CN103936557B - A kind of technique utilizing ammonia tail gas increase yield of methanol processed - Google Patents
A kind of technique utilizing ammonia tail gas increase yield of methanol processed Download PDFInfo
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- CN103936557B CN103936557B CN201410198411.6A CN201410198411A CN103936557B CN 103936557 B CN103936557 B CN 103936557B CN 201410198411 A CN201410198411 A CN 201410198411A CN 103936557 B CN103936557 B CN 103936557B
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/1516—Multisteps
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Abstract
The invention discloses a kind of technique utilizing ammonia tail gas increase yield of methanol processed, comprise the following steps: A, synthetic ammonia tailgas import; B, gas-liquid separation; C, tail gas compression; D, coke-oven gas mix; E, fine de-sulfur; F, conversion; G, mixing compression; H, synthesis; I, rectifying; Synthetic ammonia tailgas in steps A is the discarded tail gas produced in Converter in Natural Gas-Based Ammonia Making Process plant running process, this synthetic ammonia tailgas carries out gas-liquid separation by gas-liquid separator in stepb, fluent meterial in synthetic ammonia tailgas is by gas-liquid separator separates, and the gas after separation enters next step process by pipeline.The invention provides a kind of technique utilizing ammonia tail gas increase yield of methanol processed, improve H
2utilization ratio, reduce gas purging amount, improve the fund utilization rate of enterprise, the burden that reduce further enterprise improves income, strengthens the competitive power of enterprise.
Description
Technical field
The present invention relates to a kind of methanol process, relate to a kind of technique utilizing ammonia tail gas increase yield of methanol processed specifically.
Background technology
The H of coke-oven gas methanol device synthesis unstripped gas
2content is higher, and its H/C is up to 2.54, and the H/C of coke-oven gas methyl alcohol actual needs is 2.05-2.15, a large amount of periodic off-gases (H that such methanol device can will produce
2content reaches 70%) drain into gas ductwork, methanol emissions periodic off-gases per ton is about 800Nm
3, cause H
2waste, methyl alcohol coke-oven gas per ton consumes up to 2100Nm
3, be 30000Nm in coke-oven coal tolerance
3during/h, methanol output is only 14.29t, so substantially increases the production burden of enterprise, wastes a large amount of resources of production, be both unfavorable for that the saving of fund is also unfavorable for the protection of environment.
Summary of the invention
In view of this, the invention provides a kind of technique utilizing ammonia tail gas increase yield of methanol processed, improve H
2utilization ratio, reduce gas purging amount, improve the fund utilization rate of enterprise, the burden that reduce further enterprise improves income, strengthens the competitive power of enterprise.
For solving above technical problem, technical scheme of the present invention is:
Utilize a technique for ammonia tail gas increase yield of methanol processed, comprise the following steps:
A, synthetic ammonia tailgas import;
B, gas-liquid separation;
C, tail gas compression;
D, coke-oven gas mix;
E, fine de-sulfur;
F, conversion;
G, mixing compression;
H, synthesis;
I, rectifying.
Synthetic ammonia tailgas in steps A is the discarded tail gas produced in Converter in Natural Gas-Based Ammonia Making Process plant running process, this synthetic ammonia tailgas carries out gas-liquid separation by gas-liquid separator in stepb, fluent meterial in synthetic ammonia tailgas is by gas-liquid separator separates, and the gas after separation enters next step process by pipeline.
Tail gas compression in step C is completed by gas compressor, the quantity of this tail-gas compressor is two, two tail-gas compressors are arranged in parallel, the same time only has a tail-gas compressor to run, every platform tail-gas compressor is all three stage compression, gas in tail-gas compressor after one-level tail gas compression pressure rise to 0.27MPa, then by secondary tail gas compression by boost in pressure to 0.92MPa, finally by three grades of tail gas compression, air pressure is promoted to 2.76MPa.
Synthetic ammonia tailgas in step D after boost in pressure mixes with coke-oven coal gas phase after entering fine de-sulfur entrance, then enters step e and carries out fine de-sulfur process to mixed gas.
Step F is carried out in converter, ammonia tail gas processed after fine de-sulfur process is preheating to 520 DEG C through coke-oven gas preheater tube side, enter converter after being heated to 660 DEG C by preheating oven again, in converter, part ammonia tail gas processed and methane react, and become CO and H
2, CO and H
2and unconverted ammonia tail gas processed is called reforming gas, the reforming gas temperature of converter outlet is 960 DEG C, after waste heat boiler, coke-oven gas preheater shell side, primary pre-heater for coke oven gas, feedwater preheater, air cooler, de-salted water preheater, the temperature of this conversion gas reduces to 40 DEG C successively again, then moisture is removed by gas-liquid separator, enter normal temp zinc oxide again, finally enter step G and carry out mixing compression.
In step G mixing compression by associating compressor complete, associating compressor by transform after gas compression to 6.0MPa and temperature not higher than 100 DEG C.
