CN109181765A - A kind of multistage hydrodesulfurization equipment and its operating method - Google Patents
A kind of multistage hydrodesulfurization equipment and its operating method Download PDFInfo
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- CN109181765A CN109181765A CN201811068292.7A CN201811068292A CN109181765A CN 109181765 A CN109181765 A CN 109181765A CN 201811068292 A CN201811068292 A CN 201811068292A CN 109181765 A CN109181765 A CN 109181765A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
- C10G65/08—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a hydrogenation of the aromatic hydrocarbons
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Abstract
The present invention relates to light aromatic hydrocarbons plus hydrogen renovation technique fields, and disclose a kind of multistage hydrodesulfurization equipment and its operating method, including adding hydrogen feed pump, described plus hydrogen feed pump is from left to right successively connected with hydrogenation heat exchanger, pre-hydrogenator, pre-add hydrogen cooler, main hydrogenator A, thick desulfurization reactor, main hydrogenator B and fine de-sulfur reactor.The multistage hydrodesulfurization equipment and its operating method, by the way that pre-hydrogenator is arranged, main effect is to ensure that main hydrogenator A's is normal, continuous operation, increase the processing capacity of hydrogenation catalyst, extend the service life of catalyst, improve the continuity of equipment, to improve the purifying rate of the equipment, enable the hydrodesulfurization equipment it is lasting carry out using, the advantages of having reached multistage hydrodesulfurization, solves existing hydrodesulfurization unit, purifying rate is low, period is long, cost of investment is big, it influences hydrodesulfurization unit and operates normally the problem of using.
Description
Technical field
The present invention relates to light aromatic hydrocarbons plus hydrogen renovation technique field, specially a kind of multistage hydrodesulfurization equipment and its behaviour
Make method.
Background technique
Hydrodesulfurization refers to that organosulfur compound reacts the reaction for being converted into hydrogen sulfide and hydrocarbon with atmosphere under the action of catalyst.
When using refinery gas, casing-head gas and light petrol etc. for raw material hydrogen manufacturing, contained organosulfur compound (thioether, bite by such as mercaptan
Expect, thiophane, disulphide etc.) first hydrogenolysis generates H2S and hydrocarbon, and H2S is absorbed by ZnO again and is removed, to prevent in catalyst
Poison.The Co-Mo system that catalyst generally uses activated alumina to load.Hydrodesulfurization is actually that organic sulfur is turned by hydrogenolysis
The hydrogen sulfide being easily removed is turned to, to reach the technical process of deep removal.
Traditional hydrodesulfurization unit, first is that the process of hydrogenation plant is short, purifying rate is low；Second is that the purifying rate of hydrogenation plant
Height, but the period is long, the investment of catalyst is larger, leads to higher cost, to influence the normal operation of hydrodesulfurization unit.
Summary of the invention
The present invention provides a kind of multistage hydrodesulfurization equipment and its operating methods, have the excellent of multistage hydrodesulfurization
Point solves existing hydrodesulfurization unit, and purifying rate is low, the period is long, cost of investment is big, influences hydrodesulfurization unit normal operation
The problem of use.
