CN102585917B - Technology and system for cooling-absorbing coupling deep-removing tar from biomass gas - Google Patents
Technology and system for cooling-absorbing coupling deep-removing tar from biomass gas Download PDFInfo
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Abstract
The invention relates to a technology and a system for cooling-absorbing coupling deep-removing tar from biomass gas. The system consists of a water cooling tower, a tar absorption tower, a flashing tower, auxiliary heat exchangers and storage tanks, high-temperature biomass gas which is rich in tar enters the water cooling tower at first to be sprayed and contacted with heavy tar liquid so as to be cooled and condensed to be liquid, so that a small amount of dust and most of heavy tar steam are removed; the biomass gas purified primarily is sent to the tar absorption tower, light tar steam is fully absorbed by absorbing medium and enters into oil phase of absorption liquid, a small amount of water vapor, hydrogen sulfide and ammonia are cooled and enter into water phase of the absorption liquid, and the purified biomass gas is sent to the subsequent workshop section for use; the absorption liquid coming out from the bottom of the tar absorption tower is sent to the flashing tower, the heat discharged from the water cooling tower is used for flashing, liquid phase absorption agent after flashing is recycled and returned to the tar absorption tower after being cooled, and gas phase products are subjected to condensation and oil-water separation.
Description
Affiliated technical field
The present invention relates to a kind of coal-tar middle oil deep removal method of combustion gas that biomass thermal chemical conversion process generates, relate to a kind of technique and system of cooling-absorbing coupling deep-removing tar from biomass gas, belong to biomass energy and efficiently utilize field.
Background technology
Biomass resource belongs to renewable resources, can realize the recycle of carbon resource under ideal conditions.Biomass resource, through suitable thermochemistry or Biochemical processes, is converted into biological fuel gas, or further deep processing obtains chemical, for society provides basic chemical industry raw material or the energy.Therefore, sun power, wind energy etc. only can produce the renewable resources of electric power equal energy source relatively, and biomass resource is unique renewable resources that is converted into chemical, can be used as the substitute of fossil feedstock, for socio-economic development provides resource base.
Biomass thermal chemical conversion process is under high temperature (or cocatalyst) condition, biomass material is through super-dry, thermolysis, oxidation and reduction process, macromole is through fracture and restructuring, be converted into the process of micromolecular oil fuel or combustion gas, the method has become the major way of biomass resource utilization.The at present main application form of biomass thermal chemical conversion technology has gasification burning generating, gasification burning heat supply, pyrolysis production bio oil and gasification burning synthesis of chemicals etc.Generally speaking, this technology remains at some key obstacles in stability, the economy of gasification and the security of subsequent product use procedure of gasification, therefore do not obtain large-scale promotion application.
Along with going deep into of biomass thermal chemical conversion technical study and demonstration, the impact of the tar producing in gasification becomes one of crucial difficult problem of this technology popularization application of restriction.In biomass material thermochemistry conversion process, be accompanied by the appearance of gaseous product, can produce tar macromole.Under tar normal temperature, be a kind of chocolate thick liquid, its composition is very complicated, and the composition that can analyze has kind more than 100, also has a lot of compositions to be difficult to define.Burnt main body of oil is no less than 20 kinds, and major part is derivative and the polycyclic aromatic hydrocarbons of benzene, wherein content be greater than 5% nearly following several: naphthalene, toluene, dimethylbenzene, vinylbenzene and phenol etc., the content of other composition is generally all less than 5%.Biomass coke tar is liquid at 200 DEG C below, and 300 DEG C are gaseous state above, at high temperature can resolve into small molecules permanent gases.The subject matter of the existence restriction biomass gasification technology large-scale application of tar is as follows: 1. tar accounts for 5%～10% of combustible gas energy, at low temperature (normal temperature, approach envrionment temperature) under be difficult to be utilized together with combustion gas, cause thermochemistry conversion process inefficiency; 2. tar condenses into liquid at low temperatures, and the dust such as Yi Heshui, carbon granules are combined into dope, stops up gas pipe line and valve, and corroding metal affects system operation and safety; 3. tar is difficult to perfect combustion, and produces the particles such as carbon black, serious to the impeller infringement of the gas-fired equipment for generating electricity (as oil engine, internal combustion turbine etc.); 4. the poison gas producing after tar and burning thereof pollutes the environment.As can be seen here, the tar in combustible gas has sizable hazardness, is one of major obstacle of biomass gasification process application, must effectively process it.
