CN104193585A - System and process for preparing methyl alcohol through coke-oven gas-assisted coal gasification - Google Patents
System and process for preparing methyl alcohol through coke-oven gas-assisted coal gasification Download PDFInfo
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- CN104193585A CN104193585A CN201410384151.1A CN201410384151A CN104193585A CN 104193585 A CN104193585 A CN 104193585A CN 201410384151 A CN201410384151 A CN 201410384151A CN 104193585 A CN104193585 A CN 104193585A
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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
- C07C29/1518—Multisteps one step being the formation of initial mixture of carbon oxides and hydrogen for synthesis
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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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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
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Abstract
The invention discloses a system and a process for preparing methyl alcohol through coke-oven gas-assisted coal gasification. The system comprises a water-coal-slurry preparation unit, a coal gasification unit, a synthesis gas purification unit, a methyl alcohol synthesis unit, a coke-oven gas purification and separation unit, a triple reforming reaction unit and a gas mixer, wherein the water-coal-slurry preparation unit, the coal gasification unit, the synthesis gas purification unit and the methyl alcohol synthesis unit are sequentially connected with one another. According to the system and the process, effective utilization of coal resources is achieved by complementary utilization of elements of coal and the coke-oven gas and the waste of active elements and energy consumption, caused by a component adjustment operation, can be avoided; and since carbon dioxide and coke-oven gas are used by integration of the triple reforming reaction unit, the operation units are relatively simple, the reaction process is relatively strong in flexibility, and the equipment investment is relatively low.
Description
Technical field
The invention belongs to the energy and chemical technology field, be specifically related to system and the technique of the auxiliary gasification methyl alcohol processed of a kind of coke(oven)gas.
Background technology
Methyl alcohol is important Elementary Chemical Industry product, is the important source material of manufacturing the C1 chemical industry such as the multiple organic productss such as formaldehyde, acetic acid, methyl chloride, methylamine and methyl-sulfate and ethene and propylene.Within 2010, China's methyl alcohol production capacity reaches 3,757 ten thousand tons, and 1,575 ten thousand tons of output have become the large methanol production of the first in the world state.At present, coal mainly be take as raw material production methyl alcohol in China.
There is the high and CO of energy consumption in existing coal methanol process processed
2large two subject matters of quantity discharged.CO
2large and the low major cause of efficiency of quantity discharged is, the hydrogen-carbon ratio of the crude synthesis gas that coal gasification course produces is only 0.7 left and right, and the required hydrogen-carbon ratio of synthesizing methanol is 2.1 left and right, so crude synthesis gas need enter water coal converter unit, and the CO in synthetic gas is converted into H
2and CO
2, so just caused a large amount of CO
2the waste of discharge and carbon, conversion process consumes a large amount of energy simultaneously.
For solving the problems referred to above that exist in coal methanol process processed, the process of a kind of coal and coke(oven)gas alliance methyl alcohol processed (alkene) is suggested (application publication number CN 103694074 A), and this process schema as shown in Figure 1.This coal and coke(oven)gas alliance methanol process processed, it is whole by the methane in coke(oven)gas is done to weight in wet base, to improve the hydrogen-carbon ratio of synthesis gas from coal gasification, the synthetic gas waste of having avoided the water coal converter unit in original methanol process not processed to bring, has improved carbon utilization ratio and has reduced CO
2discharge.But, by the prepared methyl methanol syngas of this technique need by four strands its formed (synthesis gas from coal gasification, dry weight are integrated into gas, weight in wet base is integrated into gas, hydrogen), turndown ratio is little, system flexibility is lower, once raw material forms, change, this technique very likely cannot obtain meeting the synthetic gas of the synthetic required hydrogen-carbon ratio of methyl alcohol; And the introducing of too much operating unit, also make the facility investment of this process significantly increase.
Summary of the invention
For solving the shortcoming and defect part of prior art, primary and foremost purpose of the present invention is to provide the system of the auxiliary gasification methyl alcohol processed of a kind of coke(oven)gas.
Another object of the present invention is to provide a kind of technique that adopts said system to prepare methyl alcohol.
