CN103194259A - Diesel oil non-hydrodewaxing process method - Google Patents
Diesel oil non-hydrodewaxing process method Download PDFInfo
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- CN103194259A CN103194259A CN201310148533XA CN201310148533A CN103194259A CN 103194259 A CN103194259 A CN 103194259A CN 201310148533X A CN201310148533X A CN 201310148533XA CN 201310148533 A CN201310148533 A CN 201310148533A CN 103194259 A CN103194259 A CN 103194259A
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- pour point
- point depression
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Abstract
The invention relates to a diesel oil non-hydrodewaxing process method. The diesel oil non-hydrodewaxing process method comprises the following steps that: diesel oil is heated to 320-410 DEG C by a first-section pour point depressing heating furnace, and enters a first-section pour point depressing reactor for pour point depressing reaction, a reactant coming out of the first-section pour point depressing reactor enters a reactant separation tank for gas-liquid separation, and a gas phase on the top of the tank enters an atmospheric tower for rectification; a liquid phase product at the bottom of the tank is fed into a second-section pour point depressing heating furnace and is heated to 320-410 DEG C, and then enters a second-section pour point depressing reactor for second-section pour point depressing reaction, a reactant coming out of the second-section pour point depressing reactor enters the atmospheric tower for rectification; after the reactant is rectified in the atmospheric tower, C3, C4 and gasoline of distilled components on the top of the atmospheric tower enter a gasoline stabilizer for rectification, distilled C3 and C4 components on the top of the gasoline stabilizer are compressed to turn into liquefied gas, and gasoline is distilled off at the bottom of the gasoline stabilizer; diesel oil is distilled off in the first line, the second line and the third line of the atmospheric tower; and oil at the bottom of the atmospheric tower is heated to 320 DEG C and then enters a vacuum tower for rectification. The diesel oil non-hydrodewaxing process method has the advantages of good quality of products, high liquid yield, no hydrogen consumption, wide application range of raw materials and strong production flexibility.
Description
One, technical field:
What the present invention relates to is the processing method of producing diesel oil, and what be specifically related to is diesel oil non-hydro-dewaxing processing method.
Two, background technology:
Diesel motor is lower than petrolic oil consumption, thermo-efficiency is high, and unwanted component is few in the tail gas of discharge, is fit in the our times scope growing to requirement on environmental protection.Be that vehicle powered rapidly increases with diesel oil, make market constantly increase the demand of diesel oil.The main source of diesel oil is the distillate that time processing and secondary processing are produced, diesel oil in use requires its zero pour must not be higher than a certain value, to guarantee that it has good mobility at low temperatures, and general diesel oil mostly is difficult to reach this requirement, can not directly use, so need to reduce the zero pour (being the diesel oil pour point depression) of diesel oil, make it to become qualified product.Catalytic hydrodewaxing (being hydrodewaxing) is a kind of main diesel oil pour-point depressing method, distillate contacts with catalyzer in the presence of hydrogen, at high pressure and facing under the condition of hydrogen, the wax in the distillate is fallen in hydrocracking, but its main shortcoming is the reaction pressure height, need to add hydrogen in the reaction process, and the source of hydrogen is relatively more difficult, the diesel hydro-pour-reducing method is promoted be restricted.
Three, summary of the invention:
The purpose of this invention is to provide diesel oil non-hydro-dewaxing processing method, this diesel oil non-hydro-dewaxing processing method is used for solving existing diesel hydro-pour-reducing method because of needs high pressure and hydrogenation, promotes the problem that is restricted.
The technical solution adopted for the present invention to solve the technical problems is: this diesel oil non-hydro-dewaxing processing method is: diesel oil is heated to 320～410 ℃ through one section pour point depression process furnace, enter one section pour point depression reactor and carry out the pour point depression reaction, the reactant that one section pour point depression reactor comes out enters the reactants separate jar and carries out gas-liquid separation, and the tank deck gas phase enters atmospheric tower rectifying by atmospheric tower top opening for feed; Jar end liquid product is extracted out by the second-stage reaction fresh feed pump, send into two sections pour point depression process furnace and be heated to 320～410 ℃, and then enter two sections pour point depression reactors and carry out the reaction of two sections pour point depressions, the reactant that two sections pour point depression reactors come out enters atmospheric tower rectifying by atmospheric tower underfeed mouth;
After the atmospheric tower rectifying, it is C3, C4 and gasoline that the atmospheric tower top distillates composition, and through entering gasoline stabilizer rectifying after the condenser cooling, the gasoline stabilizer top distillates C3, C4 component, through compressor compresses, becomes liquefied gas and enters the liquid gas storage tank storage; The gasoline stabilizer bottom distillates gasoline; Atmospheric tower one line, two wires, three line distillate diesel fuels; Oil is heated to 320 ℃ through vacuum furnace at the bottom of the atmospheric tower, goes vacuum distillation tower rectifying again.
