CN1621142A - Hydrogenation reaction chamber for suspension of pressure drop ascending - Google Patents
Hydrogenation reaction chamber for suspension of pressure drop ascending Download PDFInfo
- Publication number
- CN1621142A CN1621142A CN 200310115515 CN200310115515A CN1621142A CN 1621142 A CN1621142 A CN 1621142A CN 200310115515 CN200310115515 CN 200310115515 CN 200310115515 A CN200310115515 A CN 200310115515A CN 1621142 A CN1621142 A CN 1621142A
- Authority
- CN
- China
- Prior art keywords
- reactor
- logistics
- pressure drop
- catalyzer
- pipeline
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000005984 hydrogenation reaction Methods 0.000 title description 10
- 230000001174 ascending effect Effects 0.000 title 1
- 239000000725 suspension Substances 0.000 title 1
- 238000000034 method Methods 0.000 claims abstract description 25
- 230000000630 rising effect Effects 0.000 claims description 7
- 230000001934 delay Effects 0.000 claims description 5
- 239000003054 catalyst Substances 0.000 abstract description 8
- 239000000463 material Substances 0.000 abstract description 2
- 230000003111 delayed effect Effects 0.000 abstract 1
- 238000007599 discharging Methods 0.000 abstract 1
- 239000002994 raw material Substances 0.000 description 11
- 239000002893 slag Substances 0.000 description 9
- 239000001257 hydrogen Substances 0.000 description 8
- 229910052739 hydrogen Inorganic materials 0.000 description 8
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 7
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 7
- 229910052742 iron Inorganic materials 0.000 description 7
- 230000000052 comparative effect Effects 0.000 description 6
- 239000013618 particulate matter Substances 0.000 description 5
- 239000011575 calcium Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000013058 crude material Substances 0.000 description 1
- 238000007324 demetalation reaction Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The present invention is hydrogenating reactor and method with delayed pressure drop raising. The cylindrical hydrogenating reactor is provided with distributing member and catalyst intercepting net in the upper part, catalyst supporting net and distributing member in the lower part, catalyst discharging port set on the cylinder wall over the catalyst supporting net, one opening in the top and one opening in the bottom. The method of delaying pressure drop raising includes: making the material flow inside the hydrogenating reactor in one direction first, altering to the opposite direction after the pressure difference reaches 0.2-0.6 MPa, and so on until reaching the maximum designed pressure difference or stopping. The present invention can overcome the jamming and pressure drop raising and prolong the operation period of residual oil hydrogenating apparatus.
Description
Technical field
The invention belongs to a kind ofly at the Apparatus for () and method therefor that has under the situation of hydrogen refining hydrocarbon ils, more particularly, is a kind of hydrogenator and method that pressure drop is risen that delay.
Background technology
It is one of main reason that causes the shortening of residual hydrogenation on-stream time that the pressure drop of the especially anterior reactor of pressure drop rising is risen.Pressure drop rising most important reason is because Fe, Ca in the raw material residual oil and solid particulate matter cause at beds deposition, obstruction reactor.
Be prolong operation cycle, WO 00/61706A discloses the method that up-flow reactor carries out residual hydrogenation of using.Set up a up-flow reactor before common reactor, comprise two kinds of catalyzer at least in up-flow reactor, wherein SA catalyzer is loaded in the bottom, and highly active catalyzer is loaded on top.Distributing disc is positioned at reactor bottom, plays quenching oil between the bed.Stock oil and hydrogen enter reactor from the bottom, flow from bottom to top then, and therefore catalyzer thereby generation microdilatancy help to overcome reactor plugs, prolong the residual hydrogenation equipment operational cycle.But even if up-flow reactor is processed Fe, Ca, residual oil that particle content is high for a long time, also can raise because of up-flow reactor stops up pressure drop, and this phenomenon once appear on the full scale plant.
