CN104941525A - Down-flow type reactor - Google Patents
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- CN104941525A CN104941525A CN201410127427.8A CN201410127427A CN104941525A CN 104941525 A CN104941525 A CN 104941525A CN 201410127427 A CN201410127427 A CN 201410127427A CN 104941525 A CN104941525 A CN 104941525A
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Abstract
The invention relates to a down-flow type reactor which comprises an upper section of gas-liquid separation area provided with a liquid collecting chamber and a lower section of catalytic reaction area provided with one or two or a plurality of catalyst beds, wherein the catalyst bed can be a fixed bed or an online replacement bed, and in the whole material flow direction in the reactor, the upper section of gas-liquid separation area and the lower section of catalytic reaction area are in a series connection relationship. According to the invention, the functions of reaction feeding gas-liquid separator and the down-flow type reactor are combined, the structure of the separator is simplified, the separation efficiency is increased, and the down-flow type reaction is particularly applicable to the combination of a separator for a pre-hydrogenation reaction effluent in a medium and low temperature coal tar deep hydrogenation upgrading process and a deep hydrogenation upgrading reactor for a pre-hydrogenation product. A liquid discharged from the liquid collecting chamber can be used as circulation oil going back to the upstream process, the rest liquid and/or gas can be taken as the pre-hydrogenation product to enter the lower section of catalytic reaction area; or a liquid discharged from the liquid collecting chamber of the separation area and gas discharged from the gas-phase space of the separation area can be respectively subjected to subsequent processing.
Description
Technical field
The present invention relates to a kind of downflow reactor, reaction feed gas-liquid separation zone and downflow system reaction zone are combined, comprise gas-liquid separation zone that liquid collecting room is set and epimere and catalytic reaction zone and the hypomere of 1 or 2 or multiple beds are set; Particularly, the present invention relates to a kind of downflow reactor combined in reaction feed gas-liquid separation zone and downflow system reaction zone for hydrocarbon hydrogenation process; More particularly, the present invention relates to the downflow reactor combined in the gas-liquid separation zone of the reaction feed of the deep hydrogenation upgrading course of reaction be made up of pre-hydrotreating reaction effluent and downflow system deep hydrogenation upgrading reaction zone that a kind of middle coalite tar deep hydrogenation upgrading processes uses.
Background technology
What use below in conjunction with middle coalite tar deep hydrogenation upgrading processes describes the present invention by the downflow reactor that the gas-liquid separation zone of the reaction feed of the deep hydrogenation upgrading course of reaction be made up of pre-hydrotreating reaction effluent and downflow system deep hydrogenation upgrading reaction zone are combined.
Middle coalite tar F1 of the present invention, it can be the coal tar pitch of the distillate such as middle coalite tar of coalite tar or middle coalite tar in full cut, usually grade containing the easy reactive component of pre-hydrogenation such as metal, alkene, phenol, polycyclic aromatic hydrocarbon, gluey pitch shape component, ash, the described easy reactive component of pre-hydrogenation causes catalyst surface coking or deposition of solid usually at reaction conditions.Middle coalite tar F1, usually containing polycyclic aromatic hydrocarbon, condensed-nuclei aromatics, gluey pitch shape component.The aromatic ring number of condensed-nuclei aromatics mentioned herein is greater than 5, and the aromatic ring number of polycyclic aromatic hydrocarbon is 3 ~ 5.
For pre-hydrogenation easy reactive component content high be rich in coalite tar F1 in the poor quality of gluey pitch shape component, its target product is that the deep hydrogenation upgrading processes of diesel oil distillate generally includes the pre-hydrotreating reaction process R1 of coal tar raw material F1 and the deep hydrogenation upgrading course of reaction R2 of pre-hydrotreating reaction effluent R1P, in order to obtain light-end products to greatest extent as gasoline, diesel oil distillate, usually the normal boiling point in oil to comprise heat cracking reaction second heat processing (such as hydrocracking or hydrocracking or coking or catalytic cracking or catalytic pyrolysis etc.) higher than the hydrocarbon component of 350 DEG C is generated to the deep hydrogenation upgrading of gluey pitch shape component.
At the pre-hydrotreating reaction process R1 of middle coalite tar raw material F1, usual use catalyst for pre-hydrogenation R1C, catalyst for pre-hydrogenation R1C can be hydrogenation protecting agent, olefins hydrogenation agent, hydrogenation deoxidation agent, HDM agent, hydrogen desulfurization agent, the single dose of aromatic hydrogenation fractional saturation catalyst etc. or the tandem compound of two agent or multi-agent or mixed loading combination, 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 admixture, olefin saturated, remove metal, remove the organic oxygen of part (such as organic phenol), remove part organic sulfur and to the easy reactive component hydrogenation of other parts (hydrotreated lube base oil of first aromatic ring in such as polycyclic aromatic hydrocarbon), therefore the reaction condition of pre-hydrotreating reaction process R1 comparatively relaxes than the reaction condition of deep hydrogenation upgrading course of reaction R2, usually, the good operating condition of pre-hydrotreating reaction process R1 is: temperature is 170 ~ 390 DEG C, pressure is 4.0 ~ 30.0MPa, catalyst for pre-hydrogenation R1C volume space velocity is 0.05 ~ 5.0hr
-1, hydrogen/feedstock oil volume ratio is 500: 1 ~ 4000: 1, usual chemical pure hydrogen consumption is 0.5 ~ 2.5% (weight of centering coalite tar F1).
At deep hydrogenation upgrading course of reaction R2, under deep hydrogenation modifying catalyst R2C (usually at least using the deep hydrogenation possessing hydrofinishing function exquisite catalyst R21C, sometimes conbined usage to possess the catalyst R22C of hydrocracking function) existence condition, described pre-hydrotreating reaction effluent R1P carries out the reaction of deep hydrogenation upgrading, generates a deep hydrogenation upgrading reaction effluent R2P be made up of hydrogen, impurity component, conventional gas hydrocarbon, conventional liq hydrocarbon; Based on the index request of the upgraded product that deep hydrogenation upgrading course of reaction R2 expects; deep hydrogenation upgrading course of reaction R2 usually must remove most of sulphur, removes most of the nitrogen, significantly reduces density of aromatic hydrocarbon, improves Cetane number, reduce density; usual chemical pure hydrogen consumption is 2.5 ~ 7.5% (weight to coal tar F1), and the reaction temperature of deep hydrogenation upgrading course of reaction R2 is generally high more than 20 DEG C, usually high more than 50 DEG C, higher more than 90 DEG C especially than the reaction temperature of pre-hydrotreating reaction process R1.The operating condition of the exquisite catalyst R21C of deep hydrogenation of deep hydrogenation upgrading course of reaction R2 is generally: temperature is 260 ~ 440 DEG C, pressure is 4.0 ~ 30.0MPa, catalyst for refining R21C volume space velocity is 0.1 ~ 4.0hr
-1, hydrogen/feedstock oil volume ratio is 500: 1 ~ 4000: 1.Deep hydrogenation upgrading course of reaction R2 sometimes conbined usage possesses the catalyst R22C of hydrocracking function, and the operating condition of catalyst R22C is generally: temperature is 300 ~ 440 DEG C, pressure is 4.0 ~ 30.0MPa, catalyst R22 volume space velocity is 0.5 ~ 4.0hr
-1, hydrogen/feedstock oil volume ratio is 500: 1 ~ 4000: 1.
