CN102559282B - Separation method of mixed gas obtained by coal gasification - Google Patents
Separation method of mixed gas obtained by coal gasification Download PDFInfo
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Abstract
The invention provides a separation method of mixed gas obtained by coal gasification. The method comprises the following steps: (1) under a pressurized gasification condition, contacting crushed coal with water so as to obtain crude gas; (2) contacting the crude gas and an organic solvent so as to quench the crude gas, wherein under the condition that the crude gas is contacted with the organic solvent, the temperature of the crude gas is reduced so that the water and naphtha fraction in the crude gas are in a gas state, and the organic solvent as well as tar fraction and at least part of diesel oil fraction in the crude gas are in a liquid state; carrying out flash vaporization on a quenching product, and fractionating the quenching product which is subjected to flash vaporization and heavy tar separation, so as to separate a first liquid-phase product and a first gas-phase product from the quenching product, wherein the fractionating condition ensures that at least part of polyatomic phenol in the quenching product is contained in the first liquid-phase product; (3) cooling the obtained first gas-phase product, so as to obtain purified gas and a second liquid-phase product; and(4) carrying out oil and water separation on the obtained second liquid-phase product. The method provided by the invention can be used for greatly lowering the wastewater processing cost and improving the technical energy utilization efficiency.
Description
Technical field
The invention relates to the separation method of the gas mixture that a kind of gasification obtains.
Background technology
Coal preparing natural gas technological line is representative with the international coal preparing natural gas of big plain in u.s.a demonstration unit (having moved 20 years) and Datang project at present, mainly adopt the Shandong strange/crushed coal pressure gasifying, the oil resistant of anti-sulphur conversion, low-temperature rectisol purify and methanation.Typical process flow is divided into broken coal, coal dust and coal gangue for first coal with extraction in the colliery carries out the coal choosing, and broken coal is used for pressurized gasification.The principal reaction of crushed coal pressure gasifying is coal and water generation water-gas reaction, and product mainly is carbon monoxide, hydrogen and methane, also has the undecomposed water of part, and a spot of coal tar.The further methanation of carbon monoxide and hydrogen obtains methane gas (being SNG).The content of methane can be up to 96% in the product gas of coal preparing natural gas technology gained, calorific value 35564kJ/m
3More than.
Yet crushed coal pressure gasifying must separate to come the product raw gas to obtaining to separate by chilling.In the chilling separating technology, the general water that adopts is as refrigerant, water is directly contacted with raw gas, the material that makes all boiling points be higher than normal temperature comprises that dust all enters subsider together, collect gas-phase product, light oil flows out from the surface, and tar-bitumen is told from the lower end, the centre is the waste water that contains phenol, ammonia and oil, and oily(waste)water is mainly by the part oil phase and water is miscible forms.Come from unreacted water in the pressurized gasification reaction because water comprises, also comprise the water that comes from as the chilling agent, therefore, the amount of oily(waste)water is bigger.The aftertreatment of oily(waste)water generally handles to remove wherein coal tar by multistage sedimentation, yet, the oil that also contains nearly 1000mg/L by the water after the multistage sedimentation processing, also need further to carry out again follow-up deamination, dephenolizing process after removing a large amount of coal tar, thereby reach process water reuse or emission standard.But, because unit phenol and polyphenol are all soluble in water, be difficult to remove.The method of dephenolize at present is generally uses solvent-extracted method earlier, by solvent the phenol extraction in the waste water is come out, and the dephenolize waste water after will extracting again afterwards carries out biochemical treatment.Because the cost of biochemical treatment is than higher, and biochemical treatment has relatively high expectations to the total phenol content in the waste water, generally can not surpass 1200mg/L.In addition, biochemical treatment is lower to the removal efficiency of polyphenol and heavy tar.Therefore, generally attempt in solvent extraction process, to extract as far as possible more polyphenol.Yet, when adopting extraction agent to carry out dephenolize, can't take into account removing of polyphenol and unit phenol, and not find the extraction agent that effectively removes polyphenol at present, even if sacrificed the decreasing ratio of a large amount of unit phenol, also still can not effectivelyly remove polyphenol and heavy tar.The decreasing ratio of existing extraction process dephenolize technology general cell phenol is about 90%, and the decreasing ratio of polyphenol is about 60%.This shows that the processing of oily(waste)water not only causes the water treatment expense to increase, and more increased the difficulty of removing phenol in waste water technology.Therefore, oily(waste)water is treated as the main weak point of selecting crushed coal pressure gasifying in the coal preparing natural gas project for use.
In addition, US4324643 discloses a kind of method that is prepared stable hydro carbons by the solid particulate carbonaceous material, this method comprises 1) be enough to produce the described solid particulate carbonaceous material of thermo-cracking under the temperature and pressure condition of gas-solid mixture, described gas-solid mixture contains granular solids and hot pyrolysis gas product, and described gas products contains the above macromole hydrocarbon of 4 carbon atoms and the instant volatile hydrocarbon free radical that generates in reaction; 2) gas solid separation obtains not containing substantially the gaseous mixture of solid; 3) the described gaseous mixture that does not contain solid is substantially mixed with the quench liquid that contains end-capping reagent, the condition of chilling makes that the instant volatile hydrocarbon free radical that generates almost can all react and termination reaction with end-capping reagent simultaneously in reaction, and the condensation simultaneously of feasible most of at least described macromole hydrocarbon, thereby obtain gas and condensation and stable hydrocarbon.And the temperature that further discloses condensation especially preferably is lower than 200 °F (namely 95 ℃), and condensed fluid is mainly hydrocarbon.
