CN105542832B - A kind of method of coke lighter hydrocarbons - Google Patents
A kind of method of coke lighter hydrocarbons Download PDFInfo
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- CN105542832B CN105542832B CN201510954546.5A CN201510954546A CN105542832B CN 105542832 B CN105542832 B CN 105542832B CN 201510954546 A CN201510954546 A CN 201510954546A CN 105542832 B CN105542832 B CN 105542832B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
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Abstract
A kind of method of coke lighter hydrocarbons, it is related to a kind of method of coke lighter hydrocarbons.The problem of there is high investment, low yield the present invention is to solve the existing method for preparing lighter hydrocarbons.Method：Gas making, electric precipitation, gas holder, pressurization, absorption, compression, conversion cooling, low-temp methanol is washed, synthesis gas compress, methanol-fueled CLC, methanol rectification, synthesis stable light hydrocarbon, lighter hydrocarbons separate.The present invention is used for coke lighter hydrocarbons.
Description
Technical field
The present invention relates to a kind of method of coke lighter hydrocarbons.
Background technology
Stable light hydrocarbon may generally serve as producing the raw material of solvent naphtha, and it, which is originated, two classes, and a class is that crude oil passes through flash distillation, from
Settled down in flashed vapour, component is heavier, color is generally transparent faint yellow or yellowish-brown；Another kind of is associated gas
Or the pentane above component that contains in other natural gases, separated by the process such as freezing and compressing, general isopentane content compared with
Height, pentane above component is less, and color is generally transparent colourless.The Downstream Market of stable light hydrocarbon, being divided by function to be divided into
Organic Chemicals and fuel oil additive two parts.When stable light hydrocarbon is used as high cleaning fuel oil additive, mediation upgrading common 93
Number quality of gasoline, while PM2.5 discharge capacity can be greatly lowered.Use the vapour produced using coal base by the stable light hydrocarbon of raw material
Oil is compared with conventional gasoline product, and PM2.5 discharge capacity will reduce nearly 80% after engine combustion.Also can directly it make as alternative fuel
With, its composition only has 27 kinds, is reduced a lot than existing 128 kinds of compositions of No. 93 gasoline, no sulphur, without fixed body impurity, high stability,
With good additional issue and corrosion resistance, the requirement of the gasoline standard of state four is significantly better than.With high-performance, few spy is polluted
Point, is preferable clean energy resource, reduces carbon emission and environmental pollution.But there is investment height, yield in the existing method for preparing lighter hydrocarbons
Low the problem of.
The content of the invention
The problem of there is high investment, low yield the present invention is to solve the existing method for preparing lighter hydrocarbons, and provide a kind of burnt
The method of charcoal lighter hydrocarbons.
A kind of method of coke lighter hydrocarbons of the present invention is specifically carried out according to the following steps：
First, coke, steam and oxygen are gasified using gas maker, the water-gas after being gasified；The oxygen
It is the 4000mmH from air separation unit2O post oxygen；The temperature of water-gas after the gasification is -40 DEG C, and gauge pressure is
0.006MPa；
2nd, the water-gas after the gasification for obtaining step one carries out dust removal process using electric dust collector, obtains electric precipitation
Water-gas；The temperature of the water-gas of the electric precipitation is 40 DEG C, and absolute pressure is 0.103MPa；
3rd, the water-gas for the electric precipitation for obtaining step 2 delivers to gas cabinet assembly, subsequently into gas pressing device, obtains
Water-gas after pressurization；The temperature of water-gas after the pressurization is 40 DEG C, and absolute pressure is 0.4MPa；
