CN108441259A - A kind of heavy benzene hydrogenation process for purification - Google Patents
A kind of heavy benzene hydrogenation process for purification Download PDFInfo
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- CN108441259A CN108441259A CN201810332553.5A CN201810332553A CN108441259A CN 108441259 A CN108441259 A CN 108441259A CN 201810332553 A CN201810332553 A CN 201810332553A CN 108441259 A CN108441259 A CN 108441259A
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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
-
- 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
- C10G2300/1096—Aromatics or polyaromatics
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
-
- 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
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4006—Temperature
-
- 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
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4012—Pressure
-
- 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 present invention relates to a kind of heavy benzene hydrogenation process for purification, heavy benzol and hydrogen are separately added into the first hydrogenation reactor and carry out pre-hydrotreating reaction by this method, reaction product, which enters, takes off benzene unit, isolate benzene, toluene and dimethylbenzene, remaining ingredient is sent into evaporator and is vaporized, after the boil-off gas of evaporator outlet is mixed with hydrogen, into carrying out hydrofining reaction in the second hydrogenation reactor, reaction product carries out rectifying separation again, respectively obtains gasoline fraction and diesel oil distillate；The invention also includes the water route temperature control systems using cycle heat transfer water, are used for recycle heat, which is equipped with feedback control system, reduces human cost.The heavy benzene hydrogenation process for purification of the present invention directly can carry out hydrotreating by counterweight benzene raw materials, promote the further utilization of coal tar, and capacity usage ratio is high, and superior product quality, catalyst life is long, and recycle heat uses in production process, energy conservation and environmental protection.
Description
Technical field
The present invention relates to technical field of petrochemical industry, specially a kind of heavy pump hydrofinishing process.
Background technology
Heavy benzol is the by-product of generation during crude benzole hydrogenation, is colourless to pale yellow oily liquid, there is similar chloroform
Smell, density 0.960-0.990g/cm3 is not soluble in water, volatile, inflammable, toxic, can be most organic with benzene, ketone, ester, alcohol etc.
Solvent is miscible.During crude benzene hydrogenation method, raw material crude benzol is detached in multi-stage evaporation device, high boiling component such as front three
Benzene, naphthalene, indane, coumarone etc. are discharged as Residual oil from multi-stage evaporation device bottom, this part Residual oil is heavy benzol.
All using heavy benzol as raw fuel stock or solvent oil processing, only only a few enterprise is used for for most domestic producer at present
Coumarone-indene resin is produced, because Petropols are more more competitive than coumarone indene resin in price and performance etc., and it is ancient
The grand resin toxic of horse, is gradually replaced by Petropols.In addition, due to containing the heterocyclic compounds such as a certain amount of O, S, N in heavy benzol
Object also has penetrating odor as solvent naphtha in addition to stability difference, and not only quality is not high when directly as fuel oil and pollutes
Environment, i.e., at present there is poor product quality, lack competitiveness or pollute environment in these purposes.Therefore, it is necessary to plus
Strong heavy benzene hydrogenation purification techniques, the new utilization ways of exploitation heavy benzol, extends coal-coking-Fine Chemical Industry chain, and it is attached to increase product
It is value added.
It pumps in unifining process again, has repeatedly heat absorption and exothermic process, need the heat in subtractive process by changing
Thermal cycle is collected, but pump unifining process is related to multiple heat-exchanger rigs again, more difficult by manpower control.
