CN108865258A - A kind of diesel oil, wax oil synthesis add hydrogen production system and method - Google Patents
A kind of diesel oil, wax oil synthesis add hydrogen production system and method Download PDFInfo
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- CN108865258A CN108865258A CN201810557576.6A CN201810557576A CN108865258A CN 108865258 A CN108865258 A CN 108865258A CN 201810557576 A CN201810557576 A CN 201810557576A CN 108865258 A CN108865258 A CN 108865258A
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- tower
- pump
- diesel oil
- raw material
- stripper
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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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/14—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including at least two different refining steps in the absence of hydrogen
-
- 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
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
-
- 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
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/1048—Middle distillates
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
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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 invention discloses the synthesis of a kind of diesel oil, wax oil to add hydrogen production system and method, which includes：Raw material blending device, for carrying out mixed processing to catalytic diesel oil, wax tailings, mixed diesel and coker gasoline；First feed pump, for carrying out pressure-increasing unit to mixed raw material；Hydrogenation reaction unit, for making the mixed raw material carry out hydrogenation reaction；Prime processing unit (plant) and rear class processing unit (plant) are respectively used to process the product progress prime separation of hydrogenation reaction and rear class separation is processed, and successively adds hydrogen wax oil and hydrogenated diesel oil to reaction product progress prime separation and rear class separation to obtain.According to market situation, the processing technology of production system can be adjusted flexibly, diesel oil or simultaneous processing diesel oil and wax oil are individually processed in selection, when raw material composition changes, adjusting process condition is not needed, the accounting of mixed raw material key component need to be only precisely controlled, it can be ensured that hydrogenated diesel oil product reaches state five, six diesel oil standard of state, has preferable applicability.
Description
Technical field
The present invention relates to the synthesis of chemical production technical field more particularly to a kind of diesel oil, wax oil add hydrogen production system and
Method.
Background technique
In Chemical Manufacture, the property of catalytic cracking diesel oil (i.e. catalytic diesel oil) is more bad, is embodied in that density is big, aromatic hydrocarbons
Content is high, Cetane number is low, calls in finished diesel fuel after adding hydrogen, easily reduces finished diesel fuel quality, and due to having in catalytic diesel oil
The reason of aromatic component, the Cetane number in catalytic diesel oil are lower.Decompressed wax oil and delay coke makeup due to Atmospheric vacuum production
It sets containing the harmful non-hydrocarbon compound such as more unsaturated hydrocarbons and sulphur, nitrogen in the wax tailings of production, these products can not reach
To the production requirement of catalytic cracking unit.In order to make the wax oil of secondary operation reach the production requirement of catalytic cracking unit, it is necessary to
Hydrofinishing is carried out to wax tailings and decompressed wax oil.Since wax oil price is relatively cheap in the market, enterprise's outsourcing wax oil is carried out
It is larger to produce and process benefit, therefore adaptability reform is carried out to original diesel hydrotreating unit, so that it has simultaneous processing bavin wax
The ability of oily mixed raw material can obtain better benefit.
Existing catalytic diesel oil processing technology process is：Diesel hydrotreating unit raw material is mainly by catalytic diesel oil, mixed diesel
(coker gas oil and bitumen diesel), coker gasoline composition, three are conveyed from tank field by pump, the on-line mixing on pipeline.After mixing
After reacted unit hydrogenation reaction, enters stripper after feed product exchanges heat and be separated into naphtha, hydrogenated diesel oil product.Tower bottom
Equipped with reboiling heating furnace, heat is provided to stripper.
In realizing process of the present invention, at least there are the following problems in the prior art for inventor's discovery：
1, in above-mentioned process process, raw material mixing is uneven, cause it is uneven in reactor temperature, affect plus
Hydrogen reaction effect；To guarantee that product quality needs to adjust the process conditions of diesel hydrotreating unit, make when raw material fluctuates
At technological fluctuation, envoy can be optimal, and there are some potential safety problemss during adjusting.
2, when raw material components change, the ratio of catalytic diesel oil raw material is easy to influence final hydrogenated diesel oil product matter
Amount, even results in that product quality is unqualified, and the adjustment of catalytic diesel oil material rate need to by virtue of experience go to adjust, and cannot refine control
System.
In conclusion existing processing unit (plant), system are easy to be influenced by upstream raw material, very to process conditions
Greatly, urgently occur now it is a kind of can flexibly, be precisely controlled processing diesel oil or can with the system of simultaneous processing diesel oil and wax oil or
Method.
Summary of the invention
In order to overcome the shortcomings of Related product in the prior art, the present invention proposes a kind of diesel oil, the synthesis of wax oil adds hydrogen raw
System and method is produced, solving the problems, such as in the prior art can only diesel oil and the single processing of wax oil progress.
The present invention provides the synthesis of a kind of diesel oil, wax oil to add hydrogen production system, including：The raw material mixing dress successively installed
It sets, the first feed pump, hydrogenation reaction unit, prime processing unit (plant) and rear class processing unit (plant)；
Raw material blending device, for being carried out at mixing to catalytic diesel oil, wax tailings, mixed diesel and coker gasoline
Reason；
First feed pump, for carrying out pressure-increasing unit to mixed raw material；
Hydrogenation reaction unit, for making the mixed raw material carry out hydrogenation reaction；
Prime processing unit (plant) and rear class processing unit (plant) are respectively used to carry out the product of hydrogenation reaction prime separation processing
Processing is separated with rear class, and prime separation and rear class separation successively are carried out to reaction product and add hydrogen wax oil and plus hydrogen bavin to obtain
Oil.
