CN106147841A - A kind of Heavy oil hydrogenation method - Google Patents
A kind of Heavy oil hydrogenation method Download PDFInfo
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- CN106147841A CN106147841A CN201510194960.0A CN201510194960A CN106147841A CN 106147841 A CN106147841 A CN 106147841A CN 201510194960 A CN201510194960 A CN 201510194960A CN 106147841 A CN106147841 A CN 106147841A
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Abstract
The invention discloses a kind of Heavy oil hydrogenation method, the method can utilize recycle hydrogen to change hydrogenation protecting reactor online.Compared with prior art, the method for the present invention can effectively extend the service cycle of heavy oil hydrogenation process, improves the online rate of heavy oil hydrogenation process, but also can be completely suitable for the transformation of existing heavy oil hydrogenation process or the design of new Residue Hydrotreating Technology.
Description
Technical field
The present invention relates to a kind of Heavy oil hydrogenation method.
Background technology
Along with the heaviness of crude oil and in poor quality, environmental protection requirement increasingly stringent, market are to light-end products
Increase in demand, oil product clean requirement and improve constantly, and increasing oil refining enterprise processes at crude oil
The processing of heavy oil scheme selecting upper employing heavy-oil hydrogenation and catalytic cracking combination of route, heavy oil hydrogenation equipment
Then become the core apparatus in these oil plants.
In heavy-oil hydrogenation technology, fixed-bed process flow process is the most ripe and easily operated, is most widely used
General technique.During fixed bed heavy-oil hydrogenation, the pollution metal in mink cell focus is easiest to be removed,
These heavy metal depositions on a catalyst, can make hydrogenation catalyst fast deactivation, causes heavy-oil hydrogenation to fill
Putting needs to stop work more catalyst changeout, the service cycle of device shortens.This problem can be reacted by increase
The volume of device is slowed down, but increases reactor volume simply and can cause significantly going up of plant investment
Rise, therefore in existing fixed bed heavy-oil hydrogenation technology, consideration based on economy, the design behaviour of device
It is generally 1 year as the cycle.And the full factory of oil plant is generally 3-4 the time between overhauls(TBO), therefore use heavy oil
It is hydrogenated with the refinery as processing of heavy oil route and can experience the heavy-oil hydrogenation dress of 2-3 time within a time between overhauls(TBO)
Put more catalyst changeout of stopping work.As the core apparatus of oil plant, during heavy oil hydrogenation equipment is stopped work and is changed agent,
It is generally required to by reduce full factory crude runs, change oil variety, increase coking plant produce load,
Tackling in methods such as tank field storage part residual oil, the economic benefit of refinery can be greatly affected.
Therefore, the difficult point encountered in above-mentioned processing of heavy oil is overcome, it is provided that a kind of Heavy oil hydrogenation method, aobvious
Write the service cycle extending heavy oil hydrogenation equipment, reduce and stop work the more catalyst changeout time, improve heavy-oil hydrogenation
The online rate of device, is to improve oil plant economic benefit problem demanding prompt solution at present.
CN103059933A discloses the hydrotreating method of a kind of high-acid high-calcium heavy crude oil.The method
Package unit is divided into low-voltage hydrogenation treatment region and high-pressure hydrogenation treatment region, and wherein low-voltage hydrogenation treatment region sets
There is multiple changeable hydrogenation protecting reactor, peracid high calcium mink cell focus can be processed as qualified catalytic cracking
Raw material.But, owing to low-voltage hydrogenation treatment region is only capable of removing the Ca in raw material, changeable by low pressure
Protection reactor can delay the beds pressure drop caused due to doped calcium to raise, and for other huge sum of money
The beds blockage problem that genus deposition causes does not has been resolved, and device still can be caused because of Ni, V etc.
Heavy metal deposition and quickly stop work.
CN1484684A disclose a kind of use replaceable and can short circuit reaction device hydrotreatment of heavy hydrocarbon fraction
Method.At initial operating stage, protection reactor A and B are sequentially connected in series operation, and B is in the downstream of A；
When protection reactor A pressure drop is the highest or after catalysqt deactivation, A cuts out more catalyst changeout, and B continues
Operating；Switch response system after A more catalyst changeout, be positioned at the downstream of protection reactor B；Work as B
Pressure drop is the highest or after catalysqt deactivation, B cuts out more catalyst changeout, and A remains in operation；B changes catalysis
Switching response system after agent, comes into operation in the downstream being positioned at protection reactor A.Circulate with this, can
Extend the service cycle of full device.But, the method needs constantly to change protection reactor A, the phase of B
To position, it is therefore desirable to numerous high pressure valves, investment height, and operating process is complicated, can give and produce band
Come risk and inconvenience.
