CN105778992A - In-situ oriented denitrifying agent and denitrifying method aiming at coking process of heavy oil with high nitrogen content - Google Patents
In-situ oriented denitrifying agent and denitrifying method aiming at coking process of heavy oil with high nitrogen content Download PDFInfo
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- CN105778992A CN105778992A CN201410805533.7A CN201410805533A CN105778992A CN 105778992 A CN105778992 A CN 105778992A CN 201410805533 A CN201410805533 A CN 201410805533A CN 105778992 A CN105778992 A CN 105778992A
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Abstract
The invention relates to an in-situ oriented denitrifying agent and denitrifying method aiming at the coking process of heavy oil with a high nitrogen content. The denitrifying agent is composed of the following components in percentage by weight: 5 to 95 wt% of polyhydroxyl organic compounds, 0 to 90 wt% of solvent, and 0 to 5 wt% of compatilizer. According to the denitrifying method, during the coking process, the denitrifying agent is directly added to enhance the coking denitrification process so as to obtain coking fraction oil with a low nitrogen content; the coking fraction oil, which is obtained through direct coking in the absence of denitrifying agent, is taken as the baseline, the denitrification rate can reach at least 50%; the requirements of processing and applications can be met, the subsequent denitrification refining treatment is not needed, the equipment investment is saved, and the production cost is reduced.
Description
Technical field
The present invention relates to a kind of high nitrogenous heavy oil treatment process, belong to PETROLEUM PROCESSING field.
Along with improving constantly that China's economic development requires, the demand of fuel oil is growing, the industrialization status of crude oil processing is more and more important, the nitrogen content that the nitrogenous heavy oil of height (including crude oil residuum Colophonium etc.) of China causes processing the fuel oil such as the gasoline, diesel wax oil that obtains is higher, it is difficult to carry out following process and use.
Original position orientation denitrifier is utilized to strengthen the coking of high nitrogenous heavy oil, nitrogen-containing compound is removed in coking situ orientation orientation, thus obtaining the coking product oil of relatively low nitrogen content, (fractional distillation can obtain wax tailings, heavy distillate, gasoline, diesel oil, crude naphtha etc.), it is available for following process directly to use, eliminates follow-up denitrogenation processing.
Background technology
The nitride of high-load in the heavy oil such as crude oil, residual oil and Colophonium and processing products obtained therefrom oil thereof, especially catalysqt deactivation when basic nitrogen compound can cause oil product following process, have a strong impact on production capacity, nitride also can reduce the oxidation stability of oil product, oil quality is made to decline, economic benefit is had a greatly reduced quality, and the burning use of high nitrogenous oil product simultaneously can aggravate atmospheric pollution.Therefore the nitrogen content reducing oil product is a big key subject of PETROLEUM PROCESSING industry.
Delayed coking is the important means of processing of heavy oil, owing to the nitrogen content of China's heavy oil is higher, causes the coking distillate that delayed coking unit produces, such as wax tailings, heavy distillate, gasoline, the nitrogen content of the oil products such as diesel oil is also higher, it is difficult to be made directly follow-up processing and use.Such as, the nitrogen content of triumph alkaline residue is up to 8500ppm, using it as the oily wax tailings nitrogen content obtained through delayed coking of coking raw material for 7000ppm, greatly exceed the nitrogen content (2800ppm) that general hydrocracking catalyst can bear, the nitrogen content obtaining coker gas oil is 2000ppm, is significantly larger than the nitrogen content (200ppm) that light diesel fuel requirement controls.Therefore coking distillate have to carry out follow-up denitrification refining process and could use.Industrial, for wax tailings, diesel oil, traditional denitrogenation method of the coking distillate such as gasoline mainly has hydrodenitrogeneration, solvent extraction denitrogenation, Complex denitrogenation, absorption denitrogenation etc., above denitrogenation method is respectively arranged with pluses and minuses, and denitrification effect is also ideal, but denitrogenation processing mode is after delayed coking unit, denitrification processing device is set coking distillate is carried out further denitrification refining process.
Given this, it is an object of the invention to utilize original position orientation denitrifier, in coking, the nitrogen-containing compound in high nitrogenous heavy oil is caught and fixes, urge to convert it into coke or inorganic gas, and then the purpose of arrival original position orientation denitrogenation, strengthen coking denitrification process, directly obtain the coking distillate of low nitrogen content, meet processing and instructions for use, eliminate follow-up denitrification refining to process, save equipment investment, reduce production cost.
