CN104194828A

CN104194828A - Inferior hydrocarbon hydrogenation method comprising reaction heat recycling step

Info

Publication number: CN104194828A
Application number: CN201410390364.5A
Authority: CN
Inventors: 何巨堂
Original assignee: Individual
Current assignee: Individual
Priority date: 2014-08-06
Filing date: 2014-08-06
Publication date: 2014-12-10

Abstract

The invention discloses an inferior hydrocarbon hydrogenation method comprising a reaction heat recycling step. The inferior hydrocarbon hydrogenation method is applicable to a hydrogenation process of medium/low temperature coal tar. The inferior hydrocarbon hydrogenation method comprises the following steps: feeding inferior hydrocarbon F1 through a first hydrogenation reaction area R1 and a second hydrogenation reaction area R2 which are connected in series, separating first hydrogenation reaction effluent R1P into a gas MTHPS-V and a liquid MTHPS-L in the section thermal high pressure separation process MTHPS, and firstly feeding a part of the high temperature liquid MTHPS-L as circulated material flow MTHPS-LR into a fractionating tower FST which is used for separating out light hydrocarbon fraction F1X from the inferior hydrocarbon F1 to obtain a hydrogenation raw material F1M from which the light hydrocarbon fraction F1X is removed when the high temperature liquid MTHPS-L is introduced into the first hydrogenation reaction area R1, that is, the first hydrogenation reaction heat is directly loaded into the fraction process of the inferior hydrocarbon F1. The inferior hydrocarbon hydrogenation method has the advantages that the process is simple, the heat utilization rate is high, and the operability of related systems can be improved.

Description

A kind of hydrocarbon method of hydrotreating inferior that comprises reaction heat recycling step

Technical field

The present invention relates to a kind of hydrocarbon method of hydrotreating inferior that comprises reaction heat recycling step, be suitable for the hydrogenation process of middle coalite tar, hydrocarbon F1 inferior is by the first hydroconversion reaction zone R1 and the second R2Liang Ge reaction zone, hydroconversion reaction zone of series connection, the first hydrogenation reaction effluent R1P is separated into gas MTHPS-V and liquid MTHPS-L at interval thermal high sepn process MTHPS, using a part of high-temp liquid MTHPS-L when recycle stream MTHPS-LR introduces the first hydroconversion reaction zone R1, make it be introduced into the separation column FST that isolates light fractions F1X and obtain the hydrogenating materials F1M of de-light fractions F1X in hydrocarbon F1 inferior, be about to the fractionation process FS that the first hydrogenation reaction heat is directly written into hydrocarbon F1 inferior, advantage is that flow process is simple, heat utilization ratio is high, and can improve the operability of related system.

Background technology

Middle coalite tar F1 of the present invention, can be that the distillate of coalite tar or middle coalite tar in full cut is such as the coal-tar pitch of middle coalite tar, conventionally contain the easy reactive component of pre-hydrogenation and grade as metal, alkene, phenol, polycyclic aromatic hydrocarbons, gluey pitch shape component, ash, the described easy reactive component of pre-hydrogenation causes catalyst surface coking or deposition of solids conventionally under reaction conditions.Middle coalite tar F1, contains polycyclic aromatic hydrocarbons, condensed-nuclei aromatics, gluey pitch shape component conventionally.The aromatic ring number of condensed-nuclei aromatics mentioned herein is greater than 5, and the aromatic ring number of polycyclic aromatic hydrocarbons is 3～5.

The deep hydrogenation method for modifying of the existing middle coalite tar F1 of part is: middle coalite tar F1 is by the first hydroconversion reaction zone R1 and the second R2Liang Ge reaction zone, hydroconversion reaction zone of series connection, the first hydrogenation reaction effluent R1P is separated into gas MTHPS-V and liquid MTHPS-L at interval thermal high sepn process MTHPS, and a part of high-temp liquid MTHPS-L is introduced to the first hydroconversion reaction zone R1 as loop temperature-control agent logistics MTHPS-LR.The technique that meets above-mentioned flow process feature can be divided into two classes:

1. the first hydroconversion reaction zone R1 is pre-hydrofining reaction process, and the second hydroconversion reaction zone R2 is deep hydrofinishing process, method as listed in table 1;

Table 1 coal tar hydro-conversion method

For coalite tar F1 in the high poor quality that is rich in gluey pitch shape component of the easy reactive component content of pre-hydrogenation, its target product is that the first hydrogenation process R1 that the deep hydrogenation upgrading process of diesel oil distillate generally includes coal tar F1 is i.e. the second hydrogenation process R2 of deep hydrogenation upgrading reaction process R2 of pre-hydrofining reaction process and the first hydrogenation reaction effluent R1P, in order to obtain to greatest extent light-end products as gasoline, diesel oil distillate, conventionally the deep hydrogenation upgrading of gluey pitch shape component is generated to the second heat processing (such as hydrocracking or hydrocracking or coking or catalytic cracking or catalytic pyrolysis etc.) that the conventional boiling point in oil comprises heat cracking reaction higher than the hydrocarbon component of 350 DEG C,

At the pre-hydrotreating reaction process R1 of middle coalite tar F1, conventionally use catalyst for pre-hydrogenation R1C, catalyst for pre-hydrogenation R1C can be hydrogenation protecting agent, olefins hydrogenation agent, hydrogenation deoxidation agent, hydrodemetallation (HDM) agent, hydrogen desulfurization agent, the single dose of aromatic hydrogenation fractional saturation catalyzer etc. or series combination or the mixed loading combination of two agent or multi-agent, under catalyst for pre-hydrogenation R1C existence condition, described middle coalite tar F1 and hydrogen carry out hydrogenation reaction, generate one by hydrogen, impurity component, conventional gas hydrocarbon, the pre-hydrotreating reaction effluent R1P of conventional liq hydrocarbon composition, object based on pre-hydrotreating reaction process R1 is filtering and removing mechanical impurity, olefin saturated, remove metal, remove the organic oxygen of part (such as organic phenol), remove part organosulfur and to the easy reactive component hydrogenation of other parts (such as the hydrogenation of first aromatic ring in polycyclic aromatic hydrocarbons is saturated), therefore the reaction conditions of pre-hydrotreating reaction process R1 comparatively relaxes than the reaction conditions of deep hydrogenation upgrading reaction process R2, conventionally, the good operational condition of pre-hydrotreating reaction process R1 is: temperature is 170～350 DEG C, pressure is 4.0～30.0MPa, catalyst for pre-hydrogenation R1C volume space velocity is 0.05～10.0hr ^-1, hydrogen/stock oil volume ratio is 100: 1～4000: 1, chemical pure hydrogen consumption is 0.15～2.5% (weight of centering coalite tar F1) conventionally,

At deep hydrogenation upgrading reaction process R2, deep hydrogenation modifying catalyst R2C (conventionally at least use possess hydrofining function the exquisite catalyzer R21C of deep hydrogenation, sometimes combine and use the catalyzer R22C that possesses hydrocracking function) under existence condition, described pre-hydrotreating reaction effluent R1P carries out the reaction of deep hydrogenation upgrading, generates a deep hydrogenation upgrading reaction effluent R2P who is made up of hydrogen, impurity component, conventional gas hydrocarbon, conventional liq hydrocarbon; The index request of the upgraded product based on deep hydrogenation upgrading reaction process R2 expection; deep hydrogenation upgrading reaction process R2 conventionally must remove most of sulphur, removes most of the nitrogen, significantly reduces density of aromatic hydrocarbon, improves cetane value, reduce density; conventionally chemical pure hydrogen consumption is 2.5～7.5% (to the weight of coal tar F1), the temperature of reaction of deep hydrogenation upgrading reaction process R2 than the temperature of reaction of pre-hydrotreating reaction process R1 general high 20 DEG C above, conventionally high 50 DEG C above, high more than 90 DEG C especially.The operational condition of the exquisite catalyzer R21C of the deep hydrogenation of deep hydrogenation upgrading reaction process R2 is generally: temperature is that 300～450 DEG C, pressure are that 4.0～30.0MPa, catalyst for refining R21C volume space velocity are 0.1～4.0hr ^-1, hydrogen/stock oil volume ratio is 500: 1～4000: 1.Deep hydrogenation upgrading reaction process R2 sometimes combines to use and possesses the catalyzer R22C of hydrocracking function, and the operational condition of catalyzer R22C is generally: temperature is that 330～440 DEG C, pressure are that 4.0～30.0MPa, catalyzer R22 volume space velocity are 0.5～4.0hr ^-1, hydrogen/stock oil volume ratio is 500: 1～4000: 1;

2. the first hydroconversion reaction zone R1, carry out hydrodemetallation (HDM) reaction and or the basis of removal of ccr by hydrotreating reaction on, also carry out hydrocracking reaction process, the second hydroconversion reaction zone R2 is deep hydrofinishing process, method as listed in table 2; In the time that the first hydroconversion reaction zone R1 also carries out hydrocracking reaction process, the service temperature of the first hydrogenation reaction effluent R1P is conventionally higher, and the service temperature that separates the liquid MTHPS-L obtaining at interval thermal high sepn process MTHPS is common also higher.

Table 2 coal tar hydro-conversion method

The problem that the present invention is concerned about is, for flow process described above, when introduce a part of high-temp liquid MTHPS-L as recycle stream MTHPS-LR the first hydroconversion reaction zone R1 serve as " hydrocarbon F1 inferior release rare dose and or the agent of reaction temperature rising temperature control and or hydrogen supply hydrocarbon and or prevent that bituminous matter from separating out solvent " time, how to utilize the thermophore function of the first hydrogenation process reaction heat that this logistics has, in optimization, coalite tar enters the first hydroconversion reaction zone R1 technological process before, be exactly particularly in how optimizing coalite tar " separate water outlet and or light fractions F1X obtain dehydration and or the hydrogenating materials F1M of de-light fractions F1X " the operating effect of sepn process.

In order to realize above-mentioned target, the present invention proposes the concept that one " utilizes high-temp liquid MTHPS-L to have the function of carrying energy agent of the first hydrogenation reaction heat; the sepn process FS of coalite tar uses as direct heat source in the first hydrogenation process reaction heat is introduced ", there is the operability that flow process is simple, heat utilization ratio is high, also can improve related system.

The method of the invention has no report.

The first object of the present invention is to propose a kind of hydrocarbon method of hydrotreating inferior that comprises reaction heat recycling step.

The second object of the present invention is to propose a kind of method of hydrotreating of the middle coalite tar that comprises reaction heat recycling step, and in the first hydrogenation process reaction heat is introduced, the sepn process FS of coalite tar uses as direct heat source.

Deep hydrogenation upgrading process for the high hydrocarbon material F1 of the pre-easy reactive component content of hydrogenation such as metal, alkene, phenol, colloid, bituminous matter is special, the present invention all can apply with high efficiente callback the first hydroconversion reaction zone reaction heat, and these logistics can be selected from one or more in following material:

1. coalite tar or its distillate or its hot procedure gained oil product;

2. coal-tar middle oil or its distillate or its hot procedure gained oil product;

3. coal-tar heavy oil or its distillate or its hot procedure gained oil product;

4. gelatin liquefaction process gained liquefied coal coil or its distillate or its hot procedure gained oil product;

5. shale oil or its distillate or its hot procedure gained oil product;

6. tar sand basic weight oil or its hot procedure gained oil product;

7. ethylene cracking tar;

8. petroleum base wax oil thermally splitting tar;

9. petroleum base heavy oil thermal course of processing gained oil product, hot procedure is coking heavy oil process or heavy oil catalytic cracking process or heavy oil catalytic pyrolysis process;

10. the high hydrocarbon ils of other easy hydrogenolysis metal content.

Summary of the invention

A kind of hydrocarbon method of hydrotreating inferior that comprises reaction heat recycling step of the present invention, is characterized in that comprising following steps:

(1) at hydrocarbon sepn process FS inferior, use separation column FST in hydrocarbon F1 inferior, separate water outlet and or light fractions F1X obtain dehydration and or the hydrogenating materials F1M of de-light fractions F1X;

Hydrocarbon F1 inferior enters separation column FST, enters separation column FST contact with the logistics based on hydrocarbon F1 inferior from the recycle stream MTHPS-LR of step (3); Hydrogenating materials F1M contains from the component of recycle stream MTHPS-LR with from the component of hydrocarbon F1 inferior;

(2) at the first hydrogenation process R1, under hydrogen and the first hydrogenation catalyst R1C existence condition, hydrogenating materials F1M at least comprise hydrodemetallation (HDM) reaction and or the first hydrogenation reaction R1R of de-carbon residue reaction obtain the first hydrogenation reaction effluent R1P;

(3) thermal high sepn process MTHPS between device, the first hydrogenation reaction effluent R1P is separated into gas MTHPS-V and liquid MTHPS-L; At least a portion gas MTHPS-V enters the second hydrogenation process R2 and contacts with the second hydrogenation catalyst R2C; Separate recycle stream MTHPS-LR and logistics MTHPS-LP from liquid MTHPS-L; At least a portion recycle stream MTHPS-LR enters the described separation column FST of step (1) and finally enters the first hydrogenation process R1 and contacts with the first hydrogenation catalyst R1C; At least a portion logistics MTHPS-LP enters the second hydrogenation process R2 and contacts with the second hydrogenation catalyst R2C;

(4) at the second hydrogenation process R2, under the second hydrogenation catalyst R2C existence condition, described gas MTHPS-V and logistics MTHPS-LP carry out the second hydrogenation reaction, generate a second hydrogenation reaction effluent R2P who is made up of hydrogen, impurity component, conventional gas hydrocarbon, conventional liq hydrocarbon;

(5) at sepn process HPS, separate the second hydrogenation reaction effluent R2P and obtain the hydrogen rich gas gas HPV and the second hydrogenated oil R2P0 that are mainly formed by hydrogen, at least a portion hydrogen rich gas gas HPV returns to hydrogenation process and recycles.

The present invention, the first hydrogenation process R1 carries out pre-hydrofining reaction conventionally, carry out pre-hydrofining reaction at the first hydrogenation process R1, under hydrogen and the first hydrogenation catalyst R1C existence condition, hydrogenating materials F1M comprise hydrodemetallation (HDM) reaction and or the pre-hydrofining reaction R1R of de-carbon residue reaction obtain the first hydrogenation reaction effluent R1P.

The present invention, the first hydrogenation process R1 is carrying out can also carrying out hydrocracking reaction R19R on pre-hydrofining reaction basis, also carry out hydrocracking reaction R19R at the first hydrogenation process R1, the first hydrogenation catalyst R1C also comprises hydrocracking catalyst R19C, and hydrogenating materials F1M carries out being converted into the first hydrogenation reaction effluent R1P after hydrocracking reaction R19R.

The present invention, at hydrocarbon sepn process FS inferior, before hydrocarbon F1 inferior enters separation column FST, from the recycle stream MTHPS-LR of step (3) conventionally with hydrocarbon F1 Hybrid Heating inferior hydrocarbon F1 inferior.

The present invention, at hydrocarbon sepn process FS inferior, hydrocarbon F1 inferior is middle coalite tar, light fractions F1X is generally carbolic oil.

The present invention, at the first hydrogenation process R1, the mode of operation of the bed R1CB of the first hydrogenation catalyst R1C of use can be upflowing or downflow system, can be selected from one or more in following pattern:

1. upflowing suspension bed;

2. upflowing ebullated bed;

3. upflowing microdilatancy bed, described upflowing microdilatancy bed, the beds of its reactor respond raw material by time the maximum height CWH of working order and the ratio K BED of the height CUH of the empty bed static condition of the beds of reactor be defined as bed expansion ratio, KBED is lower than 1.10;

4. upflowing bubbling bed;

5. upflowing moving-bed;

6. upflow fixed bed;

7. down-flow fixed bed;

8. downflow system moving-bed;

9. horizontal bed;

10. tilting bed.

The present invention, at the second hydrogenation process R2, the mode of operation of the bed R2CB of the second hydrogenation catalyst R2C of use can be upflowing or downflow system, can be selected from one or more in following pattern:

1. upflowing ebullated bed;

2. upflowing bubbling bed;

3. upflowing is expanded bed, described upflowing microdilatancy bed, the beds of its reactor respond raw material by time the maximum height CWH of working order and the ratio K BED of the height CUH of the empty bed static condition of the beds of reactor be defined as bed expansion ratio, KBED is lower than 1.10;

4. upflow fixed bed;

5. upflowing moving-bed;

6. down-flow fixed bed;

7. downflow system moving-bed;

8. horizontal bed;

9. tilting bed.

The present invention, thermal high sepn process MTHPS between device, recycle stream MTHPS-LR enters step (1) before, can be through removing the solid process LRDS of taking off of solid particulate matter to remove the solid particulate that is greater than critical diameter DN, can adopt filtration or centrifugation or distillating method, remove that to be greater than critical diameter DN be 20 microns or be the solid particulate of 10 microns.

The present invention, thermal high sepn process MTHPS between device, at least a portion logistics MTHPS-LP enters the second hydrogenation process R2 and contacts with the second hydrogenation catalyst R2C; Logistics MTHPS-LP enters step (4) and is passing through the de-solid process LPDS that removes solid particulate matter to remove the solid particulate that is greater than critical diameter DN before, can adopt filtration or centrifugation or distillating method, remove that to be greater than critical diameter DN be 10 microns or be the solid particulate of 5 microns.

The present invention, thermal high sepn process MTHPS between device, at least a portion logistics MTHPS-LP enters before the second hydrogenation process R2 contacts with the second hydrogenation catalyst R2C, can, first through removing solid particulate matter and removing the process LPDS of conventional boiling point higher than 530 DEG C of hydrocarbon components, obtain the hydrocarbon ils MTHPS-LPX of de-solid, de-heavy constituent; At least a portion hydrocarbon ils MTHPS-LPX enters the second hydrogenation process R2 and contacts with the second hydrogenation catalyst R2C.

The present invention, at hydrocarbon sepn process FS inferior, the separation column FST of use operates conventionally under reduced pressure.

The present invention, hydrocarbon F1 inferior can be selected from one or more in following material:

1. coalite tar or its distillate;

2. coal-tar middle oil or its distillate;

3. coal-tar heavy oil or its distillate;

4. gelatin liquefaction process gained liquefied coal coil or its distillate;

5. shale oil or its distillate;

6. ethylene cracking tar;

7. petroleum base wax oil thermally splitting tar;

8. tar sand basic weight oil or its hot procedure gained oil product, hot procedure is coking heavy oil process or heavy oil catalytic cracking process or heavy oil catalytic pyrolysis process;

10. other aromatic hydrocarbons weight content higher than 50% gluey pitch shape composition weight content higher than 15% hydrocarbon ils.

The present invention, hydrocarbon F1 inferior is middle coalite tar, the easy hydrogenolysis metal concentration taking its contained easy hydrogenolysis metallic compound as benchmark, can be lower than 50PPm or higher than 100PPm or higher than 200PPm.

The present invention, hydrocarbon F1 inferior is middle coalite tar, carry out pre-hydrofining reaction at the first hydrogenation process R1, under hydrogen and the first hydrogenation catalyst R1C existence condition, the pre-hydrofining reaction R1R that hydrogenating materials F1M comprises hydrodemetallation (HDM) reaction and takes off carbon residue reaction obtains the first hydrogenation reaction effluent R1P; The operational condition of the first hydrogenation process R1 can be to improve in the first hydrogenation reaction effluent R1P hydrogen supply hydrocarbon concentration as target to greatest extent.

Action Target of the present invention is generally:

(2) hydrocarbon F1 inferior is middle coalite tar, and the metal content of the conventional liq hydrocarbon in the first hydrogenation reaction effluent R1P is lower than 10PPm; The carbon residue content of the conventional liq hydrocarbon in the first hydrogenation reaction effluent R1P is lower than 1.5%;

Full cut diesel-fuel cetane number in (4) second hydrogenation reaction effluent R2P is higher than 26.

Action Target of the present invention is generally:

(2) hydrocarbon F1 inferior is middle coalite tar, and the metal content of the conventional liq hydrocarbon in the first hydrogenation reaction effluent R1P is lower than 5PPm; The carbon residue content of the conventional liq hydrocarbon in the first hydrogenation reaction effluent R1P is lower than 0.5%;

Full cut diesel-fuel cetane number in (4) second hydrogenation reaction effluent R2P is higher than 35.

The present invention, hydrocracking reaction process R3 can be set, to separate hydro-upgrading heavy oil R2P0-DO that the hydrogenated oil R2P0 gained of the second hydrogenation reaction effluent is mainly made up of higher than 350 DEG C of hydrocarbon conventional boiling point as raw material, be converted into hydrocracking reaction effluent R3P at hydrocracking reaction process R3; Hydrocracking reaction effluent R3P separates after can mixing with the second hydrogenation reaction effluent R2P.

The present invention, sepn process HPS comprises cold anticyclone sepn process LHPS conventionally, at cold anticyclone sepn process LHPS, separate the second hydrogenation reaction effluent R2P and obtain the cold high score gas gas HPV and the cold high score oil LHPL that are mainly made up of hydrogen, cold high score oil LHPL generates oily R2P0 as the second hydrogenation reaction.

The present invention, when sepn process HPS comprises thermal high sepn process THPS and cold anticyclone sepn process LHPS, at thermal high sepn process THPS, separates the second hydrogenation reaction effluent R2P and obtains hot high score gas gas THPV and hot high score oil THPL; At cold anticyclone sepn process LHPS, heat of dissociation high score gas gas THPV obtains the cold high score gas gas HPV and the cold high score oil LHPL that are mainly made up of hydrogen, and the second hydrogenation reaction generates oily R2P0 and comprises hot high score oil THPL and cold high score oil LHPL.

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

(1) hydrocarbon F1 inferior is middle coalite tar, and at hydrocarbon sepn process FS inferior, the separation column FST of use operates under reduced pressure;

The metal content of the conventional liq hydrocarbon in (2) first hydrogenation reaction effluent R1P is lower than 10PPm; The carbon residue content of the conventional liq hydrocarbon in the first hydrogenation reaction effluent R1P is lower than 1.5%;

The operational condition of the first hydrogenation process R1 is: temperature is that 170～350 DEG C, pressure are that 4.0～30.0MPa, the first hydrogenation catalyst R1C volume space velocity are 0.05～10.0hr ^-1, hydrogen/stock oil volume ratio is 100: 1～4000: 1, chemical pure hydrogen consumption is 0.15～2.5% (to the weight of hydrocarbon F1 inferior);

(3) between device, the operational condition of thermal high sepn process MTHPS is: temperature is that 170～350 DEG C, pressure are 4.0～30.0MPa;

(4) carry out deep hydrofinishing reaction process at the second hydrogenation process R2, the full cut diesel-fuel cetane number in the second hydrogenation reaction effluent R2P is higher than 26;

The operational condition of the second hydrogenation process R2 is: temperature is that 300～450 DEG C, pressure are that 4.0～30.0MPa, the second hydrogenation catalyst R21C volume space velocity are 0.1～4.0hr ^-1, hydrogen/stock oil volume ratio is 500: 1～4000: 1.

The metal content of the conventional liq hydrocarbon in (2) first hydrogenation reaction effluent R1P is lower than 5PPm; The carbon residue content of the conventional liq hydrocarbon in the first hydrogenation reaction effluent R1P is lower than 0.5%;

The operational condition of the first hydrogenation process R1 is: temperature is that 210～330 DEG C, pressure are that 12.0～18.0MPa, the first hydrogenation catalyst R1C volume space velocity are 0.2～5.0hr ^-1, hydrogen/stock oil volume ratio is 200: 1～2000: 1, chemical pure hydrogen consumption is 0.50～2.0% (to the weight of hydrocarbon F1 inferior);

(3) between device, the operational condition of thermal high sepn process MTHPS is: temperature is that 210～330 DEG C, pressure are 12.0～18.0MPa;

(4) carry out deep hydrofinishing reaction process at the second hydrogenation process R2, the full cut diesel-fuel cetane number in the second hydrogenation reaction effluent R2P is higher than 35;

The operational condition of the second hydrogenation process R2 is: temperature is that 330～420 DEG C, pressure are that 12.0～18.0MPa, the second hydrogenation catalyst R21C volume space velocity are 0.1～2.0hr ^-1, hydrogen/stock oil volume ratio is 800: 1～3000: 1.

The present invention, between device, the Action Target of thermal high sepn process MTHPS is generally: hot high score oil MTHP-L is mainly made up of higher than the hydrocarbon of 330 DEG C conventional boiling point.

The present invention, between device, the Action Target of thermal high sepn process MTHPS is generally: hot high score oil MTHP-L is mainly made up of higher than the hydrocarbon of 380 DEG C conventional boiling point.

The present invention, when between device, thermal high sepn process MTHPS arranges hydrogen rich gas air lift step:

(3) thermal high sepn process MTHPS between device, the first hydrogenation reaction effluent R1P is separated into gas MTHPS-V and liquid MTHPS-L; At least a portion gas MTHPS-V enters the second hydrogenation process R2 and contacts with the second hydrogenation catalyst R2C;

After hot high score oil MTHPS-L contacts with hydrogen rich gas gas stripping gas VH1, be separated into the hot high score oil MTHPS-LL of de-light constituent and air lift and deviate from gas MTHPS-LV; At least a portion air lift is deviate from gas MTHPS-LV and is entered the second hydrogenation process R2 and contact with the second hydrogenation catalyst R2C;

The hot high score oil of autospasy light constituent MTHPS-LL separates recycle stream MTHPS-LR and logistics MTHPS-LP; At least a portion recycle stream MTHPS-LR enters step (1) and finally enters the first hydrogenation process R1 and contacts with the first hydrogenation catalyst R1C;

At least a portion logistics MTHPS-LP obtains de-solid hydrocarbon ils MTHPS-LPDS after removing solid particulate, and the de-solid hydrocarbon ils MTHPS-LLDS of at least a portion enters the second hydrogenation process R2 and contacts with the second hydrogenation catalyst R2C.

The present invention, the hydrogen rich gas logistics of injecting the first hydrogenation process R1 is preferentially used new hydrogen.

The present invention, at the first hydrogenation process R1, hydrogen sulfide in gas phase volumetric concentration is generally 0.1～5%, is generally 0.3～1.0%.

The present invention, hydrocarbon F1 inferior is middle coalite tar, at hydrocarbon sepn process FS inferior, uses separation column FST in hydrocarbon F1 inferior, to isolate light fractions F1X to obtain the hydrogenating materials F1M of de-light fractions F1X; Light fractions F1X can be conventional boiling point lower than the hydrocarbon-fraction of 250 DEG C or conventional boiling point lower than the hydrocarbon-fraction of 350 DEG C or the conventional boiling point hydrocarbon-fraction lower than 450 DEG C; Light fractions F1X conventionally enters the second hydrogenation process R2 and contacts with the second hydrogenation catalyst R2C.

The present invention, hydrocarbon F1 inferior is middle coalite tar, at hydrocarbon sepn process FS inferior, uses separation column FST in hydrocarbon F1 inferior, to isolate light fractions F1X to obtain the hydrogenating materials F1M of de-light fractions F1X; Light fractions F1X is conventional boiling point lower than the hydrocarbon-fraction of 450 DEG C, and light fractions F1X enters the second hydrogenation process R2 and contacts with the second hydrogenation catalyst R2C; What hydrogenating materials F1M contained is defined as K from the composition weight WA of recycle stream MTHPS-LR with from the ratio of the composition weight WB of hydrocarbon F1 inferior, and K is generally 0.1～10, is generally 0.5～5, is preferably 1.0～3.0.

The present invention, can arrange the pre-hydrofining reaction process F1XR1 of light fractions F1X:

(1) hydrocarbon F1 inferior is middle coalite tar, at hydrocarbon sepn process FS inferior, uses separation column FST in hydrocarbon F1 inferior, to isolate light fractions F1X to obtain the hydrogenating materials F1M of de-light fractions F1X; Light fractions F1X enters the second hydrogenation process R2 and contacts with the second hydrogenation catalyst R2C;

(4) at the second hydrogenation process R2, the pre-hydrofining reaction process F1XR1 of light fractions F1X is set, under the pre-Hydrobon catalyst F1XR1C existence condition of hydrogen and light fractions F1X, light fractions F1X carries out pre-hydrofining reaction F1XR1R and obtains pre-hydrofining reaction effluent F1XR1P; The pre-hydrofining that comprises at least a portion light fractions F1X based on pre-hydrofining reaction effluent F1XR1P generates oily logistics F1XR1PS and enters the second hydrogenation process R2 and contact with the second hydrogenation catalyst R2C.

The present invention, can arrange the de-light constituent step MTHPS-L-FS of liquid MTHPS-L:

Liquid MTHPS-L, through de-light constituent step MTHPS-L-FS, obtains de-light constituent oil MTHPS-L-FS-P and light oil MTHPS-L-FS-L;

At least a portion light oil MTHPS-L-FS-L enters the second hydrogenation process R2 and contacts with the second hydrogenation catalyst R2C;

Autospasy light constituent oil MTHPS-L-FS-P separates recycle stream MTHPS-LR and logistics MTHPS-LP;

At least a portion recycle stream MTHPS-LR enters step (1) and finally enters the first hydrogenation process R1 and contacts with the first hydrogenation catalyst R1C;

At least a portion logistics MTHPS-LP enters the second hydrogenation process R2 and contacts with the second hydrogenation catalyst R2C.

The present invention, the de-light constituent step MTHPS-L-FS of liquid MTHPS-L can be set, its Action Target can be: adopt distillation separation method remove conventional boiling point be usually less than 130 DEG C, generally lower than 200 DEG C, especially lower than the light constituent of 250 DEG C, obtain de-light constituent oil MTHPS-L-FS-P.

The present invention, can control the temperature T A of the hydrogenating materials F1M that leaves separation column FST and hydrogenating materials F1M and enter the temperature difference DT of the initial reaction temperature TB of the first hydrogenation process R1:

(1) hydrocarbon F1 inferior is middle coalite tar, at hydrocarbon sepn process FS inferior, uses separation column FST in hydrocarbon F1 inferior, to isolate light fractions F1X to obtain the hydrogenating materials F1M of de-light fractions F1X; Leave the temperature T A of the hydrogenating materials F1M of separation column FST, the temperature difference that enters the initial reaction temperature TB of the first hydrogenation process R1 with hydrogenating materials F1M is DT, DT absolute value be usually less than 50 DEG C, generally lower than 30 DEG C, especially lower than 10 DEG C.

Embodiment

Below describe the present invention in detail.

Pressure of the present invention, refers to absolute pressure.

Conventional boiling point of the present invention refers to vapour, the liquid equilibrium temperature of material under a barometric point.

Conventional boiling range of the present invention refers to the conventional boiling spread of cut.

Petroleum naphtha of the present invention refers to conventional boiling point lower than the conventional liq hydrocarbon of 180 DEG C.

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

It is the hydro carbons of 355～490 DEG C that wax oil component of the present invention refers to conventional boiling point.

Heavy oil component of the present invention refers to conventional boiling point higher than the hydro carbons of 350 DEG C.

The aromatic ring number of condensed-nuclei aromatics mentioned herein is greater than 5, and the aromatic ring number of polycyclic aromatic hydrocarbons is 3～5.

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

Proportion of the present invention, unless stated otherwise, refers to the ratio of fluid density and normal pressure under normal pressure, 15.6 DEG C of conditions, 15.6 DEG C of Water Under density.

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

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

Impurity composition of the present invention, refers to the hydrocracking thing of non-hydrocarbon component in stock oil as water, ammonia, hydrogen sulfide, hydrogenchloride etc.

Easy hydrogenolysis metal component of the present invention, refer to the metallic compound that hydrogenolysis can occur fast under certain high temperature and hydrogen existence condition, be commonly referred to as oil soluble metal compound as iron naphthenate, calcium naphthenate etc., these components can rapid conversion be that sulfide is as iron sulphide, sulfurated lime under hydrogen sulfide existence condition, and can form particulate state throw out or coprecipitate, under certain condition, particulate matter particle diameter can be grown up.

Coal tar of the present invention, refer to coal tar or its cut of the processes such as the pyrolysis step from pyrolysis of coal or the dry distillation of coal or coal generating gas process, can be by product coalite tar or its cut of coal generating gas, also can be that coal coking pyrolysis of coal process (comprises semi-coking, middle temperature coking, high-temperature coking process) by product coal tar or its cut, coal tar of the present invention can also be the mixing oil of above-mentioned coal tar, coal tar of the present invention can also be that the extract oil that obtains through light hydrocarbon solvent extraction of above-mentioned coal tar is such as diasphaltene coal tar or its distillate.

High-temperature coking belongs to coal high temperature pyrolysis process, and the outlet temperature of pyrolytic process is generally greater than 900 DEG C, conventionally between 1000～1400 DEG C.Described coal-tar heavy oil refers to coal high temperature pyrolysis and produces the by product crude tar oil of coke and/or the production of town gas process.Coal-tar heavy oil is in primary distillation process, conventionally produce following product: the products such as light oil (topping tar), carbolic oil, naphtalene oil, lightweight washing oil, heavy wash oil, lightweight carbolineum, heavy carbolineum, pitch, carbolic oil can further be separated into crude phenols and dephenolize oil, and naphtalene oil can further be separated into thick naphthalene and de-naphtalene oil.Coal-tar heavy oil lighting end of the present invention refers to: carbolineum, washing oil, naphtalene oil, de-naphtalene oil, carbolic oil, dephenolize oil, light oil and mixing oil thereof.

Due to raw coal character and coking or all variations within the specific limits of gas-making process condition, coal tar oil properties also changes within the specific limits.The processing condition of coal tar primary distillation process and product requirement also change within the specific limits, therefore the character of coal tar lighting end also changes within the specific limits.The character of coal tar lighting end, proportion is generally 0.92～1.25, conventional boiling point is generally 60～500 DEG C and is generally 120～460 DEG C, conventionally metal content is that 5～80PPm, sulphur content are 0.4～0.8%, nitrogen content is 0.6～1.4%, oxygen level is 0.4～9.0%, conventionally water-content is 0.2～5.0%, and carbon residue content is generally 0.5～13%.

Conventionally the olefin(e) centent of coal tar lighting end is high, phenol content is high and contain more component of easily reacting under mitigation condition; therefore; the pre-hydrogenation process of coal tar lighting end of the present invention, is used the single dose of hydrogenation protecting agent, olefins hydrogenation agent, hydrogenation deoxidation agent, hydrogen desulfurization agent etc. or series combination or the mixed loading combination of two agent or multi-agent conventionally.

Coal tar heavy fractioning is coal-tar pitch cut particularly; its metal content is high, gum level is high, asphalt content is high; therefore; the pre-hydrogenation process of coal tar heavy fractioning of the present invention, is used the single dose of hydrogenation protecting agent, hydrodemetallation (HDM) agent, hydrogen desulfurization agent etc. or series combination or the mixed loading combination of two agent or multi-agent conventionally

Due to the overwhelming majority of metal concentrate on conventional boiling point higher than 350 DEG C particularly higher than in the cut of 450 DEG C, the therefore pre-hydrogenation process of Main Analysis coal tar heavy fractioning of the present invention.

Experimental study and full scale plant running all show, the pre-hydrotreating reaction process R1 of middle coalite tar, and raw material different components temperature of reaction is realistic according to being divided into following steps from low to high substantially:

The easily decomposition < high reactivity condensed-nuclei aromatics thermal condensation of hydrogenolysis metal fever and the rudimentary sulphur compound hydrogenating desulfurization of the saturated < of hydrogenation, organometallic complex catalytic hydrogenolysis, rudimentary organic phenol catalytic deoxidation, the de-carbon residue of polycyclic aromatic hydrocarbons

Said temperature scope is generally 170～350 DEG C, is generally 210～330 DEG C, clearly, this is the temperature of reaction interval of a wide region, should control first, second, third step for differing temps section according to carrying out stage by stage from low to high, be beneficial to reduction metallic sulfide formation speed, reduce pyrocondensation compound formation speed, prevent from forming stack peak value, realize the depth profiles of easy hydrogenolysis metal deposit at beds, improve the controllability of deposition reaction.

Below describe characteristic of the present invention in detail.

1. upflowing suspension bed;

2. upflowing ebullated bed;

4. upflowing bubbling bed;

5. upflowing moving-bed;

6. upflow fixed bed;

7. down-flow fixed bed;

8. downflow system moving-bed;

9. horizontal bed;

10. tilting bed.

1. upflowing ebullated bed;

2. upflowing bubbling bed;

4. upflow fixed bed;

5. upflowing moving-bed;

6. down-flow fixed bed;

7. downflow system moving-bed;

8. horizontal bed;

9. tilting bed.

1. coalite tar or its distillate;

2. coal-tar middle oil or its distillate;

3. coal-tar heavy oil or its distillate;

4. gelatin liquefaction process gained liquefied coal coil or its distillate;

5. shale oil or its distillate;

6. ethylene cracking tar;

7. petroleum base wax oil thermally splitting tar;

Action Target of the present invention is generally:

As required, any supplementary sulphur can be added to arbitrary hydrogenation process, but normally join the hydrogenation process entrance of upstream, to ensure that the necessary minimum concentration of hydrogen sulfide of reaction process is such as 500PPm (v) or 1000PPm (v) or prescribed value, to ensure that the necessary hydrogen sulfide sectional pressure of catalyzer is not less than minimum prescribed value.Described supplementary sulphur can be the material without undesirable action to hydroconversion process that sulfide hydrogen maybe can be converted into hydrogen sulfide, such as hydrogen sulfide containing gas or oil product, or contacts rear dithiocarbonic anhydride or the Methyl disulfide etc. that generates hydrogen sulfide with high-temperature hydrogen.In the time that the dilution hydrocarbon of pre-hydrotreating reaction process R1 provides with hydrogen sulfide containing hydrogenation reaction effluent form, if hydrogen sulfide quantity wherein meets the needs of pre-hydrotreating reaction process R1, can not re-use sulfur supplementary agent.

Below describe the rule of the high pressure separation process of hydrogenation reaction effluent of the present invention in detail.

The high pressure separation process of hydrogenation reaction effluent comprises cold high pressure separator conventionally, when hydrocarbon ils density in hydrogenation reaction effluent large (such as approaching with water-mass density) or viscosity is large or while being difficult to separate with emulsifying water, also need setting operation temperature to be generally the high pressure hot separator of 150～450 DEG C, now hydrogenation reaction effluent enters high pressure hot separator and be separated into the hot high score fluid body that the hot high score gas gas being mainly made up of hydrogen and are mainly made up of conventional liq hydrocarbon and the solid that may exist on volume, hot high score gas enters the cold high pressure separator that service temperature is generally 20～80 DEG C and is separated into cold high score oil and cold high score gas, because a large amount of high boiling components enter in hot high score fluid body, realize following target: cold high score oil density diminishes or viscosity diminishes or be easy to separate with water.The high pressure separation process of hydrogenation reaction effluent arranges high pressure hot separator, also possesses the advantage that reduces calorific loss, because hot high score fluid body can be avoided the use air cooler of hot high score gas experience or the process that cools of water cooler.Meanwhile, the hydrogenation process that hot part high score fluid body can be returned to upstream recycles, to improve the overall feedstock property of hydrogenation process that receives this turning oil, or to this turning oil hydrogenation that circulates.

Before hydrogenation reaction effluent or hot high score gas enter cold anticyclone separate part, conventionally first reduce temperature (being generally and reactive moieties charging heat exchange) to approximately 220～100 DEG C (these temperature should higher than sulphur hydrogenation ammonia Tc in this hydrogenation reaction effluent gas phase), then conventionally inject wherein washing water and form water filling back end hydrogenation reaction effluent, washing water for absorbing ammonia and issuable other impurity as hydrogenchloride etc., and the inevitable absorbing hydrogen sulphide of the aqueous solution after absorbing ammonia.At cold anticyclone separate part, described water filling back end hydrogenation reaction effluent is separated into: the cold high score gas being mainly made up of hydrogen on volume, cold high score oil, the main cold high score water that be made up of water and that be dissolved with ammonia, hydrogen sulfide being mainly made up of conventional liq hydrocarbon and dissolved hydrogen.Described cold high score water, wherein the content of ammonia is generally 0.5～15% (w), is preferably 1～8% (w).An object of note washing water is ammonia and the hydrogen sulfide absorbing in hydrogenation reaction effluent, prevents from forming sulphur hydrogenation ammonia or many sulphur ammonia Crystallization Plugging heat exchanger channel, increases system pressure drop.The injection rate of described washing water, should determine according to following principle: on the one hand, washing water are divided into vapour phase water and liquid phase water after injecting hydrogenation reaction effluent, and the liquid phase water yield must be greater than zero, is preferably 30% or more of washing water total amount; Again on the one hand, washing water, for absorbing the ammonia of hydrogenation reaction effluent, prevent that the ammonia concentration of high score gas is too high, reduce catalyst activity, conventionally the ammonia volumetric concentration of high score gas is more low better, is generally not more than 200PPm (v), is preferably not more than 50PPm (v).Described cold high pressure separator working pressure is that hydrogenation reaction partial pressure deducts true pressure and falls, and the difference of cold anticyclone separate part working pressure and hydrogenation reaction pressure is unsuitable too low or too high, is generally 0.35～3.2MPa, is generally 0.5～1.5MPa.The hydrogen volume concentration value of described cold high score gas, should not be too low (causing device working 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).As previously mentioned at least a portion, be generally 85～100% cold high score gas and return in hydrogenation reaction part and recycle, so that the necessary amounts of hydrogen of hydrogenation reaction part and hydrogen concentration to be provided; In order to improve plant investment efficiency, must ensure that recycle hydrogen concentration is not less than aforesaid low limit value,, distribute according to concrete feedstock property, reaction conditions, product for this reason, can get rid of methane, ethane that the described cold high score gas of a part produces to get rid of reaction.For the cold high score gas of discharge, can adopt conventional membrane separation process or pressure swing adsorption technique or oil wash technique to realize hydrogen and separate with non-hydrogen component, and the hydrogen reclaiming is used as to new hydrogen.

New hydrogen enters and adds the hydrogen that hydrogen partial consumes to supplement hydrogenation process, and new hydrogen hydrogen concentration is more high better, generally should not be lower than 95% (v), be preferably not less than 99% (v).All new hydrogen can be introduced to arbitrary hydrogenation reaction part, preferably introduce pre-hydrotreating reaction process R1.

The invention has the advantages that:

1. utilize high temperature circulation logistics MTHPS-LR to have the function of carrying energy agent of the first hydrogenation reaction heat, in the first hydrogenation process reaction heat is introduced, the sepn process FS of coalite tar uses as direct heat source, and heat utilization ratio is high;

2. utilize high temperature circulation logistics MTHPS-LR by the sepn process FS of coalite tar in direct the first hydrogenation process reaction heat introducing, saved the necessary interchanger of indirect heat exchange, simplified flow process, can reduce construction investment;

3. centering coalite tar, sneak into recycle stream MTHPS-LR, there is the effect that reduces its viscosity, low its zero pour, particularly mobility and the congealing property of the medium of coal-tar pitch existence range of this medium will be improved, the operability of improvement system, flow process scope comprises the pre-heating system, fractionating column system of the middle coalite tar before separation column, course of conveying (comprising high-pressure pump booster system) containing the hydrogenating materials of coal-tar pitch component, relates to the aspects such as pipeline, instrument, machinery, static equipment.

