CN105733716A - Process for preparing synthetic natural gas through coke-oven gas methanation - Google Patents
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Abstract
The invention relates to a process for preparing synthetic natural gas through coke-oven gas methanation. A two-stage methanation furnace is adopted. Feed gas is separated in a fresh gas liquid separation tank, such that part of possibly existing liquid water is removed; the feed gas is preheated in a fresh gas preheater, and is mixed with circulation gas preheated through a second reaction inlet heat exchanger; the mixture enters a first methanation reactor; outlet gas from the first methanation reactor is processed through an overheat device and a steam generator, such that steam is generated; the circulation gas preheated at the second reaction inlet heat exchanger is cooled and enters a second methanation reactor; outlet gas from the second methanation reactor is separated, such that part of possibly existing liquid water is removed; the gas is divided into two streams; one stream is subjected to pressurizing, pressure-stabilizing and preheating, and enters the first methanation reactor; the other stream is subjected to condensation separation, such that product gas is obtained, and is discharged from the device. The process provided by the invention has the advantages of reasonable energy utilization, low recycle ratio, and good economic benefit.
Description
Technical field
The invention belongs to oven gas comprehensive application technology field, relate to the technique that coke-oven gas methanation produces synthetic natural gas.
Background technology
CNOOC announced on January 4th, 2012, by an oven gas and extra CO2Change into synthetic natural gas (SNG) and rope company of liquefied natural gas (LNG) bid awarding Top.Oven gas is produced the technology transfer of SNG, engineering development and catalyst by the said firm.Oven gas valuable compounds therefrom is used by this technology, consumes from outside CO2, thus reducing CO2Discharge.TREMP technology is also used for methanation, and TREMP technology is China, 6 the overlapping and use on large-scale SNG devices of Korea S.Contractor is sea petroleum gas and electricity power group in subsidiary of CNOOC.Device is positioned at Heze city of Shandong province.Feeding gas is the coke-stove gas that coke-oven plant " discards ", CO2From chemical fertilizer factory.The technology platform utilizing CNOOC is converted to LNG by product SNG, and distributes to local market.
Shanxi Guo Xin Lou Jun limited energy company and Southwest Chemical Research and Design Institute (being called for short southwest institute) have signed the cooperation agreement of oven gas synthetic natural gas (SNG) project, using oven gas produced by coking as unstripped gas SNG, unit scale is 5 × 104m3/ h (in standard state), the end of the year 2011 were constructed and put into operation.This project construction investment is the 30%～40% of same size coal preparing natural gas, and project produces SNG2 × 10 per year after building up8Nm3, it is achieved coke-stove gas zero-emission, year reducing emission of carbon dioxide 338kt, sulfur dioxide 1.21kt, dust total amount 16t.This device adopts southwest institute oven gas SNG patented technology to belong to country's Eleventh Five-Year Plan science and technology supporting project key project, and the expert organized by the Department of Science and Technology is checked and accepted.
In August, 2010, the oven gas preparing natural gas assay device that Dalian Puri spy, the Shandong ferrum hero energy, the new auspicious cooperation in five rings, Chengdu complete completes 1000h long run test, and this project passes through Shandong Province's technical appraisement.CH in oven gas4、CO、CO2Total content is 40%, and H content is high.Oven gas passes through methanation reaction, major part CO, CO2Etc. changing into CH4, obtain containing H2、CH4、N2Mixing gas, the natural gas of more than 90% can be obtained by pressure-variable adsorption or membrane separation technique.This project have employed two-stage nitration thermal insulation low-pressure tail gas and do not circulate and add the multinomial innovative technology of steam, and the research of methanation catalyst and engineering process is undertaken by Dalian Pratt Chemical Technology Co., Ltd.
On December 18th, 2010; successfully driven with " Wuhai Hua Qing Nm3/ days coke-oven gas methanation CNG of Energy Science Co., Ltd 120,000 " device that Beijing Su Xi company develops cooperatively by Wuhan Kelin Fine Chemical Co., Ltd.; indicate that coke-oven gas methanation CNG successfully realizes production domesticization, be the milestone of domestic oven gas comprehensive utilization project." Wuhai Hua Qing Nm3/ days coke-oven gas methanation CNG of Energy Science Co., Ltd 120,000 " property device is mainly made up of oven gas advanced purification system, methanation system, pressure swing adsorption system part, by purifying imurity-removal, making sulfur content≤0.1mg/m in oven gas3, the product of methane concentration more than 90% is obtained by steps such as multistage methanation reaction, PSA separation of methane.This covering device feature is: 1, methanation reaction adopts circulation and multistage cold shock technique, controls methanation entrance CO content, controls methanation outlet temperature, is beneficial to being smoothed out of methanation reaction, it is suppressed that the generation of side reaction；2, methanation catalyst activity is good, Heat stability is good, and anti-carbon is good, has good low temperature activation characteristics, can also be converted by high hydrocarbon and good antioxygenic property simultaneously；3, institute's calorific requirement is obtained by methanation reaction, and the attached producing steam of waste heat can use it for anything else, and equipment investment is few, and technique is simple.Along with the adjustment to the attention of environmental protection work and energy resource structure strategy flexibility; natural gas technology is also rapidly developed and popularization and application in China, and Wuhai China coke cleaning furnace gas methanation CNG device successfully drives to illustrate the bright prospects of oven gas comprehensive utilization.
