CN104649226A - Oxygen feeding operation method at methanol conversion section - Google Patents
Oxygen feeding operation method at methanol conversion section Download PDFInfo
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- CN104649226A CN104649226A CN201310600452.9A CN201310600452A CN104649226A CN 104649226 A CN104649226 A CN 104649226A CN 201310600452 A CN201310600452 A CN 201310600452A CN 104649226 A CN104649226 A CN 104649226A
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Abstract
The invention relates to an oxygen feeding operation method at a methanol conversion section, belonging to the technical field of methanol synthesis. The operation method comprises the following working processes and steps: (1) preheating coke oven gas; (2) supplying fuel gas; (3) supplying oxygen; (4) supplying a boiler with water; (5) treating condensate; and (6) treating conversion gas. According to the oxygen feeding operation method at the methanol conversion section, the oxygen feeding of the conversion section can be conducted through 0.6MPa low-pressure steam instead of 3.0 MPa medium-pressure steam, the operation method is favorable in implementation, a great amount of time can be saved in each driving, and the running period of the production can be effectively improved. In addition, a great amount of medium-pressure stream can be saved for a power plant and other departments, the efficiency of stable production can be improved, a great amount of driving investment can be saved, and the production cost can be lowered.
Description
Technical field
The present invention relates to a kind of methanol conversion workshop section and throw oxygen methodology, belong to methanol synthesis technology field.
Background technology
At present, at methanol synthesis technology, methane conversion generally adopts pure oxygen steam reforming.Converter burner passes into oxygen and coke-oven gas burns, and produces a large amount of heat, and the coke(oven)gas after burning and steam enter in conversion catalyst layer and carries out catalytic conversion reaction, and temperature constantly reduces.When entering catalyst layer, there occurs again the catalytic conversion reaction of methane and steam, use a mouthful methane content and meet index request.
And annual value of production 100000 tons of methyl alcohol original design in, conversion section throw oxygen condition must keep vapor pressure 3.0MPa, can not lower than this pressure.To this, in the condition that some enterprises are limited, steam is raised to this pressure needs regular hour and energy consumption, also consumes a large amount of middle pressure steams simultaneously and causes material impact to producing with other link.
Summary of the invention
The object of the invention is to the defect overcoming above-mentioned technology, provide a kind of methanol conversion workshop section to throw oxygen methodology, change middle pressure steam 3.0MPa into low-pressure steam 0.6MPa, to save time, reduce energy consumption, reduce the requirement to air feed, simplify the operation.
To achieve these goals, technical scheme of the present invention is as follows:
Oxygen methodology is thrown by a kind of methanol conversion workshop section, it is characterized in that: comprise following working process and step:
(1) preheating coke-oven gas: from the coke(oven)gas in compression post, pressure≤2.1MPa, temperature 38 ~ 42 DEG C, methane content 23 ~ 27%, be sent to the pre-desulfurizer in fine de-sulfur post and remove inorganic sulfur; Coke(oven)gas after desulfurization is heated to 300 ~ 350 DEG C through the first preheater of coke(oven)gas, enter iron molybdenum hydrogenation groove and organic sulfur conversion is become inorganic sulfur, remove inorganic sulfur through iron-manganese desulfurizer groove and middle temperature zinc oxide bath again, the sulphur content going out fine de-sulfur workshop section controls to enter conversion section at below 0.1PPm.In coke(oven)gas, add 3.0MPa middle pressure steam, steam flow regulates according to the flow of coke(oven)gas, adds the coke(oven)gas after steam and is heated to after more than 400 DEG C through coke(oven)gas preheater, then is preheated to about 580 DEG C through preheating oven and enters converter top;
(2) for fuel gas: from entering together with the coke(oven)gas pressure 20KPa of wet desulphurization, the crude carbinol solution gas that comes with methanol rectification after fuel gas mixing tank mixes, a part enters bottom preheating oven, the air mixed afterfire sent here with air-blaster, for coke(oven)gas preheating provides heat; Another part fuel pneumatic transmission fine de-sulfur heating furnace after fuel gas mixing tank makes fuel;
(3) oxygen: from the oxygen in sky point workshop, purity be 99.6%, temperature 65 DEG C, pressure is 0.6MPa, enter converter top to about 300 DEG C after adding the mixing of 400 DEG C of low-pressure steam, oxygen flow exports methane content (≤1%) according to converter and regulates;
(4) oiler feed: from heat power plant de-salted water, steam tracing phlegma, methanol rectification steam condensate, enter deoxygenation case simultaneously after with the heat of steam condensate, de-salted water is heated to the 103-106 DEG C of oxygen removed in de-salted water.Deoxygenator is pressurized to 5.0MPa except after deoxidation through boiler feedpump, is heated to 180 DEG C at feedwater preheater reforming gas, and the drum through useless pot enters useless pot, produces middle pressure steam; The middle pressure steam that useless pot produces is except this workshop section of supply uses, and rich middle pressure steam is sent to low-pressure steam pipe network through temperature-decreased pressure reducer.
