CN102876411A - Method and device for producing synthetic natural gas - Google Patents
Method and device for producing synthetic natural gas Download PDFInfo
- Publication number
- CN102876411A CN102876411A CN2012103800476A CN201210380047A CN102876411A CN 102876411 A CN102876411 A CN 102876411A CN 2012103800476 A CN2012103800476 A CN 2012103800476A CN 201210380047 A CN201210380047 A CN 201210380047A CN 102876411 A CN102876411 A CN 102876411A
- Authority
- CN
- China
- Prior art keywords
- gas
- strand
- heat
- exchange equipment
- product
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides a method and a device for producing synthetic natural gas. The method is a continuous process for producing methane-rich gas with methane molar percentage at least equal to 94% by taking coal or biomass gasification products as raw materials. By the method, operation temperature of a methane reactor can be controlled effectively, problems of temperature runaway and sintering of catalysts due to high fluctuation or accidents of the raw materials can be avoided. Besides, since a methane reaction heat utilization system is provided, comprehensive utilization rate of energy is increased.
Description
Technical field
The present invention relates to a kind of method and device of producing synthetic natural gas, relate to particularly take coal or gasifying biomass product as method and the device of raw material production synthetic natural gas, belong to the synthetic natural gas technical field.
Background technology
Since last century the seventies, be accompanied by oil crisis, preparing methane from coal (synthetic natural gas or substitute natural gas) is comparatively fast developed.The main method of preparing methane from coal comprises coal hydrogenation gasification direct production methane and indirectly produces methane through synthetic gas.
Coal hydrogenation gasification is given birth to methanogenic subject matter to be had: efficiency of carbon conversion is low, the methane yield is low, gas composition is complicated, methane concentration is low and can not get high-quality synthetic natural gas etc.Comparatively speaking, coal is through the technique of producing firedamp by syngas possess skills ripening degree height, carbon utilisation rate height and the high significant advantage of methane concentration.At the beginning of the eighties in last century, German LURGI has finished the exploitation of methanation process in conjunction with the methanation catalyst of BASF AG, and is successfully applied to the coal preparing natural gas factory of big plain in u.s.a factory 389 cubic meters per day; Company of Centrica has developed HICOM technique and corresponding catalyst for the synthetic gas characteristics of BGL vapourizing furnace, and has set up 2832m
3The pilot plant of/d; Rope company of Denmark Top has successfully developed the wide temperature range type catalyzer of 700 ℃ of high temperature of the highest ability, and has developed TREMP full methanation technique.
In China, to utilize coal production city coal gas as purpose, set up ripe coal gas part methanation technology in last century: researched and developed " Partial-methanation of Water-coal Gas At Atmospheric Pressure methanation production city coal gas " technology such as Dalian Chemiclophysics Inst., Chinese Academy of Sciences; The RHM-266 type nickel that chemical fertilizer institute of the Ministry of Chemical Industry has developed take the normal pressure semi-water gas as unstripped gas is methanation catalyst and technique; Coal Mining Research Institute has developed the two stage furnace water gas methanation process.
Along with the needs of Sustainable development, energy-saving and cost-reducing, raising efficiency of energy utilization becomes direction and the trend of each technical development.For methanation, high temperature, high top pressure operation, wide temperature range type catalyzer are conducive to equipment and process intensification, and then reduce energy consumption, and improve the hot grade of methanation reaction by-product and recovery utilization rate.Given this, the wide temperature range type methanation catalyst, high temperature, high pressure full methanation technology have become the development trend of current methanation technology.A methanation commercialization of big plain in u.s.a factory is only arranged at present in the world, and in being, the low temperature methanation technology, for high temperature, the high pressure full methanation technology of methanation development trend, still do not have the precedent of industrial applications.Domestic methanation technology only stays in the part methanation at present, and catalyzer adaptive temperature narrow range, has greatly limited the comprehensive utilization ratio of energy; The part methanation technology that carries out under the normal pressure in addition is unfavorable for reaction and equipment intensification, lacks the integrated optimization of reactor design and material-energy.
Summary of the invention
Therefore, the object of the present invention is to provide method and the device of a kind of generation synthetic natural gas (Synthetic Natural Gas, SNG).
The present invention realizes by the following technical solutions.
