CN208266091U - A kind of system of preparing methanol from coke oven gas, methane and coproducing synthetic ammonia - Google Patents
A kind of system of preparing methanol from coke oven gas, methane and coproducing synthetic ammonia Download PDFInfo
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- CN208266091U CN208266091U CN201820532138.XU CN201820532138U CN208266091U CN 208266091 U CN208266091 U CN 208266091U CN 201820532138 U CN201820532138 U CN 201820532138U CN 208266091 U CN208266091 U CN 208266091U
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Abstract
The utility model provides the system of a kind of preparing methanol from coke oven gas, methane and coproducing synthetic ammonia, belongs to chemical technology field.The system comprises the oven gas compression unit being sequentially communicated, clean unit, purified gas compression unit, methanol synthesis unit I, methanation unit, separative unit and synthesis ammonia units, and the system also includes the methanol rectification units being connected to methanol synthesis unit I.The system also includes the pure oxygen reformation unit being sequentially communicated, converts gas compression unit and methanol synthesis unit II, pure oxygen reformation unit are connected to clean unit, methanol synthesis unit II is connected to methanol rectification unit.Oven gas after purification is combined by methanolizing and methanation and produces methanol and methane product by Tthe utility model system, and tail gas is generated to synthesis ammonia in conjunction with the nitrogen of space division by-product, methanol, methane and synthesis three kinds of products of ammonia are obtained simultaneously, and the yield of three kinds of products can be adjusted according to demand, improve Business survival ability.
Description
Technical field
The utility model belongs to chemical field.In particular to methanol, methane and the technology of preparing for synthesizing ammonia, it is specially a kind of
The system of preparing methanol from coke oven gas, methane and coproducing synthetic ammonia.
Background technique
Currently, coke-oven plant's by-product oven gas is mainly for the preparation of methanol or methanol by-product synthesis ammonia or methane or methane by-product
Synthesize ammonia.
Oven gas prepares methanol by-product synthesis ammonia route, is using oven gas pure oxygen reformation producing synthesis gas, synthesis gas closes
At methanol product, the periodic off-gases of synthesis extract hydrogen using PSA Technology and the mixing of space division by-product high pure nitrogen is produced
Ammonia is synthesized, since methanol-fueled CLC periodic off-gases amount is less, synthesizes ammonia preparation in addition to the carbon monoxide and carbon dioxide in unstripped gas
Content requirement is very low (being less than 10PPm), and the hydrogen yield for extracting periodic off-gases pressure-variable adsorption is low, and obtained synthesis hydrazine yield is low,
Gas after periodic off-gases extraction hydrogen also contains the clean component such as hydrogen, carbon monoxide, carbon dioxide, methane and nitrogen, makees
For fuel burn-up, underuse unfortunately.
Oven gas prepares methane by-product synthesis ammonia route, is to use methanation process by carbon monoxide in oven gas and dioxy
Change carbon and react generation methane with hydrogen, methane gas is then obtained using pressure-variable adsorption or cold separation technology or liquefied methane produces
Product, tail gas are that synthesis ammonia is produced after mixing with nitrogen rich in hydrogen gas.Since tail gas tolerance is less, obtained synthesis ammonia is produced
Measure it is low, in addition synthesis synthesis ammonia needed for high pure nitrogen need separately builds device offer, synthesis ammonia benefit not as good as methanol by-product synthesize ammonia
It is profitable, in addition after oven gas purification, also need to increase a superfinishing purification system before methanation device to be further backing out
Sulfide.
Both the above route major product only has one kind, i.e., methanol or methane, anti-market risk ability are poor.
Utility model content
The purpose of the utility model is to provide the systems of a kind of preparing methanol from coke oven gas, methane and coproducing synthetic ammonia, this is practical
Oven gas after purification is combined by methanolizing and methanation and produces methanol and methane product by novel system, and by tail gas and space division
The nitrogen of by-product, which combines, generates synthesis ammonia, while obtaining methanol, methane and synthesis three kinds of products of ammonia, and can adjust three according to demand
The yield of kind product, improves Business survival ability.