In the pre-hydrogenation process of middle coalite tar, use the association response dilution hydrocarbon being rich in hydrogen supply hydrocarbon can optimize the pre-hydrotreating reaction effect of coal tar heavy fractioning, for this reason, present inventors have proposed with the pre-hydrogenated oil of coal tar for intersolubility good be rich in hydrogen supply hydrocarbon association response dilution hydrocarbon coal tar hydro-conversion method, in patent application listed by table 1, need gas-liquid separator and deep hydrogenation upgrading course of reaction R2 that pre-hydrotreating reaction effluent is set, the partially liq that gas-liquid separator is discharged returns upstream flow process and uses as recycle oil, all the other liquids and gases are as the catalytic reaction zone of pre-hydrotreating reaction effluent penetration depth hydro-upgrading course of reaction R2, now need to arrange recycle oil circulating pump system, for circulating pump provides the liquid trap of recycle oil must be placed in high elevation location, to ensure the requirement of the necessary net positive suction head of force (forcing) pump REFL-PUMP.Or pre-hydrotreating reaction effluent can be separated into liquids and gases and carry out subsequent treatment respectively.
Table 1 needs the gas-liquid separation process of enforcement pre-hydrotreating reaction effluent and partially liq to recycle the coal tar heavy oil hydrogenating conversion process of process
Due to the deep hydrogenation upgrading course of reaction R2 of the pre-hydrotreating reaction effluent of middle coalite tar, usually strong exothermal reaction process is belonged to, reaction temperature rising is larger, in order to reduce the mean temperature of beds, deep hydrogenation upgrading course of reaction R2 uses multiple beds usually, uses quench fluid (cold hydrogen or cold oil) between beds.
In order to simplified apparatus structure and optimizing engineering design, the present invention proposes a kind of downflow reactor, reaction feed gas-liquid separation zone and downflow system reaction zone are combined, comprise gas-liquid separation zone that liquid collecting room is set and epimere and catalytic reaction zone and the hypomere of 1 or 2 or multiple beds are set, when being applied to middle coalite tar deep hydrogenation upgrading processes, the gas-liquid separation zone of the reaction feed of the deep hydrogenation upgrading course of reaction be made up of pre-hydrotreating reaction effluent and downflow system deep hydrogenation upgrading reaction zone are combined, define reactor or the reactor assembly of combination function, similar technology has no report.
Therefore, the first object of the present invention is to propose a kind of downflow reactor, reaction feed gas-liquid separation zone and downflow system reaction zone are combined, comprises gas-liquid separation zone that liquid collecting room is set and epimere and catalytic reaction zone and the hypomere of 1 or 2 or multiple beds are set.
The second object of the present invention is to propose a kind of downflow reactor combined in reaction feed gas-liquid separation zone and downflow system reaction zone for hydrocarbon hydrogenation process.
The third object of the present invention is the downflow reactor combined in the gas-liquid separation zone of the reaction feed of the deep hydrogenation upgrading course of reaction be made up of pre-hydrotreating reaction effluent and downflow system deep hydrogenation upgrading reaction zone proposing a kind of middle coalite tar deep hydrogenation upgrading processes use.
The deep hydrogenation upgrading processes R2 of or olefin(e) centent high or phenol content high or gum level high or asphalt content high or certain easy reactant content high hydrocarbon material F1 high for tenor, the present invention all can apply, and these logistics can be selected from one or more in following materials:
1. coalite tar or its distillate or its hot procedure gained oil product;
2. medium temperature coal tar or its distillate or its hot procedure gained oil product;
3. high temperature coal-tar or its distillate or its hot procedure gained oil product;
4. coal liquefaction 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 thermal cracking tars;
9. petroleum based heavy fuel oils hot procedure gained oil product, hot procedure is coking heavy oil process or heavy oil catalytic cracking process or heavy oil catalytic pyrolysis process;
The hydrocarbon ils of gluey pitch shape component that what 10. other arene content was high be rich in.
Summary of the invention
A kind of downflow reactor of the present invention, it is characterized in that: in the housing RES of a reactor RE, the hypomere REDS that the epimere REUS form reaction feed gas-liquid separation zone and the downflow system catalytic reaction zone of serial operation are formed combines, epimere REUS arranges liquid collecting room CLD, and hypomere REDS arranges 1 or 2 or multiple beds; Main charging REF autoreactor RE top enters reactor RE, and reactor RE is discharged in principal product REP autoreactor RE bottom, and the product liquid REFL from the liquid phase region of liquid collecting room CLD discharges reactor RE.
Feature of the present invention is further: hypomere REDS arranges 2 or multiple beds, and the spatial placement between beds flows into the branch road charging aperture of branch road charging REF2; As required, the space between beds also arranges the branch road feed distributor be connected with branch road charging aperture, and the process acts of branch road feed distributor is: make branch road charging REF2 be evenly distributed on the flow section of prevailing technology medium in reactor; As required, the spatial placement between beds has the hydrid component that branch road charging REF2 is mixed with upper catalyst bed laminar flow effluent, and the process acts of hydrid component is: branch road charging REF2 is mixed with lower catalyst bed laminar flow effluent.
Feature of the present invention is further: as required, the entrance of the beds that hypomere REDS is arranged, be provided with bed feed distributor, the process acts of bed feed distributor is: in reactor prevailing technology medium flow section on bed charging is evenly distributed on bottom bed.
Hypomere REDS is provided with beds, and beds can be selected from one or more in following manner:
1. beds is fixed bed.
2. beds is the online moving bed of downflow system, the online moving bed of described downflow system, in bed, processing medium flows downward, and draws off the active catalyst reduced in a continuous manner bottom bed, fills into fresh catalyst maintain bed catalyst reserve from bed top.
3. beds is downflow system online batch (-type) displacement bed, described downflow system online batch (-type) displacement bed, in bed, processing medium flows downward, and draws off the active catalyst reduced in an intermittent fashion, fills into fresh catalyst in an intermittent fashion and maintains bed catalyst reserve.
A kind of downflow reactor of the present invention, the segmentation dividing plate in isolation hypomere REDS and epimere REUS space is set in reactor shell RES, the product arranging the up flow type catalytic reaction zone of conveying hypomere REDS enters the passage DP of the gas-liquid separation zone of epimere REUS, has following 5 kinds of forms available:
1. the first form is, passage DP is arranged in outside the housing of reactor RE, and now, the epimere REUS space in reactor shell RES and hypomere REDS space isolate by segmentation dividing plate.
2. the second form is, passage DP is arranged in the housing of reactor RE, and passage DP is through segmentation dividing plate.
3. the third form is, between liquid collecting room CLD sidewall and or fluid downlink spatial between liquid collecting room CLD sidewall and reactor shell RES, carry the logistics of the gas-liquid separation zone of epimere REUS to enter the passage DP of the downflow system catalytic reaction zone of hypomere REDS exactly.