The invention provides the following technical scheme: a kind of multistage hydrodesulfurization equipment, including add hydrogen feed pump, it is described to add
Hydrogen feed pump be from left to right successively connected with hydrogenation heat exchanger, pre-hydrogenator, pre-add hydrogen cooler, main hydrogenator A,
Thick desulfurization reactor, main hydrogenator B and fine de-sulfur reactor；
The lateral surface of the hydrogenation heat exchanger includes two sealing plates being mutually permanently connected, at the top of the hydrogenation heat exchanger
Left side it is fixed be communicated with fluid inlet tube A, the left side of the hydrogenation heat exchanger bottom is fixed to be communicated with fluid outlet pipe A, it is described plus
Middle-end at the top of hydrogen heat exchanger, which is fixed, is communicated with fluid inlet tube B, and the right side fixation of the hydrogenation heat exchanger bottom is communicated with fluid
Outlet pipe B；
Described plus hydrogen feed pump includes pedestal, and the medial surface of the pedestal is fixedly connected with firm axis, the pedestal top
Left side be fixedly connected with motor cabinet, equipment motor, the right side at the top of the pedestal are fixedly installed at the top of the motor cabinet
It is fixedly installed with and adds hydrogen pump end, described plus hydrogen pump end right end includes non-driven-end bearing part, the left side at the top of the equipment motor
Side is fixedly installed with elongated end, and the right side at the top of the equipment motor is fixedly installed with motor and covers surely, described plus hydrogen pump end top
Portion is fixedly installed with ventilation end, and the quantity at the ventilation end is two, and two ventilation ends are adding hydrogen with symmetrical formal distribution
The top at end is pumped, the output end of the equipment motor is located at the right side of equipment motor, the other end of the equipment motor output end
It is connected with the left side at hydrogen pump end is added, the lateral surface of the equipment motor output end is equipped with output shaft protective cover, the output
The bottom of axis protective cover is fixedly connected with supporting linkage, is fixedly connected at the top of the bottom end of the supporting linkage and pedestal；
The pre-hydrogenator, main hydrogenator A and main hydrogenator B include consersion unit, the reaction
The lateral surface of equipment is equipped with casing, and feed inlet is offered at the top of consersion unit, and be fixedly installed on the inside of feed inlet into
Mouth diffuser, the bottom of the consersion unit offers discharge port, and exit collector is fixedly installed on the inside of discharge port, institute
The outer surface for stating consersion unit is fixedly installed with thermocouple, and the inside of the consersion unit is fixedly installed with distribution plate, and described point
Bottom with disk is fixedly installed with sediment incrustation basket, and the inside of the consersion unit is fixedly installed with catalyst support beam, the catalysis
The outer surface of agent supporting beam is fixedly installed with dress porcelain ball, and the inside of the consersion unit is fixedly installed with cold hydrogen disk, the cold hydrogen
The lower section of disk is equipped with lower part distribution plate, and lower part distribution plate includes cold hydrogen box, and the top fixation of the cold hydrogen box is communicated with cold hydrogen
Pipe, the inside of the consersion unit are fixedly installed with spraying disc, and the spraying disc is located at the underface of lower part distribution plate, described to urge
Agent supporting beam is located at the underface of distribution plate, and catalyst support beam is located at the surface of cold hydrogen disk, and the consersion unit is right
The bottom fixation of side is communicated with catalyst delivery end.
Preferably, offer gas outlet and air inlet on the outside of the hydrogenation heat exchanger, the pre-hydrogenator it is outer
Side offers air inlet, and the air inlet of the pre-hydrogenator is connected with the gas outlet of hydrogenation heat exchanger.
Preferably, the fluid inlet tube A is corresponding with fluid outlet pipe A, and fluid inlet tube B is corresponding with fluid outlet pipe B.
Preferably, the body of the pre-hydrogenator, main hydrogenator A and main hydrogenator B internal-response equipment
Product size is unequal.
It is a kind of multistage hydrodesulfurization operating method, it is described multistage hydrodesulfurizationprocess process the following steps are included:
The first step, a stage hydrogenation operation
Preliminary pre-hydrotreating reaction is carried out by pre-hydrogenator first, a stage reactors utilize the activity of NI catalyst
And selectivity, under certain temperature and pressure, hydrogen and light aromatic hydrocarbons component are mixed into catalyst bed, by light aromatic hydrocarbons component
In diolefin, styrene and derivative, indenes, part monoolefin hydrogenation；Reaction equation the following steps are included:
Main reaction: diolefin adds hydrogen to become monoolefine: CnH2n-2+H2→CnH2n, monoolefin hydrogenation become saturated hydrocarbons: CnH2n+
H2→CnH2n+2, diolefin add hydrogen to become saturated hydrocarbons: CnH2n-2+2H2→CnH2n+2, styrene hydrogenation become ethylo benzene: C6H5C2H3+
H2→C6H5C2H5, indenes be hydrogenated to indane: C9H8+H2→C9H10, sulfide removal reaction: RS+H2→R1+H2S；
Side reaction: diolefin polymerization reaction, diolefin and monoolefm polymerisations reaction, styrene self-polymeric reaction；
Thick desulfurization operations are carried out by thick desulfurization reactor after the reaction was completed；
Second step, two-stage hydrogenation operation
Second-stage hydrogenation reactor utilizes molybdenum-Raney nickel activity and selectivity, will come from one-stage hydrogenation product and hydrogen
It is mixed into reactor, monoolefin hydrogenation reaction is substantially carried out in reactor, part styrene derivative adds hydrogen and sulfide
Hydrocracking, key reaction are as follows:
Main reaction:
Monoolefin hydrogenation becomes saturated hydrocarbons: CnH2n+H2→CnH2n+2, diolefin add hydrogen to become saturated hydrocarbons: CnH2n-2+2H2→
CnH2n+2, sulfide add hydrogen to become alkane: C4H4S+2H2→C4H6+H2S, nitride adds hydrogen to become alkane: 2RN+3H2→R1+
2NH3；
Side reaction:
Hydrocracking reaction: R1-CH2-CH2-R2→R1-CH3+R2-CH3, benzene hydrogenation: C6H6+3H2→C6H12, it is unstable
Determine the side reaction that compound polymerization generates colloid and carbon；
Fine de-sulfur operation is carried out by fine de-sulfur reactor after the reaction was completed.