The invention provides a kind of method of producing synthetic natural gas.See figures.1.and.2, described method comprises the steps:
A) unstripped gas (1) 1:(0.5 ~ 5 by volume after the first heat-exchange equipment (2) is warming up to 150 ~ 400 ℃): (0 ~ 0.5): (0 ~ 0.5) is divided into first strand of unstripped gas (4), second strand of unstripped gas (5), the 3rd strand of unstripped gas (6) and the 4th strand of unstripped gas (7);
B) the first strand of unstripped gas (4) in the step a) and the first steam (39) and first strand of circulation gas (27) being mixed to get temperature is the first gas mixture (8) of 250 ~ 400 ℃, the first gas mixture (8) passed in the first paragraph methanator (9) react, obtain temperature and be 450 ~ 750 ℃ first paragraph gas product (10), this first paragraph gas product (10) is through the second heat-exchange equipment (11,11 ') and the 3rd heat-exchange equipment (13,13 ') be cooled to 250 ~ 400 ℃ of first paragraph gas products (14) after obtaining lowering the temperature;
C) it is the second gas mixture (15) of 250 ~ 400 ℃ that the first paragraph gas product (14) after the cooling that step b) is obtained and described second strand of unstripped gas (5), the second steam (40), second strand of circulation gas (28) are mixed to get temperature, the second gas mixture (15) passed in the second segment methanator (16) react, obtain temperature and be 450 ~ 700 ℃ second segment gas product (17), this second segment gas product (17) is cooled to 200 ~ 400 ℃ of second segment gas products (19) after the cooling that obtains through the 4th heat-exchange equipment (18,18 ');
D) the second segment gas product (19) after the cooling that step c) is obtained is (0.3 ~ 5) by volume: 1 is divided into circulation gas (20) and second strand of second segment gas product (21), described circulation gas (20) is cooled to the circulation gas (25) of sending into after 100 ~ 350 ℃ after recycle compressor (24) supercharging obtains supercharging through the 5th heat-exchange equipment (22), circulation gas after the supercharging (25) is warmed up to 200 ~ 350 ℃ through the 5th heat-exchange equipment (22), and then with its by volume (0.5 ~ 1): (0 ~ 0.5) is divided into described first strand of circulation gas (27) and second strand of circulation gas (28);
E) it is 200 ~ 400 ℃ the 3rd gas mixture (29) that the second strand of second segment gas product (21) that step d) is obtained and described the 3rd strand of unstripped gas (6), the 3rd steam (41) are mixed to get temperature, the 3rd gas mixture (29) passed in the 3rd section methanator (30) react, obtain temperature and be 300 ~ 550 ℃ the 3rd section gas product (31), the three section gas product (32) of the 3rd section gas product (31) after the first heat-exchange equipment (2) is cooled to 60 ~ 350 ℃ of coolings that obtain;
F) it is 60 ~ 200 ℃ the 4th gas mixture (33) that the 3rd section gas product (32) after the cooling that step e) is obtained and described the 4th strand of unstripped gas (7), the 4th steam (42) are mixed to get temperature, described the 4th gas mixture (33) passes in the 4th section methanator (36) after the 6th heat-exchange equipment (34) is warming up to 200 ~ 350 ℃ and reacts, and obtains temperature and be 250 ~ 450 ℃ the 4th section gas product (37);
G) the 4th section gas product (37) that step f) is obtained gone forward side by side through the 6th heat-exchange equipment (34) cooling, and to obtain temperature after promoting the circulation of qi liquid separates be 20 ~ 80 ℃ gas product (38).
Preferably, the molar percentage of described unstripped gas (1) is composed as follows: carbon monoxide 5 ~ 50%, carbonic acid gas 0 ~ 30%, hydrogen 20 ~ 80%, methane 0 ~ 20%.
Preferably, in described step a), the volume ratio of first strand of unstripped gas (4), second strand of unstripped gas (5), the 3rd strand of unstripped gas (6) and the 4th strand of unstripped gas (7) that described unstripped gas (1) is divided into can be 1:(0.5 ~ 2): (0 ~ 0.3): (0 ~ 0.3).
Preferably, in described step d), the circulation gas (20) that described second segment gas product (19) is divided into and the volume ratio of second strand of second segment gas product (21) can be (0.3 ~ 3): 1.
Preferably, in described step d), first strand of circulation gas (27) that described circulation gas (20) is divided into and the volume ratio of second strand of circulation gas (28) can be (0.7 ~ 1): (0 ~ 0.3).
