CN105754644A - Coal tar treatment system - Google Patents
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- CN105754644A CN105754644A CN201410780836.8A CN201410780836A CN105754644A CN 105754644 A CN105754644 A CN 105754644A CN 201410780836 A CN201410780836 A CN 201410780836A CN 105754644 A CN105754644 A CN 105754644A
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Abstract
The invention 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 dehydration tower, a first air cooler, a separator, a second heat exchanger, a coal tar charging furnace, a coal tar pressure reduction tower, a light oil blending tank, a light oil pump, a heavy oil blending tank, a heavy oil pump, a second filter, a raw material blending tank, a raw material oil pump, a make-up hydrogen compressor, a suspended-bed reactor unit, a fixed bed reactor, a pressure reduction tower, a fixed bed hot high pressure separator, a third heat exchanger, a fixed bad cold high pressure separator, a forth heat exchanger, a second air cooler, a circulating hydrogen compressor and a circulating hydrogen compressor inlet liquid separator pot. The suspended-bed reactor unit comprises a suspended-bed cracker, a hot high pressure separator, a hot low pressure separator and a cold low pressure separator. The coal tar treatment system realizes treatment on coal tar and coal tar integrated utilization product diversification and adapts to market demands.
Description
Technical field
The present invention relates to a kind of coal tar oil handling system, belong to Coal Chemical Industry and technical field of petrochemical industry.
Background technology
Coal tar is the side-product of pyrolysis of coal coke, occupies certain share in coal production.Currently, China produces tar per year and is about 9,000,000 tons, but actual working ability is only 3,000,000 tons.Owing to coke downstream chemical industry falls behind the restriction of technology, the coal tar of substantial amounts is difficult to utilize.
The traditional diamond-making technique of coal tar, with physical separation, extraction one pack system or narrow component product for target, refines washing oil, light oil, carbolineum, crude naphthalene, crude phenols and Colophonium inferior from coal tar.Due to coal tar complicated components, high added value constituent content is low, and the low value-added component that content is high is difficult by, 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 to directly utilize or discarded, not only reduce resource value but also severe contamination environment.
Floating bed hydrocracking Technology originates from German Bergius-Pier coal liquefaction technology in 1913, this technology as far back as last century the '20s just achieve industrial applications in Germany.During 1927-1943, this technology is used to overlap Direct coal liquefaction device in Germany's construction successful operation 12.This technology is adopted to produce high-quality cleaning fuel, it is achieved the increment of tar resource utilizes, and economic benefit is good.Floating bed hydrogenation floating bed hydrocracking technology, processes (LPH) containing liquid-phase hydrogenatin and gas phase hydrogenation processes (GPH) two processes.Its principle is.
(1) raw material enters suspended-bed reactor after mixing with additive and hydrogen, there is heat cracking reaction, and it is hydrogenated with saturated under high-pressure hydro state, wherein, in charging there is thermal cracking and be hydrogenated with saturated process in carbon residue, colloid, asphalitine under specific Additive, is substantially free of the generation of coke.
(2) product of suspension bed thermal cracking enters in high pressure hot separator and separates, and the gaseous product of cleaning goes fixed bed reactors in hydrogenation cracking and hydrofinishing further, produces Petroleum and the light diesel fuel of high-quality；Isolated solid matter is mainly coke, pelletize can work as Colophonium or coal-fired use.
At present, existing suspended bed device hydrogen addition technology flow process (as shown in Figure 1) is: full fraction coal tar is after High pressure feeding pump boosts, mix with additive, hydrogen, by two high pressure heat exchangers, a reaction feed heating furnace heating to uniform temperature, enter floating bed hydrogenation reactor.Suspended-bed reactor product separates in high pressure hot separator, and gas phase enters fixed bed reactors, and liquid phase (containing solid particle) enters decompression distillation system.Fixed bed reactors occur cracking refining reaction, after later separation, produces qualified products.In this flow process, full fraction of coal tar is directly entered floating bed hydrogenation device.Experimental study according to coal tar is reported, coal tar gently holds fraction (boiling range is 170-230 DEG C) it is proposed that phenolic compound, fully enters floating bed hydrogenation device, then coal tar comprehensive utilization rate variance.Light oil is directly entered floating bed hydrogenation reactor, adds the load of floating bed hydrogenation reactor, and light oil cracking becomes dry gas simultaneously, reduces product liquid yield.In coal tar, solids content is many, it does not have being directly entered floating bed hydrogenation device through reasonably de-slag operation, raw material severity is high.