4. the 4th kind of form is, the fluid downlink spatial between liquid collecting room CLD sidewall, carries the logistics of the gas-liquid separation zone of epimere REUS to enter the passage DP of the downflow system catalytic reaction zone of hypomere REDS exactly.
5. the 5th kind of form is, the fluid downlink spatial between liquid collecting room CLD sidewall and reactor shell RES, carries the logistics of the gas-liquid separation zone of epimere REUS to enter the passage DP of the downflow system catalytic reaction zone of hypomere REDS exactly.
A kind of downflow reactor of the present invention, main charging REF can for the logistics containing hydrocarbon ils.
A kind of downflow reactor of the present invention, main charging REF is the hydro-upgrading process that high aroamtic hydrocarbon raw material HDS is carried out in downflow system catalytic reaction zone that high aroamtic hydrocarbon raw material HDS, hypomere REDS are arranged;
High aroamtic hydrocarbon raw material HDS is selected from one or more in following materials:
1. coalite tar or its distillate;
2. medium temperature coal tar or its distillate;
3. high temperature coal-tar or its distillate;
4. coal liquefaction gained liquefied coal coil or its distillate;
5. shale oil or its distillate;
6. ethylene cracking tar;
7. petroleum base wax oil thermal cracking tars;
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;
9. petroleum based heavy fuel oils 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.
A kind of downflow reactor of the present invention, when carrying out the hydro-upgrading process of high aroamtic hydrocarbon raw material HDS, is characterized in that:
The operating condition of the up flow type catalytic reaction zone that hypomere REDS is arranged is: temperature is 170 ~ 480 DEG C, pressure is 4.0 ~ 30.0MPa.
A kind of downflow reactor of the present invention, discharges the product liquid REFL of reactor RE from the liquid phase region CLD of liquid collecting room, the whereabouts after force (forcing) pump boosting can be selected from one or more in following manner:
1. discharge the product liquid REFL of reactor RE from the liquid phase region CLD of liquid collecting room, after force (forcing) pump boosting, enter the reactor Inner eycle producing main charging REF use.
2. discharge the product liquid REFL of reactor RE from the liquid phase region CLD of liquid collecting room, after force (forcing) pump boosting, enter the reactor Inner eycle producing branch road charging REF2 use.
A kind of downflow reactor of the present invention, as required, epimere REUS arranges liquid collecting room CLD, by arranging the upper space UNICOM of the beds that valvular pipeline and hypomere REDS are arranged, in the reactor emergency shutdown stage, the product liquid REFL discharging reactor RE with the liquid phase region CLD from liquid collecting room rinses beds, manufactures the flowing of downflow system fluid in beds.
A kind of downflow reactor of the present invention, as required, epimere REUS, part or all of gaseous product discharges reactor RE as reaction feed flashed vapour REFV autoreactor RE top, enters reactor REFV-R.
A kind of downflow reactor of the present invention, as required, epimere REUS, part or all of product liquid REFL discharge reactor RE from the liquid phase region CLD of liquid collecting room, enter reactor REFL-R.
A kind of downflow reactor of the present invention, as required, epimere REUS, portion gas product discharges reactor RE as charging flashed vapour REFV autoreactor RE top, enters cooling procedure REFV-CS.
A kind of downflow reactor of the present invention, as required, epimere REUS, product liquid REFL discharges reactor RE from the liquid phase region CLD of liquid collecting room at least partially, enters cooling procedure REFL-CS.
Accompanying drawing explanation
Accompanying drawing is the basic function structural representation of a kind of downflow reactor RE of the present invention.As shown in drawings, in the housing RES of a reactor RE, the hypomere REDS that the epimere REUS form reaction feed gas-liquid separation zone and the downflow system catalytic reaction zone of serial operation are formed combines, the housing RES of reactor RE comprises epimere REUS and hypomere REDS, and main charging REF autoreactor RE top enters reactor RE; Epimere REUS arranges liquid collecting room CLD, and the product liquid REFL from the liquid phase region CLD of liquid collecting room discharges reactor RE, and reactor RE is discharged on possible gaseous product REFV autoreactor RE top; The segmentation dividing plate SB of isolation epimere REUS and hypomere REDS is set in reactor shell RES, the logistics arranging the gas-liquid separation zone of conveying epimere REUS enters the passage DP of the downflow system catalytic reaction zone of hypomere REDS, passage DP is arranged in the housing of reactor RE, and passage DP is through segmentation dividing plate; The hypomere REDS that downflow system catalytic reaction zone is formed comprises three beds, is provided with the distributor of branch road branch road charging REF21, has the distributor of branch road branch road charging REF22 between 2,3 beds between 1,2 beds; Reactor RE is discharged on principal product REP autoreactor RE top.
Detailed description of the invention
A kind of downflow reactor of the present invention is a kind of downflow reactor that commercial plant uses, and the macroscopic view flowing dominant direction wherein navigating within the processing medium of catalyst bed interlayer is from top to bottom; Reactor also can be called reaction tower.
Downflow reactor of the present invention, the basic element of character has usually:
1. reactor shell RES;
2. the opening (or being called adapter) in reactor shell;
3. the beds in piece housing under reactor is arranged in;
4. the segmentation dividing plate SB in epimere REUS space and hypomere REDS space is isolated;
5. the logistics arranging the gas-liquid separation zone of conveying epimere REUS enters the passage DP of the downflow system catalytic reaction zone of hypomere REDS, and passage DP can not pass segmentation dividing plate through segmentation dividing plate or by the external connecting pipe of reactor enclosure;
6. the liquid collecting room CLD in reactor upper casing is arranged in;
7. the measuring instrument may installed: the temperature-measuring part of detecting catalyst bed temperature is as thermocouple, measure the Pressure gauge of reactor assembly ad-hoc location pressure, liquid level instrument such as glass plate, floating drum, two flange difference gauge, guided wave radar, the ray level-sensing device of measuring set liquid chamber CLD liquid level;
8. feed distributor (or distributor);
9. the blender between bed;
10. rectification part is exported, as collector, vortex-proof device, demister (demister).
Downflow reactor of the present invention, accessory is external insulation material, support member (skirt or journal stirrup), basis, ladder, operating platform and the fire-fighting accessory that may exist be as steam smothering ring.According to the construction ground condition such as geology, meteorology, the conditions such as bonding apparatus weight, height, downflow reactor of the present invention needs to drive piles with the sinking speed controlling downflow reactor RE basis under its basis as required.
Downflow reactor RE of the present invention, in the housing of a reactor RE, the hypomere REDS that the epimere REUS form reaction feed gas-liquid separation zone and the downflow system catalytic reaction zone of serial operation are formed combines, the segmentation dividing plate SB in isolation hypomere REDS and epimere REUS space is set in reactor, the logistics arranging the gas-liquid separation zone of conveying epimere REUS enters the passage DP of the downflow system catalytic reaction zone of hypomere REDS, has following 2 kinds of forms available:
1. the first form is that passage DP is arranged in the housing of reactor RE, and now, passage DP is through segmentation dividing plate SB;
2. the second form is that passage DP is arranged in outside the housing of reactor RE, and now, the shell intracorporeal space of reactor RE is isolated into hypomere REDS and epimere REUS space by segmentation dividing plate.
