CN105542832A - Method for making light hydrocarbons from coke - Google Patents
Method for making light hydrocarbons from coke Download PDFInfo
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- CN105542832A CN105542832A CN201510954546.5A CN201510954546A CN105542832A CN 105542832 A CN105542832 A CN 105542832A CN 201510954546 A CN201510954546 A CN 201510954546A CN 105542832 A CN105542832 A CN 105542832A
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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
The present invention relates to a method for making light hydrocarbons from coke, and aims to solve the problems high investment and low yield of methods for making the light hydrocarbons in the prior art. The method is as follows: gas making, electric precipitation, gas tank, pressurizing, adsorption, compression, transformation cooling, low temperature methanol wash, synthesis gas compression, methanol synthesis, methanol distillation, synthesis of stable light hydrocarbons, and light hydrocarbon separation. The method is used to make the light hydrocarbons from the coke.
Description
Technical field
The present invention relates to a kind of method of coke lighter hydrocarbons.
Background technology
Stable light hydrocarbon generally can be used as produces the raw material of solvent oil, and there are two classes in its source, a class be crude oil through flash distillation, settle down from flashed vapour, component is heavier, and color is generally transparent faint yellow or yellowish brown; Another kind of is the above component of pentane contained in associated gas or other Sweet natural gases, and by freeze and the process such as compression separates, general isopentane content is higher, and the above component of pentane is less, and color is generally clear, colorless.The Downstream Market of stable light hydrocarbon, divides by function and can be divided into Organic Chemicals and fuel oil additive two portions.When stable light hydrocarbon is used as abrasive fuel oil additive, common No. 93 quality of gasolines of mediation upgrading, significantly can reduce the quantity discharged of PM2.5 simultaneously.Using with coal-based is the gasoline comparatively conventional gasoline product that the stable light hydrocarbon of raw material produces, and after engine combustion, the quantity discharged of PM2.5 will reduce nearly 80%.Also can be used as alternative fuel directly to use, its composition only has 27 kinds, reduces a lot, without sulphur, without fixed body impurity, high stability, have good additional issue and erosion resistance, be greatly better than the requirement of state four gasoline standard than existing No. 93 gasoline 128 kinds of compositions.Having high-performance, pollute few feature, is desirable clean energy, reduces carbon emission and environmental pollution.But there is the problem that investment is high, productive rate is low in the existing method preparing lighter hydrocarbons.
Summary of the invention
The present invention will solve the existing method preparing lighter hydrocarbons to there is the problem that investment is high, productive rate is low, and provides a kind of method of coke lighter hydrocarbons.
The method of a kind of coke lighter hydrocarbons of the present invention is specifically carried out according to the following steps:
One, adopt gas maker to gasify coke, steam and oxygen, obtain the water-gas after gasifying; Described oxygen is the 4000mmH from air separation facility
2o post oxygen; The temperature of the water-gas after described gasification is-40 DEG C, and gauge pressure is 0.006MPa;
Two, the water-gas after gasification step one obtained adopts electric dust collector to carry out dust removal process, obtains the water-gas of electric precipitation; The temperature of the water-gas of described electric precipitation is 40 DEG C, and absolute pressure is 0.103MPa;
The water-gas of the electric precipitation three, step 2 obtained delivers to gas cabinet assembly, then enters gas pressing device, obtains the water-gas after pressurizeing; The temperature of the water-gas after described pressurization is 40 DEG C, and absolute pressure is 0.4MPa;