4th, the water-gas after the pressurization for obtaining step 3 is purified and regenerated by TSA adsorbent equipment, obtains alternating temperature
The water-gas of absorption；The temperature of the water-gas of the temp.-changing adsorption is 40 DEG C, and absolute pressure is 0.4MPa；
5th, the water-gas for the temp.-changing adsorption for obtaining step 4 is boosted by gas compression device, is obtained after compression
Water-gas；The temperature of water-gas after the compression is 90 DEG C, and absolute pressure is 4.0MPa, and dry CO percentage composition is
45.81%；
6th, the water-gas after the compression for obtaining step 5 enters line translation, pre- recuperation of heat and cold by converting cooling device
But, conversion gas is obtained；The temperature of the conversion gas is 40 DEG C, and gauge pressure is 3.7MPa；
7th, the conversion gas that step 6 is obtained is delivered into low temperature washing device for methanol to be washed, obtains sulfur-containing tail gas, CO2Put
Air and purified gas；The sulfur-containing tail gas is vented after reclaiming methanol through tail gas recovery tower washing；The CO2Drop a hint and directly put
It is empty；The temperature of the purified gas is 25 DEG C, and gauge pressure is 3.5MPa；The cold of the low temperature washing device for methanol is carried by refrigerating plant
For；
8th, the purified gas obtained step 7 and the hydrogen-rich mixing from hydrogen recovery unit, obtain gaseous mixture, then will be mixed
Close gas and be passed through synthesis gas compression set by two sections of compressions, two sections of compressed gas are obtained, then in the compression of synthesis gas compression set
In machine cylinder by two sections of compressed gas and after the mixing compression of the circulating air from methanol synthesizer, synthesis gas is obtained；The mixing
The temperature of gas is 40 DEG C, and absolute pressure is 3.3MPa；The temperature of two sections of compressed gas is 40 DEG C, and absolute pressure is 8.17MPa；
The temperature of the circulating air from methanol synthesizer 11 is 40 DEG C, and absolute pressure is 8.17MPa；The temperature of the synthesis gas
For 73 DEG C, absolute pressure is 8.94MPa；
9th, the synthesis gas for obtaining step 8 is preheating to 235 DEG C through heat exchanger, and feeding methanol synthesizer carries out separation conjunction
Into obtaining gas and crude carbinol；The gas is circulating air and periodic off-gases, and circulating air sends into synthesis gas compression set and step 8
In the mixing of two sections of compressed gas, periodic off-gases feeding hydrogen recovery unit, the temperature of the crude carbinol is 40 DEG C, and gauge pressure is 0.5MPa；
Tenth, into methanol rectifying system after the crude carbinol obtained step 9 and the dilute alcohol water mixing from hydrogen recovery unit
Rectifying is carried out, refined methanol is obtained；Methanol content in the refined methanol is 98%；
11, the refined methanol feeding tank field storage obtained step 10, it is then from tank field that refined methanol feeding synthesis is stable
Lighter hydrocarbons facilities are synthesized, and obtain mixed light-hydrocarbon, and mixed light-hydrocarbon is sent into lighter hydrocarbons separators carries out rectifying separation, obtain LPG,
Light stable light hydrocarbon and heavy lighter hydrocarbons, that is, complete coke lighter hydrocarbons.
The beneficial effects of the invention are as follows：
The present invention, for raw material, synthetic raw gas, rough coal is produced using pure oxygen-steam normal pressure continuous gasification technology with chemical industry Jiao
After the processing such as gas removing dust, washing, cooling and electric precipitation, repressurization to gauge pressure is 4.0MPa, into after conversion regulation hydrogen-carbon ratio,
Low-temp methanol is delivered to carry out sour gas removing to meet requirement of the methanol-fueled CLC to synthesis gas, then it is stable by Material synthesis of methanol
Lighter hydrocarbons, while by-product heavy lighter hydrocarbons and LPG.
Brief description of the drawings
Fig. 1 is a kind of schematic flow sheet of the method for coke lighter hydrocarbons of the invention.