(5) phlegma is processed: the phlegma of gas-liquid separator outlet send circulating water pool or send coking quenching use, also can be sent to deaeration plant and produce de-oxygenised water further and be used;
6) process reforming gas: coke(oven)gas and oxygen, after entering converter respectively, conversion reaction occurs, and the reforming gas of generation is drawn by bottom converter, temperature≤960 DEG C, pressure≤2.2 MPa, methane content≤1.0%, enter useless pot and reclaim heat byproduct steam; Reforming gas temperature reduces to≤and 500 DEG C, then the gas mixture of coke(oven)gas and steam is heated through coke(oven)gas preheater, temperature falls about 370 DEG C, enter coke(oven)gas just preheater heating raw coke(oven)gas again, after temperature reduces to about 250 DEG C, after feedwater preheater reclaims reaction heat further, reforming gas temperature is down to 150 DEG C, is cooled to about 40 DEG C with recirculated cooling water through the first water cooler and the second water cooler; Through gas-liquid separator separates process condensate, after enter normal temp zinc oxide desulfurizer through steam heater, go out the reforming gas of zinc oxide desulfurization groove, temperature about 40 DEG C, pressure 2.0MPa is sent to compressor compresses four sections of entrances.
Beneficial effect of the present invention is: in contriver company, run through the methanol production of nearly 3 years, 3.0MPa middle pressure steam is replaced to carry out the throwing oxygen of conversion section by 0.6MPa low-pressure steam, this methodology operational excellence, save a large amount of time when each driving, effectively improve the cycle of operation of production.Also save a large amount of middle pressure steams for power plant and other department simultaneously, for company's stably manufactured improves efficiency, saved a large amount of driving fund, reduced production cost.
Embodiment
Embodiment
This methanol conversion workshop section adopts throwing oxygen methodology to carry out methanol-fueled CLC, and its detailed process comprises the following steps:
(1) preheating coke-oven gas: from the coke(oven)gas in compression post, pressure≤2.1MPa, temperature 38 ~ 42 DEG C, methane content 23 ~ 27%, be sent to the pre-desulfurizer in fine de-sulfur post and remove inorganic sulfur; Coke(oven)gas after desulfurization is heated to 300 ~ 350 DEG C through the first preheater of coke(oven)gas, enter iron molybdenum hydrogenation groove and organic sulfur conversion is become inorganic sulfur, remove inorganic sulfur through iron-manganese desulfurizer groove and middle temperature zinc oxide bath again, the sulphur content going out fine de-sulfur workshop section controls to enter conversion section at below 0.1PPm.In coke(oven)gas, add 3.0MPa middle pressure steam, steam flow regulates according to the flow of coke(oven)gas, adds the coke(oven)gas after steam and is heated to after more than 400 DEG C through coke(oven)gas preheater, then is preheated to about 580 DEG C through preheating oven and enters converter top;
