CN106854474A - A kind of new coal tar hydrogenating cracker and preparation method thereof - Google Patents
A kind of new coal tar hydrogenating cracker and preparation method thereof Download PDFInfo
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- CN106854474A CN106854474A CN201611255584.2A CN201611255584A CN106854474A CN 106854474 A CN106854474 A CN 106854474A CN 201611255584 A CN201611255584 A CN 201611255584A CN 106854474 A CN106854474 A CN 106854474A
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- tank
- high score
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- low point
- pipe
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/12—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides a kind of new coal tar hydrogenating cracker and preparation method thereof.Its technical scheme is：It is main by make-up hydrogen compressor (1),Heating furnace (2),Protection reactor (3),Preatreating reactors (4),First hot high score tank (5),First hot low point of tank (6),Debutanizing tower (7),Water main (8),Air cooling gas tank (9),First cold high score tank (10),First cold low point of tank (11),Finishing reactor (12),Cracker (13),Second hot high score tank (14),Second hot low point of tank (15),Air cooler (16),Circulating hydrogen compressor (17),Second cold high score tank (18),Circulating hydrogen compressor entrance point flow container (19),Second cold low point of tank (20),Fractionating column (21),Tower top tracheae (22),Light naphthar pipe (23),Heavy naphtha pipe (24),Kerosene pipe (25) and diesel oil pipe (26) are constituted；Beneficial effect of the present invention：Practicality reasonable in design, denitrification effect is good, low energy consumption, and production efficiency and economic benefit is greatly improved.
Description
First, technical field
The present invention relates to technical field of coal tar, especially a kind of new coal tar hydrogenating cracker and its preparation side
Method.
2nd, background technology
Because coal tar nitrogen content, tenor are high, hydrogen content is low, and hydrodenitrogeneration difficulty is big, and reaches target product
Hydrogen consumption is high needed for product, and exothermic heat of reaction is big, and traditional hydrocracking unit can not meet requirement.The present invention is using two-part complete alternation
Hydrocracking technology, processes inferior raw material.
3rd, the content of the invention
It is an object of the invention to provide a kind of new coal tar hydrogenating cracker and preparation method thereof.Its technical scheme
For：Make-up hydrogen compressor connects circulating hydrogen compressor by pipeline, and heating furnace connects protection reactor, protects reactor by pipeline
Bottom pipe connects preatreating reactors, and preatreating reactors bottom pipe connects the first hot high score tank, and Road pipeline connects respectively
Connect circulating hydrogen compressor, circulating hydrogen compressor connection circulating hydrogen compressor entrance point flow container, the first hot heat of high score tank connection first
Low point of tank, the first low point of heat pot bottom pipeline connection debutanizing tower, top duct connects air cooling gas tank, middle part pipeline through water main
The pipeline between the first cold high score tank and the first cold low point of tank is connected, air cooling gas tank middle part pipeline connects the first cold high score tank, the
One cold high score tank middle part pipeline connection first divides tank, top duct to connect the second cold high score tank, the first cold low point of tank middle part coldly
The hot low point of pipeline between tank and debutanizing tower of pipeline connection first, debutanizing tower middle part pipeline returns to heating furnace all the way, another
Road connects the pipeline between finishing reactor and fractionating column, finishing reactor bottom pipe connection cracker, cracking reaction
Device bottom pipe connects the second hot high score tank, and the pipeline between heating furnace and circulating hydrogen compressor connects the second hot high score tank respectively
Top duct and middle part pipeline, second the second hot low point of tank of hot high score pot bottom pipeline connection, top duct connection air cooler,
Air cooler connects the second cold high score tank, and the second cold high score tank middle part pipeline connects the second cold low point of tank, and top duct is connected all the way
Circulating hydrogen compressor entrance point flow container, another road connects the first cold high score tank, and the second cold low point of tank middle part pipeline connects fractionating column,
Fractionation column base pipeline is provided with tail oil delivery pipe, and top duct is provided with tower top tracheae, middle part pipeline be sequentially provided with light naphthar pipe,
Heavy naphtha pipe, kerosene pipe and diesel oil pipe, kerosene pipe and diesel oil pipe connect the pipe between finishing reactor and fractionating column respectively
Road.
