CN106008139B - A kind of coking crude benzene adds hydrogen recovery unit - Google Patents
A kind of coking crude benzene adds hydrogen recovery unit Download PDFInfo
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- CN106008139B CN106008139B CN201610343430.2A CN201610343430A CN106008139B CN 106008139 B CN106008139 B CN 106008139B CN 201610343430 A CN201610343430 A CN 201610343430A CN 106008139 B CN106008139 B CN 106008139B
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- C07C7/005—Processes comprising at least two steps in series
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Abstract
The present invention relates to a kind of coking crude benzenes to add hydrogen recovery unit, belong to chemical mechanical equipment technical field, including pretreatment unit, the pretreatment unit pipeline connects prefractionator, the prefractionator top side pipeline connects the first heat-exchange device, fractionating column is scanned in the connection of bottom side pipeline, the first heat-exchange device pipeline connects the first surge tank, and side is equipped with the first vacuum evacuation device, distinguish pipeline and connect the prefractionator top and one middle side part of extraction tower in first surge tank side, and pipeline is gone back between them and is connected with first flow regulating valve, one end pipeline connects the second heat-exchange device at the top of the extraction tower, the second heat-exchange device pipeline connects the second surge tank, the second surge tank pipeline connects the extraction tower top side and non-aromatics storage tank, technological effect is good, resource utilization is high maximum Limit reduces the content of light component in heavy benzol, while heavy benzol content is low in the light component recycled.
Description
Technical field
The present invention relates to a kind of coking crude benzenes to add hydrogen recovery unit, belongs to chemical mechanical equipment technical field.
Background technique
Benzene is important one of industrial chemicals, can be used for the fields such as synthetic resin, medicine, explosive, also can be used as organic molten
Agent uses, and the production technology level and yield of benzene are one of the marks for measuring a national chemical industry development level, faces and melts coking stock
Part company's refining benzene workshop possesses the hydrogenation plant of a set of 80,000 tons/year of crude benzol amount of processing, crude benzole hydrogenation device use coking crude benzene for
Raw material, crude benzol is by C4-C10+The impurity components composition such as rich aromatic hydrocarbons, sulfur-containing compound, nitrogenous compound, olefine and alkadienes,
It is the current important channel for obtaining purified petroleum benzin, usually by C9+Fraction is known as heavy benzol, they are in catalytic hydrogenation because polymerizeing
Reaction understands the aging of accelerator activator and increases the reaction conditions such as the temperature of reactor, pressure, needs before entering the reactor
By heavy benzol ends removal, but in course of normal operation, still containing part lighter component, C in the heavy benzol that is removed6-C8Fragrance
Hydrocarbon and these lighter components of styrene are sent into heavy benzol products pot, if simple raising fractionation column bottom temperature by as heavy benzol product
Degree, part C9+Component can be evaporated into reactor, thus the aging of accelerating reactor, the easy coking of crude benzole hydrogenation under high temperature,
How to guarantee to remove impurity under low temperature as far as possible, reduce light product amount in heavy benzol, design it is a kind of effective improve product quality,
Guarantee that the crude benzene recovery device of production capacity and separating effect is very necessary.
Summary of the invention
The technical problem to be solved in the present invention overcomes existing defect, provides a kind of coking crude benzene and adds hydrogen recovery unit, leads to
Over-sampling detection unit acquires data, is submitted to control unit, control unit be automatically adjusted to setting it is pre- evaporate tower column bottom temperature,
Tower top temperature, the parameters such as vacuum degree, the overhead reflux amount of tower, so that the lighter component in heavy benzol is extracted as far as possible, and
It is preferably minimized in the lighter component being extracted containing heavy component, by prefractionation and rectifying, separates each component, by sweeping
Choosing fractionation, recycles useful constituent in heavy constituent, good separating effect, impurity content is low, effectively prevent follow-up hydrogenation process
The reactor aging being likely to occur reduces reactor volume severity, and control precision is high, and temperature and pressure and other parameters can accomplish certainly
Dynamic to adjust, apparatus structure is reasonable.