In some embodiments of the present invention, the raw material blending device includes at least two groups for the mixed of mixed raw material
Close tank, the second feed pump and online mixer, the blending tank and second feed pump respectively with the online mixer
Connection, the output end of the online mixer connect with first feed pump；At least two groups blending tank is arranged parallel,
The alternating hybrid process of multithreading is provided, catalytic diesel oil, wax tailings and mixed diesel pass through pipeline respectively and enter described mix
Close in-tank mixing；The coker gasoline is input in online mixer after being pressurized by second feed pump, in blending tank
The mixture of output further mixes.
In some embodiments of the present invention, the entrance of the feed(raw material)inlet of the blending tank and the first feed pump is all provided with
It is equipped with the on-line detector for real-time detection raw material admixture.
In some embodiments of the present invention, the prime processing unit (plant) includes First Heat Exchanger, the first water cooler, tower
Bottom product pump, the first stripper, tower bottom reboiler furnace feed pump, reboiler furnace, the first air cooler, the second water cooler, the first tower top return
Flow tank and the first tower top return pump；The First Heat Exchanger is produced with the hydrogenation reaction unit, the first water cooler, tower bottom respectively
Product pump and the connection of the first stripper；First water cooler, tower bottom reboiler furnace feed pump, reboiler furnace and rear class processing unit (plant)
It is sequentially connected setting；The bottom product pump connection is arranged in first stripper bottom；First stripper, the first sky
Cooler, the second water cooler, the first return tank of top of the tower and the first tower top return pump circuit sequentially connection；The product of hydrogenation reaction is logical
Cross the hydrogenation reaction unit enter in the First Heat Exchanger be heated to reaction temperature and be delivered in the first stripper into
The separation of row raw material；The gas-liquid mixture isolated successively enters the first overhead reflux after the first air cooler and the second water cooler
Tank, isolates acid water in first return tank of top of the tower, and remaining product is pumped back to described by first overhead reflux
First stripper multi-cycle separation, while crude naphtha is isolated before entering first stripper；Divide in first stripper
The reaction product separated out pass sequentially through the bottom product pump, First Heat Exchanger, the first water cooler, tower bottom reboiler furnace feed pump,
Reboiler furnace enters the rear class processing unit (plant).
In some embodiments of the present invention, the rear class processing unit (plant) includes main fractionating tower, the second air cooler, third
Water cooler, the second tower top return pump, the second heat exchanger, middle section reflux pump, third tower top return pump, steams the second return tank of top of the tower
Vapour generator, the 4th water cooler, the second stripper and the 4th tower top return pump；The main fractionating tower adds with the prime respectively
Tooling sets, the second air cooler, the second tower top return pump, the second heat exchanger, middle section reflux pump, third tower top return pump and second
Stripper connection, wherein the main fractionating tower, the second air cooler, third water cooler, the second return tank of top of the tower, the second tower top return
Stream pump circuits sequentially connection, and the main fractionating tower, the second heat exchanger and middle section reflux pump circuit sequentially connection, the main fractionation
Tower, the second stripper and the 4th tower top return pump are sequentially connected, the main fractionating tower, third tower top return pump, steam generation
Device and the 4th water cooler are sequentially connected；The reaction product that prime processing unit (plant) completes the process enters the main fractionating tower and is divided
It evaporates, and passes through second heat exchanger and middle section reflux pump recovery waste heat；The gas-liquid mixture fractionated out successively passes through second
Enter the second return tank of top of the tower after air cooler and third water cooler, remaining product is pumped back to described by second overhead reflux
Main fractionating tower multi-cycle separation, while crude naphtha is isolated before entering the main fractionating tower；And pass through third tower respectively
Top reflux pump, steam generator and the 4th water cooler, which are isolated, to be added hydrogen wax oil and is returned by the second stripper and the 4th tower top
Stream pump isolates hydrogenated diesel oil.
The present invention also provides the synthesis Hydrogenation production methods of a kind of diesel oil, wax oil, are applied to described in any of the above embodiments
Diesel oil, wax oil synthesis add hydrogen production system, include the following steps：
Catalytic diesel oil, wax tailings, mixed diesel are each led into blending tank and mixed；
And be input in online mixer after being pressurized coker gasoline by second feed pump, and it is defeated in blending tank
Mixture out further mixes；
Mixed raw material carries out hydrogenation reaction by the first feed pump pressure-increasing unit to hydrogenation reaction unit；
Prime separation processing and rear class separation processing are carried out to the product of hydrogenation reaction respectively, and successively to reaction product into
The separation of row prime is separated with rear class to obtain and add hydrogen wax oil and hydrogenated diesel oil.
In some embodiments of the present invention, the method also includes：In the feed(raw material)inlet of the blending tank and
The entrance of one feed pump is respectively provided with the on-line detector for real-time detection raw material admixture.
