CN102634369A - High-temperature coal tar hydrogenation, post-delayed coking and methanol preparation by utilizing coke oven gas combined technology - Google Patents
High-temperature coal tar hydrogenation, post-delayed coking and methanol preparation by utilizing coke oven gas combined technology Download PDFInfo
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- CN102634369A CN102634369A CN2012101115696A CN201210111569A CN102634369A CN 102634369 A CN102634369 A CN 102634369A CN 2012101115696 A CN2012101115696 A CN 2012101115696A CN 201210111569 A CN201210111569 A CN 201210111569A CN 102634369 A CN102634369 A CN 102634369A
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- coke
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- coal
- methanol
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 150
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 46
- 239000011280 coal tar Substances 0.000 title claims abstract description 45
- 238000004939 coking Methods 0.000 title claims abstract description 26
- 238000005516 engineering process Methods 0.000 title claims abstract description 22
- 239000000571 coke Substances 0.000 title claims abstract description 21
- 238000002360 preparation method Methods 0.000 title abstract 4
- 239000007789 gas Substances 0.000 claims abstract description 78
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 17
- 239000001257 hydrogen Substances 0.000 claims abstract description 17
- 239000006227 byproduct Substances 0.000 claims abstract description 14
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 13
- 239000011331 needle coke Substances 0.000 claims abstract description 7
- 239000000295 fuel oil Substances 0.000 claims description 38
- 238000000034 method Methods 0.000 claims description 20
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 16
- 239000000047 product Substances 0.000 claims description 16
- 230000003111 delayed effect Effects 0.000 claims description 13
- 239000003921 oil Substances 0.000 claims description 13
- 238000006243 chemical reaction Methods 0.000 claims description 12
- 230000006837 decompression Effects 0.000 claims description 12
- 239000010426 asphalt Substances 0.000 claims description 9
- 239000003054 catalyst Substances 0.000 claims description 8
- 238000010521 absorption reaction Methods 0.000 claims description 5
- 230000015572 biosynthetic process Effects 0.000 claims description 5
- 238000003786 synthesis reaction Methods 0.000 claims description 5
- 239000004215 Carbon black (E152) Substances 0.000 claims description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 4
- 230000003139 buffering effect Effects 0.000 claims description 4
- 229910052799 carbon Inorganic materials 0.000 claims description 4
- -1 carbon hydrocarbon Chemical class 0.000 claims description 4
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 4
- 230000003197 catalytic effect Effects 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 4
- 230000005494 condensation Effects 0.000 claims description 4
- 238000005235 decoking Methods 0.000 claims description 4
- 230000000994 depressogenic effect Effects 0.000 claims description 4
- 238000004821 distillation Methods 0.000 claims description 4
- 229930195733 hydrocarbon Natural products 0.000 claims description 4
- 150000002431 hydrogen Chemical class 0.000 claims description 4
- 239000004615 ingredient Substances 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 230000003647 oxidation Effects 0.000 claims description 4
- 238000007254 oxidation reaction Methods 0.000 claims description 4
- 239000006253 pitch coke Substances 0.000 claims description 4
- 230000000087 stabilizing effect Effects 0.000 claims description 4
- 229910052717 sulfur Inorganic materials 0.000 claims description 4
- 239000011593 sulfur Substances 0.000 claims description 4
- 230000002194 synthesizing effect Effects 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 239000002994 raw material Substances 0.000 abstract description 6
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 238000004134 energy conservation Methods 0.000 abstract description 2
- 238000003915 air pollution Methods 0.000 abstract 1
- 239000002131 composite material Substances 0.000 abstract 1
- 238000001179 sorption measurement Methods 0.000 abstract 1
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000011286 gas tar Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Landscapes
- Coke Industry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a high-temperature coal tar hydrogenation, post-delayed coking and methanol preparation by utilizing coke oven gas combined technology. The combined technology comprises the following technologies: (1) a methanol preparation technology by utilizing coke oven gas, (2) a high temperature coal tar hydrogenation technology and (3) a needle coke preparation technology by utilizing a post-delayed coking technology. With the adoption of the combined technology provided by the invention, when a coking plant produces cokes, by-products coke oven gas and high-temperature coal-tar oil are produced, the coke oven gas is used as a raw material for manufacturing methanol, the by-product spread air escape of the methanol is used for preparing hydrogen through a pressure swing adsorption device and then the hydrogen is taken as the raw material for the high-temperature coal tar hydrogenation; the by-product maltha generated by the high-temperature coal tar hydrogenation enters a post-delayed coker, is used as the raw material for manufacturing the needle coke; each productive unit is connected with each step, and a circulation economic model with energy conservation and emission reduction is realized; and therefore, the composite cost is low, the air pollution of the coking plant to surrounding environment is reduced.
