CN203559012U - Coal tar treatment system - Google Patents
Coal tar treatment system Download PDFInfo
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- CN203559012U CN203559012U CN201320600022.2U CN201320600022U CN203559012U CN 203559012 U CN203559012 U CN 203559012U CN 201320600022 U CN201320600022 U CN 201320600022U CN 203559012 U CN203559012 U CN 203559012U
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Abstract
The utility model relates to a coal tar treatment system. The coal tar treatment system comprises a raw oil buffer tank, a coal tar pump, a first filter, a first heat exchanger, a dehydrating tower, a first air cooler, a separator, a second heat exchanger, a coal tar feeding furnace, a coal tar vacuum tower, a light oil mixing tank, a light oil pump, a heavy oil mixing tank, a heavy oil pump, a second filter, a raw material mixing tank, a raw material oil pump, a make-up hydrogen compressor, a suspended bed reactor unit, a fixed bed reactor, a vacuum tower, a fixed bed thermal high-pressure separator, a third heat exchanger, a fixed bed cold high-pressure separator, a fourth heat exchanger, a second air cooler, a circulating hydrogen compressor, and a liquid-separation tank at the inlet of the circulating hydrogen compressor, wherein the suspended bed reactor unit comprises a suspended bed cracking reactor, a thermal high-pressure separator, a thermal low-pressure separator and a cold low-pressure separator. By adopting the coal tar treatment system for treating the coal tar, the comprehensively utilized products of the coal tar is diversified and the market requirement can be met.
Description
Technical field
The utility model relates to a kind for the treatment of system of coal tar, belongs to Coal Chemical Industry and petrochemical technology field.
Background technology
Coal tar is the byproduct of pyrolysis of coal coke processed, occupies certain share in coal production.Current, China produces tar per year and is about 9,000,000 tons, but actual working ability is only 3,000,000 tons.Due to the restriction of the backward technology of coke downstream chemical industry, the huge coal tar of quantity is difficult to effective utilization.
The traditional diamond-making technique of coal tar, take physical sepn, extraction single component or narrow component product as target, refines washing oil, light oil, carbolineum, NAPTHALENE FLAKES. (INDUSTRIAL GRADE）, crude phenols and pitch inferior from coal tar.Due to coal tar complicated components, high added value component concentration is low, and the low value-added component that content is high is difficult to utilize, many technical disadvantages such as conventional refining technique inevitably exists flow process complexity, equipment is many, energy consumption is high, secondary pollution is serious, deficiency in economic performance.Owing to lacking a set of suitable processing scheme, cause coal tar simply directly to utilize or discarded, the environment that not only reduced resource value but also severe contamination.
Floating bed hydrocracking Technology originates from German Bergius-Pier gelatin liquefaction technology in 1913, this technology as far back as last century the '20s just in Germany, realized industrial applications.During 1927-1943, use this technology to build also successful operation 12 in Germany and overlap DCL/Direct coal liquefaction device.Adopt this technology production high-quality clean fuel, realize the increment utilization of tar resource, economic benefit is good.Floating bed hydrogenation floating bed hydrocracking technology, containing liquid-phase hydrogenatin processing (LPH) and two processes of gas phase hydrogenation processing (GPH).Its principle is:
(1) raw material enters suspended-bed reactor after mixing with additive and hydrogen, there is heat cracking reaction, and hydrogenation is saturated under high-pressure hydro state, wherein, in charging, carbon residue, colloid, bituminous matter issue heat-dissipating cracking and the saturated process of hydrogenation at specific Additive, substantially there is no the generation of coke.
(2) product of suspension bed thermally splitting enters in high pressure hot separator and separates, and clean gaseous product goes fixed-bed reactor in further hydrocracking and hydrofining, produces petroleum naphtha and the solar oil of high-quality; Isolated solid matter is mainly coke, can granulation work as pitch or coal-fired use.
At present, existing suspended bed device hydrogen addition technology flow process (as shown in Figure 1) is: full cut coal tar is after High pressure feeding pump boosts, mix with additive, hydrogen, by two high pressure heat exchangers, a reaction feed process furnace, be heated to certain temperature, enter floating bed hydrogenation reactor.Suspended-bed reactor reaction product separates in high pressure hot separator, and gas phase is entered fixed-bed reactor, and liquid phase (containing solid particulate) is entered decompression distillation system.In fixed-bed reactor, there is cracking refining reaction, after later separation, produce qualified product.In this flow process, the full cut of coal tar directly enters floating bed hydrogenation device.According to the experimental study report of coal tar, coal tar gently holds cut (boiling range is 170-230 ℃) can propose phenolic compound, all enters floating bed hydrogenation device, coal tar comprehensive utilization rate variance.Light oil directly enters floating bed hydrogenation reactor, has increased the load of floating bed hydrogenation reactor, and light oil cracking becomes dry gas simultaneously, has reduced product liquid yield.In coal tar, solids content is many, through reasonably de-slag operation, does not directly enter floating bed hydrogenation device, and raw material severity is high.
Utility model content
For solving the problems of the technologies described above, the purpose of this utility model is to provide a kind for the treatment of system of coal tar, adopt coal tar is filtered, dewaters, the reduced pressure pre-treatment such as deep drawing processing of this system, various components are processed respectively, can make the product diversification of the comprehensive utilization of coal tar, more adapt to the demand in market.
