CN106497601A - A kind of two sections of complete alternation method of hydrotreating - Google Patents
A kind of two sections of complete alternation method of hydrotreating Download PDFInfo
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- CN106497601A CN106497601A CN201510557589.XA CN201510557589A CN106497601A CN 106497601 A CN106497601 A CN 106497601A CN 201510557589 A CN201510557589 A CN 201510557589A CN 106497601 A CN106497601 A CN 106497601A
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Abstract
The invention discloses a kind of two sections of complete alternation method of hydrotreating, have the shortcomings that destruction to overcome existing hydrogenation plant high energy consumption, the flue gas of generation to environment.Its method is：Fresh feed enters one stage hydrofining reactor after exchanging heat and heat with one section of product and is reacted；A period of hydrocracking reactor is entered after one section of refined products and two-stage mixing charging heat exchange, one section of product of a period of hydrocracking reactor is mixed with second-stage reaction product again, and then sequentially entering reactive moieties piece-rate system and fractionating section piece-rate system after steam generator cooling carries out isolated hydrogenated products.
Description
Technical field
The invention belongs to field of hydrogenation, more particularly to a kind of to the low fraction hydro carbons of heavy distillat hydrocarbon cracking production cleaning
Two sections of complete alternation method of hydrotreating.
Background technology
With fast development and the rapid growth of oil product demand of petroleum industry, in the last few years, oil extraction urgency
Increase severely length, and the heaviness of oil and in poor quality degree are on the rise.Meanwhile, as countries in the world are anticipated to environmental protection
The enhancing of knowledge, environmental regulation are increasingly strict, and the prescription of oil product is improved constantly.And, with petrochemical industry
Industrial expansion, the demand of industrial chemicals also increasingly increase.Therefore, in order to depth is fully using petroleum resources,
In order to produce the energy of cleaning, hydrogenation plant is increasingly paid attention to by enterprise.
Hydrogenation plant is divided into hydrofinishing, hydro-upgrading and is hydrocracked, for reaching reaction condition, need to be compared with
High pressure and temperature, the features such as therefore all having high temperature, high pressure, face hydrogen.For meeting the anti-of hydrogenation plant
Condition and product separation requirement is answered, larger energy need to be typically expended, wherein fuel gas or fuel oil disappears
Consumption accounts for larger portion in plant energy consumption, and by taking hydrocracking unit as an example, fuel consumption accounts for device total energy consumption
More than 40%.And, substantial amounts of flue gas can be given off again while fuel is consumed, often contain COX、
NOX、SOXDeng harm is brought in the bad border for giving people to depend on for existence.And, with the fast development of oil Refining Technologies,
The oil refining apparatus scales such as hydrogenation tend to maximizing, and the harm of fuel fume emission is more serious.
Meanwhile, hydrogenation reaction is also exothermic reaction, is carrying out hydrodesulfurization, denitrogenation, alkene saturation and hydrogenation
When cracking etc. is reacted, substantial amounts of heat can be discharged.Therefore how to reduce fuel consumption using reaction heat more next
More become important research topic.
Currently, only hydrocracking unit adopts two-stage hydrogenation technique, two-stage reforming work general both at home and abroad
The first paragraph and second segment of skill be both needed to reaction feed heating furnace by material temperature rise to reaction temperature required, normally
Under operation operating mode, it is also desirable to which heat supply distinguished by two heating furnaces.Chinese patent CN1952068A (publication number) is disclosed
A kind of two-segment hydrocracking method, is mainly characterized by first paragraph unconverted oil as the second section feeding and hydrogen
Enter second segment hydrocracking reactor through oil heat exchange being generated with first paragraph after mixing, second segment is without the need for heating
Stove, investment reduction simultaneously reduce operational danger.Which is a kind of side for only arranging reaction feed heating furnace at a section
Method, the method arrange reaction feed heating furnace although cancelling in two-stage nitration, but normal operating operating mode, one section of reaction
Charging heating furnace needs for carrying out heat supply, and two-stage nitration is not provided with heating facility, however, at the initial stage of going into operation,
Reactive moieties heat up and are only capable of providing heat by heating furnace, are three reactors only using one section of charging heating furnace
Heat is provided and reaches the required condition of sulfuration, need the sufficiently long time meet, extend going into operation for device
Cycle.
Content of the invention
The purpose of the present invention is that the flue gas of generation has destruction etc. to lack to environment for existing hydrogenation plant high energy consumption
Point, and a kind of two sections of complete alternation method of hydrotreating are provided.Reaction heat is utilized using the inventive method maximizing,
Only in the stage use that goes into operation of reactionless heat, normal operating is disabled one-stage hydrogenation charging reacting furnace, treating capacity phase
Reacting furnace is fed to less secondary hydrogenation also only in the stage use that goes into operation of reactionless heat, and normal operating is disabled.
