CN203333598U - Processing device for modifying light hydrocarbons - Google Patents
Processing device for modifying light hydrocarbons Download PDFInfo
- Publication number
- CN203333598U CN203333598U CN2013203724006U CN201320372400U CN203333598U CN 203333598 U CN203333598 U CN 203333598U CN 2013203724006 U CN2013203724006 U CN 2013203724006U CN 201320372400 U CN201320372400 U CN 201320372400U CN 203333598 U CN203333598 U CN 203333598U
- Authority
- CN
- China
- Prior art keywords
- tower
- pipeline
- lighter hydrocarbons
- gas
- mixed
- 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.)
- Expired - Lifetime
Links
Images
Abstract
The utility model relates to a processing device for modifying light hydrocarbons. The processing device comprises two sets of reaction systems and a fractionation stabilization system; one set of the reaction systems comprises a reactor, as well as a light hydrocarbon naphtha feed pipeline, a mixed C4 feed pipeline and a reaction discharge pipeline which are respectively arranged on the reactor, wherein the other end of the light hydrocarbon naphtha feed pipeline is sequentially connected with a heating furnace and a light hydrocarbon naphtha raw material buffer tank, and the other end of the mixed C4 feed pipeline is connected with a mixed C4 raw material buffer tank; the fractionation stabilization system comprises a gas-liquid separation high-pressure separation tank, a fractionation tower and a stabilization tower, which are sequentially connected, wherein the tower bottom of the fractionation tower is connected with a diesel oil pipeline, the tower top of the fractionation tower is connected with the stabilization tower through a pipeline, the tower top of the stabilization tower is connected with a petroleum liquefied gas pipeline, and the tower bottom of the stabilization tower is connected with a stabilization gasoline pipeline. Compared with the prior art, the processing device disclosed by the utility model has the advantages that double-reactor operation and continuous production are realized, the capability of enabling the reactors to be burned and regenerated alternately is achieved, the long-term operation period of the device is ensured, the benefits of the device are increased and the like.
Description
Technical field
The utility model relates to lighter hydrocarbons and mixed c 4 manufacture field, specifically a kind of processing unit (plant) of lighter hydrocarbons upgrading in petrochemical industry.
Background technology
Mixed c 4 is important petrochemical complex resource, and it is the general name of alkane, monoolefine and diolefine.Refinery carbon four mainly is comprised of n-butene, iso-butylene, normal butane, Trimethylmethane and divinyl, and the component that has chemical utilization value most is mainly n-butene, iso-butylene and divinyl, is secondly normal butane.The chemical utilization of China's C-4-fraction is still in initial stage at present.The refinery casing head major part is directly advanced alkyl plant and is produced gasoline alkylate or polymer gasoline; Part is made lubricating oil additive for the production of polybutene and polyisobutene; Utilize in addition iso-butylene to produce methyl tertiary butyl ether; A small amount of iso-butylene is for the production of alkylphenol, and n-butene is for the production of sec-butyl alcohol etc." lighter hydrocarbons " are exactly a series of materials that carbon, two kinds of elements of hydrogen form with different ratio chemical combination, and wherein lighter part, just be called lighter hydrocarbons.The major ingredient of Sweet natural gas is C1, and containing a small amount of C2, the major ingredient of liquefied petroleum gas (LPG) (LPG) is C3, C4, and they are gaseous state at normal temperatures and pressures, just is the gaseous state lighter hydrocarbons.The hydrocarbon of C5, C6 is liquid at normal temperatures and pressures, and we just are its liquid light hydrocarbon.Density larger part again is exactly gasoline, kerosene and diesel oil.The raw material sources of lighter hydrocarbons are very extensive, be mainly derived from the byproduct of associated gas condensed liquid in the production processes such as oil field, gas field, Gas Purification Factory and refinery, solvent oil factory, petroleum chemical plant, ethylene plant, the sherwood oil that tops, light naphthar, the solvent oil factory produced as refinery produces, " oil at the bottom of tower " that the stable light hydrocarbon that oil (gas) field produces, Gas Purification Factory are produced etc.Oil refining enterprise lighter hydrocarbons and mixed c 4 complete processing do not have fixed form, and traditional method generally will carry out separating-purifying or isomerization is processed, and added value is low, can not accomplish the at utmost utilization of resource.