Hydrogenation plant is when changing the catalyst in reactor, owing to reactor must carry out cooling fall
Pressure, band oil, purge, a series of process such as displacement, catalyst safety therein could be drawn off；Equally,
Change reactor is cut response system after raw catelyst time, it is also desirable to carry out replacing, catalyst irrigation,
The series of preprocessing processes such as increasing temperature and pressure.Therefore, existing hydrogenation plant actually cannot realize at device
While normal operating, change and cut out the catalyst in reactor.Current existing way is, increases by one
Overlap special reactor for treatment system, including compressor, heating furnace, heat exchanger, air cooler, divide
From the equipment of the system such as device, pump, it is specifically designed to the catalyst changing changeable reactor.But, use
This method, owing to needs increase multiple devices, can be greatly increased the investment of device.
Summary of the invention
It is an object of the invention on the basis of making full use of existing hydrogenation technique, it is provided that a kind of heavy-oil hydrogenation
Method, the method can effectively extend the service cycle of heavy oil hydrogenation process, improve heavy oil hydrogenation process
Line rate, but also setting of the transformation of existing heavy oil hydrogenation process or new Residue Hydrotreating Technology can be completely suitable for
Meter.
To achieve these goals, the present invention provides a kind of Heavy oil hydrogenation method, and the method includes: a,
Heavy oil and supplementary hydrogen are sent into main hydrogenation protecting reactor and carries out hydrogenation protecting reaction, obtain hydrogenation protecting and produce
Thing；B, hydrogenation protecting product described in step a is carried out successively hydrotreating, thermal high separate and cold
High pressure separates, and obtains hot high score high score oily, cold oil and recycle hydrogen；C, by recycle hydrogen described in step b
Obtain after compression compressing recycle hydrogen；After being preheated by described compression recycle hydrogen, obtain pre-hot compression recycle hydrogen；
Described pre-hot compression recycle hydrogen, heavy oil and supplementary hydrogen are sent in described main hydrogenation protecting reactor；d、
When the pressure drop of described main hydrogenation protecting reactor reaches 0.2-1.0 MPa or its interior hydrogenation protecting catalysis
During agent inactivation, carry out standby hydrogenation protecting reactor recycle hydrogen purging, tentatively heat up, boost and
After final rise temperature, described pre-hot compression recycle hydrogen, heavy oil and supplementary hydrogen are sent into standby hydrogenation protecting reactor
Carrying out hydrogenation protecting reaction, the hydrogenation protecting product obtained carries out described hydrotreating；By described main hydrogenation
Protection reactor is replaced hydrogenation protecting catalyst under the effect of recycle hydrogen；E, standby add when described
The pressure drop of hydrogen protection reactor reaches 0.2-1.0 MPa or during its interior hydrogenation protecting catalyst inactivation,
After carrying out described main hydrogenation protecting reactor recycle hydrogen purging, tentatively heat up, boost and finally heating up,
Described pre-hot compression recycle hydrogen, heavy oil and the supplementary hydrogen main hydrogenation protecting reactor of feeding is carried out hydrogenation protecting
Reaction, the hydrogenation protecting product obtained carries out described hydrotreating；By described standby hydrogenation protecting reactor
It is replaced hydrogenation protecting catalyst under the effect of recycle hydrogen.
Preferably, wherein, hydrogenation protecting reactor carries out under the effect of recycle hydrogen described replacing to be hydrogenated with
The step of guard catalyst includes: send into together with pre-to Partial shrinkage recycle hydrogen and part hot compression recycle hydrogen
Described hydrogenation protecting reactor described hydrogenation protecting reactor is carried out purging cooling after, be re-fed into described in add
Hydrogen treatment reactor；When the purging cooling of described hydrogenation protecting reactor is complete, stop sending into described part pressure
Contracting recycle hydrogen and part pre-hot compression recycle hydrogen；After described hydrogenation protecting reactor is released, change
Hydrogenation protecting catalyst is also passed through nitrogen and carries out catalyst protection.
Preferably, wherein, hydrogenation protecting reactor Partial shrinkage recycle hydrogen hot compression pre-with part is followed
The step that ring hydrogen carries out purging, tentatively heat up, boost and finally heating up includes: by Partial shrinkage recycle hydrogen
Send into described hydrogenation protecting reactor together with hot compression recycle hydrogen pre-with part, urge more finishing changing hydrogenation protecting
The described hydrogenation protecting reactor of agent first carries out purging and preliminary intensification, then carries out boosting and final rise
Temperature；Wherein, the described Partial shrinkage recycle hydrogen hot compression pre-with part being used for purging and preliminary intensification is followed
Ring hydrogen is released, and is sent by described Partial shrinkage recycle hydrogen hot compression pre-with the part recycle hydrogen being used for finally heating up
Enter described hydrotreating reactor.