One section pour point depression process furnace is connected to one section pour point depression reactor inlet by pipeline in the such scheme, one section pour point depression reactor outlet connects separating tank by pipeline, the separating tank roof door is connected to atmospheric tower top opening for feed by pipeline, the separating tank lower part outlet is connected to two sections pour point depression process furnace by pipeline, two sections pour point depression furnace outlets are connected to two sections pour point depression reactor inlets by pipeline, and two sections pour point depression reactor outlets are connected to atmospheric tower underfeed mouth by pipeline.
One section pour point depression reactor and two sections pour point depression reactor reaction pressure are 0.3～1.5MPa in the such scheme, and air speed is 1.0h
-1
Atmospheric tower all is connected surge tank by pipeline with the vacuum distillation tower middle part in the such scheme, all can stablize to guarantee atmospheric tower and vacuum distillation tower, improves fractionation efficiency.
When one section pour point depression reactor and two sections pour point depression reactors reacted in the such scheme, the catalyzer of employing was the long-acting catalyzer ZSM-5 of the bar shaped white high zeolite of non-hydrogen cavernous structure.
Catalyzer adopts the oxidation method of making charcoal to regenerate in the such scheme, behind the catalyst deactivation, feeding nitrogen sweeps Residual oil in the reactor only, open the regeneration process furnace and feed regenerating medium steam, industrial wind, entering the reactor oxidation makes charcoal, control is burnt temperature in the reactor, when temperature does not change with the feeding amount of steam, industrial wind in the question response device, assert that catalyst regeneration finishes.
Beneficial effect:
1, the present invention designs separating tank behind one section pour point depression reactor, makes separating of oil the going out of light constituent behind the pour point depression, can avoid the secondary pour point depression of light constituent, reduces the output of liquefied gas and gasoline, improves the productive rate of diesel oil greatly, and diesel yield can reach more than 75%.
2, the present invention is under the non-hydrogen state, 320～410 ℃ of temperature of reaction, reaction pressure 0.3～1.5MPa, air speed 1.0h
-1Condition under, carry out catalytic cracking reaction by the non-hydrogen condensation point reducing catalyst that is contained in fixed bed, and generate non-condensable gas, liquefied gas, gasoline intermediates, low freezing point diesel fuel etc.Become micromolecular alkane by weighing the fatty oil chain rupture, produce C
3, C
4High value added products such as distillate, gasoline fraction oil, low freezing point diesel fuel distillate are to satisfy the demand of the different condensation point oil of oil product industry Various Seasonal demand.
3, the present invention have good product quality, liquid receive high, do not consume hydrogen, raw material wide accommodation, characteristics such as the production cycle is long and production process is pollution-free, technical process is simple, and is easy to operate, the production handiness is strong.Can realize different production decisions, thereby satisfy corresponding product requirement by adjustment raw material composition, process operation parameter.The produce market adaptive faculty that adopts this technology to produce is strong.
Four, description of drawings:
Fig. 1 is the structure drawing of device of reactive moieties of the present invention.
1 one sections pour point depression process furnace; 2 one sections pour point depression reactors; 3 separating tanks; 4 two sections pour point depression process furnace; 5 two sections pour point depression reactors.
Five, embodiment:
The present invention is described further below in conjunction with accompanying drawing:
As shown in Figure 1, this diesel oil non-hydro-dewaxing processing method is: after diesel oil carries out heat exchange by interchanger, be heated to 320～410 ℃ through one section pour point depression process furnace 1, enter one section pour point depression reactor 2 and carry out the pour point depression reaction, be provided with good sparger in the reactor, the reactant that one section pour point depression reactor 2 comes out enters reactants separate jar 3 and carries out gas-liquid separation, and the tank deck gas phase enters atmospheric tower rectifying by atmospheric tower top opening for feed; Jar end liquid product is extracted out by the second-stage reaction fresh feed pump, send into two sections pour point depression process furnace 4 and be heated to 320～410 ℃, and then enter two sections pour point depression reactors 5 and carry out the reaction of two sections pour point depressions, the reactant that two sections pour point depression reactors 5 come out enters atmospheric tower rectifying by atmospheric tower underfeed mouth.One section pour point depression reactor 2 and two sections pour point depression reactor 5 reaction pressures are 0.3～1.5MPa, and air speed is 1.0h
-1, the catalyzer of employing is the long-acting catalyzer ZSM-5 of the bar shaped white high zeolite of non-hydrogen cavernous structure.Apparatus of the present invention partly are made up of reactive moieties, regeneration section, fractionation.
