CN102154024A

CN102154024A - Hydro-conversion integration method for high-nitrogen high-arene oil

Info

Publication number: CN102154024A
Application number: CN2011100452594A
Authority: CN
Inventors: 何巨堂
Original assignee: Individual
Current assignee: Individual
Priority date: 2011-02-21
Filing date: 2011-02-21
Publication date: 2011-08-17

Abstract

The invention discloses a hydro-conversion integration method for high-nitrogen high-arene oil, being suitable for a hydro-conversion process of coal tar. The method comprises the following steps: separating a first reaction effluent E1 which is obtained from novel hydrogen FH and first hydrocarbon raw material F1 (coal tar hydro-upgraded diesel) on a first reaction part into a first high pressure hydrogen-enriched gas V1 and a first high pressure hydrocarbon liquid L1 on a first high pressure separation part S1; and feeding at least a part of V1 into a second reaction part R2 for processing a second hydrocarbon raw material F2 (coal tar), and separating a second reaction effluent E2 into a second high pressure hydrogen-enriched gas V2 and a second high pressure hydrocarbon liquid L2 on a second high pressure separation part S2, wherein diesel fraction obtained by separating the second high pressure hydrocarbon liquid L2 is used as the first hydrocarbon raw material F1. The method is especially suitable for the process of producing the diesel by intermediate-low temperature coal tar, has the obvious effects of saving high pressure operation steps (compressors, heating furnaces and the like), reducing energy consumption, lowering hydrogen, improving the yield of the diesel and the like.

Description

A kind of hydrocracking integrated approach of high nitrogen high aromatic oil

Technical field

The present invention relates to a kind of high nitrogen high aromatic oil hydrocracking integrated approach; Say especially and the present invention relates to a kind of integrated approach that utilizes new hydrogen logistics to finish the further hydro-upgrading process of coal tar hydrogenation modification gained diesel oil; More particularly the present invention relates to a kind of integrated approach that utilizes new hydrogen logistics to finish the further hydro-upgrading process of middle coalite tar hydro-upgrading gained diesel oil.

Background technology

As everyone knows, the hydrocarbon hydroconversion process is the conversion process of the consumption hydrogen of hydrocarbon feed under the hydrogen existence condition, described hydrocarbon raw material can be the hydro carbons from oil or oil shale or oil-sand or coal, the cut scope of raw material hydrocarbon from gasoline, kerosene, diesel oil, wax oil up to residual oil, in most cases above-mentioned raw materials contains assorted element such as oxygen, sulphur and nitrogen etc., and coal tar then contains a large amount of assorted elements and the assorted element of considerable part and carbon atom and constitutes ring texture.

In hydroconversion process, under the hydrogen existence condition, hydrocarbon raw material contacts with a kind of or two kinds or multiple catalyzer in one or two or more reactors, and it is that 250～530 ℃, pressure are 1.4～28.0MPa that reaction conditions is generally temperature.The reaction pressure of common described low-voltage hydrogenation, medium-pressure hydrocracking, high-pressure hydrogenation correspondence is that 4.0MPa is following, 4.0～13.5MPa, more than the 13.5MPa.The typical chemical reaction that hydroconversion process takes place comprises that hydrodemetallation (HDM), hydrogenating desulfurization, hydrogenation alkene are saturated, hydrodenitrification, aromatic hydrogenation are saturated, hydrocracking and hydroisomerization, and some reactions belong to the secondary reaction of a product.Hydroconversion reactions part effluent contains unreacted hydrogen, conversion and unconverted hydro carbons and gas products, and these gas products comprise normally gaseous hydrocarbon and foreign gas such as H ₂S, NH ₃, H ₂O.Usually, the hydroconversion process reaction effluent is separated into the hydrogen-rich gas and the hydrocarbon liquid that are circulated to reactive moieties and generates oil, common described hydrocarbon liquid generates the oily narrow fraction that obtains through fractionation and can be used as product or other hydroconversion process raw material or catalytically cracked material, especially, in hydrocracking process, it can be narrow fraction liquid product such as light naphthar, heavy naphtha, kerosene, diesel oil and hydrocracking tail oil by fractionation that described hydrocarbon liquid generates oil, can return some narrow fraction oil to reactive moieties.The initially-separate of described reaction effluent normally adopts " cold minute flow process " to finish.In cold minute flow process, reaction effluent is cooled to suitable temperature (being generally 25～65 ℃), is separated into then that hydrocarbon liquid generates oil and its hydrogen concentration is enough to be circulated to the hydrogen-rich gas that reactive moieties is used.Flow process can obtain maximum hydrogen recovery rate and raising recycle hydrogen hydrogen concentration by reducing oily ability and the oily receptivity to hydrogen of reduction generation that absorbs the conventional gas hydrocarbon of separation temperature enhancing generation in cold minute, but a considerable amount of heat energy in the loss reaction effluent still have a certain amount of dissolved hydrogen hydrogen loss simultaneously.The another kind of method of finishing the initially-separate of reaction effluent is " a thermoanalysis journey ", it can improve reaction effluent heat energy utilization rate, reduces the reaction effluent cooling load and reduce the cooling heat exchanger area, but, because reaction effluent contains more dissolved hydrogen in the hydrocarbon liquid that high pressure hot separator is discharged, it can increase hydrogen loss, because the hydrocarbon liquid quantity that cold high pressure separator is discharged reduces, it can reduce the recycle hydrogen hydrogen concentration and increase hydrogen loss.Simultaneously, the thermal high that high pressure hot separator is discharged separates gas and is cooled to certain low temperature and enters cold high pressure separator and finish gas-liquid separation to obtain the process of circulating hydrogen, still has the investment of a considerable amount of heat-energy losses and corresponding cooling equipment inevitably.

This section is described coal-tar base hydrocarbon hydroconversion process.The coal-tar base hydro carbons refers to from coal tar or coal tar time processing (such as coal tar distillation) or coal tar secondary processing (such as visbreaking thermally splitting, the coking thermally splitting of coal-tar pitch) gained hydro carbons.The coal-tar base hydrocarbon hydrogenating conversion process comprises coal tar hydrogenation modification process and coal tar hydrocracking process, and the depth of conversion of raw material and raw material hydrocarbon unit's hydrogen consumption have well-known difference.This paper does not use the reason of " coal tar hydrorefining process " saying to be: coal tar contains a large amount of assorted elements and considerable part is positioned on the loop chain, a large amount of " removing assorted element reaction " that " coal tar hydrorefining process " takes place itself is exactly " chain rupture or ring-opening reaction ", promptly there be " the hydrofining cracking effect of coal tar ", very easily cause the chaos of conception.Hydrogenation deoxidation, the hydrogenation alkene that typical coal tar hydrogenation modification process comprises hydrocarbon raw material is saturated, hydrodemetallation (HDM), hydrogenating desulfurization, hydrodenitrification and aromatic hydrocarbons are saturated, and its raw material hydrocarbon unit's hydrogen consumption numerical value is between 2.5～7.0%.Coalite tar distillate hydrogenation upgrading process hydrocarbon unit hydrogen consumption numerical value is usually between 2.5～3.5%, between 3.5～4.5%, coal-tar heavy oil carbolineum hydro-upgrading process hydrocarbon unit hydrogen consumption numerical value is usually between 5.5～7.0% usually for coal-tar middle oil distillate hydrogenation upgrading process hydrocarbon unit hydrogen consumption numerical value.The coal tar hydrocracking process is based on the hydro-upgrading process, further comprises that hydro-upgrading generates " upgrading+cracking " process that oily macromole hydrocarbon is converted into micromolecular cracking process that its raw material hydrocarbon unit's hydrogen consumption numerical value is between 3.5～9.5%.Conventional boiling range is 100～530 ℃ coal tar or a coal tar fraction, possess sulphur content height, nitrogen content height, aromaticity content height, the higher characteristics of polycyclic aromatic hydrocarbon content, to produce diesel oil is the coal-tar base hydrocarbon hydro-upgrading process of target, must finish advanced nitrogen and deeply de-aromatizing, according to state-of-the art, working pressure usually above 13.5MPa, be generally 15～20MPa, belong to high-pressure hydrogenation upgrading process.

As everyone knows, aromaticity content in the coal tar can reach 50～98% usually, nitrogen content can reach 0.3～2.0%, the important goal that coal tar hydrogenation modification is produced the diesel component process is that to finish the aromatic hydrocarbons of desired depth of diesel component saturated, reach the density and the cetane value of expection, because industrial coal tar hydrogenating unit raw material is wide fraction normally, another purpose is to finish advanced nitrogen to produce enough low hydrotreated naphtha or the enough low suitable hydrogenation wax oil of making hydrocracking raw material of nitrogen content of nitrogen content.Carry out in the saturated process of aromatic hydrocarbons at coal tar hydrogenation modification, heteroatomss such as the huge oxygen of the quantity in the coal tar, sulphur, nitrogen transform and have generated a large amount of water, hydrogen sulfide, ammonia components, based on present catalyst for hydro-upgrading technology, the hydrogenation saturation history that betides catalytic active site for aromatic component, wherein ammonia, 2 S component are because competitive adsorption has strong retardation, ammonia is stronger for the saturated retardation of aromatic hydrogenation than hydrogen sulfide, and there is detrimental action in the existence of water component to catalyst strength and stability.The process that coal tar hydrogenation modification is produced diesel component be one based on the saturated reaction process of aromatic hydrocarbons, compare with petroleum fractions hydro-upgrading process with boiling range, coal tar is because oxygen, sulphur, content of heteroatoms such as nitrogen are too high, there is a large amount of water in reaction process, hydrogen sulfide, the ammonia conversion product, the saturated performance of the aromatic hydrocarbons of catalyzer is suppressed significantly, compare with the reaction conditions of low impurity content, consequently coal-tar base hydrocarbon hydro-upgrading gained diesel oil has following characteristics: sulphur content is low, nitrogen content is low, contain more aromatic hydrocarbons, contain more naphthenic hydrocarbon, cetane value is lower, density is higher.

