CN102021044B - Method for acquiring synthesis gas by pressurizing crushed coal - Google Patents
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Abstract
The invention discloses a method for acquiring synthesis gas by pressurizing coal, comprising the following steps of: (1) contacting crushed coal with water under the condition of pressurized gasification to obtain raw coal gas; (2) contacting the obtained raw coal gas with an organic solvent and quenching, wherein the raw coal gas contains synthesis gas, tar and water, the boiling point of the tar is higher than that of the water, the contact condition between the raw coal gas and the organic solvent lowers the temperature of the raw coal gas to ensure that water in the raw coal gas is kept in a gaseous state and the tar in the raw coal is kept in a liquid state, and separating the raw coal gas to obtain a first gas-phase product and a first liquid-phase product; and (3) further cooling the obtained first gas-phase product to obtain the synthesis gas and the second liquid-phase product, and separating out the second liquid-phase product. The method in the invention ensures that the oil content in system waste water can be reduced to be below 200mg/L.
Description
Technical field
The invention relates to the method that a kind of crushed coal pressure gasifying obtains synthetic gas.
Background technology
Coal preparing natural gas technological line, at present take the international coal preparing natural gas of big plain in u.s.a demonstration unit (20 years of operation) and Datang project as representative, 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 the coal of extraction in the colliery being carried out the coal choosing, and broken coal is used for pressurized gasification.The principal reaction of crushed coal pressure gasifying is coal and the reaction of steeping in water for reconstitution unboiled water coal gas, obtains raw gas, and the main component of raw gas is synthetic gas (comprising carbon monoxide, hydrogen and methane), also has the undecomposed water of part, and a small amount 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 gas product of coal process for producing natural gained, calorific value 35564kJ/m
3Above.
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, for example, CN1318550C discloses a kind of process for pressurized gasification of dry coal fines, wherein 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 larger.The aftertreatment of oily(waste)water generally processes to remove wherein coal tar by Multistage settling, yet, the oil that also contains nearly 1000mg/L by the water after the Multistage settling 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.This shows, the processing of oily(waste)water causes the water treatment expense to increase, and therefore, oily(waste)water is treated as the main weak point of selecting crushed coal pressure gasifying in the coal preparing natural gas project.
In addition, US4324643 discloses a kind of method that is prepared stable hydro carbons by the solid particulate carbonaceous material, the 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 substantially not containing the gaseous mixture of solid; 3) the described gaseous mixture that does not substantially contain solid is mixed with the quench liquid that contains end-capping reagent, the condition of chilling so that in reaction the instant volatile hydrocarbon free radical that generates almost can all react and termination reaction with end-capping reagent simultaneously, and so that the simultaneously condensation of most of at least described macromole hydrocarbon, thereby obtain gas and condensation and stable hydrocarbon.And the temperature that further discloses condensation particularly preferably is lower than 200 °F (namely 95 ℃), and condensed fluid is mainly hydrocarbon.
Although the employing 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.
Summary of the invention
The objective of the invention is in order to overcome the defects of prior art, provide a kind of new coal pressurization to obtain the method for synthetic gas.
In order to solve the oily(waste)water problem of above-mentioned prior art, the present inventor has carried out a large amount of research, discovery is that 70-200 ℃ organic solvent (i.e. oil) is as the cooling washing composition of chilling separation by adopting temperature, and the time that the control raw gas contacts with organic solvent is 10 seconds to 120 seconds, successfully realized being separated between the organism that water in the raw gas and coal tar wet goods produce oily(waste)water, so that water and coal tar enter respectively gas phase and liquid phase, and by making gas phase further cooling and oily water separation, system's waste water oleaginousness is down to below the 200mg/L.