Preferably, wherein, carry out a liter step for gentle boosting described in include: reacted by described hydrogenation protecting
Device be tentatively warming up to reactor minimum boosting temperature more than, described hydrogenation protecting reactor is carried out boosting and
Final intensification.
Preferably, wherein, release described in and include: the oil in hydrogenation protecting reactor and/or gas are carried out
At least one processing mode in the separation of product low pressure, fractional distillation, burning and hydrogen reclaim processes.
Preferably, wherein, described hydrogenation protecting reactor is downstriker fixed bed reactors or is
Upstriker fixed bed reactors.
Preferably, wherein, described hydrogenation protecting reactor arrange 1 or series connection 2-3 platform fixed bed anti-
Answer device, load with 1 bed in every fixed bed reactors or add with 2-4 bed segmentation filling
Hydrogen guard catalyst.
Preferably, wherein, described main hydrogenation protecting reactor and the volumetric ratio of standby hydrogenation protecting reactor
For 0.1-10.
Preferably, wherein, described main hydrogenation protecting reactor and the volumetric ratio of standby hydrogenation protecting reactor
For 1-5.
Preferably, wherein, described heavy oil is selected from reduced crude, decompression residuum, decompressed wax oil, coking
At least one in wax oil, deasphalted oil and coal tar.
Preferably, wherein, the condition of described hydrogenation protecting reaction is: pressure is 2.0-20 MPa, temperature
For 260-430 DEG C, during raw material fluid, volume space velocity is 0.2-8.0 hour-1, and hydrogen/oil volume is than being (50:1)
-(600:1)。
The method that the present invention provides, can be used for the hydrotreating of heavy charge, the highest content of beary metal
And/or the oil product of high ferro calcium content, high olefin content processes.Main hydrogenation protecting reactor and standby hydrogenation are protected
Protect reactor and can the most mutually switch use, and change system online by catalyst, ingenious utilize technique
Produced recycle hydrogen, on the basis of not affecting technique normal operating, completes to inactivate hydrogenation protecting catalyst
The process of hydrogenation protecting reactor in Renewal process.Compared with prior art, this method of hydrotreating is not increasing
On the premise of new main equipment, the service cycle of heavy oil hydrogenation equipment can be extended 30-300%, from
And add the operational efficiency of heavy oil hydrogenation equipment, improve economy.
Other features and advantages of the present invention will be described in detail in detailed description of the invention part subsequently.
Accompanying drawing explanation
Accompanying drawing is used to provide a further understanding of the present invention, and constitutes the part of description, with
Detailed description below is used for explaining the present invention together, but is not intended that limitation of the present invention.?
In accompanying drawing:
Fig. 1 is the signal of the heavy oil hydrogenation equipment that a kind of detailed description of the invention of the inventive method is used
Figure.
Description of reference numerals
A main hydrogenation protecting reactor B standby hydrogenation protecting reactor
C hydrotreating reactor D high pressure hot separator
E hot high score Gas Cooler F cold high pressure separator
G circulating hydrogen compressor H recycle hydrogen preheater
A1 main hydrogenation protecting reactor inlet valve a2 main hydrogenation protecting reactor outlet valve
B1 standby hydrogenation protecting reactor inlet valve b2 standby hydrogenation protecting reactor outlet valve
Recycle hydrogen valve before the preheating of c1 reactor for treatment
C2 reactor for treatment preheating Posterior circle hydrogen valve
D1 reactor for treatment global cycle hydrogen is to main hydrogenation protecting reactor valves
D2 main hydrogenation protecting reactor Drainage valve
E1 reactor for treatment global cycle hydrogen is to standby hydrogenation protecting reactor valves
E2 standby hydrogenation protecting reactor Drainage valve
1 heavy oil feedstock 2 mixes hydrogen raw oil
3 hydrogenation protecting reaction product 4 hydrotreating reaction products
5 hot high score gas 6 hot high score oil
7 cold high scores feed 8 circulating hydrogens
9 cold high score oil 10 boost cycle hydrogen
11 hydrogenation reactions recycle hydrogen before the preheating of recycle hydrogen 12 reactor for treatment
13 reactor for treatment preheating Posterior circle hydrogen 14 reactor for treatment global cycle hydrogen
15 reactor discharges
Detailed description of the invention
Below in conjunction with accompanying drawing, the detailed description of the invention of the present invention is described in detail.It should be appreciated that
Detailed description of the invention described herein is merely to illustrate and explains the present invention, is not limited to this
Bright.