Although adopt hydrocarbon can reduce the amount of water in the system to be separated as the main component of condensing agent, yet aforesaid method can not really solve the oily(waste)water problem, and the difficulty of removing phenol in waste water technology is also bigger.
Summary of the invention
The objective of the invention is in order to overcome the above-mentioned defective of prior art, the separation method of the gas mixture that a kind of new gasification obtains is provided.
In order to solve the oily(waste)water problem of above-mentioned prior art, the present inventor has carried out a large amount of discovering, by the cooling washing composition that adopts organic solvent (i.e. oil) to separate as chilling, and the cooling temperature that the control chilling separates is enough to make the water in the described raw gas to keep gaseous state and make the tarry cut in the described raw gas be liquid state, make the organism in the oily(waste)water of the generations such as tarry cut that the remaining water of gasification reaction and gasification produce enter gas phase and liquid phase respectively, in addition, under the preferred condition of the present invention, described organic solvent can be guaranteed fully separating of water and tarry cut with the raw gas contact.The more important thing is, after chilling separates, from the chilling product, separate and obtain containing tarry cut or contain tarry cut and first liquid product of at least part of diesel oil distillate and first gas-phase product that contains water and naphtha fraction, the condition of fractionation is carried out in control to the chilling product, can make at least part of polyphenol in the chilling product be in described first liquid product, and make and only contain unit phenol in the final waste water, or only contain the polyphenol of part except unit phenol, thereby reduce the intractability of waste water greatly.
The invention provides the separation method of the gas mixture that a kind of gasification obtains, wherein, this method may further comprise the steps:
(1) under the pressurized gasification condition, broken coal is contacted with water, obtain a kind of raw gas, described raw gas contains synthetic gas, naphtha fraction, diesel oil distillate, tarry cut and water;
(2) the gained raw gas contacted with organic solvent carry out chilling, the condition that described raw gas contacts with organic solvent make the temperature of described raw gas be reduced to be enough to make water in the described raw gas and naphtha fraction to keep gaseous state and make tarry cut in described organic solvent, the raw gas and at least part of diesel oil distillate for liquid; The chilling product is carried out flash distillation, the condition of flash distillation makes from the chilling product and isolates heavy tar, chilling product after the flash distillation, that isolate behind the heavy tar is carried out fractionation, separate obtaining containing tarry cut or containing tarry cut and first liquid product of at least part of diesel oil distillate and first gas-phase product that contains water and naphtha fraction from the chilling product, the condition of described fractionation makes at least part of polyphenol in the chilling product be in described first liquid product; Described organic solvent is the inert organic solvents miscible with diesel oil distillate and/or tarry cut, and the initial boiling point of described organic solvent is higher than the boiling point of water; From the chilling product isolated contain tarry cut or contain tarry cut and first liquid product of at least part of diesel oil distillate in contain described organic solvent;
First gas-phase product cooling that (3) will obtain obtains purified gas and second liquid product;
Second liquid product that (4) will obtain carries out oily water separation.
The cooling washing composition of the separation method of the gas mixture that gasification provided by the invention obtains by adopting organic solvent to separate as chilling, and the temperature of control chilling separation, make the tar that causes forming oily(waste)water be cooled to different phases respectively with water, be separated with realization, control the condition when the chilling product carried out fractionation simultaneously, make at least part of polyphenol in the chilling product directly enter in first liquid product, and make and only containing unit phenol to from first gas-phase product that contains water and naphtha fraction, separating in the waste water that second liquid product that obtains carries out obtaining after the oily water separation, or only contain the part polyphenol except unit phenol, thereby greatly reduce the intractability of waste water, simultaneously, the oil quality of the lightweight oil that obtains after the oily water separation has also obtained remarkable improvement.This shows, adopt method provided by the invention can reduce the cost of wastewater treatment greatly, and improve the oil quality of the lightweight oil that obtains.In addition, adopt method of the present invention, earlier the chilling product is carried out flash distillation to isolate heavy tar from the chilling product, again the chilling product is carried out tarry cut that fractionation obtains when returning the oil quenching reactor as oil quenching with organic solvent, can avoid repeatedly the circulating problem of the pipeline scale that causes, because heavy tar is removed, thereby improved as the character of oil quenching with the tarry cut of organic solvent, improved the cyclically utilizing effect of quenching oil, in addition, tarry cut is carried out returning the energy utilization efficiency that has also improved process unit simultaneously again after the heat exchange through interchanger.Method provided by the invention can be used for the various separation that can produce the pressurized gasification product of oily(waste)water problem.
Description of drawings
Fig. 1 is the technology boiling range figure of separation method provided by the invention.
Embodiment
According to method provided by the invention, the chilling product is being carried out fractionation, from the chilling product, separate and obtain containing tarry cut or to contain tarry cut and first liquid product of at least part of diesel oil distillate and when containing first gas-phase product of water and naphtha fraction, the condition of described fractionation need guarantee to make at least part of polyphenol in the chilling product, the polyphenol of preferred at least 80 weight %, more preferably the polyphenol of 90-100 weight % is in described first liquid product, and make finally and only to contain unit phenol to from first gas-phase product that contains water and naphtha fraction, separating in the waste water that second liquid product that obtains carries out obtaining after the oily water separation, or only contain the part polyphenol except unit phenol, thereby greatly reduce the intractability of waste water.
Total phenol in the waste water comprises that Volatile Phenols (namely, unit phenol, unit phenol refers to have only on the aromatic ring aldehydes matter of a hydroxyl that directly links to each other) and non-volatile phenol is (namely, polyphenol, polyphenol refers to that aromatic ring has the aldehydes matter of the hydroxyl that directly links to each other more than), the content of described Volatile Phenols (unit phenol) is generally 3000-4500mg/L, and the content of non-volatile phenol (polyphenol) is generally 1500-2000mg/L.