The invention provides a kind of method of acquiring synthesis gas by pressurizing crushed coal, the method may further comprise the steps: (1) is under the pressurized gasification condition, broken coal is contacted with water, obtain a kind of raw gas that contains synthetic gas, tar and water, the boiling point of described tar is higher than the boiling point of water; (2) the gained raw gas is contacted with organic solvent carry out chilling, the condition that described raw gas contacts with organic solvent comprises that the temperature of organic solvent is 70-200 ℃, and the time is 10 seconds to 120 seconds, obtains the first gas-phase product and the first liquid product; (2) gained the first gas-phase product is further cooled off, obtain synthetic gas and second liquid phase product, isolate the second liquid phase product.
The method of acquiring synthesis gas by pressurizing crushed coal provided by the invention, by the starting temperature of control organic solvent and time that raw gas contacts with organic solvent in specified range, can realize that water in the raw gas and coal tar wet goods produce fully being separated between the organism of oily(waste)water, so that water and coal tar enter respectively gas phase and liquid phase.Thereby so that the waste water oleaginousness that oily water separation obtains is down to below the 200mg/L, really solved the oily(waste)water problem.Waste water is stripping directly, produces steam and is used for the pressurization vaporization, also can directly carry out discharging after the deamination dephenolize.This shows, adopt method provided by the invention can greatly reduce the cost of wastewater treatment.Method provided by the invention can be used for the various separation that can produce the pressurized gasification product of oily(waste)water problem.
Experimental results show that, when the temperature of organic solvent is lower than 70 ℃, although in theory by foreshortening to the duration of contact that makes organic solvent and raw gas when being less than 10 seconds, also can realize and can realize fast the cooling of raw gas, the dew-point temperature that is higher than water so that the temperature of raw gas is reduced to the condensing temperature (being liquefaction temperature) that is lower than coal tar, but, because the temperature of organic solvent is excessively low, heat exchange between raw gas and the organic solvent is too rapid, cause between raw gas and the organic solvent contact abundant not, thereby dissolving or the moisture that is included in the coal tar of raw gas have little time to overflow from coal tar, and be separated with water in oil liquid phase emulsion droplet form and the gas phase composition of having overflowed, thereby liquid phase is a large amount of water in oil liquid phase emulsion droplet, separating fully of coal tar and water can not be really realized, also just the oily(waste)water problem can not be really solved.
On the contrary, when the temperature of organic solvent is higher than 200 ℃, although the duration of contact by prolonging organic solvent and raw gas is during more than 120 seconds, also can realize the cooling of raw gas, the temperature that makes raw gas is reduced to the condensing temperature (being liquefaction temperature) that is lower than coal tar and is higher than the dew-point temperature of water, but, because the excess Temperature of organic solvent, heat exchange between raw gas and the organic solvent is too slow, cause raw gas to be in for a long time the condition of high temperature, and owing to containing a large amount of unsaturated hydrocarbons in the coal tar, these unsaturated hydrocarbons are easy to occur further polymerization under the above-mentioned condition of high temperature, cause the coal tar oil viscosity further to increase, form Jiao who is more prone to the thickness attitude, the content of oil then further reduces.In this case, the water that does not have enough time to overflow in the coal tar just is covered by among Jiao of this thickness attitude, and more difficult realization separates, thereby can not solve above-mentioned oily(waste)water problem.
Description of drawings
Fig. 1 is the process flow sheet of the method for acquiring synthesis gas by pressurizing crushed coal provided by the invention.
Embodiment
Among the present invention, described raw gas can be various crushed coal pressure gasifying products.The condition of described crushed coal pressure gasifying can be various crushed coal pressure gasifying condition well known in the art, for example, described broken coal can be not less than for size 5 millimeters various broken coal pieces, for example size is the coal cinder of 5-50 millimeter, and the condition of described pressurized gasification comprises that temperature can be 700-1300 ℃, is preferably 900-1200 ℃, pressure can be the 1.5-10 MPa, be preferably the 2-6 MPa, 2-4 MPa more preferably, the weight ratio of water and broken coal is 0.6～1.2: 1.The concrete operations of crushed coal pressure gasifying have been conventionally known to one of skill in the art, for example, can carry out pressurized gasification according to the disclosed process for pressurized gasification of dry coal fines of CN1318550C, obtain raw gas.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.
