CN1140613C - Process for unloading catalyst from petrochemical equipment - Google Patents
Process for unloading catalyst from petrochemical equipment Download PDFInfo
- Publication number
- CN1140613C CN1140613C CNB021128766A CN02112876A CN1140613C CN 1140613 C CN1140613 C CN 1140613C CN B021128766 A CNB021128766 A CN B021128766A CN 02112876 A CN02112876 A CN 02112876A CN 1140613 C CN1140613 C CN 1140613C
- Authority
- CN
- China
- Prior art keywords
- solvent
- catalysts
- finish
- catalyzer
- oil
- 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.)
- Expired - Lifetime
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to a method for unloading catalysts from petrochemical devices. Solvent and film forming agents are adopted as oil agents. The addition level of the film forming agents is 0.5 to 2% of the solvent on a volume ratio basis. Surface processing is carried out for catalysts to make one layer of special film formed on the surfaces of the catalysts, and then the catalysts are unloaded. The oil agents are stuck to the surfaces of the catalysts in a processing mode of soak, dipping or circulation contact of the catalysts and the oil agents, the processing time of the soak, the dipping or the circulation contact of the catalysts and the oil agents is from 4 hours to 10 hours, and the processing time of the circulation contact of the catalysts and the oil agents is from 10 hours to 30 hours. After the catalysts are processed by the oil agents by the present invention, catalyst dust does not occur. The present invention can provide a clean environment for unloading the catalysts.
Description
One, technical field
The inventive method is applicable to the removal of various reaction tower catalyzer in the petroleum chemistry device, especially the preparation-unloading method of hydrocracking reaction tower.
Two, background technology
Used various catalyzer in the petroleum chemistry device reaction tower, after catalyzer uses for some time, descended, or, the catalyzer in the reaction tower must be drawn off because of the equipment claimed maintenance because of it is active., the catalyzer in the reaction tower, especially the catalyzer of hydrocracking reaction tower has very strong oxidation-reduction quality.When contacting with air, the oxidation exothermic reaction can take place, make the catalyzer heating and spontaneous combustion.
For small-sized reaction tower, before unloading agent, bubbling air and steam in reaction tower are with catalyzer burning regeneration (in-place regeneration), then with the catalyzer removal., in-place regeneration needs for a long time.And, when in-place regeneration, to emit sulfurous gas, cause the environmental pollution pollution problem.
For large-scale reaction tower, for preventing catalyzer generation oxidizing reaction, in reaction tower, continue to feed a large amount of nitrogen, under nitrogen protection, unload the agent workman and be equipped with the rescue breathing gear tool, advance tower with the catalyzer removal.The agent work of unloading under the nitrogen protection is dangerous, and its risk level increases and increases with the catalyst bed number of plies.And the catalyzer that the unloads metal bucket of must packing into adds the dry ice protection, could short-term deposit.
More than two kinds of preparation-unloading methods (dry type is unloaded agent), the inside and outside catalyst dust of reaction tower is a lot.Contain carcinogens (Ni in this catalyst dust
3S
2), can endanger the healthy of workman.
Three, summary of the invention
The objective of the invention is: a kind of atmosphere that do not need protection is provided, can under air, directly unloads agent, do not have the preparation-unloading method of catalyst dust again, also improve simultaneously and unload agent efficient.
Technical solution of the present invention is: the process for unloading catalyst of petrochemical equipment, adopt special finish, and catalyzer is carried out the surface contact handle, make catalyst surface form the special film of one deck.This tunic will stop air to contact with catalyzer, make to unload agent work and can directly carry out under air.The so-called mode of handling is that immersion dipping or catalyzer contact with the finish circulation, makes catalyst surface be stained with finish.Soaking dipping or catalyzer is 4-10 hour with the time that the finish circulation contacts processing, and it is 10-30 hour that catalyzer contacts the time of handling with the finish circulation.