Wherein, described aldehydes matter mainly comprises phenol, cresols, naphthols and their derivative, as 2,5-xylenol, 2,4-xylenol, 2-propylene phenol, 3-ethyl-5 methylphenol, 2-ethyl-5-methylphenol, 3,5-xylenol, ortho-methyl phenol, 2-methyl hydroquinone, 2-methylresorcinol, 3-methyl pyrocatechol, 2-ethylphenol, 3-ethylphenol, 4-ethylphenol, p-methyl phenol, m-methyl phenol, naphthyl alcohol, 2-methyl isophthalic acid-naphthols.
The mensuration of described total phenol content and the measuring method of volatile phenol concentrations presented are as well known to those skilled in the art.For example, the mensuration of total phenol content can be with reference to " water and effluent monitoring analytical procedure " the 4th edition, and State Environmental Protection Administration writes, and the China Environmental Science Press publishes; The mensuration of described volatile phenol concentrations presented can be with reference to GB 7491-87 or HZ 502-2009, and total phenol content deducts the content that volatile phenol concentrations presented is substantially equal to non-volatile phenol, perhaps adopts gas-chromatography (GCMS) to measure the content of non-volatile phenol.
According to the present invention, because the boiling point of polyphenol is generally more than 230 ℃, and under fractionation conditions of the present invention, the boiling range of naphtha fraction is generally 45-180 ℃, and the boiling range of diesel oil distillate is generally 160-300 ℃, and the boiling range of tarry cut is generally 200-520 ℃.Therefore, for the polyphenol that guarantees there is not polyphenol in the waste water or only contain minute quantity, just need the temperature of control fractionation, make in the tarry cut at the bottom of polyphenol is retained in the fractionation Tata, and can be with water and separated not the going out of first gas-phase product of containing naphtha fraction.
According to the present invention, the chilling product is carried out fractionation, from the chilling product, separate and obtain containing tarry cut or to contain tarry cut and first liquid product of at least part of diesel oil distillate and the method that contains first gas-phase product of water and naphtha fraction comprise the chilling product is sent in the separation column, adopt first gas-phase product contain water and naphtha fraction from cat head, extraction contains tarry cut or contains tarry cut and first liquid product of at least part of diesel oil distillate at the bottom of the tower.
Under the preferable case, the condition of described fractionation comprises that pressure is the 2-6 MPa, is preferably the 2-4 MPa; The temperature of cat head can be 160-240 ℃, is preferably 170-210 ℃; Temperature at the bottom of the tower is 260-320 ℃, is preferably 280-300 ℃.Separate first gas-phase product obtain containing water and naphtha fraction from cat head, separate obtaining containing tarry cut or containing tarry cut and first liquid product of at least part of diesel oil distillate at the bottom of the tower.
According to the present invention, described fractionation conditions can also comprise reflux ratio, and described reflux ratio can be 1-5: 1, be preferably 1-3: 1.
According to the present invention, described separation column can be packing tower, also can be tray column, can also be filler and board-like compound tower.
The filler that loads in the described packing tower can be for well known to a person skilled in the art various fillers, and for example this filler can be selected from one or more in Raschig ring, Pall ring, cascade ring, saddle type ring, arc saddle type, square saddle type, Dixon ring, Cannon ring, Lamb wave line and the net corrugated regular filler.
In bubble-cap, sieve plate, inclined hole, the float valve one or more can be installed in described tray column.
In order to obtain desirable separating effect, described separation column preferably has certain stage number or theoretical plate number, and for example, its stage number or theoretical plate number can be the 6-18 piece, are preferably the 8-13 piece.
According to the present invention, described separation column can adopt and well known to a person skilled in the art various separation columns, and for example, described separation column can be made of body of the tower, tower reactor, tower reactor reboiler, cat head water cooler and return tank of top of the tower (phase-splitting).
Under the preferable case, this method also is included in separation column at least one side line extraction mouth is set, for example, at least one side line extraction mouth is set in middle part, bottom or the middle and lower part of separation column, and the extraction diesel oil distillate, in order to take out the part heat at side line, and diesel oil distillate is passed through the interchanger heat exchange, part diesel oil distillate after the heat exchange is looped back the cat head of separation column, with the diesel oil distillate of remainder as the product extraction.
Boiling range scope according to diesel oil distillate, the extraction temperature of described diesel oil distillate can be 260-300 ℃, after the interchanger heat exchange, can take out the part heat by interchanger, and the part diesel oil distillate after the heat exchange looped back the cat head of separation column, the temperature of the described part diesel oil distillate that returns can be 180-220 ℃.
The number of described side line extraction mouth can be offered as required, for example, can be 1-3.The ratio of described side line produced quantity can change between 0-100%, that is, can extraction regulate to all by the side line extraction at the bottom of all by tower.For example, can make the part diesel oil distillate after the heat exchange is looped back in the separation column by side reflux, with the diesel oil distillate of remainder as the sideline product extraction.
Described interchanger can be interchanger arbitrarily known in those skilled in the art, and for example plate-type heat exchanger, shell-and-plate(heat)exchanger, shell and tube heat exchanger, vapour generator, bevel plate heat exchanger etc. are preferably vapour generator.