Invention content
The purpose of the invention is to provide a kind of heavy pump hydrofinishing process, directly counterweight pump raw material can carry out adding hydrogen
Processing, whole process heat utilization efficiency is high, while being equipped with temperature control system, realizes water temperature control automation.In order to realize foregoing invention mesh
, present invention employs following technical schemes：
A kind of heavy pump hydrofinishing process, includes the following steps：
Step S01, heavy benzol is preheated by First Heat Exchanger；
Step S02, heavy benzol and hydrogen are separately added into the first hydrogenation reactor and carry out pre-hydrotreating reaction, reaction product enters de-
Benzene unit；
Step S03, de- benzene unit isolates benzene, toluene and dimethylbenzene, and remaining ingredient is sent into evaporator and is vaporized；
Step S04, it is anti-into hydrofinishing is carried out in the second hydrogenation reactor after the boil-off gas of evaporator outlet is mixed with hydrogen
It answers, reaction product enters back into rectifying device and respectively obtains gasoline fraction and diesel oil distillate after rectifying separation；Diesel oil distillate discharges
A bypass, the bypass connection diesel oil distillate heater 6 are additionally provided on pipeline；
Further include water route temperature control system, water route temperature control system includes recirculated water and temperature control system, and the temperature control system includes：
Sensing module, including the first temperature sensor, second temperature sensor and third temperature sensor, respectively with control
Device is connected, and is transmitted to controller for detecting temperature information in real time, and by temperature information, the first temperature sensor is arranged first
In hydrogenation reactor, second temperature sensor is arranged in the second hydrogenation reactor, and third temperature sensor is arranged in evaporator
In；
Controller for the temperature information that the transmission of real-time reception sensing module comes, and is made according to temperature information and being executed instruction,
And it is transmitted to execution module；
Execution module, including the first valve, the second valve and third valve, are respectively connected with controller, for receiving control
Transmission executes instruction, and makes the reaction of valve folding, and the first valve is arranged flows into the first hydrogenation reactor in recirculated water
On inlet pipeline, the second valve is arranged on the inlet pipeline that recirculated water flows into the second hydrogenation reactor, and the setting of third valve exists
It is connected in the bypass of diesel oil distillate heater.
Preferably, inlet pipeline output end connects the first hydrogenation reactor heat exchange, and the first hydrogenation reactor is utilized and followed
Ring water management temperature is in 120-200 DEG C of section of temperature；
Inlet pipeline output end connects the second hydrogenation reactor heat exchange, and the second hydrogenation reactor utilizes cycle water management temperature
In 300-350 DEG C of section of temperature；
The cooling water vapour being discharged in first hydrogenation reactor and the second hydrogenation reactor, is recompressed by MVR equipment, is input to
Evaporator, for providing heat source to evaporator；
The cooling water of evaporator is connected into First Heat Exchanger preheating.
Preferably, a steam point shunting part for the second hydrogenation reactor output transports to rectifying device heating；Rectifying device
The cooling water of output is connected into First Heat Exchanger preheating.
Preferably, the shunting steam, which is transported on the pipeline of rectifying device, is additionally provided with the 4th valve, and the rectifying device is set
There are the 4th temperature sensor, the 4th valve and the 4th temperature sensor to be respectively connected with controller, the 4th temperature sensing
A part of the device as the sensing module in the temperature control system of water route, the 4th valve is as the execution module in the temperature control system of water route
A part.
Compared with prior art, a kind of heavy pump hydrofinishing process of above-mentioned technical proposal is used, is had following beneficial
Effect：
One, the present invention is equipped with water route temperature control system, and the waste heat reacted in the first hydrogenation reactor and the second hydrogenation reactor is followed
Ring utilizes, and to support the heat dissipation demand of evaporator and rectifier unit, increases heat utilization efficiency；
Two, the water route temperature control system in the present invention is additionally provided with diesel oil distillate heater, and the part that system can be utilized to generate distillates
Object diesel oil, then increases heat, to supplement evaporator heat dissipation demand.
Three, the present invention is additionally provided with a set of temperature control system, can be automatically controlled according to the temperature information that temperature sensor transmits
The folding of valve is adjusted, so that the first hydrogenation reactor, the second hydrogenation reactor and evaporator are maintained at needed for reaction
Temperature to ensure the efficiency and quality of reaction, while also reducing human cost.