Summary of the invention
For solving above-mentioned technical problem, it is an object of the invention to provide a kind of coal tar oil handling system, adopt this system that coal tar is filtered, dehydration, the pretreatment such as deep vacuum distillation process, various components are respectively processed, the product diversification of the comprehensive utilization of coal tar can be made, more adapt to the demand in market.
nullFor reaching above-mentioned purpose，The invention provides a kind of coal tar oil handling system，It is characterized in that，This coal tar oil handling system includes: raw oil surge tank、Coal tar oil pump、First filter、First Heat Exchanger、Dehydrating tower、First air cooler、Separator、Second heat exchanger、Coal tar stove、Coal tar vacuum tower、Light oil blending tank、Light oil pump、Heavy oil blending tank、Petroleum pump、Second filter、Raw material blending tank、Raw oil pump、Make-up hydrogen compressor、Suspended-bed reactor unit、Fixed bed reactors、Vacuum tower、Fixing bed high pressure hot separator、3rd heat exchanger、Fixing bed cold high pressure separator、4th heat exchanger、Second air cooler、Circulating hydrogen compressor、Circulating hydrogen compressor entrance separatory tank，Described suspended-bed reactor unit includes suspension bed cracker、High pressure hot separator、Thermal low-pressure separators and cold low separator，Wherein.
Described raw oil surge tank is provided with the raw oil entrance for inputting feed coal tar, and its outlet is connected by pipeline with the entrance of the first filter, and the connection pipeline of the two is provided with coal tar oil pump.
The outlet of described first filter is connected to the entrance of described dehydrating tower by pipeline, and the connection pipeline of the two is provided with First Heat Exchanger.
The top exit of described dehydrating tower is connected by the entrance of pipeline and the first air cooler, its outlet at bottom is connected with the entrance of described coal tar stove by pipeline, further, the connection pipeline between the entrance of described dehydrating tower outlet at bottom and described coal tar stove is provided with the second heat exchanger.
The outlet of described first air cooler is connected by the entrance of pipeline with described separator.
Described separator is provided with light oil outlet and the outlet of water bag, and the outlet of described light oil is connected to described dehydrating tower and fixed bed reactors by pipeline, and the outlet of described water bag is for discharging the moisture of separation.
The outlet of described coal tar stove is connected by the entrance of pipeline with described coal tar vacuum tower.
Described coal tar vacuum tower is provided with outlet port at the bottom of top exit, vacuum 1st side cut outlet port, second line of distillation outlet port and tower, described top exit is connected with the entrance of described light oil blending tank by pipeline, described vacuum 1st side cut outlet port is for extracting light oil out and being connected with the entrance of described light oil blending tank by pipeline, described second line of distillation outlet port is for extracting wax oil out and being connected with the entrance of described heavy oil blending tank by pipeline, and outlet port at the bottom of described tower is connected with the entrance of described second filter by pipeline.
Described light oil blending tank is connected with the entrance of described fixed bed reactors by pipeline, and connection pipeline therebetween is provided with light oil pump.
Described heavy oil blending tank is connected with the entrance of described raw material blending tank by pipeline, and connection pipeline therebetween is provided with petroleum pump.
Described raw material blending tank is provided with additive entrance for inputting additive, its outlet is connected by the bottom inlet of pipeline with the suspension bed cracker of described suspended-bed reactor unit, and this pipeline is provided with raw oil pump and is connected to new hydrogen input channel, and new hydrogen input channel is provided with make-up hydrogen compressor.
The filtrate (liquid of described second filter is connected with the entrance of described heavy oil blending tank by pipeline.
The top exit of the suspension bed cracker of described suspended-bed reactor unit is connected with the entrance of described high pressure hot separator, the top exit of described high pressure hot separator is connected with the entrance of described fixed bed reactors 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 tower, the outlet at bottom of described thermal low-pressure separators is connected with the entrance of described vacuum tower by pipeline.
The outlet at bottom of described fixed bed reactors is connected with the entrance of described fixing bed high pressure hot separator by pipeline, and connection pipeline therebetween is provided with the 3rd heat exchanger.
Described vacuum tower is provided with top exit and outlet at bottom.
The top exit of described fixing bed high pressure hot separator is connected with the entrance of described fixing bed cold high pressure separator by pipeline, and the connection pipeline of the two is provided with the 4th heat exchanger and the second air cooler, and it is additionally provided with outlet at bottom.
The top exit of described fixing bed cold high pressure separator is connected with the entrance of described circulating hydrogen compressor entrance separatory tank, and it is additionally provided with two outlet at bottoms.
The top exit of described circulating hydrogen compressor entrance separatory tank is connected with the entrance of described circulating hydrogen compressor, and it is additionally provided with outlet at bottom.
The outlet of described circulating hydrogen compressor is connected with the suspension bed cracker of described fixed bed reactors, described suspended-bed reactor unit respectively by pipeline.
In above-mentioned coal tar oil handling system, it is preferable that the Shui Bao exit of described separator is provided with pump.
In above-mentioned coal tar oil handling system, it is preferable that the connection pipeline between light oil outlet and the described dehydrating tower of described separator is provided with pump.
In above-mentioned coal tar oil handling system, it is preferable that described coal tar vacuum tower includes two-stage ejector+water ring vacuum pump.
In above-mentioned coal tar oil handling system, raw oil surge tank is for receiving from extraneous coal tar raw material, and be transported in the first filter through it be filtered by coal tar oil pump, the pressurization for coal tar raw material can be realized in the process of pumping, generally can be forced into 1.4MPaG.The coal tar completing to filter at the first filter enters First Heat Exchanger to carry out heat exchange and carries out processed subsequently into dehydrating tower, and the temperature generally entering the coal tar of dehydrating tower controls at 130 DEG C.