The present invention provides a kind of Heavy oil hydrogenation method, and the method includes: a, heavy oil and supplementary hydrogen are sent into
Main hydrogenation protecting reactor carries out hydrogenation protecting reaction, obtains hydrogenation protecting product；B, by step a
Described hydrogenation protecting product carries out hydrotreating successively, thermal high separates and separates with cold anticyclone, obtains heat high
Divide high score oily, cold oil and recycle hydrogen；C, recycle hydrogen described in step b is obtained after compression compression follow
Ring hydrogen；After being preheated by described compression recycle hydrogen, obtain pre-hot compression recycle hydrogen；Described pre-hot compression is followed
Ring hydrogen, heavy oil and supplementary hydrogen are sent in described main hydrogenation protecting reactor；D, when described main hydrogenation protecting
The pressure drop of reactor reaches 0.2-1.0 MPa or during its interior hydrogenation protecting catalyst inactivation, by standby
After hydrogenation protecting reactor recycle hydrogen carries out purging, tentatively heat up, boost and finally heating up, by described
It is anti-that pre-hot compression recycle hydrogen, heavy oil and the supplementary hydrogen standby hydrogenation protecting reactor of feeding carry out hydrogenation protecting
Should, the hydrogenation protecting product obtained carries out described hydrotreating；Described main hydrogenation protecting reactor is being followed
It is replaced hydrogenation protecting catalyst under the effect of ring hydrogen；E, when described standby hydrogenation protecting reactor
Pressure drop reaches 0.2-1.0 MPa or during its interior hydrogenation protecting catalyst inactivation, is protected by described main hydrogenation
Protect after reactor recycle hydrogen carries out purging, tentatively heats up, boosts and finally heat up, by described pre-hot pressing
Contracting recycle hydrogen, heavy oil and supplementary hydrogen are sent into main hydrogenation protecting reactor and are carried out hydrogenation protecting reaction, obtain
Hydrogenation protecting product carries out described hydrotreating；By described standby hydrogenation protecting reactor at the work of recycle hydrogen
It is replaced hydrogenation protecting catalyst under with.
According to the present invention, hydrogenation protecting reactor is carried out under the effect of recycle hydrogen described hydrogenation of changing and protects
Protect the step of catalyst to may include that and send together with pre-to Partial shrinkage recycle hydrogen and part hot compression recycle hydrogen
Enter after described hydrogenation protecting reactor carries out purging cooling to described hydrogenation protecting reactor, be re-fed into described
Hydrotreating reactor；When the purging cooling of described hydrogenation protecting reactor is complete, stop sending into described part
Compression recycle hydrogen and part pre-hot compression recycle hydrogen；After described hydrogenation protecting reactor is released, more
Change hydrogenation protecting catalyst and be passed through nitrogen and carry out catalyst protection.
According to the present invention, hydrogenation protecting reactor Partial shrinkage recycle hydrogen is circulated with the pre-hot compression of part
Hydrogen carries out purging, rising the step of gentle boosting and may include that Partial shrinkage recycle hydrogen and the pre-hot pressing of part
Described hydrogenation protecting reactor sent into together by contracting recycle hydrogen, to the described hydrogen more finishing changing hydrogenation protecting catalyst
Protection reactor first carries out purging and tentatively heats up, and then carries out boosting and final intensification；Wherein, will use
Release in purging and preliminary described Partial shrinkage recycle hydrogen hot compression pre-with the part recycle hydrogen heated up, will use
Send at described hydrogenation with part pre-hot compression recycle hydrogen in the final described Partial shrinkage recycle hydrogen heated up
Reason reactor.
According to the present invention, described in the step that tentatively heats up, boost and finally heat up may include that by
Described hydrogenation protecting reactor is tentatively warming up to reactor minimum boosting temperature (MPT, Minimum
Pressurization Temperature) more than, described hydrogenation protecting reactor is carried out boosting and final rise
Temperature.Described minimum boosting temperature is well-known to those skilled in the art, is typically provided by device manufacturer,
Different according to the difference of device, typically at 50-100 degrees centigrade.
According to the present invention, by Special circulation hydrogen transfer pipeline be individually delivered to main hydrogenation protecting reactor and
The recycle hydrogen of standby hydrogenation protecting reactor inlet can come from positions different in circulating hydrogen system, can
With changed from the ratio of the recycle hydrogen of recycle hydrogen preheater upstream and downstream by regulation be delivered to main
The temperature of the circulating hydrogen of hydrogenation protecting reactor and standby hydrogenation protecting reactor inlet.Art technology
Personnel, it is understood that the hot-fluid side medium of recycle hydrogen preheater can have multiple choices, can be anti-
Answer product, it is also possible to be hot high score gas, or from other high-temperature position logistics, be not specially limited herein,
Can optimum option as required.