In some embodiments of the present invention, the prime separation, which is processed, is specially：
The product of hydrogenation reaction is entered in First Heat Exchanger by the hydrogenation reaction unit and is heated to reaction temperature simultaneously
It is delivered in the first stripper and carries out raw material separation；The gas-liquid mixture isolated successively passes through the first air cooler and the second water cooling
Enter the first return tank of top of the tower after device, acid water is isolated in first return tank of top of the tower, remaining product passes through the first tower
Top reflux is pumped back to the first stripper multi-cycle separation, while isolating rubble brain before entering first stripper
Oil；The reaction product isolated in first stripper passes sequentially through bottom product pump, First Heat Exchanger, the first water cooler, tower bottom
Reboiler furnace feed pump, reboiler furnace enter rear class processing unit (plant) and carry out rear class separation processing.
In some embodiments of the present invention, the second-order separation, which is processed, is specially：
The reaction product that completes the process of prime separation enters main fractionating tower and is fractionated, and by the second heat exchanger and in
Section reflux pump recovery waste heat；The gas-liquid mixture fractionated out successively enters the second tower after the second air cooler and third water cooler
Return tank is pushed up, remaining product is pumped back to the main fractionating tower multi-cycle separation by the second overhead reflux, while entering the master
Crude naphtha is isolated before fractionating column；And pass through third tower top return pump, steam generator and the 4th water cooler respectively
It isolates and adds hydrogen wax oil and hydrogenated diesel oil is isolated by the second stripper and the 4th tower top return pump.
Compared with prior art, the invention has the advantages that：
The embodiment of the present invention especially makes total aromatic hydrocarbons and monocycle, bicyclic virtue by the mixed raw material components of on-line analysis
The accounting of hydrocarbon ensure that charging is stablized, by raw material blending device to catalytic diesel oil, wax tailings, mixing near reasonable value
Diesel oil and coker gasoline carry out mixed processing, and the first feed pump carries out pressure-increasing unit to hydrogenation reaction unit to mixed raw material
Hydrogenation reaction is carried out, prime processing unit (plant) and rear class processing unit (plant) are respectively used to carry out prime separation to the product of hydrogenation reaction
Processing separates processing with rear class, and successively carries out prime separation and rear class separation to reaction product and add hydrogen wax oil and plus hydrogen to obtain
Diesel oil is produced compared to existing diesel oil hydrogenation, and the embodiment of the present invention with simultaneous processing diesel oil and wax oil and can react
Corresponding lock out operation is carried out at rear, according to market situation, the processing technology of production system can be adjusted flexibly, selection individually adds
Work diesel oil or simultaneous processing diesel oil and wax oil, cost are lower than single processing diesel oil and wax oil respectively, have preferably economic effect
Benefit, meanwhile, when raw material composition changes, does not need to adjust process conditions, only need strict control mixed raw material key component
Accounting, be precisely controlled, still ensure that qualified product, by on-line checking analysis ensure total aromatic hydrocarbons and monocycle, bicyclic virtue
The accounting of hydrocarbon can process catalytic diesel oil near reasonable value with maximum, while can guarantee that hydrogenated diesel oil product quality reaches state
Five standards, especially Cetane number total energy are qualified, operating condition can be adjusted flexibly, adaptability to raw material is strong, according to upstream device product feelings
Condition can be used as diesel oil hydrogenation modification device or diesel oil, wax oil hydrogenation modifying apparatus, in the case where guaranteeing key component accounting,
It may insure the poor catalytic diesel oil raw material of processing as much as possible, there is preferable applicability.
Detailed description of the invention
It to describe the technical solutions in the embodiments of the present invention more clearly, below will be to needed in the embodiment
Attached drawing is briefly described, it should be apparent that, drawings in the following description are only some embodiments of the invention, for ability
For the those of ordinary skill of domain, without creative efforts, it can also be obtained according to these attached drawings other attached
Figure.
Fig. 1 adds the theory structure schematic diagram of hydrogen production system for the synthesis of diesel oil, wax oil described in the embodiment of the present invention；
Fig. 2 is the theory structure schematic diagram of raw material blending device described in the embodiment of the present invention；
Fig. 3 is the theory structure schematic diagram of prime processing unit (plant) described in the embodiment of the present invention；
Fig. 4 is the theory structure schematic diagram of rear class processing unit (plant) described in the embodiment of the present invention；
Fig. 5 is the flow diagram of the synthesis Hydrogenation production method of diesel oil described in the embodiment of the present invention, wax oil.
Description of symbols：
100- raw material blending device, 101- blending tank, the second feed pump of 102-, 103- online mixer, 104- are examined online
Survey instrument, the first feed pump of 200-, 300- hydrogenation reaction unit, 400- prime processing unit (plant), 401- First Heat Exchanger, 402- first
Water cooler, 403- bottom product pump, the first stripper of 404-, 405- tower bottom reboiler furnace feed pump, 406- reboiler furnace, 407- first
Air cooler, the second water cooler of 408-, the first return tank of top of the tower of 409-, the first tower top return pump of 410-, 500- rear class processing unit (plant),
501- main fractionating tower, the second air cooler of 502-, 503- third water cooler, the second return tank of top of the tower of 504-, the second tower top of 505- return
Flow pump, the second heat exchanger of 506-, the middle section 507- reflux pump, 508- third tower top return pump, 509- steam generator, 510- the 4th
Water cooler, the second stripper of 511-, the 4th tower top return pump of 512-.