For achieving the above object, the present invention adopts following technical scheme:
The system of the auxiliary gasification methyl alcohol processed of a kind of coke(oven)gas, comprise that coal water slurry prepares unit, coal gasification unit, purified synthesis gas unit, coke(oven)gas purifies and separating unit, gas mixer and methyl alcohol synthesis unit, described coal water slurry is prepared unit and is provided with raw coal entrance, the coal water slurry outlet that coal water slurry is prepared unit is connected with the coal water slurry entrance of coal gasification unit by pipeline, the gasification crude synthesis gas outlet of coal gasification unit is connected with the gasification crude synthesis gas entrance of purified synthesis gas unit by pipeline, gasification crude synthesis gas outlet after the purification of purified synthesis gas unit is connected with gas mixer by pipeline, coke(oven)gas purifies with separating unit and is provided with thick coke(oven)gas entrance, and coke(oven)gas purifies and is connected with gas mixer by pipeline with the hydrogen outlet of separating unit, the methyl alcohol reacting synthesis gas outlet of gas mixer is connected with the methyl methanol syngas entrance of methyl alcohol synthesis unit by pipeline, described system also comprises tri-reforming unit,
The carbonic acid gas outlet of described purified synthesis gas unit is connected with the carbonic acid gas entrance of tri-reforming unit by pipeline;
Described coke(oven)gas purifies with the methane gas outlet of separating unit and is connected with the methane gas entrance of tri-reforming unit by pipeline; The tri-reforming syngas outlet of described tri-reforming unit is connected with gas mixer by pipeline, and described tri-reforming unit is also provided with oxygen intake and steam entry.
Adopt said system to prepare a technique for methyl alcohol, processing step is as follows:
Feed coal is prepared unit in coal water slurry and is made after coal water slurry, enters coal gasification unit and carry out coal gasification reaction together with oxygen, makes gasification crude synthesis gas; Gasification crude synthesis gas enters purified synthesis gas unit and removes sulfide and carbonic acid gas, gasification crude synthesis gas and carbonic acid gas after being purified;
The thick coke(oven)gas of raw material enters coke(oven)gas and purifies and separating unit, through purifying, obtains methane gas, hydrogen and impurity after separated; Carbonic acid gas, oxygen and water vapour that described methane gas, purified synthesis gas unit obtain enter tri-reforming unit jointly, make tri-reforming synthetic gas; Gasification crude synthesis gas after the purification that described tri-reforming synthetic gas, purified synthesis gas unit obtain and coke(oven)gas purify the hydrogen obtaining with separating unit and jointly enter gas mixer, after mixing, obtain methyl alcohol reacting synthesis gas; Described methyl alcohol reacting synthesis gas enters methyl alcohol synthesis unit, through reaction with after purifying, obtains methanol product.
Preferably, the charging mass ratio of the thick coke(oven)gas of described raw material and feed coal is (3～8): 1, and wherein the quality of thick coke(oven)gas is amounted to into the Mass Calculation of standard coal by calorific value.
Preferably, the hydrogen-carbon ratio of described gasification crude synthesis gas is 0.5～1.0.
Preferably, the composition of the thick coke(oven)gas of described raw material comprises that volume fraction is 55～60% H
2with the volume fraction CH that is 20～27%
4, the thick coke(oven)gas of raw material is 5～7 in the hydrogen-carbon ratio through purifying after purifying with separating unit.
Preferably, the service temperature of described tri-reforming unit is 800～900 ℃, and working pressure is 1atm.
Preferably, the sepn process of described thick coke(oven)gas is pressure-swing adsorption process.
Principle of the present invention is: make full use of coke(oven)gas, not only will consider the hydrogen-carbon ratio that it is high, but also will consider to have the CH of high utility value
4, can produce CO and H by reformation
2.Methane reforming have 3 by way of, namely for methane steam reforming, methane carbon dioxide reformation, and methane portion oxidation.Wherein, methane vapor reforming methane reforming with carbon dioxide is all thermo-negative reaction, process energy consumption is high, and methane carbon dioxide reformation is thermopositive reaction, if methane vapor reforming, methane carbon dioxide reformation, methane portion oxidation are coupled (methane tri-reforming), the energy of thermopositive reaction can be supplied with thermo-negative reaction, and realization response is from heat supply.Therefore, the present invention utilizes this tri-reforming coupling coke(oven)gas and gasification gas to carry out methanol production.