According to the present invention, described in release be well-known to those skilled in the art, may include that and will be hydrogenated with
Oil and/or gas in protection reactor carry out returning selected from the separation of product low pressure, fractional distillation, burning and hydrogen
At least one processing mode in receipts processes, for example, it is possible to deliver to this device reaction product low pressure separated part
Point, in fractionating system, torch bleed-off system, hydrogen recovery system or device other suitable place outer one
Place or a few place, be not specially limited herein, can be in optimized selection according to practical situation.Described reaction
Product low pressure separate section refers to that thermal low-pressure separators (being positioned at the downstream of hot high score oil) separates with cold low
Device (is positioned at the downstream of cold high score oil), low point of oil of heat out and cold low point of oil from above-mentioned two container
Enter fractionating system.
According to the present invention, described hydrogenation protecting reactor is well-known to those skilled in the art, such as,
Can be all downstriker fixed bed reactors or can be all upstriker fixed bed reactors.The present invention adds
Hydrogen protection reactor can arrange the 2-3 platform fixed bed reactors of series connection, preferably 1；Solid at every
Can load with 1 bed in fixed bed reactor or hydrogenation protecting can be loaded with 2-4 bed segmentation
Catalyst.The volumetric ratio of described main hydrogenation protecting reactor and standby hydrogenation protecting reactor can be
0.1-10, preferably 1-5.The determination of this volumetric ratio mainly foundation device is newly-built or old device
Transformation, and desired by the cycle of oparation of heavy oil hydrogenation equipment that reaches, come excellent according to practical situation
Change and select.
According to the present invention, described heavy oil is well-known to those skilled in the art, for example, it is possible to for being selected from
In reduced crude, decompression residuum, decompressed wax oil, wax tailings, deasphalted oil and coal tar at least one
Kind.It will be appreciated by persons skilled in the art that the device design according to oil plant and raw material sources situation,
The most above-mentioned heavy oil feedstock both can be used alone, it is also possible to makes with the mixing of any suitable ratio
With, to realize refinery's maximizing the benefits as target.
According to the Heavy oil hydrogenation method of the present invention, wherein said hydrogenation protecting reaction is people in the art
Known to Yuan, its main purpose is under the effect of hydrogenation protecting catalyst, makes mixed hydrogen raw oil add
Carry out hydrogenation protecting reaction in hydrogen protection reactor, with removing major part heavy metal, calcium, sodium, ferrum, consolidate
Body impurity etc., and complete most olefin saturation.In the present invention, described hydrogenation protecting
The catalyst etc. that the reactor of reaction designs and arranges, used, can enter according to conventional prior art
Row determines, there is no particular limitation to it for the present invention.
Similarly, according to the Heavy oil hydrogenation method of the present invention, wherein said hydrotreating reaction is ability
Known to field technique personnel, its main purpose is under the effect of hydrotreating catalyst, makes through described
The reacted raw material heavy oil of hydrogenation protecting deviates from the most remaining metal impurities and sulfur, nitrogen, carbon residue etc. again
And there is a small amount of cracking reaction, make raw material heavy oil modified, be especially suitable for carrying out follow-up catalytic cracking
Processing technique.In the present invention, the reactor of described hydrotreating reaction designs and arranges, used
Catalyst etc., can be determined according to conventional prior art, and there is no particular limitation to it for the present invention.
According to the present invention, the condition of described hydrogenation protecting reaction can be: pressure is 2.0-20 MPa, temperature
Degree is for 260-430 DEG C, and during raw material fluid, volume space velocity is 0.2-8.0 hour-1, hydrogen/oil volume is than being (50:1)
-(600:1).The condition of described hydrotreating reaction can be: pressure 2.0-20MPa, temperature 260-430 DEG C,
Volume space velocity 0.1-8.0hr during raw material fluid-1, hydrogen/oil volume ratio (50:1)-(1000:1).
Below in conjunction with accompanying drawing, it is provided that the detailed description of the invention of the Heavy oil hydrogenation method of the present invention.
As it is shown in figure 1, there are two hydrogenation protecting reactors in parallel in response system, it is respectively main adding
Hydrogen protection reactor A and standby hydrogenation protecting reactor B, heavy oil 1 and hydrogen 11 (for supplement hydrogen and
The mixing hydrogen of recycle hydrogen, supplementary hydrogen can mix with the compression recycle hydrogen after circulating hydrogen compressor G compresses
After conjunction add) mixed hydrogen raw oil 2 through entrance pipe enter main hydrogenation protecting reactor A, now valve
A1 and a2 opens, and valve b1 and b2 closes, and valve c1, c2, d1, d2, e1, e2 close.