The present invention have it is following the utility model has the advantages that
The multistage hydrodesulfurization equipment and its operating method, by the way that pre-hydrogenator is arranged, main effect is
It ensure that normal, the continuous operation of main hydrogenator A, and the quantity of pre-hydrogenator is two, one opens one standby, facilitates master
Hydrogenator A persistently can run, and pass through the cross-reference of main hydrogenator A and main hydrogenator B, increase
The processing capacity for having added hydrogenation catalyst extends the service life of catalyst, improves the continuity of equipment, to improve this
The purifying rate of equipment enables the hydrodesulfurization equipment is lasting to carry out using having reached the excellent of multistage hydrodesulfurization
Point solves existing hydrodesulfurization unit, and purifying rate is low, the period is long, cost of investment is big, influences hydrodesulfurization unit normal operation
The problem of use.
Detailed description of the invention
Fig. 1 is present invention process equipment flowsheet；
Fig. 2 is hydrogenation heat exchanger structural schematic diagram of the present invention；
Fig. 3 is the present invention plus hydrogen feed pump structural schematic diagram；
Fig. 4 is consersion unit structural schematic diagram of the present invention.
In figure: 1, hydrogenation heat exchanger；101, sealing plate；102, fluid inlet tube A；103, fluid outlet pipe A；104, fluid inlet tube
B；105, fluid outlet pipe B；2, pre-hydrogenator；3, pre-add hydrogen cooler；4, main hydrogenator A；5, thick desulfurization reactor；
6, main hydrogenator B；7, fine de-sulfur reactor；8, add hydrogen feed pump；801, pedestal；802, axis is consolidated；803, motor cabinet；
804, equipment motor；805, add hydrogen pump end；806, non-driven-end bearing part；807, elongated end；808, motor covers surely；809, it ventilates
End；810, output shaft protective cover；811, supporting linkage；9, consersion unit；901, inlet diffuser；902, exit collector；
903, catalyst delivery end；904, thermocouple；905, distribution plate；906, sediment incrustation basket；907, catalyst support beam；908, porcelain is filled
Ball；909, cold hydrogen disk；910, lower part distribution plate；911, cold hydrogen box；912, cold hydrogen tube；913, spraying disc.
Specific embodiment
Following will be combined with the drawings in the embodiments of the present invention, and technical solution in the embodiment of the present invention carries out clear, complete
Site preparation description, it is clear that described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.It is based on
Embodiment in the present invention, it is obtained by those of ordinary skill in the art without making creative efforts every other
Embodiment shall fall within the protection scope of the present invention.