This section hydro-upgrading process R1 that describes coal-tar base hydrocarbon hydro-upgrading gained diesel oil.In hydro-upgrading process R1, because it is low that stock oil has sulphur content, nitrogen content is low, contain more aromatic hydrocarbons, the characteristics that contain more naphthenic hydrocarbon, usually the purpose of its hydro-upgrading be gas yield condition under improve the raw material diesel cetane-number and or reduce density and or reduce condensation point, obtain fine-quality diesel oil, therefore the catalyst for hydro-upgrading that requires R1 to use has low cracking rate (cracking rate be lower than 15% even be lower than 8%), can significantly improve cetane value or reduce density or the reduction condensation point, promptly possesses high reaction preference and low hydrogen consumption, therefore described catalyst for hydro-upgrading R1C can be diesel oil high-pressure hydrogenation aromatic hydrocarbon saturation catalyst (the diesel oil weight yield is usually above 90%) or diesel oil selective hydrogenation open loop cracking catalyst (the diesel oil weight yield is usually above 93%) or precious metal high selectivity arene saturation catalyst (diesel oil weight yield about 100%), can certainly use hydrocracking catalyst for specific purpose, but, in order to ask most high diesel yield, low hydrogen consumption is not selected hydrocracking catalyst usually for use.According to state-of-the art, the working pressure of hydro-upgrading process R1 can be lower than 13.5MPa usually, be generally 6.0～10.0MPa, belongs to the MHUG process.Have diesel component selective hydrogenation open loop and take off the catalyzer of aryl functional, it can be any one suitable diesel oil selective hydrogenation open loop dearomatization catalyst, it can be the high aromaticity content catalytic diesel oil of typical petroleum base selective hydrogenation open loop dearomatization catalyst, these technology have the MCI technology of China Petroleum and Chemical Corporation Fushun Petrochemical Research Institute, the RICH technology of Beijing Research Institute of Petro-Chemical Engineering of Sinopec Group etc., and the document of putting down in writing this class technology sees Table 1.When using catalyst for hydro-upgrading R1C, the lysate diesel yield of raw material diesel component: generally greater than 85%, usually greater than 90%, more preferably greater than 95%.Catalyst for hydro-upgrading R1C, it also can be the new single catalyst that possesses above-mentioned comprehensive function of specialized designs preparation, also can be the multiple catalyst combination scheme that possesses above-mentioned comprehensive function that forms with multiple catalyzer grating, that is to say that catalyst for hydro-upgrading R1C can comprise a kind of, two or more catalyzer.As required, after hydro-sweetening catalyst agent bed can be set, this point is the common usage of hydrocracking process, when preventing to use sulphided state cracking catalyst for hydro-upgrading R1C, the light hydrocarbons liquid product of hydro-upgrading reaction (liquefied gas and or gasoline fraction) corrosion index or sulphur content exceed standard.

The publication of table 1 record selective hydrogenation open loop dearomatization catalyst

Compositing characteristic based on coal-tar base hydrocarbon hydro-upgrading gained diesel oil, raw material hydrocarbon unit's hydrogen consumption of the hydro-upgrading process R1 of coal-tar base hydrocarbon hydro-upgrading gained diesel oil is far below the raw material hydrocarbon unit weight hydrogen consumption of coal tar hydrogenation modification process, usually its numerical value is between 0.7～1.2%, it is 40～60% that common coal tar hydrogenation modification generates oily diesel oil distillate yield, therefore this hydrogen consumption conversion is 0.28～0.72% of coal tar raw material hydrogen consumption, because this process hydrogen consumption is little, thermal discharge is less, the thermophore recycle hydrogen quantity that is mainly used in the temperature rise of control bed is less, be that hydrogen to oil volume ratio is lower usually, can be controlled between 600～800, the hydrogen of this hydrogen to oil volume ratio all conversion is equivalent to 2.45～4.91% for coal tar raw material hydrocarbon unit hydrogen consumption numerical value.Clearly, the coal tar hydrogenation modification process is the coal tar hydrocracking process especially, and all new hydrogen amount can satisfy the hydrogen total amount (summation of reactor inlet amount of hydrogen and cold hydrogen quantity) that coal tar hydrogenation modification generates the hydro-upgrading process of oily diesel oil.And core purpose of the present invention be utilize the quantity of such new hydrogen logistics big, the characteristics of purity high impurity such as () no hydrogen sulfide, form hydrocarbon hydroconversion process combination process.

When factory construction coal tar hydrogenation modification device A (being generally the high consumption of high pressure hydrogen hydrogenation process), when building coal tar hydrogenation modification simultaneously and generating oily diesel oil fraction hydrogenating modification device B (force down in being generally consumption hydrogen hydrogenation process), will face following situation according to prior art: on the one hand, in order to simplify flow process, to reduce investment, usually consider that the system combined setting of recycle hydrogen is that reaction process adopts identical pressure, cause device A working pressure to raise and increase investment and energy consumption (new hydrogen compressed energy consumption and stock oil pressurization energy consumption); On the other hand, set up separately independently reactive system, select for use suitable separately reaction pressure to finish the hydrogenation reaction of expection, then the flow process complexity causes investment bigger.The present invention proposes a kind of reaction process hydrogen consumption and differs the combined method that big, reaction pressure differs bigger hydrocarbon hydroconversion process, addresses the above problem.

Have multiple about the combination process that contains two or more hydroconversion process, as method as described in US 2671754, US 3026260, US 3365388, US 3592758, US 3655551, the US 5026472, its common trait is that the hydrocarbon liquid product of upstream reaction zone effluent sepn process gained carries out the secondary hydrocracking as downstream reaction district hydrocarbon feed.Chinese patent CN 10169668 relates to a kind of logistics that will contain heavy hydrocarbon under the hydrogen existence condition and is transformed into the method that contains the low boiling point hydrocarbon logistics, the main conversion fluid stream of its first conversion zone raw material, first section effluent is separated into air-flow and liquid stream at separate part, air-flow enters second conversion zone, and second conversion zone mainly transforms hydro carbons in the air-flow.The Chinese patent ZL patent No. 99103876.2 relates to a kind of converting and combining method for hydrogenation of hydrocarbon, and its core feature is: the thermal high of first reaction effluent separates gas dependence self pressure and enters second reactive moieties, saves the special-purpose recycle hydrogen flow of second reactive moieties.Above patent does not all relate to the combined method of the hydrocarbon hydroconversion process that working pressure difference is big, the hydrogen consumption differs greatly.

Technical solution of the present invention is not appeared in the newspapers.

First purpose of the present invention is to propose a kind of coal tar hydrogenating and transforms integrated approach, utilizes new hydrogen logistics to finish the further hydro-upgrading process of coal tar hydrogenation modification gained diesel oil.

Second purpose of the present invention is to propose a kind of high nitrogen high aromatic oil hydrocracking integrated approach, utilizes new hydrogen logistics to finish the further hydro-upgrading process of high nitrogen high aromatic oil hydro-upgrading gained diesel oil.

Summary of the invention

The high aromatic hydrocarbons intermediate oil of the high nitrogen of a kind of two-stage method of the present invention hydrogenating conversion process is characterized in that comprising following steps:

1. at the first reactive moieties R1, the new hydrogen FH and the first hydrocarbon raw material F1 generate first a reaction effluent E1 who contains components such as hydrogen, hydro carbons through the hydro-upgrading reaction;

2. at the first reaction effluent high pressure separate part S1, the first reaction effluent E1 is separated into the first high pressure hydrogen-rich gas V1 that contains most of hydrogen among the first reaction effluent E1, most of conventional gas hydrocarbon component and small part conventional liq hydrocarbon component and contains the oily L1 of first generation of most of conventional liq hydrocarbon component among the first reaction effluent E1;

3. the described first high pressure hydrogen-rich gas V1 of at least a portion is imported the 4. described second reactive moieties R2 of step;

4. at the second reactive moieties R2, the high nitrogen high aromatic oil second hydrocarbon raw material F2 generates second a reaction effluent E2 who contains components such as hydrogen, hydro carbons through the hydro-upgrading reaction under the hydrogen existence condition;

5. at the second reaction effluent high pressure separate part S2, the second reaction effluent E2 is separated into the second high pressure hydrogen-rich gas V2 that contains most of hydrogen among the second reaction effluent E2, most of conventional gas hydrocarbon component and small part conventional liq hydrocarbon component and contains the oily L2 of second generation of most of conventional liq hydrocarbon component among the second reaction effluent E2;

6. the described second high pressure hydrogen-rich gas V2 of at least a portion is returned the 4. described second reactive moieties R2 of step;

7. generate oil content second and heat up in a steamer part FRAC, separate the oily L2 of second generation and obtain diesel oil distillate DS;

8. part of fraction of fuel-oil DS enters the first reactive moieties R1 as the first hydrocarbon raw material F1 at least.

The present invention is particularly suitable for the situation that the second hydrocarbon raw material F2 is middle coalite tar base hydrocarbon.

The present invention first hydrocarbon raw material F1 and the second reaction effluent E2 heat exchange enter the first reactive moieties R1 after heating up, can reclaim heat energy superfluous among the second reaction effluent E2, and when the catalyzer of the first reactive moieties R1 during for the deeply de-aromatizing noble metal catalyst of anti-sulphur not (hydrogenation dearomatization catalyst) with the saturated and low cracking function of good aromatic hydrocarbons, because the first reactive moieties R1 temperature of reaction is than low many of the second reactive moieties R2 temperature of reaction, first hydrocracking part can not be provided with reaction feed (hydrogen and or stock oil) process furnace usually.

The common recycle second high pressure hydrogen-rich gas V2, the described second high pressure hydrogen-rich gas V2 of at least a portion (most of to whole) returns the second reactive moieties R2 and recycles.The hydrogen volume concentration of the described second cold anticyclone hydrogen-rich gas V2 is not less than 70% usually, generally is not less than 75%, preferably is higher than 80%.