For achieving the above object, the utility model provides a kind for the treatment of system of coal tar, it is characterized in that, the treatment system of this coal tar comprises: stock oil surge tank, coal tar oil pump, the first strainer, First Heat Exchanger, dehydration tower, the first air cooler, separator, the second interchanger, coal tar stove, coal tar vacuum distillation tower, light oil mixing tank, light oil pump, heavy oil mixing tank, petroleum pump, the second strainer, raw material mixing tank, raw oil pump, make-up hydrogen compressor, suspended-bed reactor unit, fixed-bed reactor, vacuum distillation tower, fixed bed high pressure hot separator, the 3rd interchanger, fixed bed cold high pressure separator, the 4th interchanger, the second air cooler, circulating hydrogen compressor, circulating hydrogen compressor entrance divides flow container, described suspended-bed reactor unit comprises suspension bed cracking case, high pressure hot separator, thermal low-pressure separators and cold low separator, wherein:
Described stock oil surge tank is provided with the stock oil entrance for inputting feed coal tar, and its outlet is connected by pipeline with the entrance of the first strainer, and the connecting tube of the two is provided with coal tar oil pump;
The outlet of described the first strainer is connected to the entrance of described dehydration tower by pipeline, the connecting tube of the two is provided with First Heat Exchanger;
The top exit of described dehydration tower is connected with the entrance of the first air cooler by pipeline, its outlet at bottom is connected with the entrance of described coal tar stove by pipeline, and the connecting tube between described dehydration tower outlet at bottom and the entrance of described coal tar stove is provided with the second interchanger;
The outlet of described the first air cooler is connected with the entrance of described separator by pipeline;
Described separator is provided with light oil outlet and water contracts out mouth, and described light oil outlet is connected to described dehydration tower and fixed-bed reactor by pipeline, and described water contracts out mouth for discharging the moisture of separation;
The outlet of described coal tar stove is connected with the entrance of described coal tar vacuum distillation tower by pipeline;
Described coal tar vacuum distillation tower is extracted mouth out at the bottom of being provided with top exit, vacuum 1st side cut extraction mouth, second line of distillation extraction mouth and tower, described top exit is connected with the entrance of described light oil mixing tank by pipeline, described vacuum 1st side cut is extracted mouth out for extracting light oil out and being connected with the entrance of described light oil mixing tank by pipeline, described second line of distillation is extracted mouth out for extracting wax oil out and being connected with the entrance of described heavy oil mixing tank by pipeline, extracts mouth out and be connected with the entrance of described the second strainer by pipeline at the bottom of described tower;
Described light oil mixing tank is connected with the entrance of described fixed-bed reactor by pipeline, and the connecting tube between the two is provided with light oil pump;
Described heavy oil mixing tank is connected with the entrance of described raw material mixing tank by pipeline, and the connecting tube between the two is provided with petroleum pump;
Described raw material mixing tank is provided with additive entrance for inputting additive, its outlet is connected with the bottom inlet of the suspension bed cracking case of described suspended-bed reactor unit by pipeline, and this pipeline is provided with raw oil pump and is connected with new hydrogen input channel, new hydrogen input channel is provided with make-up hydrogen compressor;
The filtrate outlet of described the second strainer is connected with the entrance of described heavy oil mixing tank by pipeline;
The top exit of suspension bed cracking case and the entrance of described high pressure hot separator of described suspended-bed reactor unit are connected, the top exit of described high pressure hot separator is connected with the entrance of described fixed-bed reactor by pipeline, the outlet at bottom of described high pressure hot separator is connected with the entrance of described thermal low-pressure separators, the top exit of described thermal low-pressure separators is connected with the entrance of described thermal low-pressure separators, the outlet at bottom of described thermal low-pressure separators is connected with the entrance of described vacuum distillation tower, the outlet at bottom of described thermal low-pressure separators is connected with the entrance of described vacuum distillation tower by pipeline,
The outlet at bottom of described fixed-bed reactor is connected with the entrance of described fixed bed high pressure hot separator by pipeline, and the connecting tube between the two is provided with the 3rd interchanger;
Described vacuum distillation tower is provided with top exit and outlet at bottom;
The top exit of described fixed bed high pressure hot separator is connected with the entrance of described fixed bed cold high pressure separator by pipeline, and the connecting tube of the two is provided with the 4th interchanger and the second air cooler, and it is also provided with outlet at bottom;
The top exit of described fixed bed cold high pressure separator divides the entrance of flow container to be connected with described circulating hydrogen compressor entrance, and it is also provided with two outlet at bottoms;
Described circulating hydrogen compressor entrance divides the top exit of flow container and the entrance of described circulating hydrogen compressor to be connected, and it is also provided with outlet at bottom;
The outlet of described circulating hydrogen compressor is connected with the suspension bed cracking case of described fixed-bed reactor, described suspended-bed reactor unit respectively by pipeline.
In the treatment system of above-mentioned coal tar, preferably, the Shui Bao exit of described separator is provided with pump.
In the treatment system of above-mentioned coal tar, preferably, the connecting tube between light oil outlet and the described dehydration tower of described separator is provided with pump.
In the treatment system of above-mentioned coal tar, preferably, described coal tar vacuum distillation tower comprises two-stage ejector+water ring vacuum pump.
In the treatment system of above-mentioned coal tar, stock oil surge tank is for receiving the coal tar raw material coming from the outside, and be transported in the first strainer and filter through it by coal tar oil pump, in the process of pumping, can realize the pressurization for coal tar raw material, generally can be forced into 1.4MPaG.The coal tar that completes filtration at the first strainer enters First Heat Exchanger to carry out heat exchange and then enters dehydration tower and carry out processed, and the temperature that generally enters the coal tar of dehydration tower is controlled at 130 ℃.