Specific embodiment
In order to enable those skilled in the art to better understand the solution of the present invention, below in conjunction in the embodiment of the present invention
Attached drawing, technical scheme in the embodiment of the invention is clearly and completely described.Obviously, described embodiment is only
A part of the embodiment of the present invention gives presently preferred embodiments of the present invention instead of all the embodiments in attached drawing.The present invention can
To realize in many different forms, however it is not limited to embodiment described herein, on the contrary, provide the mesh of these embodiments
Be to make the disclosure of the present invention more thorough and comprehensive.Based on the embodiments of the present invention, the common skill in this field
Art personnel every other embodiment obtained without creative efforts belongs to the model that the present invention protects
It encloses.
Unless otherwise defined, all technical and scientific terms used herein and belong to technical field of the invention
The normally understood meaning of technical staff is identical.Term as used herein in the specification of the present invention is intended merely to description tool
The purpose of the embodiment of body, it is not intended that in the limitation present invention.In description and claims of this specification and above-mentioned attached drawing
Term " includes " and " having " and their any deformations, it is intended that cover and non-exclusive include.Such as contain a system
The process, method, system, product or equipment of column step or unit are not limited to listed step or unit, but optional
Ground further includes the steps that not listing or unit, or optionally further comprising intrinsic for these process, methods, product or equipment
Other step or units.
Referenced herein " embodiment " is it is meant that a particular feature, structure, or characteristic described can wrap in conjunction with the embodiments
Containing at least one embodiment of the present invention.Each position in the description occur the phrase might not each mean it is identical
Embodiment, nor the independent or alternative embodiment with other embodiments mutual exclusion.Those skilled in the art explicitly and
Implicitly understand, embodiment described herein can be combined with other embodiments.
Fig. 1 adds the theory structure schematic diagram of hydrogen production system for the synthesis of diesel oil, wax oil described in the embodiment of the present invention, refering to
Shown in Fig. 1, the diesel oil, wax oil synthesis add hydrogen production system to include that the raw material blending device 100, first successively installed is fed
Pump 200, hydrogenation reaction unit 300, prime processing unit (plant) 400 and rear class processing unit (plant) 500；The raw material blending device 100
For to catalytic diesel oil (catalytic cracking device comes, for the diesel product of catalytic cracking unit production), wax tailings (self-dalay
Coking plant production gasoline products), mixed diesel (from device for asphalt come diesel product and delayed coking unit come diesel oil
The mixture of product, catalytic diesel oil and wax tailings) and coker gasoline progress mixed processing；First feed pump 200 is used
In to mixed raw material progress pressure-increasing unit；For making, the mixed raw material carries out the hydrogenation reaction unit 300 plus hydrogen is anti-
It answers；The prime processing unit (plant) 400 and the rear class processing unit (plant) 500 are respectively used to carry out prime to the product of hydrogenation reaction
Separation processing separate processing with rear class, and successively to reaction product carry out prime separation and rear class separate with obtain add hydrogen wax oil with
Hydrogenated diesel oil.
Fig. 2 is the theory structure schematic diagram of raw material blending device 100 described in the embodiment of the present invention, as shown in fig.2, described
Raw material blending device 100 includes blending tank 101, the second feed pump 102 and the on-line mixing that at least two groups are used for mixed raw material
Device 103, the blending tank 101 and second feed pump 102 connection with the online mixer 103 respectively, it is described online
The output end of mixer 103 is connect with first feed pump 200, the feed(raw material)inlet of the blending tank 101 and the first charging
The entrance of pump 200 is provided with the on-line detector 104 for real-time detection raw material admixture；In embodiments of the present invention,
The setting parallel of at least two groups blending tank 101, provides the alternating hybrid process of multithreading, one group of blending tank 101 is held wherein
When row hybrid process operates, other blending tanks 101 can execute feeding or other operations, by alternately working, Ke Yiji
The quantity of the efficiency of big raising mixed process, the blending tank 101 is selected according to actual demand, for example, can for three groups,
Four groups etc., there is no restriction to this for the embodiment of the present invention；Catalytic diesel oil, wax tailings and mixed diesel are entered by pipeline respectively
Mixing in the blending tank 101；Since the coker gasoline density is small, readily volatilized, unevenness is mixed with diesel gas oil in storage tank
It is even, thus the embodiment of the present invention by second feed pump 102 be pressurized after be input in online mixer 103, with blending tank
The mixture exported in 101 further uniformly mixes, and the mixture can be made to be heated in the hydrogenation reaction unit 300 equal
It is even.