The working pressure of the described second reactive moieties R2 is higher than the difference of the working pressure of the first reactive moieties R1: be not less than 3.0MPa usually, generally be not less than 5.0MPa.

The catalyzer of the described first reactive moieties R1, can be to have optionally catalyst for hydro-upgrading of the saturated and higher open loop of good aromatic hydrocarbons, can be the deeply de-aromatizing noble metal catalyst of not anti-sulphur, also can be the two combination (first raw material hydrocarbon F1 series connection by using the deeply de-aromatizing noble metal catalyst of anti-sulphur not (hydrogenation dearomatization catalyst) with the saturated and low cracking function of good aromatic hydrocarbons preposition bed and the use sulfide type have an optionally rearmounted bed of catalyst for hydro-upgrading of the saturated and higher open loop of good aromatic hydrocarbons).

When condition was suitable, effect of the present invention was: first hydrocracking part is not provided with special-purpose circulating hydrogen compressor, and first hydrocracking part is not provided with reaction feed (hydrogen and or stock oil) process furnace.

The operational condition of each step of the present invention is generally:

1. the working pressure of the first reactive moieties R1 is that 3.5～20.0MPa, service temperature are 200～420 ℃;

2. the service temperature of the first cold anticyclone separate part S1 is below 100 ℃; The special-purpose circulating hydrogen compressor of first reactive moieties is not set;

4. the working pressure of the second reactive moieties R2 is that 3.5～28.0MPa, service temperature are 250～480 ℃;

5. the service temperature of the second cold anticyclone separate part S2 is below 100 ℃.

The operational condition of each step of the present invention is preferably:

1. the working pressure of the first reactive moieties R1 is that 3.5～13.5MPa, service temperature are that 200～400 ℃, hydrogen/stock oil volume ratio are 300: 1～1000: 1;

2. the first cold anticyclone separate part S1 service temperature is 30～65 ℃; The special-purpose circulating hydrogen compressor of first reactive moieties is not set;

4. the working pressure of the second reactive moieties R2 is that 13.5～25.0MPa, service temperature are 270～440 ℃;

5. the service temperature of the second cold anticyclone separate part S2 is 30～65 ℃.

When the present invention was applied to coal-tar base hydrocarbon hydroconversion process, the operational condition of each step was generally:

1. the first raw material hydrocarbon F1 is that 170～370 ℃ of diesel components are formed by conventional boiling range mainly, and the operational condition of the first reactive moieties R1 is: temperature is 250 ℃～480 ℃, and pressure is 3.5～20.0MPa, and the hydrogenation catalyst volume space velocity is 0.05～15hr ^-1, hydrogen/stock oil volume ratio is 400: 1～800: 1; The first hydrocarbon raw material F1 in the unit weight hydrogen consumption of the first reactive moieties R1 less than 2%;

4. the second raw material hydrocarbon F2 is the coal-tar base distillate, and the operational condition of the second reactive moieties R2 is: temperature is 250～480 ℃, and pressure is 8.0～25.0MPa; The hydrogenation catalyst volume space velocity is 0.05～15hr ^-1, hydrogen/stock oil volume ratio is 400: 1～4000: 1; The second hydrocarbon raw material F2 in the unit weight hydrogen consumption of the second reactive moieties R2 greater than 3%; The working pressure of the second reactive moieties R2 is than the working pressure height of first reactive moieties R1 3.0MPa at least;

1. the first hydrocarbon raw material F1 in the unit weight hydrogen consumption of the first reactive moieties R2 less than 1.5%;

2. the service temperature of the first cold anticyclone separate part S1 is 35～60 ℃;

4. the second hydrocarbon raw material F2 in the unit weight hydrogen consumption of the second reactive moieties R2 greater than 4.0%; The working pressure of the second reactive moieties R2 is than the working pressure height of first reactive moieties R1 5.0MPa at least;

5. the service temperature of the second cold anticyclone separate part S2 is 35～60 ℃.

When the present invention was applied to coal-tar base hydrocarbon hydroconversion process, the operational condition of each step was preferably:

1. the first hydrocarbon raw material F1 in the unit weight hydrogen consumption of the first reactive moieties R2 less than 1.3%;

2. the service temperature of the first cold anticyclone separate part S1 is 40～55 ℃;

4. the second hydrocarbon raw material F2 in the unit weight hydrogen consumption of the second reactive moieties R2 greater than 5.0%; The working pressure of the second reactive moieties R2 is than the working pressure height of first reactive moieties R1 7.0MPa at least;

5. the service temperature of the second cold anticyclone separate part S2 is 40～55 ℃.

The present invention can further comprise the hydrocracking process of coal-tar base distillate hydrogenation upgrading gained wax oil:

7. generate oil content second and heat up in a steamer part FRAC, separate the oily L2 of second generation and obtain the main cut VS that forms by the wax oil component;

9. at least a portion cut VS is entered the 3rd reactive moieties R3 as the 3rd hydrocarbon raw material F3,

10. at the 3rd reactive moieties R3, the 3rd hydrocarbon raw material F3 generates the 3rd a reaction effluent E3 who contains components such as hydrogen, hydro carbons through hydrocracking reaction under the hydrogen existence condition; Separate E3 and obtain the 3rd high pressure hydrogen-rich gas V1 that forms by most of hydrogen, most of conventional gas hydrocarbon component and small part conventional liq hydrocarbon component among the E3 and the oily L3 of the 3rd generation that forms by the most of conventional liq hydrocarbon component among the E3, the oily L3 of at least a portion the 3rd generation finally enters the second generation oil content and heats up in a steamer part FRAC, and the 3rd diesel component that generates among the oily L3 enters among the diesel oil distillate DS.

The 3rd generates oily L3 finally enters second and generate one of mode that oil content heats up in a steamer part FRAC and be: 10. the 3rd reaction effluent E3 enters the 5. described second cold anticyclone separate part S2 of step, most of hydrogen among the E3, most of conventional gas hydrocarbon component and small part conventional liq hydrocarbon component enter among the second high pressure hydrogen-rich gas V2, and the most of conventional liq hydrocarbon component among the E1 enters second and generates among the oily L2.

The 3rd generates oily L3 finally enters second and generate one of mode that oil content heats up in a steamer part FRAC and be: 10. the 3rd reaction effluent E3 enters the 4. described second reactive moieties R2 of step and contacts with the second reactive moieties hydrogenation catalyst.

Because entering the second generation oil content, the oily L3 of the 3rd generation of the 3rd reactive moieties R3 heats up in a steamer part FRAC, diesel component among the oily L3 of the 3rd generation enters among the diesel oil distillate DS and finally obtains high yield upgrading at the first reactive moieties R1, therefore, use the high hydrocracking catalyst of diesel yield at the 3rd reactive moieties R3, can obtain the summation effect that reduces working pressure, low hydrogen is consumed, increases diesel yield.

The operational condition of the 3rd reactive moieties R3 is generally: temperature is 250～480 ℃, and pressure is 3.5～28.0MPa; The hydrogenation catalyst volume space velocity is 0.05～15hr ^-1, hydrogen/stock oil volume ratio is 400: 1～4000: 1.

The operational condition of the 3rd reactive moieties R3 is generally: temperature is 300～420 ℃, and pressure is 3.5～13.5MPa; The hydrogenation catalyst volume space velocity is 0.2～1.5hr ^-1, hydrogen/stock oil volume ratio is 600: 1～1500: 1.

The working pressure of the working pressure of the 3rd reactive moieties R3 and the first reactive moieties R1, suitable basically identical.

Embodiment

Below describe the present invention in detail.

Pressure of the present invention is absolute pressure.

The composition of component of the present invention or concentration or content or yield value unless stated otherwise, are the weight basis value.

Proportion of the present invention unless stated otherwise, refers to the ratio of water-mass density under fluid density and normal pressure under normal pressure, the 15.6 ℃ of conditions, the 15.6 ℃ of conditions.

Impurity composition of the present invention or impurity element refer to the hydride of non-hydrocarbon component in the reaction raw materials such as water, ammonia, hydrogen sulfide, hydrogenchloride etc.

Conventional gas hydrocarbon of the present invention refers to and is the gasiform hydro carbons under the normal condition, comprises methane, ethane, propane, butane.

Conventional liq hydrocarbon of the present invention refers to the hydro carbons that is in a liquid state under the normal condition, comprises the hydro carbons that pentane and boiling point thereof are higher.

" conventional boiling point " described herein speech refers to the vapor-liquid equilibrium temperature of material under a standard atmosphere pressure condition.Unless dated especially, boiling point described herein refers to conventional boiling temperature.Can measure its boiling temperature with the ASTM-D86 method for gasoline and lighter hydro carbons, can test its boiling temperature with the ASTM-D1160 method for heavy gas oil and heavier charging.Gasoline boiling point boiling range is about 80～210 ℃, the conventional boiling point boiling range of light gas oil is about 150～350 ℃, and heavy oil is conventional boiling point boiling range be about 350～540 ℃ gas oil and boiling point at the residual oil more than 350 ℃ and boiling point at the vacuum residuum more than 550 ℃, unless dated especially, the boiling point boiling range refers to the conventional boiling temperature scope from 5% cut point to 95% cut point.

Petroleum naphtha component of the present invention or gasoline component refer to conventional boiling point and are lower than 180 ℃ conventional liq hydrocarbon.

It is 180～355 ℃ hydro carbons that diesel component of the present invention refers to conventional boiling point.

It is 355～530 ℃ hydro carbons that wax oil component of the present invention refers to conventional boiling point.

Two-stage method hydrocarbon oil hydrogenation conversion process of the present invention refers to hydrotreatment process that raw material hydrocarbon is converted into the finished product and comprises two hydrogenation reaction systems (one-stage hydrogenation reactive system and secondary hydrogenation reactive system) and supporting hydrogenated oil separate part (secondary hydrogenation generates separating of oil part and the one-stage hydrogenation that may exist generates separating of oil part).Two hydrogenation reaction systems form overall serial flow on the stock oil flow process.

The hydrogenated oil separate part is separated into the narrow fraction oil product with hydrogenated oil, uses equipment such as separation column usually.