Summary of the inventionA kind of denitrifier for high nitrogenous coking heavy oil process that the present invention relates to and denitrogenation method, suitable in crude oil, residual oil (decompression, normal pressure, cracking), de-oiled asphalt, coal tar asphalt, thermal cracking tars, catalytic cracking clarified oil, the heavy oil such as heavy distillate and wax slop and miscella thereof, strengthen its fixed nitrogen denitrification in coking, more nitrogen-containing compound original position orientation is made to be converted into coke, thus obtaining meeting the coking distillate of the low nitrogen content of following process and instructions for use, process chart is as shown in Figure 1, Fig. 1 is denitrification process flow chart, denitrifier and the blended entrance coking tower of fractionating column base oil.
Consisting of of original position orientation denitrifier: polyhydroxy organic compound (only containing tri-kinds of elements of C, H, O, including aromatic series and aliphatic polyhydroxy compound, it is possible to containing carbonyl) 5-95wt%, solvent 0-90wt% and compatilizer 0-5wt%.Wherein polyol can be in aromatic polyhydroxy compounds such as polyatomic phenol as tea polyphenols, catechol, hydroquinone or neighbour (to) mixture of Benzodiazepines, antioxidant 246 etc., or aliphatic polyhydroxy compound can be straight chain, side chain or cyclic polyhydroxy compound, straight chain polyol, such as polyvinyl alcohol, Polyethylene Glycol, sorbitol, glycerol, glyceraldehyde, mannitol etc.；Side chain polyol, such as tetramethylolmethane etc.；Cyclic polyhydroxy compound, such as various carbohydrates and the derivants thereof such as cyclohexanhexanol and glucose, sucrose, cellulose, starch, one or more complex of above compound.Solvent can be water, ethanol, isopropanol, one or more complex in butanol.Compatilizer is anion or nonionic surfactant, one or more complex in Polyethylene Glycol, polyoxyethylene ether, dodecylbenzene sodium sulfonate, sodium lauryl sulphate, dodecyl sodium sulfate, OP-7, OP-10, AEO-7, AEO-9, the Main Function that wherein compatilizer adds is to promote better mass transfer between denitrifier and raw oil.
The present invention is directed to the main operational steps of the laboratory simulation coking that high nitrogenous coking heavy oil process original position orientation denitrogenation adopts as follows:
1. it is re-dubbed original position orientation denitrifier as stated above；
2. above-mentioned denitrifier is mixed to join in heat-resistant pressure-resistant reactor by the amount of quality oil ratio 1:20-1:1 and heavy oil, carries out 475-525 DEG C, 0.15-0.25MPa, the pyrogenetic reaction of 6-12h, difference according to denitrifier, can carry out the precoking reaction of 3-6h, 150-200 DEG C before pyrogenetic reaction；
3. pyrogenetic reaction is collected after terminating and is obtained coking distillate, measures its (alkali) nitrogen content；
4. coking distillate can be carried out fractional distillation as required, obtain the light oils such as wax tailings, heavy distillate, diesel oil, gasoline, for following process or use.
【Detailed description of the invention】
Embodiment 1
By polyvinyl alcohol 33wt%, deionized water 22wt%, acetic acid 44wt% and p-methyl benzenesulfonic acid 1% are re-dubbed denitrifier, with delayed coking unit feed oil (residual oil 65wt%, crude oil 35wt%, nitrogen content is 5672ppm) for raw oil, it is 1:20 by oil ratio, pressure reactor carries out 480 DEG C, the pyrogenetic reaction 9h of 0.25MPa, the coking distillate being obtained by reacting, not add coking distillate that the direct coking of denitrifier obtains for benchmark, total nitrogen content falls below 775ppm from 2871ppm, total nitrogen removal efficiency is 73.0%, basic nitrogen falls below 187ppm from 923ppm, basic nitrogen removal rate is 79.7%.
Embodiment 2
By sorbitol 64wt%, deionized water 32wt% and Polyethylene Glycol 4wt% is re-dubbed denitrifier, with the fractionating column base oil (nitrogen content is for 6311ppm) in delayed coking unit for raw oil, it is 1:15 by oil ratio, pressure reactor carries out 500 DEG C, the pyrogenetic reaction 12h of 0.2MPa, the coking distillate being obtained by reacting, not add coking distillate that the direct coking of denitrifier obtains for benchmark, total nitrogen content falls below 1001ppm from 3194ppm, total nitrogen removal efficiency is 68.7%, and basic nitrogen falls below 279ppm from 990ppm, and basic nitrogen removal rate is 71.8%.
Embodiment 3
By glucose 40wt%, deionized water 59wt%, dodecylbenzene sodium sulfonate 0.5wt% and dodecyl sodium sulfate 0.5wt% is re-dubbed denitrifier, feed oil with atmospheric and vacuum distillation unit, crude oil (nitrogen content is 4711ppm) is raw oil, it is 1:8 by oil ratio, after carrying out the precoking reaction 5h at 180 DEG C in pressure reactor, carry out 520 DEG C, the pyrogenetic reaction 10h of 0.2MPa, the coking distillate being obtained by reacting, not add coking distillate that the direct coking of denitrifier obtains for benchmark, total nitrogen content falls below 736ppm from 2274ppm, total nitrogen removal efficiency is 67.6%, basic nitrogen falls below 247ppm from 732ppm, basic nitrogen removal rate is 66.3%.