The hydrogenation protecting reaction product 3 obtained enters and carries out hydrotreating reaction in hydrotreating reactor C,
The hydrotreating reaction product 4 obtained enters follow-up piece-rate system.When in hydrogenation protecting reactor A
Catalysqt deactivation or pressure drop rise to 0.2-1.0MPa time, open valve b1 and b2, close valve
A1, switches to mixed hydrogen raw oil 2 carry out hydrogenation protecting reaction in standby hydrogenation protecting reactor B,
To hydrogenation protecting reaction product enter hydrotreating reactor C carry out hydrotreating reaction；Meanwhile,
Opening valve c1, c2 and d1, main hydrogenation protecting reactor A is entered by the hydrogen for self-loopa hydrogen system
Row purging, cooling, cross valve a2 and from standby hydrogenation protecting from reactor A hydrogen circulation out
Hydrogenation protecting reaction product in reactor B enters hydrotreating reactor C in the lump.Work as reactor A
After completing purging and cooling, close valve a2, c1, c2 and d1, open valve d2, after bleed-off system
Do respective handling more catalyst changeout, and the new catalyst changed is implemented nitrogen protection.When standby hydrogenation
When catalyst in protection reactor B will inactivate or pressure drop will rise to 0.2-1.0MPa, need
The main hydrogenation protecting reactor A more finishing changing catalyst is carried out increasing temperature and pressure, be first turned on valve c1,
C2, d1 and d2, carry out purging displacement and be tentatively warming up to reactor minimum boosting temperature reactor A
(MPT, Minimum Pressurization Temperature) more than 100 DEG C, closes valve d2, profit
With recycle hydrogen, reactor A is boosted, open valve a2, utilize recycle hydrogen intensification final to reactor A
To temperature required, opening valve a1 afterwards, close valve c1, c2 and d1, reactor A is hydrogenated with
Protection reaction.Reaction is can be used for by the method that reactor A is replaced catalyst and increasing temperature and pressure
Device B.By main hydrogenation protecting reactor A and the switching in turn of standby hydrogenation protecting reactor B with make
With, until after the hydrotreating catalyst in hydrotreating reactor C thoroughly inactivates, device is stopped work and is changed
All catalyst.Thus, make full use of recycle hydrogen system, increase existing heavy oil hydrogenation equipment need not
Under conditions of equipment, extend the service cycle of heavy oil hydrogenation equipment significantly.
Embodiment it is provided below to further illustrate the present invention, but the most therefore the present invention is taken office
What limits.
The actual conditions of the present embodiment is as follows:
A) raw oil used is the miscella of decompression residuum and wax oil, and wherein decompression residuum accounts for 76wt%,
Raw oil total sulfur content is 3.01wt%, and total nitrogen content is 0.4wt%, and carbon residue content is 12.02wt%,
Content of beary metal is 99wppm, iron content 19wppm, and the density at raw oil 20 DEG C is 0.989g.cm-3,
Viscosity at 100 DEG C is 275mm2.s-1。
B) main hydrogenation protecting reactor A is the downstriker fixed bed reactors of two series connection, and catalyst is often
Individual reactor is monolayer filling.
C) standby hydrogenation protecting reactor B is downstriker fixed bed reactors, and catalyst monolayers fills
Fill out.
D) hydrotreating reactor C is set to 3 downstriker fixed bed reactors series connection, every reactor
In catalyst be all monolayer filling.
E) hydrogenation protecting reactor A entry operation condition is: pressure 18.35MPa, temperature 386 DEG C,
Raw material liquid hourly space velocity (LHSV) 0.66hr-1。
F) hydrogenation protecting reactor B entry operation condition is: pressure 18.35MPa, temperature 386 DEG C,
Raw material liquid hourly space velocity (LHSV) 0.77hr-1。
G) hydrotreating reactor C entry operation condition is: pressure 17.7MPa, temperature 365 DEG C, former
Material liquid hourly space velocity (LHSV) 0.26hr-1。
H) main hydrogenation protecting reactor A is 1.17 with the volume ratio of standby hydrogenation protecting reactor B.
I) special with what main hydrogenation protecting reactor A and standby hydrogenation protecting reactor B entrance were connected
The front recycle hydrogen (12) of reactor for treatment preheating that recycle hydrogen transfer pipeline exports from circulating hydrogen compressor
Posterior circle hydrogen (13) is preheated with from the reactor for treatment after recycle hydrogen and hot high score gas heat exchange, the two
Ratio can be changed by the aperture of respective valve and be adjusted between 0.01-100.