Biomass gas tar oil treatment process mainly comprises Physical, thermochemical method and plasma decoking method etc.Physics decoking comprises wet method and the large class of dry method two.Wet type decoking method is mainly WATER-WASHING METHOD, is that the part tar in combustible gas is cooled to liquid by water, is rinsed and takes away by water, and the method main drawback is in combustion gas, easily to carry tar droplet secretly, and can bring the secondary pollution problem of tar washed wastewater; Dry-type decoking method adopts filtering technique purifying gas, can avoid the secondary pollution to water body and soil, but in engineering application, the effect of removing tar is undesirable, and the deposition of tar is serious, and has system device complexity, the shortcomings such as operation life is short, normal and other decoking coupling.Plasma decoking method is to utilize the feature that corona discharge can decomposing organic matter to carry out removing of tar, but the method equipment manufacturing cost and working cost are high, also high than other method to the requirement of operational administrative.Thermochemistry conversion method is tar to be changed into combustion gas small molecules under certain temperature condition, improve transformation efficiency and the utilization ratio of biomass, can be divided into pyrolysis method and catalystic pyrolysis, wherein pyrolysis method energy consumption is high, and the easy carbon deposit of catalystic pyrolysis catalyzer and sintering, physical strength is also poor, thereby only has Demonstration Application on a small scale.
Remove a difficult problem for biomass gas tar oil, investigator proposes to reduce the coal-tar middle oil content of combustion gas by the method absorbing, and reaches absorption agent recycle by desorption." OLGA " (the Dutch acronym for of Holland's energy centre exploitation
washer) decoking is exactly the novel decoking process taking solvent absorbing tar as basis, and result shows: heavy tar is removed completely, and tar dew-point temperature is reduced to 25 DEG C, and tar can not condense in vapourizing furnace downstream; 99% phenols and 97% heterocyclic tar can be removed, and can save because processing by the cost of the waste water of phenols or other water-soluble blended tars pollution.Zhang Zhongcheng etc. are at " the biological fuel gas decoking technique simulation based on Aspen plus platform " (journal of Shandong university, 2008,38 (6): 95-98) in article, the solvent method decoking technique of biological fuel gas has been proposed, by the cooling and absorbing effect of solvent, by the heavies removal in tar, light constituent selectively removing, dew point coal-tar middle oil combustion gas is after treatment reduced under use temperature, thus the problems such as the line clogging that solution is produced by condensing of tar.But these two kinds of method first step detar cooling towers adopt the cooling tar of plus solvent, due to this part tar ingredients complexity, solid particulate is many, can form the mixed dust thickness, the constant boiling mixture that are difficult to separation, and separating difficulty is large, and running cost is high; The heat of combustion gas is not fully used; In addition, combustion gas dehydration is not carried out on absorption tower, the second stage simultaneously, and dehydration is further placed on to follow-up workshop section, will increase system complex degree and cost of investment.Zhou Xiaping etc. are at " adopting absorption agent to reduce the experimental study of biological tar content " (solar energy journal, 2009,30 (3): 381-384) in article, propose to combine as absorption agent using ethylene glycol, thanomin or its, carry out biological fuel gas detar, but the report of the desorption process of not being correlated with.In the patent that the old equality of Disen Heat Energy Technology Co., Ltd., Guangzhou is CN101532785A at publication number, adopt the bio oil bio oil that directly the method condensation biomass pyrolytic of spray obtains itself, the method can fully suppress the further cracking of condensability component, and can avoid causing due to additional cooling medium the loaded down with trivial details technique of later separation.But after this spray end of processing, bio oil temperature is unsuitable too low, as too low, bio oil viscosity is excessive, brings difficulty to continuous, mass-producing operation; Finish rear temperature as sprayed higher, because bio oil itself does not possess sorption, cause tar and steam that some molecules are less to be difficult to effective condensation, affect the further use of biological fuel gas.In the patent that Ma Jiade is CN101186836A at publication number, invent a kind of method that adopts useless rubber and plastic cracked oil to carry out the cooling recovery of biological flue gas, after rubber and plastic cracking, in combustion gas, can mix ash content and tiny charcoal particle, after focusing oil cooling reclaims, above-mentioned ash content and charcoal particle and tar formation dope, as directly it carried out to rectifying, can increase operation and operation difficulty.