Description
Technical field
The present invention relates to a kind of coal-tar heavy oil hydrogenation, back delayed coking and coke-oven gas system methyl alcohol combination process.
Background technology
At present, the delayed coking of Shaanxi Tianyuan company is that the full cut delayed coking of coal tar can not be carried phenol to coal tar and carries naphthalene and handle, and the part light oil fraction is cracked into the following gas of C4 in delayed coking process; Therefore; Domestic coke-oven plant great majority take the method for direct combustion power generation to handle, even recycle, also only limit to produce methyl alcohol; Still there is not complete coke-oven gas system methyl alcohol synthesis tail gas coproduction coal-tar heavy oil hydrogenation system light-weight fuel oil technology both at home and abroad; More do not realize suitability for industrialized production, or institute's hydrogenation hydrogen source adopting process is different, like coal direct gasification technology or hydrogen production from coke oven gas technology.
Summary of the invention
The objective of the invention is to overcome the weak point that exists in the above-mentioned technology, a kind of energy-conservation, reduction of discharging is provided, the coal-tar heavy oil hydrogenation that comprehensive cost is low, back delayed coking and coke-oven gas system methyl alcohol combination process.
In order to achieve the above object, the technical scheme of the present invention's employing is:
(1), coke-oven gas is produced methanol technics:
The coke-oven gas of sending here by the coke-oven plant; At first get into the voltage stabilizing of coke(oven)gas gas holder buffering; The coke(oven)gas compressor is bled and is pressurized to from gas holder and gets into smart desulfurizer behind the 2.5MPa, and the total sulfur in the gas is taken off to 0.1ppm, and methane content reaches 26% in the coke(oven)gas; Adopt the pure oxygen catalytic partial oxidation conversion process methane in the gas and a small amount of many carbon hydrocarbon to be converted into the useful composition carbon monoxide and the hydrogen of synthesizing methanol; Gas ingredients after the conversion satisfies the basic demand of methyl alcohol synthetic raw gas, and the gas after the conversion is depressed into 6.0MPa through synthetic air compressor, gets into methanol synthesizer.The synthetic 6.0MPa low pressure synthetic technology that adopts of methyl alcohol, three-column process flow is adopted in rectifying, and the refined methanol product that rectifying is seen off is stored in the finished product tank field, and the methanol synthesizer by-product is speeded to exit and is delivered to the coal-tar heavy oil hydrogenation unit;
(2), coal-tar heavy oil hydrogenation technique
Isolated coal-tar heavy oil is through the ordinary decompression column distillation in coke-oven plant's coke-oven gas; Propose the light ends oil before 380-410 ℃, get into hydrogenator, under the working condition of 12.5-16.8Ma pressure and 390 ℃; Hydrogen-oil ratio 800: 1 to 1600: 1 and special-purpose hydrogenation catalyst; Carry out hydrogenation reaction through special-purpose coal tar hydrogenation catalyst, produce the fine light-weight fuel oil, it is that the methyl alcohol synthesis tail gas passes through two-stage decompression behind 2.5Mpa that the methanol synthesizer by-product speeds to exit; Get into pressure-swing absorption apparatus and produce 99.99% pure hydrogen, as the hydrogen source of coal-tar heavy oil hydrogenation;
(3), back producing needle coke by utilizing delay coking technology
The ordinary decompression column sub product viscid bitumen of isolated coal-tar heavy oil hydrogenation unit gets in coke-oven plant's coke-oven gas; Delayed coking unit; The post-decompression oil gas of high temperature returns the coal-tar heavy oil hydrogenation unit as reactor feed through after the condensation, and the pitch coke of explaination is produced the burnt product of high-quality asphalt through water conservancy decoking and roasting assembly in the coking tower.