According to the present invention, in order to be beneficial to energy optimization more, this method also comprise with contain tarry cut or contain tarry cut and first liquid product of at least part of diesel oil distillate by the interchanger heat exchange, first liquid product after the heat exchange is as the organic solvent of step (2).Namely, to be back to before the chilling separator by first liquid product that obtains at the bottom of the fractionation Tata, carry out heat exchange by interchanger, can take out the part heat on the one hand, on the other hand, first liquid product can be returned the chilling separator and be used for quench step as the chilling agent.The taking-up temperature of described first liquid product, the temperature that namely enters interchanger is generally column bottom temperature, and namely 260-320 ℃, be preferably 260-300 ℃, temperature after the heat exchange, namely heat exchanger outlet temperature can be 160-180 ℃.For the form heat removal with steam, described interchanger is preferably vapour generator.
According to the present invention, the purpose of described flash distillation is to isolate heavy tar from the chilling product, then again with after the flash distillation, isolate chilling product behind the heavy tar and carry out tarry cut that fractionation obtains when returning the oil quenching reactor as oil quenching with organic solvent, can avoid repeatedly the circulating problem of the pipeline scale that causes, because heavy tar is removed, thereby improved as the character of oil quenching with the tarry cut of organic solvent, improved the cyclically utilizing effect of quenching oil.Under the preferable case, the condition of described flash distillation can comprise that the temperature of flash distillation can be 280-320 ℃, and the pressure difference of flash distillation can be 10-80kpa.Wherein, described heavy tar is the higher heavy tar cut of the boiling point in the tarry cut, and its boiling range is generally 450-540 ℃.
Among the present invention, the starting temperature of described raw gas is not particularly limited, and is generally 350-750 ℃, is preferably 350-650 ℃; Pressure is generally the 1-8 MPa, is preferably the 2-6 MPa, more preferably the 2-4 MPa.Among the present invention, described raw gas is preferably the crushed coal pressure gasifying product especially.In the described raw gas, be benchmark with the total amount of synthetic gas and tar, the content of synthetic gas is generally 80-99 weight %, is preferably 80-95 weight %, and the content of tar is generally 0.1-20 weight %, is preferably 0.5-15 weight %.The content of described water is the 10-60 weight % of described raw gas, is preferably 15-50 weight %.
Among the present invention, the main component of the synthetic gas in the described raw gas is carbon monoxide and hydrogen, also comprises the component that is gaseous state under the normal temperature such as methane, ethane, propane, isopropyl alkane, carbonic acid gas, hydrogen sulfide, ammonia, N in addition
2In one or more.Among the present invention, described tar is continued to use the definition of this area routine, expression boiling point height, the thick coal tar that viscosity is big.Except water, synthetic gas and tar, also comprise in the described raw gas under the normal temperature for liquid liquid ingredient such as phenol, biphenol, formic acid, gasoline, boiling point being lower than in 180 ℃ the petroleum naphtha one or more.Therefore these components all can gasify under the condition of described contact owing to more volatile, all will escape in the gas-phase product with gas form.
According to separation method provided by the invention, although as long as the condition of described contact makes the temperature of described raw gas be reduced to than making the water in the described raw gas keep the temperature required height of gaseous state, and the boiling point than tar is low, can realize that water and tar are respectively with different existing mutually, and realize being separated, thereby realize purpose of the present invention.But under the preferable case, in order to guarantee that fully whole water all enter in the gas-phase product with gaseous state, the condition of described contact makes the temperature of described raw gas be reduced to than making water in the described raw gas keep the temperature of at least 1 ℃ of the temperature required height of gaseous state, preferred high 1-200 ℃ temperature, further preferred high 1-100 ℃ temperature, further preferred high 5-50 ℃.
According to the present invention, the condition of described contact comprises the temperature of organic solvent, consumption, and the weight ratio of organic solvent and raw gas and duration of contact.Above-mentioned condition makes the tarry cut in the raw gas get final product for liquid as long as guarantee to make that the temperature of described raw gas is reduced to the water maintenance gaseous state that is enough to make in the described raw gas.Under the preferable case, the temperature of described organic solvent can be 70-200 ℃, is preferably 80-180 ℃; The consumption of organic solvent generally can be 1-10 times of described raw gas weight, and under the preferable case, the consumption of described organic solvent is 2-8 times of described raw gas weight; The time of contact can be 10-120 second, is preferably 10-100 second.
According to the present invention, the condition of controlling described contact makes the temperature of described raw gas be reduced to 280-340 ℃, preferably make the temperature of described raw gas be reduced to the 300-320 ℃ of water maintenance gaseous state that namely can satisfy to make in the described raw gas, it is liquid making the tarry cut in the raw gas, guarantees the water oil separating simultaneously.
Owing to make the water in the described raw gas keep gaseous state temperature required closely related with pressure, make the water in the described raw gas keep gaseous state temperature required also different under the different pressures.When the pressure of the preferred described raw gas of the present invention was the 1-8 MPa, the condition of controlling described contact made the temperature of described raw gas be reduced to 280-340 ℃.Further under the preferable case, the pressure of described raw gas is the 2-6 MPa, more preferably during the 2-4 MPa, the condition of described contact makes the temperature of described raw gas be reduced to 300-320 ℃.
According to the present invention, although the temperature to the organic solvent that contacts with raw gas is not particularly limited, under the preferable case, the temperature of the organic solvent that control contacts with described raw gas is 70-200 ℃, time is 10 seconds to 120 seconds, can obtain first gas-phase product and first liquid product, reach purpose of the present invention.More preferably under the situation, in order further to improve separating of coal tar and water in the raw gas, the condition that described raw gas contacts with organic solvent comprises that the temperature of organic solvent is 80-180 ℃, and the time is 10-100 second, further preferred temperature is 80-150 ℃, and the time is 20-50 second.