Industrial in addition method commonly used also has: (1) increases the protective material loadings, but this method has reduced the loadings of Primary Catalysts; (2) adopt the guard reactor that can get rid of, guard reactor short circuit when pressure drop is increased to design limit, second reactor is directly advanced in logistics, but this method will cause guard reactor to have the operational cycle of half to utilize; (3) adopt moving-burden bed reactor, but increased considerably investment; (4) adopt the suitching type guard reactor, the complicated and increase investment of handoff procedure.Therefore be necessary to seek the better and more economical method that pressure drop is risen that delays.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of hydrogenator and method that pressure drop is risen that delay.
Hydrogenator provided by the invention is tubular, it is cylindric that cylindrical shell is, and allocation member and catalyzer interception net are equipped with in cylindrical shell top, and catalyzer supporting network and allocation member are equipped with in the cylindrical shell bottom, barrel above the catalyzer supporting network has and unloads the agent mouth, and a mouth is respectively opened in the top of reactor and bottom.
Method provided by the invention comprises: logistics is flowed by a direction earlier in hydrogenator, when pressure reduction is the preferred 0.25-0.40MPa of 0.2-0.6, with the logistics direction change into former side in the opposite direction, so analogize until reaching the reactor design maximum differential pressure or device is stopped work.
Hydrogenator provided by the invention and method can overcome the obstruction of reactor and the rising of pressure drop, prolong the operational cycle of residual hydrogenation equipment.
Description of drawings
Fig. 1 is a hydrogenator structural representation provided by the invention.
Fig. 2 is the method flow synoptic diagram that pressure drop is risen that delays provided by the invention.
Embodiment
Hydrogenator provided by the invention is tubular, it is cylindric that cylindrical shell is, and allocation member and catalyzer interception net are equipped with in cylindrical shell top, and catalyzer supporting network and allocation member are equipped with in the cylindrical shell bottom, barrel above the catalyzer supporting network has and unloads the agent mouth, and a mouth is respectively opened in the top of reactor and bottom.
Method provided by the invention comprises: logistics is flowed by a direction earlier in hydrogenator, when pressure reduction is the preferred 0.25-0.40MPa of 0.2-0.6MPa, with the logistics direction change into former side in the opposite direction, so analogize until shut-down.
Below in conjunction with accompanying drawing hydrogenator provided by the present invention and method are further detailed.
Accompanying drawing 1 is a hydrogenator structural representation provided by the present invention.
Hydrogenator housing 1 provided by the invention is tubular, cylindrical shell 2 is cylindric, catalyzer is housed in the cylindrical shell, allocation member 5 and catalyzer interception net 6 are equipped with in cylindrical shell top, catalyzer supporting network 7 and allocation member 8 are equipped with in the bottom in the tube, barrel above catalyzer supporting network 7 has and unloads agent mouth 9, and a mouth is respectively opened in the top of cylindrical shell and bottom: suitable for reading 3 and end opening 4.
Accompanying drawing 2 is the method flow synoptic diagram that pressure drop is risen that delay provided by the present invention.
This method is divided into two kinds:
(1) logistics from top to bottom flows earlier
Open valve 14 and valve 24, shut-off valve 21 and valve 18 this moment.Logistics flows from top to bottom.
Logistics (comprises hydrocarbon oil crude material and hydrogen, enter hydrogenator 10 through pipeline 11, pipeline 12, valve 14, pipeline 15, pipeline 16 from reactor suitable for reading 3 successively down together), logistics is tackled the beds in net 6, the cylindrical shell 2 by allocation member 5, catalyzer successively in reactor, reacted logistics is left reactor through catalyzer supporting network 7, allocation member 8 by reactor end opening 4 successively, leaves the logistics of reactor and draws through pipeline 20, pipeline 23, valve 24, pipeline 25, pipeline 26 successively.
When pressure reduction is the preferred 0.25-0.40MPa of 0.2-0.6MPa, open valve 21 and valve 18, while shut-off valve 14 and valve 24, logistics changes into from the bottom up and flowing.
Logistics enters hydrogenator 10 through pipeline 11, pipeline 13, valve 21, pipeline 22, pipeline 20 from reactor end opening 4 successively, the beds in allocation member 8, catalyzer supporting network 7, the cylindrical shell 2 is passed through in logistics successively in reactor, reacted logistics is left reactor through catalyzer interception net 6, allocation member 5 by reactor suitable for reading 3 successively, leaves the logistics of reactor and draws through pipeline 16, pipeline 17, valve 18, pipeline 19, pipeline 26 successively.