Four, the water-gas after pressurization step 3 obtained is undertaken purifying and regenerating by TSA adsorption unit, obtains the water-gas of Temp .-changing adsorption; The temperature of the water-gas of described Temp .-changing adsorption is 40 DEG C, and absolute pressure is 0.4MPa;
The water-gas of the Temp .-changing adsorption five, step 4 obtained is boosted by gas compression device, obtains the water-gas after compressing; The temperature of the water-gas after described compression is 90 DEG C, and absolute pressure is 4.0MPa, and the percentage composition of dry CO is 45.81%;
Six, the water-gas after compression step 5 obtained is undertaken converting by conversion refrigerating unit, pre-recovery of heat and cooling, obtains conversion gas; The temperature of described conversion gas is 40 DEG C, and gauge pressure is 3.7MPa;
Seven, the conversion gas that step 6 obtains is delivered to low temperature washing device for methanol to wash, obtain sulfur-containing tail gas, CO
2drop a hint and purified gas; The emptying after tail gas recovery tower washing and recycling methyl alcohol of described sulfur-containing tail gas; Described CO
2to drop a hint direct emptying; The temperature of described purified gas is 25 DEG C, and gauge pressure is 3.5MPa; The cold of described low temperature washing device for methanol is provided by freezing plant;
Eight, purified gas step 7 obtained and the rich hydrogen mixing from hydrogen recovery unit, obtain gas mixture, then gas mixture is passed into synthetic gas compression set through two sections of compressions, obtain two sections of compressed gass, then in the compressor housing of synthetic gas compression set by two sections of compressed gass and from methanol synthesizer circulation gas mixing compression after, obtain synthetic gas; The temperature of described gas mixture is 40 DEG C, and absolute pressure is 3.3MPa; The temperature of described two sections of compressed gass is 40 DEG C, and absolute pressure is 8.17MPa; The temperature of the described circulation gas from methanol synthesizer 11 is 40 DEG C, and absolute pressure is 8.17MPa; The temperature of described synthetic gas is 73 DEG C, and absolute pressure is 8.94MPa;
Nine, synthetic gas step 8 obtained is preheating to 235 DEG C through interchanger, sends into methanol synthesizer and carries out separation synthesis, obtain gas and crude carbinol; Described gas is circulation gas and periodic off-gases, and circulation gas is sent into synthetic gas compression set and mixed with section compressed gas of two in step 8, and periodic off-gases sends into hydrogen recovery unit, and the temperature of described crude carbinol is 40 DEG C, and gauge pressure is 0.5MPa;
Ten, crude carbinol step 9 obtained and carry out rectifying from entering methanol rectifying system after the rare alcohol water mixing of hydrogen recovery unit, obtains refined methanol; Methanol content in described refined methanol is 98%;
11, refined methanol step 10 obtained is sent into tank field and is stored, then from tank field, refined methanol is sent into synthesizing stable lighter hydrocarbons facilities to synthesize, obtain mixed light-hydrocarbon, mixed light-hydrocarbon is sent into lighter hydrocarbons tripping device and carry out rectifying separation, obtain LPG, light stable light hydrocarbon and heavy lighter hydrocarbons, namely complete coke lighter hydrocarbons.
The invention has the beneficial effects as follows:
The present invention is burnt for raw material with chemical industry, pure oxygen-steam normal pressure continuous gasification technology is adopted to produce synthetic raw gas, raw gas is after the process such as dedusting, washing, cooling and electric precipitation, being forced into gauge pressure is again 4.0MPa, after entering conversion adjustment hydrogen-carbon ratio, deliver to low-temp methanol to carry out sour gas and remove to meet the requirement of methanol-fueled CLC to synthetic gas, then be Material synthesis stable light hydrocarbon with methyl alcohol, simultaneously by-product heavy lighter hydrocarbons and LPG.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the method for a kind of coke lighter hydrocarbons of the present invention.