Synthesis described in step H completes in synthetic tower, and the crude carbinol after synthesis is just completing a whole set of production technique after the rectifying of step I.
Compared with prior art, the present invention has following beneficial effect:
(1) the present invention after utilizing synthetic ammonia remaining tail gas mix the production carrying out methyl alcohol with coke-oven gas, methanol purge gas amount per ton has been reduced to 85Nm
3, decrease the output of periodic off-gases, solve H
2waste problem, methyl alcohol coke-oven gas per ton consumption has been reduced to 1700Nm
3, be 30000Nm in coke-oven coal tolerance
3during/h, methanol output can reach 17.65t, compared with prior art per hourly improves 3.36t, substantially increases the production efficiency of methyl alcohol, improves the competitive power of enterprise further;
(2) the present invention is owing to make use of synthetic ammonia tailgas to carry out the production of methyl alcohol, and this gas is the impurity such as sulfur-bearing, tar, naphthalene not, and main component is CO
2, fine de-sulfur and conversion catalyst can not be consumed, thus further reduce methyl alcohol cost, improve the utilization ratio of business capital;
(3) present invention utilizes synthetic ammonia carries out production from methyl alcohol to the tail gas of airborne release, thus methyl alcohol per ton can reduce discharging CO
20.2t, has very large promoter action and positive effect to environment protection, better protects ecotope.
Accompanying drawing explanation
Fig. 1 is FB(flow block) of the present invention.
Embodiment
Core thinking of the present invention is, provides a kind of technique utilizing ammonia tail gas increase yield of methanol processed, improves H
2utilization ratio, reduce gas purging amount, improve the fund utilization rate of enterprise, the burden that reduce further enterprise improves income, strengthens the competitive power of enterprise.
In order to make those skilled in the art understand technical scheme of the present invention better, below in conjunction with the drawings and specific embodiments, the present invention is described in further detail.
Embodiment
As shown in Figure 1, a kind of technique utilizing ammonia tail gas increase yield of methanol processed, comprises the following steps:
A, synthetic ammonia tailgas import;
B, gas-liquid separation;
C, tail gas compression;
D, coke-oven gas mix;
E, fine de-sulfur;
F, conversion;
G, mixing compression;
H, synthesis;
I, rectifying.
Synthetic ammonia tailgas in steps A is the discarded tail gas produced in Converter in Natural Gas-Based Ammonia Making Process plant running process, this synthetic ammonia tailgas carries out gas-liquid separation by gas-liquid separator in stepb, fluent meterial in synthetic ammonia tailgas is by gas-liquid separator separates, and the gas after separation enters next step process by pipeline.
Tail gas compression in step C is completed by gas compressor, the quantity of this tail-gas compressor is two, two tail-gas compressors are arranged in parallel, the same time only has a tail-gas compressor to run, every platform tail-gas compressor is all three stage compression, gas in tail-gas compressor after one-level tail gas compression pressure rise to 0.27MPa, then by secondary tail gas compression by boost in pressure to 0.92MPa, finally by three grades of tail gas compression, air pressure is promoted to 2.76MPa.
Synthetic ammonia tailgas in step D after boost in pressure mixes with coke-oven coal gas phase after entering fine de-sulfur entrance, then enters step e and carries out fine de-sulfur process to mixed gas.
Step F is carried out in converter, ammonia tail gas processed after fine de-sulfur process is preheating to 520 DEG C through coke-oven gas preheater tube side, enter converter after being heated to 660 DEG C by preheating oven again, in converter, part ammonia tail gas processed and methane react, and become CO and H
2, CO and H
2and unconverted ammonia tail gas processed is called reforming gas, the reforming gas temperature of converter outlet is 960 DEG C, after waste heat boiler, coke-oven gas preheater shell side, primary pre-heater for coke oven gas, feedwater preheater, air cooler, de-salted water preheater, the temperature of this conversion gas reduces to 40 DEG C successively again, then moisture is removed by gas-liquid separator, enter normal temp zinc oxide again, finally enter step G and carry out mixing compression.
In step G mixing compression by associating compressor complete, associating compressor by transform after gas compression to 6.0MPa and temperature not higher than 100 DEG C.
Synthesis described in step H completes in synthetic tower, and the crude carbinol after synthesis is just completing a whole set of production technique after the rectifying of step I.
Below be only the preferred embodiment of the present invention, it should be pointed out that above-mentioned preferred implementation should not be considered as limitation of the present invention, protection scope of the present invention should be as the criterion with claim limited range.For those skilled in the art, without departing from the spirit and scope of the present invention, can also make some improvements and modifications, these improvements and modifications also should be considered as protection scope of the present invention.