Owing to contain a large amount of sulphur, nitrogen, oxygen, metal etc. in the coal tar, it is that a large amount of " removing the scission reaction that impurity element forms " takes place for the treating process of target to remove sulphur, nitrogen, oxygen, metal, though its mechanism is different from the leading reaction (such as the long-chain fracture) of the hydrocracking process of petroleum base wax oil, yet on effect, will be difficult to distinguish, therefore in order to prevent the chaos of conception, this paper is divided into coal tar hydrogenation modification process and coal tar hydrocracking process with the coal-tar base hydrocarbon hydrogenating conversion process.

Accompanying drawing is the technical solution of the present invention schema, and accompanying drawing is drawn for the present invention is described, but can not limit range of application of the present invention.

Describe the present invention in detail below in conjunction with accompanying drawing. As shown in drawings, the first hydrocarbon raw material F1 that comes along pipeline 1 with along pipeline 2 and the new hydrogen logistics FH that comes enters the first reactive moieties R1, under certain effectively operating condition, finish first hydroconversion reactions (hydro-upgrading reaction), generate one and contain hydrogen, the first reaction effluent E1 of hydrocarbon component and possible foreign gas, E1 enters the first high pressure separating part S1 along pipeline 4 and finishes a high pressure separation process, generates one and contains most of hydrogen among the first reaction effluent E1, the first high pressure hydrogen-rich gas V1 of the conventional liquid hydrocarbon of foreign gas and normally gaseous hydrocarbon and small part and the oily L1 of first generation that contains most of conventional liquid hydrocarbon among the first reaction effluent E1; The first high pressure hydrogen-rich gas V1 leaves the first high pressure separating part S1 along pipeline 6, and at least a portion V1 imports the described second reactive moieties R2, and shown in the figure is the situation that whole V1 import the second reactive moieties R2. The second hydrocarbon raw material F2 (high nitrogen high aromatic oil is such as middle coalite tar) that comes along pipeline 7 with along pipeline 6 and the high pressure hydrogen-rich gas V1 that comes and may with along pipeline 8 and other hydrogen-rich gas that comes enters the second reactive moieties R2, under certain effectively operating condition, finish second hydroconversion reactions, generate second a reaction effluent E2 who contains hydrogen, foreign gas and hydrocarbon component; E2 enters the second high pressure separating part S2 along pipeline 12 and finishes a high pressure separation process, generates second a high pressure hydrogen-rich gas V2 who contains the conventional liquid hydrocarbon of most of hydrogen, foreign gas and normally gaseous hydrocarbon and small part among the second reaction effluent E2 and one and contains second of most of conventional liquid hydrocarbon and dissolved hydrogen among the second reaction effluent E2 and generate oily L2; The second high pressure hydrogen-rich gas V2 leaves the second high pressure separating part S2 along pipeline 20, and second generates oily L2 leaves the second high pressure separating part S2 along pipeline 30.

The present invention second high pressure hydrogen-rich gas V2 leaves cold anticyclone separating part S2 along pipeline 20, and at least a portion V2 returns the second reactive moieties R2 and/or the first reactive moieties R1, and V2 all returns the second reactive moieties R2 usually. Usually most of to all removing the second reactive moieties R2 as recycle hydrogen after the compressed machine superchargings of V2, the concentrate hydrogen that obtains through membrane separation plant of sub-fraction V2 enters the first reactive moieties R1 (returning in fact the second reactive moieties R2 uses sometimes.

As shown in drawings, that comes along pipeline 30 second generates oily L2 and enters second and generate oil content and heat up in a steamer part FRAC, certain effectively separate and the fractionation operation condition under, can be separated into gas, liquefied gas and narrow fraction such as naphtha, diesel oil DS, wax oil VS etc. Diesel oil DS contains a large amount of aromatic hydrocarbons usually, wherein how mononuclear aromatics has tetrahydrochysene or indane or alkylbenzene or indenes class, and how to reach indane as main take tetrahydrochysene, they derive from the hydro-conversion thing of double ring arene in the coal tar in a large number, are the upgrading objects of the present invention's first reactive moieties.

As shown in drawings, the diesel oil DS that comes along pipeline 40 enters the first reactive moieties R1 along pipeline 1 as the first hydrocarbon raw material F1 after heat exchanger HE and the second reaction effluent E2 heat exchange. The a large amount of heat energy that utilize the second reaction effluent E2 to contain directly heat the first hydrocarbon raw material F1, utilization efficiency of heat energy height. When the first reactive moieties R1 reaction temperature than the second reaction effluent E2 temperature low many time, the first reactive moieties R1 can not arrange the reaction feed heating furnace.

As shown in drawings wax oil VS usually contain a large amount of mononuclear aromatics, double ring arene, cycloalkane as, derive from a large number the conversion product of double ring arene in the coal tar or polycyclic aromatic hydrocarbon, be the cracking object of the present invention the 3rd reactive moieties R3. As shown in drawings, the 3rd hydrocarbon raw material VS that comes along pipeline 50 with along pipeline 51 and the hydrogeneous logistics that comes enters the 3rd reactive moieties R3, under certain effectively operating condition, finish the 3rd hydroconversion reactions (hydrocracking reaction), generate the 3rd a reaction effluent E3 who contains hydrogen, hydrocarbon component and possible foreign gas, E3 leaves the 3rd reactive moieties R3 along pipeline 53 and enters the separating step that third high is pressed hydrogen-rich gas V3 and the oily L3 of the 3rd generation. Finally enter the second generation oil content according to the oily L3 of the present invention's the 3rd generation and heat up in a steamer part FRAC, the 3rd diesel component that generates among the oily L3 enters among the diesel oil DS, the 3rd wax oil component that generates among the oily L3 enters among the wax oil VS, at least a portion or whole wax oil VS enter the 3rd reactive moieties R3 and carry out cracking, and the 3rd reactive moieties R3 can be part circulation cracking flow process or complete alternation cracking flow process.

The oily L3 of the present invention's the 3rd generation finally enters the second generation oil content and heats up in a steamer part FRAC, its advantage is to rely on the second generation oil content to heat up in a steamer the separation that part FRAC finishes the oily L3 of the 3rd generation, significantly simple flow, reduction investment, generate mixing formation diesel oil DS than the poor ignition quality fuel component and can't distinguishing of oil but the 3rd generates fine-quality diesel oil component and second among the oily L3, selectively being lowered of the hydrogenation reaction take the poor ignition quality fuel upgrading as target that diesel oil DS takes place at the first reactive moieties R1, efficiency of investment is lowered. In order to improve the integrated artistic efficiency of investment, the 3rd reactive moieties R3 of the present invention selects the high mild hydrocracking technology of diesel yield, does not excessively pursue its diesel product quality.

There is following features in the hydroconversion process of coal tar fine-quality diesel oil processed, because high nitrogen high aromatic oil is such as medium temperature coal tar, common nitrogen content height, the ammonia that the anterior course of reaction of one section hydrofinishing produces so that one stage hydrofining rear portion course of reaction be in the high environment of ammonia content, the aromatic saturation function of one stage hydrofining rear portion course of reaction Hydrobon catalyst is suppressed significantly, one stage hydrofining generates oily nitrogen content height, the arene content height, one stage hydrofining generates oilstone cerebrol component nitrogen content height, can not directly be used as catalytic reforming aroamtic hydrocarbon raw material processed, need to reduce nitrogen content through advanced treating; In like manner, one stage hydrofining generates oily diesel component nitrogen content height, arene content height, density is big, Cetane number is low, can not directly be used as the fine-quality diesel oil component, need, open loop cracking selective high cracking process strong through the aromatic saturation function to realize high diesel yield, low hydrogen consumption target, improve its Cetane number, reduce density; In like manner, it is big that one stage hydrofining generates oily wax oil component nitrogen content height, arene content height, density, low as its hydrogen content of cracked stock, the knot carbon speed on surface, one way overhydrocracking meeting accelerator activator activated centre, increase the micromolecular secondary cracking side reaction of crackate, need target strong through the aromatic saturation function, that the selective high cracking process of cracking is realized high diesel yield, low hydrogen consumption.

Based on the above fact, the present invention is unified into an integral body with the second reactive moieties R2, the 3rd reactive moieties R3 and the first reactive moieties R1 and treats, in the flow process of the present invention each reaction zone catalyst arrangement can form following features, and thereby realized following target of the present invention:

1. the second reactive moieties R2 uses the hydrogenation catalyst with functions such as removing impurities matter, demetalization, olefin saturated, desulfurization, denitrogenation, aromatic saturations, and the second hydrocarbon raw material F2 coal tar is finished the deep hydrogenation upgrading;

2. the 3rd reactive moieties R3, its raw material VS is that coal tar hydrogenating is processed the secondary hydrogenation wax oil among wax oil and the E2, nitrogen content, arene content has obtained decrease, under low conversion per pass condition, can significantly reduce the hydrocracking temperature, reduce secondary response quantity, prolong operation cycle, cessation reaction when the contained big molecule aromatic hydrocarbons of the 3rd reactive moieties R3 raw material is finished to a certain degree hydrocracking, diesel component among the E3 is imported to the first reactive moieties R1 to be contacted with the diesel modifying catalyst, can realize high diesel yield, the reaction of efficient diesel upgrading, finally on guaranteeing final diesel product (diesel oil among the E1) quality base, provide the integrated artistic diesel yield; Especially, for the big occasion of wax oil VS quantity, can significantly reduce the 3rd reactive moieties R3 operating pressure, decrease investment, remarkable benefit;

3. the first reactive moieties R1 can use the optimized operation condition,, give full play to the diesel modifying catalyst performance, wherein:

The diesel oil that in fact a, the first reactive moieties R1 catalyst R1C are equivalent to the coal tar hydrogenation modification process of the second reactive moieties R2 replenishes the upgrading process, compare with the second reactive moieties R2, because vapor phase ammonia concentration in the course of reaction (simultaneously common concentration of hydrogen sulfide) decrease, can improve the hydro-upgrading efficient of catalyst, improve denitrification percent, improve the aromatic saturation rate;

In fact b, the first reactive moieties R1 catalyst R1C bear the reduction density of the diesel oil of coal tar hydrogenation modification process, the vital task of raising Cetane number, with it is arranged at the second reactive moieties R2 and compares, because vapor phase ammonia concentration in the first reactive moieties R1 course of reaction (simultaneously common concentration of hydrogen sulfide) decrease, can improve reaction efficiency, reduce the R1C operating temperature, reduce gas yield;

In fact c, the first reactive moieties R1 catalyst R1C bear the reduction density of the diesel component of the 3rd reactive moieties R3 course of reaction generation, the vital task of raising Cetane number, increasing along with the 3rd reactive moieties R3 conversion per pass, the second pyrolysis reaction depth of the diesel component that the 3rd reactive moieties R3 course of reaction produces increases, and gas yield increases, the hydrogen consumption increases. Comparatively speaking, reduce the 3rd reactive moieties R3 conversion per pass, suitably control diesel quality index among the E3, the final improvement of diesel component quality is finished by the first reactive moieties R1 catalyst R1C. So, integrated artistic has suppressed the second pyrolysis reaction depth of the diesel component of the 3rd reactive moieties R3 course of reaction generation, can significantly reduce gas yield, reduce the hydrogen consumption, namely to the cracking rate of the 3rd reactive moieties R3 catalyst R3C and the cracking rate of the first reactive moieties R1 catalyst R1C, be optimized combination.

Overall flow of the present invention, can possess simultaneously coal tar hydrogenation modification generation each component of oil (diesel component and wax oil component) is finished the function of denitrogenation and aromatic saturation and suitable cracking function, strengthened overall process the aromatic saturation function, be beneficial to and suppress imperfect cracking reaction, thereby can realize target of the present invention: high catalyst efficiency, high liquid yield (high diesel yield), low unit feed hydrogen consumption, terse flow process.

According to the present invention, be present in the recycle hydrogen of the second reactive moieties R2 and the 3rd reactive moieties R3, can be series relationship or relation in parallel.

As required, use the facilities such as compressor, pump, heat exchanger, valve in relevant pipe-line system.

" the first hydro-conversion part " word refers to herein, comprise the first reactive moieties R1 and the first high pressure separating part S1 and may use first generate oily L1 separate or fractionating step in interior process.

" the second hydro-conversion part " word refers to herein, comprise the second reactive moieties R2 and the second high pressure separating part S2 and may use second generate oily L2 separate or fractionating step in interior process.

" the 3rd hydro-conversion part " word refers to herein, comprise the 3rd reactive moieties R3 and third high press separating part S3 and may use the 3rd generate oily L3 separate or fractionating step in interior process.

Need to prove that the use of " the first hydro-conversion part ", " the second hydro-conversion part ", " the 3rd hydro-conversion part " word does not consist of any restriction to actual content of the present invention just in order to say something.

To specific hydro-conversion integrating process, the practical operation condition of its each reactive moieties depends on the condition as feed composition (being material properties) and process unit process function, changes with the character of the reaction depth of raw material properties, expection and the catalyst that may use. The first reactive moieties R1 hydro-conversion operating condition comprises from reduce density hydro-upgrading condition such as diesel oil, diesel oil reduces condensation point hydro-upgrading condition, diesel oil takes off virtue and improves Cetane number hydro-upgrading condition, the use that diesel oil low hydrogen consumption improves Cetane number has the selective hydrogenation cracking conditions that the catalyst for hydro-upgrading of good aromatic saturation and higher selectivity of ring-opening carries out, middle pressure mild hydrocracking condition such as heavy diesel fuel, diesel oil takes off aromatic hydrocarbons high-pressure hydrogenation upgraded condition etc., can use diesel oil hydrofining catalyst and or diesel oil hydrogenation modification catalyst and or H-G hydrocracking catalyst. The hydrofinishing condition that relaxes is: pressure is lower than 200～350 ℃, liquid hourly space velocity (LHSV) between 3.5～10.5MPa, temperature and is higher than 0.4～3.0h^-1, hydrogen to oil volume ratio is 300～800, feedstock oil Unit Weight hydrogen consumption 0.05～0.8%; Harsh hydro-conversion condition comprises: pressure is that 6.0～20Pa, temperature are that 300～420 ℃, liquid hourly space velocity (LHSV) are 0.2～1.5h^-1, hydrogen to oil volume ratio is 600～1000, feedstock oil Unit Weight hydrogen consumption 0.8～2.0%; Moderate hydro-conversion condition and range is: the pressure of 5.0～10.0MPa, 200～380 ℃ temperature, 0.4～2h^-1Liquid hourly space velocity (LHSV), hydrogen to oil volume ratio are 400～800, feedstock oil Unit Weight hydrogen consumption 0.5～1.5%. The operating pressure of the first reactive moieties R1 of the inventive method is usually above 2.5MPa.

To specific hydro-conversion integrating process, the practical operation condition of its second reactive moieties R2 depends on the condition as feed composition and process unit process function, changes with the character of the reaction depth of raw material properties, expection and the catalyst that may use. The second reactive moieties R2 hydro-conversion operating condition comprises from the chargings such as high consumption hydrogen raw material such as coalite tar, medium temperature coal tar, carbolineum, big flow petroleum base wax oil and removes the required mitigation condition of unifining process of a part of sulphur until the harsh conditions of hydrodesulfurization or middle pressure hydrocracking or hydro-upgrading process wherein comprise the coal tar hydrogenating conversion condition. Coalite tar hydro-upgrading condition is: the pressure of 8.0～12.0MPa, 250～460 ℃ temperature, 0.4～0.8h^-1Liquid hourly space velocity (LHSV), hydrogen to oil volume ratio are 800～1200, feedstock oil Unit Weight hydrogen consumption 2.5～3.5%. Medium temperature coal tar hydro-upgrading condition is: the pressure of 15.0～20.0MPa, 300～460 ℃ temperature, 0.3～0.5h^-1Liquid hourly space velocity (LHSV), hydrogen to oil volume ratio are 1800～3000, feedstock oil Unit Weight hydrogen consumption 3.5～4.5%. High temperature coal-tar carbolineum hydro-upgrading condition is: the pressure of 15.0～25.0MPa, 330～460 ℃ temperature, 0.2～0.4h^-1Liquid hourly space velocity (LHSV), hydrogen to oil volume ratio are 2000～4000, feedstock oil Unit Weight hydrogen consumption 5.5～7.5%. If coal tar adopts hydro-upgrading and the processing of hydrocracking two-stage process, then coal tar raw material oil Unit Weight hydrogen consumption further improves such as improving 0.5～2.0%, changes according to the variation of hydro-upgrading wax oil yield.

Disclosed hydrogenation conversion catalyst has multiple, and the catalyst that wherein some are suitable can be bought from manufacturer. The first reactive moieties R1, the second reactive moieties R2 catalyst system therefor should form and expection process goal and selecting according to raw material, and therefore, the composition excursion of catalyst is very wide. Typical catalyst is made up of (support) one or more metal components on the inorganic matter refractory support that distribute, and the metal component on the catalyst is from the VIII in the periodic table of elements, V and VI family. Selected normally Ni, Co, Mo, Cr and W also contain Fe and Pt sometimes, and the form of the metal on the catalyst can be metallic element or metal oxide or metal sulfide or other compound. Every kind of tenor is 0.1～40wt% of catalyst total amount normally, although the content of metal exceeds above-mentioned scope on some catalyst. The metal active state is the catalyst of sulfide, the metallic compound of the standby catalyst of new system generally uses with oxide form, carrying out then presulfurization processes, this processing procedure can be carried out outside the field of employment, carry out but be preferably within the field of employment, particularly under the condition similar to practical application, carry out. Metal component can be attached on the inorganic amorphous carrier, such as silica, aluminium oxide or silica one aluminium oxide. Can use various technology, comprise dipping, soak and be total to mulling, metal component is attached on the refractory oxide. Used catalyst can be amorphous, the zeolite molecular sieve type or mix less the zeolite molecular sieve type in hydrocracking. Verified, the y-type zeolite of y-type zeolite and modern modification is the good catalyst of character in petroleum base wax oil hydrogenation cracking process. In addition, any technology that can oneself knows by this area comprises dipping and ion-exchange, and metal component is attached on the zeolite. For some hydrocracking process, except zeolite, in catalyst, also may use amorphous silicas one aluminium oxide, and the adhesive that in this class catalyst, usually adopts.

According to the present invention, the operating temperature of the first reactive moieties R1 250 ℃～480 ℃ especially between 300～440 ℃, the first reaction effluent E1 is cooled and is cooled to below 100 ℃, is generally 25～90 ℃, is preferably 30～60 ℃ and enters then among the first cold anticyclone separating part S1 and separate. According to the present invention, should be as far as possible approach with the outlet pressure of the first reactive moieties R1 from the pressure of the first cold anticyclone hydrogen-rich gas V1 of the first cold anticyclone separating part S1, pressure difference value between the two should determine on demand, generally should not be higher than 0.8MPa, should not be higher than 0.6MPa especially.

According to the present invention, the first cold anticyclone hydrogen-rich gas V1 that contains the conventional liquid hydrocarbon of most of hydrogen among the first reaction effluent E1, foreign gas, normally gaseous hydrocarbon and small part, common compressed machine boosts and has entered among the second reactive moieties R2 that transforms the second hydrocarbon raw material F2, and the conversion product of the first cold anticyclone hydrogen-rich gas V1 and unconverted thing have finally entered the second cold anticyclone separating part S2 as the conversion product of other charging of the part of the second reaction effluent E2 and the second reactive moieties R2. Therefore the present invention has realized reusing of hydrogen, and partial impurities gas and the normally gaseous hydrocarbon of part that the first reactive moieties R1 is produced, and the foreign gas and the normally gaseous hydrocarbon that produce with the second reactive moieties R2 concentrate among the second reaction effluent E2.