Special finish is made up of solvent and membrane-forming agent.Solvent is generally oil fuel, typically comprises solar oil (LGO), heavy gas oil (HGO), decompression diesel oil (VGO), kerosene, aviation kerosene as diesel oil, can also be a kind of, two or three mixing of above-mentioned fuel oil.The KS767 membrane-forming agent that membrane-forming agent is sold by company limited of sky, Jiangsu roc petrochemical industry special corporation uses itself and solvent, and addition is the 0.5-2% (volume ratio) of quantity of solvent.
According to the particular case of petrochemical equipment, can adopt following two kinds to the catalyst surface film, under the normal air atmospheric condition, manually unload agent after the film forming.
1. finish recycling catalyst surface filming method: in the shut-down process of device, at first importing solvent in device makes its circulation.In circulating solvent, add membrane-forming agent then, form special finish.In the finish circulation, make the surface of catalyzer form the special film that one deck can be avoided the air contact.
2. finish immersion catalyst surface becomes embrane method: after device stops, in reaction tower, inject in advance the finish that mixes by solvent such as diesel oil and membrane-forming agent, allow catalyzer in this finish, soak some hrs,, make the surface of catalyzer form the special film of one deck as 4-10 hour.
After the catalyst surface film formed, film can completely cut off catalyzer and contact with air, made that unloading agent work can directly carry out under air, must nitrogen protection.The film formed while of catalyst surface, the inwall in the reaction tower and the surface of each member also form same film, this film energy secluding air, and water contacts with steel, and the protection steel are not subjected to the corrosion of polythionic acid stress.
Characteristics of the present invention are: catalyzer does not have the generation of catalyst dust after above-mentioned finish is handled, and the clean agent environment that unloads can be provided.When adopting vacsorb to unload agent, can use air, save a large amount of nitrogen, reduce the agent expense of unloading.Pneumatic crushing mechanism for the catalyzer that hardens can adopt air, saves nitrogen.
Four, description of drawings
Fig. 1 is the synoptic diagram of finish recycling catalyst surface filming method of the present invention
Fig. 2 soaks the synoptic diagram that catalyst surface becomes embrane method for finish of the present invention
Five, specific embodiment
Describe two kinds of catalyzer films of the present invention by the following examples in conjunction with the accompanying drawings in detail.
Embodiment 1:
Fig. 1 is the synoptic diagram of finish recycling catalyst surface filming method.Valve 2 and pump 3 are arranged on stock oil pipeline 1.At pump outlet, process furnace 4 is arranged.Process furnace 4 is connected by pipeline 5 with reaction tower 7, and flange 6 is arranged on this pipeline, can insert blind plate.Reaction tower 7 links by pipeline 8 and water cooler 10 and gas-liquid separator 11, and flange 9 is arranged on pipe line 8, can insert blind plate.The top of gas-liquid separator 11 links by pipeline 13 and valve 12, makes tail gas row to other equipment.The hydrogen of gas-liquid separator 11 is sent to process furnace 4 by pipeline 14 after gas compressor 15 pressurizations.The liquid of gas-liquid separator 11 is sent to distillation tower 17 by pipeline 16.The cat head of distillation tower 17 has pipeline 18 and miscellaneous equipment to link, and pipeline 19 is arranged at the bottom of the tower.Pipeline 19 divides two-way again, and one the tunnel is by valve 21 and pipeline 22, with liquid fed downstream device.Another road is by valve 23, and the use device line 24 that goes into operation is sent to former stockline 1 with liquid, forms the liquid circulation circuit.10-30 hour cycling time.