Embodiment 4
By tea polyphenols 33wt%, isopropanol 33wt%, dehydrated alcohol 33wt% and (OP-7) 1wt% is re-dubbed denitrifier, with the wax slop (nitrogen content is for 3571ppm) of delayed coking unit production for raw oil, it is 1:20 by oil ratio, 525 DEG C are carried out in pressure reactor, the pyrogenetic reaction 6h of 0.17MPa, the coking distillate being obtained by reacting, not add coking distillate that the direct coking of denitrifier obtains for benchmark, total nitrogen content falls below 898ppm from 2185ppm, total nitrogen removal efficiency is 58.9%, basic nitrogen falls below 286ppm from 737ppm, basic nitrogen removal rate is 61.2%.
The wax tailings that coking distillate practical application of the present invention obtained obtains after carrying out fractional distillation, with the wax tailings contrast that industrial delayed coking obtains, basic nitrogen data such as table 1.
Table 1 original position orientation denitrogenation and commercial delay coking contrast
Note: commercial delay coking raw oil used is consistent with the raw oil used by example 1.
As known from Table 1, utilize original position orientation denitrifier that coking raw oil is simulated the wax tailings that coking obtains, relative to the basic nitrogen of raw oil, its change (decline) rate, far above commercial delay coking, illustrates that a large amount of basic nitrogen compound is removed by original position orientation in simulation coking.
The wax tailings obtained after the coking distillate that the present invention (one-step method: original position orientation denitrogenation) practical application obtains is carried out fractional distillation, the refining wax tailings contrast obtained after carrying out denitrification refining (two-step method: delayed coking+denitrification refining) with delayed coking gained wax tailings, basic nitrogen data and basic nitrogen removal rate such as table 2 and table 3.
Table 2 processing of heavy oil traditional handicraft and basic nitrogen removal rate (two-step method)
[1] lucky hero, Yang Yan, Mao Fenglin etc. Technics of Removing Basic Nitrogen of Coker Gatch research [J]. Chemical Industry in Guangzhou, 2006,34 (1): 45-50.
[2] monarch Songrong, Zhao Dezhi, Cao Zubin etc. the process technology of China's wax tailings and progress [J] thereof. contemporary chemical industry, 2003,32 (3): 149-151.
[3] Luan Xilin, Li Chengyong, Chen Wenyi etc. Removal of Basic Nitrogen in Coker Gatch OilUsing Adsorption Method research [J]. petrochemical industry Journal of Chinese Universities, 1999,12 (2).
Table 3 invention example and basic nitrogen removal rate (one-step method)
Note:N 0 ’ : it is not added with any denitrifier and directly simulates the basic nitrogen of coking gained wax tailings；
N 1 ’ : add the basic nitrogen of original position orientation denitrifier simulation coking gained wax tailings.
From table 2 and table 3, we can see that, the basic nitrogen removal rate of the wax tailings that the present invention is obtained, substantially suitable with the basic nitrogen removal rate of traditional coked wax oil denitrifying process for refining gained refined oil, for different denitrifiers, also has certain advantage, but prepare the wax tailings of low nitrogen content relative to traditional method (two-step method), the present invention (one-step method) is simple to operate, eliminates follow-up denitrification refining step, can significantly save equipment investment, reduce production cost.
The citing of table 4 invention example and denitrification percent
Note:N 0 : it is not added with any denitrifier and directly simulates the total nitrogen content of coking gained coking distillate；
N 1 : add the total nitrogen content of original position orientation denitrifier simulation coking gained coking distillate.
【Accompanying drawing explanation】
Fig. 1 is denitrification process flow chart, denitrifier and the blended entrance coking tower of fractionating column base oil.
Claims (6)
1. one kind refers to for the method for high nitrogenous heavy oil (as coking raw material oil) original position orientation denitrogenation, fractionating column base oil (from fractionation column base) is directly added into original position orientation denitrifier of the present invention, nitrogen-containing compound is oriented by coking seizure and fixing, promote more nitride converted coke, strengthening coking denitrification process, obtain the coking distillate of low nitrogen content, being fractionated into can the wax tailings of low nitrogen content, heavy distillate, diesel oil, gasoline etc., can be made directly following process or use, without further denitrogenation processing.
2. a kind of original position orientation denitrifier adopted for high nitrogenous coking heavy oil according to claim 1, it is characterised in that: the composition that mainly comprises of this original position orientation denitrifier is: polyhydroxy organic compound 5-95wt%, solvent 0-90wt% and compatilizer 0-5wt%.
