CN106397121A - A biogas-coke oven gas combined methanol production device - Google Patents
A biogas-coke oven gas combined methanol production device Download PDFInfo
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- CN106397121A CN106397121A CN201610641816.1A CN201610641816A CN106397121A CN 106397121 A CN106397121 A CN 106397121A CN 201610641816 A CN201610641816 A CN 201610641816A CN 106397121 A CN106397121 A CN 106397121A
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- gas
- preheater
- separator
- methanol
- biogas
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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
- C07C29/152—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 characterised by the reactor used
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- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
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Abstract
A biogas-coke oven gas combined methanol production device is disclosed. The device includes a gas-holder tank, a separator, a compressor, a filter, a pre-desulphurization tank, a preheater, a hydrogenation pre-converter, a hydrogenation converter and a middle-temperature zinc oxide desulphurization tank which are connected to an impurity remover in order. The preheater is connected to a preheating furnace, a converting furnace and a waste-heat boiler. The preheater is connected through a primary preheater to a boiler water feeding preheater, a desalted water preheater, a separator, a converted gas air cooler, a gas liquid separator, a room-temperature zinc oxide desulphurization tank, a fresh-gas filter and a synthesis gas compressor in order. The synthesis gas compressor is in circulated connection with a gas liquid separator through an interstage cooler. The synthesis gas compressor is connected to a heat exchanger and a methanol synthesis tower in order. The heater is connected to a methanol separator through an air cooler. The methanol separator is separately connected a flash evaporation tank and an alcohol washing tower. The first-stage hydrogenation converter is connected to a heating furnace. A technical problem that the utilization rate of raw materials is low is overcome.
Description
Technical field
The invention belongs to biogas and coke-stove gas co-production technology field, it is related to a kind of biogas and produces methanol dress with cog joint
Put.
Background technology
CH in biogas4Content is in 60% about, CO238% about, biogas as fuel or produces CNG, CO therein to content2
It is all invalid gas, can not embody the maximum value of biogas；And coke-stove gas pure oxygen reformation produces methanol due to hydrogen in conversion gas
Many carbon less lead to produce methanol gas synthesis efficiency low, emptying large-minded.Both gas is using or is existing big in extracting
The waste material of amount is it is impossible to be utilized effectively.
Content of the invention
Present invention aim to address prior art has the low technical problem of utilization ratio, provide a kind of biogas and coke-stove gas
Co-producing methanol device.
To achieve these goals, a kind of biogas of the present invention and cog joint produce methanol device, and it includes being provided with
Biogas import and the trash separator of coke-stove gas import；Its main points is that described trash separator is separated with gas holder, import successively by pipeline
Device, gas compressor, filter, pre- desulfurizer, coal gas just preheater, one-level hydrogenation pre-converter, one-level hydro-conversion device, in
Warm zinc oxide desulfurization groove, secondary hydrogenation converter, zinc oxide desulfurization groove and gas preheater connect；Described gas preheater and pre-
Hot stove, reburner, waste heat boiler circulation connect；Described gas preheater passes through coal gas, and just preheater is preheated with boiler feedwater successively
Device, desalination water preheater, separator, conversion gas air cooler, gas-liquid separator, normal temp zinc oxide desulfurizer, fresh air filter,
Synthesic gas compressor connects；Described synthesic gas compressor is passed through intersegmental cooler and is connected with gas-liquid separator circulation；Described synthesis
Air compressor is connected with heat exchanger and methyl alcohol synthetic reactor successively；Described heat exchanger is connected with methanol separator by air cooler；Institute
State methanol separator respectively with flash tank and wash alcohol tower and be connected；Described one-level hydro-conversion device is provided with intensification heating furnace.
Ferrum molybdenum or nickel is loaded respectively in described one-level hydrogenation pre-converter, one-level hydro-conversion device, secondary hydrogenation converter
Molybdenum catalyst layer, under the catalytic action of catalyst, realizing Organic sulfur hydro-conversion in gas is hydrogen sulfide.
The present invention utilizes biogas and coke-stove gas coproduction to produce methanol, not only increases the added value of biogas it is achieved that work
Industry, the combination of agricultural production, and improve the reaction condition of coke-stove gas methanol device, improve the profit of coke-stove gas
Use efficiency.
Appended drawings are present configuration schematic diagrams.
1- trash separator, 2- gas holder, 3- import separator, 4- gas compressor, 5- filter, the pre- desulfurizer of 6-, 7- in Fig. 1
Coal gas just preheater, 8- one-level hydrogenation pre-converter, 9- one-level hydro-conversion device, 10- middle temperature zinc oxide desulfurization groove, bis- grades of 11-
Hydro-conversion device, 12- zinc oxide desulfurization groove, 13- intensification heating furnace, 14- gas preheater, 15- preheating furnace, 16- reburner,
17- waste heat boiler, 18- feedwater preheater, 19- desalination water preheater, 20- separator, 21- conversion gas air cooler, 22- gas
Liquid/gas separator, 23- normal temp zinc oxide desulfurizer, 24- fresh air filter, 25- synthesic gas compressor, 26- intersegmental cooler,
27- gas-liquid separator, 28- heat exchanger, 29- methyl alcohol synthetic reactor, 30- air cooler, 31- methanol separator, 32- flash tank, 33- wash
Alcohol tower.