In order to solve the above-mentioned technical problems, the present invention provides the following technical solutions:
A kind of coking crude benzene adds hydrogen recovery unit, including pretreatment unit, and the pretreatment unit pipeline connects prefractionation
Tower, the prefractionator top side pipeline connect the first heat-exchange device, and fractionating column is scanned in the connection of bottom side pipeline, described
First heat-exchange device pipeline connects the first surge tank, and side is equipped with the first vacuum evacuation device, first surge tank side
Pipeline connects the prefractionator top entry and one middle side part of extraction tower respectively, and gone back between them pipeline be connected with it is first-class
Adjustable valve, extraction tower top one end pipeline connect the second heat-exchange device, the second heat-exchange device pipeline connection
Second surge tank, the second surge tank pipeline connect the extraction tower top side and non-aromatics storage tank, and between them
Also pipeline is connected with second flow regulating valve, and the extraction tower bottom pipe connects one middle side part of extractant recovery tower, the extraction
Agent recovery tower top side pipeline is taken to connect condenser, the condenser tubes connect third surge tank, and side is equipped with second
Vacuum evacuation device, the third surge tank pipeline connect the extractant recovery tower top side and one middle side part of rectifying column, and
Pipeline is gone back between them and is connected with third flow control valve, and the extractant recovery tower bottom pipe connects the extracting tower top
Portion, the rectifying column top duct connects third heat-exchange device, and a side ducts connect toluene storage tank, and the third heat is handed over
Changing device pipeline connects the 4th surge tank, the 4th surge tank pipeline connection rectifying column top side and benzene storage tank, and it
Between go back pipeline and be connected with the 4th flow control valve, the rectifier bottoms pipeline connects dimethylbenzene storage tank.
Furthermore, described to scan fractionating column top side pipeline connection condensing unit, the condensing unit pipeline connects
The dimethylbenzene surge tank is connect, the dimethylbenzene surge tank pipeline connection is scanned at the top of fractionating column and dimethylbenzene storage tank, and it
Between go back pipeline and be connected with the 5th flow control valve, it is described to scan fractionation column base pipeline connection heavy benzol recycling can and described
It scans and is additionally provided with buffer pool between fractionating column and the prefractionator.
Furthermore, between first vacuum evacuation device and the prefractionator, second vacuum evacuation device with
Pressure gauge is equipped between the extractant recovery tower, the prefractionator, extraction tower, scans fractionating column at extractant recovery tower
It is respectively equipped with temperature sensor and heating device with rectifying column intracavity bottom, and inner cavity top also is provided with the temperature sensor,
The heating device is separately connected first heat-exchange device, the second heat-exchange device and third heat-exchange device, the temperature
It spends sensor, the-vacuum evacuation device, the-five flow control valve and heating device and is electrically connected control unit, described control unit
Interior includes main control computer, and described control unit is electrically connected sample detecting unit, and sample detecting unit acquires per hour
Above-mentioned surge tank and sample data in storage tank are primary.
Furthermore, filter device is equipped in the pretreatment unit, filter device pipeline connects agitating device, described
Agitating device pipeline connects oil pump, and transmission mechanism is equipped in the agitating device, and the transmission mechanism side is equipped with feed inlet, separately
Side is equipped with overflow mechanism, and the agitating device intracavity bottom is equipped with annular-type plate.
Furthermore, the prefractionator intracavity bottom temperature is adjusted through control unit, is slowly improved by 175 DEG C, often
0.5 DEG C is increased, then stablizes 8 hours, while improving the vacuum degree of tower, increases overhead reflux, is not more than charging reflux ratio
0.4, control tower top temperature is not more than in 72 DEG C.
Furthermore, solvent/charge ratio of the extraction tower is 3.3:1.wt/wt, selects low dissolving power solvent, described
The FIC206 and lower part FIC208 solvent feed ratio of extraction tower upper pipe connection are 4:1.1.wt/wt, the rectifying tower bottom
For the temperature difference less than 4 DEG C, phegma/Produced Liquid is 2:1.wt/ in 155-158 DEG C, 116-118 DEG C of tower top temperature, tower for temperature control
wt。
The invention has the advantages that: adjust to evaporate tower column bottom temperature, the vacuum degree of tower, overhead reflux amount etc. in advance by control centre
Parameter makes to extract the lighter component in heavy benzol as far as possible, and to be mentioned in prefractionator in setting reaction condition
It is preferably minimized in the lighter component taken containing heavy component, by prefractionation and rectifying, separates each component, by scanning point
It evaporates, recycles useful constituent in heavy constituent, good separating effect, impurity content is low, effectively prevent follow-up hydrogenation process may
The reactor aging of appearance reduces reactor volume severity, and control precision is high, and temperature can accomplish to adjust automatically with pressure and other parameters
Section, waste heat obtain effective recycling, and apparatus structure is reasonable, since October is using the present apparatus, Lin Huan coking joint-stock company
Ethylo benzene in the heavy benzol of refining benzene workshop is reduced to 9% or so by original 15% or so to meta-xylene, adjacent meta-xylene content.