In above-mentioned scope particularly in the optimum condition scope, can prevent on the one hand because the temperature of organic solvent is low excessively, the gas mixture and the heat exchange between the organic solvent that contain tar are too rapid, contacting between the gas mixture that contains tar that causes and the organic solvent may be abundant inadequately, thereby dissolving or the moisture that is included in the tar of the gas mixture that contains tar may have little time to overflow from tar, and be separated with water in oil liquid phase emulsion droplet form and the gas phase composition of having overflowed, thereby be unfavorable for fully separating of tar and water, can also prevent on the other hand because the temperature of organic solvent is too high, the gas mixture and the heat exchange between the organic solvent that contain tar are too slow, the gas mixture that contains tar that causes may be in the condition of high temperature for a long time, and owing to contain a large amount of unsaturated hydrocarbons in the tar, further polymerization takes place in these unsaturated hydrocarbons easily under the above-mentioned condition of high temperature, cause the viscosity of tar to increase, formation is more prone to Jiao of thickness attitude, and the content of oil then further reduces.That is, can make to guarantee that before the chilling product is sent into separation column system's waste water oleaginousness is down to below the 200mg/L, even be low to moderate below the 50mg/L.In addition, if though not in above-mentioned optimum condition scope the time, the water oleaginousness may not reach below the 200mg/L behind the oil quenching, but, after the chilling product is carried out fractionation, the water quality of the waste water after the processing that obtains still can reach requirement of the present invention, and namely the oleaginousness in the waste water also can remain on below the 50mg/L.
In order to reduce the load that step (2) gas-phase product of winning is carried out cooling for the second time and oily water separation, the preferred described organic solvent of the present invention for can with step (2) the miscible inert organic solvents of the liquid product of winning, and the boiling point of described organic solvent is higher than the boiling point of water.Like this, after the chilling cooling, enter in the liquid phase a part as liquid product as the organic solvent of refrigerant.In addition, by use can with step (2) the miscible inert organic solvents of the liquid product of winning, can also make this organic solvent serve as washing composition simultaneously, tar is washed from the high-temperature gasification product separates, thereby more be conducive to separating of water and tar.Further under the preferable case, the boiling point of described organic solvent is than the high 50-200 of boiling point ℃ of water.Described organic solvent can be single solvent, also can be the mixed solvent of multiple organic solvent.Industrial preferred use boiling range as in 200-520 ℃ coal tar, hydrocracking tail oil, diesel oil and the wax oil one or more as described refrigerant, preferred organic solvent is the coal tar that the washing refrigerated separation is got off in the described raw gas, first liquid product that also is about to described step (2) gained partly or entirely is used as the refrigerant of chilling next time, can reduce the amount of outsourcing oil so on the one hand, save production cost, first liquid product that has also solved step (2) gained on the other hand is the emission problem of tar, and is beneficial to energy optimization.That is, this method also comprises containing tarry cut or containing tarry cut and first liquid product of at least part of diesel oil distillate returns step (2), contacts with the gained raw gas as organic solvent raw gas is carried out chilling.That is, described organic solvent is that isolated from the chilling product that step (2) obtains contains tarry cut or contain tarry cut and first liquid product of at least part of diesel oil distillate.
Among the present invention, described inert organic solvents refer under separation condition not with system to be separated in material chemical reaction further takes place or self do not take place under separation condition or the material of polymerization reaction take place not substantially.
According to method provided by the invention, the mode of described contact can be the various cooling ways of contact, for example, can or and flow contact or adverse current and flow the mode of carrying out simultaneously for counter current contact.
For the organic solvent as quenching oil is fully contacted with raw gas, effectively carry out heat exchange, washing, the present invention preferably can make quenching oil contact with raw gas with vaporific form by accessory in liquid distributor or spraying gun or other tower containers.
According to method provided by the invention, with first gas-phase product further cooling be for water, synthetic gas and light oil are separated, therefore the temperature of cooling preferably is cooled to 10-60 ℃ so that water can cool off is as the criterion, further preferably 20-50 ℃.Can realize simultaneously separating of gaseous fraction, oil phase and water like this, improve separation efficiency and organic yield.
Because the present invention only relates to the improvement to the separation method of pressurized gasification product, therefore, the preparation method of described raw gas can be method well known in the art, for example, can adopt crushed coal pressure gasifying method well known in the art to obtain.Described broken coal can be that size is not less than 5 millimeters various broken coal pieces, and for example size is the broken coal piece of 2-50 millimeter.Described pressurized gasification condition comprises that outlet rough coal gas temperature is 350-750 ℃, is preferably 350-650 ℃, and pressure can be the 1-8 MPa, is preferably the 2-6 MPa, more preferably the 2-4 MPa.Described pressurized gasification can carry out in the various vapourizing furnaces known in the art, for example, carries out in lurgi gasifier or the crushed coal pressurized-gasification furnace.
