CN100526267C - Method for reducing quenching-oil viscosity of ethene producer - Google Patents
Method for reducing quenching-oil viscosity of ethene producer Download PDFInfo
- Publication number
- CN100526267C CN100526267C CNB2006100808396A CN200610080839A CN100526267C CN 100526267 C CN100526267 C CN 100526267C CN B2006100808396 A CNB2006100808396 A CN B2006100808396A CN 200610080839 A CN200610080839 A CN 200610080839A CN 100526267 C CN100526267 C CN 100526267C
- Authority
- CN
- China
- Prior art keywords
- oil
- viscosity
- tower
- quenching
- scrubber
- 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.)
- Active
Links
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A method for breaking viscosity quenching oil of ethane apparatus is carried out by cooling pyrolysis gas from pyrolyzer, delivering it into oil-leaching tower bottom, separating from substances to form triple backflows, cooling by quenching oil at tower bottom, returning to oil-leaching tower partially, entering backflow gasoline at tower top into by pipeline, cooling substances from pyrolyzer and delivering into after system. It's stable, has high viscosity and saves energy resources.
Description
Technical field
The present invention relates to the quenching oil recycle system in the preparing ethylene by steam cracking industry.
Background technology
At present, mainly adopt the steam heat cracking technology to produce ethene in the world, scission reaction takes place in raw materials such as petroleum naphtha under temperature more than 800 ℃, and split product is cooled to 230 ℃ rapidly in the pyrolyzer outlet, enters oil scrubber then.Cat head is isolated carbon light component below nine, and oil is coiled in being called than heavy component of midsection extraction, and heavier component is a quenching oil at the bottom of the tower.Owing to contain unsaturated aromatic hydrocarbon components such as vinylbenzene, indenes in the quenching oil, under long high temperature in the circulation polymerization can take place, generate macromolecular substance, cause quenching oil viscosity constantly to increase, the quenching oil moving situation is worsened, influence the heat exchange effect, increased the power of recycle pump simultaneously, plant energy consumption is high.Serious in quenching oil viscosity height, cause recycle pump frequently to jump car, even pipeline stop up, must installing parking and just can handle.Therefore quenching oil viscosity controller problem is the difficult problem of puzzlement ethylene unit operation all the time.
Common process for reducing viscosity mainly is from designing consideration, generally is to use the visbreaking tower, by ethane outlet of still splitting gas or directly use the steam stripped mode visbreaking of steam heat.But just domestic and international ethylene industry is respectively installed practical operation situation and seen, and is though this viscosity reducing technology has certain effect, not ideal enough.Because quenching oil viscosity is higher, the oil wash column bottom temperature can't improve, and generally is controlled at about 180 ℃-190 ℃, makes steam consumption rise, and running cost increases.
The chilling oil viscosity that the quenching unit of current preparing ethylene by steam cracking technology uses is generally 30mm
2More than/the s (under 160 ℃ of states), because therefore chilling oil viscosity height must have three quenching oil pump operations (electric current is 97A), no stand-by pump.In addition, because quenching oil viscosity is higher, the oil wash column bottom temperature is controlled at generally that (under the normal circumstances, the oil wash column bottom temperature is high more, and quenching oil viscosity is big more about 180 ℃-190 ℃, the pump operation electric current is big more), can't improve, cause plant energy consumption high, individual device is because of the high reason of quenching oil viscosity, recycle pump is frequently jumped car, the steady running of serious threat ethylene unit.
Summary of the invention
The objective of the invention is to overcome the deficiencies in the prior art, a kind of new ethylene unit quenching oil process for reducing viscosity is provided, successfully solve the high problem of quenching oil viscosity in service, with save energy and guarantee ethylene unit steady running.
The steam heat cracking technique is widely used in the ethylene industry, and the pyrolyzer effluent is incorporated into the oil wash system after initial cooling, so that remove the heavy product in the pyrolyzer effluent, and reclaims heat from hot logistics.
A kind of new ethylene unit quenching oil process for reducing viscosity provided by the invention the steps include:
(1) pyrolyzer exports the splitting gas that comes and send into the oil scrubber bottom after cooling, carries out separating substances, forms three bursts of backflows, is respectively: the quenching oil component coagulates and arrives the quenching oil that forms at the bottom of the tower, stage casing dish oil and the trim the top of column gasoline that the oil scrubber middle part produces;
(2) quenching oil is after cooling at the bottom of the tower, and part is returned oil scrubber, and part is sent outside;
(3) stage casing dish oil is after cooling, and part is returned oil scrubber, and part is blended at the bottom of the tower as regulating viscosity, and part is sent outside.