The water of overflowing in the top of dehydration tower and light oil enter the first air cooler and carry out condensation, then enter separator and separate, and light oil can return to dehydration tower, also can be transported to fixed-bed reactor as raw material, and phenolic wastewater is sent into waste disposal plant.The coal tar that flow out dehydration tower bottom enters the second interchanger and carries out heat exchange, sends into the deep drawing processing of reducing pressure of coal tar vacuum distillation tower after coal tar stove heating (being generally heated to 390 ℃ of left and right).
This coal tar vacuum distillation tower can adopt " two-stage ejector+water ring vacuum pump " system to vacuumize, and tower top working pressure maintains 2kPa.The light oil of extracting out at this coal tar vacuum distillation tower top enters light oil mixing tank; The vacuum 1st side cut product (boiling range is 170-320 ℃) of coal tar vacuum distillation tower lateral line withdrawal function also enters light oil mixing tank to be mixed with above-mentioned light oil, and the raw material in light oil mixing tank is transported to the raw material as hydrocracking in fixed-bed reactor by light oil pump; The second line of distillation product (boiling range is 320-565 ℃) of coal tar vacuum distillation tower lateral line withdrawal function enters heavy oil mixing tank; Heavy oil fraction (boiling range is more than 565 ℃) at the bottom of tower enters the second strainer and removes by filter the particle of particle diameter >=25 μ m, and filter residue is sent into outside pitch granulation unit, and filtrate enters heavy oil mixing tank and second line of distillation Product mix.Mixture in heavy oil mixing tank is sent into raw material mixing tank by petroleum pump.
Raw material mixing tank is provided with additive entrance for receiving from outside additive, mixture in raw material mixing tank is transported to the raw material as hydrocracking in suspended-bed reactor by raw oil pump, mixes (on new hydrogen input channel, being provided with make-up hydrogen compressor) in course of conveying with the new hydrogen coming from the outside.
Raw material carries out cracking reaction after entering suspended-bed reactor, and reaction product separates in suspended-bed reactor, and gas phase enters fixed-bed reactor, and liquid product, the dregs of fat enter in vacuum distillation tower.The non-condensable gas at vacuum distillation tower top can be used as process furnace fuel, the product (dregs of fat) of vacuum distillation tower bottom can with from the filter residue of the second strainer, be mixed into outside pitch granulation unit.
Light oil, diesel oil distillate and suspension bed reaction product are carried out hydrocracking after entering fixed-bed reactor, the product of hydrocracking separates through entering fixed bed high pressure hot separator after the 3rd interchanger heat exchange, the product of fixed bed high pressure hot separator bottom is delivered to later separation part, and the product at top enters fixed bed cold high pressure separator and proceeds to separate after through the 4th interchanger heat exchange, the second air cooler condensation.Outside the sour water discharge system of separating in fixed bed cold high pressure separator, the recycle hydrogen that separation obtains enters circulating hydrogen compressor entrance and divides flow container to separate, cold high separatory enters later separation unit, and recycle hydrogen is sent in suspended-bed reactor unit and fixed-bed reactor as mixed hydrogen and quenching hydrogen through circulating hydrogen compressor.
The treatment system of the coal tar that the utility model provides can be for the coal tar oil treatment process comprising the following steps:
Coal tar is carried out to filter cleaner and remove the particle of particle diameter more than 25 microns, then send into dehydration tower and carry out processed, then send into vacuum distillation tower and carry out deep drawing processing;
The light oil that vacuum distillation tower top is extracted out mixes with the diesel oil distillate of vacuum distillation tower lateral line withdrawal function, then send into fixed-bed reactor and carry out hydrocracked, treated, or the light oil that vacuum distillation tower top is extracted out is sent into fixed-bed reactor and carried out hydrocracked, treated, the diesel oil distillate of vacuum distillation tower lateral line withdrawal function is directly sent into and carried phenol device as the raw material that extracts aldehydes matter;
The wax oil cut of vacuum distillation tower lateral line withdrawal function is sent into the raw material of floating bed hydrocracking device as hydrocracking reaction;
The heavy oil that vacuum distillation tower bottom is extracted out removes by filter the particle of particle diameter more than 25 microns, and filtrate is sent into the raw material of floating bed hydrocracking device as hydrocracking reaction, and filter residue is sent into prilling granulator and carried out granulation.
Aforesaid method mainly comprises charging filtration fraction, dehydration part and decompression deep drawing part, from the coal tar of tank field, after filter cleaner, dehydration, enters vacuum distillation tower deep drawing.
In vacuum distillation tower, vacuum residuum cut point is more than 565 ℃, the oil that extract out at vacuum distillation tower top is sent to fixed-bed reactor, vacuum distillation tower side line divides two lines to extract out, the diesel oil distillate that vacuum distillation tower side line (vacuum 1st side cut) is extracted out directly enters fixed-bed reactor and carries out hydrocracking reaction, and the filtrate that the wax oil cut that vacuum distillation tower side line (second line of distillation) is extracted out obtains after filtering with the residual oil of vacuum distillation tower bottom is mixed the raw material as floating bed hydrocracking device heat cracking reaction.
In said process, coal tar raw material takes off slag through strainer after boosting, and the coal tar after filtration enters dehydration tower dehydration through heat exchange, and dehydrated coal tar enters vacuum distillation tower and carries out deep drawing after heat exchange, process furnace heating.The light oil that vacuum distillation tower is extracted out mixes with the cut that vacuum 1st side cut is extracted out, sends into fixed-bed reactor and carries out hydrocracked, treated.Because phenol content in the cut of vacuum 1st side cut extraction is high, the diesel oil distillate of vacuum distillation tower lateral line withdrawal function can be sent into and carry phenol device as the raw material that extracts aldehydes matter.The cut that second line of distillation is extracted out can be used as the raw material of floating bed hydrocracking device.The heavy oil of extracting out at the bottom of tower contains solid particulate, and after filtering, filter residue can be mixed into granulation unit with the floating bed hydrocracking device vacuum distillation tower dregs of fat, and filtrate can be used as the raw material of floating bed hydrocracking device.