Advantage of the present invention is:
When the present invention makes the coke-oven plant produce coke, by-product coke producer gas and coal-tar heavy oil, coke-oven gas is as the raw material of producing methyl alcohol; The speeding of methyl alcohol by-product exitted and produced the raw material of hydrogen as the coal-tar heavy oil hydrogenation through pressure-swing absorption apparatus, and the viscid bitumen of coal-tar heavy oil hydrogenation by-product gets into the back delayed coking unit, as the raw material of producing needle coke; Each productive unit ring ring links to each other; Realized the recycling economy pattern of energy-saving and emission-reduction, therefore, comprehensive cost is low; Reduced the topsoil of coke-oven plant to surrounding environment; Coal-tar heavy oil hydrogenation, back delayed coking have realized that with coke-oven gas system methyl alcohol combination process the combination of Coal Chemical Industry industry industry chain (supply chain) intersects, and the energy utilization maximization embodies the recycling economy characteristics.
Embodiment
Describe in further detail in the face of embodiments of the invention down.
Embodiment 1,
(1), coke-oven gas is produced methanol technics:
The coke-oven gas of sending here by the coke-oven plant; At first get into the voltage stabilizing of coke(oven)gas gas holder buffering; The coke(oven)gas compressor is bled and is pressurized to from gas holder and gets into smart desulfurizer behind the 2.5MPa, and the total sulfur in the gas is taken off to 0.1ppm, and methane content reaches 26% in the coke(oven)gas; Adopt the pure oxygen catalytic partial oxidation conversion process methane in the gas and a small amount of many carbon hydrocarbon to be converted into the useful composition carbon monoxide and the hydrogen of synthesizing methanol; Gas ingredients after the conversion satisfies the basic demand of methyl alcohol synthetic raw gas, and the gas after the conversion is depressed into 6.0MPa through synthetic air compressor, gets into methanol synthesizer.The synthetic 6.0MPa low pressure synthetic technology that adopts of methyl alcohol, three-column process flow is adopted in rectifying, and the refined methanol product that rectifying is seen off is stored in the finished product tank field, and the methanol synthesizer by-product is speeded to exit and is delivered to the coal-tar heavy oil hydrogenation unit;
(2), coal-tar heavy oil hydrogenation technique
Isolated coal-tar heavy oil is through the ordinary decompression column distillation in coke-oven plant's coke-oven gas; Propose the light ends oil before 380 ℃, get into hydrogenator, under the working condition of 12.5Ma pressure and 390 ℃; Hydrogen-oil ratio 800: 1 and special-purpose hydrogenation catalyst; Carry out hydrogenation reaction through special-purpose coal tar hydrogenation catalyst, produce the fine light-weight fuel oil, it is that the methyl alcohol synthesis tail gas passes through two-stage decompression behind 2.5Mpa that the methanol synthesizer by-product speeds to exit; Get into pressure-swing absorption apparatus and produce 99.99% pure hydrogen, as the hydrogen source of coal-tar heavy oil hydrogenation;
(3), back producing needle coke by utilizing delay coking technology
The ordinary decompression column sub product viscid bitumen of isolated coal-tar heavy oil hydrogenation unit gets in coke-oven plant's coke-oven gas; Delayed coking unit; The post-decompression oil gas of high temperature returns the coal-tar heavy oil hydrogenation unit as reactor feed through after the condensation, and the pitch coke of explaination is produced the burnt product of high-quality asphalt through water conservancy decoking and roasting assembly in the coking tower.
