CN100488928C - Methanol production process - Google Patents
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- CN100488928C CN100488928C CNB2006101620609A CN200610162060A CN100488928C CN 100488928 C CN100488928 C CN 100488928C CN B2006101620609 A CNB2006101620609 A CN B2006101620609A CN 200610162060 A CN200610162060 A CN 200610162060A CN 100488928 C CN100488928 C CN 100488928C
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Abstract
The invention discloses a manufacturing technology of carbinol without gasifying and gas purifying problem, which comprises the following steps: dividing space; preparing oxygen; gasifying; transforming; desulfurizing; decarbonizing; synthesizing; distilling.
Description
Technical field
The present invention relates to the coal is the technology of feedstock production methyl alcohol, is specially a kind of methanol process.
Background technology
At present preparation methyl alcohol mainly is to be that raw material makes unstripped gas with coal or Sweet natural gas, obtains essential substance through a series of purifications and compression process and is (H
2+ CO+CO
2) gas, carry out the reaction of synthesizing methanol then.Domestic medium and small fertilizer enterprises generally adopts connection alcohol or two first explained hereafter methods, and production scale is smaller, and output is generally all below 50,000 tons.
In the general Coal Gasification Technology that adopts external comparative maturity of large-scale methyl alcohol enterprise of founding a capital and planning to build, as Texaco's coal slurry gasification technology, shell bed pulverized coal gasification technology, the strange broken coal gasification technology in Shandong, grace stove bed pulverized coal gasification technology etc.All there is weak point in various gasification technologies: 1, texaco coal-water slurry gasification.(1) ash fusion point to coal has certain requirement, generally is lower than 1400 ℃, has limited the use range of coal.(2) burner position operating mode harshness, continuous operating time is short, generally has only 30-50 days.2, shell coal gasification.(1), introducing equipment is more, construction costs is higher.(2) industrial practice is few, and it is insufficient that relative merits expose, and technical elements waits test, and 3, the grace coal gasification: use producer to prove at home, gasification efficient is low, the coal consumption height, and gaseous mass is poor, and environmental pollution is big, is difficult to promote.4, above various technology all is a foreign patent, if introduce the patent royalty that needs payment expensive, and an enterprise that produces 200000 tons of methyl alcohol per year, patent royalty is generally about 2,500 ten thousand yuan.
Gas sweetening: low-temperature rectisol and domestic independently developed NHD gas purifying technique that German LURGI is mostly adopted in domestic in recent years newly-built methyl alcohol and synthetic ammonia installation, gas sweetening, supporting CLAUS sulfur recovery unit.Weak point: 1, low-temperature rectisol need be bought patent license and key equipment, invests greatlyyer, is unfavorable for the popularization and the use of domestic proprietary technology.2, the NHD gas purifying technique is the domestic intellecture property that has, and invests also lowlyer, and methyl alcohol is washed low, but the working cost height is poor to the organosulfur receptivity.3, since China's various places coal vary, so in the gas sulphur content also difference is bigger.After above-mentioned two kinds of process solvents regeneration, sour gas has H
2S concentration is low, and the characteristics that tolerance is little so adopt single conventional CLAUS technology, can't satisfy national gaseous emission standard at all.
Summary of the invention
The present invention provides a kind of methanol process in order to solve in the prior art problem that exists in the gasification and gas sweetening when the process of preparation methyl alcohol.
The present invention is realized that by following technical scheme a kind of methanol process comprises the following steps:
One, making oxygen by air separation, this step adopts molecular sieve adsorption, the turbine boosting swell refrigeration, full filling extract rectification, compression process is produced liquid oxygen, liquid nitrogen in the hydraulic pressure.
Two, gasification, this step adopt non-molten slag-molten slag two-stage gasifier, and (patent No. of this device is 02235127.2.) coal water slurry enters the burner of top of gasification furnace and the CO that comes in from the burner pipe core
2And and body of heater top two nozzles the oxygen of spray carried out mixed firing obtain unstripped gas, temperature of reaction is at 1300～1400 ℃, high-temperature gas passes cooling and wash temperature are reduced to 200～210 ℃, pressure is 3.7～3.9MPa, and each component content is in the gas: CO40～46%, H
233～40%, CO
217～22%, CH
4400～1500X10
6-
Three, conversion and desulfurization, decarburization, gasification workshop section is come 200～210 ℃, pressure is that the saturation water coal gas of 3.7～3.9MPa is cooled to 175～180 ℃ again and enters shift converter, transformation temperature is controlled at 300～400 ℃, and CO and water reaction make CO content drop to 17～19% at last, gas after the conversion cools to 170～180 ℃ and enters the tempreture organic sulphur hydrolysis groove, make organosulfur change inorganic sulfur into, make gas cool to 35～40 ℃ again and enter desulfurization process
(1) desulfurization, the conversion atmospheric pressure that comes from transformation system is 3.4～3.6MPa, at first sends into the thionizer bottom, with the bulky amine doctor solution counter current contact of going into tower from this tower top, the H in the gas
2S and portion C O
2By solution absorption.H
2S reduces to 20mg/Nm
3
(2) pressure that comes from desulfurization workshop section is that 3.3-3.5MPa (contains CO
225%) conversion gas enters the absorption tower from bottom, decarburization absorption tower, with MDEA (N methyldiethanol amine) the solution counter current contact from tower top.CO
2Reduce to 5% (V).