Fig. 1-4, a kind of multistage hydrodesulfurization equipment are please referred to, including adds hydrogen feed pump 8, adds hydrogen feed pump 8 from a left side
It is anti-that hydrogenation heat exchanger 1, pre-hydrogenator 2, pre-add hydrogen cooler 3, main hydrogenator A4, thick desulfurization are successively connected with to the right side
Device 5, main hydrogenator B6 and fine de-sulfur reactor 7, the outside of hydrogenation heat exchanger 1 is answered to offer gas outlet and air inlet, in advance
The outside of hydrogenator 2 offers air inlet, and the air inlet of pre-hydrogenator 2 is connected with the gas outlet of hydrogenation heat exchanger 1
It connects；
The lateral surface of hydrogenation heat exchanger 1 includes two sealing plates being mutually permanently connected 101,1 top of hydrogenation heat exchanger
Left side is fixed to be communicated with fluid inlet tube A102, and the left side fixation of 1 bottom of hydrogenation heat exchanger is communicated with fluid outlet pipe A103, hydrogen is added to change
The middle-end at hot 1 top of device is fixed to be communicated with fluid inlet tube B104, and the right side fixation of 1 bottom of hydrogenation heat exchanger is communicated with fluid outlet pipe
B105, fluid inlet tube A102 is corresponding with fluid outlet pipe A103, and fluid inlet tube B104 is corresponding with fluid outlet pipe B105；
Adding hydrogen feed pump 8 includes pedestal 801, and the medial surface of pedestal 801 is fixedly connected with firm axis 802,801 top of pedestal
Left side be fixedly connected with motor cabinet 803, the top of motor cabinet 803 is fixedly installed with equipment motor 804,801 top of pedestal
Right side is fixedly installed with plus hydrogen pump end 805, and adding the right end at hydrogen pump end 805 includes non-driven-end bearing part 806, equipment motor 804
Elongated end 807 is fixedly installed on the left of top, the right side at 804 top of equipment motor is fixedly installed with motor and covers 808 surely, adds hydrogen
The top at pump end 805 is fixedly installed with ventilation end 809, and the quantity at ventilation end 809 is two, and two ventilation ends 809 are with symmetrical
Formal distribution at the top for adding hydrogen pump end 805, the output end of equipment motor 804 is located at the right side of equipment motor 804, equipment electricity
The other end of 804 output end of machine is connected with the left side at hydrogen pump end 805 is added, and the lateral surface of 804 output end of equipment motor is equipped with
Output shaft protective cover 810, the bottom of output shaft protective cover 810 are fixedly connected with supporting linkage 811, supporting linkage 811
Bottom end is fixedly connected with the top of pedestal 801；
Pre-hydrogenator 2, main hydrogenator A4 and main hydrogenator B6 include consersion unit 9, and pre-add hydrogen is anti-
Answer the volume size of device 2, main hydrogenator A4 and main hydrogenator B6 internal-response equipment 9 unequal, consersion unit 9
Lateral surface is equipped with casing, and the top of consersion unit 9 offers feed inlet, and entrance diffusion is fixedly installed on the inside of feed inlet
Device 901, the bottom of consersion unit 9 offer discharge port, and exit collector 902 is fixedly installed on the inside of discharge port, reaction
The outer surface of equipment 9 is fixedly installed with thermocouple 904, and the inside of consersion unit 9 is fixedly installed with distribution plate 905, distribution plate 905
Bottom be fixedly installed with sediment incrustation basket 906, the inside of consersion unit 9 is fixedly installed with catalyst support beam 907, catalyst support
The outer surface of beam 907 is fixedly installed with dress porcelain ball 908, and the inside of consersion unit 9 is fixedly installed with cold hydrogen disk 909, cold hydrogen disk 909
Lower section be equipped with lower part distribution plate 910, and lower part distribution plate 910 includes cold hydrogen box 911, the fixed connection in the top of cold hydrogen box 911
There is cold hydrogen tube 912, the inside of consersion unit 9 is fixedly installed with spraying disc 913, and spraying disc 913 is being located at lower part distribution plate 910 just
Lower section, catalyst support beam 907 is located at the underface of distribution plate 905, and catalyst support beam 907 is being located at cold hydrogen disk 909 just
Top, 9 right side of consersion unit bottom fixation is communicated with catalyst delivery end 903, the multistage hydrodesulfurization equipment and
Its operating method, by the way that pre-hydrogenator 2 is arranged, main effect is to ensure that main hydrogenator A4's is normal, continuous
Operation, and the quantity of pre-hydrogenator 2 is two, one opens one standby, facilitates what main hydrogenator A4 can be lasting transport
Row, and pass through the cross-reference of main hydrogenator A4 and main hydrogenator B6, the processing capacity of hydrogenation catalyst is increased, is prolonged
The service life for having grown catalyst, improves the continuity of equipment, so that the purifying rate of the equipment is improved, so that hydrogen should be added de-
Sulphur process equipment can be lasting carry out using, the advantages of having reached multistage hydrodesulfurization, solve existing hydrodesulfurization unit,
Purifying rate is low, the period is long, cost of investment is big, influences hydrodesulfurization unit and operates normally the problem of using.
