CN105195066A - Preparation equipment of biological aromatic hydrocarbon and preparation method thereof - Google Patents
Preparation equipment of biological aromatic hydrocarbon and preparation method thereof Download PDFInfo
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Abstract
The invention discloses preparation equipment of a biological aromatic hydrocarbon and a preparation method for preparing the biological aromatic hydrocarbon with the equipment. The preparation equipment and the preparation method can be used for treating all mixtures of forestry and agricultural residue biomasses and biomass raw materials. Biogas can be taken as reaction feeding carrier gas as well as lifting steam, so that a system does not need extra gas except a starting stage. Oiling agent rapid separation equipment is adopted, so that oil gas does not come into contact with a catalyst after entering a settler dilute phase space. Heat needed by coke-burning regeneration of a deactivated catalyst in a regenerator is supplied by burning and heating of powdered carbon. A part of oil slurry is returned to a reactor as recycle oil, so that the utilization ratio of the catalyst and the liquid product yield are increased. A part of fuel oil distillate and a part of biogas are taken as auxiliary supplement fuels of the regenerator for later use. Regeneration flue gas is used for producing medium-pressure superheated steam or for driving a flue gas turbine to generate power after dust removal. Industrial pollutants such as waste residues, waste water and waste gas are not discharged in a technological process, which belongs to an environmentally friendly green technological technology.
Description
Technical field
The present invention relates to a kind of preparation of biological aromatic hydrocarbons, particularly relate to a kind of with non-grain biolobic material for raw material produces preparation method and the Preparation equipment of biological aromatic hydrocarbons.
Background technology
In the prior art, aromatic hydrocarbons is a kind of important industrial chemicals, for the production of medicine, pitch, office equipment, cosmetics, television cabin, PC, refrigerator, packaging for foodstuff, sports equipment, automobile and aircraft components, insulating materials, coating, cosmetics and household care product etc.At present both at home and abroad aromatic hydrocarbons generates and mainly relies on petroleum resources, in aromatic hydrocarbons joint production, under the condition of catalyst with HTHP, the process acquisition benzene,toluene,xylene, complex process such as change, be separated through hydrogenation, reformation, aromatic hydrocarbons.The fossil fuel reserves such as oil are limited, and along with fossil fuel consumes in a large number, crude oil price constantly rises, and the chemical engineering industry cost of taking as the leading factor with oil also constantly rises.Moreover, a large amount of accessory substance and other toxic gas and waste material is produced in oil refining engineering, serious environment pollution.Therefore, find the alternative materials of renewable, environment-friendly type and be translated into the concern that aromatic hydrocarbon product just causes domestic and international many companies and research institution.
Biomass energy is the important component part of regenerative resource, and the lasting supply for the energy has vital effect, and for fossil resources, reserves are abundanter, and renewable.Living beings can produce multiple organic chemicals and fuel by efficient refining technology, utilize living beings, especially be the development and application that non-grain biolobic material prepares aromatic hydrocarbons technology, not only can reduce the dependence of aromatics production to petrochemical industry and fuel, be also the alternative techniques alleviating Global Oil shortage of resources.
In recent years, global Duo Jia petrochemical corporation (complex), biochemicals company and colleges and universities all produce great interest to biological legal system benzene,toluene,xylene technique, develop multiple technology of preparing, and obtain laboratory research achievement.It is raw material that Gevo company of the U.S. develops with living beings, first by fermentation alcohol explained hereafter living beings isobutanol, then is technology (WO, 2012061372 [P] that biological aromatic hydrocarbons produced by raw material with isobutanol; US, 20110087000 [P]).American UOP company adopts biomass material synthesization of dimethyl formamide, and pass through with ethene the furan nucleus that catalysis cycloaddition generates dimethyl formamide, then also dewater with the open loop of double-heptene derivative and obtain biological aromatic hydrocarbon product (China, 102482177 [P]; US, 20100331568 [P]).Biomass material is obtained biomass pyrolysis oil by pyrolysis technology by BASF Corp. of Germany, is converted to alkene and aromatic hydrocarbons (US, 20110275868 [P]) with it for raw material through catalytic hydroprocessing cracking reaction.Above-mentioned several biomass-making aromatics process is the good process route of current development prospect, but ubiquity process equipment composition is complicated, technical process accessory substance is difficult to process and the single shortcoming causing raw material availability lower etc. of final products, be unfavorable for its industrialization large-scale production, the technology had in addition also to need with grain crop biolobic material, if corn etc. is for raw material, to affect larger by collecting season.