While the method can save a large amount of fuel consumptions, also reduce the environmental protection pressure of enterprise.
The present invention provides a kind of two sections of complete alternation method of hydrotreating, it is characterised in that comprise the steps：
1) fresh feed is mixed with one section after hydrogen mixes as one section of mixed feeding, through the Ith heat exchanger and one section
One section of reaction feed is entered after product heat exchange and heats stove heat, enter one stage hydrofining reactor afterwards
Reacted；
2) one section of refined products of one stage hydrofining reactor are exchanged heat with two-stage mixing charging through the IIth heat exchanger,
Entering a period of hydrocracking reactor afterwards carries out hydrocracking reaction；
3) one section of product of a period of hydrocracking reactor is produced with second-stage reaction after the heat exchange of the Ith heat exchanger
Thing mixes, and then enters reactive moieties piece-rate system after steam generator cooling；
4) the cold high score gas that reactive moieties piece-rate system is isolated is mixed with the external new hydrogen of device as recycle hydrogen
Close, be divided into two parts afterwards, a part is mixed with fresh feed as one section of mixing hydrogen, another part conduct
Two-stage mixing hydrogen；
5) reactive moieties piece-rate system is isolated low point of gas and sour water carrying device, low point for isolating
Oil enters fractionating section piece-rate system；
6) the detached dry gas of fractionating section piece-rate system and light fraction carrying device, the heavy constituent conduct that isolates
Recycle oil and step 4) two-stage mixing hydrogen mix and feed as two-stage mixing, two-stage mixing charging is successively through the
Enter second-stage reaction charging heating furnace to be heated after III heat exchanger and the heat exchange of the IIth heat exchanger, enter two afterwards
Section hydrocracking reactor is reacted；
7) the second-stage reaction product of secondary hydrogenation cracker is exchanged heat with two-stage mixing charging through the IIIth heat exchanger,
Fractionating section piece-rate system is mixed into afterwards with one section of product.
One section of reaction condition of the present invention is：One stage hydrofining reactor operating pressure is 4.5～21MPa,
A period of hydrocracking reactor operating pressure is 4.3～21MPa, and two reactor average reaction temperatures are
275 DEG C～520 DEG C, total liquid hourly space velocity (LHSV) is 0.1h-1～6.0h-1, one stage hydrofining reactor inlet hydrogen oil body
Product compares 50：1～4500：1.
Second-stage reaction condition of the present invention is：4.5～21MPa of operating pressure, average reaction temperature is
215 DEG C～520 DEG C, total liquid hourly space velocity (LHSV) is 0.5h-1～12h-1, hydrogen to oil volume ratio 50：1～4500：1.
Fresh feed of the present invention can be the hydro carbons such as distillate, heavy oil, coal liquifaction and biological liquefaction；
The present invention is this have the advantage that compared with prior art：Using two-stage hydrogenation flow process, two-stage reaction charging adds
Hot stove is the stove that goes into operation, and makes full use of reaction heat, reduces fuel consumption, decreases flue gas of heating furnace
Discharge, had both reduced normal operating cost, had also reduced pressure of the device to environmental protection.And, reactive moieties
Two stoves that go into operation are set, on-stream time can be greatlyd save.
With the drawings and specific embodiments, the present invention is described in further detail below, but is not intended to limit this
Bright scope.
Description of the drawings
Fig. 1 is a kind of quick-reading flow sheets schematic diagram of two sections of complete alternation method of hydrotreating of the present invention.
Shown in figure, reference is：
1- fresh feeds, the new hydrogen of 2-, mono- section of mixed feeding of 3-, mono- section of refined products of 4-, mono- section of 5-
Product, 6- recycle hydrogens, mono- section of mixing hydrogen of 7-, 8- two-stage mixing hydrogen, low point of oil of 9-, 10- are low
Point gas, 11- sour waters, 12- dry gas, 13- light fractions I, 14- light fractions II, 15- recycle oils,
16- two-stage mixings feed, 17-- second-stage reaction products, the Ith heat exchangers of 18-, the IIth heat exchangers of 19-,
20- steam generators, the IIIth heat exchangers of 21-, mono- section of reaction feed heating furnace of 22-, 23- second-stage reactions
Charging heating furnace, 24- one stage hydrofining reactors, 25- a period of hydrocracking reactors, 26- two-stage nitration
Hydrocracking reactor, 27- circulating hydrogen compressors, 28- reactive moieties piece-rate systems, 29- fractionating sections point
From system.