The starting temperature of described raw gas is generally 350-650 ℃, is preferably 400-550 ℃; Pressure is generally the 1-10 MPa, is preferably the 2-6 MPa.In the described raw gas, the total amount of the raw gas outside to dewater is as benchmark, and the content of synthetic gas is generally the 80-99.9 % by weight, is preferably the 80-99.5 % by weight, and the content of tar is generally the 0.1-20 % by weight, is preferably the 0.5-12 % by weight.The content of described water is the 10-60 % by weight of described raw gas, is preferably the 15-50 % by weight.
Among the present invention, the main component of the synthetic gas in the described raw gas is carbon monoxide and hydrogen, also comprises in addition the component that is gaseous state under the normal temperature such as methane, ethane, propane, isopropyl alkane, carbonic acid gas, hydrogen sulfide, ammonia, N
2In one or more.Among the present invention, described tar is continued to use the definition of this area routine, the thick coal tar that the expression boiling point is high, viscosity is large.Except water, synthetic gas and tar, the light oil in the described raw gas is to be lower than in 180 ℃ the petroleum naphtha one or more for liquid liquid ingredient such as phenol, biphenol, formic acid, boiling point under the normal temperature.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 temperature of the organic solvent that control contacts with described raw gas is 70-200 ℃, time is 1 second to 120 seconds, can obtain the first gas-phase product and the first liquid product, reach purpose of the present invention, but under the preferable case, 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 of contact is 10-100 second.
Owing to making the water in the described raw gas keep gaseous state temperature required closely related with pressure, making the water in the described raw gas keep gaseous state temperature required also different under the different pressures.In order to reduce as far as possible the consumption as the organic solvent of refrigerant, the present invention preferably uses the large as far as possible organic solvent of gasification latent heat, the gasification latent heat of concrete preferred described organic solvent is greater than 50 kilojoule per kilogram, 50-2000 kilojoule per kilogram for example, the gasification latent heat of further preferred organic solvent is the 150-1000 kilojoule per kilogram.When the gasification latent heat of described organic solvent is the 50-2000 kilojoule per kilogram, the condition of described contact comprise the consumption of described organic solvent be described raw gas weight 1-15 doubly, the time of contact is can realize so that the temperature of described raw gas is reduced to 200-300 ℃ in 10 seconds to 120 seconds; When the gasification latent heat of described organic solvent is the 150-1000 kilojoule per kilogram, the condition of described contact comprises that the consumption of described organic solvent is 2-10 times of described raw gas weight, and the time of contact is that 10-45 can realize so that the temperature of described raw gas is reduced to 200-300 ℃ second.
Among the present invention, unless stated otherwise, described gasification latent heat refers to 1 gasification latent heat under the normal atmosphere.Boiling point refers to the boiling point under the standard state.
In order to reduce the load that step (1) gained gas-phase product is carried out for the second time cooling and oily water separation, the preferred described organic solvent of the present invention be can be miscible with step (1) gained liquid product inert organic solvents, 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, thereby can play to coal tar the effect of dilution visbreaking.In addition, by use can be miscible with step (1) gained liquid product inert organic solvents, can also make this organic solvent serve as simultaneously washing composition, 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.Industrially preferably use boiling range in tar or the tar to be the coal tar of 100-550 ℃ cut especially boiling range as 180-530 ℃, hydrocracking tail oil, in diesel oil and the wax oil one or more are as described refrigerant, preferred organic solvent is the coal tar that wash cooling separates in the described raw gas, the liquid product that also is about to described step (1) gained partly or entirely is used as the next time refrigerant of chilling, can reduce so on the one hand the amount of outsourcing oil, save production cost, the liquid product that has also solved on the other hand step (1) gained is the emission problem of tar.