Embodiment
Embodiment one: composition graphs 1 illustrates present embodiment, the method for a kind of coke lighter hydrocarbons of present embodiment is specifically carried out according to the following steps:
One, adopt gas maker 1 to gasify coke 18, steam 19 and oxygen, obtain the water-gas after gasifying; Described oxygen is the 4000mmH from air separation facility 17
2o post oxygen; The temperature of the water-gas after described gasification is-40 DEG C, and gauge pressure is 0.006MPa;
Two, the water-gas after gasification step one obtained adopts electric dust collector 2 to carry out dust removal process, obtains the water-gas of electric precipitation; The temperature of the water-gas of described electric precipitation is 40 DEG C, and absolute pressure is 0.103MPa;
The water-gas of the electric precipitation three, step 2 obtained delivers to gas cabinet assembly 3, then enters gas pressing device 4, obtains the water-gas after pressurizeing; The temperature of the water-gas after described pressurization is 40 DEG C, and absolute pressure is 0.4MPa;
Four, the water-gas after pressurization step 3 obtained is undertaken purifying and regenerating by TSA adsorption unit 5, obtains the water-gas of Temp .-changing adsorption; The temperature of the water-gas of described Temp .-changing adsorption is 40 DEG C, and absolute pressure is 0.4MPa;
The water-gas of the Temp .-changing adsorption five, step 4 obtained is boosted by gas compression device 6, obtains the water-gas after compressing; The temperature of the water-gas after described compression is 90 DEG C, and absolute pressure is 4.0MPa, and the percentage composition of dry CO is 45.81%;
Six, the water-gas after compression step 5 obtained is undertaken converting by conversion refrigerating unit 7, pre-recovery of heat and cooling, obtains conversion gas; The temperature of described conversion gas is 40 DEG C, and gauge pressure is 3.7MPa;
Seven, the conversion gas that step 6 obtains is delivered to low temperature washing device for methanol 8 to wash, obtain sulfur-containing tail gas 20, CO
2to drop a hint 21 and purified gas; The emptying after tail gas recovery tower washing and recycling methyl alcohol of described sulfur-containing tail gas 20; Described CO
2to drop a hint 21 direct emptying; The temperature of described purified gas is 25 DEG C, and gauge pressure is 3.5MPa; The cold of described low temperature washing device for methanol 8 is provided by freezing plant 9;
Eight, purified gas step 7 obtained and the rich hydrogen mixing from hydrogen recovery unit 10, obtain gas mixture, then gas mixture is passed into synthetic gas compression set 12 through two sections of compressions, obtain two sections of compressed gass, then in the compressor housing of synthetic gas compression set 12 by two sections of compressed gass and from methanol synthesizer 11 circulation gas mixing compression after, obtain synthetic gas; The temperature of described gas mixture is 40 DEG C, and absolute pressure is 3.3MPa; The temperature of described two sections of compressed gass is 40 DEG C, and absolute pressure is 8.17MPa; The temperature of the described circulation gas from methanol synthesizer 11 is 40 DEG C, and absolute pressure is 8.17MPa; The temperature of described synthetic gas is 73 DEG C, and absolute pressure is 8.94MPa;
Nine, synthetic gas step 8 obtained is preheating to 235 DEG C through interchanger, sends into methanol synthesizer 11 and carries out separation synthesis, obtain gas and crude carbinol; Described gas is circulation gas and periodic off-gases, and circulation gas is sent into synthetic gas compression set 12 and mixed with section compressed gas of two in step 8, and periodic off-gases sends into hydrogen recovery unit 10, and the temperature of described crude carbinol is 40 DEG C, and gauge pressure is 0.5MPa;
Ten, crude carbinol step 9 obtained and carry out rectifying from entering methanol rectifying system 13 after the rare alcohol water mixing of hydrogen recovery unit 10, obtains refined methanol; Methanol content in described refined methanol is 98%;
11, refined methanol step 10 obtained is sent into tank field 14 and is stored, then from tank field 14, refined methanol is sent into synthesizing stable lighter hydrocarbons facilities 15 to synthesize, obtain mixed light-hydrocarbon, mixed light-hydrocarbon is sent into lighter hydrocarbons tripping device 16 and carry out rectifying separation, obtain LPG22, light stable light hydrocarbon 23 and heavy lighter hydrocarbons 24, namely complete coke lighter hydrocarbons.
Gas maker described in present embodiment step one adopts pure oxygen-steam normal pressure continuous gasification process, the high (CO+H of active constituent content in the raw gas of preparation
2be 80%), and discharge without blowing air.