Water and the light oil of the top effusion of dehydrating tower enter the first air cooler and condense, and are easily separated subsequently into separator, and light oil can return dehydrating tower, it is also possible to being transported to fixed bed reactors as raw material, phenol wastewater sends into sewage-treatment plant.The coal tar flowed out bottom dehydrating tower enters the second heat exchanger and carries out heat exchange, heats feeding coal tar vacuum tower after (generally heating to about 390 DEG C) through coal tar stove and carries out deep vacuum distillation process.
This coal tar vacuum tower can adopt " two-stage ejector+water ring vacuum pump " system evacuation, and tower top operation pressure maintains 2kPa.The light oil extracted out at this coal tar vacuum tower top enters light oil blending tank；The vacuum 1st side cut product (boiling range is 170-320 DEG C) of coal tar vacuum tower lateral line withdrawal function mixes with above-mentioned light oil also into light oil blending tank, and the raw material in light oil blending tank is transported in fixed bed reactors as the raw material being hydrogenated with cracking by light oil pump；The second line of distillation product (boiling range is 320-565 DEG C) of coal tar vacuum tower lateral line withdrawal function enters heavy oil blending tank；Heavy oil fraction (boiling range is more than 565 DEG C) at the bottom of tower enters the second filter and is filtered to remove the granule of particle diameter >=25 μm, and filtering residue sends into outside Colophonium pelletizing unit, and filtrate enters heavy oil blending tank and second line of distillation Product mix.Mixture in heavy oil blending tank sends into raw material blending tank by petroleum pump.
Raw material blending tank is provided with additive entrance for receiving from outside additive, mixture in raw material blending tank is transported in suspended-bed reactor as the raw material being hydrogenated with cracking by raw oil pump, mixes (being provided with make-up hydrogen compressor on new hydrogen input channel) with from extraneous new hydrogen in course of conveying.
Raw material carries out cracking reaction after entering suspended-bed reactor, and product is easily separated in suspended-bed reactor, and gas phase enters fixed bed reactors, and liquid product, the dregs of fat then enter in vacuum tower.The fixed gas at vacuum tower top can as furnace fuel, and the product (dregs of fat) of vacuum tower bottoms can be mixed into outside Colophonium pelletizing unit with the filtering residue from the second filter.
Light oil, diesel oil distillate and suspension bed product carry out hydrogenation cracking after entering fixed bed reactors, the product of hydrogenation cracking enters fixing bed high pressure hot separator after the 3rd heat exchanger heat exchange and is easily separated, product bottom fixing bed high pressure hot separator delivers to later separation part, and the product at top then proceeds to separate at the fixing bed cold high pressure separator of entrance after the 4th heat exchanger heat exchange, the second air cooler condensation.Outside the acid water discharge system separated in fixing bed cold high pressure separator, separate the recycle hydrogen entrance circulating hydrogen compressor entrance separatory tank obtained to be easily separated, cold high separatory enters later separation unit, and recycle hydrogen is sent in suspended-bed reactor unit and fixed bed reactors as mixed hydrogen and quenching hydrogen through circulating hydrogen compressor.
Coal tar oil handling system provided by the invention may be used for the coal tar oil treatment process comprised the following steps.
Coal tar is filtered slagging-off and removes particle diameter granule more than 25 microns, be re-fed into dehydrating tower and carry out processed, be then fed into vacuum tower and carry out deep drawing process.
The light oil that vacuum tower top is extracted out is mixed with the diesel oil distillate of vacuum tower lateral line withdrawal function, it is then fed into fixed bed reactors and carries out hydrocracked, treated, or the light oil extracted out at vacuum tower top is sent into fixed bed reactors and is carried out hydrocracked, treated, and the diesel oil distillate of vacuum tower lateral line withdrawal function is sent directly into the raw material carrying phenol device as extraction aldehydes matter.
The wax oil fraction of vacuum tower lateral line withdrawal function is sent into the floating bed hydrocracking device raw material as hydrocracking reaction.
The heavy oil that vacuum tower bottoms is extracted out is filtered removing particle diameter granule more than 25 microns, and filtrate is sent into outstanding
Floating bed hydrocracking unit is as the raw material of hydrocracking reaction, and filtering residue is sent into prilling granulator and carried out pelletize.
Said method mainly includes fed filtration part, dewatering part and deep vacuum distillation part, and the coal tar from tank field enters vacuum tower deep drawing after filter cleaner, dehydration.
In vacuum tower, decompression residuum cut point is more than 565 DEG C, fixed bed reactors sent to by the oil that vacuum tower top is extracted out, vacuum tower side line divides two lines to extract out, the diesel oil distillate that vacuum tower side line (vacuum 1st side cut) is extracted out is directly entered fixed bed reactors and carries out hydrocracking reaction, and the filtrate that the wax oil fraction that vacuum tower side line (second line of distillation) is extracted out obtains after filtering with the residual oil of vacuum tower bottoms mixes the raw material as floating bed hydrocracking device heat cracking reaction.