For example, the slag-containing rate of middle coalite tar raw material is about 2.29wt%, water ratio is about 8.14wt%, and after the standing dehydration in tank field, water ratio can drop to 2-4wt%, and the water ratio of the coal tar of incoming stock oily surge tank is 2-4wt%.Coal tar after standing dehydration is sent into stock oil surge tank.
In aforesaid method, before carrying out filter cleaner, more than coal tar can first be pressurized to 1.4MPaG.This pressure treatment can realize by coal tar oil pump.
Dehydration of tar can reduce the thermal load of Distallation systm, increases equipment capacity, reduces systemic resistance and falls.The dehydration of tar extensively adopting is at present to carry out in tube furnace convection zone and single vaporization device, and moisture tar is heated to 120-130 ℃ in tube furnace convection zone, enters flash-evaporation dehydration in single vaporization device.The utility model is the method that adopts light oil azeotropic continuously dehydrating: preferably, in processed, through the coal tar filtering, be heated to 130 ℃ and then enter dehydration tower, water in coal tar and light oil form azeotropic mixture and overflow from the tower top of dehydration tower, after condensing cooling, separate, phenolic wastewater enters sewage treatment unit, and strippings is back in dehydration tower, and part is sent into fixed-bed reactor and carried out hydrocracked, treated.Through processed of the present utility model, the water ratio in coal tar can be reduced to about 0.1-0.2wt%.
Coal tar can first carry out heat exchange after processed, before entering vacuum distillation tower, enters vacuum distillation tower be then heated to 390 ℃ in coal tar process furnace after.
The tower top of vacuum distillation tower can adopt " two-stage ejector+water ring vacuum pump " system to vacuumize.Tower top working pressure is 2kPa, adopts structured packing, " dry type " reduced pressure distillation technique of high efficiency low pressure drop can significantly reduce plant energy consumption.
Vacuum distillation tower can adopt dry type decompression deep drawing technology, injected water steam not in vacuum distillation tower and coal tar stove, preferably, vacuum distillation tower arranges three grades of vaccum-pumping equipments, these three grades of vaccum-pumping equipments comprise two-stage ejector and water ring vacuum pump, and the vacuum tightness of vacuum distillation tower tower top is 2kPa.Vacuum distillation tower can adopt the structured packing (for example Mellapakplus of Sulzer company) of high throughput, low pressure drop, under lower working pressure, service temperature, obtains higher product extracting rate.Although not steam blowing, make the quality product that boiling range and decompressed wax oil are suitable poor, but for the coal tar oil treatment process providing for the utility model, heavy oil will enter suspended-bed reactor and carry out further hydrocracking processing, therefore to final quality product, can't exert an influence.
In the treating processes of vacuum distillation tower, the segmentation of feed coal tar is extracted out, and flexible utilization, realizes product diversification.Because coal tar has carried out the de-slag processing of dehydration, therefore, can reduce coal tar and enter the raw material severity of floating bed hydrocracking device.
Adopt decompression deep drawing technique at the lateral line withdrawal function boiling range of vacuum distillation tower, to be equivalent to diesel oil and the wax oil cut of crude oil ordinary decompression column, this can improve the handiness of coal tar processing.
The diesel oil distillate boiling range that vacuum distillation tower side line (vacuum 1st side cut) is extracted out is 170-320 ℃, accounts for the 30-35wt% of coal tar total amount.Vacuum 1st side cut cut can directly enter fixed-bed reactor, and (light oil that can first extract out with vacuum distillation tower top mixes, and then enter fixed-bed reactor), in suspended-bed reactor, do not process, this can reduce the thermal load of reaction feed stove, reduce suspended-bed reactor, the liquid phase load of suspension bed high pressure hot separator and pressure piping, increase the treatment capacity of suspended-bed reactor, give full play to the advantage of suspended-bed reactor processing heavy oil, by the raw material that adopts treatment process of the present utility model to enter suspended-bed reactor, can reduce 28%-32%, significantly increase unit capacity, simultaneously, also the loss that can avoid light oil cracking to cause by such processing, improve product liquid yield.In above-mentioned coal tar oil treatment process, for the cut of vacuum 1st side cut, can also adopt another kind of processing scheme, be about to vacuum 1st side cut cut and send to phenol unit processed and carry out deep processing.In such cases, for meeting the processing request of downstream phenol unit processed, the light oil that extract out at vacuum distillation tower top does not merge with vacuum 1st side cut cut, it is that the carbolic oil of 170-230 ℃ and boiling range are the diesel oil distillate of 230-320 ℃ that the cut (being the diesel oil distillate of vacuum distillation tower lateral line withdrawal function) of vacuum 1st side cut can be subdivided into boiling range, carbolic oil is directly sent into and is carried phenol device as the raw material that extracts aldehydes matter, and diesel oil distillate enters in fixed-bed reactor.
The wax oil cut boiling range that vacuum distillation tower side line (second line of distillation) is extracted out is 320-565 ℃, accounts for the 50-55% of coal tar total amount.The oil of second line of distillation cut is heavier, enters suspended-bed reactor and carries out hydrocracking.Boiling range >=565 ℃ of the residue product of vacuum distillation tower bottom, account for the 15-20% of coal tar total amount.