Downflow reactor RE of the present invention, hypomere REDS arrange 1 or 2 or multiple beds, and the working method of beds has following several form available:
1. upflow fixed bed;
2. downflow system online batch (-type) displacement bed, in bed, processing medium flows downward, and draws off the active catalyst reduced in an intermittent fashion, fills into fresh catalyst in an intermittent fashion and maintains bed catalyst reserve;
3. downflow system moving bed, in bed, processing medium flows downward, and draws off the active catalyst reduced in a continuous manner bottom bed, fills into fresh catalyst maintain bed catalyst reserve from bed top.
Downflow reactor RE of the present invention, the product liquid REFL at least partially from the liquid phase region CLD of liquid collecting room discharges reactor RE, and the mode that product liquid REFL discharges reactor RE has following several form available:
1. form A arranges opening REFL-PX on the wall of the reactor of the close base plate (being generally segmentation dividing plate) of the liquid phase region CLD of the liquid collecting room of downflow reactor RE epimere, opening REFL-PX can be 1 each or 2 or multiple, is arranged symmetrically with as far as possible between opening REFL-PX; The advantage of this form is that structure is simple, one of shortcoming is the liquid storage efficiency that the liquid level of liquid collecting room exists that certain gradient reduces liquid collecting room, two of shortcoming is the liquid storage efficiency that the liquid storage space of the liquid collecting room be positioned under the low edge of opening REFL-PX becomes that flow dead reduces liquid collecting room, and three of shortcoming is that in the liquid storage spatial flow dead band meeting deposition reaction product of liquid collecting room, entrained solid particle also may form particle concentration fluctuation to the charging of downstream units;
2. form B catheter REFL-IP in bottom (preferably the bottom at the liquid collecting room center) erector of the liquid collecting room of downflow reactor RE epimere, in device, catheter REFL-IP is connected with the opening REFL-P on the wall of the reactor of the close segmentation dividing plate of hypomere product liquid REFL is discharged reactor RE; Compared with form A, the hydraulic gradient that one of advantage is reduction of liquid collecting room improves the liquid storage efficiency of liquid collecting room, and two of advantage is the liquid storage efficiency that the flow dead in the liquid storage space having eliminated liquid collecting room improves liquid collecting room, and shortcoming is that structure is slightly complicated;
3. form A, for major diameter downflow reactor RE, in the bottom (preferably the bottom at liquid collecting room center) of the liquid collecting room of downflow reactor RE epimere, catheter REFL-IPX in 2 or multiple device is installed, in device catheter REFL-IPX converge in device after house steward be connected with the opening REFL-P on the wall of the reactor of the close segmentation dividing plate of hypomere product liquid REFL discharged reactor RE; Compared with form B, the hydraulic gradient that advantage is reduction of liquid collecting room improves the liquid storage efficiency of liquid collecting room, and shortcoming is that structure is slightly complicated;
4. form D, for downflow reactor RE particularly for major diameter downflow reactor RE, in the bottom (preferably the bottom at liquid collecting room center) of the liquid collecting room of downflow reactor RE epimere, catheter REFL-IPX in 2 or the multiple devices be arranged symmetrically with as far as possible is installed, in every prop, catheter REFL-IPX is connected with the opening REFL-PX on the wall of the reactor of the close segmentation dividing plate of hypomere and product liquid REFL is discharged reactor RE, each bypass ducts outside the reactor be arranged symmetrically with as far as possible and house steward UNICOM; Compared with form A, advantage is the house steward eliminated in reactor thus the internal installation work simplified in reactor, the opening REFL-PX unstability impact that fluids within pipes flowing causes reactor that is connected can be offset as far as possible, and shortcoming is the increase in reactor wall opening number;
5. form E, for the downflow reactor RE of single beds particularly for the major diameter downflow reactor RE of single beds, in the bottom (preferably the bottom at liquid collecting room center) of the liquid collecting room of downflow reactor RE epimere, catheter REFL-IPX in 1 device being arranged in reactor center position is installed, directly be communicated with the circulating pump be arranged in reactor after in device, catheter REFL-IPX is passed down through beds, the product liquid REFL of autoreactor RE epimere enters the lower space interior formation liquid-circulating of the lower section catalyst bed of reactor RE in the future, certainly, catheter REFL-IPX in 2 or the multiple devices be arranged symmetrically with as far as possible can also be arranged as required, this form, advantage is the tracing thermal-insulating problem solving catheter, shortens circulating path length, reduces the unstability impact that exterior liquid body product REFL causes reactor RE, shortcoming is that circulating pump is placed in reactor, and complex structure, adds capital cost of reactor, reduces security, and circulating pump for subsequent use in addition is more difficult to arrange,
6. form D, for the downflow reactor RE of single beds particularly for the major diameter downflow reactor RE of single beds, in the bottom (preferably the bottom at liquid collecting room center) of the liquid collecting room of downflow reactor RE epimere, catheter REFL-IPX in 1 device being arranged in reactor center position is installed, is connected with the opening REFL-PX on the close reactor bottom wall of hypomere after catheter REFL-IPX is passed down through beds in device and product liquid REFL is discharged reactor RE; Certainly, catheter REFL-IPX in 2 or the multiple devices be arranged symmetrically with as far as possible can also be arranged as required, each bypass ducts outside the reactor be arranged symmetrically with as far as possible and house steward UNICOM; This form, advantage is the tracing thermal-insulating problem solving catheter, reduces the unstability impact that exterior liquid body product REFL causes reactor RE; Shortcoming is that in device, catheter REFL-IPX is passed down through beds, complex structure.
The first usual way that product liquid REFL discharges reactor RE is: form D, for downflow reactor RE particularly for major diameter downflow reactor RE, in the bottom (preferably the bottom at liquid collecting room center) of the liquid collecting room of downflow reactor RE epimere, catheter REFL-IPX in 2 devices be arranged symmetrically with is installed, in every prop, catheter REFL-IPX is connected with the opening REFL-PX on the wall of the reactor of the close segmentation dividing plate of hypomere product liquid REFL is discharged reactor RE, 2 bypass ducts outside the reactor be arranged symmetrically with as far as possible and house steward UNICOM.
The second usual way that product liquid REFL discharges reactor RE is: form D, for the downflow reactor RE of single beds particularly for the major diameter downflow reactor RE of single beds, in the bottom (preferably the bottom at liquid collecting room center) of the liquid collecting room of downflow reactor RE epimere, catheter REFL-IPX in 1 device being arranged in reactor center position is installed, be connected with the opening REFL-PX on the close reactor bottom wall of hypomere after catheter REFL-IPX is passed down through beds in device and product liquid REFL is discharged reactor RE.