In June, 2010, Linda company, contemporaneity reach group, Taiyuan science and engineering engineering company and Puri spy company and sign an agreement, low-temperature heat exchange formula oven gas synthetic natural gas new technology in joint development.The synthesis pressure of above-mentioned technique is tentatively decided to be 0.4MPa～0.8MPa, and hot(test)-spot temperature is 300 DEG C～500 DEG C.Day processes coke oven tolerance 5000m3。
The coke-stove gas comprehensive utilization of Hejin, Shanxi produces liquefied natural gas (LNG) engineering by Chinese Academy of Sciences's physiochemical techniques institute as responsible party, and qualified LNG product linked through 7 days, smooth output.Impurity in oven gas adopts the elimination of combined purifying technique, the extraction and application ceramic membrane separation device of hydrogen, and what enter liquefying and rectifying unit is methane-rich gas.Qualified LNG is finally obtained by cryogenic rectification, reinstalls product storage tank.
Summary of the invention
The technique that present invention aim at providing a kind of reasonable energy utilization, recycle ratio little, good in economic efficiency, is the process producing natural gas with oven gas through methanation reaction.
In order to realize foregoing invention purpose, the technical solution used in the present invention is as follows:
Flow process adopts two sections of methanation furnaces, unstripped gas is separated off wherein operative liquid water that may be present through virgin gas separatory tank 1, entering the first methanator 2 after mixing with the circulating air after two anti-entrance heat exchangers 5 preheatings after virgin gas preheater 1 and virgin gas preheater 27 preheat successively, steam is carried out overheated, steam generator 4 through steam superheater 3 and is cooled to suitable temperature after there are steam, two anti-entrance heat exchanger 5 warm-up cycle gas and enters the second methanator 6 by the first methanator 2 exit gas.Second methanator 6 exit gas separatory tank 9 before virgin gas preheater 27, water cooler 1, compressor is separated off wherein operative liquid water that may be present, this gas is divided into two strands afterwards, one stock-traders' know-how recycle compressor 13 boosts, steady tank 14 voltage stabilizing after compressor, two anti-entrance heat exchangers 5 enter the first methanator entrance after being preheated to suitable temperature, after another stock-traders' know-how virgin gas preheater 1, water cooler 2 11, gas product separatory tank 12 condensation separation gas product goes out device.
In the above-mentioned methods, the first methanator 2 belongs to high-temperature methanation reactive moieties, and the second methanator 6 belongs to low temperature methanation reaction part.
Described first methanator 2 inlet temperature is 250 DEG C ~ 350 DEG C, and outlet temperature is 500 DEG C ~ 700 DEG C；Second methanator 6 inlet temperature is 200 DEG C ~ 300 DEG C, and outlet temperature is 220 DEG C ~ 350 DEG C.Said two methanator pressure is 0.4MPa ~ 8MPa, with the volume space velocity of dry gas calculating for 5000h in reactor-1~30000h-1。
In the above-mentioned methods, the first methanator 2 outlet arranges steam superheater 3, and its shell side walks high methane gas, and outlet temperature is 550 DEG C ~ 450 DEG C, and tube side walks superheated steam, and outlet temperature is 250 DEG C ~ 540 DEG C.
F=(n in described synthesis gasH2-nCO2)/(nCO+nCO2)=2.8 ~ 3.1, it is preferred to 2.9 ~ 3.05.
The described reactor carrying out methanation reaction is adiabatic reactor.
Described catalyst, with nickel for main active component, is aided with first, second auxiliary agent, adopts the sedimentation method to prepare reactive precursor.First auxiliary agent is transition metal, including La, Ce, Zr, Ti etc. therein one or both.Content is the 0.1%-5% of Ni mass；Second auxiliary agent be the dispersants such as triethyl group hexyl phosphoric acid, sodium lauryl sulphate, methyl anyl alcohol, cellulose derivative, polyacrylamide, guar gum, ethylene glycol, Polyethylene Glycol, fatty acid polyethylene glycol ester, glycerol therein one or more, conventional water is replaced to use as dispersant during precipitation, the 0.01-1% making consumption be Ni consumption.