When the present invention uses cold low separating part S3 step, the first cold anticyclone hydrocarbon liquid L1 is under the substantially constant condition of holding temperature, be depressurized to 0.5～5.0MPa and form gas, the logistics of liquid mixed phase, enter then cold low separating part S3 and be separated into cold low gas V3 and cold low hydrocarbon liquid L3.

When not using cold low separating part S3 step, the first cold anticyclone hydrocarbon liquid L1 may import such as in the such further process of fractionation, but exemplary application low pressure separating part S3.

According to the present invention, the second reactive moieties R2 preferably carries out the high consumption hydrogen hydroconversion reactions of the second hydrocarbon raw material F2. According to the present invention, the operating temperature of the second reactive moieties R2 250～480 ℃, especially between 300～440 ℃. According to the present invention, when the second reaction effluent E2 adopts cold high score flow process, be separated into the second cold anticyclone hydrogen-rich gas V2 and the second cold anticyclone hydrocarbon liquid L2 at the second cold anticyclone separating part S2. The operating temperature of the second cold anticyclone separating part S2 below 100 ℃, especially be generally 25～90 ℃, be preferably 30～60 ℃, the operating pressure of the second cold anticyclone separating part S2, should approach with the outlet pressure of the second reactive moieties R2 as far as possible, pressure difference value between the two should determine on demand, generally be not higher than 1.5MPa, especially be not higher than 1.0MPa, preferably be not higher than 0.7MPa.

According to the present invention, the hydrogen volume concentration that enters the cold low hydrogen-rich gas V4 of first reactive moieties should not be lower than 75%, should not be lower than 80% especially, these hydrogen-rich gases are from the separating step of the second cold anticyclone hydrocarbon liquid L2: the second cold anticyclone hydrocarbon liquid L2 is depressurized under 2.5～15.0MPa pressure condition, be generally below 100 ℃ in temperature, be down to especially 25～85 ℃, preferably under 30～65 ℃ the condition, enter cold low separating part S4, be separated into cold low hydrogen-rich gas V4 and cold low hydrocarbon liquid L4 at this.

According to the present invention, the operating condition of the second cold anticyclone separating part S2, cold low separating part S4, under the condition of recommending, the volumetric concentration that should guarantee hydrogen among the cold low hydrogen-rich gas V4 is not less than 75% or higher, wherein, the temperature of the temperature of cold low separating part S4 and the second cold anticyclone separating part S2 is basic identical. The present invention can reduce the device hydrogen loss by reclaiming the dissolved hydrogen among the hydrocarbon liquid L2.

According to the present invention, cold low hydrocarbon liquid L4 is depressurized to 0.5～5.0MPa and forms gas, the logistics of liquid mixed phase under the substantially constant condition of holding temperature, enters then cold low separating part S5 and is separated into cold low gas V5 and cold low hydrocarbon liquid L5. The operating pressure of cold low separating part S5 is compared basic identical or slightly high 0.3～1.4MPa with the operating pressure of cold low separating part S3.

When not using cold low separating part S5 step, cold low hydrocarbon liquid L4 may directly import such as in the such further process of fractionation, but recommendation low pressure separating part S5.

New hydrogen volume concentration should greater than 90% (volume), especially greater than 95% (volume), more preferably greater than 98% (volume). When first reactive moieties was used noble metal catalyst, the hydrogen sulfide volume content should be lower than 1PPm in the new hydrogen.

Temperature and pressure condition such as following table as each step 1 of the present invention:

250～480 ℃ of 3.5～20.0MPa of the first reactive moieties R1

20～70 ℃ of 3.5～20.0MPa of the first cold anticyclone separating part S1

20～70 ℃ of 0.5～5.0MPa of cold low separating part S3

250～480 ℃ of 3.5～28.0MPa of the second reactive moieties R2

20～70 ℃ of 3.5～28.0MPa of cold anticyclone separating part S2

20～70 ℃ of 3.8～13.8MPa of cold low separating part S4

20～70 ℃ of 0.5～5.0MPa of cold low separating part S5

Each step of the present invention is temperature and pressure condition such as following table preferably:

300～440 ℃ of 3.5～13.5MPa of the first reactive moieties R1

30～65 ℃ of 3.5～13.5MPa of the first cold anticyclone separating part S1

30～65 ℃ of 0.5～2.0MPa of cold low separating part S3

300～440 ℃ of 8.0～25.0MPa of the second reactive moieties R2

30～65 ℃ of 8.0～25.0MPa of cold anticyclone separating part S2

30～65 ℃ of 3.8～16.0MPa of cold low separating part S4

30～65 ℃ of 0.5～3.0MPa of cold low separating part S5

The present invention carries out the effect that can obtain in the situation of coal tar high-pressure hydrogenation upgrading reaction at the second reactive moieties R2. Because middle coalite tar high-pressure hydrogenation upgrading gained diesel oil sulfur content, nitrogen content can be lower, the first reactive moieties R1 can adopt the noble metal dearomatization catalyst, so in the situation of the present invention's coalite tar high-pressure hydrogenation upgrading reaction in the second reactive moieties R2 carries out, can obtain particularly preferred effect

The described first reactive moieties R1 or the second reactive moieties R2, the course of reaction that any additional sulphur can be added as required this reactive moieties, to guarantee necessary minimum concentration of hydrogen sulfide, guarantee that the necessary hydrogen sulfide sectional pressure of catalyst of course of reaction is not less than minimum must value: such as 800PPm or 1000PPm. Described additional sulphur can be sulfide hydrogen maybe can be converted into hydrogen sulfide the coal-tar hydrogenation process is not had the material of ill-effect, such as hydrogen sulfide containing gas or oil product, or with the carbon disulfide that is converted into hydrogen sulfide after high-temperature hydrogen contacts or DMDS etc.

Typical assembled scheme sees Table 2, only is the usefulness of giving an example, and application of the present invention is not consisted of to limit.

The typical assembled scheme of table 2

In the present invention's first hydro-conversion part, the raw material oil-hydrogen mixture contacts the effect of generation expection with catalyst under the hydro-conversion condition, and produce the logistics that one is referred to as reaction effluent usually, usually this logistics is at first carried out heat exchange with one or more strands of materials, then, reaction effluent further cools to about 50 ℃ lower temperature by heat exchanger, aerial cooler or water cooler. At last, through cooled mixed phase logistics, its gas phase is by a large amount of H₂And H₂S、H ₂O, lighter hydrocarbons such as CH₄、C ₂H ₆Deng composition, its liquid phase is made up of hydrocarbon or the hydrocarbon component of condensation, usually in the reaction effluent liquid phase water is arranged. Then, described mixed phase logistics enters a gas, liquid/gas separator. At this, as circulating hydrogen, the liquid phase of telling goes separating part to reclaim product to the gas of telling after possible processing. Owing to contain H in the reaction effluent₂S、NH ₃ Even HCl is arranged, and therefore when cooling off, it can form solids of sedimentation (amassing), and the Main Ingredients and Appearance of these precipitations is NH₄Cl and/or many sulphur ammonia. These precipitations can reduce the heat exchanger rate of heat transfer and cause the pressure drop that exceeds the quata. When first hydrocarbon raw material contains sulphur, nitrogen, empirical method that the common process of recycle hydrogen flow process adopts be set be in the heat exchanger upstream that the steam injection condensed water forms to prevent precipitation in order to described solids of sedimentation is flushed out heat exchanger in the reaction effluent. Water in the reaction effluent may also comprise water that raw material oxycompound hydro-conversion generates or/and as the water that carries of feedstock oil. The cooling reaction effluent usually can generate one and contain by H in the reaction effluent₂S、NH ₃ Separable (dissociating) water of the mixture of the soluble-salt compounds that generates. According to the present invention, when using flushing water, at the cold anticyclone separating part, be separated into cold high score oil, cold high score gas and cold high score water, water component derives from generation water and or the outside washings of hydrogenation process in the cold high score water. At the cold anticyclone separating part, if the enough height of raw material hydrocarbon oxygen content or nitrogen content when enough low so that hydrogenation reaction effluent contains abundant water and therefore do not need outside flushing water, can not add outside flushing water, but this situation are rare.

Characteristics of first hydro-conversion part of the present invention are, owing to do not have recycle hydrogen or only exist and lacked recycle hydrogen, impurity composition, conventional gas hydrocarbon component is eliminated or has been eliminated by major part in the build-up effect of first reactive moieties, in most cases, the notes flushing water process of the first reaction effluent E1 can be cancelled, first cold high pressure separator carries out vapour, liquid two is separated and gets final product, impurity composition among most of first reaction effluent E1, the impurity composition that conventional gas hydrocarbon component and second reactive moieties produce, conventional gas hydrocarbon component merges at the second cold anticyclone separating part to be processed, therefore can simple flow, reduce investment.