Embodiment
Embodiment one：Illustrate present embodiment, a kind of method tool of coke lighter hydrocarbons of present embodiment with reference to Fig. 1
Body is to carry out according to the following steps：
First, coke 18, steam 19 and oxygen are gasified using gas maker 1, the water-gas after being gasified；It is described
Oxygen is the 4000mmH from air separation unit 172O post oxygen；The temperature of water-gas after the gasification is -40 DEG C, and gauge pressure is
0.006MPa；
2nd, the water-gas after the gasification for obtaining step one carries out dust removal process using electric dust collector 2, obtains electric precipitation
Water-gas；The temperature of the water-gas of the electric precipitation is 40 DEG C, and absolute pressure is 0.103MPa；
3rd, the water-gas for the electric precipitation for obtaining step 2 delivers to gas cabinet assembly 3, subsequently into gas pressing device 4, obtains
Water-gas after to pressurization；The temperature of water-gas after the pressurization is 40 DEG C, and absolute pressure is 0.4MPa；
4th, the water-gas after the pressurization for obtaining step 3 is purified and regenerated by TSA adsorbent equipment 5, is become
The water-gas of temperature absorption；The temperature of the water-gas of the temp.-changing adsorption is 40 DEG C, and absolute pressure is 0.4MPa；
5th, the water-gas for the temp.-changing adsorption for obtaining step 4 is boosted by gas compression device 6, is obtained after compression
Water-gas；The temperature of water-gas after the compression is 90 DEG C, and absolute pressure is 4.0MPa, and dry CO percentage composition is
45.81%；
6th, the water-gas after the compression for obtaining step 5 enters line translation, pre- recuperation of heat and cold by converting cooling device 7
But, conversion gas is obtained；The temperature of the conversion gas is 40 DEG C, and gauge pressure is 3.7MPa；
7th, the conversion gas that step 6 is obtained is delivered into low temperature washing device for methanol 8 to be washed, obtains sulfur-containing tail gas 20, CO2
Drop a hint 21 and purified gas；The sulfur-containing tail gas 20 is vented after reclaiming methanol through tail gas recovery tower washing；The CO2Drop a hint 21
Directly it is vented；The temperature of the purified gas is 25 DEG C, and gauge pressure is 3.5MPa；The cold of the low temperature washing device for methanol 8 is by freezing
Device 9 is provided；
8th, the purified gas obtained step 7 and the hydrogen-rich mixing from hydrogen recovery unit 10, obtain gaseous mixture, then will
Gaseous mixture is passed through synthesis gas compression set 12 by two sections of compressions, two sections of compressed gas is obtained, then in synthesis gas compression set 12
Compresser cylinder in by two sections of compressed gas with the circulating air from methanol synthesizer 11 mixing compression after, obtain synthesis gas；
The temperature of the gaseous mixture is 40 DEG C, and absolute pressure is 3.3MPa；The temperature of two sections of compressed gas is 40 DEG C, and absolute pressure is
8.17MPa；The temperature of the circulating air from methanol synthesizer 11 is 40 DEG C, and absolute pressure is 8.17MPa；The synthesis
The temperature of gas is 73 DEG C, and absolute pressure is 8.94MPa；
9th, the synthesis gas for obtaining step 8 is preheating to 235 DEG C through heat exchanger, and feeding methanol synthesizer 11 is separated
Synthesis, obtains gas and crude carbinol；The gas is circulating air and periodic off-gases, and circulating air feeding synthesis gas compression set 12 is with walking
Two sections of compressed gas mixing in rapid eight, periodic off-gases feeding hydrogen recovery unit 10, the temperature of the crude carbinol is 40 DEG C, and gauge pressure is
0.5MPa；
Tenth, into methanol rectification dress after the crude carbinol obtained step 9 and the dilute alcohol water mixing from hydrogen recovery unit 10
13 carry out rectifying are put, refined methanol is obtained；Methanol content in the refined methanol is 98%；
11, the refined methanol feeding tank field 14 obtained step 10 is stored, and is then sent into refined methanol from tank field 14 and is synthesized
Stable light hydrocarbon device 15 is synthesized, and obtains mixed light-hydrocarbon, and mixed light-hydrocarbon is sent into lighter hydrocarbons separator 16 carries out rectifying separation,
LPG22, light stable light hydrocarbon 23 and heavy lighter hydrocarbons 24 are obtained, that is, complete coke lighter hydrocarbons.
Gas maker described in present embodiment step one use pure oxygen-steam normal pressure continuous gasification process, preparation it is thick
Active constituent content height (CO+H in coal gas2For 80%), and without blowing-out gas discharge.
Cooling device is converted described in present embodiment step 6 using heat exchange type pressurization sulphur-resistant conversion, the purpose is to thick
Coal gas is purified, and removes the impurity such as oil therein, dirt, and raw gas temperature is reached the light-off temperature of catalyst.