For the operating mode containing the easy foaming component such as gluey pitch shape component that surface tension is large, viscosity is large in product, in order to ensure degasifying effect, under the product liquid REFL installed in the liquid collecting room of downflow reactor RE epimere discharges the duty of the pipeline of reactor RE, velocity of medium generally gets lower value, is such as usually less than 1 meter per second, is generally less than 0.5 meter per second, is less than 0.2 meter per second especially.
A kind of downflow reactor of the present invention, when reaction feed gas-liquid separation zone produces gas products, the mode that reactor RE is discharged on gaseous product REFV autoreactor RE top is generally: any suitable location more than the liquid level of the liquid phase region CLD of the liquid collecting room of downflow reactor RE epimere all can arrange gaseous product REFV outlet, common scheme arranges opening REFV-PX at the top sidewall of reactor, opening REFV-PX can be 1 each or 2 or multiple, be arranged symmetrically with as far as possible between multiple opening REFV-PX, opening REFV-PX is generally 1.
A kind of downflow reactor of the present invention, reactor RE is discharged in principal product REP autoreactor RE bottom, the mode that principal product REP discharges reactor RE is generally: any suitable location of the bottom of the hypomere REDS formed in downflow system catalytic reaction zone all can arrange principal product REP outlet, common scheme arranges opening REP-PX at the lower curtate center of reactor, opening REP-PX can be 1 each or 2 or multiple, be arranged symmetrically with as far as possible between multiple opening REP-PX, opening REP-PX is generally 1.
Downflow reactor RE of the present invention, product liquid REFL at least partially from the liquid phase region CLD of liquid collecting room discharges reactor RE, when product liquid REFL enters force (forcing) pump REFL-PUMP, the absolute altitude of the liquid collecting room CLD of epimere REUS is sufficiently high, to ensure the requirement of the necessary net positive suction head of force (forcing) pump REFL-PUMP.
Downflow reactor RE of the present invention, be applicable to hydrocarbon hydrogenation process, be specially adapted to the hydrocarbon hydro-upgrading process that the reaction temperature not too high thus coking reaction of easy coking hydrocarbon ils is more weak, or be specially adapted to the hydro-upgrading process of the easy coking hydrocarbon ils containing less ash content.Downflow reactor RE of the present invention, is applicable to coal tar hydrogenation modification process, is specially adapted to the pre-hydrogenation upgrading processes of middle coalite tar.Downflow reactor RE of the present invention, can combinationally use with upstream reactor or downstream reactor, forms the reaction system of various ways.
Below describe characteristic of the present invention in detail.
A kind of downflow reactor of the present invention, it is characterized in that: in the housing RES of a reactor RE, the hypomere REDS that the epimere REUS form reaction feed gas-liquid separation zone and the downflow system catalytic reaction zone of serial operation are formed combines, epimere REUS arranges liquid collecting room CLD, and hypomere REDS arranges 1 or 2 or multiple beds; Main charging REF autoreactor RE top enters reactor RE, and reactor RE is discharged in principal product REP autoreactor RE bottom, and the product liquid REFL from the liquid phase region of liquid collecting room CLD discharges reactor RE.
Feature of the present invention is further: hypomere REDS arranges 2 or multiple beds, and the spatial placement between beds flows into the branch road charging aperture of branch road charging REF2; As required, the space between beds also arranges the branch road feed distributor be connected with branch road charging aperture, and the process acts of branch road feed distributor is: make branch road charging REF2 be evenly distributed on the flow section of prevailing technology medium in reactor; As required, the spatial placement between beds has the hydrid component that branch road charging REF2 is mixed with upper catalyst bed laminar flow effluent, and the process acts of hydrid component is: branch road charging REF2 is mixed with lower catalyst bed laminar flow effluent.
Feature of the present invention is further: as required, the entrance of the beds that hypomere REDS is arranged, be provided with bed feed distributor, the process acts of bed feed distributor is: in reactor prevailing technology medium flow section on bed charging is evenly distributed on bottom bed.
Hypomere REDS is provided with beds, and beds can be selected from one or more in following manner:
1. beds is fixed bed.
2. beds is the online moving bed of downflow system, the online moving bed of described downflow system, in bed, processing medium flows downward, and draws off the active catalyst reduced in a continuous manner bottom bed, fills into fresh catalyst maintain bed catalyst reserve from bed top.
3. beds is downflow system online batch (-type) displacement bed, described downflow system online batch (-type) displacement bed, in bed, processing medium flows downward, and draws off the active catalyst reduced in an intermittent fashion, fills into fresh catalyst in an intermittent fashion and maintains bed catalyst reserve.
A kind of downflow reactor of the present invention, the segmentation dividing plate in isolation hypomere REDS and epimere REUS space is set in reactor shell RES, the product arranging the up flow type catalytic reaction zone of conveying hypomere REDS enters the passage DP of the gas-liquid separation zone of epimere REUS, has following 5 kinds of forms available:
1. the first form is, passage DP is arranged in outside the housing of reactor RE, and now, the epimere REUS space in reactor shell RES and hypomere REDS space isolate by segmentation dividing plate.
2. the second form is, passage DP is arranged in the housing of reactor RE, and passage DP is through segmentation dividing plate.
3. the third form is, between liquid collecting room CLD sidewall and or fluid downlink spatial between liquid collecting room CLD sidewall and reactor shell RES, carry the logistics of the gas-liquid separation zone of epimere REUS to enter the passage DP of the downflow system catalytic reaction zone of hypomere REDS exactly.
4. the 4th kind of form is, the fluid downlink spatial between liquid collecting room CLD sidewall, carries the logistics of the gas-liquid separation zone of epimere REUS to enter the passage DP of the downflow system catalytic reaction zone of hypomere REDS exactly.
5. the 5th kind of form is, the fluid downlink spatial between liquid collecting room CLD sidewall and reactor shell RES, carries the logistics of the gas-liquid separation zone of epimere REUS to enter the passage DP of the downflow system catalytic reaction zone of hypomere REDS exactly.
A kind of downflow reactor of the present invention, main charging REF can for the logistics containing hydrocarbon ils.
A kind of downflow reactor of the present invention, main charging REF is the hydro-upgrading process that high aroamtic hydrocarbon raw material HDS is carried out in downflow system catalytic reaction zone that high aroamtic hydrocarbon raw material HDS, hypomere REDS are arranged;
High aroamtic hydrocarbon raw material HDS is selected from one or more in following materials:
1. coalite tar or its distillate;
2. medium temperature coal tar or its distillate;
3. high temperature coal-tar or its distillate;
4. coal liquefaction gained liquefied coal coil or its distillate;
5. shale oil or its distillate;
6. ethylene cracking tar;
7. petroleum base wax oil thermal cracking tars;
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;
9. petroleum based heavy fuel oils 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.
A kind of downflow reactor of the present invention, when carrying out the hydro-upgrading process of high aroamtic hydrocarbon raw material HDS, is characterized in that:
The operating condition of the up flow type catalytic reaction zone that hypomere REDS is arranged is: temperature is 170 ~ 480 DEG C, pressure is 4.0 ~ 30.0MPa.