When pressure reduction is 0.2-0.6MPa, open valve 14 and valve 24 again, close valve 21 and valve 18, logistics changes into from top to bottom and flowing.So analogize until reaching reactor design maximum differential pressure or device shut-down.
(2) logistics flows earlier from the bottom to top
Open valve 21 and valve 18, shut-off valve 14 and valve 24 this moment.Logistics flows from the bottom up.
Logistics enters hydrogenator 10 through pipeline 11, pipeline 13, valve 21, pipeline 22, pipeline 20 from reactor end opening 4 successively, the beds in allocation member 8, catalyzer supporting network 7, the cylindrical shell 2 is passed through in logistics successively in reactor, reacted logistics is left reactor through catalyzer interception net 6, allocation member 5 by reactor suitable for reading 3 successively, leaves the logistics of reactor and draws through pipeline 16, pipeline 17, valve 18, pipeline 19, pipeline 26 successively.
When pressure reduction is the preferred 0.25-0.40MPa of 0.2-0.6MPa, open valve 14 and valve 24, while shut-off valve 21 and valve 18, logistics changes into from top to bottom and flowing.
Logistics enters hydrogenator 10 through pipeline 11, pipeline 12, valve 14, pipeline 15, pipeline 16 from reactor suitable for reading 3 successively, logistics is tackled the beds in net 6, the cylindrical shell 2 by allocation member 5, catalyzer successively in reactor, reacted logistics is left reactor through catalyzer supporting network 7, allocation member 8 by reactor end opening 4 successively, leaves the logistics of reactor and draws through pipeline 20, pipeline 23, valve 24, pipeline 25, pipeline 26 successively.
When pressure reduction is 0.2-0.6MPa, open valve 21 and valve 18 again, shut-off valve 14 and valve 24, logistics changes into from the bottom up and flowing.So analogize until reaching reactor design maximum differential pressure or device shut-down.
The characteristics of this reactor maximum are the rising problems that can overcome the obstruction and the pressure drop of reactor, prolong the operational cycle of residual hydrogenation equipment.Flow through reactor in the fs logistics with a direction; behind the slow ascent stage of experience one pressure drop; when pressure reduction acquires a certain degree and pressure drop occurs and begin zooming sign is arranged; the logistics of switch protecting reactor flows to; make the logistics reverse direction flow cross reactor; again experience the slow ascent stage of pressure drop, until stopping work because of pressure drop reaches the maximum bearing value of equipment at last.
The present invention is applicable to the various hydrogenation units that are easy to cause the anterior pressure drop of reactor to rise, and is particularly useful for reactor and is easily stopped up by Fe, Ca and particulate matter and pressure drop is risen and cause the residual hydrogenation equipment that is forced to stop work in advance.Easily stopped up for reactor and pressure drop to be risen and cause the device that is forced to stop work by Fe, Ca and particulate matter, adopt reactor of the present invention and method, can delay pressure drop rises, the operational cycle of device is reached about the twice in common unit operational cycle, prolong the operational cycle of residual hydrogenation equipment.
Because Chinese domestic oil contains impurity such as Fe, Ca and particulate matter more, so the domestic oil of work in-process state of the present invention or other contain on the residual hydrogenation equipment of the more stock oil of Fe, Ca and particulate matter and will have application promise in clinical practice.
The following examples will give further instruction to present method, but therefore not limit present method.
Embodiment 1
Stock oil is to mix the iron naphthenate of 520ppm and the long residuum of the fine mechanical impurity of 655ppm.The catalyzer that loads in the reactor is RDM-1, and this catalyzer is a catalyst for demetalation, is produced by Chang Ling branch office of Sinopec stock company catalyst plant.
Raw material residual oil and hydrogen mixture stream enter reactor from the reactor upper end, and reacted logistics is flowed out by the reactor lower end.Test conditions is: hydrogen dividing potential drop 13.2MPa, and 385 ℃ of temperature of reaction, hydrogen-oil ratio is 400Nm
3/ m
3, air speed is 1.0h
-1, device slag input oil raw material after 460 hours pressure reduction reach 0.3MPa.
