CN106957675A - The temperature and compress control method and its method for designing and purposes of a kind of hydrogenation technique - Google Patents
The temperature and compress control method and its method for designing and purposes of a kind of hydrogenation technique Download PDFInfo
- Publication number
- CN106957675A CN106957675A CN201710211080.9A CN201710211080A CN106957675A CN 106957675 A CN106957675 A CN 106957675A CN 201710211080 A CN201710211080 A CN 201710211080A CN 106957675 A CN106957675 A CN 106957675A
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- Prior art keywords
- pressure
- temperature
- point
- control
- control point
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Classifications
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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
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
- C10G47/24—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions with moving solid particles
- C10G47/26—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions with moving solid particles suspended in the oil, e.g. slurries
-
- 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
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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 temperature of hydrogenation technique and compress control method and its method for designing and purposes, pressure release point is set in the separation system outlet or coupled upstream device or pipeline after reactor, by opening pressure of the pressure release point progressively in release reaction system, temperature at wherein described pressure release point is 30 DEG C~220 DEG C, two control points are set gradually from low to high, more than control point for the moment, rate of pressure reduction is 3 10bar/min；During more than control point two, step-down pressure speed is 10 25bar/min, the control point one：Temperature >=440 DEG C and/or pressure >=19MPa, control point two：Temperature >=460 DEG C and/or pressure >=21MPa.The invention provides the emergent management measures such as a set of hydrogenation reaction system overtemperature, superpressure, pressure release point is set after separator after especially cold high score, by the new approaches for designing pressure release speed and step so that the high-tension apparatus such as reactor and high-pressure separator can be more steady in pressure leak process.
Description
Technical field
The present invention relates to a kind of temperature of hydrogenation technique and compress control method and its method for designing and purposes, belong to oil
Chemical industry and coal chemical technology.
Background technology
Slurry bed system hydrogenation technique can effectively utilize heavy oil resources and coal resources, sulphur, nitrogen in removing raw material and again
Metal impurities, while the yield and quality of light oil are improved, while being brought challenges to traditional refining technology, due to its valency
Lattice are relatively low, and then improve the economic benefit of processing enterprise, therefore slurry bed system processing technology becomes grinding for petrochemical industry in recent years
Study carefully focus.Slurry bed system hydrogenation reactor is the nucleus equipment of the technique, is related to the success or not of whole device operation.
Hydrogenation reaction is that temperature rise is higher in strong exothermal reaction, reactor, and slurry bed system hydrogenation technique is complicated, and this is allowed for
The possibility of reactor overtemperature and superpressure is greatly increased, it is therefore necessary to which overtemperature and superpressure operating mode to reactor make anticipation, do
The safety measure of reactor overtemperature and superpressure is prevented well.
Enter hydrogenation reactor after the heated stove heating of raw material, furnace operation is improper, reactor feed is unstable, reaction
The reasons such as device outlet obstruction, paste state bed reactor interior circulation operating trouble are likely to cause reactor temperature runaway or superpressure, one
There is this operating mode in denier, and the temperature and pressure of reactor may may proceed to rise, and can aggravate light oil cracking reaction, on the one hand lose
Light oil yield, on the other hand can cause the pressure in reactor drastically to raise；It can also aggravate the generation of polycondensation reaction in addition, make
Forming apparatus is blocked.Once there is above-mentioned situation, it is necessary to which emergency action, most efficient method is exactly terminating reaction：1st, raw material is cut off
With hydrogen supply；2nd, separate liquid phase in reactor, i.e., hydrogen is separated with oil phase in reactor, terminate hydrogenation anti-
Should；3rd, media discharge will be overheated in reactor in time to go out, while reactor pressure is lowered.But above-mentioned steps 3 are places
The difficult point of temperature runaway and superpressure is managed, does not have preferable solution also at present.
The content of the invention
The present invention provides a kind of temperature and compress control method and its method for designing and purposes of hydrogenation technique, for handling
The emergencies such as the temperature runaway or superpressure of reactor.By selecting suitable pressure release point and pressure release speed by reactor pressure and temperature
Degree is down to reasonable interval.
Technical scheme is as follows：
The temperature and compress control method of a kind of hydrogenation technique, it is characterised in that separation system outlet after reactor or
Pressure release point is set on coupled upstream device or pipeline, by opening pressure of the pressure release point progressively in release reaction system
Power, wherein the temperature at pressure release point is 30 DEG C~220 DEG C, sets gradually two control points, more than control point from low to high
For the moment, rate of pressure reduction is 3-10bar/min；During more than control point two, step-down pressure speed is 10-25bar/min, the control point
One：Temperature >=440 DEG C and/or pressure >=19MPa, control point two：Temperature >=460 DEG C and/or pressure >=21MPa.