Detailed description of the invention
Attached drawing is used to provide further understanding of the present invention, and constitutes part of specification, with reality of the invention
It applies example to be used to explain the present invention together, not be construed as limiting the invention.
Fig. 1 is structure of the invention flow chart.
Fig. 2 is circuit controling drawing of the present invention.
Fig. 3 is agitating device structure chart of the present invention.
Fig. 4 is the present invention in Lin Huan coking joint-stock company's refining benzene workshop pilot experiment report screenshot.
Fig. 5 is the present invention in Lin Huan coking joint-stock company's refining benzene workshop pilot experiment heavy benzol yield tendency chart.
Figure label: 1, pretreatment unit；2, prefractionator；3, the first heat-exchange device；4, fractionating column is scanned；5, first
Surge tank；6, the first vacuum evacuation device；7, prefractionator top entry；8, extraction tower；9, first flow regulating valve；10, second
Heat-exchange device；11, the second surge tank；12, non-aromatics storage tank；13, second flow regulating valve；14, extractant recovery tower；
15, condenser, 16, third surge tank；17, the second vacuum evacuation device；18, rectifying column；19, third flow control valve；20, third
Heat-exchange device；21, toluene holding vessel；22, the 4th surge tank；23, benzene holding vessel；；24, the 4th flow control valve；25, diformazan
Benzene holding vessel；26, condensing unit；27, dimethylbenzene surge tank；28, the 5th flow control valve；29, heavy benzol recycling can；30, it buffers
Pond；31, pressure gauge；32 temperature sensors；33, heating device；34, filter device；35, agitating device；36, oil pump；37, it controls
Unit；38, sample detecting unit；39 feed inlets；40, transmission mechanism；41, overflow mechanism；42, annular-type plate.
Specific embodiment
Hereinafter, preferred embodiments of the present invention will be described with reference to the accompanying drawings, it should be understood that preferred reality described herein
Apply example only for the purpose of illustrating and explaining the present invention and is not intended to limit the present invention.
As Figure 1-Figure 5, a kind of coking crude benzene adds hydrogen recovery unit, including pretreatment unit 1, the pretreatment unit
1 pipeline connects prefractionator 2, and the 2 top side pipeline of prefractionator connects the first heat-exchange device 3, bottom side pipeline
Fractionating column 4 is scanned in connection, and 3 pipeline of the first heat-exchange device connects the first surge tank 5, and side is equipped with the first vacuum means
6 are set, 5 side of the first surge tank difference pipeline connects the prefractionator top entry 7 and 8 one middle side part of extraction tower, and
Pipeline is gone back between them and is connected with first flow regulating valve 9, and 8 top one end pipeline of extraction tower connects the second heat-exchange device
10,10 pipeline of the second heat-exchange device connects the second surge tank 11, and the second surge tank pipe 11 connects the extracting
8 top side of tower and non-aromatics storage tank 12, and go back pipeline between them and be connected with second flow regulating valve 13, the extraction tower
8 bottom pipes connect 14 1 middle side part of extractant recovery tower, and the 14 top side pipeline of extractant recovery tower connects condenser
15,15 pipeline of condenser connects third surge tank 16, and side is equipped with the second vacuum evacuation device 17, the third surge tank
16 pipelines connect 14 top side of extractant recovery tower and 18 1 middle side part of rectifying column, and go back pipeline between them and be connected with
Third flow control valve 19,14 bottom pipe of extractant recovery tower connect 8 top of extraction tower, and the rectifying column 18 pushes up
Portion's pipeline connects third heat-exchange device 20, and a side ducts connect toluene storage tank 21, and the third heat-exchange device 20 is managed
Road connects the 4th surge tank 22,22 pipeline of the 4th surge tank connection 18 top side of rectifying column and benzene storage tank 23, and it
Between go back pipeline and be connected with the 4th flow control valve 24,18 bottom pipe of rectifying column connects dimethylbenzene storage tank 25.