The utility model aim is achieved through the following technical solutions:
The system of a kind of preparing methanol from coke oven gas, methane and coproducing synthetic ammonia, the system comprises the oven gas being sequentially communicated
Compression unit, clean unit, purified gas compression unit, methanol synthesis unit I, methanation unit, separative unit and synthesis ammonia
Unit, the system also includes the methanol rectification units being connected to methanol synthesis unit I.
One of system as a kind of preparing methanol from coke oven gas described in the utility model, methane and coproducing synthetic ammonia is specific real
Example is applied, the system also includes the pure oxygen reformation units being sequentially communicated, and convert gas compression unit and methanol synthesis unit II, pure
Oxygen conversion unit is connected to clean unit, and methanol synthesis unit II is connected to methanol rectification unit.
One of system as a kind of preparing methanol from coke oven gas described in the utility model, methane and coproducing synthetic ammonia is specific real
Example is applied, the methanol synthesis unit II is also connected to methanol synthesis unit I or methanolizing unit.
One of system as a kind of preparing methanol from coke oven gas described in the utility model, methane and coproducing synthetic ammonia is specific real
Example is applied, the methanol synthesis unit II is also connected to methanation unit.
One of system as a kind of preparing methanol from coke oven gas described in the utility model, methane and coproducing synthetic ammonia is specific real
Example is applied, the pure oxygen reformation unit is passed through oxygen, and the synthesis ammonia unit is passed through nitrogen.
One of system as a kind of preparing methanol from coke oven gas described in the utility model, methane and coproducing synthetic ammonia is specific real
Apply example, nitrogen of the nitrogen from air separation unit by-product.
One of system as a kind of preparing methanol from coke oven gas described in the utility model, methane and coproducing synthetic ammonia is specific real
Example is applied, the purified gas compression unit includes heat exchanger and compressor.
One of system as a kind of preparing methanol from coke oven gas described in the utility model, methane and coproducing synthetic ammonia is specific real
Example is applied, the carbon monoxide of methanation unit and gas concentration lwevel add up to content to be less than 5PPm out.
One of system as a kind of preparing methanol from coke oven gas described in the utility model, methane and coproducing synthetic ammonia is specific real
Example is applied, when methane product is gas, the separative unit is pressure-swing absorption apparatus, and the gas after methanation passes through pressure-variable adsorption
The product rich in methane and the gas rich in hydrogen are separated into after device；When methane product is liquid, the separative unit
For cryogenic liquefying device, the gas after methanation is separated into liquid product and richness rich in methane after cryogenic liquefying device
The gas of hydrogen.
One of system as a kind of preparing methanol from coke oven gas described in the utility model, methane and coproducing synthetic ammonia is specific real
Example is applied, main group of the oven gas becomes H2、CO、CO2、CH4、N2。
The system of a kind of preparing methanol from coke oven gas of the utility model, methane and coproducing synthetic ammonia, specific embodiment are as follows:
Oven gas is divided into two parts after oven gas compression unit and clean unit processing, respectively enters methanol-fueled CLC list
Member I and methanol synthesis unit II.Ratio is adjustable between two parts, when it is desirable that when voluminous methanol product, few methane phase product,
Go the coke oven tolerance of methanol synthesis unit II with regard to big, vice versa.
Into methanol synthesis unit I purified gas be introduced into purified gas compression unit heat exchange be cooled to room temperature, then compress,
Enter I synthetic coarse methanol of methanol synthesis unit after mixing again with the periodic off-gases of methanol synthesis unit II, methanol synthesis unit I
Periodic off-gases demethanization unit.
Purified gas into methanol synthesis unit II is introduced into pure oxygen reformation unit and is converted into containing carbon monoxide, carbon dioxide
And the synthesis gas of hydrogen, synthesis gas using after conversion air pressure contracting cell compression into II synthetic coarse methanol of methanol synthesis unit,
The periodic off-gases of methanol synthesis unit II remove methanol synthesis unit I or demethanization unit.