Description of the drawings
Fig. 1 is a kind of method flow diagram of heavy benzene hydrogenation process for purification provided by the invention；
Fig. 2 is the control flow block diagram of temperature control system in embodiment 1；
Fig. 3 is the control flow block diagram of temperature control system in embodiment 2.
Reference numeral：1, the first hydrogenation reactor；2, benzene unit is taken off；3, evaporator；4, the second hydrogenation reactor；5, first
Heat exchanger；6, diesel oil distillate heater；7, MVR equipment；8, rectifying device；9, the first temperature sensor；10, second temperature senses
Device；11, third temperature sensor；12, the 4th temperature sensor；14, the first valve；15, the second valve；16, third valve；
17, the 4th valve.
Specific implementation mode
Following will be combined with the drawings in the embodiments of the present invention, and technical solution in the embodiment of the present invention carries out clear, complete
Site preparation describes, it is clear that described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.It is based on
Embodiment in the present invention, those of ordinary skill in the art obtained without making creative work it is all its
His embodiment, shall fall within the protection scope of the present invention.
Embodiment 1
The present invention provides a kind of heavy benzene hydrogenation process for purification, as shown in Figure 1, heavy benzol and hydrogen are separately added into the first hydrogenation reaction
Pre-hydrotreating reaction is carried out in device 1, reaction product, which enters, takes off benzene unit 2, isolates benzene, toluene and dimethylbenzene, and remaining ingredient is sent into
It is vaporized in evaporator 3, after the boil-off gas that evaporator 3 exports is mixed with hydrogen, into being added in the second hydrogenation reactor 4
Hydrogen refining reaction, reaction product enter back into rectifying device 8 and carry out rectifying separation, respectively obtain gasoline fraction and diesel oil distillate.It should
Gasoline fraction with mixed from the benzene,toluene,xylene that de- benzene unit 2 is isolated after be used as gasoline products.In the first hydrogenation reaction
The First Heat Exchanger 5 for preheating is equipped with before device 1.The invention also includes circulating water temperature Ore-controlling Roles, as shown in Figure 1, dotted line is
The flow direction of water, circulating water temperature Ore-controlling Role include inlet pipeline, and inlet pipeline is divided into 2 tunnels, exports all the way since on the left of Fig. 1
End connects first hydrogenation reactor heat exchange, and the first hydrogenation reactor 1 is using cycle water management temperature in 120-200 DEG C of temperature
In section；Inlet pipeline output end connects second hydrogenation reactor 4 and exchanges heat all the way, and the second hydrogenation reactor 4 utilizes cycle
Water management temperature is in 300-350 DEG C of section of temperature.
The cooling water vapour being discharged in first hydrogenation reactor 1 is recompressed by MVR equipment 7, is input to evaporator 3, is used
In give evaporator 3 provide heat source.The high-temperature water vapor being discharged in second hydrogenation reactor 4 is recompressed by MVR equipment 7,
It is input to evaporator 3, for providing heat source to evaporator 3.
In principle, the cooling water of evaporator 3 belongs to last cooling water, with a small amount of waste heat, is used for for transporting to
The First Heat Exchanger 5 of preheating, belongs to last cooling water.In view of system is sometimes, it would be desirable to be able to which therefore consumption supply is steamed
After the cooling water of hair device 3 collects, wherein separating a bypass is connected into diesel oil distillate heater 6, diesel oil distillate heater 6 is by cooling water
After being heated to steam, then it is connected into MVR equipment 7, supplements the amount of water vapour.
Strongly exothermic and diesel oil distillate heat exchange that the present invention is reasonably utilized in hydrogenation process or the combustion heat are fed
Thermal energy so that whole process reduces the whole energy consumption of system, and capacity usage ratio is high.