The utility model content
The purpose of this utility model is exactly the defect existed for prior art, and a kind of processing unit (plant) of lighter hydrocarbons upgrading is provided, and by lighter hydrocarbons petroleum naphtha and mixed c 4 deep processing, produces high value-added product.
The concrete technical scheme of the utility model is: comprise reactive system and fractionation stabilization system; Described reactive system comprise reactor with and on the lighter hydrocarbons naphtha feed pipeline, mixed c 4 feeding line and the reaction discharging pipeline that are respectively equipped with, the other end of described lighter hydrocarbons naphtha feed pipeline connects process furnace and lighter hydrocarbons feed naphtha surge tank successively, and the other end of described mixed c 4 feeding line connects mixed c 4 raw material surge tank; Described fractionation stabilization system comprises gas-liquid separation high score tank, separation column and the stabilizer tower connected successively, described reaction discharging pipeline connects Fractionator Bottom reboiler and gas-liquid separation high score tank successively, the top gas phase pipeline stable connection tower of gas-liquid separation high score tank, bottom liquid phases pipeline separation column, connect diesel oil pipe, tower top at the bottom of the tower of described separation column by pipeline stable connection tower, stable connection medium gasoline pipeline at the bottom of stabilizer tower tower top connection L. P. G gas pipeline, tower.
Such scheme also comprises:
Described reactive system is two covers arranged side by side, and two covering devices can move simultaneously.
Connection line between described lighter hydrocarbons feed naphtha surge tank and process furnace is provided with branch's connection resurgent gases facility is provided, and described Fractionator Bottom reboiler is provided with branch with the connection line of gas-liquid separation high score tank and is connected the resurgent gases recvery facility.Described Fractionator Bottom reboiler is arranged side by side two, with two cover reactive systems, is connected respectively.Control by valve, can realize a set of reaction process, the another set of resurgent gases flow process of carrying out of carrying out in two cover reactive systems.
The utlity model has the double-reactor operation can produce continuously, also can make reactor coke burning regeneration in turn, the long cycle of operation of assurance device, has improved the advantages such as device benefit.
The accompanying drawing explanation
Fig. 1 is the process schematic representation of a kind of embodiment of the utility model;
In figure: 1-lighter hydrocarbons feed naphtha surge tank, 2-mixed c 4 raw material surge tank, the 3-early gate, the 4-late gate, 5-resurgent gases valve A, 6-resurgent gases valve B, the 7-resurgent gases provides facility, the 8-early gate, the 9-late gate, 10-process furnace A, 11-process furnace B, the 12-reactor A, the 13-reactor B, 14-mixed c 4 valve, 15-mixed c 4 valve, 16-gas-liquid separation high score tank, the 17-separation column, the 18-diesel oil pipe, 19-Fractionator Bottom reboiler A, 20-Fractionator Bottom reboiler B, the 21-stabilizer tower, 22-L. P. G gas pipeline, 23-stable gasoline pipeline, the 24-valve, the 25-valve, the 26-valve, the 27-valve, 28-resurgent gases recvery facility.
Embodiment
Below in conjunction with accompanying drawing, the utility model is described further.