Change then stock oil and hydrogen mixture stream the flow direction: advance by the reactor lower end, on bring out.Reactor pressure reduction becomes 0.28MPa, proceeds operation on this basis, and pressure reduction reaches 0.65MPa after 830 hours total times (switch logistics and flow to 370 hours), and device is stopped work.
Comparative Examples 1
Catalyzer, stock oil and test conditions are identical with embodiment 1 in this Comparative Examples, and just logistics is to flow through reactor, not changing flow direction from top to bottom all the time.Device slag input oil raw material after 480 hours pressure reduction reach 0.3MPa, slag input oil raw material after 530 hours pressure reduction reach 0.65MPa, device is stopped work.Operational cycle reduces 300 hours than embodiment 1.
Embodiment 2
Catalyzer, stock oil and test conditions are identical with embodiment 1 in the present embodiment, and just to begin be to flow through reactor from bottom to up in logistics, device slag input oil raw material after 540 hours pressure reduction reach 0.3MPa.
Change the flow direction of stock oil and hydrogen mixture stream then: advance by the reactor upper end, bring out down.Proceed operation, pressure reduction reaches 0.65MPa after 930 hours total times (switch logistics and flow to 390 hours), and device is stopped work.
Comparative Examples 2
Catalyzer, stock oil and test conditions are identical with embodiment 2 in this Comparative Examples, and just logistics is to flow through reactor, not changing flow direction from bottom to up all the time.Device slag input oil raw material after 530 hours pressure reduction reach 0.3MPa, slag input oil raw material after 590 hours pressure reduction reach 0.65MPa, device is stopped work.Operational cycle reduces 340 hours than embodiment 2.
Embodiment 3
Stock oil is identical with embodiment 1 with test conditions in the present embodiment, and catalyzer is Research Institute of Petro-Chemical Engineering's laboratory synthetic spherical catalyst, and used carrier is Al
2O
3, be loaded with the oxide compound of Ni, Mo above.It is to flow through reactor from bottom to up that residual oil and hydrogen gas stream begin, be installed on slag input oil raw material after 580 hours pressure reduction reach 0.3MPa.
Change the flow direction of stock oil and hydrogen mixture stream then: advance by the reactor upper end, bring out down.Proceed operation, pressure reduction reaches 0.65MPa after 930 hours total times (switch logistics and flow to 350 hours), and device is stopped work.
Comparative Examples 3
Catalyzer, stock oil and test conditions are identical with embodiment 3 in this Comparative Examples, and just logistics is to flow through reactor, not changing flow direction from bottom to up all the time.Device slag input oil raw material after 560 hours pressure reduction reach 0.3MPa, slag input oil raw material after 610 hours pressure reduction reach 0.65MPa, device is stopped work.Operational cycle reduces 320 hours than embodiment 1.
Claims (3)
1, a kind of hydrogenator that delays the pressure drop rising, it is characterized in that this reactor is tubular, it is cylindric that cylindrical shell is, allocation member and catalyzer interception net are equipped with in cylindrical shell top, catalyzer supporting network and allocation member are equipped with in the cylindrical shell bottom, barrel above the catalyzer supporting network has and unloads the agent mouth, and a mouth is respectively opened in the top of reactor and bottom.
2, a kind of method that delays the pressure drop rising, it is characterized in that logistics is flowed by a direction earlier in hydrogenator, when pressure reduction is 0.2-0.6MPa, with the logistics direction change into former side in the opposite direction, so analogize until reaching the reactor design maximum differential pressure or device is stopped work.