A kind of downflow reactor of the present invention, discharges the product liquid REFL of reactor RE from the liquid phase region CLD of liquid collecting room, the whereabouts after force (forcing) pump boosting can be selected from one or more in following manner:
1. discharge the product liquid REFL of reactor RE from the liquid phase region CLD of liquid collecting room, after force (forcing) pump boosting, enter the reactor Inner eycle producing main charging REF use.
2. discharge the product liquid REFL of reactor RE from the liquid phase region CLD of liquid collecting room, after force (forcing) pump boosting, enter the reactor Inner eycle producing branch road charging REF2 use.
A kind of downflow reactor of the present invention, as required, epimere REUS arranges liquid collecting room CLD, by arranging the upper space UNICOM of the beds that valvular pipeline and hypomere REDS are arranged, in the reactor emergency shutdown stage, the product liquid REFL discharging reactor RE with the liquid phase region CLD from liquid collecting room rinses beds, manufactures the flowing of downflow system fluid in beds.
A kind of downflow reactor of the present invention, as required, epimere REUS, part or all of gaseous product discharges reactor RE as reaction feed flashed vapour REFV autoreactor RE top, enters reactor REFV-R.
A kind of downflow reactor of the present invention, as required, epimere REUS, part or all of product liquid REFL discharge reactor RE from the liquid phase region CLD of liquid collecting room, enter reactor REFL-R.
A kind of downflow reactor of the present invention, as required, epimere REUS, portion gas product discharges reactor RE as charging flashed vapour REFV autoreactor RE top, enters cooling procedure REFV-CS.
A kind of downflow reactor of the present invention, as required, epimere REUS, product liquid REFL discharges reactor RE from the liquid phase region CLD of liquid collecting room at least partially, enters cooling procedure REFL-CS.
The combination function reactor of the present invention's " top liquid collecting room+downflow system conversion zone ", major advantage is as follows:
1. from mechanical discipline angle, there is following advantage: functions of the equipments are compact, enormously simplify hot high-pressure separator structure, at least save two end sockets, save a large amount of alloy steel material;
2. from technology major angle, there is following advantage: built-in intersegmental passage DP, the distributor of namely can also be simultaneously the distributor of the lower apoblema of epimere REUS gas-liquid separation zone be hypomere REDS catalytic reaction zone raw material, there is multiple action, because operating efficiency is high, reduce idle space, improve space availability ratio;
3. from tube profession angle, following advantage is had: decrease the material conveying pipe between reactor and separator;
4. from Civil Specialities angle, have following advantage: the nearly all building, the structural acessory that save a platform independent separator, these annexes comprise skirt, operating platform, basis;
5. from general layout angle, following advantage is had: save floor space.
Embodiment
Medium temperature coal tar character is in table 2, be separated into primarily of normal boiling point lower than 480 DEG C hydrocarbon composition weight yield be 82% light fraction and primarily of normal boiling point higher than 480 DEG C hydrocarbon composition weight yield be the coal tar pitch of 18%, light fraction carries out deep hydrogenation upgrading separately, and coal tar pitch is used as high aroamtic hydrocarbon raw material HDS.
Hydrogen supply hydrocarbon stream SHS is selected from the pre-hydrogenated oil R1P of pre-hydrotreating reaction process R1 gained, quantity is 5 times of high aroamtic hydrocarbon raw material HDS, obtained by the gas-liquid separation process of pre-hydrotreating reaction effluent R1P, now, the logistics of hydrogen supply hydrocarbon precursor is exactly high aroamtic hydrocarbon raw material HDS self; The part by weight of hydrogen supply hydrocarbon component S H is about 25 % by weight, in logistics SHS gum level lower than 5 % by weight, carbon residue is lower than 1.5%.
The step of processes scheme is as follows:
(1), in pre-hydrotreating reaction R1R process, technic index is:
1. in the charging of catalyst for pre-hydrogenation bed, ratio KX=SH-W/HD-W, the KX=1.30 of the weight flow SH-W from the hydrogen supply hydrocarbon component S H of hydrogen supply hydrocarbon stream SHS and the weight flow HD-W of the gluey pitch shape component HD from high aroamtic hydrocarbon raw material HDS ~ 1.35;
In the liquid phase of catalyst for pre-hydrogenation bed, ratio KY=SH-CLW/HD-CLW, the KY of the weight flow SH-CLW from the hydrogen supply hydrocarbon component S H of hydrogen supply hydrocarbon stream SHS and the weight flow HD-CLW of the gluey pitch shape component HD from high aroamtic hydrocarbon raw material HDS >=1.10;
2. hydrogen to oil volume ratio is 200;
3. the Phase velocity map of high aroamtic hydrocarbon raw material HDS is: total body fluid one after another HDS-KL >=0.77, i.e. overall rate of gasification HDS-KV≤0.23;
The Phase velocity map of the gluey pitch shape component HD in high aroamtic hydrocarbon raw material HDS is: total body fluid one after another HD-KL >=0.77, i.e. overall rate of gasification HD-KV≤0.23;
4. the selection index of reaction heat, the reaction heat HDS-Q based on high aroamtic hydrocarbon raw material HDS is KZ, KZ=HDS-Q/SHS-Q, KZ >=2.1 with the ratio based on the reaction heat SHS-Q of hydrogen supply hydrocarbon stream SHS;
The working method of pre-hydrogenator R1-SB is up flow type slight expanded-bed reactor; Charging autoreactor R1-SB bottom enters, and reaction effluent R1P autoreactor R1-SB top is flowed out; Temperature be 300 ~ 320 DEG C, pressure is 15.0 ~ 17.0MPa, catalyst for pre-hydrogenation R1-CAT volume space velocity is 0.6 ~ 0.7hr
-1reaction condition under, complete pre-hydrotreating reaction and obtain pre-hydrotreating reaction effluent R1P; Described up flow type slight expanded-bed, bed expansion ratio KBED is less than 1.03;
The hydrogen rich gas logistics injecting pre-hydrogenator is preferably new hydrogen logistics, supplements time not enough with recycle hydrogen;
In pre-hydrogenator, hydrogen sulfide in gas phase volumetric concentration controls is 0.3 ~ 0.5%;
(2) Cetane number of the full cut diesel oil in deep hydrogenation upgrading reaction effluent R2P is higher than 32.
(3) at separate section HPS, be separated deep hydrogenation upgrading reaction effluent R2P and obtain generating oily R2P0 primarily of the hydrogen rich gas gas HPV of hydrogen composition and deep hydrogenation upgrading, hydrogen rich gas gas HPV returns hydrogenation process and recycles at least partially.
(4) hydrocracking reaction process R3 is set, the hydro-upgrading heavy oil R2P0-D0 formed higher than 350 DEG C of hydrocarbon primarily of normal boiling point with the hydrogenated oil R2P0 gained being separated deep hydrogenation upgrading reaction effluent R2P is for raw material, be converted into hydrocracking reaction effluent R3P at hydrocracking reaction process R3, be separated after hydrocracking reaction effluent R3P mixes with hydrogenation reaction effluent R2P.
Table 2, table 3 are medium temperature coal tar character.
Table 4 is composition and the physico-chemical property of the catalyst that the pre-hydrotreating reaction process R1 of high aroamtic hydrocarbon raw material HDS uses.
