CN205528618U - Hydrogenation device - Google Patents
Hydrogenation device Download PDFInfo
- Publication number
- CN205528618U CN205528618U CN201620284349.7U CN201620284349U CN205528618U CN 205528618 U CN205528618 U CN 205528618U CN 201620284349 U CN201620284349 U CN 201620284349U CN 205528618 U CN205528618 U CN 205528618U
- Authority
- CN
- China
- Prior art keywords
- heat exchanger
- low
- heat
- air cooler
- temperature receiver
- 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 - Fee Related
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model discloses a hydrogenation device, include the first heat exchanger, second heat exchanger, third heat exchanger and the air cooler that communicate each other through the pipeline, being connected with crude oil in the third heat exchanger cold source import and advancing the pipe, be connected with the fourth heat exchanger between export of third heat exchanger heat source and the air cooler, the formation oil in the hydrogenation ware can heat for recycle hydrogen and new hydrogen at remaining heat after a plurality of heat exchanger heat transfer through the fourth heat exchanger, like this can be with the gas quantity that reduces muddy hydrogen oil heating furnace, can reduce the load of air cooler again to realize the heat resources among the make full use of reaction sequence, reach the resources conservation.
Description
Technical field
This utility model relates to a kind of hydrogenation plant.
Background technology
Diesel hydrotreating unit technological principle is to heat up subsequently into hydrogenation reactor after raw oil mixes with new hydrogen, sulfur nitrogen oxygen etc. contained in removing diesel oil, thus improve diesel quality, reacted generation oil is cooled, the liquid phase diesel oil carrying device that high-low pressure obtains after separating, the vapor phase hydrogen obtained recycles through the compressor compression new hydrogen of mix supplement, the process of the cooling that heats up is needed during whole, cool down as reacted generation oil is directly entered air cooler after heat exchanger heat exchange, heat consumption is there is during cooling, but isolated hydrogen mix with crude oil before only 65 DEG C, remain a need for heating, there is the phenomenon of the wasting of resources in hydrogenation plant the most of the prior art.
Utility model content
The technical problems to be solved in the utility model is for drawbacks described above, it is provided that a kind of hydrogenation plant, this hydrogenation plant can make full use of the heat resources in course of reaction.
nullIn order to solve above-mentioned technical problem，This utility model includes the First Heat Exchanger being interconnected by pipeline、Second heat exchanger、3rd heat exchanger and air cooler，Connect in described 3rd heat exchanger low-temperature receiver import and have crude oil inlet pipe，It is structurally characterized in that: connecting between described 3rd heat exchanger thermal source outlet and air cooler has the 4th heat exchanger，Connected by mixing tube between described First Heat Exchanger low-temperature receiver import and the outlet of the 3rd heat exchanger low-temperature receiver，The upper connection of described First Heat Exchanger low-temperature receiver outlet has mixed hydrogen oil heating furnace，Connect on described mixed hydrogen oil heating furnace and have hydrogenation reactor，Described hydrogenation reactor successively with First Heat Exchanger、Second heat exchanger、3rd heat exchanger、4th heat exchanger connects with air cooler，It is communicated with high-pressure separator on described air cooler，It is communicated with compressor on described high-pressure separator，Connected by connecting tube between the low-temperature receiver import of described compressor and the 4th heat exchanger，Described 4th heat exchanger low-temperature receiver outlet has recycle hydrogen return pipe with being connected between mixing tube，Connect in described connecting tube and have new hydrogen inlet pipe.
Connect on described high-pressure separator and have low pressure separator, described low pressure separator and the connection of the second heat exchanger.
Advantageous effect after employing such scheme is: the generation oil in hydrogenation reactor can be heated to recycle hydrogen and new hydrogen by the 4th heat exchanger at remaining heat after multiple heat exchanger heat exchange, the most i.e. can reduce the gas consumption of mixed hydrogen oil heating furnace, the load of air cooler can be reduced again, thus realize making full use of the heat resources in course of reaction, reach resources conservation.
Accompanying drawing explanation
Below in conjunction with the accompanying drawings detailed description of the invention of the present utility model is described in further detail:
Fig. 1 is structural representation of the present utility model.