At the second cold anticyclone separating part S2, the second reaction effluent E2 reduces earlier temperature (generally being and the second reactive moieties raw material heat exchange) usually to about 220～100 ℃ (this temperature should be higher than sulphur hydrogenation ammonia crystallization temperature), mixes then second reaction effluent after the formation water filling with the washings that add. Washings are used for absorbing ammonia and issuable other impurity such as the hydrogen chloride etc. of second reaction effluent, and the aqueous solution behind the absorbing ammonia must absorb the hydrogen sulfide in second reaction effluent. The described second cold anticyclone separating part comprises cooling, the separating step of second reaction effluent after the water filling, second reaction effluent reduces earlier temperature (usually using aerial cooler and or water cooler) usually to about 30～70 ℃, best 30～60 ℃ after the described water filling, in this temperature-fall period, after the water filling in second reaction effluent water vapour be condensed into gradually liquid phase, hydrogen sulfide after ammonia after the absorption water filling in second reaction effluent and the further absorption water filling in second reaction effluent forms the second cold high score water liquid. Second reaction effluent cooling and in second cold high pressure separator, being separated into after the final described water filling: second a cold anticyclone hydrogen-rich gas V2 gas that on volume, is mainly formed by hydrogen, the second cold anticyclone hydrocarbon liquid L2 and main second a cold high score water W2 liquid that contains ammonia that is formed by water that is mainly formed by the conventional liq hydrocarbon. The described second cold high score water W2, wherein the content of ammonia is generally 1～15% (w), is preferably 3～8% (w). Definite principle of washings injection rate is, on the one hand, washings are divided into vapour phase water and liquid phase water after injecting second reaction effluent, and the liquid phase water yield must be greater than zero, be preferably the washings total amount 30% or more, entirely vaporize to prevent water; On the other hand, the direct purpose of injecting washings is the ammonia that absorbs second reaction effluent at the second cold anticyclone separating part, the ammonia concentration that prevents the second cold anticyclone hydrogen-rich gas V2 is too high, gather at reaction system, reduce catalyst activity, the ammonia concentration of the common second cold anticyclone hydrogen-rich gas V2 is more low more good, generally is not more than 200PPm, preferably is not more than 50PPm; On the one hand, the direct purpose of another of washings is the hydrogen sulfide that absorbs simultaneously in second reaction effluent again, prevents that the process that cools of second reaction effluent from forming sulphur hydrogenation ammonia or many sulphur ammonia Crystallization Plugging heat exchanger channel, increases system pressure drop. The described second cold anticyclone separating part, its second cold high pressure separator operating pressure is that the second reactive moieties pressure deducts actual pressure and falls, the difference of the second cold high pressure separator pressure and the second reactive moieties pressure, should not cross low or too high, be generally 0.5～1.2MPa, be preferably 0.5～0.8MPa. The described second cold anticyclone hydrogen-rich gas V2 gas, its density of hydrogen value, should not be excessively low (causing the device operating pressure to rise), generally should be not less than 70% (v), should be not less than 80% (v), preferably be not less than 85% (v). According to the present invention, as previously mentioned at least a portion, be generally 85～100% the described second cold anticyclone hydrogen-rich gas V2 and enter second reactive moieties and use. In order to improve plant investment efficient, must guarantee that the second cold anticyclone hydrogen-rich gas V2 hydrogen concentration is not less than aforesaid low limit value, for this reason, distribute according to concrete feedstock property, reaction condition, product, can get rid of methane, ethane that the described second cold anticyclone hydrogen-rich gas V2 of a part (hereinafter to be referred as second cold anticyclone hydrogen-rich gas discharging gas) produces to get rid of reaction. For second cold anticyclone hydrogen-rich gas discharging gas, can adopt conventional membrane separation process or pressure swing adsorption technique or oil wash technology to realize that hydrogen separates with non-hydrogen gas component, and the hydrogen that reclaims is used as new hydrogen.

Sometimes the reaction effluent separation process scheme is not directly to cool off and the single-stage separation method, but more complicated separation method such as US3402122, US3586619, US3371029, US3371030, US4159937, US384799 or the described method of Chinese patent CN8919875. First hydro-conversion of flow process of the present invention part or the second hydro-conversion part, its reaction effluent separation method can use any suitable separation method, for example can be cold minute flow process or thermal shunt journey.

A kind of hydrocarbon hydroconversion process mode is the secondary hydro-conversion, the liquid phase stream that the high-pressure separator of first order hydroconversion zone is told (or its separated logistics) and the second level hydroconversion zone that enters the downstream after the hydrogen of some mixes, described second level hydroconversion zone can operate under similar or significantly different conditions, and can use the catalyst that is different from the use of first order hydroconversion zone. For example, heavy oil fraction or coal tar at first carry out hydrofinishing at first order hydroconversion zone, and the liquid-phase product of first order hydroconversion zone enters second level hydroconversion zone reactor to carry out the hydrogenation cracking then. Up to now, a kind of or two kinds of hydro-conversion technological processes partly of existing multiple different use. The variation of technological process has: the reactor in product to the first district in a circulation part first district, or the specific product of a part of Second Region that circulates (generally being heavy component) is to the reactor in first district, or the specific product of a part of Second Region that circulates (generally being heavy component) is to the reactor of Second Region. Flow process of the present invention can be applicable to various possible modified flow, and the present invention can be used for the first order or the second level of secondary hydroconversion process.

The method that accompanying drawing is described comprises that also low pressure is converted to the energy input of logistics of high pressure and the energy that is converted to the logistics of low pressure from high pressure reclaims, to improve energy utilization efficiency. The conventional equipment of use as turbine so perhaps uses the conventional equipment as pump or compressor to import energy in process to reclaim these energy from process.

When the second reactive moieties R2 of second hydro-conversion part uses a plurality of reactors, V1 can enter in the middle of the arbitrary reactor inlet or reactor of second reactive moieties, or enter the second reactive moieties R2 and contact with its beds with any other effective means, V1 contacts the mode of the second reactive moieties R2 beds, and is unrestricted. Such as the pressure minimum point that can enter the second reactive moieties hydrogen closed circuit (circulating hydrogen compressor entrance) or pressure peak (circulating hydrogen compressor outlet) or any reactor.

Major advantage of the present invention is:

1. first reactive moieties utilizes the new hydrogen of second reactive moieties to satisfy first course of reaction recycle hydrogen quantity (in other words hydrogen to oil volume ratio) requirement, reduced significantly the Special circulation hydrogen amount that first reactive moieties exists, therefore, one of effect of the present invention is ideally to cancel the first circulating hydrogen compressor system, thereby significantly reduces investment outlay;

Therefore 2. the new hydrogen of first reactive moieties and second reactive moieties has been realized uniting compression and has been boosted, and two of effect of the present invention are, realized compressor maximization, reduced the make-up hydrogen compressor number of units, cut down the consumption of energy simultaneously thereby significantly saved investment;

3. because most of foreign gas hydrogen sulfide, ammonia that first reactive moieties produces can directly enter second reactive moieties, under the usual conditions, the first reaction effluent separation process can not water filling, can slow down significantly the first cold anticyclone separating part burn into and simplify system;

When 4. the first reactive moieties activity of hydrocatalyst state is sulfide type, usually need to inject sulfur supplementary agent to guarantee the concentration of hydrogen sulfide of necessary reaction gas flow, the part of the foreign gas hydrogen sulfide that first reactive moieties produces has entered second reactive moieties, thereby improved concentration of hydrogen sulfide in the second reaction process gas, for second reactive moieties of reconstructed coal tar, can reduce the consumption that replenishes sulphur;

5. first reactive moieties can arrange not have hydrogen sulfide hydrogenation process, such as noble metal catalyst deeply de-aromatizing hydrogenation unit, diesel yield height, hydrogen consume low, because the first reactive moieties temperature of reaction is low, the second reaction effluent E2 heat exchange of the first hydrocarbon raw material F1 and high potential temperature is reclaimed and is entered the first reactive moieties R1 after heat energy heats up, and the first reactive moieties R1 is not provided with hydrogenation charging process furnace;

6. the first reactive moieties hydrogen purity height can effectively reduce the operation stagnation pressure, reduces construction investment.

7. because the second cold anticyclone separate part pressure is higher than the first cold anticyclone separate part pressure, simple process flow can realize that the second cold high score oil is partly dissolved the recovery of hydrogen: the 3rd separate part is set, the 3rd gas enters the first cold anticyclone separate part and utilizes the first cold high score oil dissolving power to remove the part hydro carbons, then hydrogen component use compressor C2 finish the compression enter second reactive moieties, do not need to be provided with dedicated compressor; When the 3rd gas density of hydrogen was lower than the first cold high score gas density of hydrogen, effect was obvious.

Embodiment one

When going into operation, calculated in device year by 8000 hours/year.

Second hydrogenation process, its hydrocarbon raw material F2 is that boiling range is 165～505 ℃ of coal-tar middle oil distillates, F2 sulphur content 0.65% weight, nitrogen content 0.87% weight, F2 flow rate 62.5t/h, this hydrogenation process raw material hydrocarbon unit hydrogen consumption (comprising dissolved hydrogen) is 6.25% (43430Nm ³/ h).The F2 hydrocracking process adopts the secondary work flow, and the first step is that hydro-upgrading process, the second stage are " heavy gas oil+wax oil " (conventional boiling point between 350～505 ℃ hydro-upgrading wax oil) hydrocracking process.First step hydro-upgrading process hydrogenation conditions is: temperature is that 320～400 ℃, pressure are the condition of high voltage of 16.0～18.0MPa, first reactor inlet amounts of hydrogen 125000Nm ³/ h (hydrogen to oil volume ratio is 2000), beds such as first step hydro-upgrading process uses that hydrodemetallation (HDM), deoxidation, alkene are saturated, desulfurization, denitrogenation, aromatic hydrocarbons are saturated, this hydro-upgrading process raw material hydrocarbon unit hydrogen consumption (comprising dissolved hydrogen) is 5.05% (35091Nm3/h,), the target of second stage reaction process is to make hydrocracking raw material oil 50% (weight) of having an appointment be converted into boiling point and be lower than 350 ℃ conversion product, and boiling point is higher than 350 ℃ no conversion hydrocarbon and all is recycled to the second reactive moieties cracking catalyst bed and realizes full the conversion.

The first hydrocarbon raw material F1 of the present invention's first reactive moieties processing is the narrow fraction diesel oil of second reaction effluent fractionation part, narrow fraction diesel oil character is: boiling range is 170～350 ℃, sulphur content 4PPm (weight), nitrogen content 10PPm (weight), about 43% (weight) of aromaticity content, cetane value 27, and (20 ℃ of volumetric flow rates are 39.8m to F1 flow rate 35t/h ³/ h), the F1 hydro-upgrading is reflected at one and uses 2 to have the saturated and higher open loop of good aromatic hydrocarbons and optionally carry out reactions such as aromatic hydrocarbons is saturated in the reactor of catalyst for hydro-upgrading (MCI catalyzer or RICH catalyzer or the suitable catalyzer of function) bed, and the first reactive moieties reactant gases hydrogen sulfide volumetric concentration is controlled to be 1000PPm; The sulphur content of the hydro-upgrading diesel oil of producing is lower than 1PPm, nitrogen content is lower than 1PPm, cetane value about 33.First hydrogenation conditions is: temperature is that 320～370 ℃, pressure are the middle press strip spare of 6.4～8.0MPa, and this unifining process raw material hydrocarbon unit hydrogen consumption (comprising dissolved hydrogen) is 1.25% (4864Nm ³/ h), the reactor inlet hydrogen to oil volume ratio is 700, reactor inlet hydrogen volume absolute quantity is 27860Nm ³/ h, the second beds cold hydrogen quantity that enters the mouth is less than 7000Nm ³/ h, the two addition, promptly first hydrogenation process is less than 34860Nm with amount of hydrogen ³/ h.