Summary of the invention
The object of the invention is to overcome the limitation of above-mentioned biomass gas tar oil removal methods, the advantage of the cooling and absorption process of a kind of combination is provided, low cost is technique and the system of a kind of cooling-absorbing coupling deep-removing tar from biomass gas of the coal-tar middle oil and water of deep removal biological fuel gas simultaneously, and by-product coke oil production.
Technical scheme of the present invention is achieved in that first the high-temperature biomass gas that is rich in tar steam being generated by biomass gasifying furnace enters tar water cooling tower after dedusting, contact with tar heavy oil (referring to that boiling point is higher than the tar of 100 DEG C) liquid, most of heavy tar steam is cooled to liquid, and a small amount of dust in biological fuel gas and most of heavy tar steam are removed; Biological fuel gas after rough purification, be admitted to tar absorption tower, in this tower, tar light oil (referring to that boiling point is lower than the tar of 100 DEG C) steam is absorbed medium and fully absorbs, enter the oil phase of absorption liquid, a small amount of ammonia, hydrogen sulfide and water vapor are cooled, and enter the water of absorption liquid, and the biological fuel gas after purification is sent into follow-up workshop section; Be admitted to flashing tower from absorption liquid out at the bottom of tar absorption tower, utilize water cooling tower liberated heat to carry out flash distillation, tar absorption tower is returned in the cooling rear circulation of liquid absorbent after flash distillation, gas-phase product is through condensation and oily water separation, obtain respectively tar light oil product, containing the recycled offgas of a small amount of lighter hydrocarbons, and a small amount of deposed ammonia.
Concrete technical scheme of the present invention is: a kind of system of cooling-absorbing coupling deep-removing tar from biomass gas, it is characterized in that, formed by water cooling tower 1, tar absorption tower 4, flashing tower 5, First Heat Exchanger 2A, the second interchanger 2B, interchanger 6, tar heavy oil storage tank 3A and tar light oil storage tank 3B; Described water cooling tower 1 is provided with underfeed mouth, bottom discharge mouth, top discharge mouth and top spray opening for feed, tar heavy oil storage tank 3A is provided with top opening for feed, top discharge mouth, bottom discharge mouth and bottom discharge port, tar absorption tower 4 is provided with underfeed mouth, bottom discharge mouth, top discharge mouth and top spray opening for feed, the 4 in-built years liquid absorbent f in tar absorption tower, flashing tower 5 is provided with top opening for feed, top discharge mouth and bottom discharge mouth; Tar light oil storage tank 3B is provided with its top feed mouth, bottom discharge port and bottom discharge mouth; Condenser 6 is provided with upper air vent; Water cooling tower 1 top discharge mouth connects tar absorption tower 4 underfeed mouths, water cooling tower 1 bottom discharge mouth and First Heat Exchanger 2A connect, the top opening for feed that the discharge port of First Heat Exchanger 2A connects tar storage tank 3A enters tar heavy oil storage tank 3A, and the top spray opening for feed of tar heavy oil storage tank 3A top discharge mouth and water cooling tower 1 is connected; The bottom discharge mouth on tar absorption tower 4 connects the top opening for feed of flashing tower 5, the bottom discharge mouth of flashing tower 5 connects the second interchanger 2B, the outlet of the second interchanger 2B connects tar absorption tower 4 top spray opening for feeds, the top gas discharge port of flashing tower 5 connects condenser 6, and the outlet at bottom of condenser 6 connects its top feed mouth of tar light oil storage tank 3B.
