CN106957675B - The temperature and compress control method and its design method and purposes of a kind of hydrogenation technique - Google Patents
The temperature and compress control method and its design method and purposes of a kind of hydrogenation technique Download PDFInfo
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- CN106957675B CN106957675B CN201710211080.9A CN201710211080A CN106957675B CN 106957675 B CN106957675 B CN 106957675B CN 201710211080 A CN201710211080 A CN 201710211080A CN 106957675 B CN106957675 B CN 106957675B
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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 design method and purposes, pressure release point is set in the separation system outlet or coupled upstream device or pipeline after reactor, by opening the pressure release point progressively pressure 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, decompression 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 design method 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, remove sulphur in raw material, nitrogen 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 strong exothermal reaction, and temperature rise is higher in reactor, and slurry bed system hydrogenation technique is complicated, and this is allowed for
The possibility of reactor overtemperature and superpressure greatly increases, 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
Circulate operation failure and other reasons are likely to cause reactor temperature runaway or superpressure in device outlet obstruction, paste state bed reactor, and 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；The generation of polycondensation reaction can also be aggravated in addition, made
Forming apparatus blocks.Once there is the above situation, it is necessary to which emergency action, most efficient method are exactly terminating reaction：1st, raw material is cut off
Supplied with hydrogen；2nd, separate liquid phase in reactor, i.e., hydrogen separates with oil phase in reactor, and it is anti-to terminate hydrogenation
Should；3rd, media discharge will be overheated in reactor to go out, while reactor pressure is lowered in time.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 design method and purposes of hydrogenation technique, for handling
The emergency such as the temperature runaway of reactor or superpressure.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 the pressure release point progressively pressure in release reaction system
Power, wherein the temperature at pressure release point is 30 DEG C~220 DEG C, two control points is set gradually from low to high, more than control point
For the moment, rate of pressure reduction 3-10bar/min；During more than control point two, decompression 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 preferable control point is arranged on cryogenic high pressure separator outlet.
The preferable control point connects with reaction system.
The pressure decay rate at the preferable control point is used by Valve controlling, valve and is automatically controlled and/or controlled manually.
Quantity >=1 of preferable pressure relief valve, it is used in parallel when more than one.
Preferably drawing off medium delivers to flare system.
Preferable temperature and pressure control system also receives the finger of other state of emergency signals in addition to monitoring point pressure signal is received
Order.
After preferable startup pressure release, by signal feed apparatus control system.
The reaction mass into device is preferably initially switched off after more than control point.
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 refer 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 design method 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
Press 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
Reduce, reaction heat is carried over, and reaction speed gradually reduces, and the purpose that being finally reached reduces reaction temperature passes through the drop that reasonably cools
Speed is pressed, first, can ensure that the temperature and pressure of reactor is down to reasonable traffic coverage or shut-down；Second, it can ensure
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,
Have the function that protection equipment；Third, cold high score releases the clean gaseous substance that medium is cold conditions, torch system can be immediately discharged to
System, it is not necessary to additionally increase special flare system, reduce operation risk and investment.
The control point connects 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, 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 to react 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, and 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, to avoid thermometer or sensor from failure state occur, 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, total pressure release speed is 21bar/min, and two relief valves make simultaneously
With.
Reactor 15 is exported between cold high score 3 exports and is not provided with valve, to ensure that cold high score 3 connects with reactor 15, lets out
Before pressure valve pressure signal picks up from valve, 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 surpasses
When crossing 20MPa, relief valve A is opened, pressure release speed is 6bar/min, if reactor pressure continues to increase, is exceeded
22MPa, then valve B is also opened, total pressure release speed is 21bar/min, and two relief valves use simultaneously.
Stop coal and hydrogen charging before pressure release, close down reactor cycles pump, to cut off reaction.
Service condition according to above-described embodiment using the pressure releasing method of the present invention is right in coal state bed hydroprocessing technique
Good application effect is achieved in safety guarantee, the measure is simple to operate, and automaticity is high, improves the safety of production
Property.
The preferable embodiment of the present invention 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 readily occur 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 (9)
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 or pipeline for being connected, by opening the pressure release point progressively pressure 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 3-10bar/min；During more than control point two, rate of pressure reduction 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 for claim 1, it is characterised in that the control point is arranged on cryogenic high pressure separator outlet.
3. according to the method for claim 1, it is characterised in that the pressure decay rate of the pressure release point is adopted by Valve controlling, valve
With automatically controlling and/or control manually.
4. according to the method for claim 1, it is characterised in that quantity >=1 of pressure relief valve, when more than one parallel connection make
With.
5. according to the method for claim 1, it is characterised in that draw off medium and deliver to flare system.
6. according to the method for claim 1, it is characterised in that after starting pressure release, by signal feed apparatus control system.
7. according to the method for claim 1, it is characterised in that the reaction mass into device is initially switched off behind arrival control point.
8. the purposes of any methods describeds of claim 1-7, 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.
9. a kind of temperature of hydrogenation technique and the design method of compress control method, it is characterised in that point of the design after reactor
From pressure release point is set on system outlet or coupled upstream device or pipeline, by opening pressure release point progressively release reaction
Pressure in system, wherein the temperature at 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 3-10bar/min；During more than control point two, decompression 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 |
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| Publication Number | Publication Date |
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| CN106957675A CN106957675A (en) | 2017-07-18 |
| CN106957675B true 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 |
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| WO (1) | WO2018177400A1 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| 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 |
| 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 |
| US10946358B2 (en) | 2018-08-16 | 2021-03-16 | Beijing Aerospace Propulsion Institute | Skid-mounted depressurizing system |
| CN110292899B (en) * | 2019-04-19 | 2021-06-08 | 东南大学 | High-temperature microwave reaction kettle combined device and reaction method |
| 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 |
| 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 |
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 |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1322701A (en) * | 1969-04-01 | 1973-07-11 | Waddleton N | Apparatus for converting liquid fatty nitriles to amines |
| CN104449824B (en) * | 2014-12-05 | 2016-03-30 | 北京石油化工工程有限公司 | A kind of slurry-bed hydrocracking product separation decompression group assembly system |
| 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 |
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2017
- 2017-03-31 CN CN201710211080.9A patent/CN106957675B/en active Active
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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 |
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| CN106957675A (en) | 2017-07-18 |
| WO2018177400A1 (en) | 2018-10-04 |
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