Catalyst carrier is made up of the complex salt of aluminium oxide with aluminum, magnesium, and wherein aluminium oxide is with γ-Al2O3Or δ-Al2O3Or α-Al2O3Form exists, and the complex salt of aluminum and magnesium is with MgAl2O4Form exists.
The inventive method is compared with existing coke-oven gas methanation process, have the following advantages and prominent effect, structure of reactor and flow process are simple, can reasonably utilize the huge heat that methanation reaction releases, the superheated steam of by-product high potential by the combination of reactor.
Accompanying drawing explanation
Fig. 1 is the process flow diagram of embodiment of the present invention coal based synthetic gas methanation synthetic natural gas.
Detailed description of the invention
Below in conjunction with drawings and Examples being described in detail to the present invention.
Embodiment 1
As shown in Figure 1, the 0.4MPa come from upstream, unstripped gas (the gas composition molar fraction H of 40 DEG C20.5841、CO0.1106、CO20.0043、CH40.2053、N20.0391、C2H60.0366、C3H80.0201) it is separated off wherein operative liquid water that may be present through virgin gas separatory tank 1, after virgin gas preheater 1 and virgin gas preheater 27 preheat successively temperature rise to 280 DEG C mix with the circulating air after two anti-entrance heat exchangers 5 are preheated to 280 DEG C after enter the first methanator 2, after there is methanation reaction, first methanator 2 Outlet Gas Temperature rises to 600 DEG C, it is overheated through steam superheater 3, steam to be carried out, there is steam in steam generator 4, two anti-entrance heat exchanger 5 warm-up cycle gas are cooled to 480 DEG C successively, 300 DEG C, the second methanator 6 is entered after 265 DEG C.After there is methanation reaction, second methanator 6 Outlet Gas Temperature rises to 304 DEG C, this is worked off one's feeling vent one's spleen and virgin gas preheater 27, after water cooler 1 heat exchange, temperature reduces to 250 DEG C successively, after 200 DEG C, before compressor, separatory tank 9 is separated off the operative liquid water wherein existed, this gas is divided into two strands afterwards, one stock-traders' know-how recycle compressor 13 boosts, steady tank 14 voltage stabilizing after compressor, two anti-entrance heat exchangers 5 enter the first methanator entrance after being preheated to 280 DEG C, another stock-traders' know-how virgin gas preheater 1, water cooler 2 11, obtain gas product after gas product separatory tank 12 condensation separation and go out device.
Embodiment 2
As shown in Figure 1, the 1.0MPa come from upstream, unstripped gas (the gas composition molar fraction H of 40 DEG C20.5841、CO0.1106、CO20.0043、CH40.2053、N20.0391、C2H60.0366、C3H80.0201) it is separated off wherein operative liquid water that may be present through virgin gas separatory tank 1, after virgin gas preheater 1 and virgin gas preheater 27 preheat successively temperature rise to 280 DEG C mix with the circulating air after two anti-entrance heat exchangers 5 are preheated to 280 DEG C after enter the first methanator 2, after there is methanation reaction, first methanator 2 Outlet Gas Temperature rises to 620 DEG C, it is overheated through steam superheater 3, steam to be carried out, there is steam in steam generator 4, two anti-entrance heat exchanger 5 warm-up cycle gas are cooled to 510 DEG C successively, 300 DEG C, the second methanator 6 is entered after 265 DEG C.After there is methanation reaction, second methanator 6 Outlet Gas Temperature rises to 317 DEG C, this is worked off one's feeling vent one's spleen and virgin gas preheater 27, after water cooler 1 heat exchange, temperature reduces to 250 DEG C successively, after 200 DEG C, before compressor, separatory tank 9 is separated off the operative liquid water wherein existed, this gas is divided into two strands afterwards, one stock-traders' know-how recycle compressor 13 boosts, steady tank 14 voltage stabilizing after compressor, two anti-entrance heat exchangers 5 enter the first methanator entrance after being preheated to 280 DEG C, another stock-traders' know-how virgin gas preheater 1, water cooler 2 11, obtain gas product after gas product separatory tank 12 condensation separation and go out device.