The present invention also provides the technique of the cooling-absorbing coupling deep-removing tar from biomass gas that utilizes said system, concrete steps are: first the high-temperature biomass gas a of tar steam that what biomass gasifying furnace obtained be rich in enters water cooling tower 1 by water cooling tower 1 underfeed mouth after dedusting, tar heavy oil liquid spraying by water cooling tower 1 top spray opening for feed is cooling, cooling fluid flows into First Heat Exchanger 2A by water cooling tower 1 bottom discharge mouth, cooling liberated heat is taken away by heat transferring medium b, the cooling tar heavy oil obtaining enters tar heavy oil storage tank 3A through tar heavy oil storage tank 3A top opening for feed, in tar heavy oil storage tank 3A, tar heavy oil carries out standing separation and removes residual oil c, residual oil c is discharged by tar heavy oil storage tank 3A bottom discharge mouth, tar heavy oil d is discharged as product by tar heavy oil storage tank 3A bottom discharge port, part tar heavy oil d returns to water cooling tower by tar heavy oil storage tank 3A top discharge mouth through water cooling tower 1 top spray opening for feed, as spraying cooling medium, from the water cooling tower 1 top discharge mouth biological fuel gas that removes tar heavy oil out, be sent to tar absorption tower 4 underfeed mouths and enter tar absorption tower 4, in tar absorption tower 4, tar light oil steam is absorbed agent f and fully absorbs, enter the oil phase of absorption liquid, ammonia, hydrogen sulfide and water vapor are cooled, and enter the water of absorption liquid, and the biological fuel gas e after purification is admitted to follow-up workshop section through tar absorption tower 4 top discharge mouths, enter flashing tower 5 from absorption liquid out at the bottom of 4 towers of tar absorption tower by flashing tower 5 top opening for feeds, utilize First Heat Exchanger 2A liberated heat to carry out heating flash evaporation through heat transferring medium b, absorption agent f after flash distillation enters the second interchanger 2B by flashing tower 5 bottom discharge mouths, after the second interchanger 2B is cooling, return to tar absorption tower 4 by the 4 top spray opening for feed circulations of tar absorption tower, the gas-phase product of flashing tower 5 top discharge mouths utilizes heat-eliminating medium h to carry out condensation in condenser 6, the liquid product of condenser 6 enters tar light oil storage tank 3B, the recycled offgas g of top discharge mouth, biomass gasifying furnace is returned in circulation, further participate in gasification reaction, tar light oil storage tank 3B bottom discharge port is tar light oil product i, and bottom discharge mouth is deposed ammonia j.Described tar heavy oil is boiling point higher than the tar of 100 DEG C, and tar light oil is boiling point lower than the tar of 100 DEG C.
Tar treatment process of the present invention and system adaptability to raw material are wide, and biological fuel gas comprises the combustion gas obtaining of gasifying of various fixed beds and biomass fluid bed gasification furnace, and the combustion gas of being rich in tar and bio oil that obtains of destructive distillation or half retort process.
Tar of the present invention absorption tower 4, absorption temperature is the temperature of the environment cools medium of 10～40 DEG C, ensure that tar light oil is absorbed agent and fully absorbs, enter oil phase, make to export the dew point of the coal-tar middle oil dew point of biological fuel gas lower than normal temperature, can condensation in follow-up use procedure, pollute pipeline and valve etc., combustion gas is fully purified; In addition, absorbing medium has cooling effect, and a small amount of water vapor containing in biological fuel gas is condensed, enter absorption liquid water, a small amount of ammonia and hydrogen sulfide etc., be absorbed and enter absorption liquid water, steam can be at the follow-up use procedure condensation of combustion gas, can etching apparatus, and impact operation.Absorption agent f in described tar absorption tower 4, it is non-polar oil cut, can fully absorb the tar in combustion gas, reduce tar dew point, immiscible with water, or be slightly soluble in water, for carbonatoms is greater than 9 at least one that are less than in 25 stable hydrocarbon, benzene neutral derivant, naphthalene and neutral derivant thereof, and boiling range scope is 150～300 DEG C.
The present invention has following beneficial effect:
(1) unstripped gas wide adaptability, biological fuel gas comprises the combustion gas obtaining of gasifying of various fixed beds and biomass fluid bed gasification furnace, and the combustion gas of being rich in tar and bio oil that obtains of destructive distillation or half retort process;
(2) can carry out degree of depth decoking to combustion gas, tar is down under the dew point of use temperature, ensure at follow-up not condensation of use procedure, etching apparatus;
(3) adopt tar heavy oil to spray decoking to biological fuel gas, spraying cooling is effective, can remove tar heavy oil, and a small amount of dust in wash-out biological fuel gas; Tar heavy oil is simultaneously as spraying cooling agent and product, need not additional heat-eliminating medium, reduce separation difficulty and cost;
(4) tar light oil adopts absorption agent to absorb, and has concurrently and absorbs and cooling effect, and sorption can be down to tar light oil below dew-point temperature, ensures the safe handling at subsequent process; Decoking process is cooled dehydrated, deamination simultaneously, has avoided subsequent process further water in combustion gas to be removed, and has simplified decoking flow process, has saved cost;
(5) tar light oil and tar heavy oil are sold as product respectively, have saved the cost that follow-up cut " cutting " is processed;
(6) by spraying cooling liberated heat, reclaim the heating heat as flash separation tower, save the energy consumption of tar treating processes;
(7) tar treating processes of the present invention, energy consumption is low, and light, tar heavy oil is respectively as byproduct, without disposals of pollutants such as waste water.