It is preferred that the control point be arranged on cryogenic high pressure separator outlet.
It is preferred that the control point connected with reaction system.
It is preferred that the control point pressure decay rate by Valve controlling, valve is using automatically controlling and/or control manually.
It is preferred that pressure relief valve quantity >=1, it is used in parallel when more than one.
Preferably draw off medium and deliver to flare system.
It is preferred that temperature and pressure control system receive the fingers of other state of emergency signals in addition to monitoring point pressure signal is received, also
Order.
It is preferred that startup pressure release after, by signal feed apparatus control system.
It is preferred that the reaction mass being initially switched off after more than control point into device.
A kind of temperature of foregoing hydrogenation technique and the purposes of compress control method, it is characterised in that for heavy oil hydrogenation process
Or oily coal hydrogenation slurry bed system hydrogenation technique, the heavy oil hydrogenation process refers to residual oil, catalytic slurry, de-oiled asphalt, coal tar
One or more are combined as raw material and are processed；The coal state bed hydroprocessing technique refer to crude oil, residual oil, catalytic slurry,
One or more kinds of combinations in de-oiled asphalt and coal tar are combined as raw material progress with the one or more in lignite, bituminous coal
The weight of processing, oil and coal is 30-97 than proportion:70-3.
A kind of temperature of foregoing hydrogenation technique and the method for designing of compress control method.
Invention effect
The invention provides emergent management measures such as a set of hydrogenation reaction system overtemperature, superpressures, after separator especially
Pressure release point is set after cold high score, by the new approaches for designing pressure release speed and step so that reactor and high-pressure separator are contour
Pressure equipment can be more steady in pressure leak process.
Control point is set after cold high score, by opening pressure of the control point progressively in release reaction system, reaction pressure
Reduction, reaction heat is carried over, and reaction speed is gradually reduced, and the purpose for being finally reached reduction reaction temperature passes through the drop that reasonably cools
Speed is pressed, one is that the temperature and pressure that ensure that reactor is down to reasonable traffic coverage or shut-down；Two be that ensure that
The high-tension apparatus such as reactor, high-pressure separator and pipeline and valve etc. are not impacted by excessively intense pressure in pressure leak process,
Reach the effect of protection equipment；Three be the clean gaseous substance that cold high score releases that medium is cold conditions, can be immediately discharged to torch system
System, it is not necessary to additionally increase special flare system, reduce operation risk and investment.
The control point is connected with reaction system, i.e. the pressure of control point detection truly can reflect in reactor
Pressure.
Brief description of the drawings
Fig. 1 is the reactor sketch of the embodiment of the present invention, and each label lists as follows in figure：
The hot high scores of 1-, 2- temperature high scores, the cold high scores of 3-, low point of 4- heat, low point of 5- temperature, cold low point of 6-, 7- reaction products, 8-
Cold oil, 9- pressure release lines, the cold high score gas-phase products of 10-, the cold low point of gas-phase product of 11-, the cold low point of liquid product of 12-, 13- waste water,
Low point of oil-phase product of 14- temperature, 15- reactors 1.
Embodiment
For the specific features of the present invention are expanded on further, it will be illustrated with reference to Fig. 1, the introduction of this example is coal state
Bed (with inner circulation structure) hydrogenation technique decompression technique, include connected mode as shown in Figure 1 connection reactor 15, heat height
Point 1, warm high score 2, cold high score 3, low point 4 of heat, low point 5 of temperature, cold low point 6, each stage material indicated in figure is respectively reaction life
Into thing 7, cold oil 8, pressure release line 9, cold high score gas-phase product 10, cold low point of gas-phase product 11, cold low point of liquid product 12, waste water
13, warm low point of oil-phase product 14.
Pressure release point is arranged on cold high score 3 and exported, respectively valve A and valve B, is arranged in parallel, and valve is two formula valves, and it is let out
It is respectively 6bar/min and 15bar/min to press speed.
During 15 normal operating of reactor, outlet operating temperature (OUT) is no more than 455 DEG C, and pressure is no more than 19MPa, because hydrogenation splits
It is exothermic reaction to change reaction, failure state occurs to avoid thermometer or sensor, three thermometers is set, according to two from three
Mode reads temperature, when operation temperature is more than 455 DEG C, starts pressure-relief valve A, pressure release speed is 6bar/min, if reactor 1
Interior temperature continues to raise, and has exceeded 465 DEG C, then opens valve B, and total pressure release speed is 21bar/min, and two relief valves make simultaneously
With.