Claims (6)
1. utilize a technique for ammonia tail gas increase yield of methanol processed, it is characterized in that, comprise the following steps:
A, synthetic ammonia tailgas import;
B, gas-liquid separation;
C, tail gas compression;
D, coke-oven gas mix;
E, fine de-sulfur;
F, conversion;
G, mixing compression;
H, synthesis;
I, rectifying;
Step F is carried out in converter, ammonia tail gas processed after fine de-sulfur process is preheating to 520 DEG C through coke-oven gas preheater tube side, enter converter after being heated to 660 DEG C by preheating oven again, in converter, part ammonia tail gas processed and methane react, and become CO and H
2, CO and H
2and unconverted ammonia tail gas processed is called reforming gas, the reforming gas temperature of converter outlet is 960 DEG C, after waste heat boiler, coke-oven gas preheater shell side, primary pre-heater for coke oven gas, feedwater preheater, air cooler, de-salted water preheater, the temperature of this conversion gas reduces to 40 DEG C successively again, then moisture is removed by gas-liquid separator, enter normal temp zinc oxide again, finally enter step G and carry out mixing compression.
2. a kind of technique utilizing ammonia tail gas increase yield of methanol processed according to claim 1, it is characterized in that, synthetic ammonia tailgas in steps A is the discarded tail gas produced in Converter in Natural Gas-Based Ammonia Making Process plant running process, this synthetic ammonia tailgas carries out gas-liquid separation by gas-liquid separator in stepb, fluent meterial in synthetic ammonia tailgas is by gas-liquid separator separates, and the gas after separation enters next step process by pipeline.
3. a kind of technique utilizing ammonia tail gas increase yield of methanol processed according to claim 2, it is characterized in that, tail gas compression in step C is completed by gas compressor, the quantity of this tail-gas compressor is two, two tail-gas compressors are arranged in parallel, the same time only has a tail-gas compressor to run, every platform tail-gas compressor is all three stage compression, gas in tail-gas compressor after one-level tail gas compression pressure rise to 0.27MPa, then by secondary tail gas compression by boost in pressure to 0.92MPa, finally by three grades of tail gas compression, air pressure is promoted to 2.76MPa.
4. a kind of technique utilizing ammonia tail gas increase yield of methanol processed according to claim 3, it is characterized in that, synthetic ammonia tailgas in step D after boost in pressure mixes with coke-oven coal gas phase after entering fine de-sulfur entrance, then enters step e and carries out fine de-sulfur process to mixed gas.
5. a kind of technique utilizing ammonia tail gas increase yield of methanol processed according to claim 1, it is characterized in that, in step G mixing compression by associating compressor complete, associating compressor by transform after gas compression to 6.0MPa and temperature not higher than 100 DEG C.
6. a kind of technique utilizing ammonia tail gas increase yield of methanol processed according to claim 1, it is characterized in that, the synthesis described in step H completes in synthetic tower, and the crude carbinol after synthesis is just completing a whole set of production technique after the rectifying of step I.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101096331A (en) * | 2007-07-10 | 2008-01-02 | 庞玉学 | Method for integral production of liquid ammonia and methanol and/or dimethyl ether by using coke oven gas as raw material |
| CN101239887A (en) * | 2008-02-01 | 2008-08-13 | 七台河宝泰隆煤化工有限公司 | Technique for coproducing methanol from coke oven gas and fuel products by hydrogenating coal tar prepared from tail gas of methanol preparation |
| CN101284761A (en) * | 2008-06-06 | 2008-10-15 | 西北化工研究院 | Process for combined preparing methylic alcohol, natural gas for automobile and synthesis ammonia form industrial end gas rich in carbon and hydrogen |
| CN102924228A (en) * | 2012-11-28 | 2013-02-13 | 西南化工研究设计院有限公司 | Method for producing methanol from semi-coke furnace tail gas |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0597125A (en) * | 1991-10-01 | 1993-04-20 | Komatsu Ltd | Pull-out tension control device of band-shaped material |
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2014
- 2014-05-12 CN CN201410198411.6A patent/CN103936557B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101096331A (en) * | 2007-07-10 | 2008-01-02 | 庞玉学 | Method for integral production of liquid ammonia and methanol and/or dimethyl ether by using coke oven gas as raw material |
| CN101239887A (en) * | 2008-02-01 | 2008-08-13 | 七台河宝泰隆煤化工有限公司 | Technique for coproducing methanol from coke oven gas and fuel products by hydrogenating coal tar prepared from tail gas of methanol preparation |
| CN101284761A (en) * | 2008-06-06 | 2008-10-15 | 西北化工研究院 | Process for combined preparing methylic alcohol, natural gas for automobile and synthesis ammonia form industrial end gas rich in carbon and hydrogen |
| CN102924228A (en) * | 2012-11-28 | 2013-02-13 | 西南化工研究设计院有限公司 | Method for producing methanol from semi-coke furnace tail gas |
Non-Patent Citations (1)
| Title |
|---|
| 合成氨生产中的废弃利用与节能效益;任东;《北京节能》;19950630(第6期);第44-45页 * |
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