Brief description of the drawings
Fig. 1 is system schematic of the present invention, wherein 1-water cooling tower; 2A-First Heat Exchanger; 2B-the second interchanger; 3A-tar heavy oil storage tank; 3B-tar light oil storage tank; 4-tar absorption tower; 5-flashing tower; 6-condenser; A-is rich in the biological fuel gas of tar; B-heat transferring medium; C-residual oil; D-tar heavy oil; Biological fuel gas after e-purifies; F-absorption agent; G-recycled offgas; H-heat-eliminating medium; I-tar light oil product; J-deposed ammonia
Embodiment
The present invention is further described by following examples, but does not therefore limit the scope of application of the present invention.
As shown in Figure 1, biological fuel gas removes the system of tar to system schematic of the present invention, is made up of water cooling tower 1, tar absorption tower 4, flashing tower 5, First Heat Exchanger 2A, the second interchanger 2B, tar heavy oil storage tank 3A and tar light oil storage tank 3B; Described water cooling tower 1 is provided with underfeed mouth, bottom discharge mouth, top discharge mouth and top spray opening for feed, tar heavy oil storage tank 3A is provided with top opening for feed, top discharge mouth, bottom discharge mouth and bottom discharge port, tar absorption tower 4 is provided with underfeed mouth, bottom discharge mouth, top discharge mouth and top spray opening for feed, the 4 in-built years liquid absorbent f in tar absorption tower, absorption agent f is the mixture of n-propyl hexanaphthene (5%wt), naphthalene (10%wt) and 1-methyl-2-ethylbenzene (90%wt), and boiling range is 150～180 DEG C; Flashing tower 5 is provided with top opening for feed, top discharge mouth and bottom discharge mouth, and tar light oil storage tank 3B is provided with its top feed mouth, bottom discharge port and bottom discharge mouth; Water cooling tower 1 top gas outlet connects tar absorption tower 4 underfeed mouths, water cooling tower 1 bottom discharge port and First Heat Exchanger 2A connect, the discharging of First Heat Exchanger 2A enters the top opening for feed of tar heavy oil storage tank 3A, and the top spray opening for feed of tar heavy oil storage tank 3A top discharge mouth and water cooling tower 1 is connected; The bottom discharge on tar absorption tower 4 enters flashing tower 5 top opening for feeds, tar absorption tower 4 top spray opening for feeds are sent in the bottom liquid discharging of flashing tower 5 after the second interchanger 2B is cooling, the top gas discharge port of flashing tower 5 connects condenser 6, and cooled product enters tar light oil storage tank 3B by tar light oil storage tank 3B its top feed mouth.
600 DEG C of high-temperature biomass gas a of what biomass gasifying furnace obtained be rich in tar, are mainly flammable CO, H
2deng combustiblecomponents, contain tar macromole steam, after dedusting, first enter water cooling tower 1 through water cooling tower underfeed mouth, by tar heavy oil spraying cooling, the bottom coohng liquid First Heat Exchanger 2A that flows through, cooling liberated heat is taken away by the heat transferring medium b of First Heat Exchanger 2A; The cooling tar heavy oil obtaining, contains the heavier tar of composition and the residual oil containing more ash content, and temperature is 150 DEG C, enters tar heavy oil storage tank 3A by tar heavy oil storage tank 3A top opening for feed; In tar heavy oil storage tank 3A, to carry out standing separation and remove after residual oil c, a part is discharged by lower part outlet as tar heavy oil d product, and another part is turned back to the spray opening for feed of water cooling tower 1 by top discharge mouth, as spraying cooling medium; From the water cooling tower 1 top biological fuel gas that removes tar heavy oil out, be admitted to tar absorption tower 4 bottom feed mouths, absorption temperature is 30 DEG C; In tar absorption tower 4, tar light oil steam is absorbed agent f and fully absorbs, and enters the oil phase of absorption liquid, ammonia, hydrogen sulfide and water vapor are cooled, enter the water of absorption liquid, the tar depoint depression of the biological fuel gas e after purification is low to moderate-5 DEG C, the follow-up use procedure etching apparatus that can not condense; Be admitted to flashing tower 5 top opening for feeds from absorption liquid out at the bottom of 4 towers of tar absorption tower, utilize First Heat Exchanger 2A liberated heat to carry out heating flash evaporation through heat transferring medium b, flash vaporization point is 140 DEG C, tar absorption tower 4 top spray opening for feeds are returned in liquid absorbent f after flash distillation circulation after the heat-eliminating medium h of the second interchanger 2B is cooling, gas-phase product utilizes heat-eliminating medium h to carry out condensation in condenser 6, phlegma is entered in tar light oil storage tank 3B and is carried out oily water separation by top, obtain respectively tar light oil product i, and a small amount of deposed ammonia j; Condensation process non-condensable gases is the recycled offgas g containing a small amount of lighter hydrocarbons, and the biomass gasifying furnace that returns capable of circulation participates in gasification reaction.