Detailed description of the invention
As it is shown in figure 1, this hydrogenation plant includes First Heat Exchanger the 1, second heat exchanger the 2, the 3rd heat exchanger 3 and the air cooler 8 being interconnected by pipeline, the low-temperature receiver import of the 3rd heat exchanger 3 connects and has crude oil inlet pipe 18.Connect between 3rd heat exchanger 3 thermal source outlet and air cooler 8 and have the 4th heat exchanger 9.Connected by mixing tube 4 between First Heat Exchanger 1 low-temperature receiver import and the outlet of the 3rd heat exchanger 3 low-temperature receiver.The upper connection of First Heat Exchanger 1 low-temperature receiver outlet has mixed hydrogen oil heating furnace 6, connect on mixed hydrogen oil heating furnace 6 and have hydrogenation reactor 7, hydrogenation reactor 7 connects with First Heat Exchanger the 1, second heat exchanger the 2, the 3rd heat exchanger the 3, the 4th heat exchanger 9 and air cooler 8 successively, high-pressure separator 10 it is communicated with on air cooler 8, compressor 11 it is communicated with on high-pressure separator 10, connected by connecting tube 19 between compressor 11 and the low-temperature receiver import of the 4th heat exchanger 9,4th heat exchanger 9 low-temperature receiver outlet has recycle hydrogen return pipe 12 with being connected between mixing tube 4, and connecting tube 19 connects new hydrogen inlet pipe 5.Connect on high-pressure separator 10 and have low pressure separator 16, low pressure separator 16 and the low-temperature receiver inlet communication of the second heat exchanger 2.
nullWork process of the present utility model: raw oil enters crude oil inlet pipe 18，And heated by low-temperature receiver import entrance the 3rd heat exchanger 3，Raw oil after heating enters in mixing tube 4，New hydrogen enters connecting tube 19 by new hydrogen inlet pipe 5，Then by after the 4th heat exchanger 9 heat exchange also in mixing tube 4，New hydrogen and raw oil are mixed to get mixed hydrogen oil in mixing tube 4，Mixed hydrogen oil enters First Heat Exchanger 1 and carries out secondary heat exchange，Heat subsequently into mixed hydrogen oil heating furnace 6，Mixed hydrogen oil after heating enters hydrogenation reactor 7，In removing diesel oil, institute's Trialkylamine Type etc. are rear produces generation oil，Generate oil and pass sequentially through First Heat Exchanger 1、Second heat exchanger 2、3rd heat exchanger 3 and the 4th heat exchanger 9 heat exchange，Gradually reduce the temperature generating oil，Cool down subsequently into air cooler 8，Generation oil after cooling enters high-pressure separator 10 and separates，The recycle hydrogen of isolated enters compressor 11 and is compressed，Recycle hydrogen after compression enters connecting tube 19 and mixes with new hydrogen，After new hydrogen and recycle hydrogen mixing, common the 4th heat exchanger 9 that enters heats，Then mix in mixing tube 4 with raw oil，Recycle hydrogen and new hydrogen mixing circulation thus can be made to utilize.The hydraulic oil that high-pressure separator 10 obtains after separating enters in low pressure separator 16 and carries out low pressure separation and obtain low point of oil, and low point of oil enters the second heat exchanger 2 by low-temperature receiver import and carries out heat exchange, and low point of oil after heating enters stripper.In this utility model, the oil of the generation in hydrogenation reactor 7 can be used for heating to recycle hydrogen and new hydrogen by the 4th heat exchanger 9 at remaining heat after multiple heat exchanger heat exchange, the most i.e. can reduce the gas consumption of mixed hydrogen oil heating furnace 6, the load of air cooler 8 can be reduced again, thus realize making full use of the heat resources in course of reaction.
This utility model is not limited to above-mentioned detailed description of the invention, those skilled in the art, on the premise of without departing from spirit and scope of the present utility model, can do some changes and modification.Protection domain of the present utility model should be as the criterion with claim of the present utility model.