It is a kind of multistage hydrodesulfurization operating method, multistage hydrodesulfurizationprocess process the following steps are included:
The first step, a stage hydrogenation operation
Preliminary pre-hydrotreating reaction is carried out by pre-hydrogenator 2 first, a stage reactors utilize the work of NI catalyst
Property and selectivity, under certain temperature and pressure, hydrogen and light aromatic hydrocarbons component are mixed into catalyst bed, by light aromatic hydrocarbons group
Diolefin, styrene and derivative, indenes, part monoolefin hydrogenation in point；Reaction equation the following steps are included:
Main reaction: diolefin adds hydrogen to become monoolefine: CnH2n-2+H2→CnH2n, monoolefin hydrogenation become saturated hydrocarbons: CnH2n+
H2→CnH2n+2, diolefin add hydrogen to become saturated hydrocarbons: CnH2n-2+2H2→CnH2n+2, styrene hydrogenation become ethylo benzene: C6H5C2H3+
H2→C6H5C2H5, indenes be hydrogenated to indane: C9H8+H2→C9H10, sulfide removal reaction: RS+H2→R1+H2S；
Side reaction: diolefin polymerization reaction, diolefin and monoolefm polymerisations reaction, styrene self-polymeric reaction；
Thick desulfurization operations are carried out by thick desulfurization reactor 5 after the reaction was completed；
Second step, two-stage hydrogenation operation
Second-stage hydrogenation reactor utilizes molybdenum-Raney nickel activity and selectivity, will come from one-stage hydrogenation product and hydrogen
It is mixed into reactor, monoolefin hydrogenation reaction is substantially carried out in reactor, part styrene derivative adds hydrogen and sulfide
Hydrocracking, key reaction are as follows:
Main reaction:
Monoolefin hydrogenation becomes saturated hydrocarbons: CnH2n+H2→CnH2n+2, diolefin add hydrogen to become saturated hydrocarbons: CnH2n-2+2H2→
CnH2n+2, sulfide add hydrogen to become alkane: C4H4S+2H2→C4H6+H2S, nitride adds hydrogen to become alkane: 2RN+3H2→R1+
2NH3；
Side reaction:
Hydrocracking reaction: R1-CH2-CH2-R2→R1-CH3+R2-CH3, benzene hydrogenation: C6H6+3H2→C6H12, it is unstable
Determine the side reaction that compound polymerization generates colloid and carbon；
Fine de-sulfur operation is carried out by fine de-sulfur reactor 7 after the reaction was completed.
The operating method of pre-hydrogenator: in pre-hydrogenator 2, light component is in low temperature liquid phase in light aromatic hydrocarbons raw material
Down plus hydrogen, light component enters in pre-hydrogenator 2 after mixing with liquid phase circulation material in light aromatic hydrocarbons raw material, and hydrogen is by fresh hydrogen
Enter reactor together with raw material, diolefin, styrene and derivative, indenes and part monoolefine are selectively added in reactor
Hydrogen obtains stable drippolene.
As the process of operation makes catalyst since colloid and polymer constantly accumulate on catalyst activity surface
Activity decline, when activity drops to highest inlet operating temperature up to 110 DEG C, product quality be can not reach when requiring, catalysis
Agent must regenerate, the temporary poisonous substance of 2 catalyst of pre-hydrogenator such as: free water and sulphur can influence catalyst activity, because
Free water and sulphur is avoided to enter reactor when this operation.
The deviation of temperature is very little in pre-hydrogenator 2, however temperature can be generated by reacting the operating result under overtemperature
Deviation, this maloperation can lead to aromatic plus hydrogen, it is a high exothermic reaction, and under normal circumstances, aromatic series is
It is nonreactive, when being put into the catalyst of new high activity in equipment, it is very big to there is a possibility that temperature deviation, but hereafter with
The accumulation of process time, this possibility are being successively decreased, and when being equipped with raw catelyst reactor when going into operation, to examine reactor
Bed temperature rise, such as occurs temperature deviation, and device will stop.
If 2 product diene value content of pre-hydrogenator is more than code requirement, reactor inlet temperature will increase, usually
Inlet temperature adjusts 1~2 DEG C, when inlet temperature is excessively high, is also easy to produce temperature of reactor deviation, therefore to avoid entering in excessively high
It is operated at a temperature of mouthful.