Fig. 3 is the theory structure schematic diagram of prime processing unit (plant) 400 described in the embodiment of the present invention, as shown in fig.3, described
Prime processing unit (plant) 400 includes First Heat Exchanger 401, the first water cooler 402, bottom product pump the 403, first stripper 404, tower
Bottom reboiler furnace feed pump 405, reboiler furnace 406, the first air cooler 407, the second water cooler 408, the first return tank of top of the tower 409 and
First tower top return pump 410；The First Heat Exchanger 401 respectively with the hydrogenation reaction unit 300, the first water cooler 402, tower
Bottom product pump 403 and the connection of the first stripper 404；First water cooler 402, tower bottom reboiler furnace feed pump 405, reboiler furnace
406 and rear class processing unit (plant) 500 be sequentially connected setting；403 connection of bottom product pump is arranged in first stripper
404 bottoms；First stripper 404, the first air cooler 407, the second water cooler 408, the first return tank of top of the tower 409 and
One tower top return pump 410 circuits sequentially connection；The product of hydrogenation reaction enters described by the hydrogenation reaction unit 300
It is heated to reaction temperature in one heat exchanger 401 and is delivered in the first stripper 404 to carry out raw material separation；The gas-liquid isolated is mixed
It closes object and successively enters the first return tank of top of the tower 409, the first air cooler 407 after the first air cooler 407 and the second water cooler 408
Air-cooled and water cooling is carried out to condense it to the gas-liquid mixture for being located at 404 tower top of the first stripper respectively with the second water cooler 408
In acid water (hydrogen sulfide containing water), isolate acid water in first return tank of top of the tower 409, first tower top returns
Stream tank 409 plays the purpose of settle and separate acid water and crude naphtha for storing tower top material；Remaining product passes through described
First tower top return pump 410 returns to 404 multi-cycle separation of the first stripper, if crude naphtha reaches expected quality, together
When crude naphtha isolated by first tower top return pump 410 before entering first stripper 404；First stripping
The reaction product isolated in tower 404 pass sequentially through bottom product pump 403, First Heat Exchanger 401, the first water cooler 402,
Tower bottom reboiler furnace feed pump 405, reboiler furnace 406 enter the rear class processing unit (plant) 500, wherein the tower bottom reboiler furnace into
Material pump 405 is heated for being pressurized to reaction product with being passed into the reboiler furnace 406, is led to after being heated to suitable temperature
Enter into the rear class processing unit (plant) 500.
Fig. 4 is the theory structure schematic diagram of rear class processing unit (plant) 500 described in the embodiment of the present invention, as shown in fig.4, described
Rear class processing unit (plant) 500 include main fractionating tower 501, the second air cooler 502, third water cooler 503, the second return tank of top of the tower 504,
Second tower top return pump 505, the second heat exchanger 506, middle section reflux pump 507, third tower top return pump 508, steam generator
509, the 4th water cooler 510, the second stripper 511 and the 4th tower top return pump 512；The main fractionating tower 501 respectively with institute
State prime processing unit (plant) 400, the second air cooler 502, the second tower top return pump 505, the second heat exchanger 506, middle section reflux pump
507, third tower top return pump 508 and the connection of the second stripper 511, wherein the main fractionating tower 501, the second air cooler
502, third water cooler 503, the second return tank of top of the tower 504, the second tower top return pump 505 circuit sequentially connection, the main fractionation
Tower 501, the second heat exchanger 506 and middle section reflux pump 507 circuit sequentially connection, the main fractionating tower 501, the second stripper
511 and the 4th tower top return pump 512 be sequentially connected, the main fractionating tower 501, third tower top return pump 508, steam generator
509 and the 4th water cooler 510 be sequentially connected；The reaction product that prime processing unit (plant) 400 completes the process enters the main fractionation
Tower 501 is fractionated, and passes through 507 recovery waste heat of second heat exchanger 506 and middle section reflux pump；The gas-liquid fractionated out is mixed
It closes object and successively carries out air-cooled and water cooling after the second air cooler 502 and third water cooler 503 into the second return tank of top of the tower
504, remaining product returns to 501 multi-cycle separation of main fractionating tower by second tower top return pump 505, while entering institute
Crude naphtha is isolated by second tower top return pump 505 before stating main fractionating tower 501；Hydrogenation reaction product passes through second
Stripper 511 is carried out product separation while hydrogenated diesel oil is separated and sent out using the 4th tower top return pump 512；After separation plus hydrogen
Reaction product gives deaerated water heat by the pressurization of third tower top return pump 508, steam generator 509, generates steam and takes heat away,
And it is isolated after 510 water cooling of the 4th water cooler and adds hydrogen wax oil.