Compare with the technology of coke(oven)gas alliance methyl alcohol processed with existing coal, the present invention has the following advantages and beneficial effect:
(1) compare current coal and coke(oven)gas alliance methanol process processed, the present invention is by a methane tri-reforming device be coupled methane dry reforming reaction, methane-steam reforming and partial oxidation reaction of methane, this makes production process pass through a tri-reforming unit, the whole reaction member of original methane dry weight and methane-steam reforming unit have been replaced, the operating unit of having simplified coal and preparing methanol from coke oven gas process, has reduced facility investment.
(2) methyl methanol syngas of current coal and coke(oven)gas alliance methanol process processed, by three bursts of logistics, combined, therefore the turndown ratio of system is lower at present, when raw material composition slightly changes, the synthetic gas that just cannot obtain meeting the synthetic demand of methyl alcohol, system flexibility is low.The new process that the present invention proposes has reduced the constituent fluxion amount of methyl methanol syngas, has improved system flexibility and turndown ratio.Meanwhile, owing to having simplified technique, operational stability is high.
(3) compare current coal and coke(oven)gas alliance methanol process processed, the present invention is owing to having reduced the whole and steam reforming unit of methane dry weight that energy consumption is higher, so the efficiency of process can improve more than 8%, and carbon utilization ratio can improve more than 5%.
Accompanying drawing explanation
Fig. 1 is current coal and coke(oven)gas alliance methanol technics schematic diagram processed.Wherein 101 prepare unit for coal water slurry, and 102 is coal gasification unit, and 103 is purified synthesis gas unit, 104 is methyl alcohol synthesis unit, and 105 for coke(oven)gas purifies and separating unit, and 106 is the dry reformer unit of methane, 107 is methane vapor reforming unit, and 108 is gas mixer; 200～215 is logistics numbering, and wherein 200 is feed coal, and 201 is coal water slurry, 202 is oxygen, and 203 is gasification crude synthesis gas, and 204 is the gasification crude synthesis gas after purifying, 205,215 is carbonic acid gas, 206 is methyl methanol syngas, and 207 is methyl alcohol, and 208 is coke(oven)gas, 209,210,211 is methane, 212 is hydrogen, and 213 for dry weight is integrated into gas, and 214 weight in wet bases are integrated into gas.
Fig. 2 is the auxiliary coal methanol technics schematic diagram processed of coke(oven)gas of the present invention.Wherein 109 is tri-reforming unit; 200～218 is logistics numbering, and wherein 216 is oxygen, and 217 is water vapour, and 218 is tri-reforming synthetic gas, and 219 for the coke(oven)gas such as tar purify the impurity obtaining, operating unit or logistics that all the other numberings are identical with same reference numeral in Fig. 1.
Embodiment
Below in conjunction with embodiment and accompanying drawing, the present invention is described in further detail, but embodiments of the present invention are not limited to this.
The system of the auxiliary gasification methyl alcohol processed of a kind of coke(oven)gas of the present invention, as shown in Figure 2, comprise that coal water slurry prepares unit 101, coal gasification unit 102, purified synthesis gas unit 103, coke(oven)gas purifies and separating unit 105, gas mixer 108 and methyl alcohol synthesis unit 104, described coal water slurry is prepared unit 101 and is provided with raw coal entrance, the coal water slurry outlet that coal water slurry is prepared unit 101 is connected with the coal water slurry entrance of coal gasification unit 102 by pipeline, the gasification crude synthesis gas outlet of coal gasification unit 102 is directly connected with the gasification crude synthesis gas entrance of purified synthesis gas unit 103 by pipeline, gasification crude synthesis gas outlet after the purification of purified synthesis gas unit 103 is connected with gas mixer 108 by pipeline, coke(oven)gas purifies with separating unit 105 and is provided with thick coke(oven)gas entrance, and coke(oven)gas purifies and is connected with gas mixer 108 by pipeline with the hydrogen outlet of separating unit 105, the methyl alcohol reacting synthesis gas outlet of gas mixer 108 is connected with the methyl methanol syngas entrance of methyl alcohol synthesis unit 104 by pipeline, described system also comprises tri-reforming unit 109,
The carbonic acid gas outlet of purified synthesis gas unit 103 is connected with the carbonic acid gas entrance of tri-reforming unit 109 by pipeline;
Coke(oven)gas purifies with the methane gas outlet of separating unit 105 and is connected with the methane gas entrance of tri-reforming unit 109 by pipeline; The tri-reforming syngas outlet of tri-reforming unit 109 is connected with gas mixer 108 by pipeline.
