CN1090668C - Coking inhibiting method for ethylene cracker - Google Patents
Coking inhibiting method for ethylene cracker Download PDFInfo
- Publication number
- CN1090668C CN1090668C CN99119353A CN99119353A CN1090668C CN 1090668 C CN1090668 C CN 1090668C CN 99119353 A CN99119353 A CN 99119353A CN 99119353 A CN99119353 A CN 99119353A CN 1090668 C CN1090668 C CN 1090668C
- Authority
- CN
- China
- Prior art keywords
- additive
- described method
- type
- coking
- pressing down
- 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 - Fee Related
Links
Images
Abstract
The present invention provides a coking inhibiting additive and a coking inhibiting method using the coking inhibiting additive. The coking inhibiting additive which is used for inhibiting, reducing or eliminating the coking of a schizolysis device is prepared from an organic compound (I type) containing phosphorus and amine, and an organic compound (II) containing sulfur phospham and alkali metal; the coking inhibiting additive is used in the amount of 50 to 400 ppm by the weight of raw oil. In the coking inhibiting method, the coking inhibiting additive is added in the raw material stream of the device in the position of a continuous injection port at the front end of an initial reaction point of reaction. The coking inhibiting additive can be used for reducing the coking amount of a furnace tube and a quick cooling boiler by 25 to 90%.
Description
In petroleum hydrocarbon thermo-cracking system olefin process, cracking furnace pipe and quenching boiler are easy to coking usually, have shortened the cycle of operation of industrial installation and have reduced economic benefit.In order to prevent, reduce, to suppress or get rid of coking, people have carried out a large amount of research to the mechanism that coking forms, and have proposed to prevent, reduce, suppress or get rid of the various methods of coking, and one of them is among the additive adding raw material.
The seventies, Nalco company is studied high-temperature coking and control thereof.United States Patent (USP) 4024048 and 4042049 discloses a kind of method that reduces or get rid of hydrodesulfurization unit or catalyzer coking in succession.This method is inhibition or scale removal additive, and promptly a spot of phosphoric acid or phosphorous acid one ester or diester before hydrodesulfurization process begins, or add in the hydrogenating desulfurization logistics in hydrodesulfurization process.
The nineties, Exxon, Kellogg, Amoco, Phillipps, mechanisms such as Linde, scale removal additive has separately been carried out the amplification or the commerical test [M.Wyrostek M.Rupp PYROKATSteamcraking in coad Craking-coils Technology and Scale Demonstration1998] of different scales, [D.M.Taylor, L.LM.Allen, T.F.McCall Amoco and coking Technologya process forInhibiting coking pyrolysis furnaces April 17-21 1994], [R.E.Blown, phillips pyro co, L.E.Greenwood Phillips pyro co, G, J.CallejasPhillips pyro co, C.Berliner, The.M.W.Kellogg co TechnollogyforApplication in Ethylene Plant], [Youdong Tong ABB Lummus Globae 9thEthylene Technollogy Seminer June 14-17 1998].
Except injecting in raw material the suppressant additive, United States Patent (USP) 4962264 also discloses and applied rare earth element such as Ce, La etc. on inside pipe wall, generates the scale suppression coating, as metal protective film.
Russ P RU 2119524 discloses a series of basic metal inorganic salt has been added the scission reaction system, the catalytic gasification coking, and unique addition means is provided.
In China, in ethylene producing device, the technical study at cracking high-temperature area use coking inhibitor still is in laboratory scale at present.In order to guarantee full scale plant running period, regulate from operational condition and material choice aspect.Therefore, limit effective throughput of device to a certain extent, lost some product yields, or give up some useful raw materials, caused total economic benefit to reduce.
The inventor is at problems of the prior art, through experimental study discovery chronically, in the ethylene producing device system, add the additive that stops coking parent (Jiao Yuan) coking, the one side passivating metallic surfaces, make burnt body particle be difficult to be attached on the wall, can also divide simultaneously and defocus the body size distribution, change the form of coking body, make fine and close spheroidal graphite shape Jiao become unformed or thread Jiao, thereby be convenient to burn off and cleaning, reduced coke cleaning consumption, prolonged the life-span of equipment operation time and equipment.
Therefore, the purpose of this invention is to provide a kind of coking suppressant additive, a kind of ethylene producing device cracking furnace pipe and quenching boiler coke suppressant additive of being used for particularly is provided.
Another object of the present invention provides a kind of method of using the coking suppressant additive to suppress coking.
The coking suppressant additive that the present invention uses, a kind of is that code name CI853 is phosphorous and organic double compound (I type) amine, another kind is that code name CI954 is sulfur-bearing phosphamidon and alkali-metal organic double compound (II type).Its structure expression is respectively:
In I formula and the II formula:
R
1-R
5Represent alkyl respectively, wherein R
1, R
2And R
4Represent that respectively carbon atom is the alkyl of 1-22, preferred carbonatoms is the alkyl of 3-20, and more preferably carbonatoms is the alkyl of 5-15;
R
3And R
5Represent that respectively carbonatoms is the alkyl of 2-20, preferred carbonatoms is the alkyl of 5-18, and more preferably carbonatoms is the alkyl of 8-13;
Me is selected from least a basic metal or its combination of lithium, sodium, potassium, rubidium, caesium;
The basic metal degree of neutralization is less than the sixth of hydroxyl value in the organic double compound molecule;
The acid amides radix is at least 1/3rd of hydroxyl value in the organic double compound molecule.
The example that presses down burnt additive of the present invention comprises: for example the I type has:
[nC
4H
9PO(C
4H
9O)N(C
2H
5)
3]·[nC
4H
9PO(C
4H
9O)
2]
[CH
3PO(C
7H
15O)N(C
3H
7)
2]·[CH
3PO(C
7H
15O)
2]
[C
2H
5PO(C
5H
11O)NHC
4H
9]·[C
2H
5PO(C
5H
11O)
2]
[C
8H
17PO(C
8H
17O)N(C
2H
5)
3]·[C
8H
17PO(C
8H
17O)
2]
[C
8H
17PO (C
8H
17O) NC
4H
9O] [C
8H
17PO (C
8H
17O)
2] etc.;
The II type has:
[C
8H
17PS(C
8H
17S)N(C
2H
5)
3]·[C
8H
17PS(SK)(C
8H
17O)]
[C
5H
11PS(C
5H
11S)N(C
3H
7)
2]·[C
5H
11PS(SK)(C
5H
11O)]
[C
2H
5PS(C
5H
11S)N(C
3H
7)
2]·[C
2H
5PS(SNa)(C
5H
11O)]
[nC
4H
9PS (C
4H
9S) N (C
2H
5)
3] [nC
4H
9PS (SK) (C
4H
9O)] etc.
But of the present invention burnt additive is yellow and amber oily transparent liquid, contains phosphino-, amide group and basic metal group.The I type is a kind of organic double compound of phosphorous and amine, and the boiling range scope is 151-224 ℃; Density in the time of 20 ℃ is 0.9240; Viscosity in the time of 20 ℃ is 7.41 centistokes(cst)s; Refractive index in the time of 20 ℃ is 1.4790.The II type is a kind of Vitamin B1 Phosphate and alkali-metal organic double compound of containing, and the boiling range scope is 143-233 ℃; Density in the time of 20 ℃ is 0.9300; Viscosity in the time of 20 ℃ is 3.80 centistokes(cst)s; Refractive index in the time of 20 ℃ is 1.4991.
But of the present invention burnt additive is dissolved in organic solvent, and is instant in polar solvent.The example of these organic solvents comprises: alkanes for example, as normal hexane, normal heptane, hexanaphthene and octane-iso etc.; Ethers is as ether, butyl ether and sherwood oil etc.; Ketone is as acetone and pentanone etc.; Alcohols is as ethanol, propyl alcohol, butanols and octanol etc.; Aromatic hydrocarbons is as benzene, toluene, ethylbenzene and dimethylbenzene etc.
Additive add the implantation site, be arranged on the front end of the leap temperature (being the initial action point) of scission reaction, the mouth of pipe bore Φ at decanting point place, be generally 0.5-10mm, be preferably 1.0-8mm, more preferably 1.0-3.0mm, linear speed by total material is designed to the pore shape, and becoming parabolic angle α with logistics, its angle is the 40-50 degree, is preferably the 44-46 degree.The coking at boiler tube and quenching boiler two places can both be inhibited.
Before cracking furnace pipe fed cracking stock, elder generation fed II type additive 1-4 hour with the amount of 0.2 weight %-0.3 weight % of raw material oil mass, and then fed cracking stock.If cracking stock is to be lighter than the petroleum naphtha light hydrocarbon, then continue amount feeding II type additive with 0.02 weight % of raw material oil mass; Overweight the solar oil heavy hydrocarbon if cracking stock belongs to, then the amount with 0.02 weight % of raw material oil mass continues to feed I type additive.
Test is carried out on the simulation cracker, and the processing power of simulator is a 3Kg/h stock oil.Simulator can be simulated the working condition of industrial crack device more widely, as type pyrolyzer such as SRT-I-SRT-V, GK-V, USC, and by the association of coking kinetics, prediction full scale plant situation.The block diagram of the breaking test of simulator is shown in Fig. 1.
In Fig. 1,1 expression convection zone, 2 expression pyrolyzer radiation sections, 3 expression quenching boilers, 4 expression oil scrubbers, 5 expression stock oils, 6 expression dilution steam generations, 7 expressions add the equipment of inhibitor, 8 expression crossover points.
Fig. 2 represents that schematically inhibitor adds the angle that Inbound is become with the Flow of Goods and Materials direction.
Test petroleum naphtha, solar oil and the tail oil of used cracking stock aromatic index (BMCI) value at 9-40.Survey the burnt cycle, petroleum naphtha 10-12 hour, diesel oil and tail oil 8-10 hour.Burnt amount quantitatively after the employing running finishes, is measured coke and is changed into CO and CO
2Amount come quantitatively.Test used stock oil performance, see Table 1.Process of the test and result are as follows.
Comparative example 1
Test cracking stock solar oil BMCI value 39, proportion D
15.560.8100, simulate industrial SRT-II type pyrolyzer processing condition, 0.45 second residence time, thinning ratio 0.75,780 ℃ of coil outlet temperatures, do not add any additive that presses down, move 8 hours, at the end, recording the tube coking amount is 2235ppm (stock oil weight relatively).
Embodiment 1
Raw material and the control condition identical with comparative example 1, the I type additive 200ppm of continuous injection weight of oil in service (stock oil weight relatively) is with the 1 identical time of operation of comparative example.During rundown, recording the tube coking amount is 386ppm (stock oil weight relatively), compares with comparative example 1, and burnt amount has reduced 82.73%.
Raw material and the control condition identical with comparative example 1, continuous injection II type additive 200ppm in service (stock oil weight relatively) moves 8 hours.During rundown, recording the tube coking amount is 357ppm (stock oil weight relatively), compares with comparative example 1, and burnt amount reduces 84.02%.Comparative example 2
Industrial crack raw material petroleum naphtha BMCI value 11.19, proportion D
15.560.7260, simulate industrial SRT-III type pyrolyzer processing condition, 0.35 second residence time, 840 ℃ of coil outlet temperatures, thinning ratio 0.50, do not add any additive that presses down, move after 12 hours, record tube coking amount 281ppm (relative stock oil weight); Quenching boiler coke amount 59.0ppm (stock oil weight relatively).
Raw material and the control condition identical with comparative example 2, continuous injection II type additive 200ppm in service (stock oil weight relatively) move after 12 hours, recorded tube coking amount 218ppm (relative stock oil weight); Quenching boiler coke amount 24.ppm (stock oil weight relatively).With comparative example 2 contrasts, boiler tube reduces coking 22.42%, and quenching boiler coke reduces 59.33%.
Raw material and the control condition identical with comparative example 2, drop into before the raw material, feed the II type additive of the 0.02 weight % amount of raw material oil mass earlier, drop into cracking stock oil after 2 hours, and the continuous simultaneously II type additive 100ppm (stock oil weight relatively) that injects, after moving at 12 o'clock, recording the tube coking amount is 189ppm (stock oil weight relatively); The quenching boiler coke amount is 8.0ppm (a stock oil weight relatively).Compare with comparative example 2, the tube coking amount has reduced 32.73%; The quenching boiler coke amount has reduced 86.44%.Comparative example 3
Industrial cracking stock solar oil BMCI14.94, proportion D
15.560.8138, simulate industrial SRT-III type pyrolyzer processing condition, 0.35 second residence time, 820 ℃ of coil outlet temperatures, thinning ratio 0.75, do not add any suppressant additive, move after 8 hours, recording the tube coking amount is 109ppm (stock oil weight relatively); The quenching boiler coke amount is 27.6ppm (a stock oil weight relatively).
Embodiment 5
Raw material and the control condition identical with comparative example 3, continuous injection I type additive in service are 200ppm (stock oil weight relatively), moves after 8 hours, and recording the tube coking amount is 65Mppm (relative stock oil weight); The quenching boiler coke amount is 11ppm (a stock oil weight relatively).Compare with comparative example 3, the tube coking amount has reduced 40.36%; The quenching boiler coke amount has reduced 60.30%.
Raw material and the control condition identical with example 5, with example 4 described identical pretreatment processs, inject I type additive 200ppm (stock oil weight relatively) continuously, move after 8 hours, recording the tube coking amount is 52ppm (stock oil weight relatively), and the quenching boiler coke amount is 8.8ppm (a stock oil weight relatively).Relatively example 3 tube coking amounts have reduced 50.1%; The quenching boiler coke amount has reduced 74.85%.Comparative example 4
Industry decompression diesel oil (tail oil) BMCI9.34, proportion D
15.560.8460, simulate industrial SRT-IV type pyrolyzer processing condition, 0.30 second residence time, 823 ℃ of coil outlet temperatures, rare ratio 0.80, do not add any additive place that presses down, move 8 hours.During rundown, recording the tube coking amount is 127ppm (raw material oil mass relatively); The quenching boiler coke amount is 24ppm (a raw material oil mass relatively).
Raw material and the control condition identical with comparative example 4, continuous injection II type additive 200ppm in service (stock oil weight relatively) move after 8 hours, and recording the tube coking amount is 85ppm (relative stock oil weight); The quenching boiler coke amount is 8.0ppm (a stock oil weight relatively), compares with comparative example 4, and the tube coking amount has reduced 33.07%; The quenching boiler coke amount has reduced 66.67%.
Raw material and the control condition identical with comparative example 4, with example 4 described identical treatment processs, inject II type additive 200ppm (stock oil weight relatively) continuously, move after 8 hours, record tube coking amount 68.5ppm (stock oil weight relatively), quenching boiler coke amount 6.5ppm (stock oil weight relatively) compares with comparative example 4, and the tube coking amount has reduced 41%; The quenching boiler coke amount has reduced 82.67%.
The model of injecting additive continuously is generally relevant with the raw material composition, and I type additive is applicable to that sulphur content is higher than the 200ppm heavy distillate, and II type additive is applicable to light ends oil and the heavy secondary processing oil that sulphur content is lower.
Use the sample result of inhibitor comprehensive more as shown in table 2.
Table 1 test cracking stock rerum natura
| The performance raw material | The industry solar oil | Industrial naphthas | Industry decompression diesel oil | The test solar oil | ||
| Proportion D 15.56℃ | 0.8138 | 0.7260 | 0.8462 | 0.8224 | ||
| Molecular-weight average wt | 230 | 120 | 454 | 200 | ||
| Sulphur content (wt%) | 330 | 170 | 620 | 135 | ||
| Flow process v% ℃ | Initial boiling point | 209 | 44.5 | 375 | 130 | |
| 10 | 234 | 77 | 429 | 135 | ||
| 30 | 258 | 105 | 467 | 155 | ||
| 50 | 284 | 123 | 477 | 185 | ||
| 70 | 314 | 137 | 488 | 220 | ||
| 90 | 364 | 153 | 498 | 255 | ||
| Do | 370 | 254 | 525 | 350 | ||
| Aromatic index BMCI | 14.94 | 11.19 | 9.34 | 39.00 | ||
| Group composition wt% | Paraffinic hydrocarbons | 88.75 | 59.99 | 95.57 | 63.84 | |
| Naphthenic hydrocarbon | 34.47 | |||||
| Aromatic hydrocarbons | 11.25 | 5.64 | 4.43 | 36.16 | ||
Table 2. test-results
| The test sequence number | Raw material | Temperature of reaction ℃ | The second residence time | Thinning ratio wt/wt | The additive model | The relative raw material of additive capacity ppm | The burnt amount of effect reduces wt% | |
| Boiler tube | Boiler | |||||||
| Comparative example 1 | The test solar oil | 780 | 0.45 | 0.75 | - | 0 | 0 | |
| Example 1 | The test solar oil | 780 | 0.45 | 0.75 | The I type | Continuous 200 | 82.73 | |
| Example 2 | The test solar oil | 780 | 0.45 | 0.75 | The I type | Continuous 200 | 84.02 | |
| Comparative example 2 | Industrial naphthas | 840 | 0.35 | 0.50 | - | 0 | 0 | 0 |
| Example 3 | Industrial naphthas | 840 | 0.35 | 0.50 | The II type | Continuous 200 | 22.42 | 59.33 |
| Example 4 | Industrial naphthas | 840 | 0.35 | 0.50 | II type II type | During | 32.73 | 86.44 |
| Comparative example 3 | The industry solar oil | 820 | 0.35 | 0.75 | - | 0 | 0 | 0 |
| Example 5 | The industry solar oil | 820 | 0.35 | 0.75 | The I type | Continuous 200 | 40.36 | 60.30 |
| Example 6 | The industry solar oil | 820 | 0.35 | 0.75 | II type I type | During | 50.10 | 74.85 |
| Comparative example 4 | The industry tail oil | 823 | 0.30 | 0.80 | - | 0 | 0 | 0 |
| Example 7 | The industry tail oil | 823 | 0.30 | 0.80 | The II type | Continuous 200 | 33.07 | 66.67 |
| Example 8 | The industry tail oil | 823 | 0.30 | 0.80 | II type II type | During | 41.0 | 82.67 |
The above embodiments only are to be used for further describing the present invention, make it can understand the present invention better.Under the situation that does not deviate from spirit of the present invention, modification or improvement that those skilled in the art can make the present invention, all within the scope of the invention.Scope of the present invention proposes in the appended claims in the back.
Claims (14)
1. an inhibition, reduce or get rid of the method for petroleum cracking system ethylene unit cracking furnace pipe and quenching boiler coke, it is characterized in that being added on the described device suppressing the coking additive, described additive is that the phosphorous of I type is to contain Vitamin B1 Phosphate and alkali-metal organic double compound with amine organic double compound and/or II type, and their structure expression is respectively:
I type: the organic double compound of phosphorous and amine:
II type: sulfur-bearing phosphamidon and alkali-metal organic double compound:
In above-mentioned two formulas:
R
1, R
2And R
4Be respectively the alkyl that carbonatoms is 1-22;
R
3And R
5Represent that respectively carbonatoms is the alkyl of 2-20;
Me represents to be selected from least a basic metal of lithium, sodium, potassium, rubidium or caesium;
The basic metal degree of neutralization is less than the sixth of hydroxyl value in the organic double compound molecule;
The acid amides radix is at least 1/3rd of hydroxyl value in the organic double compound molecule.
2. by the described method of claim 1, it is characterized in that pressing down R in the burnt additive
1, R
2And R
4Representing carbonatoms respectively is the alkyl of 3-20.
3. by the described method of claim 2, it is characterized in that pressing down R in the burnt additive
1, R
2And R
4Representing carbonatoms respectively is the alkyl of 5-10.
4. by the described method of claim 1, it is characterized in that pressing down R in the burnt additive
3And R
5Representing carbonatoms respectively is the alkyl of 5-18.
5. by the described method of claim 4, it is characterized in that pressing down R in the burnt additive
3And R
5Representing carbonatoms respectively is the alkyl of 8-13.
6. by the described method of claim 1, it is characterized in that pressing down burnt additive and be selected from [nC
4H
9PO (C
4H
9O) N (C
2H
5)
3] [nC
4H
9PO (C
4H
9O)
2], [CH
3PO (C
7H
15O) N (C
3H
7)
2] .[CH
3PO (C
7H
15O)
2], [C
2H
5PO (C
5H
11O) NHC
4H
9] [C
2H
5PO (C
5H
11O)
2], [C
8H
17PO (C
8H
17O) N (C
2H
5)
3] [C
8H
17PO (C
8H
17O)
2], [C
8H
17PO (C
8H
17O) NC
4H
9O] [C
8H
17PO (C
8H
17O)
2], [C
8H
17PS (C
8H
17S) N (C
2H
5)
3] [C
8H
17PS (SK) (C
8H
17O)], [C
5H
11PS (C
5H
11S) N (C
3H
7)
2] [C
5H
11PS (SK) (C
5H
11O)], [C
2H
5PS (C
5H
11S) N (C
3H
7)
2] [C
2H
5PS (SNa) (C
5H
11O)], [nC
4H
9PS (C
4H
9S) N (C
2H
5)
3] [nC
4H
9PS (SK) (C
4H
9O)] at least a in.
7. by the described method of claim 1, it is characterized in that pressing down burnt additive and after being dissolved in organic solvent, add.
8. by the described method of claim 7, it is characterized in that organic solvent is selected from least a in alkanes, ethers, ketone, alcohols, the aromatic hydrocarbons.
9. by the described method of claim 1, it is characterized in that I type and/or II type press down burnt additive in cracker adding in service.
10. by the described method of claim 1, it is characterized in that before the scission reaction pipe drops into cracking stock, the II type is pressed down burnt additive fed the 1-4 of system hour, after feeding cracking stock, be accompanied by material feeding I type or II type and press down burnt additive.
11. by the described method of claim 1, it is characterized in that pressing down burnt additive is to add at the continuous inlet that presses down burnt additive that is arranged on reaction initial action point front end.
12. by the described method of claim 1, it is characterized in that pressing down burnt additive is to add with the linear velocity identical with the material that adds point.
13. by the described method of claim 1, it is characterized in that the amount of relative cracking stock, adding the amount that presses down burnt additive is 50ppm-400ppm.
14. by the described method of claim 1, it is characterized in that pressing down burnt additive, to be used for gaseous alkanes, petroleum naphtha, solar oil or decompression diesel oil be the cracking system of raw material.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99119353A CN1090668C (en) | 1999-09-10 | 1999-09-10 | Coking inhibiting method for ethylene cracker |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99119353A CN1090668C (en) | 1999-09-10 | 1999-09-10 | Coking inhibiting method for ethylene cracker |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1247887A CN1247887A (en) | 2000-03-22 |
| CN1090668C true CN1090668C (en) | 2002-09-11 |
Family
ID=5280848
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN99119353A Expired - Fee Related CN1090668C (en) | 1999-09-10 | 1999-09-10 | Coking inhibiting method for ethylene cracker |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1090668C (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7425259B2 (en) * | 2004-03-09 | 2008-09-16 | Baker Hughes Incorporated | Method for improving liquid yield during thermal cracking of hydrocarbons |
| CN1305786C (en) * | 2004-08-13 | 2007-03-21 | 北京斯伯乐科学技术研究院 | Antisludging agent used in cracking gas compressor in an ethylene apparatus and its using method |