Certainly, it should be noted that the embodiment of the present invention is not limited to using at the same time to diesel oil, wax oil simultaneous processing
Scene, In some embodiments of the present invention, diesel oil of the present invention, wax oil synthesis add hydrogen production system can also be only
Diesel product is carried out plus hydrogen produces, specifically：
By the reboiler furnace 406 in prime separator be adjusted to respectively with the first stripper 404, tower bottom reboiler furnace feed pump
405 circuit sequentially connection, and the first water cooler 402 is not connect with the tower bottom reboiler furnace feed pump 405, simultaneously close off rear class separation
Device 500, catalytic diesel oil directly pass through the first feed pump 200 and enter the progress hydrogenation reaction of hydrogenation reaction unit 300, add hydrogen anti-
The product answered is entered by the hydrogenation reaction unit 300 to be heated to reaction temperature in the First Heat Exchanger 401 and conveys
Raw material separation is carried out in the first stripper 404；The gas-liquid mixture isolated successively passes through the first air cooler 407 and the second water
Enter the first return tank of top of the tower 409 after cooler 408, the first air cooler 407 and the second water cooler 408 are respectively to positioned at the first stripping
The gas-liquid mixture of 404 tower top of tower carries out air-cooled and water cooling to condense acid water therein (hydrogen sulfide containing water), described the
Acid water is isolated in one return tank of top of the tower 409, first return tank of top of the tower 409 plays quiet for storing tower top material
Set the purpose of separation acid water and crude naphtha；Remaining product returns to first vapour by first tower top return pump 410
404 multi-cycle separation of stripper leads to before entering first stripper 404 simultaneously if crude naphtha reaches expected quality
It crosses first tower top return pump 410 and isolates crude naphtha, wherein the tower bottom reboiler furnace feed pump 405 is used for reaction
Product booster is heated with being passed into the reboiler furnace 406, and first stripping is passed into after being heated to suitable temperature
In tower 404；The reaction product isolated in first stripper 404 passes sequentially through the bottom product and pumps 403, First Heat Exchanger
401, the first water cooler 402 isolates hydrogenated diesel oil；According to market situation, production system can be adjusted flexibly in the embodiment of the present invention
Processing technology, the micro-adjustment of adaptability is carried out to the connection relationships of the various components in prime separator 400, selection is independent
Process diesel oil or simultaneous processing diesel oil and wax oil.
In embodiments of the present invention, the diesel oil, wax oil synthesis add hydrogen production system by on-line analysis it is mixed
Raw material components especially make total aromatic hydrocarbons and monocycle, the accounting of double ring arene near reasonable value, ensure that charging is stablized, pass through
Raw material blending device 100 carries out mixed processing, the first charging to catalytic diesel oil, wax tailings, mixed diesel and coker gasoline
Pump 200 pairs mixing raw material carry out pressure-increasing units to hydrogenation reaction units 300 carry out hydrogenation reaction, prime processing unit (plant) 400 with
And rear class processing unit (plant) 500 is respectively used to carry out the product of hydrogenation reaction prime separation processing and rear class separation processing, and according to
It is secondary that hydrogen wax oil and hydrogenated diesel oil are added to obtain to reaction product progress prime separation and rear class separation, correspondingly, guaranteeing to add hydrogen
While the yield of product, can processing catalytic diesel oil as much as possible, that is, carry out plus hydrogen production when, first determine need plus
The catalytic diesel oil processing capacity of work, then further according to specific ingredient, to determine other components (such as mixed diesel, wax tailings etc.)
Processing capacity, compared to existing diesel oil hydrogenation produce, the embodiment of the present invention can be with simultaneous processing diesel oil and wax oil and anti-
Corresponding lock out operation should be carried out after the completion, according to market situation, the processing technology of production system can be adjusted flexibly, selection is single
Solely processing diesel oil or simultaneous processing diesel oil and wax oil, cost are lower than single processing diesel oil and wax oil respectively, have preferably warp
Ji benefit, meanwhile, it when raw material composition changes, does not need to adjust process conditions, only needs strict control mixed raw material crucial
The accounting of component, is precisely controlled, and still ensures that qualified product, ensures total aromatic hydrocarbons and monocycle, double by on-line checking analysis
The accounting of cycloaromatics can process catalytic diesel oil near reasonable value with maximum, while can guarantee that hydrogenated diesel oil product quality reaches
To state five, six diesel oil standard of state, especially Cetane number total energy is qualified, operating condition can be adjusted flexibly, adaptability to raw material is strong, according to upper
Device product situation is swum, can be used as diesel oil hydrogenation modification device or diesel oil, wax oil hydrogenation modifying apparatus, is guaranteeing key component
In the case where accounting, it can be ensured that the poor catalytic diesel oil raw material of processing as much as possible has preferable applicability.
On the basis of the above embodiments, Fig. 5 is the synthesis Hydrogenation production method of diesel oil described in the embodiment of the present invention, wax oil
Flow diagram, as shown in fig.5, the synthesis Hydrogenation production method of the diesel oil, wax oil be applied to above-mentioned any embodiment
The synthesis of the diesel oil, wax oil adds hydrogen production system, specifically comprises the following steps：
S101：Catalytic diesel oil, wax tailings, mixed diesel are each led into blending tank and mixed；
S102：And be input in online mixer after being pressurized coker gasoline by second feed pump, and it mixes
The mixture exported in tank further mixes；
S103：Mixed raw material carries out hydrogenation reaction by the first feed pump pressure-increasing unit to hydrogenation reaction unit；
S104：Prime separation processing and rear class separation processing are carried out to the product of hydrogenation reaction respectively, and successively to reaction
Product carries out prime separation and is separated with rear class to obtain and add hydrogen wax oil and hydrogenated diesel oil.
Wherein, the method also includes：It is respectively provided in the feed(raw material)inlet of the blending tank and the entrance of the first feed pump
On-line detector for real-time detection raw material admixture.