(3), the desulfurization of complexing iron, after step (1) finishes, after the bulky amine liquid decompression of coming out at the bottom of the absorption tower, through the solution heat exchanger heat exchange, enter flash drum, under the pressure of 0.4MPa, with the H in the solution
2, CO, and portion C O
2Flash distillation is come out, H in the flashed vapour
2S content is at 1000～1500mg/Nm
3, go out the flashed vapour (CO of regeneration overhead
2And H
2S), be sent to complexing iron desulfurization process.
After step (2) finished, the solution that comes out at the bottom of the absorption tower entered one and dodges tower and carry out high pressure flash after decompression, and the gas that flashes off is delivered to complexing iron desulfurization process.MDEA (N methyldiethanol amine) solution that is come out by a sudden strain of a muscle tower bottom enters two sudden strain of a muscle towers, carries out low pressure flash, and the carbon dioxide that flash distillation is come out is delivered to complexing iron desulfurization process.
The flashed vapour that produces in step (1) and (2) is adopted the desulfurization of complexing iron, and pressure is under the 0.06MPa, enters complexing iron absorption tower, with complexing iron doctor solution counter current contact.Resurgent gases H
2S content is less than 10mg/Nm
3,
Four, synthetic, rectifying, (CO is about 25%, CO for the unstripped gas that last step is made
25%, H
2About 68%) is synthetic coarse methanol under the pressure of 6.48～6.8MPa at pressure, makes refined methanol by rectifying again.
Technical superiority of the present invention:
CO in the two stage type gas metallization processes
2In vapourizing furnace and O
2Reaction generates CO, has both reduced CO
2Discharging has increased gas effective constituent again, and every technic index makes moderate progress.Effective constituent (CO+H
2) 〉=85% improves 2 percentage points than Texaco, and efficiency of carbon conversion 〉=98% improves 1.5 percentage points than Texaco.
Process gas comes out directly to enter transformation system after dedusting from two sections stoves, adopts bulky amine and the decarburization of MDEA double-stage desulfurizing after the conversion, to satisfy the methanol production requirement.(wherein major part is CO to stripping gas
2), take chromium to close iron and absorb wherein H
2S is to guarantee CO
2For urea, liquid CO
2Producing needs.Chromium closes ferrous solution and takes jet oxidative regeneration, and the sulfur recovery continuous sulfur melting obtains elemental sulfur. and bulky amine and MDEA adopt heating decompression regeneration in this flow process, do not have any liquid gas discharging, and be environmentally friendly.
Two stage type gas metallization processes and gas purifying technique that the present invention adopts in the pre-treatment process of preparation methyl alcohol, broken through conventional thought, overcome the deficiency of external device effectively, process design and device fabrication are all domesticized, and have reduced investment, characteristics such as the construction period is short, level of automation is high, safe operation coefficient height, easy handling.
Embodiment
Embodiment 1: a kind of methanol process, comprise the following steps,
(1), making oxygen by air separation, this step is a common process well known to those skilled in the art
(2), gasification, this step adopts non-molten slag-molten slag two-stage gasifier, coal water slurry enters the burner of top of gasification furnace and the CO that comes in from the burner pipe core
2, and and body of heater top two nozzles the oxygen of spray carried out mixed firing obtain unstripped gas, temperature of reaction is at 1300 ℃, high-temperature gas passes cooling and wash temperature are reduced to 200 ℃, pressure is 3.7MPa,
(3), conversion and desulfurization, decarburization, gasification workshop section is come 200 ℃, pressure is that the saturation water coal gas of 3.7MPa is cooled to 175 ℃ again and enters shift converter, transformation temperature is controlled at 300 ℃, and CO and water reaction make CO content drop to 17～19% at last, gas after the conversion cools to 170 ℃ and enters the tempreture organic sulphur hydrolysis groove, make organosulfur change inorganic sulfur into, make gas cool to 35 ℃ again and enter desulfurization process
(1) desulfurization, the conversion atmospheric pressure that comes from transformation system is 3.4MPa, at first sends into the thionizer bottom, with the bulky amine doctor solution counter current contact of going into tower from this tower top, the H in the gas
2S and portion C O
2By solution absorption, the preparation of bulky amine doctor solution, the mass ratio of bulky amine and water is 1:2～2.5.