Specific embodiment
As shown in figure 1, a kind of two sections of complete alternation method of hydrotreating, it is characterised in that comprise the steps：
1) fresh feed 1 is mixed with one section after hydrogen 7 mixes as one section of mixed feeding 3, through the Ith heat exchanger
18 exchange heat with one section of product 5 after enter one section of reaction feed heating furnace 22 and heat, enter afterwards one section plus
Hydrogen finishing reactor 24 is reacted；
2) one section of refined products 4 of one stage hydrofining reactor 24 are through the IIth heat exchanger 19 and two-stage mixing
Charging 16 exchanges heat, and entering a period of hydrocracking reactor 25 afterwards carries out hydrocracking reaction；
3) with two after one section of product 5 of a period of hydrocracking reactor 25 exchanges heat through the Ith heat exchanger 18
Section product 17 mixes, and then enters reactive moieties piece-rate system 28 after the cooling of steam generator 20；
4) the cold high score gas that reactive moieties piece-rate system 28 is isolated as recycle hydrogen 6 through recycle compressor
After 27, the new hydrogen 2 external with device mixes, and is divided into two parts afterwards, and a part is used as one section of mixing hydrogen 7
Mix with fresh feed 1, another part is used as two-stage mixing hydrogen 8；
5) 11 carrying device of low point of gas 10 and sour water that reactive moieties piece-rate system 28 is isolated, separates
The low point of oil 9 for going out enters fractionating section piece-rate system 29；
6) fractionating section piece-rate system 29 is separated dry gas 12, light fraction I 13 and light fraction II 14
Carrying device, the heavy constituent that isolates is used as recycle oil 15 and step 4) two-stage mixing hydrogen 8 mix conduct
Two-stage mixing charging 16, two-stage mixing charging 16 are exchanged heat through the IIIth heat exchanger 21 and the IIth heat exchanger 19 successively
Enter second-stage reaction charging heating furnace 23 afterwards to be heated, enter secondary hydrogenation cracker 26 afterwards and enter
Row reaction；
7) the second-stage reaction product 17 of secondary hydrogenation cracker 26 is through the IIIth heat exchanger 21 and two-stage mixing
Charging 16 exchanges heat, and is mixed into fractionating section piece-rate system 28 with one section of product 5 afterwards and is separated.
One section of reaction condition is：24 operating pressure of one stage hydrofining reactor be 4.5～21MPa, one
Section hydrocracking reactor 25 operating pressure is 4.3～21MPa, and two reactor average reaction temperatures are
275 DEG C～520 DEG C, total liquid hourly space velocity (LHSV) is 0.1h-1～6.0h-1, 25 entrance hydrogen of a period of hydrocracking reactor oil
Volume ratio 50：1～4500：1.
The second-stage reaction condition is：4.5～the 21MPa of operating pressure of secondary hydrogenation cracker 26, puts down
Reaction temperature is 215 DEG C～520 DEG C, and total liquid hourly space velocity (LHSV) is 0.5h-1～12h-1, hydrogen to oil volume ratio 50：1～
4500：1.
The fresh feed 1 can be the hydro carbons such as distillate, heavy oil, coal liquifaction and biological liquefaction；
The form of the Ith heat exchanger 18 is unrestricted, can be wound around heat exchange of heat pipe, and screw thread contracting may be selected
Tight ring heat exchanger, can meet can all using for heat transfer requirements.
The form of one section of reaction feed heating furnace 22 and second-stage reaction charging heating furnace 23 is unrestricted,
It can be hotline heater etc.；The stove that goes into operation is, only reactionless heat or reaction heat is relatively low goes into operation the stage
Use, it can also be used to damage.
The form of the one stage hydrofining reactor 24 is unrestricted, can adopt up flow type, can adopt dirty
Formula；Fixed bed can be adopted, suspension bed can be adopted, ebullated bed may also be employed.
The hydrocracking reactor 25, can be the anti-of the effects such as hydrofinishing, hydro-upgrading, hydrodewaxing
Answer device.
The reactive moieties piece-rate system 28 is partially separated flow process for popular response, should have water injection facility, can be with
For thermal shunt journey, alternatively cold split flow, desulphurization of recycle hydrogen can be set, can not also be set, low point of QI prostration can be set
Sulfur, can not also set.
The fractionating section piece-rate system 29 can be stripper+fractionating column flow process, and bottom of towe can set reboiler furnace, also may be used
With steam stripping, strip tower top dry gas and can be arranged as required to desulphurization system, fractionating column is set according to product requirement
Corresponding side stripper is put, side stripper bottom can set reboiler, it is also possible to steam stripping.
The fractionating section piece-rate system 29 can arrange lighter hydrocarbons recovery part according to Production requirement, comprising deethanization
Tower, debutanizing tower and absorption tower etc..