The crude carbinol that methanol synthesis unit I and methanol synthesis unit II synthesize send methanol rectification unit to produce refined methanol production
Product.
In methanation unit, carbon monoxide and carbon dioxide are completely converted into the periodic off-gases of methanol synthesis unit I
Methane, subsequently into separative unit.
Separative unit is arranged according to methane product type, and when methane product is gas, separative unit is pressure-variable adsorption
Device, the gas after methanation are separated into the product rich in methane and the gas rich in hydrogen after pressure-swing absorption apparatus；
When methane product is liquid, separative unit is cryogenic liquefying device, and the gas after methanation divides after cryogenic liquefying device
From for the liquid product rich in methane and rich in the gas of hydrogen.
The nitrogen rich in hydrogen gas and air separation unit by-product that separative unit comes out enters after being mixed in a certain ratio to be closed
The standby synthesis ammonolysis product of ammonification unit style.
Compared with prior art, the utility model has the following beneficial effects:
1, methanol, methane and synthesis three kinds of products of ammonia are obtained simultaneously, and can adjust the yield of three kinds of products according to demand；
2, there is methanol synthesis unit before methanation unit, do not need superfinishing purification system, reduce investment outlay；
3, mostly as the nitrogen source for producing synthesis ammonia after nitrogen boosts with system in oven gas, supplement nitrogen amount is saved,
And save supplement nitrogen compression energy consumption.
Detailed description of the invention
Fig. 1 is the process flow diagram of a kind of preparing methanol from coke oven gas of the utility model, methane and coproducing synthetic ammonia system.
Fig. 2 is the process flow diagram of a kind of preparing methanol from coke oven gas of embodiment 1, methane and coproducing synthetic ammonia.
Fig. 3 is the process flow diagram of a kind of preparing methanol from coke oven gas of embodiment 2, methane and coproducing synthetic ammonia.
Specific embodiment
With reference to the accompanying drawing, the utility model is described in detail.
In order to make the purpose of the utility model, technical solutions and advantages more clearly understood, below in conjunction with attached drawing and implementation
Example, the present invention will be further described in detail.It should be appreciated that specific embodiment described herein is only used to explain
The utility model is not used to limit the utility model.
Embodiment 1
The process flow of a kind of preparing methanol from coke oven gas of the present embodiment, methane and coproducing synthetic ammonia is as follows:
Process is as shown in Figure 2.The present embodiment is with 60000Nm3For/h raw coke oven gas, oven gas is mainly organized as H2:
58.7%, CO:9.0%, CO2: 2.8%, CH4: 23.0%, N2: 3.5%, CnHm:2.5%, by oven gas compression unit pressure
It is reduced to 2.4Mpa (G) and enters clean unit, in clean unit, the impurity such as tar and naphthalene in oven gas are adsorbed abjection,
Organic sulfur in oven gas is deviate from by hydrodesulfurization, and the total sulfur of the purified gas of clean unit is less than 0.1PPm out, and temperature 300~
380 DEG C, pressure 2.2Mpa (G), flow 60000Nm3/ h, purified gas are divided into two parts: 30000Nm3/ h purified gas enters pure oxygen and turns
Change unit；30000Nm3/ h purified gas enters evolution purified gas compression unit.
Pure oxygen 5280Nm is added in pure oxygen reformation unit3/ h, the hydro carbons such as methane, ethane in purified gas are largely converted into
Carbon monoxide, carbon dioxide and hydrogen, the conversion gas of pure oxygen reformation unit is mainly organized as H out2: 70.9%, CO:18.6%,
CO2: 6.9%, CH4: 0.8%, N2: 2.3%, flow 46270Nm3/ h, 40 DEG C of temperature, pressure 1.95Mpa (G), into conversion gas
Compression unit is compressed to 5.3Mpa (G), subsequently into II synthesizing methanol of methanol synthesis unit.Methanol synthesis unit II synthesizes thick
Methanol is mainly organized as CH3OH:79.2%, H2O:19.4%, flow 17700kg/h go methanol rectification unit to produce methanol production
Product；The periodic off-gases of methanol synthesis unit II are mainly organized as H2: 78.3%, CO:3.3%, CO2: 4.8%, CH4: 3.2%, N2:
9.6%, flow 11090Nm3/ h, 40 DEG C of temperature, pressure 4.95Mpa (G) removes methanol synthesis unit I.