Claims (2)
- null1. a hydrogenation plant，Including the First Heat Exchanger (1) being interconnected by pipeline、Second heat exchanger (2)、3rd heat exchanger (3) and air cooler (8)，Connect in described 3rd heat exchanger (3) low-temperature receiver import and have crude oil inlet pipe (18)，It is characterized in that: connecting between described 3rd heat exchanger (3) thermal source outlet and air cooler (8) has the 4th heat exchanger (9)，Connected by mixing tube (4) between described First Heat Exchanger (1) low-temperature receiver import and the outlet of the 3rd heat exchanger (3) low-temperature receiver，The upper connection of described First Heat Exchanger (1) low-temperature receiver outlet has mixed hydrogen oil heating furnace (6)，The upper connection of described mixed hydrogen oil heating furnace (6) has hydrogenation reactor (7)，Described hydrogenation reactor (7) successively with First Heat Exchanger (1)、Second heat exchanger (2)、3rd heat exchanger (3)、4th heat exchanger (9) connects with air cooler (8)，High-pressure separator (10) it is communicated with on described air cooler (8)，Compressor (11) it is communicated with on described high-pressure separator (10)，Connected by connecting tube (19) between described compressor (11) and the low-temperature receiver import of the 4th heat exchanger (9)，Described 4th heat exchanger (9) low-temperature receiver outlet has recycle hydrogen return pipe (12) with being connected between mixing tube (4)，The upper connection of described connecting tube (19) has new hydrogen inlet pipe (5).
- Hydrogenation plant the most according to claim 1, is characterized in that: the upper connection of described high-pressure separator (10) has low pressure separator (16), described low pressure separator (16) to connect with the second heat exchanger (2).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620284349.7U CN205528618U (en) | 2016-04-08 | 2016-04-08 | Hydrogenation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620284349.7U CN205528618U (en) | 2016-04-08 | 2016-04-08 | Hydrogenation device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205528618U true CN205528618U (en) | 2016-08-31 |
Family
ID=57140994
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201620284349.7U Expired - Fee Related CN205528618U (en) | 2016-04-08 | 2016-04-08 | Hydrogenation device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205528618U (en) |
-
2016
- 2016-04-08 CN CN201620284349.7U patent/CN205528618U/en not_active Expired - Fee Related
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106118705A (en) | A kind of continuous reaction system and method for microalgae hydrothermal liquefaction preparing bio-oil | |
| CN103896280B (en) | A kind of operation method of polysilicon cold hydrogenation | |
| CN106635706B (en) | Differential pressure distillation energy-saving production device and method for white spirit with double distillation retorts | |
| CN106595128A (en) | Heat pump type crude oil dehydration and heating system and method | |
| CN113063310A (en) | Hydrogenation heat exchange system and heat exchange process adopting multi-strand wound tube type heat exchanger | |
| CN113091498A (en) | Hydrogenation heat exchange system and heat exchange process adopting multi-strand wound tube type heat exchanger | |
| CN101445747A (en) | Hydrofining process integration method | |
| CN105586212B (en) | The integration of equipments and method of rice wine semi-solid ferment | |
| CN104593057B (en) | A kind of delayed coking unit of low energy consumption | |
| CN205528618U (en) | Hydrogenation device | |
| CN102583461A (en) | Device and method for preheating by utilizing steam condensate water for aluminum oxide high-pressure digestion process | |
| CN102167327A (en) | Reaction system for producing polycrystalline silicon by using multiple polycrystalline silicon reduction furnaces and operating method of reaction system | |
| CN218665919U (en) | Device for continuous acid-free refining of olefin-containing oil | |
| CN215893283U (en) | Reduction tail gas waste heat recovery system | |
| CN103013817A (en) | Liquefaction equipment and liquefaction process for producing alcohol by using starchiness as raw material | |
| CN202876402U (en) | Device for recovering methylsiloxane high cyclic body | |
| CN102923731B (en) | Utilizing device and method for cold energy in high-purity ammonia preparation process | |
| CN214892793U (en) | Hydrogenation heat exchange system adopting multi-strand winding tube type heat exchanger | |
| CN214892794U (en) | Hydrogenation heat exchange system adopting multi-strand winding tube type heat exchanger | |
| CN202730036U (en) | Heat recovery system | |
| CN215288655U (en) | Diesel oil upgrading device feeding hydrogen preheating energy recovery system | |
| CN210855900U (en) | Equipment for producing polyol by utilizing steelmaking blast furnace gas | |
| CN104046714B (en) | A kind of reduction reaction shaft furnace waste heat recovery cyclic utilization system | |
| CN203065153U (en) | Hydrogen recovery device for hydrogen-containing mixed tail gas | |
| CN205710633U (en) | A kind of synthesis gas methanation multi-joint-production apparatus |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20160831 Termination date: 20170408 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |