CN1560198A - Additive for enhancing and delaying light oil recovery rate of coke apparatus - Google Patents
Additive for enhancing and delaying light oil recovery rate of coke apparatus Download PDFInfo
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Abstract
The invention is an additive of increasing the light oil yield of a delayed coking device and its preparing method, and its composition in weigh share: thermolysis active substance 10-20 portion, free-group chain reaction inhibitor 30-40, anticoking agent 20-30, and solvent 10-20. The preferred composition in weight portion: thermolysis active substance 13-17 portions, free-group chain reaction inhibitor 34-38, anticoking agent 23-26 shares, and solvent 13-18.
Description
Technical Field
The invention belongs to the field of oil refining additives, and relates to an additive for improving the yield of light oil of a delayed coking device.
Technical Field
Delayed coking is a process for converting residual oil into gas, light and medium distillates and coke by deep thermal cracking, and is used in oil refinery to increase the yield of light oil and produce petroleum Coke (CH)xWherein x<1). Compared with catalytic cracking, the method has the advantages of less equipment investment, simple production process, low operation cost and the like.
The delayed coking unit is one of the main units for light oil processing in oil refinery, and the improvement of the yield of light oil in the unit is an important target for the technical improvement. For increasing the economic efficiency of delayed coking unitsThe key point is to reduce coke and dry gas (C)1And C2Hydrocarbon) and increase in the yield of liquid product, i.e., light oil (liquid recovery for short). For a long time, the yield of light oil has been increased at home and abroad from the following two aspects: (1) the residual oil is hydrogenated and then coked, the method not only can greatly improve the liquid yield, but also can improve the product quality, but the investment and the operation cost of the method are too high and are not feasible economically. (2) Optimizing operation conditions, such as the American continental oil company, improving the liquid yield by four operation measures of reducing the circulation ratio, reducing the pressure, improving the temperature and deeply drawing residual oil, but the method has the limitation of improving the liquid yield, and the liquid yield can only be improved by 1 percent on the original basis.
Various additives are added into raw material residual oil, so that the generation of coke and dry gas is reduced, and the method is the simplest, most convenient and most economical method for improving liquid yield. At present, no research and application report for improving the liquid yield by using additives in the delayed coking process exists at home and abroad.
Disclosure of Invention
In view of the above-mentioned drawbacks of the prior art, it is an object of the present invention to provide a special additive which is directly added to a raw material for delayed coking to improve the yield of a liquid oil product by suppressing the generation of coke and dry gas. Another object of the present invention is to provide a process for the preparation of such additives.
The purpose of the invention is realized by the following technical scheme.
The additive provided by the invention comprises the following components:
10-20 parts by weight of a thermal cracking active substance,
30-40 parts of free radical chain reaction inhibitor,
20-30 parts by weight of an anti-coking agent,
10-20 parts of solvent.
Preferably:
13-17 parts by weight of a thermal cracking active substance,
34-38 parts of free radical chain reaction inhibitor,
23-26 parts by weight of an anti-coking agent,
13-18 parts of solvent.
The thermal cracking active substance is a common thermal cracking active substance; preferably block polyether block copolymerized by polyoxyethylene and polyoxypropylene having molecular weight of 5000-12000, C8-C12Alkylphenol polyoxyethylene ether sulfonate or sorbitan polyoxyethylene ether sulfonate.
The radical chain reaction inhibitor is a general radical chain reaction inhibitor, preferably pentaerythritol tetrakis [ β - (3, 5-di-tert-butyl-4-hydroxyphenyl) propionate], octadecyl β - (3, 5-di-tert-butyl-4-hydroxyphenyl) propionate, N-phenyl- α naphthylamine, didodecyldiphenylamine, styryl octyldiphenylamine, or phenyl phosphite.
The anti-coking agent is a common anti-coking agent; preferred are sulfenamides (structural formula shown below)(wherein R is1、R2、R3Are all C8-C12Alkyl group of (1), C6-C10Alkylated phenols, 2, 6-di-tert-butyl-p-cresol, styrenated phenol or N-nitroso-phenyl- β -naphthylamine.
The solvent is an organic solvent; preferably kerosene or diesel.
The basic principle of improving liquid yield is as follows:
when residual oil is subjected to delayed coking, the following complex and parallel network reactions occur
The above thermal cracking reaction can be described by a free radical chain reaction mechanism:
(1) initiation of the chain
First homolytic cracking of hydrocarbon molecules under heated conditions to form free radicals
(2) Development of chains
(3) Decomposition of free radicals
The free radicals can decompose to form olefin molecules and new free radicals, the decomposition occurring at the β bond position of the carbon atom with the unpaired electron, for example:
the yield of dry gas in the thermal cracking products is higher than that in the catalytic cracking.
(4) Chain termination
The synthesized high molecular active substance is added, and can interact with unpaired electrons to enable free radicals to generate homolytic reaction, thereby reducing the generation of cracking gas.
The coke formation is a combination of thermal decomposition and condensation reactions, and the mechanism is:
(1) chain initiation
(2) Chain development
Under the catalysis of trace oxygen and transition metal:
(3) asphaltene, coke formation
The asphalt base is prepared by removing H from asphaltene+The latter substance.
The asphalt is a hydrocarbon compound and is a black viscous liquid, semi-liquid or solid substance mainly comprising asphaltene and resin.
The asphaltene is a polycyclic aromatic hydrocarbon containing oxygen, nitrogen and sulfur heteroatoms, and has specific gravity and carbon-hydrogen ratio higher than those of colloid.
The colloid is polycyclic or condensed aromatic hydrocarbon compound containing oxygen, nitrogen and sulfur heteroatoms, has an average molecular weight of 600-800, and is a semi-liquid colloid substance with reddish brown to dark brown.
The synthesized polymer active substance can also react with peroxide (ROOH) to stop the chain reaction, thereby reducing the generation of coke.
The additive only changes the product distribution in the delayed coking process, and does not change the distillation range, density, hydrocarbon cluster composition, carbon residue and other quality indexes of liquid products such as gasoline, diesel oil, wax oil (hydrocarbons with the boiling point higher than 500 ℃ and higher than 350 ℃), and the like. The additive is an oil-soluble organic compound, and has no influence on subsequent processing processes such as coking gasoline, coking diesel oil hydrofining, coking wax oil catalytic cracking, coking wax oil catalytic hydrogenation and the like.
The invention also provides a preparation method of the additive. The preparation method comprises the following steps: adding a solvent into an enamel stirring reaction kettle, slowly heating to 60-110 ℃ within 1-2 hours, then sequentially adding a thermal cracking active substance, a free radical chain reaction inhibitor and an anti-coking agent according to a proportion, stirring for reaction for 1-2 hours, cooling, and filtering to remove solid impurities to obtain a finished product.
The additive is used in industrial production, and is added into the raw material of delayed coking, and the addition amount of the additive is 100-500 ppm; preferably 100-300 ppm; more preferably 300 ppm.
The additive provided by the invention is used, and the industrial test of a delayed coking device with annual treatment capacity of 100 ten thousand tons shows that the yield of light oil can be improved by 3-5%. The additive provided by the invention is used in the delayed coking, and has the advantages of simple operation, low cost, high liquid yield and high economic benefit.
Drawings
FIG. 1 is a delayed coking simulation industrialization testing device
The reference numbers illustrate: 1-a water vapor generator; 2-a residuum storage tank; 3-plunger metering pump; 4-steam regulating valve; 5-a water vapor flow meter; 6-residual oil flow regulating valve; 7-heating furnace temperature controller; 8-oil residue tank; 9-heating a furnace tube; 10-heating furnace; 11-furnace outlet temperature recorder; 12-a coke drum; 13-a condenser; 14-coking product receiver
Detailed Description
Example 1
1700g of kerosene is firstly added into an enamel stirring reaction kettle, the temperature is slowly raised to 80 ℃ within 1.5 hours, then 1650g of sorbitan polyoxyethylene ether sulfonate, 3500g of styryl octyl diphenylamine and 2500g of 2, 6-di-tert-butyl p-cresol are sequentially added, the stirring reaction is carried out for 2 hours, and the finished product is obtained after cooling and filtering to remove solid impurities.
Example 2
1600g of diesel oil is firstly added into an enamel stirring reaction kettle, the temperature is slowly raised to 80 ℃ within 1.5 hours, then 1600g of block polyether of polyoxyethylene and polyoxypropylene block copolymerization with molecular weight of 7000, 3600g of pentaerythrityl tetrakis [ β - (3, 5-di-tert-butyl-4-hydroxyphenyl) propionate]and 2550g of styrenated phenol are sequentially added, the stirring reaction is carried out for 80 minutes, the cooling is carried out, and the solid impurities are removed by filtering, thus obtaining the finished product.
Example 3
1800g of kerosene is added into an enamel stirring reaction kettle, the temperature is slowly raised to 70 ℃ within 2 hours, then 1850g of octyl phenol polyoxyethylene ether sulfonate, 3900g of β - (3, 5-di-tert-butyl-4-hydroxyphenyl) octadecyl propionate and 2700g N-nitroso-phenyl- β -naphthylamine are sequentially added, the stirring reaction is carried out for 1.5 hours, and the finished product is obtained after cooling and filtering to remove solid impurities.
Example 4
Adding 1900g of diesel oil into an enamel stirring reaction kettle, slowly heating to 100 ℃ within 2 hours, then sequentially adding 1900g of block polyether of polyoxyethylene and polyoxypropylene block copolymer with the molecular weight of 10000, 3850g of didodecyldiphenylamine and 2950g of octylated phenol, stirring for reacting for 100 minutes, cooling, and filtering to remove solid impurities to obtain the finished product.
Example 5
Firstly 1350g of kerosene is added into an enamel stirring reaction kettle, the temperature is slowly raised to 90 ℃ within 80 minutes, and then 1450g of decyl phenol polyoxyethylene ether sulfonate, 3400g N-phenyl- α naphthylamine and 2450g of decyl phenol polyoxyethylene ether sulfonate are sequentially added(wherein R is1Is octyl, R2Is undecyl, R3Octyl), stirring and reacting for 80 minutes, cooling, and filtering to remove solid impurities to obtain the finished product.
Example 6
1100g of diesel oil is firstly added into an enamel stirring reaction kettle, the temperature is slowly raised to 80 ℃ within 70 minutes, and then 1200g of undecyl phenol polyoxyethylene ether sulfonic acid ester, 3200g of phenyl phosphite ester and 2150g of phenyl phosphite ester are sequentially added
(wherein R is1Is decyl, R2Is decyl, R3Nonyl) to react for 1.5 hours under stirring, and then the finished product is obtained after cooling and filtering to remove solid impurities.
Example 7 (delayed coking simulation industrialization test)
a. A delayed coking simulation industrialized test device is shown in attached figure 1.
b. Main apparatus and equipment
Serial number name model/specification origin
Self-made stainless steel phi 400 x 400 of 1 water vapor generator
Built-in electric heating rod
2 residual oil storage tank phi 200X 200 stainless steel cylindrical container self-made
3 plunger metering pump J-10/63/50 Hangzhou river stoning device
Standby Ltd
4 heating furnace temperature controller SR25-IP-N-060000 Tokyo Japan
5 heating furnace tube phi 4 stainless steel self-made
6 heating furnace Sk-2-3-10 Shenyang electric furnace factory
7 furnace outlet temperature recorder LM14-204 Shanghai Dahua instrument factory
Self-made 8 coking tower phi 200X 1000 stainless steel
9 condenser phi 10 x 500 glass self-made
c. Test Process conditions
The blank test and the test using the additive both adopt the following operating conditions:
1) the charging temperature of the residual oil is 100 +/-1 DEG C
2) The temperature of the heating furnace is 590 +/-2 DEG C
3) Residual oil tapping temperature of 496 +/-2 DEG C
4) Steam injection 2% (mass flow of residual oil)
5) The flow rate of the residual oil in the furnace tube is 1.3(m/s) (at the charging temperature of the residual oil)
6) Furnace tube diameter 4(mm) (inner diameter)
7) Residual oil flow 1.0(L/min)
d. Test procedure
1) Starting the electric heating furnace, adjusting the temperature of the temperature controller to be 590 ℃, and adjusting the heating speed to be 10-20 ℃/min;
2) opening a tracing band of a residual oil storage tank, and controlling the temperature of residual oil to be 100 ℃;
3) starting a residual oil metering pump until the residual oil flow reaches a stable value;
4) starting a water vapor generator, controlling the temperature to be 200 ℃, and regulating the flow by using an emptying valve to enable the flow of water vapor to reach 20 mL/min;
5) opening a residual oil flow valve;
6) recording the outlet temperature of the residual oil, keeping the outlet temperature of the residual oil at 496 ℃, and if the outlet temperature of the residual oil is not at the temperature, adjusting the temperature of the heating furnace to enable the outlet temperature of the residual oil to reach the temperature;
7) cutting gasoline fraction at a temperature of less than 205 ℃, diesel oilfraction at a temperature of 206-330 ℃ and wax oil fraction at a temperature of 331-350 ℃;
8) residual oil consumption was calculated from the loss in weight in the residual oil storage tank, coke amount was weighed, and gas yield was calculated according to the following formula:
gas yield-residual oil consumption-gasoline quantity-diesel oil quantity-wax oil quantity-coke quantity
The amounts are all by weight.
9) When the additive is used for testing, the additive is added into a residual oil storage tank according to 300ppm, is uniformly stirred, and then the testing is carried out according to the steps.
e. Test materials
The test feed was vacuum residue and its physical properties are shown in the table below.
| Item | Relative density Degree (d)4 20) | Freezing point (℃) | Residual carbon material Percentage by weight Content (wt.) (％) | Mass C Is composed of Measurement of (％) | Mass of H Is composed of Measurement of (％) | Mass of S Is composed of Measurement of (％) | Mass of N Is composed of Measurement of (％) | Quality of Ni Is composed of Measurement of (ppm) | V mass Is composed of Measurement of (ppm) |
| Results | 0.9546 | 36 | 14.8 | 86.4 | 112 | 0.9 | 05 | 67 | 4.6 |
f. Blank test (no additive) results
Two blank tests were performed and the results are shown in the table below.
| Raw materials Quality of (g) | Gasoline (gasoline) | Diesel oil | Wax oil | Coke | Gas (es) | Total liquid Yield (%) | |||||
| Yield of the product (g) | Yield of (％) | Yield of the product (g) | Yield of (％) | Yield of the product (g) | Yield of (％) | Yield of the product (g) | Yield of (％) | Yield of the product (g) | Yield of (％) | ||
| 202 | 14.9 | 7.38 | 80.3 | 39.75 | 38.3 | 18.96 | 54.21 | 26.8 | 14.4 | 7.13 | 66.09 |
| 980 | 71.1 | 7.25 | 390.4 | 39.84 | 187.4 | 19.12 | 259.7 | 26.5 | 71.4 | 7.29 | 66.21 |
g. Tests with additives
Two tests were carried out with 300ppm of additive under the same operating conditions as the blank, and the results are given in the following table.
| Raw materials Quality of (g) | Gasoline (gasoline) | Diesel oil | Wax oil | Coke | Gas (es) | Total liquid Yield (%) | |||||
| Yield of the product (g) | Yield of (％) | Yield of the product (g) | Yield of (％) | Yield of the product (g) | Yield of (％) | Yield of the product (g) | Yield of (％) | Yield of the product (g) | Yield of (％) | ||
| 200 | 15.6 | 7.80 | 85.7 | 42.85 | 41.4 | 20.70 | 51.4 | 25.70 | 5.9 | 2.95 | 71.35 |
| 994 | 77.7 | 7.82 | 426.5 | 42.91 | 205.2 | 20.64 | 255.2 | 25.67 | 29.4 | 2.96 | 71.37 |
From the comparison of the two tables, it can be seen that the total liquid yield (gasoline, diesel oil and wax oil) is increased by about 5% after the additives are added. Wherein, diesel oil is increased by about 3 percent, wax oil is increased by about 1.5 percent, gasoline is increased by about 0.5 percent, gas is reduced by about 4 percent, and coke is reduced by about 1 percent.
h. Effect of additive addition on liquid yield enhancement
| Additives in Amount of (ppm) | Amount of residual oil (g) | Liquid mixing Oil mass (g) | Total liquid yield (％) | Increase of total liquid yield Added value (%) | Coke yield (％) | Gas yield (％) |
| 0 | 994 | 655.2 | 65.92 | 0 | 26.64 | 7.44 |
| 100 | 1022 | 692.8 | 69.79 | 1.87 | 25.53 | 6.68 |
| 200 | 1016 | 704.5 | 69.34 | 3.42 | 25.50 | 5.16 |
| 300 | 994 | 709.4 | 71.37 | 5.45 | 25.70 | 2.96 |
| 500 | 1008 | 718.3 | 71.26 | 5.34 | 25.51 | 3.23 |
As can be seen from the above table, the total liquid yield increased by 1.87% when the additive was added at 100ppm, by 3.42% when the additive was added at 200ppm, by 5.45% when the additive was added at 300ppm, and by no more when the additive was added at 500 ppm.
i. Distillation test results
The simulation tests (including blank tests and additive test) and the distillation tests of the mixed oil from the coking tower are carried out, and the wax oil with the gasoline boiling range of-180 ℃ at the initial boiling point, 180 ℃ for diesel oil and 350 ℃ at the temperature higher than 350 ℃ is cut. The results of the tests are shown in the following table.
| Additive agent Amount of the composition used (ppm) | Mixed oil Quantity (g) | Gasoline quantity (g) | Gasoline recycling device Rate (g) | Gasoline seal Degree g/cm3) | Diesel oil mass (g) | Diesel oil collector Percentage (%) | Density of diesel oil (g/cm3) | Wax oil Quantity (g) | Wax oil recovery Percentage (%) | Loss of distillation Medicine for treating diabetes | Loss of distillation Loss rate (％) |
| 0 | 655.2 | 65.6 | 10.01 | 0.7088 | 194.9 | 29.75 | 0.8764 | 164.6 | 25.12 | 6.81 | 1.04 |
| 100 | 692.8 | 71.1 | 10.26 | 0.7051 | 218.7 | 31.57 | 0.8767 | 172.5 | 24.90 | 7.40 | 1.07 |
| 200 | 704.5 | 72.9 | 10.34 | 0.7067 | 228.9 | 32.49 | 0.8649 | 177.0 | 25.12 | 9.79 | 1.39 |
| 500 | 718.3 | 74.8 | 10.41 | 0.7068 | 248.7 | 34.76 | 0.8788 | 179.2 | 24.59 | 8.19 | 1.14 |
The gasoline yield, diesel yield, wax oil yield and distillation loss in the above tables are calculated for the feedstock residue. As can be seen from the data in the table, the yield of the wax oil is not changed greatly after the additive is used, the yield of the gasoline is slightly increased, and the diesel oil is mainly increased.
j. Chemical composition analysis of coking products
① analysis result of gasoline composition
Gasoline fraction hydrocarbon composition and sulfur and nitrogen content
| Alkane(s) (mass%) | Cycloalkanes (mass%) | Olefins (mass%) | Aromatic hydrocarbons (mass%) | Total up to (mass%) | Sulfur (μg/g) | Nitrogen is present in (μg/g) | |
| Blank space | 37.6 | 8.4 | 34.2 | 19.6 | 99.8 | 1060 | 182 |
| Adding additives Additive agent | 35.8 | 8.1 | 35.1 | 20.7 | 99.7 | 1078 | 194 |
② analysis result of diesel oil composition
Hydrocarbon composition and S/N content of diesel oil fraction
| Alkane(s) (mass%) | Olefins (mass%) | Aromatic hydrocarbons (mass%) | Total up to (mass%) | Sulfur (mass%) | Nitrogen is present in (mass%) | |
| Blank space | 46.3 | 31.6 | 21.7 | 99.6 | 0.32 | 0.13 |
| Adding additives | 45.2 | 32.4 | 22.1 | 99.7 | 0.33 | 0.12 |
③ wax oil composition analysis results
Wax oil fraction composition and sulfur, nitrogen and carbon residue content
| Saturated hydrocarbons (quality) ％) | Aromatic hydrocarbons (mass%) | Colloid plus asphalt Quality of food (mass%) | Total up to (mass%) | Sulfur (mass%) | Nitrogen is present in (mass%) | Carbon residue (mass%) | |
| Blank space | 55.0 | 38.5 | 6.2 | 99.7 | 0.64 | 0.31 | 0.42 |
| Adding additives | 54.9 | 38.3 | 6.4 | 99.6 | 0.62 | 0.34 | 0.46 |
As can be seen from the above tables, the use of the additive has no significant effect on the physicochemical properties of the resulting oil.
Claims (8)
1. An additive for increasing the yield of light oil from a delayedcoker, said additive comprising:
10-20 parts by weight of a thermal cracking active substance,
30-40 parts of free radical chain reaction inhibitor,
20-30 parts by weight of an anti-coking agent,
10-20 parts of solvent.
2. The additive for increasing the yield of light oil from a delayed coker of claim 1, wherein said additive is comprised of:
13-17 parts by weight of a thermal cracking active substance,
34-38 parts of free radical chain reaction inhibitor,
23-26 parts by weight of an anti-coking agent,
13-18 parts of solvent.
3. The additive as claimed in claim 1 or 2, wherein the thermally cleavable active substance is a block polyether of block copolymerization of polyoxyethylene and polyoxypropylene having a molecular weight of 5000-8-C12Any one of alkylphenol polyoxyethylene ether sulfonate and sorbitan polyoxyethylene ether sulfonate;
wherein the free radical chain reaction inhibitor is any one of tetra [ β - (3, 5-di-tert-butyl-4-hydroxyphenyl) propionic acid]pentaerythritol ester, β - (3, 5-di-tert-butyl-4-hydroxyphenyl) propionic acid octadecyl ester, N-phenyl- α naphthylamine, didodecyldiphenylamine, styryl octyl diphenylamine and phenyl phosphite ester;
wherein the anti-coking agent is sulfenamide
(wherein R is1、R2、R3Are all C8-C12Alkyl group of (1), C6-C10Any one of alkylated phenol, 2, 6-di-tert-butyl-p-cresol, styrenated phenol and N-nitroso-phenyl- β -naphthylamine;
wherein the solvent is selected from one of kerosene and diesel oil.
4. A preparation method of an additive for improving the yield of light oil of a delayed coking unit comprises the following components:
10-20 parts by weight of a thermal cracking active substance,
30-40 parts of free radical chain reaction inhibitor,
20-30 parts by weight of an anti-coking agent,
10-20 parts by weight of a solvent,
the method is characterized by comprising the following steps: adding a solvent into an enamel stirring reaction kettle, slowly heating to 60-110 ℃ within 1-2 hours, then sequentially adding a thermal cracking active substance, a free radical chain reaction inhibitor and an anti-coking agent according to a proportion, stirring for reaction for 1-2 hours, cooling, and filtering to remove solid impurities to obtain the additive to be prepared.
5. A preparation method of an additive for improving the yield of light oil of a delayed coking unit comprises the following components:
13-17 parts by weight of a thermal cracking active substance,
34-38 parts of free radical chain reaction inhibitor,
23-26 parts by weight of an anti-coking agent,
13-18 parts by weight of a solvent,
the method is characterized by comprising the following steps: adding a solvent into an enamel stirring reaction kettle, slowly heating to 60-110 ℃ within 1-2 hours, then sequentially adding a thermal cracking active substance, a free radical chain reaction inhibitor and an anti-coking agent according to a proportion, stirring for reaction for 1-2 hours, cooling, and filtering to remove solid impurities to obtain the additive to be prepared.
6. Use of an additive according to any one of claims 1, 2 or 3 in an amount of from 100ppm to 500ppm in a feed system of a delayed coking system.
7. Use of the additive according to any one of claims 1, 2 or 3 in an amount of 100-300ppm in the feed system of a delayed coking system.
8. Use of the additive of any of claims 1, 2, or 3 in an amount of 300ppm to a feed system of a delayed coking system.
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| Application Number | Priority Date | Filing Date | Title |
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| CNB2004100061463A CN1239394C (en) | 2004-03-04 | 2004-03-04 | Additive for enhancing and delaying light oil recovery rate of coke apparatus |
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| Application Number | Priority Date | Filing Date | Title |
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| CNB2004100061463A CN1239394C (en) | 2004-03-04 | 2004-03-04 | Additive for enhancing and delaying light oil recovery rate of coke apparatus |
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| CN1239394C CN1239394C (en) | 2006-02-01 |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101113367B (en) * | 2007-07-19 | 2010-11-10 | 茂名学院 | Adding substance for reducing furnace tube deposition coking and improving liquid yield of delayed coker |
| CN102311755A (en) * | 2010-06-29 | 2012-01-11 | 中国石油化工股份有限公司 | Auxiliary agent used for increasing yield of delayed-coked liquid products |
| CN102311757A (en) * | 2010-06-29 | 2012-01-11 | 中国石油化工股份有限公司 | Method for improving yield of delayed coking liquid product |
| CN102311756A (en) * | 2010-06-29 | 2012-01-11 | 中国石油化工股份有限公司 | Addition agent for thermal inversion process of heavy oil and preparation method of addition agent |
| CN102585881A (en) * | 2012-03-12 | 2012-07-18 | 宜兴汉光高新石化有限公司 | Additive for promoting residual oil thermal cracking reaction and preparing method and application thereof |
| CN112778994A (en) * | 2020-12-31 | 2021-05-11 | 中海石油(中国)有限公司湛江分公司 | High-temperature-resistant high-salt surfactant composition and preparation method and application thereof |
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2004
- 2004-03-04 CN CNB2004100061463A patent/CN1239394C/en not_active Expired - Fee Related
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101113367B (en) * | 2007-07-19 | 2010-11-10 | 茂名学院 | Adding substance for reducing furnace tube deposition coking and improving liquid yield of delayed coker |
| CN102311755A (en) * | 2010-06-29 | 2012-01-11 | 中国石油化工股份有限公司 | Auxiliary agent used for increasing yield of delayed-coked liquid products |
| CN102311757A (en) * | 2010-06-29 | 2012-01-11 | 中国石油化工股份有限公司 | Method for improving yield of delayed coking liquid product |
| CN102311756A (en) * | 2010-06-29 | 2012-01-11 | 中国石油化工股份有限公司 | Addition agent for thermal inversion process of heavy oil and preparation method of addition agent |
| CN102311757B (en) * | 2010-06-29 | 2013-11-06 | 中国石油化工股份有限公司 | Method for improving yield of delayed coking liquid product |
| CN102311756B (en) * | 2010-06-29 | 2013-11-27 | 中国石油化工股份有限公司 | Addition agent for thermal inversion process of heavy oil and preparation method of addition agent |
| CN102311755B (en) * | 2010-06-29 | 2013-12-25 | 中国石油化工股份有限公司 | Auxiliary agent used for increasing yield of delayed-coked liquid products |
| CN102585881A (en) * | 2012-03-12 | 2012-07-18 | 宜兴汉光高新石化有限公司 | Additive for promoting residual oil thermal cracking reaction and preparing method and application thereof |
| CN102585881B (en) * | 2012-03-12 | 2014-08-13 | 宜兴汉光高新石化有限公司 | Additive for promoting residual oil thermal cracking reaction and preparing method and application thereof |
| CN112778994A (en) * | 2020-12-31 | 2021-05-11 | 中海石油(中国)有限公司湛江分公司 | High-temperature-resistant high-salt surfactant composition and preparation method and application thereof |
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| CN1239394C (en) | 2006-02-01 |
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