According to a kind of embodiment of the present invention, the separation method of the gas mixture that described gasification obtains as shown in Figure 1.Raw gas is directly contacted with organic solvent in gas-liquid separator such as chilling separator, obtain containing gas water gaseous product and contain the chilling product of the liquid product of tarry cut, composition in the described gas mixture that contains tar except tar as the component that is gaseous state under water and the normal temperature substantially or all as described in the gaseous product, whole or most tar are in described liquid product, the chilling product is carried out flash distillation, and isolate the heavy tar cut, with after the flash distillation, the chilling product of isolating behind the heavy tar carries out fractionation in separation column, obtain containing first gas-phase product of water and naphtha fraction from cat head, contain tarry cut or contain tarry cut and first liquid product of at least part of diesel oil distillate at the bottom of tower, the condition of described fractionation makes at least part of polyphenol in the chilling product be in described first liquid product; From the chilling product isolated contain tarry cut or contain tarry cut and first liquid product of at least part of diesel oil distillate in contain described organic solvent; After further heat exchange is namely cooled off in water wash column with described first gas-phase product, coal gas after being purified (mainly being the component that is gaseous state under the normal temperature) and second liquid product (mainly being water and lightweight oil), by further oily water separation, obtain water and lightweight oil.Described first liquid product by interchanger, is carried out heat exchange as vapour generator, and first liquid product after the heat exchange is returned in the chilling separator; In addition, at separation column at least one side line extraction mouth is set, for example, in separation column, the bottom arranges at least one side line extraction mouth, the extraction diesel oil distillate, and with diesel oil distillate by the interchanger heat exchange, the part diesel oil distillate after the heat exchange is looped back in the separation column by side reflux, with the diesel oil distillate of remainder as the product extraction.
The following examples will the present invention is described further.
Embodiment 1
This embodiment is for the separation method that the gas mixture that gasification provided by the invention obtains is described.
Adopt technology shown in Figure 1, water vapor is carried out pressurized gasification with big or small sending at 1: 1 with weight ratio for the brown coal broken coal of 5-50 millimeter (relevant rerum natura sees table 1 for details) in the vapourizing furnace, the bottom temp of vapourizing furnace is 1200 ℃, head temperature is 500 ℃, base pressure is 3.5MPa, top pressure is 3MPa, obtain pressure and be 3MPa, temperature and be the gas mixture that 500 ℃ crushed coal pressure gasifying product namely contains tar and discharge (composition outside dewatering is as shown in table 2, and the content of water is 30 weight % of crushed coal pressure gasifying product total amount) from top of gasification furnace.
Be 3 MPas with this pressure then, temperature is that 500 ℃ crushed coal pressure gasifying product is 100 ℃ with 1000 kilograms/hour flow and temperature, boiling range is 200-500 ℃, flow is that 2800 kilograms/hour coal tar contacts in the chilling separator, contact (condition of contact makes the temperature of described raw gas be reduced to 320 ℃) after 25 seconds, the chilling product is carried out flash distillation, the temperature of flash distillation is 320 ℃, the pressure difference of flash distillation is 20kPa, from the chilling product, isolate heavy tar, with after the flash distillation, isolating chilling product behind the heavy tar sends into and carries out fractionation in the separation column, the operational condition of separation column comprises that pressure is 3 MPas, tower top temperature is 196 ℃, the tower reactor temperature is 300 ℃, reflux ratio is 3: 1, and stage number is 13.
First liquid product is discharged at the bottom of tower, first gas-phase product is overflowed from cat head, and first gas-phase product is sent in the subsider coal gas after the collection and purification after further being cooled to 50 ℃ by water wash column, liquid in the subsider is left standstill natural layering, isolate wherein water and oil phase.The result is that water is transparent, and oleaginousness is 35mg/L, and polyphenol content is 200mg/L, and unit phenol content is 3000mg/L.First liquid product at the bottom of the tower learns that by analysis water content is 0.2 weight %.
Described first liquid product is carried out heat exchange by vapour generator (temperature in is 300 ℃, and temperature out is 180 ℃), and steam takes place, and first liquid product after the heat exchange is returned in the chilling separator; In addition, a side line extraction mouth is set in the middle and lower part of separation column, extraction diesel oil distillate (the extraction temperature is 280 ℃), and with diesel oil distillate by the interchanger heat exchange, part after the heat exchange (50%) diesel oil distillate is looped back the cat head of separation column, with the diesel oil distillate of remainder as the product extraction.
Embodiment 2
This embodiment is for the separation method that the gas mixture that gasification provided by the invention obtains is described.
Adopt technology shown in Figure 1, water vapor is carried out pressurized gasification with big or small sending at 1: 1 with weight ratio for the brown coal broken coal of 5-50 millimeter (relevant rerum natura sees table 1 for details) in the vapourizing furnace, the bottom temp of vapourizing furnace is 1000 ℃, head temperature is 300 ℃, base pressure is 3MPa, top pressure is 2.5MPa, the crushed coal pressure gasifying product that obtains pressure and be 2.5 MPas, temperature and be 300 ℃ is discharged (composition outside dewatering is as shown in table 2, and the content of water is 50 weight % of crushed coal pressure gasifying product total amount) from the top.
Be 2.5 MPas with this pressure then, temperature is that 300 ℃ crushed coal pressure gasifying product is 150 ℃ with 1500 kilograms/hour flow and temperature, boiling range is 280-480 ℃, flow is that 2200 kilograms/hour hydrocracking tail oil contacts in the chilling separator, contact (condition of contact makes the temperature of described raw gas be reduced to 300 ℃) after 40 seconds, the chilling product is carried out flash distillation, the temperature of flash distillation is 300 ℃, the pressure difference of flash distillation is 35kPa, from the chilling product, isolate heavy tar, with after the flash distillation, isolating chilling product behind the heavy tar sends into and carries out fractionation in the separation column, the operational condition of separation column comprises that pressure is 2 MPas, tower top temperature is 170 ℃, the tower reactor temperature is 280 ℃, reflux ratio is 2: 1, and stage number is 10.First liquid product is discharged at the bottom of tower, first gas-phase product is overflowed from cat head, gas-phase product is sent in the subsider after further being cooled to 40 ℃ by water wash column, coal gas after the collection and purification leaves standstill natural layering with the liquid in the subsider, isolates wherein water and oil phase, the discovery water is transparent, oleaginousness is 20mg/L, and polyphenol content is 10mg/L, and unit phenol content is 3000mg/L.Liquid product learns that by analysis water content is 0.3 weight % at the bottom of the tower.