In above process, through the de-slag of filter after coal tar raw material boosting, the coal tar after filtration enters dehydrating tower dehydration through heat exchange, and dehydrated coal tar enters vacuum tower after heat exchange, heating furnace heating and carries out deep drawing.The fraction that the light oil that vacuum tower is extracted out is extracted out with vacuum 1st side cut mixes, and sends into fixed bed reactors and carries out hydrocracked, treated.Owing in the fraction that vacuum 1st side cut is extracted out, phenol content is high, the diesel oil distillate of vacuum tower lateral line withdrawal function can be sent into the raw material carrying phenol device as extraction aldehydes matter.The fraction that second line of distillation is extracted out can as the raw material of floating bed hydrocracking device.The heavy oil extracted out at the bottom of tower contains solid particle, and after filtering, filtering residue can be mixed into pelletizing unit with the floating bed hydrocracking device vacuum tower dregs of fat, and filtrate can 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%, moisture content is about 8.14wt%, and after tank field stands dehydration, moisture content can descend to 2-4wt%, and the moisture content of the coal tar namely entering raw oil surge tank is 2-4wt%.Stand the coal tar after dehydration and send into raw oil surge tank.
In the above-mentioned methods, before being filtered slagging-off, coal tar can first be pressurized to more than 1.4MPaG.This pressurized treatments can be realized by coal tar oil pump.
Dehydration of tar can reduce the thermic load of Distallation systm, increases equipment capacity, reduces SR and drops.Dehydration of tar widely used at present is to carry out in tube furnace convection section and flush distillation device, and moisture tar heats to 120-130 DEG C in tube furnace convection section, enters flash-evaporation dehydration in flush distillation device.The present invention is then the method adopting light oil azeotropic continuous dehydration: preferably, in processed, coal tar through filtering is heated to 130 DEG C subsequently into dehydrating tower, water and light oil in coal tar form azeotropic mixture and overflow from the tower top of dehydrating tower, it is easily separated after condensed cooling, phenol wastewater enters sewage treatment unit, and strippings is back in dehydrating tower, and part is sent into fixed bed reactors and carried out hydrocracked, treated.Through the processed of the present invention, the moisture content in coal tar can be reduced to about 0.1-0.2wt%.
Coal tar after processed, enter before vacuum tower and can first carry out heat exchange, enter vacuum tower after being then heated to 390 DEG C in coal tar heating furnace.
The tower top of vacuum tower can adopt " two-stage ejector+water ring vacuum pump " system evacuation.Tower top operation pressure is 2kPa, adopts the structured packing of high efficiency low pressure drop, " dry type " reduced pressure distillation technique that plant energy consumption can be greatly reduced.
Vacuum tower can adopt dry type deep vacuum distillation technology, it is not injected into water vapour, it is preferable that vacuum tower arranges three grades of vaccum-pumping equipments in vacuum tower and coal tar stove, these three grades of vaccum-pumping equipments include two-stage ejector and water ring vacuum pump, and the vacuum of vacuum tower tower top is 2kPa.Vacuum tower can adopt the structured packing (such as the Mellapakplus of Sulzer company) of high throughput, low pressure drop, at relatively low operation pressure, operation temperature, it is thus achieved that higher product extracting rate.Although not steam blowing so that the product quality that boiling range is suitable with decompressed wax oil is poor, but for coal tar oil handling side provided by the invention
Method, entrance suspended-bed reactor is carried out further hydrogenation cracking processing by heavy oil, and therefore final product quality can't produce impact.
In the processing procedure of vacuum tower, feed coal tar segmentation is extracted out, flexible utilization, it is achieved product diversification.Owing to coal tar has carried out the de-Slag treatment of dehydration, therefore, it can reduce coal tar and enter the raw material severity of floating bed hydrocracking device.
Adopting deep vacuum distillation technique to be equivalent to diesel oil and the wax oil fraction of crude oil ordinary decompression column at the lateral line withdrawal function boiling range of vacuum tower, this can improve the motility of coal tar processing.
The diesel oil distillate boiling range that vacuum tower side line (vacuum 1st side cut) is extracted out is 170-320 DEG C, accounts for coal tar total amount
30-35wt%.Vacuum 1st side cut fraction can be directly entered fixed bed reactors, and (light oil that can first extract out with vacuum tower top mixes, then fixed bed reactors are entered back into), suspended-bed reactor is not processed, this can reduce the thermic 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 treating capacity of suspended-bed reactor, give full play to the advantage of suspended-bed reactor processing heavy oil, by adopting the raw material that the processing method of the present invention enters suspended-bed reactor can reduce 28%-32%, unit capacity is significantly increased, simultaneously, the loss that light oil cracking causes can also be avoided by such process, improve product liquid yield.In above-mentioned coal tar oil treatment process, the fraction for vacuum 1st side cut can also adopt another kind of processing scheme, sends to phenol unit processed by vacuum 1st side cut fraction and carries out deep processing.In such cases, for meeting the processing request of downstream phenol unit, the light oil that vacuum tower top is extracted out does not merge with vacuum 1st side cut fraction, the fraction (i.e. the diesel oil distillate of vacuum tower lateral line withdrawal function) of vacuum 1st side cut can be subdivided into carbolic oil that boiling range is 170-230 DEG C and boiling range is the diesel oil distillate of 230-320 DEG C, carbolic oil is sent directly into and carries phenol device as the raw material extracting aldehydes matter, and diesel oil distillate enters in fixed bed reactors.