(4) trim the top of column gasoline enters oil scrubber, and pyrolyzer sends into the back system after the logistics cooling the most at last.
Equipment in the ethylene unit quenching oil process for reducing viscosity provided by the invention mainly comprises oil scrubber 1 and quenching oil interchanger 2 and dish oil heat exchanger 3.The splitting gas that the pyrolyzer outlet comes is through tentatively cooling off after pipeline 11 is sent into oil scrubber 1 bottom, through 4,5,6 three strands of reflux cooling, the heaviest quenching oil component coagulates at the bottom of tower and forms quenching oil in the material, quenching oil enters interchanger 2 coolings through pipeline 7, major part is returned oil scrubber 1 through pipeline 4, and small part is sent outside through pipeline 13.The dish oil that oil scrubber 1 middle part produces enters interchanger 3 coolings through pipeline 8, and major part is returned oil scrubber 1 through pipeline 5, and as adjusting viscosity, send outside through pipeline 14 by small part at the bottom of pipeline 9 is blended into tower for part dish oil.Trim the top of column gasoline enters through pipeline 6, and pyrolyzer comes the logistics cooling after pipeline 10 is sent into the back system the most at last.
Can described in the above-mentioned steps (3) be blended at the bottom of the tower as the stage casing dish oil of regulating viscosity in add viscosity depressant, make it to enter jointly the oil scrubber bottom, regulate the chilling oil viscosity jointly.
Accompanying drawing 1 is the oil wash system flow sketch of method provided by the present invention.
Among the figure:
1: oil scrubber 2: quenching oil interchanger 3: the dish oil heat exchanger
4-6: reflux cooling pipeline 7-14: other pipelines
The viscosity reductant that uses in the methods of the invention can contain following substances: sulfonic acid 20%, dispersant 15%, N.N diethyl hydroxylamine 12% (weight percent forms, and is lower same), water treatment agent 12%, antioxidant 5%, quench oil antioxidant 10%, petroleum refining corrosion inhibiter 16%, varsol 10%. Viscosity reductant can 6-10ppm concentration be injected into the quench oil circulatory system, with the further quench oil stream dynamic characteristic of improving, reduce viscosity. The preferred DBSA of sulfonic acid wherein, the preferred 2.6-BHT of antioxidant.
Step 3) is blended into that the stage casing dish oil flow of quenching oil circulation pump porch at the bottom of tower as adjusting viscosity is generally 20-100t/h according to quench oil viscosity situation at the bottom of the tower in. The quench oil internal circulating load is 900-1100t/h at the bottom of the tower.
The method provided by the invention periodic analysis quench oil viscosity that can be in operation is according to viscosity index at any time adjustment disk oil and viscosity reductant injection rate.
Can will be rich in the Seal Oil of the drippolene of aromatic hydrocarbons component as quenching oil circulation pump, further to play the visbreaking effect, the drippolene amount of being blended into is 3t/h.
Use process for reducing viscosity provided by the invention, the oil wash column bottom temperature can be brought up to more than 210 ℃ by about 180 ℃-190 ℃, and quench oil viscosity is by 30mm2/ s (160 ℃) drops to 20mm2/ s (160 ℃), minimum 12mm2/ s (160 ℃), the chilling oil pump can change two operations into by three operations, and running current obviously is reduced to about 77A. Owing to the raising of quench oil running temperature, reclaimed the heat of system, the heat exchanger steam generating amount obviously increases, and the high-grade steam amount of filling into obviously reduces. Therefore, use ethylene unit Reduce viscosity method provided by the invention, both solved the high problem of ethylene unit quench oil viscosity in service, effectively guaranteed again device production steady in a long-term, reduced simultaneously the energy resource consumption of ethylene unit.
Embodiment
Now in conjunction with the embodiments the present invention is described in detail.
Embodiment 1:
Adopt the quenching system shown in the accompanying drawing 1, major equipment comprises oil scrubber 1 and quenching oil interchanger 2 and dish oil heat exchanger 3.