3, according to the method for claim 2, it is characterized in that when pressure reduction is 0.25-0.40MPa, with the logistics direction change into former side in the opposite direction, so analogize until reaching the reactor design maximum differential pressure or device is stopped work.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200310115515 CN1275684C (en) | 2003-11-28 | 2003-11-28 | Hydrogenation reaction chamber for suspension of pressure drop ascending |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200310115515 CN1275684C (en) | 2003-11-28 | 2003-11-28 | Hydrogenation reaction chamber for suspension of pressure drop ascending |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1621142A true CN1621142A (en) | 2005-06-01 |
| CN1275684C CN1275684C (en) | 2006-09-20 |
Family
ID=34760473
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200310115515 Expired - Lifetime CN1275684C (en) | 2003-11-28 | 2003-11-28 | Hydrogenation reaction chamber for suspension of pressure drop ascending |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1275684C (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102443411A (en) * | 2010-10-13 | 2012-05-09 | 中国石油化工股份有限公司 | Process method for prolonging operation period of hydrogenation device |
| CN102443410A (en) * | 2010-10-13 | 2012-05-09 | 中国石油化工股份有限公司 | Method for prolonging operation period of hydrogenation device |
-
2003
- 2003-11-28 CN CN 200310115515 patent/CN1275684C/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102443411A (en) * | 2010-10-13 | 2012-05-09 | 中国石油化工股份有限公司 | Process method for prolonging operation period of hydrogenation device |
| CN102443410A (en) * | 2010-10-13 | 2012-05-09 | 中国石油化工股份有限公司 | Method for prolonging operation period of hydrogenation device |
| CN102443411B (en) * | 2010-10-13 | 2013-12-04 | 中国石油化工股份有限公司 | Process method for prolonging operation period of hydrogenation device |
| CN102443410B (en) * | 2010-10-13 | 2013-12-04 | 中国石油化工股份有限公司 | Method for prolonging operation period of hydrogenation device |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1275684C (en) | 2006-09-20 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| RU2570948C2 (en) | Hydrotreating method for heavy hydrocarbons in interchangeable reactors including at least one stage of catalytic layer bypass | |
| CN102453530B (en) | Hydrogenation method for processing heavy oil | |
| MX2007002668A (en) | Process and installation for conversion of heavy petroleum fractions in a boiling bed with integrated production of middle distillates with a very low sulfur content. | |
| CN101591565B (en) | Hydrogenation and refining method of gasoline with poor quality | |
| KR20180014775A (en) | Method for converting feedstocks comprising a hydrotreatment step, a hydrocracking step, a precipitation step and a sediment separation step, in order to produce fuel oils | |
| CN103305271B (en) | The combined technical method of a kind of residual oil/middle coalite tar lighting | |
| CN103540353A (en) | Hydrogenation combined process method for treating coal tar and residual oil | |
| CN103059981B (en) | Coal tar hydrogenation method | |
| CN1766058A (en) | Coal tar whole fraction hydrotreatment process | |
| TW201716562A (en) | Heavy oil hydrogenation processing system and heavy oil hydrogenation processing method | |
| CN103305269A (en) | Method for producing gasoline and diesel by directly hydrogenating medium and low temperature coal tar | |
| CN1144860C (en) | Process for hydrogenating residual oil | |
| CN103540351A (en) | Combined process method for treating coal tar whole fraction | |
| CN1275684C (en) | Hydrogenation reaction chamber for suspension of pressure drop ascending | |
| CN103059987B (en) | Hydrotreatment method for coal tar | |
| CN107875978B (en) | Grading filling method and application of hydrogenation catalyst | |
| CN1940029A (en) | Low-hydrogenloss hydrogenation of high-output qulified diesel oil | |
| CN113862035B (en) | Method for producing high-end needle coke raw material from catalytic cracking slurry oil | |
| CN102061192B (en) | Hydrogenation treatment method for inferior feedstock oil | |
| CN106701187A (en) | Method for treating residual oil | |
| CN111676058B (en) | Residual oil hydrogenation reactor with alternately changed material flow directions, residual oil hydrogenation system comprising reactor and residual oil hydrogenation process | |
| CN114806631B (en) | Method for prolonging operation period of fixed bed heavy oil hydrogenation device | |
| CN111676055B (en) | Residual oil hydrogenation reactor, residual oil hydrogenation system containing same and residual oil hydrogenation process | |
| CN111676057B (en) | Residual oil hydrogenation reactor with multiple independent reaction units, residual oil hydrogenation system containing reactor and residual oil hydrogenation process | |
| CN116410788B (en) | Poor-quality heavy oil slurry bed hydrocracking treatment equipment and treatment method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20060920 |