Embodiment 2
As the biological fuel gas detar system of embodiment 1, biological fuel gas temperature is 600 DEG C, and tar content is 600mg/Nm
3.The cooling temperature of First Heat Exchanger is 140 DEG C; Absorption agent is n-Hexadecane, and boiling point is 287 DEG C, and tar absorption tower absorption temperature is 25 DEG C; Flashing tower service temperature is 135 DEG C.After purification, the tar depoint depression of biological fuel gas is low to moderate-5 DEG C, the follow-up use procedure etching apparatus that can not condense.
Embodiment 3
As the biological fuel gas detar system of embodiment 1, biological fuel gas temperature is 550 DEG C, and tar content is 700mg/Nm
3.The cooling temperature of First Heat Exchanger is 120 DEG C; Absorption agent is propyl benzene, and boiling point is 160 DEG C, and tar absorption tower absorption temperature is 10 DEG C; Flashing tower service temperature is 110 DEG C.After purification, the tar depoint depression of biological fuel gas is low to moderate-2 DEG C, the follow-up use procedure etching apparatus that can not condense.
As the biological fuel gas detar system of embodiment 1, biological fuel gas temperature is 550 DEG C, and tar content is 1000mg/Nm
3.The cooling temperature of First Heat Exchanger is 145 DEG C; Absorption agent is naphthalene, and boiling point is 218 DEG C, and tar absorption tower absorption temperature is 15 DEG C; Flashing tower service temperature is 136 DEG C.After purification, the tar depoint depression of biological fuel gas is low to moderate-8 DEG C, the follow-up use procedure etching apparatus that can not condense.
As the biological fuel gas detar system of embodiment 1, biological fuel gas temperature is 650 DEG C, and tar content is 900mg/Nm
3.The cooling temperature of First Heat Exchanger is 140 DEG C; Absorption agent is the mixture of dimethyl styrene (15%wt), indenes (75%wt) and certain herbaceous plants with big flowers alkane (10%wt), and boiling range is 160～190 DEG C, and tar absorption tower absorption temperature is 20 DEG C; Flashing tower service temperature is 130 DEG C.After purification, the tar depoint depression of biological fuel gas is low to moderate-3 DEG C, the follow-up use procedure etching apparatus that can not condense.
As the biological fuel gas detar system of embodiment 1, biological fuel gas temperature is 700 DEG C, and tar content is 850mg/Nm
3.The cooling temperature of First Heat Exchanger is 130 DEG C; Absorption agent is the mixture of 1-hendecene (35%wt), dimethyl ethylbenzene (10%wt) and indenes (55%wt), and boiling range is 180～210 DEG C, and tar absorption tower absorption temperature is 35 DEG C; Flashing tower service temperature is 125 DEG C.After purification, the tar depoint depression of biological fuel gas is low to moderate-7 DEG C, the follow-up use procedure etching apparatus that can not condense.
Embodiment 7
As the biological fuel gas detar system of embodiment 1, biological fuel gas temperature is 800 DEG C, and tar content is 1100mg/Nm
3.The cooling temperature of First Heat Exchanger is 120 DEG C; Absorption agent is the mixture of tetramethyl-benzene (45%wt), naphthalene (50%wt) and coumarone (5%wt), and boiling range is 200～230 DEG C, and tar absorption tower absorption temperature is 20 DEG C; Flashing tower service temperature is 110 DEG C.After purification, the tar depoint depression of biological fuel gas is low to moderate-8 DEG C, the follow-up use procedure etching apparatus that can not condense.