Concrete operations are as follows: after the device operation downtime began, when the temperature in the reaction tower dropped to 300 ℃ of left and right sides, the valve of closing raw material spool road was opened valve 25 simultaneously, was that fuel oil imports in the device by pipeline 26 with solvent oil.Close the valve 21 that leads at the bottom of the distillation Tata in the dirty device pipeline 22, the opening unit valve 23 in the pipeline 24 that goes into operation utilizes the pipeline that goes into operation, and makes solvent begin circulation in being.Open valve 27 and by pipeline 28 membrane-forming agent is injected in the round-robin solvent, form special finish, finish circulation 10-30 hour makes catalyst surface form the special film of one deck.With oil discharging, with gas with process furnace 4, pipeline 5, oily purges are gone out in 7 li catalyzer of reaction tower and the reaction tower bottom tube line 8, the catalyst temperature with 7 li of reaction towers drops to below 40-50 ℃ simultaneously.Opening valve 12 will be that interior hydrogen is discharged through exhaust pipe 13, and pressure release makes intrasystem pressure near normal atmosphere.After system carried out nitrogen replacement, the flange 6 and 9 places of pipeline 5 and 8 li inserted blind plate before and after reaction tower, with the blind envelope of reaction tower pipeline.Open reaction tower bottom discharge openings 29, unload agent by gravity.Or adopt vacsorb to unload agent from the reaction tower top.Because of catalyst surface film forming when unloading agent, do not need to use nitrogen protection, directly under air, unload agent.
Embodiment 2:
Fig. 2 is that finish soaks the synoptic diagram that catalyst surface becomes embrane method.Opening valve 25 is that fuel oil imports to 34 li of storage tanks through pipeline 26 with solvent oil.Open valve 27 and membrane-forming agent is injected in the storage tank 34 internal solvent oil, in advance finish 35 is modulated through pipeline 28.Solvent and membrane-forming agent at room temperature simple agitation get final product.
After device stops by general shut-down operation, the flange 9 place's mounted valves 30 in reaction tower 7 bottom line 8, and link to each other with storage tank 34 with pipeline 31.Open valve 36, finish 35 is sent to 7 li catalyzer in finish submergence tower of reaction tower through pipeline 38 usefulness pumps 37.For preventing in the air admission reaction tower,, open valve 32 and in tower, pour nitrogen through pipeline 33 in reaction tower oiling agent 35.Allow catalyzer in finish, soak then 8-10 hour, catalyzer is carried out surface treatment, make the special film of its surperficial shape one deck.Open valve 30 then the oil in the reaction tower is discharged into 34 li of grooves, insert blind plate at flange 9 places, the blind envelope of reaction tower pipeline.
Identical with embodiment 1, open reaction tower bottom discharge openings 29, under air, unload agent by gravity.Or adopt vacsorb to unload agent from the reaction tower top.
Solvent among the embodiment is generally oil fuel, view apparatus comprises solar oil (LGO), heavy gas oil (HGO), decompression diesel oil (VGO), kerosene, aviation kerosene with the convenient diesel oil that uses of oil, two kinds or three kinds that also can be are mixed into solvent, as solar oil and heavy gas oil (HGO) and decompression diesel oil (VGO) mixes, kerosene and aviation kerosene mixes, and for example diesel oil and kerosene mixing and for example.Above-mentioned blended ratio was from 1: 1 to 1: 3.
Claims (5)
1, a kind of process for unloading catalyst of petrochemical equipment, it is characterized in that adopting the finish of solvent and membrane-forming agent, the membrane-forming agent addition is the 0.5-2% of solvent volume, catalyzer is carried out the surface contact handle, make catalyst surface form the special film of one deck, and then unload agent.
2, by the process for unloading catalyst of the described petrochemical equipment of claim 1, it is characterized in that solvent is generally oil fuel, promptly diesel oil comprises solar oil, heavy gas oil, decompression diesel oil, kerosene, a kind of, two or three mixing in the aviation kerosene.
3,, it is characterized in that in solvent, adding membrane-forming agent by the process for unloading catalyst of the described petrochemical equipment of claim 1.
4, by the process for unloading catalyst of the described petrochemical equipment of claim 1, it is characterized in that in the shut-down process of device, at first in device, import solvent, make its circulation, in circulating solvent, add membrane-forming agent then, form special finish, 10-30 hour cycling time.