Low temperature washing device for methanol operating pressure described in present embodiment step 7 is high, CO2Partial pressure is higher, and total sulfur is removed to
Below 0.1ppm, can be simultaneously selectively by sulfide in gas, CO2, HCN, the impurity removal such as oils it is clean, and solution
Absorbability is big, internal circulating load is small, power consumption and regeneration energy consumption are low, solvent is cheap, operating cost is low.
Synthesis gas compression set described in present embodiment step 8 is divided using purified gas and circulating air joint compressor set
Two sections of compressions, are mixed, final compressor outlet pressure 8.94MPa (A), centrifugal, steam with purified gas and circulating air in cylinder
Turbine drives, and unit cycle of oparation is long, it is not necessary to standby host, and flow is simple, and efficiency high, energy-saving effect is notable.
Methanol synthesizer described in present embodiment step 9 uses the isothermal methanol synthesis reactors of I.M.C.
Methanol rectifying system uses three-column process flow described in present embodiment step 10.
Hydrogen recovery unit described in present embodiment step 8 uses pressure-variable adsorption or UF membrane.
Stable light hydrocarbon device is synthesized described in present embodiment step 11 and uses one-step method, methanol conversion system two is eliminated
The step of methyl ether, methanol step in the presence of ZSM-5 molecular sieve catalyst is converted into lighter hydrocarbons and LPG, and its technological process is short, production
Product selectivity is high, and catalyst stability and single pass life are high.
Present embodiment, for raw material, synthetic raw gas is produced using pure oxygen-steam normal pressure continuous gasification technology with chemical industry Jiao,
After the processing such as raw gas removing dust, washing, cooling and electric precipitation, repressurization to gauge pressure is 4.0MPa, and hydrogen carbon is adjusted into conversion
Than after, deliver to low-temp methanol and carry out sour gas removing to meet requirement of the methanol-fueled CLC to synthesis gas, then the conjunction by raw material of methanol
Into stable light hydrocarbon, while by-product heavy lighter hydrocarbons and LPG.
Embodiment two：Present embodiment from unlike embodiment one：Coke described in step one
18 particle diameter is 10mm~50mm, adds speed for 102916kg/h.Other are identical with embodiment one.
Embodiment three：Present embodiment from unlike embodiment one or two：Described in step one
The speed that is passed through of steam 19 is 37500kg/h.Other are identical with embodiment one or two.
Embodiment four：Unlike one of present embodiment and embodiment one to three：Institute in step one
The speed that is passed through for the oxygen stated is 50000Nm3/h.Other are identical with one of embodiment one to three.
Embodiment five：Unlike one of present embodiment and embodiment one to four：Institute in step 7
The refrigerating plant 9 stated compresses refrigeration using ammonia.Other are identical with one of embodiment one to four.
Embodiment six：Unlike one of present embodiment and embodiment one to five：Institute in step 7
That states conversion gas is passed through speed for 263922.7Nm3/h.Other are identical with one of embodiment one to five.
Embodiment seven：Unlike one of present embodiment and embodiment one to six：Institute in step 9
The periodic off-gases and the mass ratio of circulating air stated are 1:(15~20).Other are identical with one of embodiment one to six.
Embodiment eight：Unlike one of present embodiment and embodiment one to seven：In step 11
The speed of the refined methanol feeding synthesis stable light hydrocarbon device 15 is 75.1t/h.Other are one of with embodiment one to seven
It is identical.