In order to more reasonably adjust the temperature and heat supply balance of whole system, many places are arranged the present invention in Fig. 1
Flow control valve, for example, inlet pipeline since on the left of Fig. 1, is divided into 2 tunnels, there is flow control valve on 2 tunnels separated；
It is also equipped with flow control valve on diesel oil distillate pipeline before diesel oil distillate heater 6；It is discharged in second hydrogenation reactor 4
Cooling water vapour is divided into two branches and is respectively equipped with the cooling water and evaporator 3 that flow control valve and rectifying device 8 export
Cooling water collect after, main road is equipped with flow control valve for adjusting bypass flow.
In addition, the present invention eventually passes through the cooling water of First Heat Exchanger 5, inlet pipeline can be transported to reuse, ultimately formed
The saving of water resource.
Wherein, the operating condition of first hydrogenation reactor 1 is：Pressure 8-12MPa, 120-200 DEG C of temperature, volume are empty
Speed 0.5-6/h, hydrogen to oil volume ratio 100-500:1；The operating condition of second hydrogenation reactor 4 is：Pressure 8-12MPa,
300-350 DEG C of temperature, volume space velocity 0.3-0.8/h, hydrogen to oil volume ratio 500-1000:1.It is set in first hydrogenation reactor 1
There is the first catalyst bed, for the catalyst of first catalyst bed using Pd as active component, Mo is auxiliary agent, and γ-Al2O3 are
Carrier, wherein the load capacity of active component Pd is 3%-8%, and the load capacity of Mo is 1%-3%, and the weight ratio of Pd and Mo is 2:1~
4:1.The second catalyst bed is equipped in second hydrogenation reactor 4, the catalyst of second catalyst bed is lived with W2N
Property component, Fe is auxiliary agent, γ-Al2O3 be carrier, wherein the load capacity of active component W2N be 6% ~ 13%, the load of auxiliary agent Fe
Amount is 0.5% ~ 5%, and the weight ratio of W2N and Fe is 1.5:1~5:1.
In the present invention, in order to form heat recovery cycle, water route temperature control system is had additional, water route temperature control system includes cycle
Water and temperature control system, temperature control system include：
Sensing module, including the first temperature sensor 9, second temperature sensor 10 and third temperature sensor 11, respectively with
Controller is connected, and controller, the setting of the first temperature sensor 9 are transmitted to for detecting temperature information in real time, and by temperature information
In the first hydrogenation reactor 1, second temperature sensor 10 is arranged in the second hydrogenation reactor 2, third temperature sensor 11
It is arranged in evaporator 3；
Controller for the temperature information that the transmission of real-time reception sensing module comes, and is made according to temperature information and being executed instruction,
And it is transmitted to execution module；
Execution module, including the first valve 14, the second valve 15 and third valve 16, are respectively connected with controller, for connecing
Executing instruction for controlling transmission is received, and makes the reaction of valve folding, the setting of the first valve 14 flows into first plus hydrogen in recirculated water
On the inlet pipeline of reactor 1, the second valve 15 is arranged on the inlet pipeline that recirculated water flows into the second hydrogenation reactor 4, the
Three valves 16 are arranged in the bypass of connection diesel oil distillate heater 6.