Referring to Fig. 1, a kind of processing unit (plant) of lighter hydrocarbons upgrading, comprise reactive system and a set of fractionation stabilization system that two covers are arranged side by side; Wherein a set of reactive system comprise reactor A 12 with and on the lighter hydrocarbons naphtha feed pipeline, mixed c 4 feeding line and the reaction discharging pipeline that are respectively equipped with, the other end of lighter hydrocarbons naphtha feed pipeline connects process furnace A10, late gate 4, early gate 3 and lighter hydrocarbons feed naphtha surge tank 1 successively, and the other end of mixed c 4 feeding line connects mixed c 4 14 and mixed c 4 raw material surge tank 2 successively; Another set of reactive system comprise reactor B 13 with and on the lighter hydrocarbons naphtha feed pipeline, mixed c 4 feeding line and the reaction discharging pipeline that are respectively equipped with, the other end of lighter hydrocarbons naphtha feed pipeline connects process furnace B11, late gate 9, early gate 8 and lighter hydrocarbons feed naphtha surge tank 1 successively, and the other end of mixed c 4 feeding line connects mixed c 4 15 and mixed c 4 raw material surge tank 2 successively; Be respectively equipped with take-off line on pipeline between late gate 4 and early gate 3, late gate 9 and early gate 8, be respectively equipped with valve resurgent gases valve 5 and resurgent gases valve 6 on take-off line, resurgent gases valve 5 provides facility 7 to be connected with resurgent gases valve 6 and after connecing by pipeline and resurgent gases.The fractionation stabilization system comprises gas-liquid separation high score tank 16, separation column 17 and the stabilizer tower 21 connected successively, reaction discharging pipeline on reactor A 12 connects Fractionator Bottom reboiler B20, valve 26 and gas-liquid separation high score tank 16 successively, and the reaction discharging pipeline on reactor B 13 connects Fractionator Bottom reboiler A19, valve 24 and gas-liquid separation high score tank 16 successively; The top gas phase pipeline stable connection tower 21 of gas-liquid separation high score tank 16, bottom liquid phases pipeline separation column 17, connect diesel oil pipe 18, tower top at the bottom of the tower of separation column 17 by pipeline stable connection tower 21, stable connection medium gasoline pipeline 23 at the bottom of stabilizer tower 21 tower tops connection L. P. G gas pipelines 22, tower; Fractionator Bottom reboiler A19, Fractionator Bottom reboiler B 20 are provided with branch with the connection line of gas-liquid separation high score tank 16 and are connected resurgent gases recvery facility 28, are respectively equipped with valve 25,27 on take-off line.
Said apparatus can adopt following two kinds of operating modes:
One: two cover reactive system of operating mode moves simultaneously.
The operation that simultaneously goes into operation of two cover reactor A 12, reactor B 13, under this operating mode, resurgent gases valve 5, resurgent gases valve 6, valve 25, valve 27 are all in closure state, and other valves are in opened condition.
Reaction feed is divided into two portions, lighter hydrocarbons petroleum naphtha part and mixed c 4 part.Each reactor feed has two portions.
Lighter hydrocarbons petroleum naphtha part is divided two-way from lighter hydrocarbons feed naphtha surge tank 1 out: a road is through early gate 3, late gate 4, enter reactor A 12 again after reaction heating furnace A10 heats up, reaction product enters gas-liquid separation high score tank 16 after Fractionator Bottom reboiler B20 heat exchange; Another road is through early gate 8, late gate 9, then enters reactor B 13 after reaction heating furnace B11 heats up, and reaction product enters gas-liquid separation high score tank 16 after Fractionator Bottom reboiler A19 heat exchange.
The mixed c 4 part is also divided two-way: a part enters mixed c 4 raw material surge tank 2 Hou， mono-tunnels by the external mixed c 4 component of device and enters reactor A 12 through mixed c 4 valve 14; Another road enters reactor B 13 through mixed c 4 valve 15,
Gas-liquid separation high score tank 16 carries out the liquid phase separation, and gas phase enters stabilizer tower 21 from top, and liquid phase enters separation column 17.At the bottom of the separation column tower, diesel oil flows out and collects by diesel oil pipe 18.Separation column tower oil end process and the thermal source of reaction product heat exchange as reboiler.Overhead product enters stabilizer tower 21.Stabilizer tower is also a kind of rectifying tower, and tower top goes out oil liquefied gas and enters the rear collection of L. P. G gas pipeline 22, goes out stable gasoline 23 at the bottom of tower and enters the rear collection of stable gasoline pipeline 23.
Operating mode two: wherein a set of reactive system operation.
Go into operation operation, reactor B 13 of the two cover reactor A 12 of take burnt state as example in regeneration, and under this operating mode, resurgent gases valve 5, early gate 8, mixed c 4 valve 15, valve 24 are all in closure state, and other valves are in opened condition.
Reaction feed is divided into two portions, lighter hydrocarbons petroleum naphtha part and mixed c 4 part.