Summary of the invention
For above-mentioned shortcoming and defect of the prior art, the object of the present invention is to provide and be a kind ofly applicable to various biomass material, simple, easy and simple to handle, all process byproducts of technological process can rationally apply and method and the Preparation equipment of biological aromatic hydrocarbons are prepared in the biomass fluid bed catalytic cracking of non-pollutant discharge.
The object of the invention is to be achieved through the following technical solutions:
A kind of Preparation equipment of biological aromatic hydrocarbons, comprise fluidized-bed reactor, regenerator, heat collector, fractionating column and gas-liquid separator, fluidized-bed reactor bottom is provided with entrance, top is provided with catalyst outlet, top is provided with oil gas vent, described catalyst outlet is by pipeline communication regenerator, and described oil gas vent is communicated with fractionating column; Regenerator bottoms is provided with air inlet, and top is provided with regenerated flue gas outlet, is communicated with the medium inlet of heat collector by pipeline with media outlet; Described fractionating column comprises the slurry oil outlet being arranged on bottom and the fuel oil fraction outlet be arranged on sidewall and diesel oil distillate and exports, and fractionating column top exit is communicated with gas-liquid separator; Described gas-liquid separator is provided with biological flue gas outlet, the outlet of biological aromatic fraction and water out.
Preferably, described fluidized-bed reactor is upstriker fluidized-bed reactor, described upstriker fluidized-bed reactor comprises the reactor being arranged on bottom, finish quick disconnector and cyclone separator, described cyclone separator is positioned at the top of fluidized-bed reactor, described finish quick disconnector is positioned at the below of cyclone separator, described reactor is positioned at the below of finish quick disconnector, described reactor, the conducting successively of finish quick disconnector and cyclone separator, described Cyclone outlet is communicated with oil gas vent, the input port of reactor is the entrance of fluidized-bed reactor, the outlet of described finish quick disconnector is catalyst outlet.
Preferably, described regenerator is upper and lower eclipsed form regenerative system, comprise superposed first regenerator and the Second reactivator being positioned at bottom, described first regenerator is communicated with the medium inlet of heat collector, Second reactivator is communicated with the media outlet of heat collector, have regenerated flue gas outlet at the first regenerator overhead, Second reactivator has catalyst input port.
Preferably, the entrance below described fluidized-bed reactor comprises material inlet, promotes steam inlet, recycle oil import, chilling agent import and regenerated catalyst import.