The splitting gas that the pyrolyzer outlet comes is through tentatively being cooled to 230 ℃ after pipeline 11 is sent into oil scrubber 1 bottom, through 4,5,6 three strands of reflux cooling, the heaviest quenching oil component coagulates at the bottom of tower and forms quenching oil in the material, quenching oil enters interchanger 2 coolings through pipeline 7, major part is returned oil scrubber 1 through pipeline 4, and small part is sent outside through pipeline 13.
The dish oil that oil scrubber 1 middle part produces enters interchanger 3 coolings through pipeline 8, and major part is returned oil scrubber 1 through pipeline 5, and as adjusting viscosity, send outside through pipeline 14 by small part at the bottom of pipeline 9 is blended into tower for part dish oil.
Trim the top of column gasoline enters through pipeline 6, and pyrolyzer comes logistics to be cooled to 105 ℃ after pipeline 10 is sent into the back system the most at last.
The isolated part of oil scrubber stage casing dish oil is blended into section quenching oil pump entry at the bottom of the tower with the flow of 30t/h.The quenching oil internal circulating load is 1000t/h at the bottom of the tower.
Embodiment 2:
Add viscosity depressant in the quenching oil recycle system: viscosity depressant together enters oil scrubber 1 bottom through pipeline 12 together with the dish oil of pipeline 9, regulates quenching oil viscosity jointly.
As adding viscosity depressant in the middle part dish oil of regulating viscosity, the weight percent of each component consists of in the viscosity depressant: Witco 1298 Soft Acid 20%, dispersion agent 15%, N.N diethyl hydroxylamine 12%, water conditioner 12%, 2.6-ditertbutylparacresol 5%, quenching oil oxidation inhibitor 10%, refining of petroleum inhibiter 16%, varsol (C at the bottom of being blended into tower
9) 10%.The implantation concentration of viscosity depressant is 6-10ppm.
Comparative Examples 1:
Adopt the identical operational scheme of embodiment 1, difference is not comprise in the operational scheme of Comparative Examples 1 the material line 9 and 12 among Fig. 1.When column bottom temperature was increased to 200 ℃, quenching oil viscosity can't be analyzed, behind long-play under the quenching oil high viscosity state because motor overload produces the pump trip phenomenon.Have to reduce temperature (190 ℃) operation, temperature can't reach design conditions (215 ℃) at the bottom of the oil scrubber, device energy recovery poor effect, and energy consumption rises.
Table 1 embodiment 2 and Comparative Examples 1 effect comparison:
| Temperature at the bottom of the oil scrubber | Quenching oil viscosity | Quenching oil pump operation quantity | The pump electric current | |
| Before the enforcement | 190℃ | 30mm 2/s(160℃) | 3 | 97A |
| After the enforcement | 215℃ | <20mm 2/s(160℃) | 2 | 77A |
Claims (4)
1. an ethylene unit quenching oil process for reducing viscosity the steps include:
1) pyrolyzer exports the splitting gas that comes and send into the oil scrubber bottom after cooling, carries out separating substances, forms three bursts of backflows, is respectively: the quenching oil component coagulates and arrives the quenching oil that forms at the bottom of the tower, stage casing dish oil and the trim the top of column gasoline that the oil scrubber middle part produces;
2) quenching oil is after cooling at the bottom of the tower, and part is returned oil scrubber, and part is sent outside;
3) stage casing dish oil is after cooling, and part is returned oil scrubber, and part is blended at the bottom of the tower as regulating viscosity, and part is sent outside;
4) trim the top of column gasoline enters oil scrubber, and pyrolyzer sends into the back system after the logistics cooling the most at last.
2, the method for claim 1 is characterized in that being blended at the bottom of the tower as adding viscosity depressant in the stage casing dish oil of regulating viscosity in the step 3).
3, the method for claim 1, it is characterized in that in the step 3) to be blended at the bottom of the tower as stage casing dish oil flow at quenching oil pump entry place at the bottom of tower of regulating viscosity be 20-100t/h.