The prime separation, which is processed, is specially：The product of hydrogenation reaction enters first by the hydrogenation reaction unit and changes
It is heated to reaction temperature in hot device and is delivered in the first stripper to carry out raw material separation；The gas-liquid mixture isolated successively passes through
Enter the first return tank of top of the tower after crossing the first air cooler and the second water cooler, isolates acidity in first return tank of top of the tower
Water, remaining product is pumped back to the first stripper multi-cycle separation by the first overhead reflux, while entering first vapour
Crude naphtha is isolated before stripper；The reaction product isolated in first stripper passes sequentially through bottom product pump, first changes
Hot device, the first water cooler, tower bottom reboiler furnace feed pump, reboiler furnace enter rear class processing unit (plant) and carry out rear class separation processing.
The second-order separation is processed：The reaction product that prime separation completes the process enters main fractionating tower and is divided
It evaporates, and passes through the second heat exchanger and middle section reflux pump recovery waste heat；It is air-cooled that the gas-liquid mixture fractionated out successively passes through second
Enter the second return tank of top of the tower after device and third water cooler, remaining product is pumped back to the main fractionating tower by the second overhead reflux
Multi-cycle separation, while crude naphtha is isolated before entering the main fractionating tower；And pass through third overhead reflux respectively
Pump, steam generator and the 4th water cooler, which are isolated, adds hydrogen wax oil and by the second stripper and the 4th tower top return pump point
Separate out hydrogenated diesel oil.
Diesel oil described in the embodiment of the present invention, wax oil synthesis Hydrogenation production method can through the foregoing embodiment provided by
Diesel oil, wax oil synthesis add hydrogen production system execute, the diesel oil, wax oil synthesis Hydrogenation production method have above-described embodiment
The diesel oil, wax oil synthesis add the corresponding functional component of hydrogen production system and beneficial effect, referring specifically to above-mentioned diesel oil,
The synthesis of wax oil adds the embodiment of hydrogen production system, and details are not described herein for the embodiment of the present invention.
In above-described embodiment provided by the present invention, it should be understood that disclosed system and method can pass through it
Its mode is realized.For example, system embodiment described above is only schematical, for example, the division of the component, only
Only a kind of logical function partition, there may be another division manner in actual implementation, for example, multiple components can combine or
It is desirably integrated into another system, or some features can be ignored or not executed.
The module or component as illustrated by the separation member may or may not be physically separated, as
The component that module or component is shown may or may not be physical module, both can be located in one place, or can also
To be distributed over a plurality of network elements.Some or all of the modules therein or component can be selected according to the actual needs real
The purpose of existing this embodiment scheme.
The above is only the embodiment of the present invention, are not intended to limit the scope of the patents of the invention, although with reference to the foregoing embodiments
Invention is explained in detail, still can be to aforementioned each specific reality for coming for those skilled in the art
It applies technical solution documented by mode to modify, or equivalence replacement is carried out to part of technical characteristic.It is all to utilize this
The equivalent structure that description of the invention and accompanying drawing content are done directly or indirectly is used in other related technical areas, similarly
Within the invention patent protection scope.
Claims (9)
1. the synthesis of a kind of diesel oil, wax oil adds hydrogen production system, which is characterized in that including successively install raw material blending device,
First feed pump, hydrogenation reaction unit, prime processing unit (plant) and rear class processing unit (plant)；
Raw material blending device, for carrying out mixed processing to catalytic diesel oil, wax tailings, mixed diesel and coker gasoline；
First feed pump, for carrying out pressure-increasing unit to mixed raw material；
Hydrogenation reaction unit, for making the mixed raw material carry out hydrogenation reaction；
Prime processing unit (plant) and rear class processing unit (plant) are respectively used to carry out the product of hydrogenation reaction prime separation processing with after
Grade separation processing, and prime separation and rear class separation successively are carried out to obtain plus hydrogen wax oil and hydrogenated diesel oil to reaction product.
2. the synthesis of diesel oil according to claim 1, wax oil adds hydrogen production system, it is characterised in that：The raw material mixing
Device includes blending tank, the second feed pump and the online mixer that at least two groups are used for mixed raw material, the blending tank and institute
State connection of second feed pump respectively with the online mixer, the output end of the online mixer and first feed pump
Connection；At least two groups blending tank is arranged parallel, provides the alternating hybrid process of multithreading, catalytic diesel oil, wax tailings with
And mixed diesel passes through pipeline into the mixing in-tank mixing respectively；The coker gasoline is pressurized by second feed pump
After be input in online mixer, further mixed with the mixture exported in blending tank.
3. the synthesis of diesel oil according to claim 2, wax oil adds hydrogen production system, it is characterised in that：The blending tank
The entrance of feed(raw material)inlet and the first feed pump is provided with the on-line detector for real-time detection raw material admixture.