Among the present invention, described inert organic solvents refer under separation condition not with system to be separated in material chemical reaction further occurs or self do not occur under separation condition or the basic material of polymerization reaction take place not.
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 passes through accessory in liquid distributor or spraying gun or other tower containers so that quenching oil contacts with raw gas with vaporific form.
According to method provided by the invention, the product that the gained cat head is overflowed further cooling is for water, synthetic gas and light oil are separated, and 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.
According to preferred implementation of the present invention, as shown in Figure 1, the method of obtaining synthetic gas by broken coal provided by the invention comprises carries out pressurized gasification with broken coal, the gas-phase product raw gas that pressurized gasification is obtained contacts with organic solvent, carrying out chilling separates, the first gas-phase product that obtains containing the first liquid product of tar and contain water, then with after the further heat exchange cooling of gained the first gas-phase product, obtain purified gas and second liquid phase product, the second liquid phase product is carried out oily water separation in subsider, obtain water and lightweight oil.
The present invention is described further for the following examples.
Embodiment 1
This embodiment is used for illustrating the method for acquiring synthesis gas by pressurizing crushed coal provided by the invention.
Adopt technique 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 physical property 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 % by weight of crushed coal pressure gasifying product total amount) from top of gasification furnace.
Then be 3 MPas with this pressure, temperature is that 500 ℃ crushed coal pressure gasifying product is take 1000 kg/hrs flow and temperature as 100 ℃, boiling range is 180-300 ℃, flow is that 2800 kg/hrs coal tar contacts in the chilling separator, contact after 80 seconds, liquid product (temperature is 350 ℃) is discharged at the bottom of tower, in contact process, gas-phase product (temperature is 250 ℃) is overflowed from cat head, gas-phase product is further sent in the subsider by behind the interchanger indirect heat exchange to 50 ℃, collection is from subsider top escaping gas component, liquid in the subsider is left standstill natural layering, isolate wherein water and organic phase.The result is that water is transparent, and oleaginousness is 50mg/L.Liquid product learns that by analysis water content is 0.2 % by weight at the bottom of the tower.
Embodiment 2
This embodiment is used for illustrating that crushed coal pressure gasifying provided by the invention obtains the method for synthetic gas.
Adopt technique 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 physical property 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 % by weight of crushed coal pressure gasifying product total amount) from the top.
Then be 2.5 MPas with this pressure, temperature is that 300 ℃ crushed coal pressure gasifying product is take 1500 kg/hrs flow and temperature as 150 ℃, boiling range is 180-300 ℃, flow is that 3200 kg/hrs hydrocracking tail oil contacts in the chilling separator, contact after 30 seconds, liquid product (temperature is 220 ℃) is discharged at the bottom of tower, gas-phase product (temperature is 210 ℃) is overflowed from cat head, gas-phase product is further sent in the subsider by behind the interchanger indirect heat exchange to 40 ℃, collection is from subsider top escaping gas component, liquid in the subsider is left standstill natural layering, isolate wherein water and organic phase, the discovery water is transparent, and oleaginousness is 100mg/L.Liquid product learns that by analysis water content is 0.3 % by weight at the bottom of the tower.
Embodiment 3
This embodiment obtains the method for synthetic gas for illustrating that coal provided by the invention pressurizes.
Adopt technique 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 physical property 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 % by weight of crushed coal pressure gasifying product total amount) from the top.
Then be 3.5 MPas with this pressure, temperature is that 650 ℃ crushed coal pressure gasifying product is take 800 kg/hrs flow and temperature as 100 ℃, boiling range is 180-300 ℃, flow is that 3000 kg/hrs coal tar contacts in the chilling separator, contact after 50 seconds, liquid product (temperature is 400 ℃) is discharged at the bottom of tower, gas-phase product (temperature is 280 ℃) is overflowed from cat head, gas-phase product is further sent in the subsider by after the water wash column heat exchange to 40 ℃, collection is from subsider top escaping gas component, liquid in the subsider is left standstill natural layering, isolate wherein water and organic phase, the discovery water is transparent, and oleaginousness is 150mg/L.Liquid product is learnt water content 0.4 % by weight by analysis at the bottom of the tower.