A preparation method for biological aromatic hydrocarbons, comprises the steps:
S1, is ground into particle by biomass material, and grain diameter is less than 50 orders;
S2, cures more than 3 hour with the temperature of 90 DEG C by the biomass material after pulverizing, makes its water content lower than 5wt% in tumble drying stove;
S3, be fed in reactor by the biomass material mixed feeding carrier gas obtained through S2 process, lifting steam and catalyst by the entrance of fluidized-bed reactor, described catalyst is molecular sieve, and the aperture of described catalyst is 4-5.5nm, and particle diameter is 70-150 order; Under the effect of catalyst, biomass material generation cracking, deoxidation and isomerization reaction, generate the oil gas of gas phase, the decaying catalyst of solid phase and powdered carbon, wherein, feed material carrier gas temperature is 230 DEG C, promoting vapor (steam) temperature is 370 DEG C, the temperature of catalyst is 670 DEG C, and the entry operation pressure of fluidized-bed reactor is 0.3-0.8MPa, operating temperature 500-590 DEG C, average operation gas speed is 18-25m/s, and the reaction time is 2-4s;
S4, the oil gas of gas phase and the decaying catalyst of solid phase and powdered carbon isolate the solid matter of 65-75wt% through quick disconnector, then gas-solid phase mixture enters cyclone separator and is separated, separated oil gas enters in fractionating column by bottom, the operating pressure of cyclone separator is 0.21-0.71MPa, operating temperature is 520-600 DEG C, and operating gas velocity is 20-29m/s;
S5, the catalyst dry powder of inactivation and powdered carbon leave from fluidized-bed reactor top and enter the first regenerator coke burning regeneration, obtain the catalyst, plant ash and the regenerated flue gas that regenerate, regenerated flue gas is exported by regenerated flue gas and discharges, catalyst and the plant ash of regeneration are entered by the medium inlet of heat collector, enter in Second reactivator by the media outlet of heat collector after heat-obtaining, first regenerator operation pressure is 0.2-0.5MPa, operating temperature is 600-700 DEG C, Second reactivator operating pressure is 0.3-0.9MPa, and operating temperature is 650-750 DEG C;
S6, the catalyst of regeneration and plant ash are again entered in reactor by regenerator sloped tube in Second reactivator, and the catalyst temperature temperature entered in reactor of regeneration is 670 DEG C; Within every 120-160 hour, take out the 2wt% of catalyst circulation amount from Second reactivator lower end discharge port, supplement the fresh catalyst with amount simultaneously, because catalyst is different with the density of plant ash, the catalyst of taking-up and the mixture of plant ash is separated, the pure catalyst recycling of separating-purifying by the mode of sedimentation;
S7, the oil gas entered in fractionating column obtains slurry oil, fuel oil fraction, diesel oil distillate, water, biological aromatic fraction and biological flue gas after fractionation, wherein biological aromatic fraction, water and biological flue gas are by collecting respectively after gas-liquid separator process, slurry oil is discharged by the slurry oil outlet of fractionation column base, and fuel oil fraction and diesel oil distillate are discharged by the fuel oil fraction outlet on fractionating column sidewall and diesel oil distillate outlet;
S8, using slurry oil as recycle oil, biological aromatic fraction or water as chilling agent, using biological flue gas after compressor boosting as promoting steam and feed material carrier gas, by pipeline and oil pump, recycle oil and chilling agent are distinguished pump to recycle oil import and chilling agent import.
Preferably, in step s3, feed material carrier gas is 1: 10-1: 15 with the volume flow ratio of lifting steam, and biomass material is 1: 20-1: 30 with mass flow of catalyst ratio.
Preferably, in step s 8, the mass flow ratio of recycle oil and reaction feed is 0.1: 1-0.3: 1; The mass flow ratio of chilling agent and raw material is 0.05: 1-0.2: 1.
Preferably, to the regenerated flue gas produced in the first regenerator through dust removal process, the regenerated flue gas after process is sent into flue gas turbine expander and drive flue gas turbine expander generating.
Preferably, described biomass material is agriculture and forestry organic waste material.
Preferably, described agriculture and forestry organic waste material is one or wherein any two or three mixture of the stalk of crops, cot or wood chip.
Compared with prior art, the embodiment of the present invention at least has the following advantages:
1, the present invention can be used for processing all agriculture and forestry organic waste material biolobic materials, as stalk, rice husk, cotton stem, corncob, wood chip etc., also can process the mixture of this type of biomass material, to the strong adaptability of raw material.
2, the biological flue gas of one of process byproducts can be used as reaction feed carrier gas and promotes steam, and except the stage of going into operation, system does not need outer supplied gas.
3, reactor outlet of the present invention adopts finish quick separating equipment, oil gas to be entered after settler dilute phase space no longer and catalyst exposure, controls the catalytic reaction degree of depth.
4, the heat of the catalyst of inactivation in a regenerator required for coke burning regeneration is generated heat by powdered carbon combustion provides, and makes the present invention not need to consume other fossil fuel under the state of stable conditions.
5, green coke amount of the present invention is large, even if adopt the measures such as CO imperfect combustion, burning liberated heat also exceedes the thermally equilibrated needs of reaction-regeneration system, is therefore designed with heat collector in regenerator outside, in occurring, press through vapours.