The wax oil fraction boiling range that vacuum tower side line (second line of distillation) is extracted out is 320-565 DEG C, accounts for the 50-55% of coal tar total amount.The oil of second line of distillation fraction is heavier, enters suspended-bed reactor and carries out hydrogenation cracking.Boiling range >=565 DEG C of the residue product of vacuum tower bottoms, account for the 15-20% of coal tar total amount.
Owing to coal tar dregginess is big, slag cannot be eliminated by the preposition coarse filtration of raw material, and the present invention is by vacuum tower
The heavy oil of bottom filters again, it is possible to reduce enter the invalid component of floating bed hydrocracking device (solid particle is that coal dust etc. does not convert component).By being again filtered to remove the particle diameter solid particle more than 25 μm, residue at the bottom of the tower of the vacuum tower of filtering residue and suspended-bed reactor is mixed into Colophonium pelletizing unit, filtrate enters heavy oil surge tank with the fraction of second line of distillation and mixes, then pass through petroleum pump and deliver to floating bed hydrogenation raw material blending tank, this tank can add from extraneous additive, then deliver in suspended-bed reactor again through raw oil pump, pumping procedure can mix with from extraneous new hydrogen, that is: the filtrate that the heavy oil that the wax oil fraction of vacuum tower lateral line withdrawal function and vacuum tower bottoms are extracted out is filtrated to get is sent in floating bed hydrocracking device raw material blending tank, mix with from outside additive, and entrance floating bed hydrocracking device after mix with from outside new hydrogen after raw oil pump.Such processing mode can optimize the feed composition of slurry-bed hydrocracking device.By the Appropriate application to sideline product, optimize the charging of slurry-bed hydrocracking device, it is possible to increase suspended-bed reactor utilization rate, increase floating bed hydrocracking device motility.
Slurry-bed hydrocracking device is three-phase fluid bed reactor.In three-phase fluid bed reactor, the fluidisation of solid particle is limited primarily by the liquid that flows upwardly through to particle surface frictional force, thus producing granule drag force upwards.By the distribution of distillation of reducing pressure, heavy constituent ratio in suspended-bed reactor material being increased, liquid phase content increases, and improves bed fluidization situation.The problem such as simultaneously reaction medium time of staying length in suspended-bed reactor, cracking reaction can be overcome excessive.
Reaction process etc. in suspended-bed reactor and fixed bed reactors all can carry out in a conventional manner, and follow-up reaction process can also carry out in a conventional manner, is not modified, and maintains existing procedure.
Coal tar is carried out processing the product diversification of the comprehensive utilization that can make coal tar by coal tar oil handling system provided by the present invention, is suitable for the market demand.
Adopt coal tar oil handling system provided by the present invention that the reactant (reducing the diesel oil following components without entering suspension bed) into suspended-bed reactor when carrying out coal tar oil handling, can be reduced, it also is able to reduce the solid particle not converted, that is the process system of the present invention is adopted, suspended-bed reactor can process more coal tar, improves utilization ratio of device；The vacuum 1st side cut that coal tar vacuum tower is extracted out and tower top light oil can be directly entered fixed bed reaction, thus avoiding 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, in the present invention being schematically illustrated and explaining, not delimit the scope of the invention.Wherein.
Fig. 1 is the process chart of prior art.
The structural representation of the coal tar oil handling system that Fig. 2 provides for embodiment 1.
Main Reference label declaration.
nullOutlet port 10D at the bottom of the 10C tower of a fixing high pressure hot separator 23 the 4th heat exchanger 24 second air cooler 25 of raw oil surge tank 1 coal tar oil pump 2 first filter 3 First Heat Exchanger 4 dehydrating tower 5 first air cooler 6 separator 7 second heat exchanger 8 coal tar stove 9 coal tar vacuum tower 10 light oil blending tank 11 light oil pump 12 heavy oil blending tank 13 petroleum pump 14 second filter 15 raw material blending tank 16 raw oil pump 17 make-up hydrogen compressor 18 suspension bed cracker 19-1 high pressure hot separator 19-2 thermal low-pressure separators 19-3 cold low separator 19-4 fixed bed reactors 20 vacuum tower 21 the 3rd heat exchanger 22 fixing 10B second line of distillation outlet port, a cold high pressure separator 26 circulating hydrogen compressor entrance separatory tank 27 circulating hydrogen compressor 28 top exit 10A vacuum 1st side cut outlet port.
Detailed description of the invention
In order to the technical characteristic of the present invention, purpose and beneficial effect are more clearly understood from, referring now to Figure of description, technical scheme is carried out described further below, but it is not intended that to the present invention can the restriction of practical range.
Embodiment 1.