Reactor 15 is exported between cold high score 3 is exported and is not provided with valve, to ensure that cold high score 3 is connected with reactor 15, lets out
Pressure valve pressure signal is picked up from before valve, and pressure and reactor pressure difference are fixed herein, so pressure herein can be true
Pressure in reaction response device.During 15 normal operating of reactor, operating pressure is no more than 20MPa, to avoid pressure gauge or sensing
There is failure state in device, sets three pressure gauges, pressure is read in the way of two from three, when operating pressure exceedes when pressure is super
When crossing 20MPa, relief valve A is opened, pressure release speed is 6bar/min, if reactor pressure continues to increase, is exceeded
22MPa, then also open valve B, and total pressure release speed is 21bar/min, and two relief valves are used simultaneously.
Stop coal and hydrogen charging before pressure release, reactor cycles pump is closed down, to cut off reaction.
It is right in coal state bed hydroprocessing technique according to service condition of the above-described embodiment using the pressure releasing method of the present invention
Good application effect is achieved in safety guarantee, the measure is simple to operate, and high degree of automation, improve the safety of production
Property.
The present invention preferably embodiment is the foregoing is only, but protection scope of the present invention is not limited thereto,
Any one skilled in the art the invention discloses technical scope in, the change or replacement that can be readily occurred in,
It should all be included within the scope of the present invention.Therefore, protection scope of the present invention should be with the protection model of claims
Enclose and be defined.
Claims (10)
1. the temperature and compress control method of a kind of hydrogenation technique, it is characterised in that separation system outlet after reactor or with
Pressure release point is set on its upstream device being connected or pipeline, by opening pressure of the pressure release point progressively in release reaction system,
Temperature at wherein described pressure release point is 30 DEG C~220 DEG C, two control points is set gradually from low to high, more than control point one
When, rate of pressure reduction is 3-10bar/min；During more than control point two, rate of pressure reduction is 10-25bar/min, the control point one：
Temperature >=440 DEG C and/or pressure >=19MPa, control point two：Temperature >=460 DEG C and/or pressure >=21MPa.
2. according to the method described in claim 1, it is characterised in that the control point is arranged on cryogenic high pressure separator outlet.
3. according to the method described in claim 1, it is characterised in that the pressure decay rate of the pressure release point is by Valve controlling, and valve is adopted
With automatically controlling and/or control manually.
4. according to the method described in claim 1, it is characterised in that quantity >=1 of pressure relief valve, parallel connection makes when more than one
With.
5. according to the method described in claim 1, it is characterised in that draw off medium and deliver to flare system.
6. according to the method described in claim 1, it is characterised in that temperature and pressure control system is in addition to monitoring point pressure signal is received, also
Receive the instruction of other state of emergency signals.
7. according to the method described in claim 1, it is characterised in that start after pressure release, by signal feed apparatus control system.
8. according to the method described in claim 1, it is characterised in that reach the reaction mass being initially switched off behind control point into device.
9. the purposes of any methods describeds of claim 1-8, it is characterised in that for heavy oil hydrogenation process or oily coal hydrogenation slurry
Bed hydroprocessing technique, the heavy oil hydrogenation process refer to residual oil, catalytic slurry, de-oiled asphalt, one or more kinds of groups of coal tar
Raw material is combined into be processed；The coal state bed hydroprocessing technique refers to crude oil, residual oil, catalytic slurry, de-oiled asphalt and coal tar
One or more kinds of combinations in oil are combined as raw material with the one or more in lignite, bituminous coal and are processed, oil and coal
Weight is 30-97 than proportion:70-3.