6, the part in fractionation column base product slurry oil of the present invention is back to the recycle oil entrance of reactor lower part as recycle oil, improve utilization rate and the liquid yield of catalyst.
7, fluidized bed reactor designs of the present invention has overall reaction severity control district, bottom is injected a certain amount of chilling agent (self-produced gasoline fraction or water) and is optimized the time of staying, oil ratio, reaction temperature and agent oil initial contact temperature in the reactor, proper with the reaction depth controlling whole reactor.
The auxiliary postcombustion that a part in the fuel oil fraction of 8, fractionating column lower side of the present invention and the part in biological flue gas can be used as two regenerators is for subsequent use.
9, regenerator flue gas of the present invention arranges energy-recuperation system, reclaim high-temperature flue gas for the production of in press through vapours and drive flue gas turbine expander generating.And the capacity usage ratio of flue gas is improved in the flue application afterburning technology that regenerator flue gas is discharged.
10, the full tower of fractionating column of the present invention is except slurry oil circulation desuperheating section, also has stage casing backflow and top pumparound to take out full tower surplus heat.
11, technical process of the present invention is without emission of industrial pollutants such as waste residue, waste water, waste gas, belongs to environment-friendly technology.
Accompanying drawing explanation
Fig. 1 is the structural representation of the Preparation equipment of the biological aromatic hydrocarbons of the present invention.
Detailed description of the invention
Below in conjunction with Fig. 1 and embodiment, the invention will be further described, and following examples are descriptive, are not determinate, can not limit protection scope of the present invention with this.
A kind of Preparation equipment of biological aromatic hydrocarbons, comprise fluidized-bed reactor 1, regenerator, heat collector 5, fractionating column 3 and gas-liquid separator 4, fluidized-bed reactor 1 bottom is provided with entrance, top is provided with catalyst outlet 7, top is provided with oil gas vent 8, described catalyst outlet 7 is by pipeline communication regenerator, and described oil gas vent 8 is communicated with fractionating column 3; Regenerator bottoms is provided with air inlet 9, and top is provided with regenerated flue gas outlet 10, is communicated with the medium inlet 11 of heat collector 5 by pipeline with media outlet 12; Described fractionating column 3 comprises the slurry oil outlet 13 being arranged on bottom and the fuel oil fraction outlet 14 be arranged on sidewall and diesel oil distillate and exports 15, and fractionating column 3 top exit is communicated with gas-liquid separator 4; Described gas-liquid separator 4 is provided with biological flue gas outlet 16, biological aromatic fraction outlet 17 and water out 18.
Described fluidized-bed reactor 1 is upstriker fluidized-bed reactor 1, described upstriker fluidized-bed reactor 1 comprises the reactor being arranged on bottom, finish quick disconnector and cyclone separator, described cyclone separator is positioned at the top of fluidized-bed reactor 1, described finish quick disconnector is positioned at the below of cyclone separator, described reactor is positioned at the below of finish quick disconnector, described reactor, the conducting successively of finish quick disconnector and cyclone separator, described Cyclone outlet is communicated with oil gas vent 8, the input port of reactor is the entrance of fluidized-bed reactor 1, the outlet of described finish quick disconnector is catalyst outlet 7.
Described regenerator is upper and lower eclipsed form regenerative system, comprise superposed first regenerator 2 and the Second reactivator 6 being positioned at bottom, described first regenerator 2 is communicated with the medium inlet 11 of heat collector 5, Second reactivator 6 is communicated with the media outlet 12 of heat collector 5, have regenerated flue gas outlet 10 at the first regenerator 2 top, Second reactivator 6 has catalyst input port 19.
Described catalyst is molecular sieve, and the aperture of described catalyst is 4-5.5nm, and particle diameter is 70-150 order; Entrance below described fluidized-bed reactor comprises material inlet, promotes steam inlet, recycle oil import, chilling agent import and regenerated catalyst import.