Embodiment 8
As the biological fuel gas detar system of embodiment 1, biological fuel gas temperature is 550 DEG C, and tar content is 1200mg/Nm
3.The cooling temperature of First Heat Exchanger is 110 DEG C; Absorption agent is the mixture of certain herbaceous plants with big flowers alkane (5%wt), pentamethylbenzene (25%wt), biphenyl (40%wt) and indoles (30%wt), and boiling range is 230～260 DEG C, and tar absorption tower absorption temperature is 30 DEG C; Flashing tower service temperature is 105 DEG C.After purification, the tar depoint depression of biological fuel gas is low to moderate-4 DEG C, the follow-up use procedure etching apparatus that can not condense.
Embodiment 9
As the biological fuel gas detar system of embodiment 1, biological fuel gas temperature is 500 DEG C, and tar content is 950mg/Nm
3.The cooling temperature of First Heat Exchanger is 120 DEG C; Absorption agent is the mixture of dimethylnaphthalene (40%wt), acenaphthene (30%wt), 1-methyl-2-ethylbenzene (5%wt) and ditane (25%wt), boiling range is 250～280 DEG C, and tar absorption tower absorption temperature is 25 DEG C; Flashing tower service temperature is 112 DEG C.After purification, the tar depoint depression of biological fuel gas is low to moderate-10 DEG C, the follow-up use procedure etching apparatus that can not condense.
Embodiment 10
As the biological fuel gas detar system of embodiment 1, biological fuel gas temperature is 600 DEG C, and tar content is 1200mg/Nm
3.The cooling temperature of First Heat Exchanger is 150 DEG C; Absorption agent is the mixture of toluene (1%wt), indoles (10%wt), dimethylnaphthalene (80%wt) and acenaphthene (9%wt), and boiling range is 260～290 DEG C, and tar absorption tower absorption temperature is 35 DEG C; Flashing tower service temperature is 145 DEG C.After purification, the tar depoint depression of biological fuel gas is low to moderate-2 DEG C, the follow-up use procedure etching apparatus that can not condense.
Embodiment 11
As the biological fuel gas detar system of embodiment 1, biological fuel gas temperature is 900 DEG C, and tar content is 850mg/Nm
3.The cooling temperature of First Heat Exchanger is 115 DEG C; Absorption agent is the mixture of acenaphthene (60%wt), fluorenes (35%wt) and quinoline (5%wt), and boiling range is 270～300 DEG C, and tar absorption tower absorption temperature is 20 DEG C; Flashing tower service temperature is 105 DEG C.After purification, the tar depoint depression of biological fuel gas is low to moderate-8 DEG C, the follow-up use procedure etching apparatus that can not condense.
Claims (5)
1. the system of a cooling-absorbing coupling deep-removing tar from biomass gas, it is characterized in that, formed by water cooling tower (1), tar absorption tower (4), flashing tower (5), First Heat Exchanger (2A), the second interchanger (2B), condenser (6), tar heavy oil storage tank (3A) and tar light oil storage tank (3B); Described water cooling tower (1) is provided with underfeed mouth, bottom discharge mouth, top discharge mouth and top spray opening for feed, tar heavy oil storage tank (3A) is provided with top opening for feed, top discharge mouth, bottom discharge mouth and bottom discharge port, tar absorption tower (4) is provided with underfeed mouth, bottom discharge mouth, top discharge mouth and top spray opening for feed, tar absorption tower (4) in-built year liquid absorbent (f); Flashing tower (5) is provided with top opening for feed, top discharge mouth and bottom discharge mouth, and tar light oil storage tank (3B) is provided with its top feed mouth, bottom discharge port and bottom discharge mouth, and condenser (6) is provided with upper air vent; Water cooling tower (1) top discharge mouth connects the underfeed mouth on tar absorption tower (4), water cooling tower (1) bottom discharge mouth and First Heat Exchanger (2A) connect, the discharge port of First Heat Exchanger (2A) connects the top opening for feed of tar heavy oil storage tank (3A), and the top spray opening for feed of the top discharge mouth of tar heavy oil storage tank (3A) and water cooling tower (1) is connected; The bottom discharge mouth on tar absorption tower (4) connects the top opening for feed of flashing tower (5), the bottom discharge mouth of flashing tower (5) connects the second interchanger (2B), the outlet of the second interchanger (2B) connects top, tar absorption tower (4) spray opening for feed, the top gas discharge port of flashing tower (5) connects condenser (6), and the outlet at bottom of condenser (6) connects its top feed mouth of tar light oil storage tank (3B).