Table 5 is composition and the physico-chemical property of the catalyst that the deep hydrogenation upgrading course of reaction R2 of high aroamtic hydrocarbon raw material HDS uses.
Table 6 is composition and the physico-chemical property of hydrocracking reaction part catalyst.
Table 7 is pre-hydrotreating reaction process R1, deep hydrogenation upgrading course of reaction R2, the operating condition of hydrocracking reaction process R3 and product property.
The pre-hydrogenator R1-SB of this device adopts up-flow reactor, and the pre-hydrotreating reaction effluent RIP series connection that pre-hydrogenator R1-SB discharges enters and adopts the first deep hydrogenation reforming reactor of structure of the present invention and a conventional downflow trickle bed bioreactor.
First deep hydrogenation reforming reactor, adopt the knockdown downflow reactor of the present invention, in a reactor shell RES, the hypomere REDS that the epimere REUS form reaction feed gas-liquid separation zone and the downflow system catalytic reaction zone of serial operation are formed combines, epimere REUS arranges liquid collecting room CLD, hypomere REDS arranges 4 beds, and the order flow through according to raw material is respectively guard catalyst, Hydrodemetalation catalyst, removal of ccr by hydrotreating catalyst, Hydrobon catalyst; Main charging REF autoreactor RE top enters reactor RE, reactor RE is discharged in principal product REP autoreactor RE bottom, after being pressurizeed by circulating pump after the product liquid REFL discharge reactor RE of the liquid phase region CLD of liquid collecting room, return pre-hydrogenator R1-SB charging aperture.
Design parameter is as follows:
1. passage DP medium flow velocity range of choice is 0.5 ~ 8 meter per second, is preferably 1 ~ 3 meter per second;
2. the time of staying range of choice of the product liquid REFL of the liquid phase region CLD of liquid collecting room is 10 ~ 100 minutes, is preferably 30 ~ 40 minutes;
3. pump entry pipeline internal medium flow velocity is 0.2 ~ 1.0 meter per second, is preferably 0.4 ~ 1 meter per second.
Table 2 coal tar character
| Project | Numerical value |
| Bottle density (20 DEG C), kg.m -3 | 1.0658 |
| Boiling range, DEG C (simulation distil) | |
| IBP/10％/30％/50％ | 164/237/314/374 |
| 70％/80％/85％/89.2 | 435/486/542/750 |
| Sulphur, μ g.g -1 | 1800 |
| Nitrogen, μ g.g -1 | 6101 |
| C，％ | 81.36 |
| H，％ | 8.21 |
| Condensation point, DEG C | 30 |
| Carbon residue, % | 9.77 |
| Moisture, % | 4.1 |
| Sediment, % | 0.48 |
| Flash-point (remaining silent), DEG C | 126 |
| Heavy metal, μ g.g -1 | |
| Fe/Na/Ni/Mg | 108.70/5.74/1.39/56.32 |
| Ca/V/K/Pb | 362.4/0.17/16.25/11.43 |
| Co/Cu/Mn/Zn/Mo | 0.77/0.21/4.24/6.84/0.02 |
| Mass spectrum forms, % | |
| Colloid | 33.5 |
| Alkane | 11.5 |
| Cycloalkane | 5.2 |
| Monocycle/dicyclo/tri-ring/Fourth Ring | 2.7/0.7/1.3/0.5 |
| Aromatic hydrocarbons | 49.8 |
| Monocycle/dicyclo/tri-ring/Fourth Ring/five rings | 13.8/16.4/8.3/5.0/0.6 |
| Total thiophene/do not identify | 4.4/1.3 |
Table 3 coal tar true boiling-point (TBP) cutting result
| Component, % | Numerical value |
| Water | 3.07 |
| ＜170℃ | 4.30 |
| 170℃～210℃ | 1.48 |
| 210℃～230℃ | 4.81 |
| 230℃～300℃ | 14.93 |
| 300℃～500℃ | 59.28 |
| ＞500℃ | 12.13 |
| ∑ | 96.93 |
The composition of the catalyst of the pre-hydrotreating reaction process R1 use of the high aroamtic hydrocarbon raw material HDS of table 4 and physico-chemical property
The composition of the catalyst of the deep hydrogenation upgrading course of reaction R2 use of the high aroamtic hydrocarbon raw material HDS of table 5 and physico-chemical property
The composition of table 6 hydrocracking reaction part catalyst and physico-chemical property
The operating condition of table 7 pre-hydrotreating reaction process R1, deep hydrogenation upgrading course of reaction R2, hydrocracking reaction process R3 and product property table
| Sequence number | Project | Numerical value |
| 1 | Pre-hydrotreating reaction process R1 | |
| 1.1 | Reaction pressure, MPa | 15.0～17.0 |
| 1.2 | Reaction temperature, DEG C protective agent+metal remover+de-carbon residue agent+desulfurizing agent | 295～340 |
| 2 | Deep hydrogenation upgrading course of reaction R2 | |
| 2.1 | Hydrofinishing agent E volume space velocity, h -1 | 0.25～0.30 |
| 2.2 | Reactor inlet hydrogen-oil ratio, m 3n/m 3 | 1700～1800 |
| 2.3 | The nitrogen content of the naphtha cut in deep hydrogenation upgrading reaction effluent R2P, | ≯3.0 |
| 2.4 | The Cetane number of the diesel oil distillate in deep hydrogenation upgrading reaction effluent R2P | ≮35.0 |
| 2.5 | Tail oil boiling range in deep hydrogenation upgrading reaction effluent R2P, DEG C | 350～545 |
| 3 | Hydrocracking reaction process R3 | |
| 3.1 | Reaction pressure, MPa | 15.0～17.0 |
| 3.2 | Reaction temperature, DEG C | 380～420 |
| 3.3 | Hydrocracking catalyst volume space velocity, h -1 | 0.42～0.50 |
| 3.4 | Reactor inlet hydrogen-oil ratio, m 3n/m 3 | 1500 |
| 3.5 | Hydrocracking diesel cetane-number | ≮48 |
Claims (26)
1. a downflow reactor, it is characterized in that: in the housing RES of a reactor RE, the hypomere REDS that the epimere REUS form reaction feed gas-liquid separation zone and the downflow system catalytic reaction zone of serial operation are formed combines, epimere REUS arranges liquid collecting room CLD, and hypomere REDS arranges 1 or 2 or multiple beds; Main charging REF autoreactor RE top enters reactor RE, and reactor RE is discharged in principal product REP autoreactor RE bottom, and the product liquid REFL from the liquid phase region of liquid collecting room CLD discharges reactor RE.
2. downflow reactor according to claim 1, is characterized in that:
Hypomere REDS arranges 2 or multiple beds, and the spatial placement between beds flows into the branch road charging aperture of branch road charging REF2.
3. downflow reactor according to claim 2, is characterized in that:
Hypomere REDS arranges 2 or multiple beds, the branch road charging aperture of the spatial placement branch road charging REF2 between beds, space between beds also arranges the branch road feed distributor be connected with branch road charging aperture, and the process acts of branch road feed distributor is: branch road charging REF2 is evenly distributed on the flow section of prevailing technology medium in reactor.