J) main hydrogenation protecting reactor A and the special leakage path of standby hydrogenation protecting reactor B outlet
It is connected with this device reaction product low pressure separate section and flare system (not shown).
K) catalysts conditions is: use the RHT series of Sinopec Research Institute of Petro-Chemical Engineering exploitation
Heavy-oil hydrogenation catalyst, is produced by Sinopec catalyst Chang Ling branch company, and active component is Ni/Mo/Co,
Profile is butterfly, and type of feed is cloth bag filling.
L) the reactor use sequence of device is: main hydrogenation protecting reactor A-standby hydrogenation protecting reaction
Device B-main hydrogenation protecting reactor A-standby hydrogenation protecting reactor B, changes 3 hydrogenation the most online and protects
Protect catalyst.
In the present embodiment, the cycle of oparation of device can reach 3 years, with the time between overhauls(TBO) (3 of oil plant
Year) match, therefore within refinery's time between overhauls(TBO), device can continuously run, and uses altogether in 3 years
Hydrogenation catalyst 1728 tons.Using in the case of routine techniques, be i.e. not provided with changeable reactor with
And catalyst change process system, the cycle of oparation of device can only achieve 1 year, at oil plant
One interior device of time between overhauls(TBO) (3 years) needs to stop work for 2 times more catalyst changeout, needs to stop work 60 for 2 times altogether
My god, make spent hydroprocessing catalyst 2940 tons in 3 years altogether.
Claims (11)
1. a Heavy oil hydrogenation method, the method includes:
A, heavy oil and supplementary hydrogen are sent into main hydrogenation protecting reactor carry out hydrogenation protecting reaction, added
Hydrogen protection product；
B, hydrogenation protecting product described in step a is carried out successively hydrotreating, thermal high separate and cold
High pressure separates, and obtains hot high score high score oily, cold oil and recycle hydrogen；
C, by recycle hydrogen described in step b after compression obtain compress recycle hydrogen；By described compression circulation
After hydrogen preheating, obtain pre-hot compression recycle hydrogen；Described pre-hot compression recycle hydrogen, heavy oil and supplementary hydrogen are sent
Enter in described main hydrogenation protecting reactor；
D, reach 0.2-1.0 MPa or its interior hydrogenation is protected when the pressure drop of described main hydrogenation protecting reactor
When protecting catalysqt deactivation, carry out standby hydrogenation protecting reactor recycle hydrogen purging, tentatively heat up, rise
After pressure and final intensification, described pre-hot compression recycle hydrogen, heavy oil and supplementary hydrogen are sent into standby hydrogenation protecting
Reactor carries out hydrogenation protecting reaction, and the hydrogenation protecting product obtained carries out described hydrotreating；By described
Main hydrogenation protecting reactor is replaced hydrogenation protecting catalyst under the effect of recycle hydrogen；
E, reach 0.2-1.0 MPa or its interior hydrogenation when the pressure drop of described standby hydrogenation protecting reactor
During guard catalyst inactivation, carry out described main hydrogenation protecting reactor recycle hydrogen purging, tentatively heat up,
After boosting and final intensification, described pre-hot compression recycle hydrogen, heavy oil and supplementary hydrogen are sent into main hydrogenation protecting
Reactor carries out hydrogenation protecting reaction, and the hydrogenation protecting product obtained carries out described hydrotreating；By described
Standby hydrogenation protecting reactor is replaced hydrogenation protecting catalyst under the effect of recycle hydrogen.
Method the most according to claim 1, wherein, by hydrogenation protecting reactor in the effect of recycle hydrogen
Under carry out the step of described replacing hydrogenation protecting catalyst and include:
React sending into described hydrogenation protecting together with pre-to Partial shrinkage recycle hydrogen and part hot compression recycle hydrogen
After device carries out purging cooling to described hydrogenation protecting reactor, it is re-fed into described hydrotreating reactor；
When described hydrogenation protecting reactor purging cooling complete, stop send into described Partial shrinkage recycle hydrogen with
Part pre-hot compression recycle hydrogen；
After described hydrogenation protecting reactor is released, change hydrogenation protecting catalyst and be passed through nitrogen and enter
Row catalyst protection.