Embodiment 3
As shown in Figure 1, the 1.0MPa come from upstream, unstripped gas (the gas composition molar fraction H of 40 DEG C20.5841、CO0.1106、CO20.0043、CH40.2053、N20.0391、C2H60.0366、C3H80.0201) it is separated off wherein operative liquid water that may be present through virgin gas separatory tank 1, after virgin gas preheater 1 and virgin gas preheater 27 preheat successively temperature rise to 280 DEG C mix with the circulating air after two anti-entrance heat exchangers 5 are preheated to 290 DEG C after enter the first methanator 2, after there is methanation reaction, first methanator 2 Outlet Gas Temperature rises to 650 DEG C, it is overheated through steam superheater 3, steam to be carried out, there is steam in steam generator 4, two anti-entrance heat exchanger 5 warm-up cycle gas are cooled to 550 DEG C successively, 300 DEG C, the second methanator 6 is entered after 265 DEG C.After there is methanation reaction, second methanator 6 Outlet Gas Temperature rises to 335 DEG C, this is worked off one's feeling vent one's spleen and virgin gas preheater 27, after water cooler 1 heat exchange, temperature reduces to 250 DEG C successively, after 200 DEG C, before compressor, separatory tank 9 is separated off the operative liquid water wherein existed, this gas is divided into two strands afterwards, one stock-traders' know-how recycle compressor 13 boosts, steady tank 14 voltage stabilizing after compressor, two anti-entrance heat exchangers 5 enter the first methanator entrance after being preheated to 280 DEG C, another stock-traders' know-how virgin gas preheater 1, water cooler 2 11, obtain gas product after gas product separatory tank 12 condensation separation and go out device.
Embodiment 4
As shown in Figure 1, the 4.0MPa come from upstream, unstripped gas (the gas composition molar fraction H of 40 DEG C20.5783、CO0.1037、CO20.0327、CH40.2354、N20.0214、C2H60.018、C3H80.015) it is separated off wherein operative liquid water that may be present through virgin gas separatory tank 1, after virgin gas preheater 1 and virgin gas preheater 27 preheat successively temperature rise to 280 DEG C mix with the circulating air after two anti-entrance heat exchangers 5 are preheated to 290 DEG C after enter the first methanator 2, after there is methanation reaction, first methanator 2 Outlet Gas Temperature rises to 620 DEG C, it is overheated through steam superheater 3, steam to be carried out, there is steam in steam generator 4, two anti-entrance heat exchanger 5 warm-up cycle gas are cooled to 510 DEG C successively, 300 DEG C, the second methanator 6 is entered after 265 DEG C.After there is methanation reaction, second methanator 6 Outlet Gas Temperature rises to 320 DEG C, this is worked off one's feeling vent one's spleen and virgin gas preheater 27, after water cooler 1 heat exchange, temperature reduces to 250 DEG C successively, after 200 DEG C, before compressor, separatory tank 9 is separated off the operative liquid water wherein existed, this gas is divided into two strands afterwards, one stock-traders' know-how recycle compressor 13 boosts, steady tank 14 voltage stabilizing after compressor, two anti-entrance heat exchangers 5 enter the first methanator entrance after being preheated to 290 DEG C, another stock-traders' know-how virgin gas preheater 1, water cooler 2 11, obtain gas product after gas product separatory tank 12 condensation separation and go out device.
Embodiment 5
As shown in Figure 1, the 8.0MPa come from upstream, unstripped gas (the gas composition molar fraction H of 40 DEG C20.5783、CO0.1037、CO20.0327、CH40.2354、N20.0214、C2H60.018、C3H80.015) it is separated off wherein operative liquid water that may be present through virgin gas separatory tank 1, after virgin gas preheater 1 and virgin gas preheater 27 preheat successively temperature rise to 290 DEG C mix with the circulating air after two anti-entrance heat exchangers 5 are preheated to 290 DEG C after enter the first methanator 2, after there is methanation reaction, first methanator 2 Outlet Gas Temperature rises to 700 DEG C, it is overheated through steam superheater 3, steam to be carried out, there is steam in steam generator 4, two anti-entrance heat exchanger 5 warm-up cycle gas are cooled to 530 DEG C successively, 300 DEG C, the second methanator 6 is entered after 265 DEG C.After there is methanation reaction, second methanator 6 Outlet Gas Temperature rises to 346 DEG C, this is worked off one's feeling vent one's spleen and virgin gas preheater 27, after water cooler 1 heat exchange, temperature reduces to 250 DEG C successively, after 200 DEG C, before compressor, separatory tank 9 is separated off the operative liquid water wherein existed, this gas is divided into two strands afterwards, one stock-traders' know-how recycle compressor 13 boosts, steady tank 14 voltage stabilizing after compressor, two anti-entrance heat exchangers 5 enter the first methanator entrance after being preheated to 290 DEG C, another stock-traders' know-how virgin gas preheater 1, water cooler 2 11, obtain gas product after gas product separatory tank 12 condensation separation and go out device.