10. a kind of temperature of hydrogenation technique and the method for designing of compress control method, it is characterised in that design is after reactor
Pressure release point is set in separation system outlet or coupled upstream device or pipeline, progressively discharged instead by opening pressure release point
The pressure in system is answered, wherein the temperature at pressure release point is 30 DEG C~220 DEG C, two controls are set gradually from low to high
Point, more than control point for the moment, rate of pressure reduction are 3-10bar/min；During more than control point two, step-down pressure speed is 10-25bar/
Min, the control point one：Temperature >=440 DEG C and/or pressure >=19MPa, control point two：Temperature >=460 DEG C and/or pressure >=
21MPa。
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710211080.9A CN106957675B (en) | 2017-03-31 | 2017-03-31 | The temperature and compress control method and its design method and purposes of a kind of hydrogenation technique |
| PCT/CN2018/081270 WO2018177400A1 (en) | 2017-03-31 | 2018-03-30 | Temperature and pressure control method for hydrogenation process, design method therefor and use thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710211080.9A CN106957675B (en) | 2017-03-31 | 2017-03-31 | The temperature and compress control method and its design method and purposes of a kind of hydrogenation technique |
Publications (2)
| Publication Number | Publication Date |
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| CN106957675A true CN106957675A (en) | 2017-07-18 |
| CN106957675B CN106957675B (en) | 2018-03-06 |
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| CN201710211080.9A Active CN106957675B (en) | 2017-03-31 | 2017-03-31 | The temperature and compress control method and its design method and purposes of a kind of hydrogenation technique |
Country Status (2)
| Country | Link |
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| CN (1) | CN106957675B (en) |
| WO (1) | WO2018177400A1 (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2018177400A1 (en) * | 2017-03-31 | 2018-10-04 | 北京中科诚毅科技发展有限公司 | Temperature and pressure control method for hydrogenation process, design method therefor and use thereof |
| CN110215742A (en) * | 2018-03-01 | 2019-09-10 | 中石化广州工程有限公司 | A kind of method of hydrogenation plant dechlorination |
| CN110292899A (en) * | 2019-04-19 | 2019-10-01 | 东南大学 | High temperature microwave reaction kettle combined apparatus and reaction method |
| WO2020034594A1 (en) * | 2018-08-16 | 2020-02-20 | 北京航天动力研究所 | Skid-mounted depressurization system |
| CN113019038A (en) * | 2021-03-10 | 2021-06-25 | 北京中科诚毅科技发展有限公司 | Hydrogenation separation process and design method and application thereof |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110669548A (en) * | 2019-09-02 | 2020-01-10 | 国家能源集团宁夏煤业有限责任公司 | Hydrocracking reactor interlocking protection control method and control system |
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| CN201454515U (en) * | 2009-05-27 | 2010-05-12 | 杰达维（上海）医药科技发展有限公司 | Catalytic hydrogenation device |
| CN103484153A (en) * | 2012-06-13 | 2014-01-01 | 中国石油天然气股份有限公司 | Method for inhibiting hydrocracking temperature runaway by using reaction pressure |
| CN204735197U (en) * | 2015-06-02 | 2015-11-04 | 沧州华海炼油化工有限责任公司 | Hydrogenation pressure control device |
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| GB1322701A (en) * | 1969-04-01 | 1973-07-11 | Waddleton N | Apparatus for converting liquid fatty nitriles to amines |
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| CN105273747B (en) * | 2015-11-18 | 2017-05-03 | 北京中科诚毅科技发展有限公司 | Temperature control measure for slurry bed hydrogenation reactor and design method and application thereof |
| CN106957675B (en) * | 2017-03-31 | 2018-03-06 | 北京中科诚毅科技发展有限公司 | The temperature and compress control method and its design method and purposes of a kind of hydrogenation technique |
-
2017
- 2017-03-31 CN CN201710211080.9A patent/CN106957675B/en active Active
-
2018
- 2018-03-30 WO PCT/CN2018/081270 patent/WO2018177400A1/en active Application Filing
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201454515U (en) * | 2009-05-27 | 2010-05-12 | 杰达维（上海）医药科技发展有限公司 | Catalytic hydrogenation device |
| CN103484153A (en) * | 2012-06-13 | 2014-01-01 | 中国石油天然气股份有限公司 | Method for inhibiting hydrocracking temperature runaway by using reaction pressure |
| CN204735197U (en) * | 2015-06-02 | 2015-11-04 | 沧州华海炼油化工有限责任公司 | Hydrogenation pressure control device |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2018177400A1 (en) * | 2017-03-31 | 2018-10-04 | 北京中科诚毅科技发展有限公司 | Temperature and pressure control method for hydrogenation process, design method therefor and use thereof |
| CN110215742A (en) * | 2018-03-01 | 2019-09-10 | 中石化广州工程有限公司 | A kind of method of hydrogenation plant dechlorination |
| WO2020034594A1 (en) * | 2018-08-16 | 2020-02-20 | 北京航天动力研究所 | Skid-mounted depressurization system |
| US10946358B2 (en) | 2018-08-16 | 2021-03-16 | Beijing Aerospace Propulsion Institute | Skid-mounted depressurizing system |
| CN110292899A (en) * | 2019-04-19 | 2019-10-01 | 东南大学 | High temperature microwave reaction kettle combined apparatus and reaction method |
| CN113019038A (en) * | 2021-03-10 | 2021-06-25 | 北京中科诚毅科技发展有限公司 | Hydrogenation separation process and design method and application thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106957675B (en) | 2018-03-06 |
| WO2018177400A1 (en) | 2018-10-04 |
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