Specific embodiment
Referring to the drawings, a kind of biogas and cog joint produce methanol device, and it includes being provided with biogas import and coke-stove gas
The trash separator 1 of import；Described trash separator pass through pipeline successively with gas holder 2, import separator 3, gas compressor 4, filter 5,
Pre- desulfurizer 6, coal gas just preheater 7, one-level hydrogenation pre-converter 8, one-level hydro-conversion device 9, middle temperature zinc oxide desulfurization groove 10,
Secondary hydrogenation converter 11, zinc oxide desulfurization groove 12 and gas preheater 14 connect；Described gas preheater 14 and preheating furnace 15,
Reburner 16, waste heat boiler 17 circulation connect；Described gas preheater passes through coal gas, and just preheater 7 is preheated with boiler feedwater successively
Device 18, desalination water preheater 19, separator 20, conversion gas air cooler 21, gas-liquid separator 22, normal temp zinc oxide desulfurizer 23,
Fresh air filter 24, synthesic gas compressor 25 connect；Described synthesic gas compressor 25 is divided by intersegmental cooler 26 and gas-liquid
Circulate from device 27 and connect；Described synthesic gas compressor 25 is connected with heat exchanger 28 and methyl alcohol synthetic reactor 29 successively；Described heat exchanger
28 are connected with methanol separator 31 by air cooler 30；Described methanol separator 31 respectively with flash tank 32 and wash alcohol tower 33 even
Connect；It is connected with intensification heating furnace 13 on described one-level hydro-conversion device 9.Described one-level hydrogenation pre-converter, one-level hydro-conversion
All load ferrum molybdenum or nickel molybdenum catalyst in device, secondary hydrogenation converter, under the catalytic action of catalyst, realize having in gas
Machine sulfur hydro-conversion is hydrogen sulfide.
Coal gas, biogas sequentially pass through trash separator, gas compressor come by gas holder, import separator, the coke-oven coal after pressurization
Gas, biogas leach through filter and pre- desulfurizer and deliver to coal gas just preheater after mist of oil and removing inorganic sulfur, using conversion gas
Waste heat lifts temperature to 240 ~ 260 DEG C.Gas after temperature raising is through one-level hydrogenation pre-converter, one-level hydro-conversion device, having in gas
Machine sulfur here is converted into inorganic sulfur, in addition, the oxygen in gas also here and hydrogen react generation water, hydrogenation of unsaturated hydrocarbons becomes saturation
Hydrocarbon.Gas after hydro-conversion enters moderate temperature desulphurization groove, and the most inorganic sulfur removings in gas add through two grades afterwards again
Remaining organic sulfur is carried out changing into inorganic sulfur by hydrogen converter, eventually passes zinc oxide desulfurization groove and checks on, and makes total in gas
Sulfur reaches below 0.1PPm.Qualified gas is added into saturated vapor, and steam flow is adjusted according to the flow of oven gas.Add
Gas after steam heats through gas preheater, preheating furnace is preheated to 630 DEG C of entrance reburners.Oxygen from space division adds warp
Reburner is entered, oxygen flow is adjusted according to conversion heater outlet temperature after crossing the steam of preheating furnace preheating（Control≤960 DEG C）.
Coke-stove gas, biogas and oxygen are reacted after respectively enteing reburner top immediately, and conversion gas is drawn by converting furnace bottom, enters
Enter waste heat boiler and reclaim heat byproduct steam.Then conversion gas heats feeding density producer gas, biogas and steam through gas preheater,
Through coal gas, just preheater heats organic sulfur removal unit inlet gas to gas preheater outlet conversion gas, then again through boiler feedwater
Preheater, desalination water preheater reclaim the laggard separator of reaction heat further and separate condensing, more inverted Gas Cooler（Steam
Hairdo cooler）Cool to 40 DEG C after gas-liquid separator separates process condensate, through the removing of room temperature zinc oxide desulfurization groove
In gas, remaining sulfur is to below 0.10PPm.2.0MPa, 40 DEG C of conversion gas filter out after impurity through fresh air filter, enter
Enter one section of synthesic gas compressor to be forced into 3.50MPa and be warming up to 100 DEG C and be cooled to 40 DEG C, gas-liquid separator through intersegmental cooler
After separating condensed water, enter circulation section and mix with the circulating air from methanol separator, be forced into through synthesic gas compressor
The synthesis gas of 6.0MPa delivers to methanol-fueled CLC.
From synthesic gas compressor the shell side through gas-gas heat exchanger for the synthesis gas by from synthetic tower reacted go out tower heat
After gas is heated to 220 DEG C, enter synthesis top of tower.In synthetic tower, CO, CO2With H2Reaction generates first alcohol and water, also simultaneously
Micro other organic impuritiess are had to generate.Synthetic tower exhaust gas enter gas-gas heat exchanger and synthetic tower inlet tower gas heat exchange, entering implication
It is heated to more than active temperature, then enters methanol separator after cooling through air cooler and carry out gas-liquid separation, go out separating methanol
Device gas goes synthesic gas compressor to be pressurized mostly as circulating air and supplements virgin gas.Methanol separator bottom thick first out
Alcohol sends into flash tank after Liquid level adjusting valve decompression, and the solution gas overwhelming majority in crude carbinol is released.