(2) pressure that comes from desulfurization workshop section is the conversion gas of 3.3MPa, enter the absorption tower from bottom, decarburization absorption tower, with MDEA (N methyldiethanol amine) the solution counter current contact from tower top, the proportioning of MDEA (N methyldiethanol amine) solution is MDEA and quality ratio 1:1～1.5.
(3), the desulfurization of complexing iron, after step (1) finishes, after the bulky amine liquid decompression of coming out at the bottom of the absorption tower, through the solution heat exchanger heat exchange, enter flash drum, under the pressure of 0.4MPa, with the H in the solution
2, CO, and portion C O
2Flash distillation is come out, H in the flashed vapour
2S content is at 1000 ~ 1500mg/Nm
3, go out the flashed vapour (CO of regeneration overhead
2And H
2S), be sent to complexing iron desulfurization process.
After step (2) finished, the solution that comes out at the bottom of the absorption tower entered one and dodges tower and carry out high pressure flash after decompression, and the gas that flashes off is delivered to complexing iron desulfurization process.MDEA (N methyldiethanol amine) solution that is come out by a sudden strain of a muscle tower bottom enters two sudden strain of a muscle towers, carries out low pressure flash, and the carbon dioxide that flash distillation is come out is delivered to complexing iron desulfurization process.High pressure in this step and low pressure are those skilled in the art's routine and understand notion, and used flashing apparatus also is a known equipment.
The flashed vapour that produces in step (1) and (2) is adopted the desulfurization of complexing iron, and pressure is about 0.06MPa, enters complexing iron absorption tower, with complexing iron doctor solution counter current contact.Resurgent gases H
2S content is less than 10mg/Nm
3, the configuration proportion of complexing iron doctor solution is to add 10～20kg complexing iron sweetening agent, 30～40kg soda ash, 30～40kg sodium bicarbonate, 10～20kg ferrous salt in the 1000kg water.Ferrous salt such as ferrous sulfate, iron protochloride etc.Complexing iron sweetening agent generally uses the graduate product of southization.
Four, synthetic, rectifying, the unstripped gas that last step is made are synthetic coarse methanol under the pressure of 6.48MPa at pressure, make refined methanol by rectifying again.
Embodiment 2: a kind of methanol process, comprise the following steps,
(1), making oxygen by air separation,
(2), gasification, this step adopts non-molten slag-molten slag two-stage gasifier, coal water slurry enters the burner of top of gasification furnace and the CO that comes in from the burner pipe core
2, and and body of heater top two nozzles the oxygen of spray carried out mixed firing obtain unstripped gas, temperature of reaction is at 1400 ℃, high-temperature gas passes cooling and wash temperature are reduced to 206 ℃, pressure is 3.9MPa,
(3), conversion and desulfurization, decarburization, gasification workshop section is come 206 ℃, pressure is that the saturation water coal gas of 3.9MPa is cooled to 180 ℃ again and enters shift converter, transformation temperature is controlled at 400 ℃, and CO and water reaction make CO content drop to 17～19% at last, gas after the conversion cools to 175 ℃ and enters the tempreture organic sulphur hydrolysis groove, make organosulfur change inorganic sulfur into, make gas cool to 40 ℃ again and enter desulfurization process
(1) desulfurization, the conversion atmospheric pressure that comes from transformation system is 3.6MPa, at first sends into the thionizer bottom, with the bulky amine doctor solution counter current contact of going into tower from this tower top, the H in the gas
2S and portion C O
2By solution absorption,
(2) pressure that comes from desulfurization workshop section is the conversion gas of 3.4MPa, enters the absorption tower from bottom, decarburization absorption tower, with MDEA (N methyldiethanol amine) solution counter current contact from tower top,
(3), the desulfurization of complexing iron, after step (1) finishes, after the bulky amine liquid decompression of coming out at the bottom of the absorption tower, through the solution heat exchanger heat exchange, enter flash drum, under the pressure of 0.4MPa, with the H in the solution
2, CO, and portion C O
2Flash distillation is come out, H in the flashed vapour
2S content is at 1000 ~ 1500mg/Nm
3, go out the flashed vapour (CO of regeneration overhead
2And H
2S), be sent to complexing iron desulfurization process.