By the present invention, two processes are combined, after being pressurized to 8.5MPa, first reaction process and the new hydrogen logistics of second reaction process FH be divided into two-way, and one tunnel flow rate is 34860Nm ³/ h enters first reactive moieties, remains that new hydrogen by-passing mixes with the first cold anticyclone hydrogen-rich gas after compressor boost enters second reaction process to 18.5MPa.

The main operational condition of its each step sees the following form:

Embodiment according to above-mentioned condition operation, the cold low hydrogen-rich gas V4 that discharges from cold low separate part S4 return the first cold anticyclone separate part S1 contact with the first reaction effluent E1 carry dense, components such as the part methane among the V4 are absorbed, and components such as the unabsorbed hydrogen among the V4 enter the second reactive moieties R2 with the first cold anticyclone hydrogen-rich gas V1 and recycle.

Clearly, build two covers device independent of each other with the branch of routine and compare, embodiment has realized effect of the present invention, mainly shows:

1. saved the special-purpose recycle hydrogen loop compression system of first transform portion, equipment and materials such as relevant high-tension apparatus (two circulating hydrogen compressor, circulating hydrogen compressor separating tank), unit, pipeline, instrument and correlation engineering are saved, and reduce investment outlay about 450～5,000,000 yuan;

2. the new hydrogen compressed procedure division of two reaction process merges, and is very natural, and equipment and material such as relevant high pressure unit, pipeline, instrument and correlation engineering are saved;

3. cancel the notes wash-down water process of the first reaction effluent E1, saved more than 70 ten thousand yuan of construction investments.

Embodiment two

When going into operation, calculated in device year by 8000 hours/year.

Second hydrocracking part is basic identical with embodiment one.Second hydrogenation process, its hydrocarbon raw material F2 is that boiling range is 165～505 ℃ of coal-tar middle oil distillates, the F2 hydrocracking process adopts the secondary work flow, and the first step is that hydro-upgrading process, the second stage are " heavy gas oil+wax oil " (conventional boiling point between 335～505 ℃ hydro-upgrading wax oil) hydrocracking process.

The boiling point that first step hydro-upgrading process generates enters first reactive moieties between 170～335 ℃ diesel oil conversion product as the first hydrocarbon raw material F1, has formed coal tar two-stage hydrogenation combination technique.

The first hydrocarbon raw material F of first reactive moieties processing is the narrow fraction diesel oil of second reaction effluent fractionation part, the narrow fraction diesel boiling range be 170～335 ℃, sulphur content 3PPm (weight), nitrogen content 8PPm (weight), about 38% (weight) of aromaticity content, cetane value 31, (20 ℃ of volumetric flow rates are 33.1m to F1 flow rate 29t/h ³/ h), the F1 hydrofining reaction carries out reactions such as aromatic hydrocarbons is saturated in the reactor of 2 noble metal hydrogenation deeply de-aromatizing beds of a use, and the first reactive moieties reactant gases hydrogen sulfide volumetric concentration is lower than 2PPm; The sulphur content of the hydrofining diesel oil of producing is lower than 1PPm, nitrogen content is lower than 1PPm, and aromaticity content is lower than 5%, cetane value about 38.First hydrogenation conditions is: temperature is that 220～310 ℃, pressure are the middle press strip spare of 6.4～8.0MPa, and this unifining process raw material hydrocarbon unit hydrogen consumption (comprising dissolved hydrogen) is 1.05% (3385Nm ³/ h), the reactor inlet hydrogen to oil volume ratio is 800, reactor inlet hydrogen volume absolute quantity is 26480Nm ³/ h, the second beds cold hydrogen quantity that enters the mouth is less than 2300Nm ³/ h, the two addition, promptly first hydrogenation process is less than 28780Nm with amount of hydrogen ³/ h.

By the present invention, two processes are combined, after being pressurized to 8.5MPa, first reaction process and the new hydrogen logistics of second reaction process FH be divided into two-way, and one tunnel flow rate is 28780Nm ³/ h enters first reactive moieties, remains that new hydrogen by-passing mixes with the first cold anticyclone hydrogen-rich gas after compressor boost enters second reaction process to 18.5MPa.

3. cancelled the reaction feed process furnace of the first reaction effluent E1, the first hydrocarbon raw material F1 and the second reaction effluent E2 heat exchange are reclaimed and are entered the first reactive moieties R1 after heat is warming up to reactor inlet temperature, save about 1,100,000 yuan of construction investment.。

Two invention effects that embodiment shows are present in the combination of other any suitable hydrocarbon hydroconversion process equally.

Claims

1. the hydrocracking integrated approach of a high nitrogen high aromatic oil is characterized in that, comprises following steps:

2. method according to claim 2, its feature further is:

4. the second hydrocarbon raw material F2 is the coal-tar base hydrocarbon.

3. method according to claim 2, its feature further is: 8. the first hydrocarbon raw material F1 and the second reaction effluent E2 heat exchange are reclaimed and are entered the first reactive moieties R1 after heat heats up.

4. integrated technique according to claim 2, its feature further is: 5. the hydrogen volume concentration of the second cold anticyclone hydrogen-rich gas V2 is higher than 75%.

5. method according to claim 2, its feature further is: 5. the hydrogen volume concentration of the second cold anticyclone hydrogen-rich gas V2 is higher than 80%.

6. method according to claim 2, its feature further is: the working pressure of the second reactive moieties R2 is than the working pressure height of first reactive moieties R1 3.0MPa at least.

7. method according to claim 2, its feature further is: the working pressure of the second reactive moieties R2 is than the working pressure height of first reactive moieties R1 5.0MPa at least.

8. method according to claim 2, its feature further is: 1. the catalyzer of the first reactive moieties R1 is the deeply de-aromatizing noble metal catalyst of anti-sulphur not (hydrogenation dearomatization catalyst with the saturated and low cracking function of good aromatic hydrocarbons), and first hydrocracking part is not provided with reaction feed (hydrogen and or stock oil) process furnace.

9. method according to claim 2, its feature further is: 1. the catalyzer of the first reactive moieties R1 is for having optionally catalyst for hydro-upgrading of the saturated and higher open loop of good aromatic hydrocarbons.

10. method according to claim 2, its feature further is: the 1. first reactive moieties R1, the stock oil series connection by using the deeply de-aromatizing noble metal catalyst of anti-sulphur not (hydrogenation dearomatization catalyst) with the saturated and low cracking function of good aromatic hydrocarbons preposition bed and the use sulfide type have an optionally rearmounted bed of catalyst for hydro-upgrading of the saturated and higher open loop of good aromatic hydrocarbons.

11. method according to claim 2, its feature further is:

First hydrocracking part is not provided with special-purpose circulating hydrogen compressor, and first hydrocracking part is not provided with reaction feed (hydrogen and or stock oil) process furnace.

12. according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 described methods, its feature further is:

13. method according to claim 12, its feature further is:

14. according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 described methods, its feature further is:

15. method according to claim 14, its feature further is:

16. method according to claim 15, its feature further is:

17. according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 described methods, its feature further is:

10. at the 3rd reactive moieties R3, the 3rd hydrocarbon raw material F3 generates the 3rd a reaction effluent E3 who contains components such as hydrogen, hydro carbons through hydrocracking reaction under the hydrogen existence condition; Separate E3 and obtain the 3rd high pressure hydrogen-rich gas V1 that forms by most of hydrogen, most of conventional gas hydrocarbon component and small part conventional liq hydrocarbon component among the E3 and the oily L3 of the 3rd generation that forms by the most of conventional liq hydrocarbon component among the E3.

18. method according to claim 17, its feature further is:

7. at least a portion the 3rd generates oily L3 and finally enters second and generate oil content and heat up in a steamer part FRAC, and the 3rd diesel component that generates among the oily L3 enters among the diesel oil distillate DS.

19. method according to claim 18, its feature further is:

10. the 3rd reaction effluent E3 enters the 5. described second cold anticyclone separate part S2 of step, most of hydrogen among the E3, most of conventional gas hydrocarbon component and small part conventional liq hydrocarbon component enter among the second high pressure hydrogen-rich gas V2, and the most of conventional liq hydrocarbon component among the E1 enters second and generates among the oily L2.

20. method according to claim 18, its feature further is: 10. the 3rd reaction effluent E3 enters the 4. described second reactive moieties R2 of step and contacts with the second reactive moieties hydrogenation catalyst.

21. method according to claim 18, its feature further is:

10. at the 3rd reactive moieties R3, use the high hydrocracking catalyst of diesel yield.

22. method according to claim 18, its feature further is: 10. the operational condition of the 3rd reactive moieties R3 is: temperature is 250～480 ℃, and pressure is 3.5～28.0MPa; The hydrogenation catalyst volume space velocity is 0.05～15hr ^-1, hydrogen/stock oil volume ratio is 400: 1～4000: 1.

23. method according to claim 22, its feature further is: 10. the operational condition of the 3rd reactive moieties R3 is: temperature is 300～420 ℃, and pressure is 3.5～13.5MPa; The hydrogenation catalyst volume space velocity is 0.2～1.5hr ^-1, hydrogen/stock oil volume ratio is 600: 1～1500: 1.

24. method according to claim 18, its feature further is:

10. the working pressure basically identical of the working pressure of the 3rd reactive moieties R3 and the first reactive moieties R1.