More specifically, described to scan 4 top side pipeline of fractionating column connection condensing unit 26, the condensing unit 26 is managed
Road connects the dimethylbenzene surge tank 27, and 27 pipeline of the dimethylbenzene surge tank connection is scanned 4 top of fractionating column and deposited with dimethylbenzene
Storage tank 25, and go back pipeline between them and be connected with the 5th flow control valve 28, it is described to scan 4 bottom pipe of fractionating column connection heavy benzol
Recycling can 29, and described scan is additionally provided with buffer pool 30 between fractionating column 4 and the prefractionator 2, by scanning, make in heavy benzol
Part aromatic hydrocarbons further recycled, reduce heavy benzol in light component content.
More specifically, between first vacuum evacuation device 6 and the prefractionator 2, second vacuum evacuation device
Pressure gauge 31, the prefractionator 2, extractant recovery tower 14, extraction tower are equipped between 17 and the extractant recovery tower 14
8, it scans fractionating column 4 and 18 intracavity bottom of rectifying column is respectively equipped with temperature sensor 32 and heating device 33, and inner cavity top
Equipped with the temperature sensor 32, the heating device 33 is separately connected first heat-exchange device 3, the second heat-exchange device
10 with third heat-exchange device 19, the temperature sensor 32,1-2 vacuum evacuation device, five flow control valve of 1-5 and heating
Device 33 is electrically connected control unit 37, includes main control computer in described control unit 37, and described control unit 37 is electrically
Sample detecting unit 38 is connected, and sample detecting unit 38 acquires above-mentioned surge tank per hour and sample data in storage tank is primary,
It using the temperature, pressure and analysis data of acquisition, is carried out by main control computer analysis integrated, issues an instruction to adjust regurgitant volume
It with the operation of vacuum evacuation device, not only adjusts rapidly, and control ratio of precision is manually high, equipment is made to be constantly in best production item
Part.
More specifically, it is equipped with filter device 34 in the pretreatment unit 1,34 pipeline of filter device connects agitating device
35,35 pipeline of agitating device connects oil pump 36, is equipped with transmission mechanism 40, the transmission mechanism 40 in the agitating device 35
Side is equipped with feed inlet 39, and the other side is equipped with overflow mechanism 41, and 35 intracavity bottom of agitating device is equipped with annular-type plate 42,
Filtering helps to remove the solid impurity in crude benzol, facilitates the separation of subsequent fractionation operation, and annular-type plate mainly changes
Liquid flow direction makes each component in transmission mechanism operating, and crude benzol mixes more evenly, and overflow mechanism can work as a buffer, recycling
Receiving portions overflow.
More specifically, the 2 intracavity bottom temperature of prefractionator is adjusted through control unit, is slowly improved by 175 DEG C, often
0.5 DEG C is increased, then stablizes 8 hours, while improving the vacuum degree of tower, increases overhead reflux, is not more than charging reflux ratio
0.4, control tower top temperature is 3.3:1.wt/wt no more than the solvent/charge ratio in 72 DEG C, controlling the extraction tower 8, is selected low
Dissolving power solvent makes the aromatic enrichment end of extraction tower keep enough selectivity, uniformly heats up, and kept for a period of time, can prevent
Only other boiling point components are distillated because of localized hyperthermia, cause distillate impure.
More specifically, the FIC206 and lower part FIC208 solvent feed ratio of 8 upper pipe of the extraction tower connection are 4:
1.1.wt/wt, 18 column bottom temperature of rectifying column control in 155-158 DEG C, 116-118 DEG C of tower top temperature, tower the temperature difference less than 4
DEG C, phegma/Produced Liquid is 2:1.wt/wt, adjusts tower top temperature by control regurgitant volume, it is ensured that rectifying processing temperature is kept
It is constant, and it is in optimum state, rectifying separating effect is more preferable, obtains more ideal creation data.