A preparation method for biological aromatic hydrocarbons, comprises the steps:
S1, is ground into particle by biomass material, and grain diameter is less than 50 orders; Described biomass material is agriculture and forestry organic waste material, and agriculture and forestry organic waste material is one or wherein any two or three mixture of the stalk of crops, cot or wood chip.
S2, cures more than 3 hour with the temperature of 90 DEG C by the biomass material after pulverizing, makes its water content lower than 5wt% in tumble drying stove;
S3, by the biomass material mixed feeding carrier gas obtained through S2 process, lifting steam and catalyst are fed in reactor by the entrance of fluidized-bed reactor 1, under the effect of catalyst, biomass material generation cracking, deoxidation and isomerization reaction, generate the oil gas of gas phase, the decaying catalyst of solid phase and powdered carbon, wherein, feed material carrier gas temperature is 230 DEG C, promoting vapor (steam) temperature is 370 DEG C, the temperature of catalyst is 670 DEG C, the entry operation pressure of fluidized-bed reactor 1 is 0.6MPa, operating temperature 540 DEG C, average operation gas speed is 23m/s, reaction time is 3.0s,
S4, the oil gas of gas phase and the decaying catalyst of solid phase and powdered carbon isolate the solid matter of 65-75wt% through quick disconnector, then gas-solid phase mixture enters cyclone separator and is separated, efficiency separator is 99.999%, separated oil gas enters in fractionating column 3 by bottom, the operating pressure of cyclone separator is 0.38MPa, and operating temperature is 530 DEG C, and operating gas velocity is 22m/s;
S5, the catalyst dry powder of inactivation and powdered carbon leave from fluidized-bed reactor 1 top and enter the first regenerator 2 coke burning regeneration, in first regenerator 2, part thermocatalyst enters heat collector 5, heat-obtaining amount is always burn thermal discharge 5 ~ 15%, obtain the catalyst, plant ash and the regenerated flue gas that regenerate, regenerated flue gas exports 10 by regenerated flue gas and discharges, hot-air is introduced bottom Second reactivator 6, reclaimable catalyst coke burning regeneration institute calorific requirement is provided by powdered carbon, regenerated flue gas temperature 670 DEG C, composition comprises CO2, CO and H2O, and wherein CO burns into CO2 completely through afterburning; Catalyst and the plant ash of regeneration are entered by the medium inlet 11 of heat collector 5, enter in Second reactivator 6 by the media outlet 12 of heat collector 5 after heat-obtaining, first regenerator 2 operating pressure is 0.45MPa, operating temperature is 640 DEG C, Second reactivator 6 operating pressure is 0.57MPa, and operating temperature is 720 DEG C;
S6, the catalyst of regeneration and plant ash are again entered in reactor by regenerator sloped tube in Second reactivator 6, and the catalyst temperature temperature entered in reactor of regeneration is 670 DEG C; Within every 120-160 hour, take out the 2wt% of catalyst circulation amount from Second reactivator 6 lower end discharge port, supplement the fresh catalyst with amount simultaneously, because catalyst is different with the density of plant ash, the catalyst of taking-up and the mixture of plant ash is separated by the mode of sedimentation, separative efficiency can reach 99.99%, the pure catalyst recycling of separating-purifying;
S7, the oil gas entered in fractionating column 3 obtains slurry oil, fuel oil fraction, diesel oil distillate, water, biological aromatic fraction and biological flue gas after fractionation, wherein biological aromatic fraction, water and biological flue gas are collected after being processed by gas-liquid separator 4 respectively, slurry oil is discharged by the slurry oil outlet 13 bottom fractionating column 3, and fuel oil fraction and diesel oil distillate are discharged by the fuel oil fraction outlet 14 on fractionating column 3 sidewall and diesel oil distillate outlet 15; Fractionating column 3 operating condition is 0.27MPa, oil gas obtains 6 kinds of products after entering fractionating column 3, that composition is based on the biological flue gas of CO, CO2, CH4, H2 respectively, the biological aromatic fraction of 110 ~ 200 DEG C, water, the biodiesel cut 12 of 200 ~ 350 DEG C, temperature is more than or equal to fuel oil fraction and the slurry oil of 350 DEG C.