Lighter hydrocarbons petroleum naphtha part from lighter hydrocarbons feed naphtha surge tank 1 out by early gate 3, late gate 4, after heating up, reaction heating furnace A10 enters reactor A 12 again, after entering mixed c 4 raw material surge tank 2 by the external mixed c 4 component of device, mix 14 through valve and enter reactor A 12; Reaction product enters gas-liquid separation high score tank 16 after Fractionator Bottom reboiler B20 heat exchange; Gas-liquid separation high score tank 16 carries out the liquid phase separation, and gas phase enters stabilizer tower 21 from top, and liquid phase enters separation column 17.At the bottom of the separation column tower, diesel oil flows out and collects by diesel oil pipe 18.Separation column tower oil end process and the thermal source of reaction product heat exchange as reboiler.Overhead product enters stabilizer tower 21.Stabilizer tower is also a kind of rectifying tower, and tower top goes out oil liquefied gas and enters the rear collection of L. P. G gas pipeline 22, goes out stable gasoline 23 at the bottom of tower and enters the rear collection of stable gasoline pipeline 23.
The resurgent gases flow process: resurgent gases provides facility 7 through resurgent gases valve 6, late gate 9 by resurgent gases, enter successively process furnace B 11, reactor B 13, in reactor, from the bed top, burn from top to bottom, burn rear high temperature cigarette through Fractionator Bottom reboiler A19, flow out to resurgent gases recvery facility 28 by valve 25, regeneration gas recycles, and is adjusted according to the reactor batch temperature changing conditions.
For those skilled in the art, under the prerequisite that does not break away from the utility model principle, likely to concrete size, or local structure make some improvements and modifications, and these improvements and modifications also should be considered as protection domain of the present utility model.
Claims (4)
1. the processing unit (plant) of a lighter hydrocarbons upgrading, is characterized in that: comprise reactive system and fractionation stabilization system; Described reactive system comprise reactor with and on the lighter hydrocarbons naphtha feed pipeline, mixed c 4 feeding line and the reaction discharging pipeline that are respectively equipped with, the other end of described lighter hydrocarbons naphtha feed pipeline connects process furnace and lighter hydrocarbons feed naphtha surge tank successively, and the other end of described mixed c 4 feeding line connects mixed c 4 raw material surge tank; Described fractionation stabilization system comprises gas-liquid separation high score tank, separation column and the stabilizer tower connected successively, described reaction discharging pipeline connects Fractionator Bottom reboiler and gas-liquid separation high score tank successively, the top gas phase pipeline stable connection tower of gas-liquid separation high score tank, bottom liquid phases pipeline separation column, connect diesel oil pipe, tower top at the bottom of the tower of described separation column by pipeline stable connection tower, stable connection medium gasoline pipeline at the bottom of stabilizer tower tower top connection L. P. G gas pipeline, tower.
2. the processing unit (plant) of lighter hydrocarbons upgrading according to claim 1, it is characterized in that: described reactive system is two covers arranged side by side.
3. the processing unit (plant) of lighter hydrocarbons upgrading according to claim 1 and 2, it is characterized in that: the connection line between described lighter hydrocarbons feed naphtha surge tank and process furnace is provided with branch's connection resurgent gases facility is provided, and described Fractionator Bottom reboiler is provided with branch with the connection line of gas-liquid separation high score tank and is connected the resurgent gases recvery facility.