| CN100352899C (en) * | 2005-10-11 | 2007-12-05 | 杭州市化工研究院有限公司 | Ethene compressor cleaning media |
| CN101161785B (en) * | 2006-10-12 | 2011-06-15 | 中国石油化工股份有限公司 | Method for suppressing coking and carbonizing for hydrocarbons steam cracking unit |
| CN101294100B (en) * | 2007-04-28 | 2012-05-30 | 中国石油化工股份有限公司 | Method for inhibiting hydrocarbons steam cracking furnace from coking |
| CN101318872B (en) * | 2008-07-22 | 2010-12-15 | 北京斯伯乐科学技术研究院 | Ethylene cracking furnace coking restrainer and its use method |
| CN104560106A (en) * | 2013-10-15 | 2015-04-29 | 中国石油化工股份有限公司 | Inhibitor and device for slowing down coking of ethylene cracking furnace pipe, and application method |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4962264A (en) * | 1989-10-23 | 1990-10-09 | Betz Laboratories, Inc. | Methods for retarding coke formation during pyrolytic hydrocarbon processing |
| CN1157006A (en) * | 1994-09-05 | 1997-08-13 | 国际壳牌研究有限公司 | Process for thermal cracking of residual hydrocarbon oil |
| CN1218095A (en) * | 1997-11-24 | 1999-06-02 | 中国石油化工总公司 | Coking and scaling inhibitor and preparation and use thereof |
-
1999
- 1999-09-10 CN CN99119353A patent/CN1090668C/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4962264A (en) * | 1989-10-23 | 1990-10-09 | Betz Laboratories, Inc. | Methods for retarding coke formation during pyrolytic hydrocarbon processing |
| CN1157006A (en) * | 1994-09-05 | 1997-08-13 | 国际壳牌研究有限公司 | Process for thermal cracking of residual hydrocarbon oil |
| CN1218095A (en) * | 1997-11-24 | 1999-06-02 | 中国石油化工总公司 | Coking and scaling inhibitor and preparation and use thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1247887A (en) | 2000-03-22 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1090668C (en) | Coking inhibiting method for ethylene cracker | |
| BR112012023845A2 (en) | process for converting lignin into liquid hydrocarbons | |
| CN101037618A (en) | Coking inhibitor and preparation method and application thereof | |
| CN1827744A (en) | Method for processing crude oil with high acid value | |
| BRPI0619740A2 (en) | process to produce a branched hydrocarbon component | |
| CN1304534C (en) | Inhibition of viscosity increase and fouling in hydrocarbon streams including unsaturation | |
| EP2716741A1 (en) | C heavy oil composition and method for producing same | |
| US3979279A (en) | Treatment of lube stock for improvement of oxidative stability | |
| RU2213125C1 (en) | Process of production of environmentally safe low-viscosity marine engine fuel | |
| CN1267536C (en) | Desulfurizing method for distillate | |
| RU2149888C1 (en) | Method for production of low-viscosity marine fuel | |
| CN102500140B (en) | High temperature resistant defoamer for delaying coking reaction tower | |
| US2417415A (en) | Hydrocarbon treatment | |
| CN1990839A (en) | Lubricating oil oxidation stability additive composition and preparation method thereof | |
| JP5116966B2 (en) | gasoline | |
| US20140213836A1 (en) | Thermal cracking of impurities in triglyceride mixtures | |
| CN100338191C (en) | Anti-coking agent, and its preparation and use method | |
| US3370010A (en) | Mineral lubricating oil containing polymer having anti-wear properties | |
| Barber et al. | The Role of Lubricant Additives in Controlling Abnormal Combustion (ORI) | |
| WO2019129626A1 (en) | Method for reducing fouling in catalytic cracking | |
| CN85109037A (en) | Improved selective vaporization process | |
| CN110607188B (en) | Pretreating agent and pretreating method for heavy oil fluidized processing raw material | |
| CA1258245A (en) | Process for the preparation of gasoline | |
| CN103897790A (en) | Air compressor oil and preparation method thereof | |
| Hancock et al. | A chemista [euro][TM] s perspective on organic fouling in ethylene operations |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20020911 Termination date: 20170910 |