Beneficial effects of the present invention are verified by following examples：
A kind of method of coke lighter hydrocarbons is specifically carried out according to the following steps：
First, coke 18, steam 19 and oxygen are gasified using gas maker 1, the water-gas after being gasified；It is described
Oxygen is the 4000mmH from air separation unit 172O post oxygen；The temperature of water-gas after the gasification is -40 DEG C, and gauge pressure is
0.006MPa；
2nd, the water-gas after the gasification for obtaining step one carries out dust removal process using electric dust collector 2, obtains electric precipitation
Water-gas；The temperature of the water-gas of the electric precipitation is 40 DEG C, and absolute pressure is 0.103MPa；
3rd, the water-gas for the electric precipitation for obtaining step 2 delivers to gas cabinet assembly 3, subsequently into gas pressing device 4, obtains
Water-gas after to pressurization；The temperature of water-gas after the pressurization is 40 DEG C, and absolute pressure is 0.4MPa；
4th, the water-gas after the pressurization for obtaining step 3 is purified and regenerated by TSA adsorbent equipment 5, is become
The water-gas of temperature absorption；The temperature of the water-gas of the temp.-changing adsorption is 40 DEG C, and absolute pressure is 0.4MPa；
5th, the water-gas for the temp.-changing adsorption for obtaining step 4 is boosted by gas compression device 6, is obtained after compression
Water-gas；The temperature of water-gas after the compression is 90 DEG C, and absolute pressure is 4.0MPa, and dry CO percentage composition is
45.81%；
6th, the water-gas after the compression for obtaining step 5 enters line translation, pre- recuperation of heat and cold by converting cooling device 7
But, conversion gas is obtained；The temperature of the conversion gas is 40 DEG C, and gauge pressure is 3.7MPa；
7th, the conversion gas that step 6 is obtained is delivered into low temperature washing device for methanol 8 to be washed, obtains sulfur-containing tail gas 20, CO2
Drop a hint 21 and purified gas；The sulfur-containing tail gas is vented after reclaiming methanol through tail gas recovery tower washing；The CO2Drop a hint directly
Emptying；The temperature of the purified gas is 25 DEG C, and gauge pressure is 3.5MPa；The cold of the low temperature washing device for methanol 8 is by refrigerating plant 9
There is provided；
8th, the purified gas obtained step 7 and the hydrogen-rich mixing from hydrogen recovery unit 10, obtain gaseous mixture, then will
Gaseous mixture is passed through synthesis gas compression set 12 by two sections of compressions, two sections of compressed gas is obtained, then in synthesis gas compression set 12
Compresser cylinder in by two sections of compressed gas with the circulating air from methanol synthesizer 11 mixing compression after, obtain synthesis gas；
The temperature of the gaseous mixture is 40 DEG C, and absolute pressure is 3.3MPa；The temperature of two sections of compressed gas is 40 DEG C, and absolute pressure is
8.17MPa；The temperature of the circulating air from methanol synthesizer 11 is 40 DEG C, and absolute pressure is 8.17MPa；The synthesis
The temperature of gas is 73 DEG C, and absolute pressure is 8.94MPa；
9th, the synthesis gas for obtaining step 8 is preheating to 235 DEG C through heat exchanger, and feeding methanol synthesizer 11 is separated
Synthesis, obtains gas and crude carbinol；The gas is circulating air and periodic off-gases, and circulating air feeding synthesis gas compression set 12 is with walking
Two sections of compressed gas mixing in rapid eight, periodic off-gases feeding hydrogen recovery unit 10, the temperature of the crude carbinol is 40 DEG C, and gauge pressure is
0.5MPa；
Tenth, into methanol rectification dress after the crude carbinol obtained step 9 and the dilute alcohol water mixing from hydrogen recovery unit 10
13 carry out rectifying are put, refined methanol is obtained；Methanol content in the refined methanol is 98%；
11, the refined methanol feeding tank field 14 obtained step 10 is stored, and is then sent into refined methanol from tank field 14 and is synthesized
Stable light hydrocarbon device 15 is synthesized, and obtains mixed light-hydrocarbon, and mixed light-hydrocarbon is sent into lighter hydrocarbons separator 16 carries out rectifying separation,
LPG22, light stable light hydrocarbon 23 and heavy lighter hydrocarbons 24 are obtained, that is, complete coke lighter hydrocarbons.
Gas maker described in the present embodiment step one uses pure oxygen-steam normal pressure continuous gasification process, the rough coal of preparation
Active constituent content height (CO+H in gas2For 80%), and without blowing-out gas discharge.
Cooling device is converted described in the present embodiment step 6 using heat exchange type pressurization sulphur-resistant conversion, the purpose is to rough coal
Gas is purified, and removes the impurity such as oil therein, dirt, and raw gas temperature is reached the light-off temperature of catalyst.