Embodiment 2,
(1), coke-oven gas is produced methanol technics:
The coke-oven gas of sending here by the coke-oven plant; At first get into the voltage stabilizing of coke(oven)gas gas holder buffering; The coke(oven)gas compressor is bled and is pressurized to from gas holder and gets into smart desulfurizer behind the 2.5MPa, and the total sulfur in the gas is taken off to 0.1ppm, and methane content reaches 26% in the coke(oven)gas; Adopt the pure oxygen catalytic partial oxidation conversion process methane in the gas and a small amount of many carbon hydrocarbon to be converted into the useful composition carbon monoxide and the hydrogen of synthesizing methanol; Gas ingredients after the conversion satisfies the basic demand of methyl alcohol synthetic raw gas, and the gas after the conversion is depressed into 6.0MPa through synthetic air compressor, gets into methanol synthesizer.The synthetic 6.0MPa low pressure synthetic technology that adopts of methyl alcohol, three-column process flow is adopted in rectifying, and the refined methanol product that rectifying is seen off is stored in the finished product tank field, and the methanol synthesizer by-product is speeded to exit and is delivered to the coal-tar heavy oil hydrogenation unit;
(2), coal-tar heavy oil hydrogenation technique
Isolated coal-tar heavy oil is through the ordinary decompression column distillation in coke-oven plant's coke-oven gas; Propose the light ends oil before 410 ℃, get into hydrogenator, under the working condition of 16.8Ma pressure and 390 ℃; Hydrogen-oil ratio 1600: 1 and special-purpose hydrogenation catalyst; Carry out hydrogenation reaction through special-purpose coal tar hydrogenation catalyst, produce the fine light-weight fuel oil, it is that the methyl alcohol synthesis tail gas passes through two-stage decompression behind 2.5Mpa that the methanol synthesizer by-product speeds to exit; Get into pressure-swing absorption apparatus and produce 99.99% pure hydrogen, as the hydrogen source of coal-tar heavy oil hydrogenation;
(3), back producing needle coke by utilizing delay coking technology
The ordinary decompression column sub product viscid bitumen of isolated coal-tar heavy oil hydrogenation unit gets in coke-oven plant's coke-oven gas; Delayed coking unit; The post-decompression oil gas of high temperature returns the coal-tar heavy oil hydrogenation unit as reactor feed through after the condensation, and the pitch coke of explaination is produced the burnt product of high-quality asphalt through water conservancy decoking and roasting assembly in the coking tower.
Claims (1)
1. a coal-tar heavy oil hydrogenation, back delayed coking and coke-oven gas system methyl alcohol combination process is characterized in that:
(1), coke-oven gas is produced methanol technics:
The coke-oven gas of sending here by the coke-oven plant; At first get into the voltage stabilizing of coke(oven)gas gas holder buffering; The coke(oven)gas compressor is bled and is pressurized to from gas holder and gets into smart desulfurizer behind the 2.5MPa, and the total sulfur in the gas is taken off to 0.1ppm, and methane content reaches 26% in the coke(oven)gas; Adopt the pure oxygen catalytic partial oxidation conversion process methane in the gas and a small amount of many carbon hydrocarbon to be converted into the useful composition carbon monoxide and the hydrogen of synthesizing methanol; Gas ingredients after the conversion satisfies the basic demand of methyl alcohol synthetic raw gas, and the gas after the conversion is depressed into 6.0MPa through synthetic air compressor, gets into methanol synthesizer.The synthetic 6.0MPa low pressure synthetic technology that adopts of methyl alcohol, three-column process flow is adopted in rectifying, and the refined methanol product that rectifying is seen off is stored in the finished product tank field, and the methanol synthesizer by-product is speeded to exit and is delivered to the coal-tar heavy oil hydrogenation unit;