In a kind of preferred embodiment of the present invention, described method also comprises utilizes the methanation reaction heat release in the following manner: make the oiler feed (43 from the battery limit (BL), 43 ') enter drum (44,44 '), make from drum (44,44 ') the first oiler feed (45,45 ') enter the second heat-exchange equipment (11,11 ') or the 3rd heat-exchange equipment (13,13 ') produce the first saturation steam (46,46 ') of 3 ~ 10MPa, make from drum (44,44 ') the second oiler feed (47,47 ') enter the second saturation steam (48 that the 4th heat-exchange equipment (18,18 ') produces 3 ~ 10MPa, 48 '), from the 3rd saturation steam (49,49 ') of drum (44,44 ') through the 3rd heat-exchange equipment (13,13 ') or the second heat-exchange equipment (11,11 ') heat up, obtain temperature and be 300 ~ 550 ℃ superheated vapour (50,50 ').
In the above-mentioned mode of utilizing the methanation reaction heat release, when the first oiler feed (45,45 ') entered the second heat-exchange equipment (11,11 '), the 3rd saturation steam (49,49 ') heated up through the 3rd heat-exchange equipment (13,13 '); When the first oiler feed (45,45 ') entered the 3rd heat-exchange equipment (13,13 '), the 3rd saturation steam (49,49 ') heated up through the second heat-exchange equipment (11,11 ').
According to the method for production synthetic natural gas provided by the invention, the method is take coal or gasifying biomass product as raw material, the production synthetic natural gas, and the molar percentage that contains methane in the synthetic natural gas product of gained is more than 94%.
On the other hand, the present invention also provides the device that is used for above-mentioned production synthesis of natural gas method provided by the invention, and this device comprises:
Methanator comprises be used to the first paragraph methanator (9) that carries out methanation reaction, second segment methanator (16), the 3rd section methanator (30) and the 4th section methanator (36);
Heat-exchange equipment, comprise the first heat-exchange equipment (2), the second heat-exchange equipment (11 for heating and/or cooling gas, 11 '), the 3rd heat-exchange equipment (13,13 '), the 4th heat-exchange equipment (18,18 '), the 5th heat-exchange equipment (22) and the 6th heat-exchange equipment (34);
Recycle compressor comprises for the recycle compressor (24) with the circulation gas supercharging.
In the preferred embodiment of present device, described first paragraph methanator (9), second segment methanator (16), the 3rd section methanator (30) and the 4th section methanator (36) are insulation fix bed methanator.
Preferably, described device also comprises drum (44,44 '), is used to heat-exchange equipment that oiler feed is provided and accepts the saturation steam that heat-exchange equipment produces, and simultaneously saturation steam is delivered to heat-exchange equipment.Particularly, described drum (44,44 ') be used to the second heat-exchange equipment (11,11 ') or the 3rd heat-exchange equipment (13,13 ') that the first oiler feed (45 is provided, 45 '), be that the 4th heat-exchange equipment (18,18 ') provides the second oiler feed (47,47 '), and accept the second heat-exchange equipment (11,11 ') or the 3rd heat-exchange equipment (13,13 ') the first saturation steam (46,46 ') and the 4th heat-exchange equipment (18 that produce, 18 ') the second saturation steam (48 of producing, 48 '), simultaneously the 3rd saturation steam (49,49 ') is delivered to the 3rd heat-exchange equipment (13,13 ') or the second heat-exchange equipment (11,11 ').
Preferably, described heat-exchange equipment is selected from useless pot and vapor superheater.
Preferably, described device also comprises desulphurization reactor, is used for unstripped gas is carried out deep desulfuration.
Preferably, described device also comprises deoxidation reactor, is used for unstripped gas is carried out degree of depth deoxidation.
Preferably, described device also comprises gas-liquid separator, for separating of the water of condensation in the process gas.
The invention provides a kind of continuous processing flow process and device that contains the synthetic natural gas more than the methane 94mol% take coal or gasifying biomass product as raw material production.Technical process provided by the invention is as follows: unstripped gas is divided into four strands after preheating, wherein first strand of unstripped gas with enter the first paragraph methanator after steam, first strand of circulation gas mix and react; Second strand of unstripped gas with enter the second segment methanator after first paragraph gas product, steam, second strand of circulation gas mix and react, the second segment gas product is divided into two strands, enter the first paragraph methanator after the first stock-traders' know-how recycle compressor supercharging, enter the 3rd section methanator after second strand of second segment gas product and the 3rd strand of unstripped gas, the vapor mixing and react; Enter the 4th section methanator after the 3rd section gas product and the 4th strand of unstripped gas, the vapor mixing and react, the 4th section gas product obtains gas product after gas-liquid separation.