2. one kind is utilized the technique of the cooling-absorbing coupling deep-removing tar from biomass gas of system as claimed in claim 1, concrete steps are: first the high-temperature biomass gas (a) of tar steam that what biomass gasifying furnace obtained be rich in enters water cooling tower (1) by water cooling tower (1) underfeed mouth after dedusting, tar heavy oil liquid spraying by water cooling tower (1) top spray opening for feed is cooling, cooling fluid flows into First Heat Exchanger (2A) by water cooling tower (1) bottom discharge mouth, cooling liberated heat is taken away by heat transferring medium (b), the cooling tar heavy oil obtaining enters tar heavy oil storage tank (3A) through tar heavy oil storage tank (3A) top opening for feed, in tar heavy oil storage tank (3A), tar heavy oil carries out standing separation and removes residual oil (c), residual oil (c) is discharged by tar heavy oil storage tank (3A) bottom discharge mouth, tar heavy oil (d) is discharged as product by tar heavy oil storage tank (3A) bottom discharge port, part tar heavy oil (d) returns to water cooling tower (1) by tar heavy oil storage tank (3A) top discharge mouth through water cooling tower (1) top spray opening for feed, as spraying cooling medium, from water cooling tower (1) the top discharge mouth biological fuel gas that removes tar heavy oil out, be sent to tar absorption tower (4) underfeed mouth and enter tar absorption tower (4), in tar absorption tower (4), tar light oil steam is absorbed agent (f) and fully absorbs, enter the oil phase of absorption liquid, ammonia, hydrogen sulfide and water vapor are cooled, and enter the water of absorption liquid, and the biological fuel gas (e) after purification is admitted to follow-up workshop section through tar absorption tower (4) top discharge mouth, enter flashing tower (5) from absorption liquid out at the bottom of the tower of tar absorption tower (4) by flashing tower (5) top opening for feed, utilize First Heat Exchanger (2A) liberated heat to carry out heating flash evaporation through heat transferring medium (b), absorption agent (f) after flash distillation enters the second interchanger (2B) by flashing tower (5) bottom discharge mouth, after the second interchanger (2B) is cooling, return to tar absorption tower (4) by the spray opening for feed circulation of top, tar absorption tower (4), the gas-phase product of flashing tower (5) top discharge mouth utilizes heat-eliminating medium (h) to carry out condensation in condenser (6), the liquid product of condenser (6) enters tar light oil storage tank (3B), the recycled offgas (g) of top discharge mouth, biomass gasifying furnace is returned in circulation, further participate in gasification reaction, tar light oil storage tank (3B) bottom discharge port be tar light oil product (i), bottom discharge mouth is deposed ammonia (j).
3. technique according to claim 2, the cooling temperature that it is characterized in that First Heat Exchanger (2A) is 100～150 DEG C.
4. technique according to claim 2, the absorption temperature that it is characterized in that tar absorption tower (4) is the temperature of 10～40 DEG C of environment cools media.
5. technique according to claim 2, the service temperature that it is characterized in that flashing tower (5) is 100～150 DEG C, and lower than 5～10 DEG C of the cooling temperatures of First Heat Exchanger (2A).
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| CN103087780A (en) * | 2013-02-08 | 2013-05-08 | 南京工业大学 | Multi-stage deep removing process of biomass gas tar |
| CN103333718A (en) * | 2013-03-29 | 2013-10-02 | 张晓� | Separation method for gas comprising solid dust and tar gas |
| CN104987887B (en) * | 2015-08-05 | 2017-06-27 | 华陆工程科技有限责任公司 | The method for producing coal tar and synthesis gas as raw material with rich oil coal |
| CN108753372A (en) * | 2018-07-25 | 2018-11-06 | 易高环保能源研究院有限公司 | The device and method of oil wash purification and Oil Recovery for pyrolysis gas |
| CN109504468A (en) * | 2018-12-26 | 2019-03-22 | 陕西煤业化工集团神木天元化工有限公司 | The recovery system of coal tar in a kind of pyrolysis coal gas |
| CN109456803A (en) * | 2018-12-27 | 2019-03-12 | 陕西煤业化工集团神木天元化工有限公司 | The recovery system of light components in a kind of pyrolysis coal gas |
| CN109971516A (en) * | 2019-03-25 | 2019-07-05 | 上海电气集团股份有限公司 | A kind of tar absorbent and preparation method thereof |
| JP7131460B2 (en) * | 2019-03-29 | 2022-09-06 | 三菱ケミカル株式会社 | Analysis method and analysis device for tar-containing gas |
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