Low temperature washing device for methanol operating pressure described in the present embodiment step 7 is high, CO2Partial pressure is higher, and total sulfur is removed to
Below 0.1ppm, can be simultaneously selectively by sulfide in gas, CO2, HCN, the impurity removal such as oils it is clean, and solution
Absorbability is big, internal circulating load is small, power consumption and regeneration energy consumption are low, solvent is cheap, operating cost is low.
Synthesis gas compression set described in the present embodiment step 8 is divided to two using purified gas and circulating air joint compressor set
Section compression, is mixed, final compressor outlet pressure 8.94MPa (A), centrifugal, steam is saturating with purified gas and circulating air in cylinder
Flat driving, unit cycle of oparation is long, it is not necessary to which standby host, flow is simple, and efficiency high, energy-saving effect is notable.
Methanol synthesizer described in the present embodiment step 9 uses the isothermal methanol synthesis reactors of I.M.C.
Methanol rectifying system uses three-column process flow described in the present embodiment step 10.
Hydrogen recovery unit described in the present embodiment step 8 uses pressure-variable adsorption or UF membrane.
Stable light hydrocarbon device is synthesized described in the present embodiment step 11 and uses one-step method, methanol is eliminated and converts diformazan processed
The step of ether, methanol step in the presence of ZSM-5 molecular sieve catalyst is converted into lighter hydrocarbons and LPG, and its technological process is short, product
Selectivity is high, and catalyst stability and single pass life are high.
The present embodiment, for raw material, produces synthetic raw gas, slightly with chemical industry Jiao using pure oxygen-steam normal pressure continuous gasification technology
After the processing such as coal gas removing dust, washing, cooling and electric precipitation, repressurization to gauge pressure is 4.0MPa, and hydrogen-carbon ratio is adjusted into conversion
Afterwards, low-temp methanol is delivered to carry out sour gas removing to meet requirement of the methanol-fueled CLC to synthesis gas, then using methanol as Material synthesis
Stable light hydrocarbon, while by-product heavy lighter hydrocarbons and LPG.
Claims (8)
1. a kind of method of coke lighter hydrocarbons, it is characterised in that the method for coke lighter hydrocarbons is specifically carried out according to the following steps：
First, coke (18), steam (19) and oxygen are gasified using gas maker (1), the water-gas after being gasified；Institute
It is the 4000mmH from air separation unit (17) to state oxygen2O post oxygen；The temperature of water-gas after the gasification is -40 DEG C, table
Press as 0.006MPa；
2nd, the water-gas after the gasification for obtaining step one carries out dust removal process using electric dust collector (2), obtains electric precipitation
Water-gas；The temperature of the water-gas of the electric precipitation is 40 DEG C, and absolute pressure is 0.103MPa；
3rd, the water-gas for the electric precipitation for obtaining step 2 delivers to gas cabinet assembly (3), subsequently into gas pressing device (4), obtains
Water-gas after to pressurization；The temperature of water-gas after the pressurization is 40 DEG C, and absolute pressure is 0.4MPa；
4th, the water-gas after the pressurization for obtaining step 3 is purified and regenerated by TSA adsorbent equipment (5), obtains alternating temperature
The water-gas of absorption；The temperature of the water-gas of the temp.-changing adsorption is 40 DEG C, and absolute pressure is 0.4MPa；
5th, the water-gas for the temp.-changing adsorption for obtaining step 4 is boosted by gas compression device (6), after being compressed
Water-gas；The temperature of water-gas after the compression is 90 DEG C, and absolute pressure is 4.0MPa, and dry CO percentage composition is
45.81%；
6th, the water-gas after the compression for obtaining step 5 enters line translation, pre- recuperation of heat and cold by converting cooling device (7)
But, conversion gas is obtained；The temperature of the conversion gas is 40 DEG C, and gauge pressure is 3.7MPa；
7th, the conversion gas that step 6 is obtained is delivered into low temperature washing device for methanol (8) to be washed, obtains sulfur-containing tail gas (20), CO2