After hydrogenation reaction is a strong exothermal reaction, thus reaction starts, the first hydrogenation reactor 1 and the second hydrogenation reaction
Temperature in device 4 increases rapidly, 9 device of the first temperature sensing being now placed in the first hydrogenation reactor 1, and adds hydrogen positioned at second
10 monitoring temperature information of second temperature sensor in reactor 4, and the temperature information is transmitted to controller, controller receives
After temperature information, instruction is made, the first valve 14 and the second valve 15 are opened, because in chemical reaction, temperature can constantly occur
Variation, in order to more reasonably adjust the temperature and heat supply balance of whole system, the first valve 14, the second valve 15 and the
Three valves 16 are flow control valve, and controller can adjust opening for the first valve 14 and the second valve 15 according to temperature information
Conjunction degree, so that the temperature change of the flow velocity cooperation hydrogenation reaction of recirculated water.Because the temperature of the first hydrogenation reactor 1 is 120-
200 DEG C, the temperature of the second hydrogenation reactor 4 is 300-350 DEG C, and temperature is above the boiling point of water, and recirculated water adds by first
Gasification is high-temperature steam after hydrogen reactor 1 and the second hydrogenation reactor 4, from the first hydrogenation reactor 1 and the second hydrogenation reactor 4
The high-temperature steam of middle outflow enters after MVR equipment 7 is compressed provides heat for evaporator 3.Third temperature sensor 11 is located at evaporation
In device 3, the temperature controller detected in real time in evaporator 3 is made according to the temperature information from third temperature sensor 11 received
Go out instruction, when the heat that the high-temperature steam flowed out from the first hydrogenation reactor 1 and the second hydrogenation reactor 4 provides can not also expire
The demand of sufficient evaporator 3, that is, the temperature that third temperature sensor 11 detects is less than evaporator 3 when evaporating required temperature,
Controller controls third valve 16 and opens, and can control suitable 16 opening and closing degree of third valve according to temperature requirements, because
Third valve 16 is arranged in the bypass of connection diesel oil distillate heater 6, and the opening and closing degree of control third valve 16 can control
The flow of diesel oil distillate, to feed institute's calorific requirement in evaporator 3 in right amount.The circulating water temperature flowed out from evaporator 3 is relatively low, follows
Ring is to First Heat Exchanger 5 for being preheated to hydrogenation reaction.
Embodiment 2
The present embodiment, which only has, has any different at one with embodiment 1, difference lies in the high-temperature steam being discharged in the second hydrogenation reactor 4,
It is divided into as two branches, one of branch is recompressed by MVR equipment 7, is input to evaporator 3, for giving evaporator 3 to provide
Heat source；A water vapour point for another branch shunting transports to the heating of rectifying device 8.Correspondingly, what rectifying device 8 exported
Cooling water belongs to last cooling water, belongs to last for transporting to the First Heat Exchanger 5 for preheating with a small amount of waste heat
Cooling water.
Correspondingly, shunting steam, which is transported on the pipeline of rectifying device 8, is additionally provided with the 4th valve 17, the rectifying device 8 is set
There are the 4th temperature sensor 12, the 4th valve 17 and the 4th temperature sensor 12 to be respectively connected with controller, the 4th temperature
A part of the sensor 12 as the sensing module in the temperature control system of water route is spent, the 4th valve 17 is as in the temperature control system of water route
A part for execution module.Temperature information that controller is provided according to the 4th temperature sensor 12 adjusts opening for the 4th valve 17
Conjunction degree, to meet the heat demand of distillation process.
Above description has fully disclosed the specific implementation mode of the present invention.It should be pointed out that being familiar with the field
Technical staff is to any change for being done of specific implementation mode of the present invention all without departing from the range of claims of the present invention.
Correspondingly, the scope of the claims of the invention is also not limited only to previous embodiment.
Claims (4)
1. a kind of heavy pump hydrofinishing process, includes the following steps：
Step S01, heavy benzol is preheated by First Heat Exchanger；
Step S02, heavy benzol and hydrogen are separately added into the first hydrogenation reactor and carry out pre-hydrotreating reaction, reaction product enters de-
Benzene unit；
Step S03, de- benzene unit isolates benzene, toluene and dimethylbenzene, and remaining ingredient is sent into evaporator and is vaporized；
Step S04, it is anti-into hydrofinishing is carried out in the second hydrogenation reactor after the boil-off gas of evaporator outlet is mixed with hydrogen
It answers, reaction product enters back into rectifying device and respectively obtains gasoline fraction and diesel oil distillate after rectifying separation；Diesel oil distillate discharges
A bypass is additionally provided on pipeline, the bypass connects diesel oil distillate heater；
It is characterized in that：Further include water route temperature control system, water route temperature control system includes recirculated water and temperature control system, the temperature control system
System includes：
Sensing module, including the first temperature sensor, second temperature sensor and third temperature sensor, respectively with control
Device is connected, and is transmitted to controller for detecting temperature information in real time, and by temperature information, the first temperature sensor is arranged first
In hydrogenation reactor, second temperature sensor is arranged in the second hydrogenation reactor, and third temperature sensor is arranged in evaporator
In；
Controller for the temperature information that the transmission of real-time reception sensing module comes, and is made according to temperature information and being executed instruction,
And it is transmitted to execution module；
Execution module, including the first valve, the second valve and third valve, are respectively connected with controller, for receiving control
Transmission executes instruction, and makes the reaction of valve folding, and the first valve is arranged flows into the first hydrogenation reactor in recirculated water
On inlet pipeline, the second valve is arranged on the inlet pipeline that recirculated water flows into the second hydrogenation reactor, and the setting of third valve exists
It is connected in the bypass of diesel oil distillate heater.