(2), coal-tar heavy oil hydrogenation technique
Isolated coal-tar heavy oil is through the ordinary decompression column distillation in coke-oven plant's coke-oven gas; Propose the light ends oil before 380-410 ℃, get into hydrogenator, under the working condition of 12.5-16.8Ma pressure and 390 ℃; Hydrogen-oil ratio 800: 1 to 1600: 1 and special-purpose hydrogenation catalyst; Carry out hydrogenation reaction through special-purpose coal tar hydrogenation catalyst, produce the fine light-weight fuel oil, it is that the methyl alcohol synthesis tail gas passes through two-stage decompression behind 2.5Mpa that the methanol synthesizer by-product speeds to exit; Get into pressure-swing absorption apparatus and produce 99.99% pure hydrogen, as the hydrogen source of coal-tar heavy oil hydrogenation;
(3), back producing needle coke by utilizing delay coking technology
The ordinary decompression column sub product viscid bitumen of isolated coal-tar heavy oil hydrogenation unit gets in coke-oven plant's coke-oven gas; Delayed coking unit; The post-decompression oil gas of high temperature returns the coal-tar heavy oil hydrogenation unit as reactor feed through after the condensation, and the pitch coke of explaination is produced the burnt product of high-quality asphalt through water conservancy decoking and roasting assembly in the coking tower.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012101115696A CN102634369A (en) | 2012-04-17 | 2012-04-17 | High-temperature coal tar hydrogenation, post-delayed coking and methanol preparation by utilizing coke oven gas combined technology |
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| Application Number | Priority Date | Filing Date | Title |
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| CN2012101115696A CN102634369A (en) | 2012-04-17 | 2012-04-17 | High-temperature coal tar hydrogenation, post-delayed coking and methanol preparation by utilizing coke oven gas combined technology |
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| CN102634369A true CN102634369A (en) | 2012-08-15 |
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| CN2012101115696A Pending CN102634369A (en) | 2012-04-17 | 2012-04-17 | High-temperature coal tar hydrogenation, post-delayed coking and methanol preparation by utilizing coke oven gas combined technology |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103305246A (en) * | 2013-06-08 | 2013-09-18 | 华电重工股份有限公司 | Pyrolytic poly-generation method of low-rank coal and system |
| CN103642511A (en) * | 2013-12-16 | 2014-03-19 | 陕西师范大学 | Preparation method of high-quality needle coke raw material |
| CN104341267A (en) * | 2014-10-11 | 2015-02-11 | 神华集团有限责任公司 | Method for preparing methanol from high-sulfur coal |
| CN104945224A (en) * | 2015-05-08 | 2015-09-30 | 徐州伟天化工有限公司 | Methanol production process |
| CN105294394A (en) * | 2015-05-08 | 2016-02-03 | 徐州伟天化工有限公司 | Methanol co-production recycling system |
| CN106281447A (en) * | 2016-10-17 | 2017-01-04 | 北京神雾环境能源科技集团股份有限公司 | A kind of coal tar maximizes and produces light Fuel and the method and system of needle coke |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103305246A (en) * | 2013-06-08 | 2013-09-18 | 华电重工股份有限公司 | Pyrolytic poly-generation method of low-rank coal and system |
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| CN103642511B (en) * | 2013-12-16 | 2015-05-20 | 陕西师范大学 | Preparation method of high-quality needle coke raw material |
| CN104341267A (en) * | 2014-10-11 | 2015-02-11 | 神华集团有限责任公司 | Method for preparing methanol from high-sulfur coal |
| CN104945224A (en) * | 2015-05-08 | 2015-09-30 | 徐州伟天化工有限公司 | Methanol production process |
| CN105294394A (en) * | 2015-05-08 | 2016-02-03 | 徐州伟天化工有限公司 | Methanol co-production recycling system |
| CN106281447A (en) * | 2016-10-17 | 2017-01-04 | 北京神雾环境能源科技集团股份有限公司 | A kind of coal tar maximizes and produces light Fuel and the method and system of needle coke |
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Application publication date: 20120815 |