Convert refrigerating unit described in present embodiment step 6 and adopt heat exchange type pressurization sulfur-resisting transformation, its objective is and raw gas is purified, remove the impurity such as oil wherein, dirt, and make raw gas temperature reach the light-off temperature of catalyst.
Described in present embodiment step 7, low temperature washing device for methanol working pressure is high, CO
2dividing potential drop is higher, and total sulfur is removed to below 0.1ppm, can simultaneously selectively by sulfide in gas, CO
2, HCN, the impurity removal such as oils be clean, and solution receptivity is large, internal circulating load is little, power consumption and regeneration energy consumption is low, solvent low price, process cost are low.
Synthetic gas compression set described in present embodiment step 8 adopts purified gas and circulation gas associating compressor unit, divide two sections of compressions, mix in cylinder with purified gas and circulation gas, final compressor top hole pressure 8.94MPa (A), centrifugal, steam turbine drives, unit cycle of operation is long, does not need standby host, and flow process is simple, efficiency is high, and energy-saving effect is remarkable.
Methanol synthesizer described in present embodiment step 9 adopts the isothermal methanol sythesis reactor of I.M.C.
Methanol rectifying system described in present embodiment step 10 adopts three-column process flow.
Hydrogen recovery unit described in present embodiment step 8 adopts pressure-variable adsorption or membrane sepn.
Synthesizing stable lighter hydrocarbons facilities described in present embodiment step 11 adopts single stage method, eliminate the step of methanol conversion preparing dimethy ether, methyl alcohol ZSM-5 molecular sieve catalyzer effect next step be converted into lighter hydrocarbons and LPG, its technical process is short, product selectivity is high, catalyst stability and single pass life high.
Present embodiment is burnt for raw material with chemical industry, pure oxygen-steam normal pressure continuous gasification technology is adopted to produce synthetic raw gas, raw gas is after the process such as dedusting, washing, cooling and electric precipitation, being forced into gauge pressure is again 4.0MPa, after entering conversion adjustment hydrogen-carbon ratio, deliver to low-temp methanol to carry out sour gas and remove to meet the requirement of methanol-fueled CLC to synthetic gas, then be Material synthesis stable light hydrocarbon with methyl alcohol, simultaneously by-product heavy lighter hydrocarbons and LPG.
Embodiment two: present embodiment and embodiment one unlike: the particle diameter of the coke 18 described in step one is 10mm ~ 50mm, and adding speed is 102916kg/h.Other are identical with embodiment one.
Embodiment three: present embodiment and embodiment one or two unlike: the speed that passes into of the steam 19 described in step one is 37500kg/h.Other are identical with embodiment one or two.
Embodiment four: one of present embodiment and embodiment one to three unlike: the speed that passes into of the oxygen described in step one is 50000Nm
3/ h.Other are identical with one of embodiment one to three.
Embodiment five: one of present embodiment and embodiment one to four unlike: the freezing plant 9 described in step 7 adopts ammonia compression refrigeration.Other are identical with one of embodiment one to four.
Embodiment six: one of present embodiment and embodiment one to five unlike: the speed that passes into of conversion gas described in step 7 is 263922.7Nm
3/ h.Other are identical with one of embodiment one to five.
Embodiment seven: one of present embodiment and embodiment one to six unlike: the mass ratio of the periodic off-gases described in step 9 and circulation gas is 1:(15 ~ 20).Other are identical with one of embodiment one to six.
Embodiment eight: the speed that one of present embodiment and embodiment one to seven send into synthesizing stable lighter hydrocarbons facilities 15 unlike: refined methanol described in step 11 is 75.1t/h.Other are identical with one of embodiment one to seven.