After step (2) finished, the solution that comes out at the bottom of the absorption tower entered one and dodges tower and carry out high pressure flash after decompression, and the gas that flashes off is delivered to complexing iron desulfurization process.MDEA (N methyldiethanol amine) solution that is come out by a sudden strain of a muscle tower bottom enters two sudden strain of a muscle towers, carries out low pressure flash, and the carbon dioxide that flash distillation is come out is delivered to complexing iron desulfurization process.
The flashed vapour that produces in step (1) and (2) is adopted the desulfurization of complexing iron, and pressure is about 0.06MPa, enters complexing iron absorption tower, with complexing iron doctor solution counter current contact.Resurgent gases H
2S content is less than 10mg/Nm
3,
Four, synthetic, rectifying, the unstripped gas that last step is made are synthetic coarse methanol under the pressure of 6.8MPa at pressure, make refined methanol by rectifying again.
Embodiment 3: a kind of methanol process, comprise the following steps,
(1), making oxygen by air separation,
(2), gasification, this step adopts non-molten slag-molten slag two-stage gasifier, coal water slurry enters the burner of top of gasification furnace and the CO that comes in from the burner pipe core
2, and and body of heater top two nozzles the oxygen of spray carried out mixed firing obtain unstripped gas, temperature of reaction is at 1350 ℃, high-temperature gas passes cooling and wash temperature are reduced to 210 ℃, pressure is 3.85MPa,
(3), conversion and desulfurization, decarburization, gasification workshop section is come 210 ℃, pressure is that the saturation water coal gas of 3.85MPa is cooled to 180 ℃ again and enters shift converter, transformation temperature is controlled at 370～380 ℃, and CO and water reaction make CO content drop to 17～19% at last, gas after the conversion cools to 180 ℃ and enters the tempreture organic sulphur hydrolysis groove, make organosulfur change inorganic sulfur into, make gas cool to 37 ℃ again and enter desulfurization process
(1) desulfurization, the conversion atmospheric pressure that comes from transformation system is 3.6MPa, at first sends into the thionizer bottom, with the bulky amine doctor solution counter current contact of going into tower from this tower top, the H in the gas
2S and portion C O
2By solution absorption,
(2) pressure that comes from desulfurization workshop section is the conversion gas of 3.5MPa, enters the absorption tower from bottom, decarburization absorption tower, with MDEA (N methyldiethanol amine) solution counter current contact from tower top,
Four, synthetic, rectifying, the unstripped gas that last step is made are synthetic coarse methanol under the pressure of 6.6MPa at pressure, make refined methanol by rectifying again.
Claims (3)
1, a kind of methanol process is characterized in that: comprises the following steps,
(1), making oxygen by air separation,
(2), gasification, this step adopts non-molten slag-molten slag two-stage gasifier, coal water slurry enters the burner of top of gasification furnace and the CO that comes in from the burner pipe core
2, and and body of heater top two nozzles the oxygen of spray carried out mixed firing obtain unstripped gas, temperature of reaction is at 1300～1400 ℃, high-temperature gas passes cooling and wash temperature are reduced to 200～210 ℃, pressure is 3.7～3.9MPa,
(3), conversion and desulfurization, decarburization, 200～210 ℃ that gasification workshop section is come, pressure is 3.7～3.9
The saturation water coal gas of MPa is cooled to 175～180 ℃ again and enters shift converter, transformation temperature is controlled at 300～400 ℃, CO and water reaction, make CO content drop to 17～19% at last, gas after the conversion cools to 170～180 ℃ and enters the tempreture organic sulphur hydrolysis groove, make organosulfur change inorganic sulfur into, make gas cool to 35～40 ℃ again and enter desulfurization process
(1) desulfurization, the conversion atmospheric pressure that comes from transformation system is 3.4～3.6MPa, at first sends into the thionizer bottom, with the bulky amine doctor solution counter current contact of going into tower from this tower top, the H in the gas
2S and portion C O
2By solution absorption,
(2) pressure that comes from desulfurization workshop section is the conversion gas of 3.3-3.5MPa, enters the absorption tower from bottom, decarburization absorption tower, with N methyldiethanol amine solution counter current contact from tower top,
Four, synthetic, rectifying, the unstripped gas that last step is made are synthetic coarse methanol under the pressure of 6.48～6.8MPa at pressure, make refined methanol by rectifying again.