Because coal tar dregginess is large, the preposition coarse filtration of raw material cannot eliminate slag, and the utility model filters again by the heavy oil to vacuum distillation tower bottom, can reduce into the invalid component of floating bed hydrocracking device (solid particulate is coal dust etc. do not transform component).By again removing by filter particle diameter, be greater than the solid particulate of 25 μ m, at the bottom of the tower of the vacuum distillation tower of filter residue and suspended-bed reactor, residue is mixed into pitch granulation unit, filtrate enters heavy oil surge tank with the cut of second line of distillation and mixes, then by petroleum pump, deliver to floating bed hydrogenation raw material mixing tank, in this tank, can add the additive coming from the outside, and then deliver in suspended-bed reactor by raw oil pump, in pumping procedure, can mix with the new hydrogen coming from the outside, that is: the heavy oil that extract out the wax oil cut of vacuum distillation tower lateral line withdrawal function and vacuum distillation tower bottom filters the filtrate obtaining and sends in floating bed hydrocracking device raw material mixing tank, with from outside additive, mix, and enter floating bed hydrocracking device after mixing with from the new hydrogen of outside after raw oil pump.Such processing mode can be optimized the feed composition of slurry-bed hydrocracking device.By the reasonable utilization to sideline product, optimize the charging of slurry-bed hydrocracking device, can improve suspended-bed reactor utilization ratio, increase the handiness of floating bed hydrocracking device.
Slurry-bed hydrocracking device is three-phase fluid bed reactor.In three-phase fluid bed reactor, the liquid that the fluidisation of solid particulate is mainly upwards flow through is to particle surface frictional force, thereby generation is to particle drag force upwards.By the distribution of underpressure distillation, make to increase into heavy constituent ratio in suspended-bed reactor material, liquid phase content increases, and improves bed fluidization situation.Can overcome the problems such as in suspended-bed reactor, the reaction medium residence time is long, cracking reaction is excessive simultaneously.
Reaction process in suspended-bed reactor and fixed-bed reactor etc. all can carry out in a conventional manner, and follow-up reaction process also can carry out in a conventional manner, does not change, and maintains existing procedure.
The treatment system of coal tar provided by the utility model is processed the product diversification of the comprehensive utilization that can make coal tar to coal tar, more can meeting the market requirement.
While adopting the treatment system of coal tar provided by the utility model to carry out coal tar oil handling, can reduce the reactant (reducing without the following component of the diesel oil that enters suspension bed) into suspended-bed reactor, also can reduce the solid particulate not transforming, that is to say and adopt treatment system of the present utility model, suspended-bed reactor can be processed more coal tar, improves utilization ratio of device; Vacuum 1st side cut and tower top light oil that coal tar vacuum distillation tower is extracted out can directly enter fixed bed reaction, thereby avoid light oil to be cracked into dry gas at suspended-bed reactor, improve the liquid yield of product.
Accompanying drawing explanation
The following drawings is only intended to the utility model to schematically illustrate and explain, does not limit scope of the present utility model.Wherein:
Fig. 1 is the process flow sheet of prior art;
The structural representation of the treatment system of the coal tar that Fig. 2 provides for embodiment 1.
Main drawing reference numeral explanation:
A buffer tank the raw oil, coal tar pump 2, a first filter 3, a first heat exchanger 4, the dehydration column 5 of the first air cooler 6, separator 7, the first two heat exchangers 8, 9 furnace feed coal tar, coal tar vacuum tower, 10 mixing tank 11 the gas oil, light oil pump 12, and heavy oil mixing tank 13, pump 14 weight , the second filter 15, the raw material mixing tank 16, the raw material pump 17, and new hydrogen compressors 18, suspended bed cracking reactor 19-1, 19-2 hot high pressure separator , hot low pressure separator 19-3, 19-4 cold low pressure separator, the fixed bed reactor 20, vacuum tower 21, a third heat exchanger 22, the fixed bed heat high pressure separator 23, the fourth heat exchanger 24, the second air cooler 25, a fixed-bed cold high pressure separator 26,,, recycle hydrogen compressor inlet of the tank 27,,, recycle hydrogen compressor 28 top outlet 10A,,, less pumping line outlet 10B,,, by second extraction port 10C,,, pumping the bottoms outlet 10D
Embodiment
For technical characterictic of the present utility model, object and beneficial effect being had more clearly, understand, referring now to Figure of description, the technical solution of the utility model is carried out to following detailed description, but can not be interpreted as restriction that can practical range of the present utility model.
Embodiment 1
The present embodiment provides a kind for the treatment of system of coal tar, and its structure as shown in Figure 2.