Beneficial effect of the present invention is verified by following examples:
A kind of method of coke lighter hydrocarbons is specifically carried out according to the following steps:
One, adopt gas maker 1 to gasify coke 18, steam 19 and oxygen, obtain the water-gas after gasifying; Described oxygen is the 4000mmH from air separation facility 17
2o post oxygen; The temperature of the water-gas after described gasification is-40 DEG C, and gauge pressure is 0.006MPa;
Two, the water-gas after gasification step one obtained adopts electric dust collector 2 to carry out dust removal process, obtains the water-gas of electric precipitation; The temperature of the water-gas of described electric precipitation is 40 DEG C, and absolute pressure is 0.103MPa;
The water-gas of the electric precipitation three, step 2 obtained delivers to gas cabinet assembly 3, then enters gas pressing device 4, obtains the water-gas after pressurizeing; The temperature of the water-gas after described pressurization is 40 DEG C, and absolute pressure is 0.4MPa;
Four, the water-gas after pressurization step 3 obtained is undertaken purifying and regenerating by TSA adsorption unit 5, obtains the water-gas of Temp .-changing adsorption; The temperature of the water-gas of described Temp .-changing adsorption is 40 DEG C, and absolute pressure is 0.4MPa;
The water-gas of the Temp .-changing adsorption five, step 4 obtained is boosted by gas compression device 6, obtains the water-gas after compressing; The temperature of the water-gas after described compression is 90 DEG C, and absolute pressure is 4.0MPa, and the percentage composition of dry CO is 45.81%;
Six, the water-gas after compression step 5 obtained is undertaken converting by conversion refrigerating unit 7, pre-recovery of heat and cooling, obtains conversion gas; The temperature of described conversion gas is 40 DEG C, and gauge pressure is 3.7MPa;
Seven, the conversion gas that step 6 obtains is delivered to low temperature washing device for methanol 8 to wash, obtain sulfur-containing tail gas 20, CO
2to drop a hint 21 and purified gas; The emptying after tail gas recovery tower washing and recycling methyl alcohol of described sulfur-containing tail gas; Described CO
2to drop a hint direct emptying; The temperature of described purified gas is 25 DEG C, and gauge pressure is 3.5MPa; The cold of described low temperature washing device for methanol 8 is provided by freezing plant 9;
Eight, purified gas step 7 obtained and the rich hydrogen mixing from hydrogen recovery unit 10, obtain gas mixture, then gas mixture is passed into synthetic gas compression set 12 through two sections of compressions, obtain two sections of compressed gass, then in the compressor housing of synthetic gas compression set 12 by two sections of compressed gass and from methanol synthesizer 11 circulation gas mixing compression after, obtain synthetic gas; The temperature of described gas mixture is 40 DEG C, and absolute pressure is 3.3MPa; The temperature of described two sections of compressed gass is 40 DEG C, and absolute pressure is 8.17MPa; The temperature of the described circulation gas from methanol synthesizer 11 is 40 DEG C, and absolute pressure is 8.17MPa; The temperature of described synthetic gas is 73 DEG C, and absolute pressure is 8.94MPa;
Nine, synthetic gas step 8 obtained is preheating to 235 DEG C through interchanger, sends into methanol synthesizer 11 and carries out separation synthesis, obtain gas and crude carbinol; Described gas is circulation gas and periodic off-gases, and circulation gas is sent into synthetic gas compression set 12 and mixed with section compressed gas of two in step 8, and periodic off-gases sends into hydrogen recovery unit 10, and the temperature of described crude carbinol is 40 DEG C, and gauge pressure is 0.5MPa;
Ten, crude carbinol step 9 obtained and carry out rectifying from entering methanol rectifying system 13 after the rare alcohol water mixing of hydrogen recovery unit 10, obtains refined methanol; Methanol content in described refined methanol is 98%;
11, refined methanol step 10 obtained is sent into tank field 14 and is stored, then from tank field 14, refined methanol is sent into synthesizing stable lighter hydrocarbons facilities 15 to synthesize, obtain mixed light-hydrocarbon, mixed light-hydrocarbon is sent into lighter hydrocarbons tripping device 16 and carry out rectifying separation, obtain LPG22, light stable light hydrocarbon 23 and heavy lighter hydrocarbons 24, namely complete coke lighter hydrocarbons.
Gas maker described in the present embodiment step one adopts pure oxygen-steam normal pressure continuous gasification process, the high (CO+H of active constituent content in the raw gas of preparation
2be 80%), and discharge without blowing air.