Claims (9)
1. the technique of a coke-oven gas methanation synthetic natural gas, it is characterized in that: adopt two sections of methanation furnaces, unstripped gas is separated off wherein operative liquid water that may be present through virgin gas separatory tank, entering the first methanator after mixing with the circulating air after two anti-entrance heat exchangers preheatings after virgin gas preheater one and virgin gas preheater two preheat successively, steam is carried out entering the second methanator after overheated, steam generator generation steam, two anti-entrance heat exchanger warm-up cycle air cooling but by the first methanator exit gas through steam superheater；Second methanator exit gas separatory tank before virgin gas preheater two, water cooler one, compressor is separated off wherein operative liquid water that may be present, this gas is divided into two strands afterwards, enter the first methanator entrance after one stock-traders' know-how recycle compressor boosting, steady tank voltage stabilizing after compressor, two anti-entrance heat exchanger preheatings, obtain gas product after another stock-traders' know-how virgin gas preheater one, water cooler two, gas product separatory tank condensation separation and go out device.
2. technique as claimed in claim 1, it is characterised in that the first methanator belongs to high-temperature methanation reactive moieties, and the second methanator belongs to low temperature methanation reaction part.
3. technique as claimed in claim 1, it is characterised in that the first methanator inlet temperature is 250 DEG C ~ 350 DEG C, and outlet temperature is 500 DEG C ~ 700 DEG C；Second methanator inlet temperature is 200 DEG C ~ 300 DEG C, and outlet temperature is 220 DEG C ~ 350 DEG C.
4. technique as claimed in claim 1, it is characterised in that two methanator pressure are 1MPa ~ 8MPa.
5. technique as claimed in claim 1, it is characterised in that with the volume space velocity of dry gas calculating for 5000h in two methanators-1~30000h-1。
6. technique as claimed in claim 1, it is characterised in that the first methanator outlet arranges steam superheater, and its shell side walks high methane gas, and outlet temperature is 550 DEG C ~ 450 DEG C；Tube side walks superheated steam, and outlet temperature is 250 DEG C ~ 540 DEG C.
7. technique as claimed in claim 1, it is characterised in that f=(n in described synthesis gasH2-nCO2)/(nCO+nCO2)=2.8~3.1。
8. technique as claimed in claim 1, it is characterised in that f=(n in described synthesis gasH2-nCO2)/(nCO+nCO2)=2.9~3.05。
9. technique as claimed in claim 1, it is characterised in that described in carry out the reactor of methanation reaction and be adiabatic reactor.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108203609A (en) * | 2018-02-05 | 2018-06-26 | 中国石油化工股份有限公司 | A kind of short route process for synthesizing methane |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4133825A (en) * | 1976-05-21 | 1979-01-09 | British Gas Corporation | Production of substitute natural gas |
| CN101508922A (en) * | 2009-03-16 | 2009-08-19 | 西南化工研究设计院 | Methanation reaction process using oven gas to prepare substitute natural gas |
| CN102021054A (en) * | 2010-12-22 | 2011-04-20 | 西南化工研究设计院 | New process for synthesizing natural gas by methanation of coke oven gas |
| CN103509618A (en) * | 2012-06-29 | 2014-01-15 | 中国石油化工股份有限公司 | Methanation technique for preparing synthetic natural gas from coal-based synthetic gas |
| CN103740426A (en) * | 2012-10-17 | 2014-04-23 | 中国石油化工股份有限公司 | Method of producing substitute natural gas by methanation of synthesis gas |
-
2014
- 2014-12-11 CN CN201410754326.3A patent/CN105733716A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4133825A (en) * | 1976-05-21 | 1979-01-09 | British Gas Corporation | Production of substitute natural gas |
| CN101508922A (en) * | 2009-03-16 | 2009-08-19 | 西南化工研究设计院 | Methanation reaction process using oven gas to prepare substitute natural gas |
| CN102021054A (en) * | 2010-12-22 | 2011-04-20 | 西南化工研究设计院 | New process for synthesizing natural gas by methanation of coke oven gas |
| CN103509618A (en) * | 2012-06-29 | 2014-01-15 | 中国石油化工股份有限公司 | Methanation technique for preparing synthetic natural gas from coal-based synthetic gas |
| CN103740426A (en) * | 2012-10-17 | 2014-04-23 | 中国石油化工股份有限公司 | Method of producing substitute natural gas by methanation of synthesis gas |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108203609A (en) * | 2018-02-05 | 2018-06-26 | 中国石油化工股份有限公司 | A kind of short route process for synthesizing methane |
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