Catalyzer of the present invention adopts the oxidation method of making charcoal to regenerate, behind the catalyst deactivation, feeding nitrogen sweeps Residual oil in the reactor only, open the regeneration process furnace and feed regenerating medium steam, industrial wind, entering the reactor oxidation makes charcoal, control is burnt temperature in the reactor, when temperature does not change with the feeding amount of steam, industrial wind in the question response device, assert that catalyst regeneration finishes.
The apparatus structure that reactive moieties of the present invention adopts is, one section pour point depression process furnace 1 is connected to one section pour point depression reactor 2 entrance by pipeline, one section pour point depression reactor 2 outlet connects separating tank 3 by pipeline, separating tank 3 roof doors are connected to atmospheric tower top opening for feed by pipeline, separating tank 3 lower part outlets are connected to two sections pour point depression process furnace 4 by pipeline, two sections pour point depression process furnace 4 outlets are connected to two sections pour point depression reactor 5 entrances by pipeline, and two sections pour point depression reactor 5 outlets are connected to atmospheric tower underfeed mouth by pipeline.
After the atmospheric tower rectifying, it is C3, C4 and gasoline that the atmospheric tower top distillates composition, and through entering gasoline stabilizer rectifying after the condenser cooling, the gasoline stabilizer top distillates C3, C4 component, through compressor compresses, becomes liquefied gas and enters the liquid gas storage tank storage; The gasoline stabilizer bottom distillates gasoline; Atmospheric tower one line, two wires, three line distillate diesel fuels; Oil is heated to 320 ℃ through vacuum furnace at the bottom of the atmospheric tower, goes vacuum distillation tower rectifying again.Specific as follows:
It is C3, C4 and gasoline that the atmospheric tower top distillates composition, and through entering gasoline stabilizer rectifying after the condenser cooling, the gasoline stabilizer top distillates C3, C4 component, through compressor compresses, becomes liquefied gas and enters the liquid gas storage tank storage.
The gasoline stabilizer bottom distillates gasoline, extracts out through pump and enters the gasoline tank storage.Quality of gasoline reaches national 90# gasoline standard.
Atmospheric tower one line goes out diesel oil, extracts heat exchange out, cools off and go diesel oil tank to store through pump, and diesel quality reaches country-35# diesel oil standard.
The atmospheric tower two wires goes out diesel oil, extracts heat exchange out, cools off and go diesel oil tank to store through pump, and diesel quality reaches country-30# diesel oil standard.
Atmospheric tower three lines go out diesel oil, extract heat exchange out, cool off and go diesel oil tank to store through pump, and diesel quality reaches country-20# diesel oil standard.
Oil is extracted out by pump at the bottom of the atmospheric tower, and vacuum furnace is heated to 320 ℃, goes vacuum distillation tower rectifying again.
The vacuum distillation tower top goes out diesel oil, through the supercooler cooling, removes the diesel oil receiving tank, is extracted out by pump and goes diesel fuel tank to store, and diesel quality reaches country-10# diesel oil standard.
Vacuum distillation tower one line goes out diesel oil, extracts heat exchange out, cools off and go diesel oil tank to store through pump, and diesel quality reaches country-10# diesel oil standard.
The vacuum distillation tower two wires goes out diesel oil, extracts heat exchange out, cools off and go diesel oil tank to store through pump, and diesel quality reaches national 0# diesel oil standard.
The vacuum distillation tower bottom goes out base oil, extracts heat exchange out, cools off and go diesel oil tank to store through pump, can do aluminium foil oil or boiler oil.
The present invention is by the selective cracking process, there is shape-selective molecular sieve to exist down, normal paraffin generation cracking reaction in reaction process in the raw material, " wax " selectivity in the raw material is split branch, the condensation point of diesel oil is reduced, can produce low-coagulation diesel oil, increase production gasoline and lighter hydrocarbons simultaneously, reaction process is strong heat absorption.