4. the synthesis of diesel oil according to claim 1, wax oil adds hydrogen production system, it is characterised in that：The prime processing
Device include First Heat Exchanger, the first water cooler, bottom product pump, the first stripper, tower bottom reboiler furnace feed pump, reboiler furnace,
First air cooler, the second water cooler, the first return tank of top of the tower and the first tower top return pump；The First Heat Exchanger respectively with institute
State hydrogenation reaction unit, the first water cooler, bottom product pump and the connection of the first stripper；First water cooler, tower bottom weight
Boiling stove feed pump, reboiler furnace and rear class processing unit (plant) are sequentially connected setting；Bottom product pump connection setting is described the
One stripper bottom；First stripper, the first air cooler, the second water cooler, the first return tank of top of the tower and the first tower top
Reflux pump circuits sequentially connection；The product of hydrogenation reaction is entered in the First Heat Exchanger by the hydrogenation reaction unit to be added
Heat is to reaction temperature and is delivered to progress raw material separation in the first stripper；The gas-liquid mixture isolated successively passes through the first sky
Enter the first return tank of top of the tower after cooler and the second water cooler, isolates acid water in first return tank of top of the tower, it is remaining
Product is pumped back to the first stripper multi-cycle separation by first overhead reflux, while entering first stripper
Crude naphtha is isolated before；The reaction product isolated in first stripper passes sequentially through bottom product pump, first changes
Hot device, the first water cooler, tower bottom reboiler furnace feed pump, reboiler furnace enter the rear class processing unit (plant).
5. the synthesis of diesel oil according to claim 1, wax oil adds hydrogen production system, it is characterised in that：The rear class processing
Device includes main fractionating tower, the second air cooler, third water cooler, the second return tank of top of the tower, the second tower top return pump, the second heat exchange
Device, middle section reflux pump, third tower top return pump, steam generator, the 4th water cooler, the second stripper and the 4th overhead reflux
Pump；The main fractionating tower respectively with the prime processing unit (plant), the second air cooler, the second tower top return pump, the second heat exchanger, in
Section reflux pump, third tower top return pump and the connection of the second stripper, wherein the main fractionating tower, the second air cooler, third water
Cooler, the second return tank of top of the tower, the second tower top return pump circuit sequentially connection, the main fractionating tower, the second heat exchanger and in
Section reflux pump circuits sequentially connection, and the main fractionating tower, the second stripper and the 4th tower top return pump are sequentially connected, the master
Fractionating column, third tower top return pump, steam generator and the 4th water cooler are sequentially connected；Prime processing unit (plant) completes the process
Reaction product enters the main fractionating tower and is fractionated, and passes through second heat exchanger and middle section reflux pump recovery waste heat；
The gas-liquid mixture fractionated out successively enters the second return tank of top of the tower, remaining product after the second air cooler and third water cooler
It is pumped back to the main fractionating tower multi-cycle separation by second overhead reflux, while being separated before entering the main fractionating tower
Crude naphtha out；And it is isolated by third tower top return pump, steam generator and the 4th water cooler add hydrogen wax oil respectively
And hydrogenated diesel oil is isolated by the second stripper and the 4th tower top return pump.
6. the synthesis Hydrogenation production method of a kind of diesel oil, wax oil, be applied to the described in any item diesel oil of the claims 1-5,
The synthesis of wax oil adds hydrogen production system, which is characterized in that includes the following steps：
Catalytic diesel oil, wax tailings, mixed diesel are each led into blending tank and mixed；
And be input in online mixer after being pressurized coker gasoline by second feed pump, and it is exported in blending tank
Mixture further mixes；
Mixed raw material carries out hydrogenation reaction by the first feed pump pressure-increasing unit to hydrogenation reaction unit；
Prime separation processing and rear class separation processing are carried out to the product of hydrogenation reaction respectively, and before successively carrying out to reaction product
Grade separation is separated with rear class to obtain and add hydrogen wax oil and hydrogenated diesel oil.
7. the synthesis Hydrogenation production method of diesel oil according to claim 6, wax oil, which is characterized in that the method is also wrapped
It includes：It is respectively provided in the feed(raw material)inlet of the blending tank and the entrance of the first feed pump for real-time detection raw material admixture
On-line detector.
8. the synthesis Hydrogenation production method of diesel oil according to claim 6, wax oil, which is characterized in that the prime separation
Processing is specially：
The product of hydrogenation reaction is entered in First Heat Exchanger by the hydrogenation reaction unit to be heated to reaction temperature and conveys
Raw material separation is carried out in the first stripper；The gas-liquid mixture isolated is successively after the first air cooler and the second water cooler
Into the first return tank of top of the tower, acid water is isolated in first return tank of top of the tower, remaining product is returned by the first tower top
Stream is pumped back to the first stripper multi-cycle separation, while isolating crude naphtha before entering first stripper；The
The reaction product isolated in one stripper passes sequentially through bottom product pump, First Heat Exchanger, the first water cooler, tower bottom reboiler furnace
Feed pump, reboiler furnace enter rear class processing unit (plant) and carry out rear class separation processing.
9. the synthesis Hydrogenation production method of diesel oil according to claim 6, wax oil, which is characterized in that the second-order separation
Processing is specially：
The reaction product that prime separation completes the process enters main fractionating tower and is fractionated, and is returned by the second heat exchanger and middle section
Stream pump recovery waste heat；The gas-liquid mixture fractionated out successively enters the second tower top after the second air cooler and third water cooler and returns
Tank is flowed, remaining product is pumped back to the main fractionating tower multi-cycle separation by the second overhead reflux, while entering the main fractionation
Crude naphtha is isolated before tower；And pass through third tower top return pump, steam generator and the separation of the 4th water cooler respectively
Out plus hydrogen wax oil and hydrogenated diesel oil is isolated by the second stripper and the 4th tower top return pump.
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Application publication date: 20181123 |