The total internal circulating load of pre-hydrogenator 2 will control in a certain range, 2 liquid phase feeding temperature of pre-hydrogenator
Controller TV20201 will be by automatic adjustment, by the internal circulating load of cooler E2013, to provide entrance required by reactor
Temperature, 2 recycle oil of pre-hydrogenator have triple role, first is that reducing the ratio for entering colloid in hydrogenator material；Two
It is to increase air speed, increases and colloid on catalyst bed is washed away；Third is that being conducive to taking away for reaction heat, polymerization is reduced.
It should be noted that, in this document, relational terms such as first and second and the like are used merely to a reality
Body or operation are distinguished with another entity or operation, are deposited without necessarily requiring or implying between these entities or operation
In any actual relationship or order or sequence.Moreover, the terms "include", "comprise" or its any other variant are intended to
Non-exclusive inclusion, so that the process, method, article or equipment including a series of elements is not only wanted including those
Element, but also including other elements that are not explicitly listed, or further include for this process, method, article or equipment
Intrinsic element.
It although an embodiment of the present invention has been shown and described, for the ordinary skill in the art, can be with
A variety of variations, modification, replacement can be carried out to these embodiments without departing from the principles and spirit of the present invention by understanding
And modification, the scope of the present invention is defined by the appended.
Claims (5)
1. a kind of multistage hydrodesulfurization equipment, including add hydrogen feed pump (8), it is characterised in that: described plus hydrogen feed pump (8)
From left to right successively it is connected with hydrogenation heat exchanger (1), pre-hydrogenator (2), pre-add hydrogen cooler (3), main hydrogenator A
(4), thick desulfurization reactor (5), main hydrogenator B (6) and fine de-sulfur reactor (7)；
The lateral surface of the hydrogenation heat exchanger (1) includes two sealing plates being mutually permanently connected (101), the hydrogenation heat exchanger
(1) the left side fixation at the top of is communicated with fluid inlet tube A (102), and the left side fixation of hydrogenation heat exchanger (1) bottom is communicated with stream
Body outlet pipe A (103), the middle-end fixation at the top of the hydrogenation heat exchanger (1) are communicated with fluid inlet tube B (104), the hydrogenation and heat-exchange
The right side fixation of device (1) bottom is communicated with fluid outlet pipe B (105)；
Described plus hydrogen feed pump (8) include pedestal (801), and the medial surface of the pedestal (801) is fixedly connected with firm axis
(802), the left side at the top of the pedestal (801) is fixedly connected with motor cabinet (803), and the top of the motor cabinet (803) is fixed
It is equipped with equipment motor (804), the right side at the top of the pedestal (801) is fixedly installed with plus hydrogen pump end (805), described plus hydrogen pump
The right end for holding (805) includes non-driven-end bearing part (806), and the left side at the top of the equipment motor (804), which is fixedly installed with, prolongs
It stretches end (807), the right side at the top of the equipment motor (804) is fixedly installed with motor and covers (808) surely, described plus hydrogen pump end
(805) ventilation end (809) is fixedly installed at the top of, the quantity of ventilation end (809) is two, and two ventilation ends
(809) with symmetrical formal distribution at the top for adding hydrogen pump end (805), the output end of the equipment motor (804) is located at equipment
The right side of motor (804), the other end of equipment motor (804) output end are connected with the left side of hydrogen pump end (805) is added,
The lateral surface of equipment motor (804) output end is equipped with output shaft protective cover (810), the output shaft protective cover (810)
Bottom is fixedly connected with supporting linkage (811), and the bottom end of the supporting linkage (811) and the top of pedestal (801) are fixed
Connection；
The pre-hydrogenator (2), main hydrogenator A (4) and main hydrogenator B (6) include consersion unit (9),
The lateral surface of the consersion unit (9) is equipped with casing, and feed inlet is offered at the top of consersion unit (9), and feed inlet is interior
Side is fixedly installed with inlet diffuser (901), and the bottom of the consersion unit (9) offers discharge port, and the inside of discharge port
It is fixedly installed with exit collector (902), the outer surface of the consersion unit (9) is fixedly installed with thermocouple (904), described anti-
The inside of equipment (9) is answered to be fixedly installed with distribution plate (905), the bottom of the distribution plate (905) is fixedly installed with sediment incrustation basket
(906), the inside of the consersion unit (9) is fixedly installed with catalyst support beam (907), the catalyst support beam (907)
Outer surface be fixedly installed with dress porcelain ball (908), the inside of the consersion unit (9) is fixedly installed with cold hydrogen disk (909), described
The lower section of cold hydrogen disk (909) is equipped with lower part distribution plate (910), and lower part distribution plate (910) includes cold hydrogen box (911), described cold
The top fixation of hydrogen case (911) is communicated with cold hydrogen tube (912), and the inside of the consersion unit (9) is fixedly installed with spraying disc
(913), the spraying disc (913) is located at the underface of lower part distribution plate (910), and the catalyst support beam (907), which is located at, divides
Underface with disk (905), and catalyst support beam (907) is located at the surface of cold hydrogen disk (909), the consersion unit (9)
The bottom fixation of right side is communicated with catalyst delivery end (903).