A part in biological aromatic fraction or water is as chilling agent, and be connected to reactor inlet, the mass flow ratio of chilling agent and biomass material is 0.09: 1.
A part in slurry oil, as recycle oil, is connected to reactor inlet, and the mass flow ratio of recycle oil and biomass material is 0.15: 1.
A part in biological flue gas recycles as lifting steam and feed material carrier gas after compressor boosting, and feed material carrier gas is 1: 12 with the volume flow ratio of lifting steam, and remainder can be used for domestic gas or produces steam and electric power.
To the regenerated flue gas produced in the first regenerator 2 through dust removal process, the regenerated flue gas after process is entered energy-recuperation system, send into flue gas turbine expander and drive flue gas turbine expander generating.
The above; be only the present invention's preferably detailed description of the invention, but protection scope of the present invention is not limited thereto, is anyly familiar with those skilled in the art in the technical scope that the present invention discloses; the change that can expect easily or replacement, all should be encompassed within protection scope of the present invention.Therefore, protection scope of the present invention should be as the criterion with the protection domain of claims.
Claims (10)
1. the Preparation equipment of a biological aromatic hydrocarbons, it is characterized in that, comprise fluidized-bed reactor, regenerator, heat collector, fractionating column and gas-liquid separator, fluidized-bed reactor bottom is provided with entrance, top is provided with catalyst outlet, top is provided with oil gas vent, and described catalyst outlet is by pipeline communication regenerator, and described oil gas vent is communicated with fractionating column; Regenerator bottoms is provided with air inlet, and top is provided with regenerated flue gas outlet, is communicated with the medium inlet of heat collector by pipeline with media outlet; Described fractionating column comprises the slurry oil outlet being arranged on bottom and the fuel oil fraction outlet be arranged on sidewall and diesel oil distillate and exports, and fractionating column top exit is communicated with gas-liquid separator; Described gas-liquid separator is provided with biological flue gas outlet, the outlet of biological aromatic fraction and water out.
2. the Preparation equipment of biological aromatic hydrocarbons according to claim 1, it is characterized in that, described fluidized-bed reactor is upstriker fluidized-bed reactor, described upstriker fluidized-bed reactor comprises the reactor being arranged on bottom, finish quick disconnector and cyclone separator, described cyclone separator is positioned at the top of fluidized-bed reactor, described finish quick disconnector is positioned at the below of cyclone separator, described reactor is positioned at the below of finish quick disconnector, described reactor, the conducting successively of finish quick disconnector and cyclone separator, described Cyclone outlet is communicated with oil gas vent, the input port of reactor is the entrance of fluidized-bed reactor, the outlet of described finish quick disconnector is catalyst outlet.
3. the Preparation equipment of biological aromatic hydrocarbons according to claim 2, it is characterized in that, described regenerator is upper and lower eclipsed form regenerative system, comprise superposed first regenerator and the Second reactivator being positioned at bottom, described first regenerator is communicated with the medium inlet of heat collector, Second reactivator is communicated with the media outlet of heat collector, has regenerated flue gas outlet, Second reactivator has catalyst input port at the first regenerator overhead.
4. according to the Preparation equipment of the arbitrary described biological aromatic hydrocarbons of claim 1-3, it is characterized in that, the entrance below described fluidized-bed reactor comprises material inlet, promotes steam inlet, recycle oil import, chilling agent import and regenerated catalyst import.