Its preparation method comprises the following steps：(1), weighted BMO spaces：Feedstock oil and recycle oil mixing 110t/h, enter
Pretreated feedstock surge tank, is pressurizeed by pretreated feedstock pump, is mixed with mixed hydrogen, and exchanging heat, then enter heating furnace is heated to 350 DEG C, so
The protection reactor and preatreating reactors into series connection react afterwards, 390 DEG C of reactor outlet temperature；Reaction effluent is passed through
Entering the hot high score of pretreatment after cooling carries out three phase separation, and system pressure is 17.8MPa, and gas phase enters the cold high score of pretreatment, oil
Mutually enter low point of pretreatment heat, oil phase of the gas phase with cold high score after air cooling mixes, further separated into pre-processing cold low point,
Cold low point of oil enters fractionating section, and fractionation pressure is 0.2MPa；(2), hydrocracking reaction：The oil of fractionating section is pre-processed, is entered
Enter Hydrocracking Raw Oil surge tank, after being pressurizeed by pump, mix with mixed hydrogen, adding for series connection is entered after 360 DEG C through exchanging heat, being heated to
Hydrogen finishing reactor and hydrocracking reactor, 380 DEG C of outlet temperature；Carried out into heat of cracking high score after reaction effluent cooling
Three phase separation, after gas phase cooling, into the cold high score of cracking, the gas phase of cold high score is delivered to and follows hydrogen desulphurization system；Oil phase enters cracking
Low point of heat, after low point of gas phase cooling of heat, the oil phase with cold high score mixes, and into cracking, cold low point further separates, cold low point of gas
Sending out battery limit (BL) carries out Recovery Purifying, and cold low point of oil is then through sending into main stripper fractionating section, fractionation pressure 1.2MPa.
Inferior feedstock oil is processed using two-part Extinction Hydrocracking technology, if pretreatment unit and hydrocracking reaction
Unit, there is independent piece-rate system respectively, shares make-up hydrogen compressor and circulating hydrogen compressor.
Beneficial effect of the present invention：Practicality reasonable in design, inferior raw material is processed using two-part Extinction Hydrocracking technology
Oil, if pretreatment unit and hydrocracking reaction unit, there is independent piece-rate system respectively, shares make-up hydrogen compressor and recycle hydrogen
Compressor, denitrification effect of the present invention is good, low energy consumption, and production efficiency and economic benefit is greatly improved.
4th, illustrate
Fig. 1 is structural representation of the invention.
5th, specific embodiment
As shown in figure 1, a kind of new coal tar hydrogenating cracker and preparation method thereof, its mainly by make-up hydrogen compressor 1,
Heating furnace 2, protection reactor 3, preatreating reactors 4, first the 5, first hot low point of tank 6, debutanizing tower 7, main water of hot high score tank
Pipe 8, air cooling gas tank 9, first the 10, first cold low point of tank 11 of cold high score tank, finishing reactor 12, the heat of cracker 13, second
High score tank 14, second hot low point of tank 15, air cooler 16, circulating hydrogen compressor 17, the second cold high score tank 18, circulating hydrogen compressor enter
Mouth point cold low point of tank 20 of flow container 19, second, fractionating column 21, tower top tracheae 22, light naphthar pipe 23, heavy naphtha pipe 24, kerosene
Pipe 25 and diesel oil pipe 26 are constituted；Make-up hydrogen compressor 1 connects circulating hydrogen compressor 17 by pipeline, and heating furnace 2 is connected by pipeline
Protection reactor 3, protection reactor 3 bottom pipe connection preatreating reactors 4, the bottom pipe of preatreating reactors 4 connection the
One hot high score tank 5, Road pipeline connects circulating hydrogen compressor 17, the connection circulating hydrogen compressor entrance of circulating hydrogen compressor 17 respectively
Flow container 19, the first first hot low point of tank 6 of the hot connection of high score tank 5, the first low point of the heat bottom pipe of tank 6 connection debutanizing tower 7 is divided to push up
Through the connection air cooling of water main 8 gas tank 9, middle part pipeline is connected between the cold low point of tank 11 of the first cold high score tank 10 and first portion's pipeline
Pipeline, the middle part pipeline of air cooling gas tank 9 connects the first cold high score tank 10, and the middle part pipeline of the first cold high score tank 10 connects first and divides coldly
Tank 11, top duct connects the second cold high score tank 18, middle part the first hot low point of tank 6 of pipeline connection of the first cold low point of tank 11 and de- fourth
Pipeline between alkane tower 7, the middle part pipeline of debutanizing tower 7 returns to heating furnace 2, another road connection finishing reactor 12 and fractionation all the way
Pipeline between tower 21, the bottom pipe of finishing reactor 12 connection cracker 13, the connection of the bottom pipe of cracker 13
Second hot high score tank 14, the pipeline between heating furnace 2 and circulating hydrogen compressor 17 connects the top of the second hot high score tank 14 respectively
Pipeline and middle part pipeline, second the second hot low point of tank 15 of the hot bottom pipe of high score tank 14 connection, top duct connection air cooler 16,
Air cooler 16 connects the second cold high score tank 18, and the middle part pipeline of the second cold high score tank 18 connects the second cold low point of tank 20, top duct
Connection circulating hydrogen compressor entrance divides flow container 19 all the way, and another road connects the first cold high score tank 10, the middle part of the second cold low point of tank 20
Pipeline connects fractionating column 21, and the bottom pipe of fractionating column 21 is provided with tail oil delivery pipe 27, and top duct is provided with tower top tracheae 22, middle part
Pipeline is sequentially provided with light naphthar pipe 23, heavy naphtha pipe 24, kerosene pipe 25 and diesel oil pipe 26, kerosene pipe 25 and diesel oil pipe 26
The pipeline between finishing reactor 12 and fractionating column 21 is connected respectively.