The treatment system of this coal tar comprises: stock oil surge tank 1, coal tar oil pump 2, the first strainer 3, First Heat Exchanger 4, dehydration tower 5, the first air cooler 6, separator 7, the second interchanger 8, coal tar stove 9, coal tar vacuum distillation tower 10, light oil mixing tank 11, light oil pump 12, heavy oil mixing tank 13, petroleum pump 14, the second strainer 15, raw material mixing tank 16, raw oil pump 17, make-up hydrogen compressor 18, suspended-bed reactor unit, fixed-bed reactor 20, vacuum distillation tower 21, the 3rd interchanger 22, fixed bed high pressure hot separator 23, the 4th interchanger 24, the second air cooler 25, fixed bed cold high pressure separator 26, circulating hydrogen compressor entrance divides flow container 27, circulating hydrogen compressor 28, suspended-bed reactor unit comprises suspension bed cracking case 19-1, high pressure hot separator 19-2, thermal low-pressure separators 19-3, cold low separator 19-4, wherein:
Stock oil surge tank 1 is provided with the stock oil entrance for inputting feed coal tar, and its outlet is connected by pipeline with the entrance of the first strainer 3, and the connecting tube of the two is provided with coal tar oil pump 2;
The outlet of the first strainer 3 is connected to the entrance of dehydration tower 5 by pipeline, the connecting tube of the two is provided with First Heat Exchanger 4;
The top exit of dehydration tower 5 is connected with the entrance of the first air cooler 6 by pipeline, its outlet at bottom is connected with the entrance of coal tar stove 9 by pipeline, and the connecting tube between dehydration tower 5 outlet at bottoms and the entrance of coal tar stove 9 is provided with the second interchanger 8;
The outlet of the first air cooler 6 is connected with the entrance of separator 7 by pipeline;
Separator 7 is provided with light oil outlet and water contracts out mouth, and light oil outlet is connected to dehydration tower 5, fixed-bed reactor 20 by pipeline, and water contracts out mouth for discharging the moisture of separation;
The outlet of coal tar stove 9 is connected with the entrance of coal tar vacuum distillation tower 10 by pipeline;
Coal tar vacuum distillation tower 10 is provided with top exit 10A, vacuum 1st side cut is extracted a mouthful 10D out at the bottom of extracting a mouthful 10B, second line of distillation extraction mouthful 10C and tower out, top exit 10A is connected with the entrance of light oil mixing tank 11 by pipeline, vacuum 1st side cut is extracted mouthful 10B out for extracting diesel oil distillate out and being connected with the entrance of light oil mixing tank 11 by pipeline, second line of distillation is extracted mouthful 10C out for extracting wax oil out and being connected with the entrance of heavy oil mixing tank 13 by pipeline, extracts a mouthful 10D out and be connected with the entrance of the second strainer 15 by pipeline at the bottom of tower;
Light oil mixing tank 11 is connected with the entrance of fixed-bed reactor 20 by pipeline, and the connecting tube between the two is provided with light oil pump 12;
Heavy oil mixing tank 13 is connected with the entrance of raw material mixing tank 16 by pipeline, and the connecting tube between the two is provided with petroleum pump 14;
Raw material mixing tank 16 is provided with additive entrance for inputting additive, its outlet is connected with the bottom inlet of suspension bed cracking case 19-1 by pipeline, and this pipeline is provided with raw oil pump 17 and is connected with new hydrogen input channel, new hydrogen input channel is provided with make-up hydrogen compressor 18;
The filtrate outlet of the second strainer 15 is connected with the entrance of heavy oil mixing tank 13 by pipeline;
The top exit of suspension bed cracking case 19-1 is connected with the entrance of high pressure hot separator 19-2, the top exit of high pressure hot separator 19-2 is connected with the entrance of fixed-bed reactor 20 by pipeline, the outlet at bottom of high pressure hot separator 19-2 is connected with the entrance of thermal low-pressure separators 19-3, the top exit of thermal low-pressure separators 19-3 is connected with the entrance of cold low separator 19-4, the outlet at bottom of thermal low-pressure separators 19-3 is connected with the entrance of vacuum distillation tower 21, and the outlet at bottom of cold low separator 19-4 is connected with the entrance of vacuum distillation tower 21 by pipeline;
The outlet at bottom of fixed-bed reactor 20 is connected with the entrance of fixed bed high pressure hot separator 23 by pipeline, and the connecting tube between the two is provided with the 3rd interchanger 22;
Vacuum distillation tower 21 is provided with top exit and outlet at bottom;
The top exit of fixed bed high pressure hot separator 23 is connected with the entrance of fixed bed cold high pressure separator 26 by pipeline, and the connecting tube of the two is provided with the 4th interchanger 24 and the second air cooler 25, and it is also provided with outlet at bottom;
The top exit of fixed bed cold high pressure separator 26 divides the entrance of flow container 27 to be connected with circulating hydrogen compressor entrance, and it is also provided with two outlet at bottoms;
Circulating hydrogen compressor entrance divides the top exit of flow container 27 to be connected with the entrance of circulating hydrogen compressor 28, and it is also provided with outlet at bottom;
The outlet of circulating hydrogen compressor 28 is connected with fixed-bed reactor 20, suspension bed cracking case 19-1 respectively by pipeline.