In order to prevent the accumulation of noble gases in synthesis system, continuously a small amount of recyclegas conduct to be discharged from system
Periodic off-gases, by regulating valve（Manually）The periodic off-gases controlling, enter and wash alcohol tower bottom, the water counter current contacting spraying with tower top,
Methanol in gas is dissolved in water, and forms dilute alcohol water and discharges from bottom of towe.From washing alcohol tower top gas out and flash tank out
Solution gas mixing after, a part is sent to reforming unit and makees fuel gas, and remaining enters fuel gas system.The crude carbinol of flash tank and washing
The dilute alcohol Shui Song methanol rectification workshop section that alcohol tower is discharged purifies or enters tank field storage.
Claims (2)
1. a kind of biogas and cog joint produce methanol device it is characterised in that described device includes being provided with biogas import
Trash separator with coke-stove gas import；It is characterized in that described trash separator pass through pipeline successively with gas holder, import separator, gas pressure
Contracting machine, filter, pre- desulfurizer, coal gas just preheater, one-level hydrogenation pre-converter, one-level hydro-conversion device, middle temperature zinc oxide
Desulfurizer, secondary hydrogenation converter, zinc oxide desulfurization groove and gas preheater connect；Described gas preheater and preheating furnace, turn
Change stove, waste heat boiler circulation connects；Described gas preheater pass through coal gas just preheater successively with feedwater preheater, desalination
Water preheater, separator, conversion gas air cooler, gas-liquid separator, normal temp zinc oxide desulfurizer, fresh air filter, synthesis gas
Compressor connects；Described synthesic gas compressor is passed through intersegmental cooler and is connected with gas-liquid separator circulation；Described synthesis gas compression
Machine is connected with heat exchanger and methyl alcohol synthetic reactor successively；Described heat exchanger is connected with methanol separator by air cooler；Described methanol
Separator respectively with flash tank and wash alcohol tower and be connected；Described one-level hydro-conversion device is provided with intensification heating furnace.
2. a kind of biogas and cog joint produce methanol device it is characterised in that described one-level according to claim 1
Ferrum molybdenum or nickel molybdenum catalyst layer is loaded respectively in hydrogenation pre-converter, one-level hydro-conversion device, secondary hydrogenation converter.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610641816.1A CN106397121A (en) | 2016-08-08 | 2016-08-08 | A biogas-coke oven gas combined methanol production device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610641816.1A CN106397121A (en) | 2016-08-08 | 2016-08-08 | A biogas-coke oven gas combined methanol production device |
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| Publication Number | Publication Date |
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| CN106397121A true CN106397121A (en) | 2017-02-15 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610641816.1A Pending CN106397121A (en) | 2016-08-08 | 2016-08-08 | A biogas-coke oven gas combined methanol production device |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107699296A (en) * | 2017-10-25 | 2018-02-16 | 山西潞安煤基精细化学品有限公司 | A kind of one-level hydrogenation pre-converter for setting up heating pipeline |
| CN108530265A (en) * | 2017-03-03 | 2018-09-14 | 陕西黑猫焦化股份有限公司 | Coke-stove gas methanol preparation system and process of preparing |
| CN108531223A (en) * | 2017-03-03 | 2018-09-14 | 陕西黑猫焦化股份有限公司 | Coke oven gas desulfurization hydroconversion process method |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5998489A (en) * | 1997-01-21 | 1999-12-07 | Mitsubishi Heavy Industries, Ltd. | Methanol preparation process |
| CN104945224A (en) * | 2015-05-08 | 2015-09-30 | 徐州伟天化工有限公司 | Methanol production process |
| CN204874343U (en) * | 2015-08-12 | 2015-12-16 | 黄进前 | Marsh gas and coke oven gas joint production methyl alcohol device |
-
2016
- 2016-08-08 CN CN201610641816.1A patent/CN106397121A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5998489A (en) * | 1997-01-21 | 1999-12-07 | Mitsubishi Heavy Industries, Ltd. | Methanol preparation process |
| CN104945224A (en) * | 2015-05-08 | 2015-09-30 | 徐州伟天化工有限公司 | Methanol production process |
| CN204874343U (en) * | 2015-08-12 | 2015-12-16 | 黄进前 | Marsh gas and coke oven gas joint production methyl alcohol device |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108530265A (en) * | 2017-03-03 | 2018-09-14 | 陕西黑猫焦化股份有限公司 | Coke-stove gas methanol preparation system and process of preparing |
| CN108531223A (en) * | 2017-03-03 | 2018-09-14 | 陕西黑猫焦化股份有限公司 | Coke oven gas desulfurization hydroconversion process method |
| CN107699296A (en) * | 2017-10-25 | 2018-02-16 | 山西潞安煤基精细化学品有限公司 | A kind of one-level hydrogenation pre-converter for setting up heating pipeline |
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Application publication date: 20170215 |