable of achieving rapid start-up and shutdown |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN216192101U true CN216192101U (en) | 2022-04-05 |
Family
ID=80890132
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202122584847.7U Active CN216192101U (en) | 2021-10-26 | 2021-10-26 | Alkylation reaction system capable of achieving rapid start-up and shutdown |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN216192101U (en) |
-
2021
- 2021-10-26 CN CN202122584847.7U patent/CN216192101U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104151119A (en) | Method for preparing isooctane by deep processing of n-butane | |
| CN110203986A (en) | The method for reducing the system of ammonia-nitrogen content and reducing ammonia-nitrogen content | |
| JP2017525666A (en) | Method for producing nitrobenzene | |
| CN103922900A (en) | Method for removing sulfide in methyl tertiary butyl ether through double-solvent extractive distillation | |
| CN110845734B (en) | System and method for hydrolyzing organochlorosilane and refining hydrochloric acid | |
| CN216192101U (en) | Alkylation reaction system capable of achieving rapid start-up and shutdown | |
| CN110028374A (en) | A kind of aviation fuel high-octane isooctane and preparation method thereof | |
| CN113831936A (en) | Alkylation reaction system capable of achieving rapid start-up and shutdown | |
| CN207944042U (en) | A kind of process system preparing propionic ester | |
| CN108587684A (en) | A kind of joint aromatics production line CONTINUOUS REFORMER unit | |
| CN106854126B (en) | A kind of process units that isooctane is prepared with iso-butane, butene alkylation | |
| CN209338419U (en) | A kind of cyclohexene production energy-saving system | |
| JP4654584B2 (en) | Handling of (meth) acrylic ester-containing liquid | |
| CN216536970U (en) | Deisobutanizer energy-saving separation system | |
| CN110156555B (en) | Fuel oil recovery process | |
| CN212610438U (en) | Tar distillation heat transfer device | |
| CN114105754A (en) | Organic sodium salt treatment process and device in toluene oxidation process | |
| CN206940777U (en) | A kind of production equipment of ton polyphenylene oxide | |
| CN108893136B (en) | Treatment method of dirty oil generated by delayed coking heavy steam blowing | |
| CN205933757U (en) | Retrieve process systems of HCl and petrol mediation component on lenient side in hydro carbons gas | |
| CN101260036A (en) | Modified technique for refined unit in acrylic acid production device | |
| CN102311770B (en) | Reduced-pressure flash tank and reduced-pressure distillation method | |
| CN105861027B (en) | A kind of system that HCl and gasoline blend component are reclaimed from process gas | |
| CN217989308U (en) | Safety interlock system for vinylene carbonate production system | |
| CN217092104U (en) | System for accelerating initiation speed of oxidation reactor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20240325 Address after: No. 88, Dongfang Avenue, Zhapu Town, Jiaxing City, Zhejiang Province, 314201 Patentee after: ZHEJIANG MEIFU PETROLEUM CHEMICAL CO.,LTD. Country or region after: China Address before: 314000 floor 2, building 3, No. 988, Yashan West Road, gangang District, Jiaxing City, Zhejiang Province Patentee before: Zhejiang maidui Technology Co.,Ltd. Country or region before: China |