Comparative Examples 1
By acquiring synthesis gas by pressurizing crushed coal, different is according to the method for embodiment 1, and the temperature of coal tar is 50 ℃, and the time of contact is 5 seconds, obtains gaseous fraction (synthetic gas), water and oil phase.The result is that water is translucent, and oleaginousness is 500mg/L.Liquid product learns that by analysis water content is 2 % by weight at the bottom of the tower.
Comparative Examples 2
By acquiring synthesis gas by pressurizing crushed coal, different is according to the method for embodiment 1, and the temperature of coal tar is 300 ℃, and the time of contact is 5 minutes, obtains gaseous fraction (synthetic gas), water and oil phase.The result is that water is translucent, and oleaginousness is 600mg/L.Liquid product learns that by analysis water content is 2.1 % by weight at the bottom of the tower.
Table 1
| Project | Brown coal |
| Technical analysis (% by weight) War Wad Aad Vad Sad | 36.90 17.81 12.02 29.49 1.21 |
| Ultimate analysis (% by weight) Car Har Oar Nar Sar | 52.23 3.20 12.06 0.61 1.21 |
| Ash fusion point (℃) T1 T2 T3 | 1160 1200 1220 |
Annotate:
War---represent coal-fired moisture as received coal; Wad---the coal-fired dry basic moisture of expression; Har---represent that coal-fired as received basis hydrogen divides; 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 that coal-fired as received basis carbon divides; Oar---represent that coal-fired as received basis oxygen divides; Nar---represent that coal-fired as received basis nitrogen divides; Sar---represent coal-fired as received basis sulphur content; T1---softening temperature, ℃; T2---hemispherical temperature, ℃; T3---melt temperature, ℃.
Table 2
| Form (% by weight) | Embodiment 1 | Embodiment 2 | Embodiment 3 | Comparative Examples 1 | Comparative Examples 2 |
| H 2 | 3.59 | 3.61 | 3.58 | 3.59 | 3.60 |
| CO | 19.68 | 19.75 | 19.56 | 19.68 | 19.68 |
| CO 2 | 62.88 | 63.09 | 62.71 | 62.88 | 62.88 |
| CH 4 | 7.57 | 7.35 | 7.65 | 7.57 | 7.57 |
| N 2 | 0.34 | 0.34 | 0.34 | 0.34 | 0.33 |
| C 2 | 0.39 | 0.36 | 0.39 | 0.39 | 0.39 |
| C 3 | 0.39 | 0.35 | 0.39 | 0.39 | 0.39 |
| H 2S | 0.50 | 0.50 | 0.51 | 0.50 | 0.50 |
| NH 3 | 0.17 | 0.17 | 0.17 | 0.17 | 0.17 |
| HCN | 0.01 | 0.01 | 0.01 | 0.01 | 0.01 |
| C 6H 6O | 0.39 | 0.39 | 0.39 | 0.39 | 0.39 |
| C 6H 6O 2 | 0.26 | 0.26 | 0.26 | 0.26 | 0.26 |
| Petroleum naphtha (＜180 ℃) | 0.41 | 0.38 | 0.41 | 0.41 | 0.41 |
| Middle oil (180-360 ℃) | 1.60 | 1.57 | 1.70 | 1.60 | 1.60 |
| Heavy oil (＞360 ℃) | 1.82 | 1.87 | 1.93 | 1.82 | 1.82 |
| ∑ | 100.00 | 100.00 | 100.00 | 100.00 | 100.00 |
| The oil product total amount | 4.48 | 4.47 | 4.69 | 4.48 | 4.48 |
Table 3
| Embodiment 1 | Embodiment 2 | Embodiment 3 | Comparative Examples 1 | Comparative Examples 2 | |
| W/O content (% by weight) | 0.2 | 0.3 | 0.4 | 2 | 2.1 |
| Oil-contg in the water (mg/L) | 50 | 100 | 150 | 500 | 600 |
From the results shown in Table 3, adopt method provided by the invention can effectively realize oily water separation in raw gas and the raw gas, thereby effectively solve the oily(waste)water problem, and Comparative Examples 1 and Comparative Examples 2 are respectively because the temperature of quenching oil is too low and too high, W/O content after the separation is higher, oil-contg is higher in the water, can not realize well oily water separation, thereby can not solve the oil-containing water problem.This shows, can the temperature of quenching oil and duration of contact be the key points that solve the oily(waste)water problem.