Present embodiments providing a kind of coal tar oil handling system, its structure is as shown in Figure 2.
nullThis coal tar oil handling system includes: raw oil surge tank 1、Coal tar oil pump 2、First filter 3、First Heat Exchanger 4、Dehydrating tower 5、First air cooler 6、Separator 7、Second heat exchanger 8、Coal tar stove 9、Coal tar vacuum tower 10、Light oil blending tank 11、Light oil pump 12、Heavy oil blending tank 13、Petroleum pump 14、Second filter 15、Raw material blending tank 16、Raw oil pump 17、Make-up hydrogen compressor 18、Suspended-bed reactor unit、Fixed bed reactors 20、Vacuum tower 21、3rd heat exchanger 22、Fixing bed high pressure hot separator 23、4th heat exchanger 24、Second air cooler 25、Fixing bed cold high pressure separator 26、Circulating hydrogen compressor entrance separatory tank 27、Circulating hydrogen compressor 28，Suspended-bed reactor unit includes suspension bed cracker 19-1、High pressure hot separator 19-2、Thermal low-pressure separators 19-3、Cold low separator 19-4，Wherein.
Raw oil surge tank 1 is provided with the raw oil entrance for inputting feed coal tar, and its outlet is connected by pipeline with the entrance of the first filter 3, and the connection pipeline of the two is provided with coal tar oil pump 2.
The outlet of the first filter 3 is connected to the entrance of dehydrating tower 5 by pipeline, and the connection pipeline of the two is provided with First Heat Exchanger 4.
The top exit of dehydrating tower 5 is connected by the entrance of pipeline and the first air cooler 6, its outlet at bottom is connected with the entrance of coal tar stove 9 by pipeline, further, the connection pipeline between the entrance of dehydrating tower 5 outlet at bottom and coal tar stove 9 is provided with the second heat exchanger 8.
The outlet of the first air cooler 6 is connected by the entrance of pipeline with separator 7.
Separator 7 is provided with light oil outlet and the outlet of water bag, and light oil outlet is connected to dehydrating tower 5, fixed bed reactors 20 by pipeline, and the outlet of water bag is for discharging the moisture of separation.
The outlet of coal tar stove 9 is connected by the entrance of pipeline with coal tar vacuum tower 10.
Coal tar vacuum tower 10 is provided with outlet port 10D at the bottom of top exit 10A, vacuum 1st side cut outlet port 10B, second line of distillation outlet port 10C and tower, top exit 10A is connected with the entrance of light oil blending tank 11 by pipeline, vacuum 1st side cut outlet port 10B is for extracting diesel oil distillate out and being connected with the entrance of light oil blending tank 11 by pipeline, second line of distillation outlet port 10C is for extracting wax oil out and being connected with the entrance of heavy oil blending tank 13 by pipeline, and outlet port 10D at the bottom of tower is connected by the entrance of pipeline and the second filter 15.
Light oil blending tank 11 is connected with the entrance of fixed bed reactors 20 by pipeline, and connection pipeline therebetween is provided with light oil pump 12.
Heavy oil blending tank 13 is connected with the entrance of raw material blending tank 16 by pipeline, and connection pipeline therebetween is provided with petroleum pump 14.
Raw material blending tank 16 is provided with additive entrance for inputting additive, its outlet is connected by the bottom inlet of pipeline with suspension bed cracker 19-1, and this pipeline is provided with raw oil pump 17 and is connected to new hydrogen input channel, and new hydrogen input channel is provided with make-up hydrogen compressor 18.
The filtrate (liquid of the second filter 15 is connected with the entrance of heavy oil blending tank 13 by pipeline.
The top exit of suspension bed cracker 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 reactors 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 tower 21, and the outlet at bottom of cold low separator 19-4 is connected with the entrance of vacuum tower 21 by pipeline.
The outlet at bottom of fixed bed reactors 20 is connected with the entrance of fixing bed high pressure hot separator 23 by pipeline, and connection pipeline therebetween is provided with the 3rd heat exchanger 22.
Vacuum tower 21 is provided with top exit and outlet at bottom.
The top exit of fixing bed high pressure hot separator 23 is connected with the entrance of fixing bed cold high pressure separator 26 by pipeline, and the connection pipeline of the two is provided with the 4th heat exchanger 24 and the second air cooler 25, and it is additionally provided with outlet at bottom.
The top exit of fixing bed cold high pressure separator 26 is connected with the entrance of circulating hydrogen compressor entrance separatory tank 27, and it is additionally provided with two outlet at bottoms.
The top exit of circulating hydrogen compressor entrance separatory tank 27 is connected with the entrance of circulating hydrogen compressor 28, and it is additionally provided with outlet at bottom.
The outlet of circulating hydrogen compressor 28 is connected with fixed bed reactors 20, suspension bed cracker 19-1 respectively by pipeline.
The coal tar oil handling system that the present embodiment provides may be used for the coal tar oil treatment process comprised the following steps.
Coal tar from tank field is inputted in raw oil surge tank 1 with the mass flow of 75t/h, then utilizes coal tar oil pump 2 coal tar raw material to be transported in the first filter 3 and be filtered, by the pressure raising value 1.4MPaG of coal tar in pumping procedure.