Into purified gas compression unit purified gas first pass through heat exchanger heat exchange cool to 40 DEG C, then by purification air pressure
Contracting machine is compressed to 4.8Mpa (G), with from the periodic off-gases of methanol synthesis unit II mix after enter methanol synthesis unit I synthesize first
Alcohol.The crude carbinol that methanol synthesis unit I synthesizes mainly is organized as CH3OH:72.5%, H2O:26.0%, flow 4042kg/h, goes
Methanol rectification unit produces methanol product；The periodic off-gases of methanol synthesis unit I are mainly organized as H2: 62.6%, CO:2.8%,
CO2: 3.1%, CH4: 22.4%, N2: 6.6%, CnHm:2.3%, flow 31850Nm3/ h, 40 DEG C of temperature, pressure 4.63Mpa
(G), demethanization unit.
Enter methanol rectification unit after the crude carbinol mixing that methanol synthesis unit I and methanol synthesis unit II synthesize, passes through
Rectifying obtains refined methanol product 18760kg/h.
Carbon monoxide and carbon dioxide are reacted with hydrogen in methanation unit, in periodic off-gases generates methane, out methanation
Carbon monoxide and carbon dioxide add up to content to be less than 5PPm in the gas of unit, and gas is mainly organized as H2: 52.9%, CH4:
35.8%, N2: 8.3%, CnHm:2.9%, flow 25230Nm3/ h, 40 DEG C of temperature, pressure 4.43Mpa (G), into pressure-variable adsorption
Device is separated by pressure-swing absorption apparatus, respectively obtains two strands of gases, one is rich in methane gas, and main group becomes H2:
6.2%, CH4: 83.2%, N2: 3.9%, CnHm:6.7%, flow 10850Nm3/ h, as product methane gas, another stock is rich in
Hydrogen, main group become H2: 88.2%, CH4: 0.1%, N2: 117%, flow 14380Nm3/ h, pressure 4.4Mpa (G), with
The 2545Nm of air separation unit by-product3Enter synthesis ammonia unit after/h supplement nitrogen mixing and produce synthesis ammonolysis product, synthesizes hydrazine yield
6190kg/h。
Embodiment 2
The process flow of a kind of preparing methanol from coke oven gas of the present embodiment, methane and coproducing synthetic ammonia is as follows:
Process is as shown in Figure 3.The present embodiment is with 80000Nm3For/h raw coke oven gas, oven gas is mainly organized as H2:
58.7%, CO:9.0%, CO2: 2.8%, CH4: 23.0%, N2: 3.5%, CnHm:2.5%, by oven gas compression unit pressure
It is reduced to 2.4Mpa (G) and enters clean unit, in clean unit, the impurity such as tar and naphthalene in oven gas are adsorbed abjection,
Organic sulfur in oven gas is deviate from by hydrodesulfurization, and the total sulfur of the purified gas of clean unit is less than 0.1PPm out, and temperature 300~
380 DEG C, pressure 2.2Mpa (G), flow 80000Nm3/ h, purified gas are divided into two parts: 30000Nm3/ h purified gas enters pure oxygen and turns
Change unit；50000Nm3/ h purified gas enters evolution purified gas compression unit.