Contain independent steam system in the technique of the present invention, steam is mixed into corresponding methanator with unstripped gas respectively, can control preferably the reactor outlet temperature; but the flow modulation of this steam mixes with unstripped gas on the one hand, reduces CO content in the unstripped gas; the control temperature of reaction; but Optimization Technology reduces circulating flow rate on the other hand, reduces system energy consumption; improve energy utilization efficiency; also can be under the condition of unstripped gas fluctuation, control temperature of reaction, guard catalyst.Steam at least a portion derives from the steam of heat-exchange equipment by-product.
Contain the production of steam system of utilizing methanation reaction heat in the technique of the present invention, can produce according to actual needs saturation steam and the superheated vapour of different grades.Oiler feed enters drum, and drum is that heat-exchange equipment is carried oiler feed and collected the saturation steam that heat-exchange equipment produces by riser by downtake, and saturation steam is delivered to heat-exchange equipment heats up and obtain superheated vapour.
If still contain a small amount of carbon monoxide and carbonic acid gas in the gas product of the present invention, the further reaction of gas can be obtained the finished product.
Compared with prior art, the present invention has realized coal or the gasifying biomass product synthetic gas full methanation after purifying is come the production synthetic natural gas, and it is reasonable to have a technical process, possesses operability; Capacity usage ratio is high, save energy, advantages of environment protection.
Description of drawings
Below, describe by reference to the accompanying drawings embodiment of the present invention in detail, wherein:
Fig. 1 is the process flow sheet that the present invention produces a kind of embodiment of synthesis of natural gas method;
Fig. 2 is the process flow sheet that the present invention produces the another embodiment of synthesis of natural gas method;
Fig. 3 is low temperature methanation process schema in the tradition, is used for comparing with production synthesis of natural gas method provided by the invention.
Embodiment
Below in conjunction with embodiment the present invention is further described in detail, the embodiment that provides is only in order to illustrate the present invention, rather than in order to limit the scope of the invention.
Present embodiment is a kind of preferred implementation of the production method of synthetic natural gas provided by the invention, and the process flow sheet of present embodiment as shown in Figure 1.
A) coal or biomass are met the unstripped gas of requirement through gasification unit, converter unit and clean unit.Unstripped gas 1 is warming up to unstripped gas 3 after obtaining heating up after 190 ~ 210 ℃ through the first heat-exchange equipment 2.Unstripped gas 3 after the intensification is divided into four bursts of logistics, that is: first strand of unstripped gas 4, second strand of unstripped gas 5, the 3rd strand of unstripped gas 6 and the 4th strand of unstripped gas 7.
B) first strand of unstripped gas 4 mixed with the first steam 39, first strand of circulation gas 27, obtain temperature and be the first gas mixture 8 of 290 ~ 310 ℃, it is passed into carry out methanation reaction in the first paragraph methanator 9, obtain temperature and be 640 ~ 660 ℃ first paragraph gas product 10.First paragraph gas product 10 is through the second heat-exchange equipment 11 and the cooling of the 3rd heat-exchange equipment 13, obtains temperature and be the first paragraph gas product 14 after 270 ~ 290 ℃ the cooling, simultaneously by-product saturation steam and superheated vapour.
C) the first paragraph gas product 14 after will lowering the temperature mixes with second strand of unstripped gas 5, the second steam 40, second strand of circulation gas 28, obtain temperature and be the second gas mixture 15 of 290 ~ 310 ℃, it is passed into carry out methanation reaction in the second segment methanator 16, obtain temperature and be 600 ~ 620 ℃ second segment gas product 17.Second segment gas product 17 is cooled to second segment gas product 19 after obtaining lowering the temperature after 270 ~ 290 ℃ through the 4th heat-exchange equipment 18.