Working principle of the present invention: crude benzol raw material first passes through filtering and impurity removing, mixes by agitating device 35, with oil pump 36 from stirring
The extraction of 35 bottom of device is mixed, prefractionator 2 is sent into, temperature sensor 32 and pressure gauge in fractionating column are received by control unit 37
31 data automatically adjust the work of the first vacuum evacuation device 6 and the shunting operation of first flow regulating valve 9, adjust regurgitant volume
With vacuum degree in tower, and then change 2 tower top temperature of prefractionator and tower pressure interior force, overhead product passes through first flow regulating valve 9
8 middle part of extraction tower is branched to, 8 overhead product of extraction tower recycles heat by the second heat-exchange device 10, then passes through second
Adjustable valve 13, for controlling 8 head temperature of extraction tower, another part is directly recovered as non-aromatic hydrocarbon product for a part reflux, takes out
8 tower bottom product of stripper flows into the middle part of extractant recovery tower 14, and after tower bottom heating, top product is after condenser condenses, stream
Through third flow control valve 19, a part is back to 14 top of extractant recovery tower, and another part flows into the middle part of rectifying column 18,
14 tower bottom product of extractant recovery tower is sent to 8 top of extraction tower, is recycled, the second vacuum evacuation device 17 is made in control unit 37
Operation is vacuumized to extraction tower 8 with lower, the heavy benzol that 2 bottom of prefractionator generates, which enters, scans 4 middle part of fractionating column, scans fractionating column
4 tops generate dimethylbenzene, and 18 top product of rectifying column recycles heat by third heat-exchange device 20, adjust by the 4th flow
The shunting of valve 24, part flow into 18 top of rectifying column, and to adjust tower top temperature, part, which is flowed out, is used as benzaldehyde product, in rectifying column 18
Between effluent as toluene product, bottom product outflow is used as dimethylbenzene, and fractionating column 4 is scanned in the inflow of 2 bottom product of prefractionator
Middle part is fractionated, and top product partial reflux, which enters, to be scanned at the top of fractionating column, to control tower top temperature, is partially used as diformazan
Benzaldehyde product, tower bottom product outflow are used as heavy benzol, and the heat of recycling can directly be used for each tower tower bottom heating together with heating device
It uses, uninterruptedly chemically examines finished product detection, data are sent to control unit 37, as foundation is adjusted, scan fractionation into crossing, weight
Light component content is lower in benzene, is flowed back by adjusting, and guarantees that tower top is in best cut point, extractant recovery tower 14 realizes
Extractant recycles, and has saved extractant consumption, prefractionation and rectifying operation, has separated light component, the present apparatus
Rectifying operating efficiency is substantially increased, high degree of automation, good separating effect, extractant consumption is low, and it is convenient to control to adjust, heat
Utilization rate is high, by from October last year since Lin Huan coking joint-stock company's refining benzene workshop use, ethylo benzene in heavy benzol, pair between two
Toluene, adjacent meta-xylene content are reduced to 9% or so by original 15% or so, more than 200 ten thousand yuan of extra earning of year.
The above are the preferable embodiments of the present invention, and those skilled in the art in the invention can also be to above-mentioned embodiment party
Formula is changed and is modified, and therefore, the invention is not limited to above-mentioned specific embodiment, all those skilled in the art exist
Made any conspicuous improvement, replacement or modification all belong to the scope of protection of the present invention on the basis of the present invention.