4. the processing unit (plant) of lighter hydrocarbons upgrading according to claim 3, it is characterized in that: described Fractionator Bottom reboiler is arranged side by side two, with two cover reactive systems, is connected respectively.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013203724006U CN203333598U (en) | 2013-06-27 | 2013-06-27 | Processing device for modifying light hydrocarbons |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013203724006U CN203333598U (en) | 2013-06-27 | 2013-06-27 | Processing device for modifying light hydrocarbons |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203333598U true CN203333598U (en) | 2013-12-11 |
Family
ID=49702288
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2013203724006U Expired - Lifetime CN203333598U (en) | 2013-06-27 | 2013-06-27 | Processing device for modifying light hydrocarbons |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203333598U (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106520187A (en) * | 2015-09-14 | 2017-03-22 | 中国石油天然气股份有限公司 | Light gasoline hydrocarbon recombination etherification catalytic rectification process and device thereof |
| CN106770891A (en) * | 2016-12-30 | 2017-05-31 | 神华集团有限责任公司 | Catalyst test apparatus and evaluation method |
| WO2022157617A1 (en) * | 2021-01-25 | 2022-07-28 | Designer Fuels Llc | Systems and methods for separating hydrocarbons with substantially reduced emissions |
| US11697774B2 (en) | 2021-01-25 | 2023-07-11 | Designer Fuels Llc | Systems and methods for separating hydrocarbons with substantially reduced emissions |
-
2013
- 2013-06-27 CN CN2013203724006U patent/CN203333598U/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106520187A (en) * | 2015-09-14 | 2017-03-22 | 中国石油天然气股份有限公司 | Light gasoline hydrocarbon recombination etherification catalytic rectification process and device thereof |
| CN106520187B (en) * | 2015-09-14 | 2018-04-06 | 中国石油天然气股份有限公司 | A kind of light petrol hydrocarbon restructuring etherificate catalytic rectification process and its device |
| CN106770891A (en) * | 2016-12-30 | 2017-05-31 | 神华集团有限责任公司 | Catalyst test apparatus and evaluation method |
| WO2022157617A1 (en) * | 2021-01-25 | 2022-07-28 | Designer Fuels Llc | Systems and methods for separating hydrocarbons with substantially reduced emissions |
| US11697774B2 (en) | 2021-01-25 | 2023-07-11 | Designer Fuels Llc | Systems and methods for separating hydrocarbons with substantially reduced emissions |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP3341577B1 (en) | Recovery and re-use of waste energy in industrial facilities | |
| CN103305246B (en) | Pyrolytic poly-generation method of low-rank coal and system | |
| CN103880577B (en) | For the reaction product separation system of preparing propylene from methanol and methanol-to-olefins | |
| CN203333598U (en) | Processing device for modifying light hydrocarbons | |
| CN104194826B (en) | A kind of processing method reducing delayed coking reaction dry gas yied | |
| JP5301574B2 (en) | Method for refining FT synthetic oil and mixed crude oil | |
| CN105175205B (en) | A kind of bio-oil prepares the method that carboxylate methyl ester catalytic aromatization prepares aromatic hydrocarbons | |
| CN104098419A (en) | System and method for preparing low-carbon olefin through adopting coal, natural gas and methyl alcohol | |
| CN102512933A (en) | Method for treating and utilizing oxidation sweetening tail gas | |
| CN109554189B (en) | Method for preparing low-carbon olefin by cracking petroleum hydrocarbon under reduced pressure | |
| CN103864564B (en) | Technique for processing methanol-to-propylene by-products | |
| CN102876359B (en) | A kind of system and method processing condensate oil | |
| CN104098437A (en) | Method for co-production of methanol, liquefied natural gas and hydrogen by employing coke oven gas | |
| CN103450928B (en) | A kind of production method of aromatization modification gasoline | |
| CN208517350U (en) | A kind of hydrocarbon-rich gas reutilization system generated in coking plant | |
| CN203700287U (en) | Device for recycling and reusing waste gas produced during gasoline hydrogenation | |
| CN103289739A (en) | Method for modification by coupling hydrodesulfurization of FCC (Fluid Catalytic Cracking) gasoline and aromatization of liquefied petroleum gas | |
| CN105132063A (en) | Preparation process of liquefied petroleum gas | |
| CN203904277U (en) | Device for recovering gas at top of stabilization tower of gasoline hydrogenation device | |
| CN109022031A (en) | Reduce the delayed coking method and processing of heavy oil method of sewage discharge | |
| CN203904279U (en) | Recycling device for gasoline hydrogenation stripping gases and fractionating gases | |
| CN208218783U (en) | A kind of naphtha cut with auxiliary distillation column is into desulfurizer | |
| CN109554194B (en) | Cracking device for preparing low-carbon olefin by cracking petroleum hydrocarbon under reduced pressure | |
| CN201087183Y (en) | Technology device for comprehensive utilization of petrified waste | |
| CN203559019U (en) | C4 non-hydrogenation aromatization production device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20131211 |