Claims (4)
1. a kind of two sections of complete alternation method of hydrotreating, it is characterised in that comprise the steps：
1) fresh feed is mixed with one section after hydrogen mixes as one section of mixed feeding, through the Ith heat exchanger and one section
One section of reaction feed is entered after product heat exchange and heats stove heat, enter one stage hydrofining reactor afterwards
Reacted；
2) one section of refined products of one stage hydrofining reactor are exchanged heat with two-stage mixing charging through the IIth heat exchanger,
Entering a period of hydrocracking reactor afterwards carries out hydrocracking reaction；
3) one section of product of a period of hydrocracking reactor is produced with second-stage reaction after the heat exchange of the Ith heat exchanger
Thing mixes, and then enters reactive moieties piece-rate system after steam generator cooling；
4) the cold high score gas that reactive moieties piece-rate system is isolated is mixed with the external new hydrogen of device as recycle hydrogen
Close, be divided into two parts afterwards, a part is mixed with fresh feed as one section of mixing hydrogen, another part conduct
Two-stage mixing hydrogen；
5) reactive moieties piece-rate system is isolated low point of gas and sour water carrying device, low point for isolating
Oil enters fractionating section piece-rate system；
6) the detached dry gas of fractionating section piece-rate system and light fraction carrying device, the heavy constituent conduct that isolates
Recycle oil and step 4) two-stage mixing hydrogen mix and feed as two-stage mixing, two-stage mixing charging is successively through the
Enter second-stage reaction charging heating furnace to be heated after III heat exchanger and the heat exchange of the IIth heat exchanger, enter two afterwards
Section hydrocracking reactor is reacted；
7) the second-stage reaction product of secondary hydrogenation cracker is exchanged heat with two-stage mixing charging through the IIIth heat exchanger,
Fractionating section piece-rate system is mixed into afterwards with one section of product.
2. a kind of two sections of complete alternation method of hydrotreating according to claim 1, it is characterised in that：Described one
Section hydrofining reactor operating pressure is 4.5～21MPa, and a period of hydrocracking reactor operating pressure is
4.3～21MPa, two reactor average reaction temperatures are 275 DEG C～520 DEG C, and total liquid hourly space velocity (LHSV) is 0.1h-1~
6.0h-1, one stage hydrofining reactor inlet hydrogen to oil volume ratio 50：1～4500：1.
3. a kind of two sections of complete alternation method of hydrotreating according to claim 1 and 2, it is characterised in that：Institute
Stating secondary hydrogenation cracker reaction condition is：4.5～21MPa of operating pressure, average reaction temperature is
215 DEG C～520 DEG C, total liquid hourly space velocity (LHSV) is 0.5h-1～12h-1, hydrogen to oil volume ratio 50：1～4500：1.
4. a kind of two sections of complete alternation method of hydrotreating according to claim 1, it is characterised in that：Described new
Fresh charging is distillate, heavy oil, coal liquifaction and/or biological liquefaction.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510557589.XA CN106497601A (en) | 2015-09-06 | 2015-09-06 | A kind of two sections of complete alternation method of hydrotreating |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201510557589.XA CN106497601A (en) | 2015-09-06 | 2015-09-06 | A kind of two sections of complete alternation method of hydrotreating |
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| Publication Number | Publication Date |
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| CN106497601A true CN106497601A (en) | 2017-03-15 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109020824A (en) * | 2018-10-11 | 2018-12-18 | 成都科特瑞兴科技有限公司 | A kind of formamide separation system and formamide separating technology |
| CN113831935A (en) * | 2020-06-23 | 2021-12-24 | 中国石油化工股份有限公司 | Hydrocracking device |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1050572A3 (en) * | 1999-05-05 | 2001-06-06 | Bar-Co Processes Joint Venture | Residual oil fluid catalytic cracking process |
| CN1782023A (en) * | 2004-11-30 | 2006-06-07 | 中国石油化工股份有限公司 | Separating method for hydrocarbon oil catalytic cracking reaction products |
| CN1952068A (en) * | 2005-10-19 | 2007-04-25 | 中国石油化工股份有限公司 | Hydrocracking method |
-
2015
- 2015-09-06 CN CN201510557589.XA patent/CN106497601A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1050572A3 (en) * | 1999-05-05 | 2001-06-06 | Bar-Co Processes Joint Venture | Residual oil fluid catalytic cracking process |
| CN1782023A (en) * | 2004-11-30 | 2006-06-07 | 中国石油化工股份有限公司 | Separating method for hydrocarbon oil catalytic cracking reaction products |
| CN1952068A (en) * | 2005-10-19 | 2007-04-25 | 中国石油化工股份有限公司 | Hydrocracking method |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109020824A (en) * | 2018-10-11 | 2018-12-18 | 成都科特瑞兴科技有限公司 | A kind of formamide separation system and formamide separating technology |
| CN113831935A (en) * | 2020-06-23 | 2021-12-24 | 中国石油化工股份有限公司 | Hydrocracking device |
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Application publication date: 20170315 |
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