2, methanol process according to claim 1 is characterized in that: in step (three)
Additional step (3), the desulfurization of complexing iron after step (1) finishes, after the bulky amine liquid decompression of coming out at the bottom of the absorption tower, through the solution heat exchanger heat exchange, enter flash drum, under the pressure of 0.4MPa, with the H in the solution
2, CO, and portion C O
2Flash distillation is come out, H in the flashed vapour
2S content is at 1000～1500mg/Nm
3, go out the flashed vapour CO of regeneration overhead
2And H
2S is sent to complexing iron desulfurization process,
After step (2) finishes, the solution that comes out at the bottom of the absorption tower is after decompression, enter a sudden strain of a muscle tower and carry out high pressure flash, the gas that flashes off is delivered to complexing iron desulfurization process, the N methyldiethanol amine solution that is come out by a sudden strain of a muscle tower bottom enters two sudden strain of a muscle towers, carry out low pressure flash, the carbon dioxide that flash distillation is come out is delivered to complexing iron desulfurization process
The flashed vapour that produces in step (1) and (2) is adopted the desulfurization of complexing iron, and pressure is under the 0.06MPa, enters complexing iron absorption tower, with complexing iron doctor solution counter current contact.
3, methanol process according to claim 1 and 2 is characterized in that: comprises the following steps,
(1), making oxygen by air separation,
(2), gasification, this step adopts non-molten slag-molten slag two-stage gasifier, coal water slurry enters the burner of top of gasification furnace and the CO that comes in from the burner pipe core
2, and and body of heater top two nozzles the oxygen of spray carried out mixed firing obtain unstripped gas, temperature of reaction is at 1350 ℃, high-temperature gas passes cooling and wash temperature are reduced to 210 ℃, pressure is 3.85MPa,
(3), conversion and desulfurization, decarburization, gasification workshop section is come 210 ℃, pressure is that the saturation water coal gas of 3.85MPa is cooled to 180 ℃ again and enters shift converter, transformation temperature is controlled at 370～380 ℃, and CO and water reaction make CO content drop to 17～19% at last, gas after the conversion cools to 180 ℃ and enters the tempreture organic sulphur hydrolysis groove, make organosulfur change inorganic sulfur into, make gas cool to 37 ℃ again and enter desulfurization process
(1) desulfurization, the conversion atmospheric pressure that comes from transformation system is 3.6MPa, at first sends into the thionizer bottom, with the bulky amine doctor solution counter current contact of going into tower from this tower top, the H in the gas
2S and portion C O
2By solution absorption,
(2) pressure that comes from desulfurization workshop section is the conversion gas of 3.5MPa, enters the absorption tower from bottom, decarburization absorption tower, with N methyldiethanol amine solution counter current contact from tower top,
Four, synthetic, rectifying, the unstripped gas that last step is made are synthetic coarse methanol under the pressure of 6.6MPa at pressure, make refined methanol by rectifying again.
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|---|---|---|---|
| CNB2006101620609A CN100488928C (en) | 2006-12-11 | 2006-12-11 | Methanol production process |
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|---|---|---|---|
| CNB2006101620609A CN100488928C (en) | 2006-12-11 | 2006-12-11 | Methanol production process |
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| CN105367383A (en) * | 2014-08-25 | 2016-03-02 | 蒋小华 | Methyl-alcohol production technology |
| CN105861086B (en) * | 2016-05-10 | 2019-04-26 | 中国科学院理化技术研究所 | Utilize the process of gasification gas and coke-stove gas co-production of liquefied natural gas, methanol and liquefied ammonia |
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Address after: Shanxi Linyi Fenxi Road West, No. 2000 Patentee after: Shanxi Yangmei Fengxi fertilizer industry (Group) Limited by Share Ltd. Linyi Branch Address before: Shanxi Linyi Zhai Road No. 3 Patentee before: SHANXI FENGXI FERTILIZER Group |
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| TR01 | Transfer of patent right |
Effective date of registration: 20091016 Address after: No. 279, the Yellow River Avenue, Yuncheng, Shanxi Patentee after: Shanxi Yangmei Fengxi fertilizer industry (Group) Limited by Share Ltd. Address before: Shanxi Linyi Fenxi Road West, No. 2000 Patentee before: Shanxi Yangmei Fengxi fertilizer industry (Group) Limited by Share Ltd. Linyi Branch |
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| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20090520 Termination date: 20151211 |
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| EXPY | Termination of patent right or utility model |