Claims (6)
1. a kind of coking crude benzene adds hydrogen recovery unit, including pretreatment unit (1), which is characterized in that the pretreatment unit (1)
Pipeline connects prefractionator (2), and prefractionator (2) the top side pipeline connects the first heat-exchange device (3), bottom side
Pipeline connection is scanned fractionating column (4), and the first heat-exchange device (3) pipeline connects the first surge tank (5), and side is equipped with the
One vacuum evacuation device (6), the first surge tank (5) side difference pipeline connect the prefractionator top entry (7) and take out
(8) one middle side part of stripper, and go back pipeline between them and be connected with first flow regulating valve (9), one end at the top of the extraction tower (8)
Pipeline connects the second heat-exchange device (10), and the second heat-exchange device (10) pipeline connects the second surge tank (11), described
Second surge tank pipe (11) road connects extraction tower (8) top side and non-aromatics storage tank (12), and also manages between them
Road is connected with second flow regulating valve (13), and extraction tower (8) bottom pipe connects (14) one middle side part of extractant recovery tower,
Extractant recovery tower (14) the top side pipeline connects condenser (15), condenser (15) the pipeline connection third buffering
Tank (16), and side is equipped with the second vacuum evacuation device (17), third surge tank (16) pipeline connects the extractant recycling
Tower (14) top side and (18) one middle side part of rectifying column, and go back pipeline between them and be connected with third flow control valve (19),
Extractant recovery tower (14) bottom pipe connects at the top of the extraction tower (8), rectifying column (18) the top duct connection
Third heat-exchange device (20), and side ducts connection toluene storage tank (21), third heat-exchange device (20) pipeline connect
The 4th surge tank (22) is connect, the 4th surge tank (22) pipeline connects rectifying column (18) top side and benzene storage tank (23),
And pipeline is gone back between them and is connected with the 4th flow control valve (24), rectifying column (18) the bottom pipe connection dimethylbenzene storage
Tank (25).
2. a kind of coking crude benzene adds hydrogen recovery unit according to claim 1, it is characterised in that: described to scan fractionating column (4)
Top side pipeline connects condensing unit (26), and condensing unit (26) pipeline connects the dimethylbenzene surge tank (27), institute
It states the connection of dimethylbenzene surge tank (27) pipeline and scans fractionating column (4) top and dimethylbenzene storage tank (25), and also managed between them
Road is connected with the 5th flow control valve (28), described to scan fractionating column (4) bottom pipe connection heavy benzol recycling can (29) and described
It scans and is additionally provided with buffer pool (30) between fractionating column (4) and the prefractionator (2).
3. a kind of coking crude benzene adds hydrogen recovery unit according to claim 1, it is characterised in that: first vacuum evacuation device
(6) it is all provided between the prefractionator (2), between second vacuum evacuation device (17) and the extractant recovery tower (14)
Have pressure gauge (31), the prefractionator (2), extraction tower (8), scans fractionating column (4) and rectifying column at extractant recovery tower (14)
(18) intracavity bottom is respectively equipped with temperature sensor (32) and heating device (33), and inner cavity top also is provided with the temperature sensing
Device (32), the heating device (33) are separately connected first heat-exchange device (3), the second heat-exchange device (10) and third
Heat-exchange device (19), the temperature sensor (32), 1-2 vacuum evacuation device, five flow control valve of 1-5 and heating device
(33) control unit (37) are electrically connected, include main control computer in described control unit (37), and described control unit (37)
It is electrically connected sample detecting unit (38), and sample detecting unit (38) acquires sample in above-mentioned surge tank and storage tank per hour
Data are primary.
4. a kind of coking crude benzene adds hydrogen recovery unit according to claim 1, it is characterised in that: the pretreatment unit (1)
Interior to be equipped with filter device (34), filter device (34) pipeline connects agitating device (35), agitating device (35) the pipeline connection
Oil pump (36), the agitating device (35) is interior to be equipped with transmission mechanism (40), and transmission mechanism (40) side is equipped with feed inlet
(39), the other side is equipped with overflow mechanism (41), and agitating device (35) intracavity bottom is equipped with annular-type plate (42).
5. a kind of coking crude benzene adds hydrogen recovery unit according to claim 1, it is characterised in that: in the prefractionator (2)
Chamber bottom temp is adjusted through control unit, is slowly improved by 175 DEG C, every to increase 0.5 DEG C, is then stablized 8 hours, is improved simultaneously
The vacuum degree of tower increases overhead reflux, makes to feed reflux ratio no more than 0.4, control tower top temperature is not more than in 72 DEG C.
6. a kind of coking crude benzene adds hydrogen recovery unit according to claim 1, solvent/charge ratio of the extraction tower (8) is
3.3:1.wt/wt, selects low dissolving power solvent, and the FIC206 and lower part FIC208 of extraction tower (8) the upper pipe connection are molten
Agent charge ratio is 4:1.1.wt/wt, and rectifying column (18) column bottom temperature control is at 155-158 DEG C, tower top temperature 116-118
DEG C, for the temperature difference less than 4 DEG C, phegma/Produced Liquid is 2:1.wt/wt in tower.
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| CN106008139A (en) | 2016-10-12 |
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