Claims (13)
1. the method for an acquiring synthesis gas by pressurizing crushed coal, the method may further comprise the steps: (1) is under the pressurized gasification condition, broken coal is contacted with oxygen with water vapor, obtain a kind of raw gas that contains synthetic gas, tar and water, the boiling point of described tar is higher than the boiling point of water; (2) the gained raw gas is contacted with organic solvent carry out chilling, the condition that described raw gas contacts with organic solvent comprises that the temperature of organic solvent is 70-200 ℃, and the time is 10 seconds to 120 seconds, obtains the first gas-phase product and the first liquid product; (2) gained the first gas-phase product is further cooled off, obtain synthetic gas and second liquid phase product, isolate the second liquid phase product.
2. method according to claim 1, wherein, the condition that described raw gas contacts with organic solvent comprises that the temperature of organic solvent is 80-180 ℃, the time of contact is 10-100 second.
3. method according to claim 1 and 2, wherein, the temperature of described raw gas is 350-650 ℃, pressure is the 1.5-10 MPa, the consumption of described organic solvent be described raw gas weight 1-15 doubly.
4. method according to claim 3, wherein, the temperature of described raw gas is 400-550 ℃, pressure is the 2-6 MPa, the consumption of described organic solvent be the described gas mixture weight that contains tar 2-10 doubly.
5. according to claim 1,2 or 4 described methods, wherein, the gasification latent heat of described organic solvent is the 50-2000 kilojoule per kilogram, the condition of described contact is so that the temperature of described raw gas is reduced to 200-300 ℃.
6. method according to claim 5, wherein, described organic solvent is the inert organic solvents miscible with tar, and the boiling point of described organic solvent is higher than the boiling point of water, the first liquid product contains tar and organic solvent.
7. method according to claim 6, wherein, described organic solvent is that boiling range is 100-550 ℃ cut in tar or the tar.
8. method according to claim 6, wherein, described organic solvent is that boiling range is one or more in 180-530 ℃ coal tar, diesel oil and the hydrocracking tail oil.
9. according to claim 1,2 or 4 described methods, wherein, described organic solvent is the inert organic solvents that boiling point is lower than water, the second liquid product contains described organic solvent.
10. method according to claim 9, wherein, the method also comprises carries out oily water separation with the second liquid product.
11. method according to claim 1, wherein, in the described raw gas, the content of tar is the 0.1-20 % by weight of the raw gas total amount outside dewatering; The content of described water is the described 10-60 % by weight that contains the raw gas of tar.
12. method according to claim 11, wherein, in the described raw gas, the content of tar is the 0.5-15 % by weight of the raw gas total amount outside dewatering; The content of described water is the described 15-50 % by weight that contains the raw gas of tar.
13. method according to claim 1, wherein, described broken coal is that size is that the coal cinder of 5-80 millimeter, the condition of described pressurized gasification comprise that temperature is 700-1300 ℃, and pressure is the 1.5-10 MPa, and the weight ratio of water and broken coal is 0.6-1.2: 1.
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Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6312505B1 (en) * | 1999-11-19 | 2001-11-06 | Energy Process Technologies, Inc. | Particulate and aerosol remover |
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