(2) for fuel gas: from entering together with the coke(oven)gas pressure 20KPa of wet desulphurization, the crude carbinol solution gas that comes with methanol rectification after fuel gas mixing tank mixes, a part enters bottom preheating oven, the air mixed afterfire sent here with air-blaster, for coke(oven)gas preheating provides heat; Another part fuel pneumatic transmission fine de-sulfur heating furnace after fuel gas mixing tank makes fuel;
(3) oxygen: from the oxygen in sky point workshop, purity be 99.6%, temperature 65 DEG C, pressure is 0.6MPa, enter converter top to about 300 DEG C after adding the mixing of 400 DEG C of low-pressure steam, oxygen flow exports methane content (≤1%) according to converter and regulates;
(4) oiler feed: from heat power plant de-salted water, steam tracing phlegma, methanol rectification steam condensate, enter deoxygenation case simultaneously after with the heat of steam condensate, de-salted water is heated to the 103-106 DEG C of oxygen removed in de-salted water.Deoxygenator is pressurized to 5.0MPa except after deoxidation through boiler feedpump, is heated to 180 DEG C at feedwater preheater reforming gas, and the drum through useless pot enters useless pot, produces middle pressure steam; The middle pressure steam that useless pot produces is except this workshop section of supply uses, and rich middle pressure steam is sent to low-pressure steam pipe network through temperature-decreased pressure reducer.
(5) phlegma is processed: the phlegma of gas-liquid separator outlet send circulating water pool or send coking quenching use, also can be sent to deaeration plant and produce de-oxygenised water further and be used;
6) process reforming gas: coke(oven)gas and oxygen, after entering converter respectively, conversion reaction occurs, and the reforming gas of generation is drawn by bottom converter, temperature≤960 DEG C, pressure≤2.2 MPa, methane content≤1.0%, enter useless pot and reclaim heat byproduct steam; Reforming gas temperature reduces to≤and 500 DEG C, then the gas mixture of coke(oven)gas and steam is heated through coke(oven)gas preheater, temperature falls about 370 DEG C, enter coke(oven)gas just preheater heating raw coke(oven)gas again, after temperature reduces to about 250 DEG C, after feedwater preheater reclaims reaction heat further, reforming gas temperature is down to 150 DEG C, is cooled to about 40 DEG C with recirculated cooling water through the first water cooler and the second water cooler; Through gas-liquid separator separates process condensate, after enter normal temp zinc oxide desulfurizer through steam heater, go out the reforming gas of zinc oxide desulfurization groove, temperature about 40 DEG C, pressure 2.0MPa is sent to compressor compresses four sections of entrances.
The above is the preferred embodiment of the present invention; it should be pointed out that for those skilled in the art, under the premise without departing from the principles of the invention; can also make some improvements and modifications, these improvements and modifications are also considered as protection scope of the present invention.