4, the method for claim 1 is characterized in that and will be rich in the sealing oil of the pyrolysis gasoline of aromatic hydrocarbons component as the quenching oil recycle pump.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100808396A CN100526267C (en) | 2006-05-18 | 2006-05-18 | Method for reducing quenching-oil viscosity of ethene producer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100808396A CN100526267C (en) | 2006-05-18 | 2006-05-18 | Method for reducing quenching-oil viscosity of ethene producer |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101074184A CN101074184A (en) | 2007-11-21 |
| CN100526267C true CN100526267C (en) | 2009-08-12 |
Family
ID=38975480
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2006100808396A Active CN100526267C (en) | 2006-05-18 | 2006-05-18 | Method for reducing quenching-oil viscosity of ethene producer |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100526267C (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101962565B (en) * | 2010-10-19 | 2013-03-20 | 惠生工程（中国）有限公司 | Quench oil viscosity reducing process for two quench oil systems |
| CN103305259B (en) * | 2012-03-16 | 2015-08-19 | 中国石油化工股份有限公司 | A kind of method reducing ethylene unit quenching oil viscosity |
| CN106811223A (en) * | 2017-03-22 | 2017-06-09 | 福建省环境工程有限公司 | A kind of tar processing method and processing unit |
| DE102018002086A1 (en) * | 2018-03-09 | 2019-09-12 | Borsig Gmbh | quench |
| CN113122298B (en) * | 2020-01-15 | 2022-07-15 | 中韩(武汉)石油化工有限公司 | Method for reducing viscosity of styrene tar and improving fluidity |
-
2006
- 2006-05-18 CN CNB2006100808396A patent/CN100526267C/en active Active
Non-Patent Citations (6)
| Title |
|---|
| 乙烯装置急冷油系统减粘剂的研究. 刘陆军等.石油与天然气化工，第35卷第3期. 2006 |
| 乙烯装置急冷油系统减粘剂的研究. 刘陆军等.石油与天然气化工，第35卷第3期. 2006 * |
| 乙烯装置急冷油系统研究进展. 侯经纬等.化工进展，第24卷第10期. 2005 |
| 乙烯装置急冷油系统研究进展. 侯经纬等.化工进展，第24卷第10期. 2005 * |
| 减粘塔减粘技术在乙烯装置上的应用. 胡天生等.乙烯工业，第17卷第2期. 2005 |
| 减粘塔减粘技术在乙烯装置上的应用. 胡天生等.乙烯工业，第17卷第2期. 2005 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101074184A (en) | 2007-11-21 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100526267C (en) | Method for reducing quenching-oil viscosity of ethene producer | |
| CN103305259B (en) | A kind of method reducing ethylene unit quenching oil viscosity | |
| CN103305257B (en) | Method for reducing viscosity of quenching oil of ethylene unit | |
| CN103131467B (en) | A kind of processing method of selectively hydrogenating and desulfurizing inferior gasoline and device | |
| CN103571533B (en) | A kind of coal tar hydrogenating system and method | |
| WO2016110253A1 (en) | Cold regenerated catalyst circulation method and device therefor | |
| CN101323553B (en) | Method for improving ethylene apparatus quench oil tower bottom temperature | |
| CN104140847A (en) | Method for production of high-octane gasoline by modification of Fischer-Tropsch synthetic naphtha | |
| CN103305260B (en) | A kind of system and method reducing ethylene unit quenching oil viscosity | |
| CN102585899B (en) | Full liquid phase hydrogenation method of coal tar | |
| CN108546565A (en) | Heavy oil delayed coking method and device | |
| CN103305258B (en) | Method for reducing viscosity of quenching oil of ethylene unit | |
| CN105623736A (en) | Whole-fraction catalytic thermal-cracking method for high-temperature coal tar | |
| CN103666560A (en) | Method for increasing yields of low-carbon olefins and aromatics by coker gasoline steam cracking | |
| CN100473712C (en) | Technical flow of hydrogenation of gasoline through catalytic cracking full distillate | |
| CN105985815A (en) | Method for controlling benzene content of benzene-washed coke oven gas in coke oven gas benzene washing system | |
| CN105566029B (en) | A kind of method for reducing ethylene unit energy consumption | |
| CN103834438B (en) | A kind of processing method of hydrogenating desulfurization | |
| CN103059955B (en) | Method for producing clean gasoline from catalytic cracking gasoline | |
| CN103834439B (en) | A kind of method of deep hydrodesulfurizationof | |
| CN103059949B (en) | Catalytic cracking gasoline desulfurization method | |
| CN105567292B (en) | A kind of method for reducing ethylene unit energy consumption | |
| CN103789022A (en) | Hydrogenation process | |
| CN103059954A (en) | Method for reducing catalytic cracking gasoline sulfur content | |
| CN102732285B (en) | Method for alleviating coking of coke tower top oil gas pipeline |
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 |