4. downflow reactor according to claim 2, is characterized in that:
Hypomere REDS arranges 2 or multiple beds, the branch road charging aperture of the spatial placement branch road charging REF2 between beds, spatial placement between beds has the hydrid component that branch road charging REF2 is mixed with upper catalyst bed laminar flow effluent, and the process acts of hydrid component is: branch road charging REF2 is mixed with lower catalyst bed laminar flow effluent.
5. downflow reactor according to claim 1, is characterized in that:
The entrance of beds that hypomere REDS is arranged, be provided with bed feed distributor, the process acts of bed feed distributor is: in reactor prevailing technology medium flow section on bed charging is evenly distributed on bottom bed.
6. downflow reactor according to claim 2, is characterized in that:
The entrance of beds that hypomere REDS is arranged, be provided with bed feed distributor, the process acts of bed feed distributor is: in reactor prevailing technology medium flow section on bed charging is evenly distributed on bottom bed.
7. downflow reactor according to claim 1, is characterized in that:
Beds is fixed bed.
8. downflow reactor according to claim 1, is characterized in that:
Beds is the online moving bed of downflow system, the online moving bed of described downflow system, in bed, processing medium flows downward, and draws off the active catalyst reduced in a continuous manner bottom bed, fills into fresh catalyst maintain bed catalyst reserve from bed top.
9. downflow reactor according to claim 1, is characterized in that:
Beds is downflow system online batch (-type) displacement bed, described downflow system online batch (-type) displacement bed, in bed, processing medium flows downward, and draws off the active catalyst reduced in an intermittent fashion, fills into fresh catalyst in an intermittent fashion and maintains bed catalyst reserve.
10. downflow reactor according to claim 1, is characterized in that:
The segmentation dividing plate of isolation epimere REUS and hypomere REDS is set in reactor shell RES, the logistics arranging the gas-liquid separation zone of conveying epimere REUS enters the passage DP of the downflow system catalytic reaction zone of hypomere REDS, passage DP is arranged in outside the housing of reactor RE, now, the epimere REUS space in reactor shell RES and hypomere REDS space isolate by segmentation dividing plate.
11. downflow reactors according to claim 1, is characterized in that:
The segmentation dividing plate of isolation epimere REUS and hypomere REDS is set in reactor shell RES, the logistics arranging the gas-liquid separation zone of conveying epimere REUS enters the passage DP of the downflow system catalytic reaction zone of hypomere REDS, passage DP is arranged in the housing of reactor RE, and passage DP is through segmentation dividing plate.
12. downflow reactors according to claim 1, is characterized in that:
Liquid collecting room CLD is set in the epimere of reactor shell RES, between liquid collecting room CLD sidewall and or fluid downlink spatial between liquid collecting room CLD sidewall and reactor shell RES, carry the logistics of the gas-liquid separation zone of epimere REUS to enter the passage DP of the downflow system catalytic reaction zone of hypomere REDS exactly.
13. downflow reactors according to claim 1, is characterized in that:
Liquid collecting room CLD is set in the epimere of reactor shell RES, the fluid downlink spatial between liquid collecting room CLD sidewall, carries the logistics of the gas-liquid separation zone of epimere REUS to enter the passage DP of the downflow system catalytic reaction zone of hypomere REDS exactly.
14. downflow reactors according to claim 1, is characterized in that:
Liquid collecting room CLD is set in the epimere of reactor shell RES, the fluid downlink spatial between liquid collecting room CLD sidewall and reactor shell RES, carries the logistics of the gas-liquid separation zone of epimere REUS to enter the passage DP of the downflow system catalytic reaction zone of hypomere REDS exactly.
15. downflow reactors according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14, is characterized in that: main charging REF is the logistics containing hydrocarbon ils.
16. downflow reactors according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14, it is characterized in that: main charging REF is that the hydro-upgrading process of high aroamtic hydrocarbon raw material HDS is carried out in the downflow system catalytic reaction zone that high aroamtic hydrocarbon raw material HDS, hypomere REDS are arranged;
High aroamtic hydrocarbon raw material HDS is selected from one or more in following materials:
1. coalite tar or its distillate;
2. medium temperature coal tar or its distillate;
3. high temperature coal-tar or its distillate;
4. coal liquefaction gained liquefied coal coil or its distillate;
5. shale oil or its distillate;
6. ethylene cracking tar;
7. petroleum base wax oil thermal cracking tars;
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;
9. petroleum based heavy fuel oils 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.
17. downflow reactors according to claim 16, is characterized in that:
The operating condition of the downflow system catalytic reaction zone that hypomere REDS is arranged is: temperature is 170 ~ 480 DEG C, pressure is 4.0 ~ 30.0MPa.
18. downflow reactors according to claim 16, is characterized in that:
Discharge the product liquid REFL of reactor RE from the liquid phase region CLD of liquid collecting room, after force (forcing) pump boosting, enter the reactor Inner eycle producing main charging REF use.
19. downflow reactors according to claim 16, is characterized in that:
Discharge the product liquid REFL of reactor RE from the liquid phase region CLD of liquid collecting room, after force (forcing) pump boosting, enter the reactor Inner eycle producing branch road charging REF2 use.
20. downflow reactors according to claim 16, is characterized in that:
Epimere REUS arranges liquid collecting room CLD, by arranging the upper space UNICOM of the beds that valvular pipeline and hypomere REDS are arranged, in the reactor emergency shutdown stage, the product liquid REFL discharging reactor RE with the liquid phase region CLD from liquid collecting room rinses beds, manufactures the flowing of downflow system fluid in beds.
21. downflow reactors according to claim 16, is characterized in that:
Epimere REUS, gaseous product discharges reactor RE as reaction feed flashed vapour REFV autoreactor RE top, enters reactor REFV-R.
22. downflow reactors according to claim 16, is characterized in that:
Epimere REUS, portion gas product discharges reactor RE as charging flashed vapour REFV autoreactor RE top, enters reactor REFV-R.
23. downflow reactors according to claim 16, is characterized in that:
Epimere REUS, product liquid REFL discharges reactor RE from the liquid phase region CLD of liquid collecting room at least partially, enters reactor REFL-R.
24. downflow reactors according to claim 16, is characterized in that:
Epimere REUS, whole product liquid REFL discharge reactor RE from the liquid phase region CLD of liquid collecting room, enter reactor REFL-R.
25. downflow reactors according to claim 16, is characterized in that:
Epimere REUS, portion gas product discharges reactor RE as charging flashed vapour REFV autoreactor RE top, enters cooling procedure REFV-CS.
26. downflow reactors according to claim 16, is characterized in that:
Epimere REUS, product liquid REFL discharges reactor RE from the liquid phase region CLD of liquid collecting room at least partially, enters cooling procedure REFL-CS.
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| CN112048345A (en) * | 2020-09-28 | 2020-12-08 | 姚英 | Organic sulfur conversion reactor for blast furnace gas |
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Application publication date: 20150930 |