Method the most according to claim 1, wherein, circulates hydrogenation protecting reactor Partial shrinkage
The step that hydrogen hot compression pre-with part recycle hydrogen carries out purging, tentatively heat up, boost and finally heating up includes:
React sending into described hydrogenation protecting together with pre-to Partial shrinkage recycle hydrogen and part hot compression recycle hydrogen
Device, first carries out purging and preliminary liter to the described hydrogenation protecting reactor more finishing changing hydrogenation protecting catalyst
Temperature, then carries out boosting and final intensification；
Wherein, the described Partial shrinkage recycle hydrogen hot compression pre-with part being used for purging and preliminary intensification is followed
Ring hydrogen is released, and is sent by described Partial shrinkage recycle hydrogen hot compression pre-with the part recycle hydrogen being used for finally heating up
Enter described hydrotreating reactor.
Method the most according to claim 3, wherein, described in carry out liter the step of gentle boosting and include:
Described hydrogenation protecting reactor is tentatively warming up to more than reactor minimum boosting temperature, adds described
Hydrogen protection reactor carries out boosting and final intensification.
5. release described according to the method for Claims 2 or 3, wherein, and include: hydrogenation protecting is anti-
The oil in device and/or gas is answered to carry out in the separation of product low pressure, fractional distillation, burning and hydrogen reclaim
At least one processing mode processes.
Method the most according to claim 1, wherein, described hydrogenation protecting reactor is downstriker
Fixed bed reactors or be upstriker fixed bed reactors.
Method the most according to claim 1, wherein, described hydrogenation protecting reactor arranges 1 or string
The 2-3 platform fixed bed reactors of connection, with 1 bed filling or with 2-4 in every fixed bed reactors
Individual bed segmentation filling hydrogenation protecting catalyst.
Method the most according to claim 1, wherein, described main hydrogenation protecting reactor and standby hydrogenation
The volumetric ratio of protection reactor is 0.1-10.
Method the most according to claim 1, wherein, described main hydrogenation protecting reactor and standby hydrogenation
The volumetric ratio of protection reactor is 1-5.
Method the most according to claim 1, wherein, described heavy oil is selected from reduced crude, decompression slag
At least one in oil, decompressed wax oil, wax tailings, deasphalted oil and coal tar.
11. methods according to claim 1, wherein, the condition of described hydrogenation protecting reaction is: pressure
For 2.0-20 MPa, temperature is 260-430 DEG C, and during raw material fluid, volume space velocity is 0.2-8.0 hour-1,
Hydrogen/oil volume is than being (50:1)-(600:1).
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106917163A (en) * | 2017-03-13 | 2017-07-04 | 中国科学院过程工程研究所 | A kind of hydrocarbon cracking prepares the reaction system and its processing method and purposes of carbon fiber |
| CN110684557A (en) * | 2018-07-06 | 2020-01-14 | 中国石油化工股份有限公司 | Residual oil hydrotreating method and system |
| CN112980508A (en) * | 2019-12-12 | 2021-06-18 | 中国石化工程建设有限公司 | Heavy oil hydrogenation method and system thereof |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3544449A (en) * | 1968-12-03 | 1970-12-01 | Cities Service Res & Dev Co | Removing tetrahydrofuran insolubles from a hydrogenation feedstock |
| CN102311794A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Diesel hydrogenation method |
| CN103059928A (en) * | 2011-10-24 | 2013-04-24 | 中国石油化工股份有限公司 | Hydrotreating device and application thereof as well as residual oil hydrotreating method |
-
2015
- 2015-04-22 CN CN201510194960.0A patent/CN106147841B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3544449A (en) * | 1968-12-03 | 1970-12-01 | Cities Service Res & Dev Co | Removing tetrahydrofuran insolubles from a hydrogenation feedstock |
| CN102311794A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Diesel hydrogenation method |
| CN103059928A (en) * | 2011-10-24 | 2013-04-24 | 中国石油化工股份有限公司 | Hydrotreating device and application thereof as well as residual oil hydrotreating method |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106917163A (en) * | 2017-03-13 | 2017-07-04 | 中国科学院过程工程研究所 | A kind of hydrocarbon cracking prepares the reaction system and its processing method and purposes of carbon fiber |
| CN106917163B (en) * | 2017-03-13 | 2019-06-14 | 中国科学院过程工程研究所 | A kind of hydrocarbon cracking prepares the reaction system and its processing method and purposes of carbon fiber |
| CN110684557A (en) * | 2018-07-06 | 2020-01-14 | 中国石油化工股份有限公司 | Residual oil hydrotreating method and system |
| CN110684557B (en) * | 2018-07-06 | 2021-12-17 | 中国石油化工股份有限公司 | Residual oil hydrotreating method and system |
| CN112980508A (en) * | 2019-12-12 | 2021-06-18 | 中国石化工程建设有限公司 | Heavy oil hydrogenation method and system thereof |
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