Pure oxygen 5280Nm is added in pure oxygen reformation unit3/ h, the hydro carbons such as methane, ethane in purified gas are largely converted into
Carbon monoxide, carbon dioxide and hydrogen, the conversion gas of conversion unit is mainly organized as H out2: 70.9%, CO:18.6%, CO2:
6.9%, CH4: 0.8%, N2: 2.3%, flow 46270Nm3/ h, 40 DEG C of temperature, pressure 1.95Mpa (G), into conversion air pressure contracting
Cell compression is to 5.3Mpa (G), subsequently into II synthesizing methanol of methanol synthesis unit.The crude carbinol that methanol synthesis unit II synthesizes
Main group becomes CH3OH:79.2%, H2O:19.4%, flow 17700kg/h go methanol rectification unit to produce methanol product；First
The periodic off-gases of alcohol synthesis unit II are mainly organized as H2: 78.3%, CO:3.3%, CO2: 4.8%, CH4: 3.2%, N2: 9.6%,
Flow 11090Nm3/ h, 40 DEG C of temperature, pressure 4.95Mpa (G), demethanization unit.
Into purified gas compression unit purified gas first pass through heat exchanger heat exchange cool to 40 DEG C, then by purification air pressure
Contracting machine is compressed to 4.8Mpa (G), into I synthesizing methanol of methanol synthesis unit.The main group of crude carbinol that methanol synthesis unit I synthesizes
As CH3OH:79.0%, H2O:18.9%, flow 4730kg/h go methanol rectification unit to produce methanol product；Methanol-fueled CLC list
The periodic off-gases of member I are mainly organized as H2: 60.3%, CO:3.1%, CO2: 3.2%, CH4: 24.6%, N2: 5.9%, CnHm:
2.6%, flow 47815Nm3/ h, 40 DEG C of temperature, pressure 4.63Mpa (G) is mixed with from the periodic off-gases of methanol synthesis unit II
Demethanization unit afterwards.
Enter methanol rectification unit after the crude carbinol mixing that methanol synthesis unit I and methanol synthesis unit II synthesize, passes through
Rectifying obtains refined methanol product 18680kg/h.
Carbon monoxide and carbon dioxide are reacted with hydrogen in methanation unit, in periodic off-gases generates methane, out methanation
Carbon monoxide and carbon dioxide add up to content to be less than 5PPm in the gas of unit, and gas is mainly organized as H2: 45.9%, CH4:
43.2%, N2: 7.6%, CnHm:3.3%, flow 37010Nm3/ h, 40 DEG C of temperature, pressure 4.43Mpa (G), into cryogenic liquefying
Device.It separates, obtains in dehydrogenation column overhead rich in hydrogen, main group becomes H by cryogenic liquefying device dehydrogenation tower rectifying2:
89.9%, CH4: 0.6%, N2: 9.5%, flow 18293Nm3/ h, pressure 3.9Mpa (G), with air separation unit by-product
3744Nm3Enter synthesis ammonia unit after/h supplement nitrogen mixing and produce synthesis ammonolysis product, synthesizes hydrazine yield 8022kg/h, dehydrogenation tower
Tower bottom is obtained rich in methane liquid, and main group becomes H2: 2.9%, CH4: 84.9%, N2: 5.7%, CnHm:6.6%, temperature-
106 DEG C, pressure 3.9Mpa (G), flow 18716Nm3Then/h will be enriched in nitrogen gas by denitrification column and deviate from from tower top, main
It organizes as H2: 33.3%, CH4: 1.5%, N2: 65.2%, flow 1627Nm3/ h, pressure 0.5Mpa (G), as fuel gas,
Denitrogenation tower bottom is liquid methane product, and main group becomes CH4: 92.8%, CnHm:7.2%, -133 DEG C of temperature, pressure
0.5Mpa (G), flow 17090Nm3/h。
The above is only the preferred embodiment of the utility model only, is not intended to limit the utility model, all at this
Made any modifications, equivalent replacements, and improvements etc., should be included in the utility model within the spirit and principle of utility model
Protection scope within.