Convert refrigerating unit described in the present embodiment step 6 and adopt heat exchange type pressurization sulfur-resisting transformation, its objective is and raw gas is purified, remove the impurity such as oil wherein, dirt, and make raw gas temperature reach the light-off temperature of catalyst.
Described in the present embodiment step 7, low temperature washing device for methanol working pressure is high, CO
2dividing potential drop is higher, and total sulfur is removed to below 0.1ppm, can simultaneously selectively by sulfide in gas, CO
2, HCN, the impurity removal such as oils be clean, and solution receptivity is large, internal circulating load is little, power consumption and regeneration energy consumption is low, solvent low price, process cost are low.
Synthetic gas compression set described in the present embodiment step 8 adopts purified gas and circulation gas associating compressor unit, divide two sections of compressions, mix in cylinder with purified gas and circulation gas, final compressor top hole pressure 8.94MPa (A), centrifugal, steam turbine drives, unit cycle of operation is long, does not need standby host, and flow process is simple, efficiency is high, and energy-saving effect is remarkable.
Methanol synthesizer described in the present embodiment step 9 adopts the isothermal methanol sythesis reactor of I.M.C.
Methanol rectifying system described in the present embodiment step 10 adopts three-column process flow.
Hydrogen recovery unit described in the present embodiment step 8 adopts pressure-variable adsorption or membrane sepn.
Synthesizing stable lighter hydrocarbons facilities described in the present embodiment step 11 adopts single stage method, eliminate the step of methanol conversion preparing dimethy ether, methyl alcohol ZSM-5 molecular sieve catalyzer effect next step be converted into lighter hydrocarbons and LPG, its technical process is short, product selectivity is high, catalyst stability and single pass life high.
The present embodiment is burnt for raw material with chemical industry, pure oxygen-steam normal pressure continuous gasification technology is adopted to produce synthetic raw gas, raw gas is after the process such as dedusting, washing, cooling and electric precipitation, being forced into gauge pressure is again 4.0MPa, after entering conversion adjustment hydrogen-carbon ratio, deliver to low-temp methanol to carry out sour gas and remove to meet the requirement of methanol-fueled CLC to synthetic gas, then be Material synthesis stable light hydrocarbon with methyl alcohol, simultaneously by-product heavy lighter hydrocarbons and LPG.
Claims (8)
1. a method for coke lighter hydrocarbons, is characterized in that the method for coke lighter hydrocarbons is specifically carried out according to the following steps:
One, adopt gas maker (1) to gasify coke (18), steam (19) and oxygen, obtain the water-gas after gasifying; Described oxygen is the 4000mmH from air separation facility (17)
2o post oxygen; The temperature of the water-gas after described gasification is-40 DEG C, and gauge pressure is 0.006MPa;
Two, the water-gas after gasification step one obtained adopts electric dust collector (2) to carry out dust removal process, obtains the water-gas of electric precipitation; The temperature of the water-gas of described electric precipitation is 40 DEG C, and absolute pressure is 0.103MPa;
The water-gas of the electric precipitation three, step 2 obtained delivers to gas cabinet assembly (3), then enters gas pressing device (4), obtains the water-gas after pressurizeing; The temperature of the water-gas after described pressurization is 40 DEG C, and absolute pressure is 0.4MPa;
Four, the water-gas after pressurization step 3 obtained is undertaken purifying and regenerating by TSA adsorption unit (5), obtains the water-gas of Temp .-changing adsorption; The temperature of the water-gas of described Temp .-changing adsorption is 40 DEG C, and absolute pressure is 0.4MPa;
The water-gas of the Temp .-changing adsorption five, step 4 obtained is boosted by gas compression device (6), obtains the water-gas after compressing; The temperature of the water-gas after described compression is 90 DEG C, and absolute pressure is 4.0MPa, and the percentage composition of dry CO is 45.81%;
Six, the water-gas after compression step 5 obtained is undertaken converting by conversion refrigerating unit (7), pre-recovery of heat and cooling, obtains conversion gas; The temperature of described conversion gas is 40 DEG C, and gauge pressure is 3.7MPa;