The solid particle of particle diameter >=25 μm in coal tar is removed by the first filter 3, then coal tar enters First Heat Exchanger 4, the temperature of coal tar rises to 130 DEG C, enter dehydrating tower 5 and remove most water, the moisture content 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 dehydrating tower 5, enter in separator 7 after the first air cooler 6 condensation, in separator 7, moisture separates with light oil, strippings is back in dehydrating tower 5, it is partially into the fixed bed reactors 20 raw material as hydrogenation cracking, phenol wastewater sends into sewage disposal system.
Coal tar after dehydration leaves by bottom dehydrating tower 5, enters the second heat exchanger 8 and carries out heat exchange, is heated to 390 DEG C subsequently into coal tar stove 9, enters coal tar vacuum tower 10 afterwards.
Adopting high efficiency low pressure drop filler in coal tar vacuum tower 10 tower, the vacuum degree control at top is 2kPa, and coal tar vacuum tower 10 is extracted light oil distillate out by top exit 10A and enters light oil blending tank 11；Coal tar vacuum tower 10 sets two side lines, vacuum 1st side cut product (boiling range is the diesel oil distillate of 170-320 DEG C) is extracted out by vacuum 1st side cut outlet port 10B, the light oil that vacuum 1st side cut product entrance light oil blending tank 11 is extracted out with coal tar vacuum tower 10 top mixes, then pass through light oil pump 12 and be transported in fixed bed reactors 20 as the raw material being hydrogenated with cracking, mass flow during conveying is 21.8t/h, and medium temperature is 108 DEG C；Extracting the second line of distillation product wax oil fraction of 320-565 DEG C (boiling range be) out by second line of distillation outlet port 10C, second line of distillation product input heavy oil blending tank 13, its mass flow is 38.9t/h, and medium temperature is 227 DEG C；Discharging residual oil by outlet port 10D at the bottom of tower, its mass flow is 13.6t/h, and medium temperature is 374 DEG C；Residual oil enters the second filter 15 and is filtered removing the solid particle of particle diameter >=25 μm, and filtrate enters heavy oil blending tank 13 and second line of distillation Product mix, and filtering residue delivers to the Colophonium pelletizing unit of its exterior.
The mixture of the second line of distillation product in heavy oil blending tank 13 and filtrate is transported in raw material blending tank 16 by petroleum pump 14, and raw material blending tank 16 is inputted from outside additive by additive input pipe so that it is mix with said mixture.
The raw material that material in raw material blending tank 16 is transported in suspension bed cracker 19-1 as cracking reaction by raw oil pump 17, and mixed from outside new hydrogen by what new hydrogen input channel inputted with by make-up hydrogen compressor 18 in course of conveying.
The product of suspension bed cracker 19-1 is after piece-rate system separates, and gas-phase product enters and participates in reaction in fixed bed reactors 20, and the liquid product bottom it then enters vacuum tower 21 and is easily separated.
Fixed gas is discharged at vacuum tower 21 top, and fixed gas as furnace fuel, can discharge residue bottom vacuum tower 21, delivers to the Colophonium pelletizing unit of its exterior after the filtering residue mixing of this part residue and the second filter 15 together.
The product of fixed bed reactors 20 is left by tower bottom outlet, after the 3rd heat exchanger 22 heat exchange, enter fixing bed high pressure hot separator 23 to be easily separated, the high separatory of heat that outlet at bottom is discharged delivers to follow-up segregation apparatus, the hot high score gas in top enters fixing bed cold high pressure separator 28 after the 4th heat exchanger the 24, second air cooler 25 and is easily separated, discharge acid water and cold high score oil, separate the recycle hydrogen obtained and enter circulating hydrogen compressor entrance separatory tank 27.
Separate the recycle hydrogen obtained and by circulating hydrogen compressor 28 and be transported to fixed bed reactors 20 and suspended-bed reactor unit as mixed hydrogen and quenching hydrogen, in circulating hydrogen compressor 28, set recycle hydrogen separatory tank, lime set is collected and discharges, it is to avoid enter compressor gas band liquid.
By adopting the coal tar oil treatment process of the present embodiment, it is possible to reduce the reaction feed of suspended-bed reactor nearly 30%, optimize floating bed hydrocracking device charging, decrease the solid particle not converted, and it is possible to obtain more product, it is achieved the comprehensive utilization of coal tar.Vacuum 1st side cut and tower top light oil that coal tar vacuum tower is extracted out can be directly entered fixed bed reaction, it is to avoid light oil is cracked into dry gas at suspended-bed reactor, improves the liquid yield of product.