Coal gasification unit 102 is also provided with oxygen intake, and coke(oven)gas purifies with separating unit 105 and is also provided with the outlet of coke(oven)gas purification impurity, and methyl alcohol synthesis unit 104 is also provided with methyl alcohol outlet; Tri-reforming unit 109 is also provided with oxygen intake and steam entry.
From Fig. 2, can see, it is as follows that the present invention adopts said system to prepare the processing step of methyl alcohol:
Feed coal 200 is prepared unit 101 through coal water slurry and is made after coal water slurry 201, enters coal gasification unit 102 and carry out coal gasification reaction together with oxygen 202, makes gasification crude synthesis gas 203; Gasification crude synthesis gas 203 enters purified synthesis gas unit 103 and removes sulfide and carbonic acid gas, the synthesis gas from coal gasification 204 after being purified and carbonic acid gas 205;
The thick coke(oven)gas 208 of raw material enters coke(oven)gas and purifies and separating unit 105, through purifying, obtains methane gas 209, hydrogen 212 and impurity 219 after separated; Described methane gas 209 enters tri-reforming unit 109 jointly with carbonic acid gas 205, oxygen 216 and water vapour 217 that purified synthesis gas unit 103 obtains, makes tri-reforming synthetic gas 218; Synthesis gas from coal gasification 204 after the purification that described tri-reforming synthetic gas 218, purified synthesis gas unit 103 obtain and coke(oven)gas purify the hydrogen 212 obtaining with separating unit 105 and jointly enter gas mixture 108, after mixing, obtain methyl alcohol reacting synthesis gas 206; Described methyl alcohol reacting synthesis gas 206 enters methyl alcohol synthesis unit 104, through reaction with after purifying, obtains methanol product 207.
The difference of the prior art shown in the auxiliary gasification methanol technics processed of coke(oven)gas of the present invention and Fig. 1 is: in (1) system of the present invention, methane by coke(oven)gas resulting separation after purifying, do not need to enter respectively the whole and wet reformer unit of dry weight to produce synthetic gas, but directly enter tri-reforming unit.Tri-reforming can absorb the CO of coal gasification course discharge
2.The hydrogen that coke(oven)gas separation obtains with directly mixes with the synthetic gas after gasification and tri-reforming, to regulate hydrogen-carbon ratio.
(2) in system of the present invention, the synthetic required synthetic gas of methyl alcohol is comprised of synthesis gas from coal gasification, tri-reforming synthetic gas and the hydrogen that obtained by coke(oven)gas separation, and the hydrogen-carbon ratio of this synthetic gas is 2.1～2.15 left and right.Compare coal methanol process processed separately, the synthetic gas that the flow process that the present invention proposes produces regulates hydrogen-carbon ratio without entering water coal converter unit.
Embodiment 1
Specifically being implemented as follows of the auxiliary gasification methyl alcohol system processed of coke(oven)gas of the present embodiment:
The feed coal flow that enters technique of the present invention is 250t/h.Raw coke oven gas flow is 350t/h.The composition of coke(oven)gas is in Table 1.The auxiliary total figure of coal methanol technics flow process processed of coke(oven)gas is referring to Fig. 2:
Feed coal 200 is prepared unit through coal water slurry and is made after coal water slurry 201, enters coal gasification unit 101 and carry out coal gasification reaction together with oxygen 202, makes gasification crude synthesis gas 203; Gasification crude synthesis gas 203 enters purified synthesis gas unit 103 and removes sulfide and carbonic acid gas, the synthesis gas from coal gasification 204 after being purified and carbonic acid gas 205;
The thick coke(oven)gas 208 of raw material enters coke(oven)gas and purifies and separating unit 105, through purifying, obtains methane gas 209, hydrogen 212 and impurity 219 after separated; Described methane gas 209 enters tri-reforming unit 109 jointly with carbonic acid gas 205, oxygen 216 and water vapour 217 that purified synthesis gas unit 103 obtains, makes tri-reforming synthetic gas 218; Synthesis gas from coal gasification 204 after the purification that described tri-reforming synthetic gas 218, purified synthesis gas unit 103 obtain and coke(oven)gas purify the hydrogen 212 obtaining with separating unit 105 and jointly enter gas mixture 108, after mixing, obtain methyl alcohol reacting synthesis gas 206; Described methyl alcohol reacting synthesis gas 206 enters methyl alcohol synthesis unit 104, through reaction with after purifying, obtains methanol product 207.