Claims (6)
1. diesel oil non-hydro-dewaxing processing method, it is characterized in that: this diesel oil non-hydro-dewaxing processing method is: diesel oil is heated to 320～410 ℃ through one section pour point depression process furnace (1), enter one section pour point depression reactor (2) and carry out the pour point depression reaction, the reactant that one section pour point depression reactor (2) comes out enters reactants separate jar (3) and carries out gas-liquid separation, and the tank deck gas phase enters atmospheric tower rectifying by atmospheric tower top opening for feed; Jar end liquid product is extracted out by the second-stage reaction fresh feed pump, send into two sections pour point depression process furnace (4) and be heated to 320～410 ℃, and then enter two sections pour point depression reactors (5) and carry out the reaction of two sections pour point depressions, the reactant that two sections pour point depression reactors (5) come out enters atmospheric tower rectifying by atmospheric tower underfeed mouth;
After the atmospheric tower rectifying, it is C3, C4 and gasoline that the atmospheric tower top distillates composition, and through entering gasoline stabilizer rectifying after the condenser cooling, the gasoline stabilizer top distillates C3, C4 component, through compressor compresses, becomes liquefied gas and enters the liquid gas storage tank storage; The gasoline stabilizer bottom distillates gasoline; Atmospheric tower one line, two wires, three line distillate diesel fuels; Oil is heated to 320 ℃ through vacuum furnace at the bottom of the atmospheric tower, goes vacuum distillation tower rectifying again.
2. diesel oil non-hydro-dewaxing processing method according to claim 1, it is characterized in that: described one section pour point depression process furnace (1) is connected to one section pour point depression reactor (2) entrance by pipeline, one section pour point depression reactor (2) outlet connects separating tank (3) by pipeline, separating tank (3) roof door is connected to atmospheric tower top opening for feed by pipeline, separating tank (3) lower part outlet is connected to two sections pour point depression process furnace () by pipeline, two sections pour point depression process furnace (4) outlet is connected to two sections pour point depression reactors (5) entrance by pipeline, and two sections pour point depression reactors (5) outlet is connected to atmospheric tower underfeed mouth by pipeline.
3. diesel oil non-hydro-dewaxing processing method according to claim 2, it is characterized in that: described one section pour point depression reactor (2) and two sections pour point depression reactors (5) reaction pressure are 0.3～1.5MPa, and air speed is 1.0h
-1
4. diesel oil non-hydro-dewaxing processing method according to claim 3 is characterized in that: described atmospheric tower all is connected surge tank by pipeline with the vacuum distillation tower middle part.
5. diesel oil non-hydro-dewaxing processing method according to claim 4, it is characterized in that: when described one section pour point depression reactor and two sections pour point depression reactors reacted, the catalyzer of employing was the long-acting catalyzer ZSM-5 of the bar shaped white high zeolite of non-hydrogen cavernous structure.
6. diesel oil non-hydro-dewaxing processing method according to claim 5, it is characterized in that: described catalyzer adopts the oxidation method of making charcoal to regenerate, behind the catalyst deactivation, feeding nitrogen sweeps Residual oil in the reactor only, open the regeneration process furnace and feed regenerating medium steam, industrial wind, enter the reactor oxidation and make charcoal, burn temperature in the control reactor, when temperature does not change with the feeding amount of steam, industrial wind in the question response device, assert that catalyst regeneration finishes.
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| CN201310148533XA CN103194259A (en) | 2013-04-10 | 2013-04-10 | Diesel oil non-hydrodewaxing process method |
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| CN201310148533XA Pending CN103194259A (en) | 2013-04-10 | 2013-04-10 | Diesel oil non-hydrodewaxing process method |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4284529A (en) * | 1979-12-14 | 1981-08-18 | Mobil Oil Corporation | Hydrocarbon conversion catalyst |
| CN1245200A (en) * | 1998-08-18 | 2000-02-23 | 中国石油化工集团公司 | Process for depressing coagulation of fractional oil with non-critical hydrogen |
| CN1258718A (en) * | 1998-12-30 | 2000-07-05 | 广饶县金利润滑油厂 | Lubricating oil non-hydrogen condensation point reducing catalyst |
-
2013
- 2013-04-10 CN CN201310148533XA patent/CN103194259A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4284529A (en) * | 1979-12-14 | 1981-08-18 | Mobil Oil Corporation | Hydrocarbon conversion catalyst |
| CN1245200A (en) * | 1998-08-18 | 2000-02-23 | 中国石油化工集团公司 | Process for depressing coagulation of fractional oil with non-critical hydrogen |
| CN1258718A (en) * | 1998-12-30 | 2000-07-05 | 广饶县金利润滑油厂 | Lubricating oil non-hydrogen condensation point reducing catalyst |
Non-Patent Citations (1)
| Title |
|---|
| 郑祥林: "非临氢降凝工艺设计", 《当代化工》, vol. 37, no. 3, 27 August 2008 (2008-08-27) * |
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Application publication date: 20130710 |