Specific embodiment 1：
Weighted BMO spaces unit sets protection reactor and a hydrotreating reactor, independent piece-rate system and
Debutanizing tower, debutanizing tower base oil part loops back weighted BMO spaces unit raw material surge tank, partly delivers to Hydrocracking unit
Feed surge tank；Hydrocracking unit sets refined and two reactors of cracking, after the oily separated, fractionation of cracking reaction generation,
Naphtha, kerosene and diesel oil go out device as product, and tail oil and part coal diesel cycle return Hydrocracking unit feed surge tank,
Weighted BMO spaces and Hydrocracking unit share make-up hydrogen compressor and circulating hydrogen compressor.
(1), weighted BMO spaces：Feedstock oil and recycle oil mixing 110t/h, into pretreated feedstock surge tank, by advance
Reason raw material pump pressurization, mix with mixed hydrogen, and exchanging heat, then enter heating furnace is heated to 350 DEG C, subsequently into series connection protection reactor with
Preatreating reactors reacts, 390 DEG C of reactor outlet temperature；Reaction effluent enters into the hot high score of pretreatment after cooling
Row three phase separation, system pressure is 17.8MPa, and gas phase enters the cold high score of pretreatment, and oil phase enters low point of pretreatment heat, gas phase warp
Oil phase after air cooling with cold high score mixes, and is further separated into pre-processing cold low point, and cold low point of oil enters fractionating section, is fractionated
Pressure is 0.2MPa；(2), hydrocracking reaction：The oil of fractionating section is pre-processed, into Hydrocracking Raw Oil surge tank, by
After pump pressurization, mix with mixed hydrogen, through exchanging heat, being heated to enter the hydrofining reactor of series connection after 360 DEG C and be hydrocracked anti-
Answer device, 380 DEG C of outlet temperature；Three phase separation is carried out into heat of cracking high score after reaction effluent cooling, after gas phase cooling, is entered
The cold high score of cracking, the gas phase of cold high score is delivered to and follows hydrogen desulphurization system；Oil phase enters low point of the heat of cracking, after low point of gas phase cooling of heat,
Oil phase with cold high score mixes, and into cracking, cold low point further separates, and cold low point of pneumatic transmission goes out battery limit (BL) carries out Recovery Purifying, cold low
Divide oil then through sending into main stripper fractionating section, fractionation pressure 1.2MPa.
Inferior feedstock oil is processed using two-part Extinction Hydrocracking technology, if pretreatment unit and hydrocracking reaction
Unit, there is independent piece-rate system respectively, shares make-up hydrogen compressor and circulating hydrogen compressor.
Claims (3)
1. a kind of new coal tar hydrogenating cracker and preparation method thereof, it is characterised in that：Make-up hydrogen compressor (1) is by pipeline
Connection circulating hydrogen compressor (17), heating furnace (2) connects protection reactor (3) by pipeline, protects reactor (3) bottom pipe
Connection preatreating reactors (4), preatreating reactors (4) bottom pipe connects the first hot high score tank (5), and Road pipeline connects respectively
Connect circulating hydrogen compressor (17), circulating hydrogen compressor (17) connection circulating hydrogen compressor entrance point flow container (19), the first hot high score
The hot low point of tank (6) of tank (5) connection first, first low point of tank (6) bottom pipe of heat connects debutanizing tower (7), and top duct is through master
Water pipe (8) connects air cooling gas tank (9), and middle part pipeline connects the pipe between the first cold high score tank (10) and the first cold low point of tank (11)
Road, air cooling gas tank (9) middle part pipeline connects the first cold high score tank (10), and the first cold high score tank (10) middle part pipeline connection first is cold
Ground point tank (11), top duct connects the second cold high score tank (18), and first cold low point of tank (11) middle part pipeline the first heat of connection is low
The pipeline divided between tank (6) and debutanizing tower (7), debutanizing tower (7) middle part pipeline returns to heating furnace (2) all the way, and another road connects
Connect the pipeline between finishing reactor (12) and fractionating column (21), finishing reactor (12) bottom pipe connection cracker
(13), cracker (13) bottom pipe connects the second hot high score tank (14), heating furnace (2) and circulating hydrogen compressor (17) it
Between pipeline connect the top duct and middle part pipeline of the second hot high score tank (14), the second hot high score tank (14) bottom pipe respectively
The hot low point of tank (15) of connection second, top duct connects air cooler (16), and air cooler (16) connects the second cold high score tank (18), the
Two cold high score tank (18) middle part pipelines connect the second cold low point of tank (20), and top duct connects circulating hydrogen compressor entrance point all the way
Flow container (19), another road connects the first cold high score tank (10), and the second cold low point of tank (20) middle part pipeline connects fractionating column (21), point
Evaporate tower (21) bottom pipe and be provided with tail oil delivery pipe (27), top duct is provided with tower top tracheae (22), and middle part pipeline is sequentially provided with
Light naphthar pipe (23), heavy naphtha pipe (24), kerosene pipe (25) and diesel oil pipe (26), kerosene pipe (25) and diesel oil pipe (26)
The pipeline between finishing reactor (12) and fractionating column (21) is connected respectively.