Wherein, the service temperature of tri-reforming device is 850 ℃, and working pressure is 1atm, and other operating units are with reference to current coal methanol process operating mode processed.
The composition of table 1 coke(oven)gas
| Composition | H 2 | CH 4 | CO | CO 2 | N 2 | O 2 | C mH n |
| Volume fraction % | 59.5 | 24.8 | 6.5 | 5.5 | 3.2 | 0.3 | 0.2 |
By flowsheeting software, Aspen carries out modeling Simulation to the present embodiment meter, and its analog result is in Table 2.
Table 2 analog result
| Logistics numbering | 203 | 211 | 213 | 214 | 209 | 215 | 212 | 217 |
| Molar fraction | ? | ? | ? | ? | ? | ? | ? | ? |
| N 2 | 0.004 | 0.006 | 0.01 | 0 | 0.006 | 0.005 | 0.067 | 0.019 |
| O 2 | trace | 0.002 | 0.95 | 0 | trace | trace | 0.006 | 0.002 |
| Ar | 0.001 | 0 | 0.04 | 0 | 0.001 | trace | 0 | Trace |
| H 2O | 0.224 | trace | 0 | 1.0 | trace | trace | 0 | trace |
| CO | 0.356 | 0.014 | 0 | 0 | 0.558 | 0.330 | 0.086 | 0.319 |
| COS | trace | 0 | 0 | 0 | trace | trace | 0 | trace |
| CO 2 | 0.135 | trace | 0 | 0 | trace | 0.005 | 0 | 0.003 |
| H 2S | 0.003 | trace | 0 | 0 | trace | trace | trace | trace |
| H 2 | 0.277 | 0.002 | 0 | 0 | 0.434 | 0.660 | 0.84 | 0.652 |
| CH 4 | trace | 0.976 | 0 | 0 | trace | trace | 0.001 | 0.005 |
| Molar flow, kmol/hr | 28202 | 7495 | 678 | 4212 | 17993 | 27105 | 19645 | 64743 |
| Mass rate, t/hr | 598.3 | 122 | 21.9 | 75.8 | 301 | 295 | 121.2 | 717.3 |
| Temperature, ℃ | 152 | 65 | 110 | 25 | 240 | 240 | 240 | 240 |
| Pressure, bar | 28 | 23 | 41 | 1.0 | 23 | 82 | 82 | 82 |
The unit consumption of product of technical process and energy expenditure, calculate energy efficiency through signature.From table 2, can see 56% the CO that tri-reforming unit has absorbed that gasification produces
2, and CH
4be converted into together CO and H
2, not only reduced CO
2discharge, and increased the amount of available gas, synthetic more methyl alcohol.Now, CO
2reduce discharging 61.2%, carbon utilization ratio brings up to 84.1%.Raising due to carbon utilization ratio, the former consumption of coal that makes alliance process produce same amount methanol product is only 28% of independent coal methanol process processed, the total energy that has significantly reduced system drops into, therefore this process has higher efficiency, than independent coal methanol process processed, has improved 16.8 percentage points.
By above-mentioned the present embodiment 1 and coal of the prior art and coke(oven)gas alliance methyl alcohol processed (concrete technology as shown in Figure 1) and coal separately methanol technics processed compare, result is as shown in table 3.Compare coal and coke(oven)gas alliance methanol technics processed, efficiency of the present invention has improved 13%, and carbon utilization ratio has improved 6%.Compare coal methanol technics processed separately, efficiency of the present invention has improved 17%, the raising of carbon utilization ratio 28%.
The methyl alcohol leading indicator contrast processed of table 3 the present invention and coal
Above-described embodiment is preferably embodiment of the present invention; but embodiments of the present invention are not restricted to the described embodiments; other any do not deviate from change, the modification done under spirit of the present invention and principle, substitutes, combination, simplify; all should be equivalent substitute mode, within being included in protection scope of the present invention.