3. a kind of original position orientation denitrifier adopted for high nitrogenous coking heavy oil according to claim 2, its constituent is characterised by: only containing tri-kinds of elements of C, H, O in this polyol, it is likely to containing carbonyl, can be aromatic series or aliphatic polyhydroxy compound, wherein, aromatic polyhydroxy compounds can be various polyatomic phenol, as tea polyphenols, catechol, hydroquinone or neighbour (to) mixture of Benzodiazepines, antioxidant 246 etc.；Aliphatic polyhydroxy compound can be straight chain, side chain or cyclic polyhydroxy compound, straight chain polyol, such as polyvinyl alcohol, Polyethylene Glycol, sorbitol, glycerol, glyceraldehyde, mannitol etc.；Side chain polyol, such as tetramethylolmethane etc.；Cyclic polyhydroxy compound, such as various carbohydrates and derivants thereof such as cyclohexanhexanol and glucose, sucrose, cellulose, starch；Polyol in this original position orientation denitrifier can be one or more complex of above-mentioned a few apoplexy due to endogenous wind.
4. a kind of original position orientation denitrifier adopted for high nitrogenous coking heavy oil according to claim 2, its constituent is characterised by: solvent can be water, ethanol, isopropanol, one or more complex in butanol.
5. a kind of original position orientation denitrifier adopted for high nitrogenous coking heavy oil according to claim 2, its constituent is characterised by: compatilizer is anion or nonionic surfactant, one or more complex in Polyethylene Glycol, polyoxyethylene ether, dodecylbenzene sodium sulfonate, sodium lauryl sulphate, dodecyl sodium sulfate, OP-7, OP-10, AEO-7, AEO-9, the Main Function that compatilizer adds is to promote better mass transfer between denitrifier and raw oil.
6. a kind of major experimental operating procedure for the original position orientation denitrogenation method of high nitrogenous coking heavy oil employing according to claim 1 is: be mixed to join in heat-resistant pressure-resistant reactor by above-mentioned original position orientation denitrifier by certain agent oil quality ratio (1:20-1:1) and the nitrogenous heavy oil of height, carry out 475-525 DEG C, 0.15-0.25MPa, the pyrogenetic reaction of 6-12h, obtain coke and coking distillate, wherein optimum experimental operating conditions is temperature 500 DEG C, pressure 0.2MPa, scorch time 6h；A kind of denitrogenation method adopted for high nitrogenous coking heavy oil according to claim 1, its for the nitrogenous heavy oil of height (coking raw material oil), can be crude oil, residual oil (decompression, normal pressure, cracking), de-oiled asphalt, coal tar asphalt, thermal cracking tars, catalytic cracking clarified oil, one or more in heavy distillate and wax slop etc..
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108641744A (en) * | 2018-05-11 | 2018-10-12 | 金浦新材料股份有限公司 | A kind of denitrifier and its preparation method and application for petroleum oil product denitrogenation |
| US10266745B2 (en) | 2017-02-03 | 2019-04-23 | Saudi Arabian Oil Company | Anti-bit balling drilling fluids, and methods of making and use thereof |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4169781A (en) * | 1978-06-02 | 1979-10-02 | Chevron Research Company | Denitrification by furfural-ferric chloride extraction of coker oil |
| CN101928597A (en) * | 2010-02-04 | 2010-12-29 | 涿州贝尔森生化科技发展有限公司 | Vacuum residue processing method |
| CN101955797A (en) * | 2010-10-22 | 2011-01-26 | 华东理工大学 | Method for inhibiting alkaline nitrides in coker gatch |
| CN102485842A (en) * | 2010-12-03 | 2012-06-06 | 中国石油天然气股份有限公司 | Method for processing fixed bed fishing coker gas oil |
| CN103224807A (en) * | 2013-05-10 | 2013-07-31 | 中国石油大学(华东) | Process for carrying out complextion and denitrification on coker gas oil |
-
2014
- 2014-12-23 CN CN201410805533.7A patent/CN105778992A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4169781A (en) * | 1978-06-02 | 1979-10-02 | Chevron Research Company | Denitrification by furfural-ferric chloride extraction of coker oil |
| CN101928597A (en) * | 2010-02-04 | 2010-12-29 | 涿州贝尔森生化科技发展有限公司 | Vacuum residue processing method |
| CN101955797A (en) * | 2010-10-22 | 2011-01-26 | 华东理工大学 | Method for inhibiting alkaline nitrides in coker gatch |
| CN102485842A (en) * | 2010-12-03 | 2012-06-06 | 中国石油天然气股份有限公司 | Method for processing fixed bed fishing coker gas oil |
| CN103224807A (en) * | 2013-05-10 | 2013-07-31 | 中国石油大学(华东) | Process for carrying out complextion and denitrification on coker gas oil |
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