2. a kind of multistage hydrodesulfurization equipment according to claim 1, it is characterised in that: the hydrogenation heat exchanger
(1) gas outlet and air inlet are offered on the outside of, offer air inlet, the pre-add on the outside of the pre-hydrogenator (2)
The air inlet of hydrogen reactor (2) is connected with the gas outlet of hydrogenation heat exchanger (1).
3. a kind of multistage hydrodesulfurization equipment according to claim 1, it is characterised in that: the fluid inlet tube A
(102) corresponding with fluid outlet pipe A (103), and fluid inlet tube B (104) is corresponding with fluid outlet pipe B (105).
4. a kind of multistage hydrodesulfurization equipment according to claim 1, it is characterised in that: the pre-hydrogenator
(2), the volume size of main hydrogenator A (4) and main hydrogenator B (6) internal-response equipment (9) is unequal.
5. a kind of operating method of multistage hydrodesulfurization, it is characterised in that: the multistage hydrodesulfurizationprocess process includes following
Step:
The first step, a stage hydrogenation operation
Preliminary pre-hydrotreating reaction is carried out by pre-hydrogenator (2) first, a stage reactors utilize the activity of NI catalyst
And selectivity, under certain temperature and pressure, hydrogen and light aromatic hydrocarbons component are mixed into catalyst bed, by light aromatic hydrocarbons component
In diolefin, styrene and derivative, indenes, part monoolefin hydrogenation；Reaction equation the following steps are included:
Main reaction: diolefin adds hydrogen to become monoolefine: CnH2n-2+H2→CnH2n, monoolefin hydrogenation become saturated hydrocarbons: CnH2n+H2→
CnH2n+2, diolefin add hydrogen to become saturated hydrocarbons: CnH2n-2+2H2→CnH2n+2, styrene hydrogenation become ethylo benzene: C6H5C2H3+H2→
C6H5C2H5, indenes be hydrogenated to indane: C9H8+H2→C9H10, sulfide removal reaction: RS+H2→R1+H2S；
Side reaction: diolefin polymerization reaction, diolefin and monoolefm polymerisations reaction, styrene self-polymeric reaction；
Thick desulfurization operations are carried out by thick desulfurization reactor (5) after the reaction was completed；
Second step, two-stage hydrogenation operation
Second-stage hydrogenation reactor utilizes molybdenum-Raney nickel activity and selectivity, will mix from one-stage hydrogenation product with hydrogen
Into reactor, monoolefin hydrogenation reaction is substantially carried out in reactor, part styrene derivative adds hydrogen and sulfide to add hydrogen
Cracking, key reaction are as follows:
Main reaction:
Monoolefin hydrogenation becomes saturated hydrocarbons: CnH2n+H2→CnH2n+2, diolefin add hydrogen to become saturated hydrocarbons: CnH2n-2+2H2→
CnH2n+2, sulfide add hydrogen to become alkane: C4H4S+2H2→C4H6+H2S, nitride adds hydrogen to become alkane: 2RN+3H2→R1+
2NH3；
Side reaction:
Hydrocracking reaction: R1-CH2-CH2-R2→R1-CH3+R2-CH3, benzene hydrogenation: C6H6+3H2→C6H12, destabilization
Close the side reaction that object polymerization generates colloid and carbon；
Fine de-sulfur operation is carried out by fine de-sulfur reactor (7) after the reaction was completed.
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| CN112745892A (en) * | 2019-10-30 | 2021-05-04 | 中国石油化工股份有限公司 | Residual oil hydrotreating method |
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