Claims (7)
1. the system of the auxiliary gasification methyl alcohol processed of a coke(oven)gas, comprise that coal water slurry prepares unit, coal gasification unit, purified synthesis gas unit, coke(oven)gas purifies and separating unit, gas mixer and methyl alcohol synthesis unit, described coal water slurry is prepared unit and is provided with raw coal entrance, the coal water slurry outlet that coal water slurry is prepared unit is connected with the coal water slurry entrance of coal gasification unit by pipeline, the gasification crude synthesis gas outlet of coal gasification unit is connected with the gasification crude synthesis gas entrance of purified synthesis gas unit by pipeline, gasification crude synthesis gas outlet after the purification of purified synthesis gas unit is connected with gas mixer by pipeline, coke(oven)gas purifies with separating unit and is provided with thick coke(oven)gas entrance, and coke(oven)gas purifies and is connected with gas mixer by pipeline with the hydrogen outlet of separating unit, the methyl alcohol reacting synthesis gas outlet of gas mixer is connected with the methyl methanol syngas entrance of methyl alcohol synthesis unit by pipeline, it is characterized in that, described system also comprises tri-reforming unit,
The carbonic acid gas outlet of described purified synthesis gas unit is connected with the carbonic acid gas entrance of tri-reforming unit by pipeline;
Described coke(oven)gas purifies with the methane gas outlet of separating unit and is connected with the methane gas entrance of tri-reforming unit by pipeline; The tri-reforming syngas outlet of described tri-reforming unit is connected with gas mixer by pipeline, and described tri-reforming unit is also provided with oxygen intake and steam entry.
2. utilize system described in claim 1 to prepare a technique for methyl alcohol, it is characterized in that, described processing step is as follows:
Feed coal is made and is entered coal gasification unit after coal water slurry together with oxygen and carry out coal gasification reaction, makes gasification crude synthesis gas; Gasification crude synthesis gas enters purified synthesis gas unit and removes sulfide and carbonic acid gas, gasification crude synthesis gas, carbonic acid gas and sulfide after being purified;
The thick coke(oven)gas of raw material enters coke(oven)gas and purifies and separating unit, through purifying, obtains methane gas, hydrogen and impurity after separated; Carbonic acid gas, oxygen and water vapour that described methane gas and purified synthesis gas unit obtain enter tri-reforming unit jointly, make tri-reforming synthetic gas; Gasification crude synthesis gas after the purification that described tri-reforming synthetic gas, purified synthesis gas unit obtain and coke(oven)gas purify the hydrogen obtaining with separating unit and jointly enter gas mixture, after mixing, obtain methyl alcohol reacting synthesis gas; Described methyl alcohol reacting synthesis gas enters methyl alcohol synthesis unit, through reaction with after purifying, obtains methanol product.
3. technique according to claim 2, is characterized in that, the charging mass ratio of the thick coke(oven)gas of described raw material and feed coal is (3～8): 1, and wherein the quality of thick coke(oven)gas is amounted to into the Mass Calculation of standard coal by calorific value.
4. technique according to claim 2, is characterized in that, the hydrogen-carbon ratio of described gasification crude synthesis gas is 0.5～1.0.
5. technique according to claim 2, is characterized in that, the thick coke(oven)gas of described raw material comprises that volume fraction is 55～60% H
2with the volume fraction CH that is 20～27%
4, the thick coke(oven)gas of raw material is 5～7 in the hydrogen-carbon ratio through purifying after purifying with separating unit.
6. technique according to claim 2, is characterized in that, the service temperature of described tri-reforming unit is 800～900 ℃, and working pressure is 1atm.
7. technique according to claim 2, is characterized in that, the sepn process of the thick coke(oven)gas of described raw material is pressure-swing adsorption process.
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| CN108299158A (en) * | 2018-03-19 | 2018-07-20 | 合肥工业大学 | A kind of integrated chemical chain and carbon dioxide utilize the ammonia from coal system and method for technology |
| CN109020780A (en) * | 2018-08-03 | 2018-12-18 | 华南理工大学 | A kind of coal gasification coupling coking of coal methanol system and method |
| CN110002954A (en) * | 2019-04-30 | 2019-07-12 | 华南理工大学 | A kind of coal gasification couples the process and device of coking of coal methanol with joint production acid or ester |
| CN110002955A (en) * | 2019-04-30 | 2019-07-12 | 华南理工大学 | A kind of process and device of coal gasification coupling coking of coal methanol with joint production ethylene glycol and LNG |
| CN110002933A (en) * | 2019-04-03 | 2019-07-12 | 浙江天禄环境科技有限公司 | A kind of method that low-order coal sub-prime prepares methanol and low-carbon alkene using Poly-generation |
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