Seven, the conversion gas that step 6 obtains is delivered to low temperature washing device for methanol (8) to wash, obtain sulfur-containing tail gas (20), CO
2to drop a hint (21) and purified gas; The emptying after tail gas recovery tower washing and recycling methyl alcohol of described sulfur-containing tail gas; Described CO
2to drop a hint direct emptying; The temperature of described purified gas is 25 DEG C, and gauge pressure is 3.5MPa; The cold of described low temperature washing device for methanol (8) is provided by freezing plant (9);
Eight, purified gas step 7 obtained and the rich hydrogen mixing from hydrogen recovery unit (10), obtain gas mixture, then gas mixture is passed into synthetic gas compression set (12) through two sections of compressions, obtain two sections of compressed gass, then in the compressor housing of synthetic gas compression set (12) by two sections of compressed gass and from methanol synthesizer (11) circulation gas mixing compression after, obtain synthetic gas; The temperature of described gas mixture is 40 DEG C, and absolute pressure is 3.3MPa; The temperature of described two sections of compressed gass is 40 DEG C, and absolute pressure is 8.17MPa; The temperature of the described circulation gas from methanol synthesizer (11) is 40 DEG C, and absolute pressure is 8.17MPa; The temperature of described synthetic gas is 73 DEG C, and absolute pressure is 8.94MPa;
Nine, synthetic gas step 8 obtained is preheating to 235 DEG C through interchanger, sends into methanol synthesizer (11) and carries out separation synthesis, obtain gas and crude carbinol; Described gas is circulation gas and periodic off-gases, circulation gas is sent into synthetic gas compression set (12) and is mixed with section compressed gas of two in step 8, periodic off-gases sends into hydrogen recovery unit (10), and the temperature of described crude carbinol is 40 DEG C, and gauge pressure is 0.5MPa;
Ten, crude carbinol step 9 obtained and carry out rectifying from entering methanol rectifying system (13) after the rare alcohol water mixing of hydrogen recovery unit (10), obtains refined methanol; Methanol content in described refined methanol is 98%;
11, refined methanol step 10 obtained is sent into tank field (14) and is stored, then from tank field (14), refined methanol is sent into synthesizing stable lighter hydrocarbons facilities (15) to synthesize, obtain mixed light-hydrocarbon, mixed light-hydrocarbon is sent into lighter hydrocarbons tripping device (16) and carry out rectifying separation, obtain LPG (22), light stable light hydrocarbon (23) and heavy lighter hydrocarbons (24), namely complete coke lighter hydrocarbons.
2. the method for a kind of coke lighter hydrocarbons according to claim 1, it is characterized in that the particle diameter of the coke (18) described in step one is 10mm ~ 50mm, adding speed is 102916kg/h.
3. the method for a kind of coke lighter hydrocarbons according to claim 1, is characterized in that the speed that passes into of the steam (19) described in step one is 37500kg/h.
4. the method for a kind of coke lighter hydrocarbons according to claim 1, is characterized in that the speed that passes into of the oxygen described in step one is 50000Nm
3/ h.
5. the method for a kind of coke lighter hydrocarbons according to claim 1, is characterized in that the freezing plant (9) described in step 7 adopts ammonia compression refrigeration.
6. the method for a kind of coke lighter hydrocarbons according to claim 1, is characterized in that the speed that passes into of conversion gas described in step 7 is 263922.7Nm
3/ h.
7. the method for a kind of coke lighter hydrocarbons according to claim 1, is characterized in that the mass ratio of the periodic off-gases described in step 9 and circulation gas is 1:(15 ~ 20).
8. the method for a kind of coke lighter hydrocarbons according to claim 1, is characterized in that the speed of feeding synthesizing stable lighter hydrocarbons facilities of refined methanol described in step 11 (15) is 75.1t/h.
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Citations (2)
| 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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Patent Citations (2)
| 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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