Described first liquid product is carried out heat exchange by vapour generator (temperature in is 280 ℃, and temperature out is 190 ℃), and steam takes place, and first liquid product after the heat exchange is returned in the chilling separator; In addition, a side line extraction mouth is set in the bottom of separation column, extraction diesel oil distillate (the extraction temperature is 265 ℃), and with diesel oil distillate by the interchanger heat exchange, part after the heat exchange (30%) diesel oil distillate is looped back the cat head of separation column, with the diesel oil distillate of remainder as the product extraction.
Embodiment 3
This embodiment is for the separation method that the gas mixture that gasification provided by the invention obtains is described.
Adopt technology shown in Figure 1, water vapor is carried out pressurized gasification with big or small sending at 1: 1 with weight ratio for the brown coal broken coal of 5-50 millimeter (relevant rerum natura sees table 1 for details) in the vapourizing furnace, the bottom temp of vapourizing furnace is 1300 ℃, head temperature is 650 ℃, base pressure is 4MPa, top pressure is 3.5MPa, the crushed coal pressure gasifying product that obtains pressure and be 3.5 MPas, temperature and be 650 ℃ is discharged (composition outside dewatering is as shown in table 2, and the content of water is 20 weight % of crushed coal pressure gasifying product total amount) from the top.
Be 3.5 MPas with this pressure then, temperature is that 650 ℃ crushed coal pressure gasifying product is 80 ℃ with 800 kilograms/hour flow and temperature, boiling range is 200-500 ℃, flow is that 2500 kilograms/hour coal tar contacts in the chilling separator, contact (condition of contact makes the temperature of described raw gas be reduced to 340 ℃) after 30 seconds, the chilling product is carried out flash distillation, the temperature of flash distillation is 340 ℃, the pressure difference of flash distillation is 50kPa, from the chilling product, isolate heavy tar, with after the flash distillation, isolating chilling product behind the heavy tar sends into and carries out fractionation in the separation column, the chilling product sent into carry out fractionation in the separation column, the operational condition of separation column comprises that tower top pressure is 4 MPas, tower top temperature is 220 ℃, the tower reactor temperature is 325 ℃, reflux ratio is 4: 1, and stage number is 8.First liquid product is discharged at the bottom of tower, first gas-phase product is overflowed from cat head, first gas-phase product is sent in the subsider after further being cooled to 40 ℃ by water wash column, coal gas after the collection and purification leaves standstill natural layering with the liquid in the subsider, isolates wherein water and oil phase, the discovery water is transparent, oleaginousness is 50mg/L, and polyphenol content is 800mg/L, and unit phenol content is 3000mg/L.Liquid product is learnt water content 0.4 weight % by analysis at the bottom of the tower.
Described first liquid product is carried out heat exchange by vapour generator (temperature in is 325 ℃, and temperature out is 200 ℃), and steam takes place, and first liquid product after the heat exchange is returned in the chilling separator; In addition, two side line extraction mouths are set in the bottom of separation column, difference extraction diesel oil distillate (the extraction temperature is 290 ℃), and with diesel oil distillate by the interchanger heat exchange, part after the heat exchange (80%) diesel oil distillate is looped back the cat head of separation column, with the diesel oil distillate of remainder as the product extraction.
Embodiment 4
This embodiment is used for explanation separation method provided by the invention.
Method according to embodiment 1 is obtained synthetic gas, and different is, the temperature of coal tar is 50 ℃, and the time of contact is 10 seconds, obtains gaseous fraction, water and oil phase, and wherein, water is not really transparent, and its oleaginousness is 500mg/L.The water that gained chilling product is carried out obtaining after the fractionation remains transparent, and oleaginousness is 35mg/L, and polyphenol content is 200mg/L, and unit phenol content is 2500mg/L.
Table 1
Annotate:
War---represent coal-fired as received basis moisture; Wad---the coal-fired dry basic moisture of expression; Har---represent coal-fired as received basis hydrogen branch; Aad---the coal-fired dry basic ash content of expression; Vad---the coal-fired dry basic volatile matter of expression; Sad---the coal-fired dry basic sulphur content of expression; Car---represent coal-fired as received basis carbon branch; Oar---represent coal-fired as received basis oxygen branch; Nar---represent coal-fired as received basis nitrogen branch; Sar---represent coal-fired as received basis sulphur content; T1---softening temperature, ℃; T2---hemispherical temperature, ℃; T3---melt temperature, ℃.