5, by the process for unloading catalyst of the described petrochemical equipment of claim 1, after it is characterized in that device stops, in reaction tower, inject the finish that mixes by solvent and membrane-forming agent in advance, allow catalyzer in this finish, soak 4-10 hour, make the surface of catalyzer form the special film of one deck.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021128766A CN1140613C (en) | 2002-04-12 | 2002-04-12 | Process for unloading catalyst from petrochemical equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021128766A CN1140613C (en) | 2002-04-12 | 2002-04-12 | Process for unloading catalyst from petrochemical equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1376765A CN1376765A (en) | 2002-10-30 |
| CN1140613C true CN1140613C (en) | 2004-03-03 |
Family
ID=4742315
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB021128766A Expired - Lifetime CN1140613C (en) | 2002-04-12 | 2002-04-12 | Process for unloading catalyst from petrochemical equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1140613C (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112871219B (en) * | 2021-01-14 | 2022-09-06 | 上海阳申石化设备安装有限公司 | Flame-retardant composition for hydrogenation catalysis and use method thereof |
-
2002
- 2002-04-12 CN CNB021128766A patent/CN1140613C/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| CN1376765A (en) | 2002-10-30 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103933845B (en) | A kind of system for the treatment of boats and ships discharging waste gas | |
| WO2000039252A1 (en) | System and method for desulfurizing gasoline or diesel fuel to produce a low sulfur-content fuel for use in an internal combustion engine | |
| CN108187480B (en) | Ship exhaust gas desulfurization system | |
| CN1140613C (en) | Process for unloading catalyst from petrochemical equipment | |
| CN107569990A (en) | The depriving hydrogen sulphide of sulfurous gas-efficient oxidation regeneration integrated method and system | |
| CN110155968A (en) | Inert gas reclamation set and inert gas reuse method | |
| CN208150970U (en) | Inert gas equipment for reclaiming | |
| US20100264060A1 (en) | Process for removal of contaminants in oil | |
| CN113423931A (en) | Pretreatment desulfurization control and monitoring system of marine engine | |
| CN114514060A (en) | Pretreatment desulfurization method for bunker fuel oil by using pretreatment desulfurizing agent | |
| CN110104704A (en) | A kind of method and device of sour water processing sump oil | |
| CN108636078B (en) | Pretreatment agent and pretreatment method for organic waste gas of oil and gas operation station | |
| Siswantoro et al. | Modification of sea water scrubber system into fresh water of inert gas system on the crude oil tanker 85,000 dwt | |
| CN112391202A (en) | Wharf storage tank, ship inerting and oil gas recovery integrated device | |
| CN210656816U (en) | Continuous reforming agent injection device | |
| CN207667658U (en) | Magnesia high-temperature reactor | |
| CN221759769U (en) | Diesel hydrogenation equipment | |
| CN1923969A (en) | Method of adding liquid auxiliary agent in half-regeneration reformer | |
| CN219032303U (en) | Oil removal tower for discharging active carbon by wind stirring | |
| CN205024172U (en) | Ultrasonic wave is fuel desulfurization system integrated equipment that links for auxiliary vehicle | |
| CN114073992B (en) | Oxygen-enriched regeneration device and method for redox desulfurization process and application | |
| CN218844459U (en) | Marine methanol fuel supply pressurization system | |
| CN114082277B (en) | Fine desulfurization purification process for waste lubricating oil hydrogenation tail gas | |
| CN215049975U (en) | Modularized natural gas skid-mounted desulfurization device | |
| CN214990788U (en) | Ultrapure water treatment equipment with reverse osmosis membrane |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| 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 | ||
| C56 | Change in the name or address of the patentee | ||
| CP03 | Change of name, title or address |
Address after: Qinhuai Longpan Road District of Nanjing City, Jiangsu province 210001 No. 418 court 6 floor -33 elegant Patentee after: Jiangsu Peng petrochemical Polytron Technologies Inc Address before: 210011 No. 406, Zhongshan North Road, Jiangsu, Nanjing Patentee before: Tianpeng Special Petrochemical Engineering Co., Ltd., Jiangsu |
|
| CX01 | Expiry of patent term |
Granted publication date: 20040303 |
|
| CX01 | Expiry of patent term |