Claims (4)
- null1. a coal tar oil handling system，It is characterized in that，This coal tar oil handling system includes: raw oil surge tank、Coal tar oil pump、First filter、First Heat Exchanger、Dehydrating tower、First air cooler、Separator、Second heat exchanger、Coal tar stove、Coal tar vacuum tower、Light oil blending tank、Light oil pump、Heavy oil blending tank、Petroleum pump、Second filter、Raw material blending tank、Raw oil pump、Make-up hydrogen compressor、Suspended-bed reactor unit、Fixed bed reactors、Vacuum tower、Fixing bed high pressure hot separator、3rd heat exchanger、Fixing bed cold high pressure separator、4th heat exchanger、Second air cooler、Circulating hydrogen compressor、Circulating hydrogen compressor entrance separatory tank，Described suspended-bed reactor unit includes suspension bed cracker、High pressure hot separator、Thermal low-pressure separators and cold low separator，Wherein: described raw oil surge tank is provided with the raw oil entrance for inputting feed coal tar，Its outlet is connected by pipeline with the entrance of the first filter，The connection pipeline of the two is provided with coal tar oil pump；The outlet of described first filter is connected to the entrance of described dehydrating tower by pipeline, and the connection pipeline of the two is provided with First Heat Exchanger；The top exit of described dehydrating tower is connected by the entrance of pipeline and the first air cooler, its outlet at bottom is connected with the entrance of described coal tar stove by pipeline, further, the connection pipeline between the entrance of described dehydrating tower outlet at bottom and described coal tar stove is provided with the second heat exchanger；The outlet of described first air cooler is connected by the entrance of pipeline with described separator；Described separator is provided with light oil outlet and the outlet of water bag, and the outlet of described light oil is connected to described dehydrating tower and fixed bed reactors by pipeline, and the outlet of described water bag is for discharging the moisture of separation；The outlet of described coal tar stove is connected by the entrance of pipeline with described coal tar vacuum tower；Described coal tar vacuum tower is provided with outlet port at the bottom of top exit, vacuum 1st side cut outlet port, second line of distillation outlet port and tower, and described top exit is connected with the entrance of described light oil blending tank by pipeline, and described vacuum 1st side cut outlet port is used for extracting light oil out and by managingRoad is connected with the entrance of described light oil blending tank, and described second line of distillation outlet port is for extracting wax oil out and being connected with the entrance of described heavy oil blending tank by pipeline, and outlet port at the bottom of described tower is connected with the entrance of described second filter by pipeline；Described light oil blending tank is connected with the entrance of described fixed bed reactors by pipeline, and connection pipeline therebetween is provided with light oil pump；Described heavy oil blending tank is connected with the entrance of described raw material blending tank by pipeline, and connection pipeline therebetween is provided with petroleum pump；Described raw material blending tank is provided with additive entrance for inputting additive, its outlet is connected by the bottom inlet of pipeline with the suspension bed cracker of described suspended-bed reactor unit, and this pipeline is provided with raw oil pump and is connected to new hydrogen input channel, and new hydrogen input channel is provided with make-up hydrogen compressor；The filtrate (liquid of described second filter is connected with the entrance of described heavy oil blending tank by pipeline；The top exit of the suspension bed cracker of described suspended-bed reactor unit is connected with the entrance of described high pressure hot separator, the top exit of described high pressure hot separator is connected with the entrance of described fixed bed reactors 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 tower, the outlet at bottom of described cold low separator is connected with the entrance of described vacuum tower by pipeline；The outlet at bottom of described fixed bed reactors is connected with the entrance of described fixing bed high pressure hot separator by pipeline, and connection pipeline therebetween is provided with the 3rd heat exchanger；Described vacuum tower is provided with top exit and outlet at bottom；The top exit of described fixing bed high pressure hot separator is connected with the entrance of described fixing bed cold high pressure separator by pipeline, and the connection pipeline of the two is provided with the 4th heat exchanger and the second air cooler, and it is additionally provided with outlet at bottom；The top exit of described fixing bed cold high pressure separator is connected with the entrance of described circulating hydrogen compressor entrance separatory tank, and it is additionally provided with two outlet at bottoms；The top exit of described circulating hydrogen compressor entrance separatory tank is connected with the entrance of described circulating hydrogen compressor, and it is additionally provided with outlet at bottom；The outlet of described circulating hydrogen compressor is connected with the suspension bed cracker of described fixed bed reactors, described suspended-bed reactor unit respectively by pipeline.
- 2. coal tar oil handling system according to claim 1, it is characterised in that the Shui Bao exit of described separator is provided with pump.
- 3. coal tar oil handling system according to claim 1, it is characterised in that the connection pipeline between light oil outlet and the described dehydrating tower of described separator is provided with pump.
- 4. coal tar oil handling system according to claim 1, it is characterised in that described coal tar vacuum tower includes two-stage ejector+water ring vacuum pump.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107355682A (en) * | 2017-05-16 | 2017-11-17 | 胜利油田森诺胜利工程有限公司 | Heavy crude petroleum originates from certainly mixes diluent device |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107355682A (en) * | 2017-05-16 | 2017-11-17 | 胜利油田森诺胜利工程有限公司 | Heavy crude petroleum originates from certainly mixes diluent device |
| CN107355682B (en) * | 2017-05-16 | 2019-07-30 | 胜利油田森诺胜利工程有限公司 | Heavy crude petroleum originates from certainly mixes diluent device |
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Application publication date: 20160713 |