2. a kind of new coal tar hydrogenating cracker and preparation method thereof according to claim 1, it is characterised in that：Its system
Preparation Method comprises the following steps：(1), weighted BMO spaces：Feedstock oil and recycle oil mixing 110t/h are slow into pretreated feedstock
Tank is rushed, is pressurizeed by pretreated feedstock pump, mixed with mixed hydrogen, exchanging heat, then enter heating furnace is heated to 350 DEG C, subsequently into series connection
Protection reactor and preatreating reactors react, 390 DEG C of reactor outlet temperature；Reaction effluent enters pre- after cooling
Processing hot high score carries out three phase separation, and system pressure is 17.8MPa, and gas phase enters the cold high score of pretreatment, and oil phase enters pretreatment
Low point of heat, oil phase of the gas phase with cold high score after air cooling mixes, and is further separated into pre-processing cold low point, and cold low point of oil enters
Fractionating section, fractionation pressure is 0.2MPa；(2), hydrocracking reaction：The oil of fractionating section is pre-processed, into being hydrocracked original
The oily surge tank of material, after being pressurizeed by pump, mixes with mixed hydrogen, and the hydrofining reactor connected is entered after 360 DEG C through exchanging heat, being heated to
And hydrocracking reactor, 380 DEG C of outlet temperature；After reaction effluent cooling three phase separation, gas are carried out into heat of cracking high score
After mutually cooling down, into the cold high score of cracking, the gas phase of cold high score is delivered to and follows hydrogen desulphurization system；Oil phase enters low point of the heat of cracking, and heat is low
After dividing gas phase cooling, the oil phase with cold high score mixes, and into cracking, cold low point is further separated, and cold low point of pneumatic transmission goes out battery limit (BL) to be carried out
Recovery Purifying, cold low point of oil is then through sending into main stripper fractionating section, fractionation pressure 1.2MPa.
3. a kind of new coal tar hydrogenating cracker according to claim 1 or claim 2 and preparation method thereof, it is characterised in that：
Inferior feedstock oil is processed using two-part Extinction Hydrocracking technology, if pretreatment unit and hydrocracking reaction unit, point
There is not independent piece-rate system, share make-up hydrogen compressor and circulating hydrogen compressor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611255584.2A CN106854474A (en) | 2016-12-30 | 2016-12-30 | A kind of new coal tar hydrogenating cracker and preparation method thereof |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201611255584.2A CN106854474A (en) | 2016-12-30 | 2016-12-30 | A kind of new coal tar hydrogenating cracker and preparation method thereof |
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| CN106854474A true CN106854474A (en) | 2017-06-16 |
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| CN201611255584.2A Pending CN106854474A (en) | 2016-12-30 | 2016-12-30 | A kind of new coal tar hydrogenating cracker and preparation method thereof |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108998092A (en) * | 2018-09-12 | 2018-12-14 | 山东齐创石化工程有限公司 | The technique of hydrotreating heavy traffic paving asphalt distillate production lube base oil |
| CN110923008A (en) * | 2019-05-21 | 2020-03-27 | 何巨堂 | Poor-quality hydrocarbon hydrogenation method for circulating liquid hydrogenation without passing through at least part of protective agent bed layer |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108998092A (en) * | 2018-09-12 | 2018-12-14 | 山东齐创石化工程有限公司 | The technique of hydrotreating heavy traffic paving asphalt distillate production lube base oil |
| CN108998092B (en) * | 2018-09-12 | 2020-08-25 | 山东齐创石化工程有限公司 | Process for producing lubricating oil base oil by hydrotreating heavy-traffic asphalt distillate |
| CN110923008A (en) * | 2019-05-21 | 2020-03-27 | 何巨堂 | Poor-quality hydrocarbon hydrogenation method for circulating liquid hydrogenation without passing through at least part of protective agent bed layer |
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Application publication date: 20170616 |
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