2. a kind of heavy pump hydrofinishing process according to claim 1, it is characterised in that：Inlet pipeline output end connects institute
The heat exchange of the first hydrogenation reactor is stated, the first hydrogenation reactor is using cycle water management temperature in 120-200 DEG C of section of temperature；
Inlet pipeline output end connects the second hydrogenation reactor heat exchange, and the second hydrogenation reactor utilizes cycle water management temperature
In 300-350 DEG C of section of temperature；
The cooling water vapour being discharged in first hydrogenation reactor and the second hydrogenation reactor, is recompressed by MVR equipment, is input to
Evaporator, for providing heat source to evaporator；
The cooling water of evaporator is connected into First Heat Exchanger preheating.
3. a kind of heavy pump hydrofinishing process according to claim 1, it is characterised in that：The output of second hydrogenation reactor
A steam point shunting part transports to rectifying device heating；The cooling water of rectifying device output is connected into First Heat Exchanger preheating.
4. a kind of heavy pump hydrofinishing process according to claim 3, it is characterised in that：The shunting steam transports to rectifying
The 4th valve is additionally provided on the pipeline of equipment, the rectifying device is equipped with the 4th temperature sensor, the 4th valve and the 4th
Temperature sensor is respectively connected with controller, one as the sensing module in the temperature control system of water route of the 4th temperature sensor
Point, a part of the 4th valve as the execution module in the temperature control system of water route.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810332553.5A CN108441259A (en) | 2018-04-13 | 2018-04-13 | A kind of heavy benzene hydrogenation process for purification |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810332553.5A CN108441259A (en) | 2018-04-13 | 2018-04-13 | A kind of heavy benzene hydrogenation process for purification |
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| Publication Number | Publication Date |
|---|---|
| CN108441259A true CN108441259A (en) | 2018-08-24 |
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ID=63199905
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810332553.5A Pending CN108441259A (en) | 2018-04-13 | 2018-04-13 | A kind of heavy benzene hydrogenation process for purification |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104774648A (en) * | 2015-03-18 | 2015-07-15 | 大连理工大学 | Heavy benzol hydrofining method of clean fuel oil |
| CN205759793U (en) * | 2016-05-27 | 2016-12-07 | 山东华鸿化工有限公司 | A kind of Nitrobenzene Rectification system |
| CN107365241A (en) * | 2017-06-28 | 2017-11-21 | 徐州东兴能源有限公司 | A kind of crude benzole hydrogenation process for refining |
-
2018
- 2018-04-13 CN CN201810332553.5A patent/CN108441259A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104774648A (en) * | 2015-03-18 | 2015-07-15 | 大连理工大学 | Heavy benzol hydrofining method of clean fuel oil |
| CN205759793U (en) * | 2016-05-27 | 2016-12-07 | 山东华鸿化工有限公司 | A kind of Nitrobenzene Rectification system |
| CN107365241A (en) * | 2017-06-28 | 2017-11-21 | 徐州东兴能源有限公司 | A kind of crude benzole hydrogenation process for refining |
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