Claims (10)
1. the system of a kind of preparing methanol from coke oven gas, methane and coproducing synthetic ammonia, which is characterized in that the system comprises be sequentially communicated
Oven gas compression unit, clean unit, purified gas compression unit, methanol synthesis unit I, methanation unit, separative unit with
And synthesis ammonia unit, the system also includes the methanol rectification units being connected to methanol synthesis unit I.
2. the system of a kind of preparing methanol from coke oven gas, methane and coproducing synthetic ammonia as described in claim 1, which is characterized in that described
System further includes the pure oxygen reformation unit being sequentially communicated, and converts gas compression unit and methanol synthesis unit II, pure oxygen reformation list
Member is connected to clean unit, and methanol synthesis unit II is connected to methanol rectification unit.
3. the system of a kind of preparing methanol from coke oven gas, methane and coproducing synthetic ammonia as claimed in claim 2, which is characterized in that described
Methanol synthesis unit II is also connected to methanol synthesis unit I or methanolizing unit.
4. the system of a kind of preparing methanol from coke oven gas, methane and coproducing synthetic ammonia as claimed in claim 2, which is characterized in that described
Methanol synthesis unit II is also connected to methanation unit.
5. the system of a kind of preparing methanol from coke oven gas, methane and coproducing synthetic ammonia as claimed in claim 2, which is characterized in that described
Pure oxygen reformation unit is passed through oxygen, and the synthesis ammonia unit is passed through nitrogen.
6. the system of a kind of preparing methanol from coke oven gas, methane and coproducing synthetic ammonia as claimed in claim 5, which is characterized in that described
Nitrogen of the nitrogen from air separation unit by-product.
7. the system of a kind of preparing methanol from coke oven gas, methane and coproducing synthetic ammonia as described in claim 1, which is characterized in that described
Purified gas compression unit includes heat exchanger and compressor.
8. the system of a kind of preparing methanol from coke oven gas, methane and coproducing synthetic ammonia as described in claim 1, which is characterized in that go out first
The carbon monoxide and gas concentration lwevel of alkylation unit add up to content to be less than 5PPm.
9. the system of a kind of preparing methanol from coke oven gas, methane and coproducing synthetic ammonia as described in claim 1, which is characterized in that work as first
When alkane product is gas, the separative unit is pressure-swing absorption apparatus, and the gas after methanation divides after pressure-swing absorption apparatus
From for the product rich in methane and rich in the gas of hydrogen；When methane product is liquid, the separative unit is cryogenic liquid
Makeup is set, and the gas after methanation is separated into liquid product rich in methane after cryogenic liquefying device and rich in hydrogen
Gas.
10. the system of a kind of preparing methanol from coke oven gas, methane and coproducing synthetic ammonia as described in claim 1, which is characterized in that described
Main group of oven gas becomes H2、CO、CO2、CH4、N2。
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| CN201820532138.XU CN208266091U (en) | 2018-04-16 | 2018-04-16 | A kind of system of preparing methanol from coke oven gas, methane and coproducing synthetic ammonia |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201820532138.XU CN208266091U (en) | 2018-04-16 | 2018-04-16 | A kind of system of preparing methanol from coke oven gas, methane and coproducing synthetic ammonia |
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Address after: No. 5 high tech Zone Gaopeng road in Chengdu city of Sichuan Province in 610041 Patentee after: Haohua Chemical Technology Group Co.,Ltd. Address before: No. 5 high tech Zone Gaopeng road in Chengdu city of Sichuan Province in 610041 Patentee before: SICHUAN TIANYI SCIENCE AND TECHNOLOGY Co.,Ltd. |
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Effective date of registration: 20200803 Address after: No. 5 high tech Zone Gaopeng road in Chengdu city of Sichuan Province in 610041 Patentee after: SOUTHWEST RESEARCH & DESIGN INSTITUTE OF CHEMICAL INDUSTRY Address before: No. 5 high tech Zone Gaopeng road in Chengdu city of Sichuan Province in 610041 Patentee before: Haohua Chemical Technology Group Co.,Ltd. |