Claims (1)
1. an oxygen methodology is thrown by methanol conversion workshop section, it is characterized in that: comprise following working process and step:
(1) preheating coke-oven gas: from the coke(oven)gas in compression post, pressure≤2.1MPa, temperature 38 ~ 42 DEG C, methane content 23 ~ 27%, is sent to the pre-desulfurizer in fine de-sulfur post and removes inorganic sulfur; Coke(oven)gas after desulfurization is heated to 300 ~ 350 DEG C through the first preheater of coke(oven)gas, enter iron molybdenum hydrogenation groove and organic sulfur conversion is become inorganic sulfur, remove inorganic sulfur through iron-manganese desulfurizer groove and middle temperature zinc oxide bath again, the sulphur content going out fine de-sulfur workshop section controls to enter conversion section at below 0.1PPm; In coke(oven)gas, add 3.0MPa middle pressure steam, steam flow regulates according to the flow of coke(oven)gas, adds the coke(oven)gas after steam and is heated to after more than 400 DEG C through coke(oven)gas preheater, then is preheated to about 580 DEG C through preheating oven and enters converter top;
(2) for fuel gas: from entering together with the coke(oven)gas pressure 20KPa of wet desulphurization, the crude carbinol solution gas that comes with methanol rectification after fuel gas mixing tank mixes, a part enters bottom preheating oven, the air mixed afterfire sent here with air-blaster, for coke(oven)gas preheating provides heat; Another part fuel pneumatic transmission fine de-sulfur heating furnace after fuel gas mixing tank makes fuel;
(3) oxygen: from the oxygen in sky point workshop, purity be 99.6%, temperature 65 DEG C, pressure is 0.6MPa, enter converter top to about 300 DEG C after adding the mixing of 400 DEG C of low-pressure steam, oxygen flow exports methane content (≤1%) according to converter and regulates;
(4) oiler feed: from heat power plant de-salted water, steam tracing phlegma, methanol rectification steam condensate, enter deoxygenation case simultaneously after with the heat of steam condensate, de-salted water is heated to the 103-106 DEG C of oxygen removed in de-salted water; Deoxygenator is pressurized to 5.0MPa except after deoxidation through boiler feedpump, is heated to 180 DEG C at feedwater preheater reforming gas, and the drum through useless pot enters useless pot, produces middle pressure steam; The middle pressure steam that useless pot produces is except this workshop section of supply uses, and rich middle pressure steam is sent to low-pressure steam pipe network through temperature-decreased pressure reducer;
(5) phlegma is processed: the phlegma of gas-liquid separator outlet send circulating water pool or send coking quenching use, also can be sent to deaeration plant and produce de-oxygenised water further and be used;
(6) process reforming gas: coke(oven)gas and oxygen, after entering converter respectively, conversion reaction occurs, and the reforming gas of generation is drawn by bottom converter, temperature≤960 DEG C, pressure≤2.2 MPa, methane content≤1.0%, enter useless pot and reclaim heat byproduct steam; Reforming gas temperature reduces to≤and 500 DEG C, then the gas mixture of coke(oven)gas and steam is heated through coke(oven)gas preheater, temperature falls about 370 DEG C, enter coke(oven)gas just preheater heating raw coke(oven)gas again, after temperature reduces to about 250 DEG C, after feedwater preheater reclaims reaction heat further, reforming gas temperature is down to 150 DEG C, is cooled to about 40 DEG C with recirculated cooling water through the first water cooler and the second water cooler; Through gas-liquid separator separates process condensate, after enter normal temp zinc oxide desulfurizer through steam heater, go out the reforming gas of zinc oxide desulfurization groove, temperature about 40 DEG C, pressure 2.0MPa is sent to compressor compresses four sections of entrances.
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| CN201310600452.9A CN104649226A (en) | 2013-11-25 | 2013-11-25 | Oxygen feeding operation method at methanol conversion section |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106809804A (en) * | 2017-01-25 | 2017-06-09 | 中国天辰工程有限公司 | A kind of natural gas reforming unit technique lime set recycling system and method |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4238403A (en) * | 1975-03-03 | 1980-12-09 | Imperial Chemical Industries Limited | Methanol synthesis process |
| 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 |
| CN101704712A (en) * | 2009-10-29 | 2010-05-12 | 山西焦化股份有限公司 | Technological method for preparing methanol by combining coke oven gas with water gas |
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- 2013-11-25 CN CN201310600452.9A patent/CN104649226A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4238403A (en) * | 1975-03-03 | 1980-12-09 | Imperial Chemical Industries Limited | Methanol synthesis process |
| 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 |
| CN101704712A (en) * | 2009-10-29 | 2010-05-12 | 山西焦化股份有限公司 | Technological method for preparing methanol by combining coke oven gas with water gas |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106809804A (en) * | 2017-01-25 | 2017-06-09 | 中国天辰工程有限公司 | A kind of natural gas reforming unit technique lime set recycling system and method |
| CN106809804B (en) * | 2017-01-25 | 2019-01-22 | 中国天辰工程有限公司 | A kind of natural gas reforming unit technique lime set recycling system and method |
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Application publication date: 20150527 |