The present invention, can be applied to any suitable hydrocarbon hydrogenation process inferior.

Claims

1. a hydrocarbon method of hydrotreating inferior that comprises reaction heat recycling step, is characterized in that comprising following steps:

2. method according to claim 1, is characterized in that:

(2) carry out pre-hydrofining reaction at the first hydrogenation process R1, under hydrogen and the first hydrogenation catalyst R1C existence condition, hydrogenating materials F1M comprise hydrodemetallation (HDM) reaction and or the pre-hydrofining reaction R1R of de-carbon residue reaction obtain the first hydrogenation reaction effluent R1P.

3. method according to claim 1, is characterized in that:

(2) also carry out hydrocracking reaction R19R at the first hydrogenation process R1, the first hydrogenation catalyst R1C also comprises hydrocracking catalyst R19C, and hydrogenating materials F1M carries out being converted into the first hydrogenation reaction effluent R1P after hydrocracking reaction R19R.

4. method according to claim 1, is characterized in that:

(1) at hydrocarbon sepn process FS inferior, before hydrocarbon F1 inferior enters separation column FST, from recycle stream MTHPS-LR and the hydrocarbon F1 Hybrid Heating inferior hydrocarbon F1 inferior of step (3).

5. method according to claim 2, is characterized in that:

6. method according to claim 3, is characterized in that:

7. method according to claim 1, is characterized in that:

(1) at hydrocarbon sepn process FS inferior, hydrocarbon F1 inferior is middle coalite tar, and light fractions F1X is carbolic oil.

8. method according to claim 2, is characterized in that:

9. method according to claim 3, is characterized in that:

10. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(2), at the first hydrogenation process R1, the mode of operation of the bed R1CB of the first hydrogenation catalyst R1C of use is upflowing or downflow system.

11. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(2), at the first hydrogenation process R1, the mode of operation of the bed R1CB of the first hydrogenation catalyst R1C of use, is selected from one or more in following pattern:

1. upflowing suspension bed;

2. upflowing ebullated bed;

4. upflowing bubbling bed;

5. upflowing moving-bed;

6. upflow fixed bed;

7. down-flow fixed bed;

8. downflow system moving-bed;

9. horizontal bed;

10. tilting bed.

12. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(4), at the second hydrogenation process R2, the mode of operation of the bed R2CB of the second hydrogenation catalyst R2C of use is upflowing or downflow system.

13. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(4), at the second hydrogenation process R2, the mode of operation of the bed R2CB of the second hydrogenation catalyst R2C of use, is selected from one or more in following pattern:

1. upflowing ebullated bed;

2. upflowing bubbling bed;

4. upflow fixed bed;

5. upflowing moving-bed;

6. down-flow fixed bed;

7. downflow system moving-bed;

8. horizontal bed;

9. tilting bed.

14. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(3) thermal high sepn process MTHPS between device, recycle stream MTHPS-LR enters step (1) before through removing the solid process LRDS of taking off of solid particulate matter to remove the solid particulate that is greater than critical diameter DN.

15. according to method described in claim 14, it is characterized in that:

(3) thermal high sepn process MTHPS between device, the de-solid process LRDS that removes solid particulate matter of recycle stream MTHPS-LR process, adopts filtration or centrifugation or distillating method, removes that to be greater than critical diameter DN be the solid particulate of 20 microns.

16. according to method described in claim 14, it is characterized in that:

(3) thermal high sepn process MTHPS between device, the de-solid process LRDS that removes solid particulate matter of recycle stream MTHPS-LR process, adopts filter method, removes that to be greater than critical diameter DN be the solid particulate of 10 microns.

17. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(3) thermal high sepn process MTHPS between device, at least a portion logistics MTHPS-LP enters the second hydrogenation process R2 and contacts with the second hydrogenation catalyst R2C; Logistics MTHPS-LP enters step (4) and is passing through the de-solid process LPDS that removes solid particulate matter to remove the solid particulate that is greater than critical diameter DN before.

18. according to method described in claim 17, it is characterized in that:

(3) thermal high sepn process MTHPS between device, logistics MTHPS-LP, through removing the de-solid process LPDS of solid particulate matter, adopts filtration or centrifugation or distillating method, removes that to be greater than critical diameter DN be the solid particulate of 10 microns.

19. according to method described in claim 17, it is characterized in that:

(3) thermal high sepn process MTHPS between device, the de-solid process DS that removes solid particulate matter of recycle stream MTHPS-LR process, adopts distillating method, removes that to be greater than critical diameter DN be the solid particulate of 5 microns.

20. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(3) thermal high sepn process MTHPS between device, at least a portion logistics MTHPS-LP enters before the second hydrogenation process R2 contacts with the second hydrogenation catalyst R2C, first, through removing solid particulate matter and removing the process LPDS of conventional boiling point higher than 530 DEG C of hydrocarbon components, obtain the hydrocarbon ils MTHPS-LPX of de-solid, de-heavy constituent; At least a portion hydrocarbon ils MTHPS-LPX enters the second hydrogenation process R2 and contacts with the second hydrogenation catalyst R2C.

21. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(1) at hydrocarbon sepn process FS inferior, the separation column FST of use operates under reduced pressure.

22. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

Hydrocarbon F1 inferior is selected from one or more in following material:

1. coalite tar or its distillate;

2. coal-tar middle oil or its distillate;

3. coal-tar heavy oil or its distillate;

4. gelatin liquefaction process gained liquefied coal coil or its distillate;

5. shale oil or its distillate;

6. ethylene cracking tar;

7. petroleum base wax oil thermally splitting tar;

23. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(1) hydrocarbon F1 inferior is middle coalite tar, and the easy hydrogenolysis metal concentration taking its contained easy hydrogenolysis metallic compound as benchmark is lower than 50PPm.

24. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(1) hydrocarbon F1 inferior is middle coalite tar, and the easy hydrogenolysis metal concentration taking its contained easy hydrogenolysis metallic compound as benchmark is higher than 100PPm.

25. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(1) hydrocarbon F1 inferior is middle coalite tar, and the easy hydrogenolysis metal concentration taking its contained easy hydrogenolysis metallic compound as benchmark is higher than 200PPm.

26. according to method described in claim 1 or 2 or 4 or 5 or 7 or 8, it is characterized in that:

(2) hydrocarbon F1 inferior is middle coalite tar, carry out pre-hydrofining reaction at the first hydrogenation process R1, under hydrogen and the first hydrogenation catalyst R1C existence condition, the pre-hydrofining reaction R1R that hydrogenating materials F1M comprises hydrodemetallation (HDM) reaction and takes off carbon residue reaction obtains the first hydrogenation reaction effluent R1P; The operational condition of the first hydrogenation process R1 is to improve to greatest extent in the first hydrogenation reaction effluent R1P hydrogen supply hydrocarbon concentration as target.

27. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

28. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

29. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(6) hydrocracking reaction process R3 is set, to separate hydro-upgrading heavy oil R2P0-DO that the hydrogenated oil R2P0 gained of the second hydrogenation reaction effluent is mainly made up of higher than 350 DEG C of hydrocarbon conventional boiling point as raw material, be converted into hydrocracking reaction effluent R3P at hydrocracking reaction process R3.

30. according to method described in claim 22, it is characterized in that:

31. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(6) hydrocracking reaction process R3 is set, to separate hydro-upgrading heavy oil R2P0-DO that the hydrogenated oil R2P0 gained of the second hydrogenation reaction effluent is mainly made up of higher than 350 DEG C of hydrocarbon conventional boiling point as raw material, be converted into hydrocracking reaction effluent R3P at hydrocracking reaction process R3, hydrocracking reaction effluent R3P separates after mixing with the second hydrogenation reaction effluent R2P.

32. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(5) sepn process HPS comprises cold anticyclone sepn process LHPS, at cold anticyclone sepn process LHPS, separate the second hydrogenation reaction effluent R2P and obtain the cold high score gas gas HPV and the cold high score oil LHPL that are mainly made up of hydrogen, cold high score oil LHPL generates oily R2P0 as the second hydrogenation reaction.

33. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(5) sepn process HPS comprises thermal high sepn process THPS and cold anticyclone sepn process LHPS;

At thermal high sepn process THPS, separate the second hydrogenation reaction effluent R2P and obtain hot high score gas gas THPV and hot high score oil THPL;

At cold anticyclone sepn process LHPS, heat of dissociation high score gas gas THPV obtains the cold high score gas gas HPV and the cold high score oil LHPL that are mainly made up of hydrogen, and the second hydrogenation reaction generates oily R2P0 and comprises hot high score oil THPL and cold high score oil LHPL.

34. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

35. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

36. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(3) thermal high sepn process MTHPS between device, hot high score oil MTHP-L is mainly made up of higher than the hydrocarbon of 330 DEG C conventional boiling point.

37. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(3) thermal high sepn process MTHPS between device, hot high score oil MTHP-L is mainly made up of higher than the hydrocarbon of 380 DEG C conventional boiling point.

38. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

39. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(2) the hydrogen rich gas logistics of injection the first hydrogenation process R1 is new hydrogen.

40. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(2), at the first hydrogenation process R1, hydrogen sulfide in gas phase volumetric concentration is 0.1～5%.

41. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(2), at the first hydrogenation process R1, hydrogen sulfide in gas phase volumetric concentration is 0.3～1.0%.

42. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(1) hydrocarbon F1 inferior is middle coalite tar, at hydrocarbon sepn process FS inferior, uses separation column FST in hydrocarbon F1 inferior, to isolate light fractions F1X to obtain the hydrogenating materials F1M of de-light fractions F1X; Light fractions F1X is conventional boiling point lower than the hydrocarbon-fraction of 250 DEG C.

43. according to method described in claim 42, it is characterized in that:

(1) hydrocarbon F1 inferior is middle coalite tar, and at hydrocarbon sepn process FS inferior, light fractions F1X is conventional boiling point lower than the hydrocarbon-fraction of 350 DEG C.

44. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(1) hydrocarbon F1 inferior is middle coalite tar, and at hydrocarbon sepn process FS inferior, light fractions F1X is conventional boiling point lower than the hydrocarbon-fraction of 450 DEG C.

45. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(1) hydrocarbon F1 inferior is middle coalite tar, at hydrocarbon sepn process FS inferior, uses separation column FST in hydrocarbon F1 inferior, to isolate light fractions F1X to obtain the hydrogenating materials F1M of de-light fractions F1X; Light fractions F1X is conventional boiling point lower than the hydrocarbon-fraction of 250 DEG C, and light fractions F1X enters the second hydrogenation process R2 and contacts with the second hydrogenation catalyst R2C.

46. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(1) hydrocarbon F1 inferior is middle coalite tar, at hydrocarbon sepn process FS inferior, uses separation column FST in hydrocarbon F1 inferior, to isolate light fractions F1X to obtain the hydrogenating materials F1M of de-light fractions F1X; Light fractions F1X is conventional boiling point lower than the hydrocarbon-fraction of 350 DEG C, and light fractions F1X enters the second hydrogenation process R2 and contacts with the second hydrogenation catalyst R2C.

47. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(1) hydrocarbon F1 inferior is middle coalite tar, at hydrocarbon sepn process FS inferior, uses separation column FST in hydrocarbon F1 inferior, to isolate light fractions F1X to obtain the hydrogenating materials F1M of de-light fractions F1X; Light fractions F1X is conventional boiling point lower than the hydrocarbon-fraction of 450 DEG C, and light fractions F1X enters the second hydrogenation process R2 and contacts with the second hydrogenation catalyst R2C.

48. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(1) hydrocarbon F1 inferior is middle coalite tar, at hydrocarbon sepn process FS inferior, uses separation column FST in hydrocarbon F1 inferior, to isolate light fractions F1X to obtain the hydrogenating materials F1M of de-light fractions F1X; Light fractions F1X is conventional boiling point lower than the hydrocarbon-fraction of 450 DEG C, and light fractions F1X enters the second hydrogenation process R2 and contacts with the second hydrogenation catalyst R2C; What hydrogenating materials F1M contained is defined as K from the composition weight WA of recycle stream MTHPS-LR with from the ratio of the composition weight WB of hydrocarbon F1 inferior, and K is 0.1～10.

49. according to method described in claim 48, it is characterized in that:

(1) K is 0.5～5.

50. according to method described in claim 48, it is characterized in that:

(1) K can be 1.0～3.0.

51. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

52. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

53. according to method described in claim 52, it is characterized in that:

(3) thermal high sepn process MTHPS between device, liquid MTHPS-L is through de-light constituent step MTHPS-L-FS, adopts distillation separation method to remove conventional boiling point lower than the light constituent of 130 DEG C, obtains de-light constituent oil MTHPS-L-FS-P.

54. according to method described in claim 52, it is characterized in that:

(3) thermal high sepn process MTHPS between device, liquid MTHPS-L is through de-light constituent step MTHPS-L-FS, adopts distillation separation method to remove conventional boiling point lower than the light constituent of 200 DEG C, obtains de-light constituent oil MTHPS-L-FS-P.

55. according to method described in claim 52, it is characterized in that:

(3) thermal high sepn process MTHPS between device, liquid MTHPS-L is through de-light constituent step MTHPS-L-FS, adopts distillation separation method to remove conventional boiling point lower than the light constituent of 250 DEG C, obtains de-light constituent oil MTHPS-L-FS-P.

56. according to method described in claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9, it is characterized in that:

(1) hydrocarbon F1 inferior is middle coalite tar, at hydrocarbon sepn process FS inferior, uses separation column FST in hydrocarbon F1 inferior, to isolate light fractions F1X to obtain the hydrogenating materials F1M of de-light fractions F1X; Leave the temperature T A of the hydrogenating materials F1M of separation column FST, the temperature difference that enters the initial reaction temperature TB of the first hydrogenation process R1 with hydrogenating materials F1M is DT, and DT absolute value is lower than 50 DEG C.

57. according to method described in claim 56, it is characterized in that:

(1) DT absolute value is lower than 30 DEG C.

58. according to method described in claim 56, it is characterized in that:

(1) DT absolute value is lower than 10 DEG C.