The treatment system of the coal tar that the present embodiment provides can be for the coal tar oil treatment process comprising the following steps:
In mass rate input stock oil surge tank 1 by the coal tar from tank field with 75t/h, then utilize coal tar oil pump 2 that coal tar raw material is transported in the first strainer 3 and is filtered, in pumping procedure by the pressure improvement value 1.4MPaG of coal tar;
The first strainer 3 is removed the solid particulate of the particle diameter >=25 μ m in coal tar, then coal tar enters First Heat Exchanger 4, the temperature of coal tar rises to 130 ℃, enter dehydration tower 5 and remove most water, the water ratio of tower ground coal tar is about 0.1%, moisture leaves and takes out of a small amount of light oil from the top of dehydration tower 5, through after the first air cooler 6 condensations, enter in separator 7, in separator 7, moisture is Fen Li with light oil, strippings is back in dehydration tower 5, part enters the raw material of fixed-bed reactor 20 as hydrocracking, phenolic wastewater is sent into Sewage treatment systems,
Coal tar after dehydration leaves by dehydration tower 5 bottoms, enters the second interchanger 8 and carries out heat exchange, then enters coal tar stove 9 and is heated to 390 ℃, enters afterwards coal tar vacuum distillation tower 10;
In coal tar vacuum distillation tower 10 towers, adopt high efficiency low pressure drop filler, the vacuum degree control at top is 2kPa, and coal tar vacuum distillation tower 10 is extracted out light oil distillate and entered light oil mixing tank 11 by top exit 10A; Coal tar vacuum distillation tower 10 is established two side lines, by vacuum 1st side cut, extract mouthful 10B out and extract vacuum 1st side cut product (boiling range is the diesel oil distillate of 170-320 ℃) out, vacuum 1st side cut product introduction light oil mixing tank 11 mixes with the light oil that extract out at coal tar vacuum distillation tower 10 tops, then by light oil pump 12, be transported to the raw material as hydrocracking in fixed-bed reactor 20, mass rate during conveying is 21.8t/h, and medium temperature is 108 ℃; By second line of distillation, extract mouthful 10C out and extract second line of distillation product (boiling range is the wax oil cut of 320-565 ℃) out, second line of distillation product input heavy oil mixing tank 13, its mass rate is 38.9t/h, medium temperature is 227 ℃; By extracting mouthful 10D at the bottom of tower out, discharge residual oil, its mass rate is 13.6t/h, and medium temperature is 374 ℃; Residual oil enters the second strainer 15 and removes by filter the solid particulate of particle diameter >=25 μ m, and filtrate enters heavy oil mixing tank 13 and second line of distillation Product mix, and filter residue is delivered to the pitch granulation unit of system outside;
Second line of distillation product in heavy oil mixing tank 13 and the mixture of filtrate are transported in raw material mixing tank 16 by petroleum pump 14, and raw material mixing tank 16 is inputted from outside additive by additive input tube, and it is mixed with said mixture;
Material in raw material mixing tank 16 is transported to the raw material as cracking reaction in suspension bed cracking case 19-1 by raw oil pump 17, and by the new hydrogen from outside of new hydrogen input channel input, mixes in course of conveying with by make-up hydrogen compressor 18;
The reaction product of suspension bed cracking case 19-1 is after separation system separates, and gas-phase product enters in fixed-bed reactor 20 and participates in reaction, and the liquid product of its bottom enters vacuum distillation tower 21 and separates;
Non-condensable gases are discharged at vacuum distillation tower 21 tops, and non-condensable gas can be used as process furnace fuel, and residues are discharged in vacuum distillation tower 21 bottoms, deliver to the pitch granulation unit of system outside together with after the filter residue of this part residue and the second strainer 15 mixes;
The product of fixed-bed reactor 20 is left by tower bottom outlet, after the 3rd interchanger 22 heat exchange, entering fixed bed high pressure hot separator 23 separates, the high separatory of heat that outlet at bottom is discharged is delivered to follow-up tripping device, the hot high score gas in top separates through entering fixed bed cold high pressure separator 28 after the 4th interchanger 24, the second air cooler 25, discharge sour water and cold high score oil, the recycle hydrogen that separation obtains enters circulating hydrogen compressor entrance and divides flow container 27;
The recycle hydrogen that separation obtains by circulating hydrogen compressor 28 and be transported to fixed-bed reactor 20 and suspended-bed reactor unit as mixed hydrogen and quenching hydrogen, in circulating hydrogen compressor 28, establish recycle hydrogen and divide flow container, lime set is collected and discharged, avoid into compressor gas band liquid.
By adopting the coal tar oil treatment process of the present embodiment, can reduce the reaction feed of suspended-bed reactor nearly 30%, optimized the charging of floating bed hydrocracking device, also reduced the solid particulate not transforming, and, can obtain more product, realize the comprehensive utilization of coal tar.Vacuum 1st side cut and tower top light oil that coal tar vacuum distillation tower is extracted out can directly enter fixed bed reaction, have avoided light oil to be cracked into dry gas at suspended-bed reactor, have improved the liquid yield of product.