5. a preparation method for biological aromatic hydrocarbons, is characterized in that, comprises the steps:
S1, is ground into particle by biomass material, and grain diameter is less than 50 orders;
S2, cures more than 3 hour with the temperature of 90 DEG C by the biomass material after pulverizing, makes its water content lower than 5wt% in tumble drying stove;
S3, be fed in reactor by the biomass material mixed feeding carrier gas obtained through S2 process, lifting steam and catalyst by the entrance of fluidized-bed reactor, described catalyst is molecular sieve, and the aperture of described catalyst is 4-5.5nm, and particle diameter is 70-150 order; Under the effect of catalyst, biomass material generation cracking, deoxidation and isomerization reaction, generate the oil gas of gas phase, the decaying catalyst of solid phase and powdered carbon, wherein, feed material carrier gas temperature is 230 DEG C, promoting vapor (steam) temperature is 370 DEG C, the temperature of catalyst is 670 DEG C, and the entry operation pressure of fluidized-bed reactor is 0.3-0.8MPa, operating temperature 500-590 DEG C, average operation gas speed is 18-25m/s, and the reaction time is 2-4s;
S4, the oil gas of gas phase and the decaying catalyst of solid phase and powdered carbon isolate the solid matter of 65-75wt% through quick disconnector, then gas-solid phase mixture enters cyclone separator and is separated, separated oil gas enters in fractionating column by bottom, the operating pressure of cyclone separator is 0.21-0.71MPa, operating temperature is 520-600 DEG C, and operating gas velocity is 20-29m/s;
S5, the catalyst dry powder of inactivation and powdered carbon leave from fluidized-bed reactor top and enter the first regenerator coke burning regeneration, obtain the catalyst, plant ash and the regenerated flue gas that regenerate, regenerated flue gas is exported by regenerated flue gas and discharges, catalyst and the plant ash of regeneration are entered by the medium inlet of heat collector, enter in Second reactivator by the media outlet of heat collector after heat-obtaining, first regenerator operation pressure is 0.2-0.5MPa, operating temperature is 600-700 DEG C, Second reactivator operating pressure is 0.3-0.9MPa, and operating temperature is 650-750 DEG C;
S6, the catalyst of regeneration and plant ash are again entered in reactor by regenerator sloped tube in Second reactivator, and the catalyst temperature temperature entered in reactor of regeneration is 670 DEG C; Within every 120-160 hour, take out the 2wt% of catalyst circulation amount from Second reactivator lower end discharge port, supplement the fresh catalyst with amount simultaneously, be separated the catalyst of taking-up and the mixture of plant ash by the mode of sedimentation, the pure catalyst recycling of separating-purifying;
S7, the oil gas entered in fractionating column obtains slurry oil, fuel oil fraction, diesel oil distillate, water, biological aromatic fraction and biological flue gas after fractionation, wherein biological aromatic fraction, water and biological flue gas are by collecting respectively after gas-liquid separator process, slurry oil is discharged by the slurry oil outlet of fractionation column base, and fuel oil fraction and diesel oil distillate are discharged by the fuel oil fraction outlet on fractionating column sidewall and diesel oil distillate outlet;
S8, using slurry oil as recycle oil, biological aromatic fraction or water as chilling agent, using biological flue gas after compressor boosting as promoting steam and feed material carrier gas, by pipeline and oil pump, recycle oil and chilling agent are distinguished pump to recycle oil import and chilling agent import.
6. the preparation method of biological aromatic hydrocarbons according to claim 5, is characterized in that, in step s3, feed material carrier gas is 1:10-1:15 with the volume flow ratio of lifting steam, and biomass material and mass flow of catalyst are than being 1:20-1:30.
7. the preparation method of biological aromatic hydrocarbons according to claim 5, is characterized in that, in step s 8, the mass flow ratio of recycle oil and reaction feed is 0.1:1-0.3:1; The mass flow ratio of chilling agent and raw material is 0.05:1-0.2:1.
8. the preparation method of biological aromatic hydrocarbons according to claim 5, is characterized in that, to the regenerated flue gas produced in the first regenerator through dust removal process, the regenerated flue gas after process is sent into flue gas turbine expander and drives flue gas turbine expander generating.
9. the preparation method of biological aromatic hydrocarbons according to claim 5, is characterized in that, described biomass material is agriculture and forestry organic waste material.
10. the preparation method of biological aromatic hydrocarbons according to claim 9, is characterized in that, described agriculture and forestry organic waste material is one or wherein any two or three mixture of the stalk of crops, cot or wood chip.
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| CN114053962A (en) * | 2021-11-08 | 2022-02-18 | 大连凯飞化学股份有限公司 | Fluidized bed reaction system and method for in-situ catalytic synthesis of thymol |
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