Table 2
| Form (weight %) | Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 |
| H 2 | 3.59 | 3.61 | 3.58 | 3.59 |
| CO | 19.68 | 19.75 | 19.56 | 19.68 |
| C0 2 | 62.88 | 63.09 | 62.71 | 62.88 |
| CH 4 | 7.57 | 7.35 | 7.65 | 7.57 |
| N 2 | 0.34 | 0.34 | 0.34 | 0.34 |
| C 2 | 0.39 | 0.36 | 0.39 | 0.39 |
| C 3 | 0.39 | 0.35 | 0.39 | 0.39 |
| H 2S | 0.50 | 0.50 | 0.51 | 0.50 |
| NH 3 | 0.17 | 0.17 | 0.17 | 0.17 |
| HCN | 0.01 | 0.01 | 0.01 | 0.01 |
| With C 6H 6The O meter, unit phenol content | 0.39 | 0.39 | 0.39 | 0.39 |
| With C 6H 6O 2Meter, polyphenol content | 0.26 | 0.26 | 0.26 | 0.26 |
| Boiling point is less than 180 ℃ cut | 0.41 | 0.38 | 0.41 | 0.41 |
| Boiling point is 180-360 ℃ cut | 1.60 | 1.57 | 1.70 | 1.60 |
| Boiling point is greater than 360 ℃ cut | 1.82 | 1.87 | 1.93 | 1.82 |
| ∑ | 100.00 | 100.00 | 100.00 | 100.00 |
| The oil product total amount | 4.48 | 4.47 | 4.69 | 4.48 |
Claims (15)
1. the separation method of the gas mixture that obtains of a gasification is characterized in that this method may further comprise the steps:
(1) under the pressurized gasification condition, broken coal is contacted with water, obtain a kind of raw gas, described raw gas contains synthetic gas, naphtha fraction, diesel oil distillate, tarry cut and water;
(2) the gained raw gas is contacted with organic solvent carry out chilling, the condition that described raw gas contacts with organic solvent makes the temperature of described raw gas be reduced to be enough to make water and the naphtha fraction maintenance gaseous state in the described raw gas and to make tarry cut and at least part of diesel oil distillate in described organic solvent, the raw gas be liquid state, and the condition that described raw gas contacts with organic solvent makes the temperature of described raw gas be reduced to than making the water in the described raw gas keep at least 1 ℃ of the temperature required height of gaseous state; The chilling product is carried out flash distillation, the condition of flash distillation makes from the chilling product and isolates heavy tar, with after the flash distillation, the chilling product of isolating behind the heavy tar carries out fractionation, from the chilling product, separate and obtain containing tarry cut or contain tarry cut and first liquid product of at least part of diesel oil distillate and first gas-phase product that contains water and naphtha fraction, the method that the chilling product is carried out fractionation comprises to be sent into the chilling product in the separation column, first gas-phase product that contains water and naphtha fraction from the cat head extraction, extraction contains tarry cut or contains tarry cut and first liquid product of at least part of diesel oil distillate at the bottom of the tower, the condition of described fractionation makes at least part of polyphenol in the chilling product be in described first liquid product, the condition of described fractionation comprises: pressure is the 2-6 MPa, the temperature of cat head is 160-240 ℃, and the temperature at the bottom of the tower is 260-320 ℃; Described organic solvent is the inert organic solvents miscible with diesel oil distillate and/or tarry cut, and the initial boiling point of described organic solvent is higher than the boiling point of water; From the chilling product isolated contain tarry cut or contain tarry cut and first liquid product of at least part of diesel oil distillate in contain described organic solvent;
First gas-phase product cooling that (3) will obtain obtains purified gas and second liquid product;
Second liquid product that (4) will obtain carries out oily water separation.
2. method according to claim 1, wherein, the condition of described fractionation makes the polyphenol of at least 80 weight % in the chilling product be in described first liquid product.
3. method according to claim 2, wherein, the condition of described fractionation makes the polyphenol of the 90-100 weight % in the chilling product be in described first liquid product.
4. method according to claim 1, wherein, the condition of described fractionation comprises: pressure is the 2-4 MPa, and the temperature of cat head is 180-210 ℃, the temperature at the bottom of the tower is 280-300 ℃.
5. method according to claim 1, wherein, this method also is included in separation column at least one side line extraction mouth is set, and extraction diesel oil distillate, and with diesel oil distillate by the interchanger heat exchange, part diesel oil after the heat exchange is looped back in the separation column by side reflux, with the diesel oil distillate of remainder as the sideline product extraction.
6. method according to claim 1, wherein, the water that the condition that described raw gas contacts with organic solvent makes the temperature of described raw gas be reduced to and makes in the described raw gas keeps temperature required high 1-100 ℃ of gaseous state.
7. according to claim 1 or 6 described methods, wherein, the condition of described contact makes the temperature of described raw gas be reduced to 280-340 ℃.
8. method according to claim 7, wherein, the condition of described contact makes the temperature of described raw gas be reduced to 300-320 ℃.
9. according to claim 1 or 6 described methods, wherein, the temperature of described raw gas is 350-750 ℃, and pressure is the 1-8 MPa; The condition of described contact comprises that the temperature of organic solvent is 70-200 ℃, and the consumption of organic solvent is 1-10 times of described raw gas weight, and the time of contact is 10-120 second.
10. method according to claim 9, wherein, the temperature of described raw gas is 350-650 ℃, pressure is the 2-6 MPa; The temperature of organic solvent is 80-180 ℃, and the consumption of organic solvent is 2-8 times of described raw gas weight, and the time of contact is 10-100 second.
11. according to claim 1 or 6 described methods, wherein, described organic solvent is that boiling range is one or more in 200-520 ℃ coal tar, diesel oil and the hydrocracking tail oil.
12. method according to claim 1, wherein, this method also comprise with contain tarry cut or contain tarry cut and first liquid product of at least part of diesel oil distillate by the interchanger heat exchange, first liquid product after the heat exchange is as the organic solvent of step (2).
13. method according to claim 12, wherein, described interchanger is vapour generator.
14. method according to claim 1, wherein, the condition of flash distillation comprises that the temperature of flash distillation is 280-320 ℃, and the pressure difference of flash distillation is 10-80kpa.
15. method according to claim 1, wherein, described broken coal is that size is that the coal cinder of 2-50 millimeter, the condition of described pressurized gasification comprise that gas outlet temperature is 350-750 ℃, and pressure is the 1-8 MPa.
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