Claims (4)
1. the treatment system of a coal tar, it is characterized in that, the treatment system of this coal tar comprises: stock oil surge tank, coal tar oil pump, the first strainer, First Heat Exchanger, dehydration tower, the first air cooler, separator, the second interchanger, coal tar stove, coal tar vacuum distillation tower, light oil mixing tank, light oil pump, heavy oil mixing tank, petroleum pump, the second strainer, raw material mixing tank, raw oil pump, make-up hydrogen compressor, suspended-bed reactor unit, fixed-bed reactor, vacuum distillation tower, fixed bed high pressure hot separator, the 3rd interchanger, fixed bed cold high pressure separator, the 4th interchanger, the second air cooler, circulating hydrogen compressor, circulating hydrogen compressor entrance divides flow container, described suspended-bed reactor unit comprises suspension bed cracking case, high pressure hot separator, thermal low-pressure separators and cold low separator, wherein:
Described stock oil surge tank is provided with the stock oil entrance for inputting feed coal tar, and its outlet is connected by pipeline with the entrance of the first strainer, and the connecting tube of the two is provided with coal tar oil pump;
The outlet of described the first strainer is connected to the entrance of described dehydration tower by pipeline, the connecting tube of the two is provided with First Heat Exchanger;
The top exit of described dehydration tower is connected with the entrance of the first air cooler by pipeline, its outlet at bottom is connected with the entrance of described coal tar stove by pipeline, and the connecting tube between described dehydration tower outlet at bottom and the entrance of described coal tar stove is provided with the second interchanger;
The outlet of described the first air cooler is connected with the entrance of described separator by pipeline;
Described separator is provided with light oil outlet and water contracts out mouth, and described light oil outlet is connected to described dehydration tower and fixed-bed reactor by pipeline, and described water contracts out mouth for discharging the moisture of separation;
The outlet of described coal tar stove is connected with the entrance of described coal tar vacuum distillation tower by pipeline;
Described coal tar vacuum distillation tower is extracted mouth out at the bottom of being provided with top exit, vacuum 1st side cut extraction mouth, second line of distillation extraction mouth and tower, described top exit is connected with the entrance of described light oil mixing tank by pipeline, described vacuum 1st side cut is extracted mouth out for extracting light oil out and being connected with the entrance of described light oil mixing tank by pipeline, described second line of distillation is extracted mouth out for extracting wax oil out and being connected with the entrance of described heavy oil mixing tank by pipeline, extracts mouth out and be connected with the entrance of described the second strainer by pipeline at the bottom of described tower;
Described light oil mixing tank is connected with the entrance of described fixed-bed reactor by pipeline, and the connecting tube between the two is provided with light oil pump;
Described heavy oil mixing tank is connected with the entrance of described raw material mixing tank by pipeline, and the connecting tube between the two is provided with petroleum pump;
Described raw material mixing tank is provided with additive entrance for inputting additive, its outlet is connected with the bottom inlet of the suspension bed cracking case of described suspended-bed reactor unit by pipeline, and this pipeline is provided with raw oil pump and is connected with new hydrogen input channel, new hydrogen input channel is provided with make-up hydrogen compressor;
The filtrate outlet of described the second strainer is connected with the entrance of described heavy oil mixing tank by pipeline;
The top exit of suspension bed cracking case and the entrance of described high pressure hot separator of described suspended-bed reactor unit are connected, the top exit of described high pressure hot separator is connected with the entrance of described fixed-bed reactor by pipeline, the outlet at bottom of described high pressure hot separator is connected with the entrance of described thermal low-pressure separators, the top exit of described thermal low-pressure separators is connected with the entrance of described cold low separator, the outlet at bottom of described thermal low-pressure separators is connected with the entrance of described vacuum distillation tower, the outlet at bottom of described cold low separator is connected with the entrance of described vacuum distillation tower by pipeline,
The outlet at bottom of described fixed-bed reactor is connected with the entrance of described fixed bed high pressure hot separator by pipeline, and the connecting tube between the two is provided with the 3rd interchanger;
Described vacuum distillation tower is provided with top exit and outlet at bottom;
The top exit of described fixed bed high pressure hot separator is connected with the entrance of described fixed bed cold high pressure separator by pipeline, and the connecting tube of the two is provided with the 4th interchanger and the second air cooler, and it is also provided with outlet at bottom;
The top exit of described fixed bed cold high pressure separator divides the entrance of flow container to be connected with described circulating hydrogen compressor entrance, and it is also provided with two outlet at bottoms;
Described circulating hydrogen compressor entrance divides the top exit of flow container and the entrance of described circulating hydrogen compressor to be connected, and it is also provided with outlet at bottom;
The outlet of described circulating hydrogen compressor is connected with the suspension bed cracking case of described fixed-bed reactor, described suspended-bed reactor unit respectively by pipeline.
2. the treatment system of coal tar according to claim 1, is characterized in that, the Shui Bao exit of described separator is provided with pump.
3. the treatment system of coal tar according to claim 1, is characterized in that, the connecting tube between light oil outlet and the described dehydration tower of described separator is provided with pump.
4. the treatment system of coal tar according to claim 1, is characterized in that, described coal tar vacuum distillation tower comprises two-stage ejector+water ring vacuum pump.
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| CN201320600022.2U CN203559012U (en) | 2013-09-25 | 2013-09-25 | Coal tar treatment system |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103484159A (en) * | 2013-09-25 | 2014-01-01 | 北京石油化工工程有限公司 | Matching technology method for optimizing feeding of coal tar suspended bed hydrocracker |
| CN106566572A (en) * | 2016-11-07 | 2017-04-19 | 中国石油大学(华东) | Process for producing high-softening-point gilsonite from coal tar heavy oil through vacuum deep extraction |
| CN110872530A (en) * | 2018-09-04 | 2020-03-10 | 武汉金中石化工程有限公司 | Coal tar pretreatment method and system |
| CN113897210A (en) * | 2021-10-26 | 2022-01-07 | 山东汇邦新材料有限公司 | External separation system of suspension bed and use method thereof |
-
2013
- 2013-09-25 CN CN201320600022.2U patent/CN203559012U/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103484159A (en) * | 2013-09-25 | 2014-01-01 | 北京石油化工工程有限公司 | Matching technology method for optimizing feeding of coal tar suspended bed hydrocracker |
| CN103484159B (en) * | 2013-09-25 | 2015-06-24 | 北京石油化工工程有限公司 | Matching technology method for optimizing feeding of coal tar suspended bed hydrocracker |
| CN106566572A (en) * | 2016-11-07 | 2017-04-19 | 中国石油大学(华东) | Process for producing high-softening-point gilsonite from coal tar heavy oil through vacuum deep extraction |
| CN110872530A (en) * | 2018-09-04 | 2020-03-10 | 武汉金中石化工程有限公司 | Coal tar pretreatment method and system |
| CN113897210A (en) * | 2021-10-26 | 2022-01-07 | 山东汇邦新材料有限公司 | External separation system of suspension bed and use method thereof |
| CN113897210B (en) * | 2021-10-26 | 2023-12-26 | 山东汇邦新材料有限公司 | External separation system of suspension bed and application method thereof |
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