Drop a hint (21) and purified gas；The sulfur-containing tail gas is vented after reclaiming methanol through tail gas recovery tower washing；The CO2Drop a hint straight
Connect emptying；The temperature of the purified gas is 25 DEG C, and gauge pressure is 3.5MPa；The cold of the low temperature washing device for methanol (8) is by freezing
Device (9) is provided；
8th, the purified gas obtained step 7 and the hydrogen-rich mixing from hydrogen recovery unit (10), obtain gaseous mixture, then will be mixed
Close gas and be passed through synthesis gas compression set (12) by two sections of compressions, two sections of compressed gas are obtained, then in synthesis gas compression set
(12) in compresser cylinder by two sections of compressed gas and after the mixing compression of the circulating air from methanol synthesizer (11), closed
Into gas；The temperature of the gaseous mixture is 40 DEG C, and absolute pressure is 3.3MPa；The temperature of two sections of compressed gas is 40 DEG C, definitely
Pressure is 8.17MPa；The temperature of the circulating air from methanol synthesizer (11) is 40 DEG C, and absolute pressure is 8.17MPa；
The temperature of the synthesis gas is 73 DEG C, and absolute pressure is 8.94MPa；
9th, the synthesis gas for obtaining step 8 is preheating to 235 DEG C through heat exchanger, and feeding methanol synthesizer (11) carries out separation conjunction
Into obtaining gas and crude carbinol；The gas is circulating air and periodic off-gases, and circulating air feeding synthesis gas compression set (12) is with walking
Two sections of compressed gas mixing in rapid eight, periodic off-gases feeding hydrogen recovery unit (10), the temperature of the crude carbinol is 40 DEG C, and gauge pressure is
0.5MPa；
Tenth, into methanol rectifying system after the crude carbinol obtained step 9 and the dilute alcohol water mixing from hydrogen recovery unit (10)
(13) rectifying is carried out, refined methanol is obtained；Methanol content in the refined methanol is 98%；
11, refined methanol feeding tank field (14) storage obtained step 10, then refined methanol is sent into synthesize from tank field (14)
Stable light hydrocarbon device (15) is synthesized, and obtains mixed light-hydrocarbon, and mixed light-hydrocarbon is sent into lighter hydrocarbons separator (16) carries out rectifying
Separation, obtains LPG (22), light stable light hydrocarbon (23) and heavy lighter hydrocarbons (24), that is, completes coke lighter hydrocarbons.
2. a kind of method of coke lighter hydrocarbons according to claim 1, it is characterised in that the coke described in step one
(18) particle diameter is 10mm~50mm, adds speed for 102916kg/h.
3. a kind of method of coke lighter hydrocarbons according to claim 1, it is characterised in that the steam described in step one
(19) the speed that is passed through is 37500kg/h.
4. a kind of method of coke lighter hydrocarbons according to claim 1, it is characterised in that oxygen described in step one
Speed is passed through for 50000Nm3/h。
5. a kind of method of coke lighter hydrocarbons according to claim 1, it is characterised in that the freezing dress described in step 7
Put (9) and refrigeration is compressed using ammonia.
6. a kind of method of coke lighter hydrocarbons according to claim 1, it is characterised in that conversion gas described in step 7
Speed is passed through for 263922.7Nm3/h。
7. a kind of method of coke lighter hydrocarbons according to claim 1, it is characterised in that the periodic off-gases described in step 9
Mass ratio with circulating air is 1:(15~20).
8. a kind of method of coke lighter hydrocarbons according to claim 1, it is characterised in that refined methanol described in step 11
The speed of feeding synthesis stable light hydrocarbon device (15) is 75.1t/h.
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| WO2012118511A1 (en) * | 2011-03-03 | 2012-09-07 | Sri International | Gasification of a carbonaceous material |
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2015
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1304913A (en) * | 2000-07-17 | 2001-07-25 | 中国科学院山西煤炭化学研究所 | Process for synthesizing hydrocarbon from syntehtic gas |
| WO2012118511A1 (en) * | 2011-03-03 | 2012-09-07 | Sri International | Gasification of a carbonaceous material |
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