D) the second segment gas product 19 after will lowering the temperature is divided into two strands: first strand of second segment gas product 20 and second strand of second segment gas product 21.First strand of second segment gas product 20 is cooled to first strand of second segment gas product 23 after obtaining lowering the temperature after 160 ~ 180 ℃ through the 5th heat-exchange equipment 22.First strand of second segment gas product 23 after the cooling enters recycle compressor 24 superchargings, obtains circulation gas 25, and the loop compression acc power is 1163kW.Circulation gas 25 heats up through the 5th heat-exchange equipment 22, obtains temperature and be the circulation gas 26 after 250 ~ 270 ℃ the intensification.Circulation gas 26 after heating up is divided into two strands, that is: first strand of circulation gas 27 and second strand of circulation gas 28.First strand of circulation gas 27 and second strand of circulation gas 28 enter respectively in first paragraph and the second segment methanator and react.
E) second strand of second segment gas product 21 mixes with the 3rd strand of unstripped gas 6 and the 3rd steam 41, obtain temperature and be 270 ~ 290 ℃ the 3rd gas mixture 29, it is sent in the 3rd section methanator 30 carry out methanation reaction, obtain temperature and be 470 ~ 490 ℃ the 3rd section gas product 31.The 3rd section gas product 31 through the first heat-exchange equipment 2 be cooled to 90 ~ 110 ℃ obtain cooling after the 3rd section gas product 32.
F) the 3rd section gas product 32 and the 4th strand of unstripped gas 7, the 4th steam 42 are mixed to get the 4th gas mixture 33 after the cooling.The 4th gas mixture 33 heated up through the 6th heat-exchange equipment 34 obtains the 4th gas mixture 35 after temperature is 240 ~ 260 ℃ intensification, it is sent in the 4th section methanator 36 carry out methanation reaction, obtains temperature and be 350 ~ 370 ℃ the 4th section gas product 37.
G) the 4th section gas product 37 be through 34 coolings of the 6th heat-exchange equipment, and obtaining temperature through gas-liquid separation again is 30 ~ 50 ℃ gas product 38(SNG).
Wherein, the technique of utilizing of methanation reaction heat release comprises: drum 44 is sent in the oiler feed 43 from the battery limit (BL) after preheating, enter respectively the second heat-exchange equipment 11 and the 4th heat-exchange equipment 18 production the first saturation steam 46 and the second saturation steams 48 from the first oiler feed 45 in the drum 44 and the second oiler feed 47 by downtake, the first saturation steam 46 and the second saturation steam 48 enter drum 44 through riser, the 3rd saturation steam 49 that drum 44 produces heats up through the 3rd heat-exchange equipment 13, and the superheated vapour 50 that obtains temperature and be 440 ~ 460 ℃ is sent the battery limit (BL).
Wherein, the volume ratio of first strand of unstripped gas 4, second strand of unstripped gas 5, the 3rd strand of unstripped gas 6 and the 4th strand of unstripped gas 7 is 1:1.22:0.11:0, the volume ratio of first strand of second segment gas product 20 and second strand of second segment gas product 21 is 0.9:1, and the volume ratio of first strand of circulation gas 27 and second strand of circulation gas 28 is 0.9:0.1.
Below by the gas composition parameter of each logistics in the table 1, a situation arises to have described intuitively the reality of each workshop section's methanation reaction in the technical process shown in Figure 1.
Table 1
The explanation of logistics numbering: 1 is unstripped gas; 8 is the first gas mixture; 10 is the first paragraph gas product; 15 is the second gas mixture; 17 is the second segment gas product; 29 is the 3rd gas mixture; 31 is the 3rd section gas product; 35 is the 4th gas mixture; 37 is the 4th section gas product; 23 are first strand of second segment gas product after the cooling; 38 is gas product SNG; 50 is superheated vapour.
Present embodiment is a kind of preferred implementation of the production method of synthetic natural gas provided by the invention, and the process flow sheet of present embodiment as shown in Figure 2.
A) coal or biomass are met the unstripped gas of requirement through gasification unit, converter unit and clean unit.Unstripped gas 1 is warming up to unstripped gas 3 after obtaining heating up after 170 ~ 190 ℃ through the first heat-exchange equipment 2.Unstripped gas 3 after the intensification is divided into four bursts of logistics, that is: first strand of unstripped gas 4, second strand of unstripped gas 5, the 3rd strand of unstripped gas 6 and the 4th strand of unstripped gas 7.
B) first strand of unstripped gas 4 mixed with the first steam 39, first strand of circulation gas 27, obtain temperature and be the first gas mixture 8 of 250 ~ 270 ℃, it is passed into carry out methanation reaction in the first paragraph methanator 9, obtain temperature and be 610 ~ 630 ℃ first paragraph gas product 10.First paragraph gas product 10 is through the second heat-exchange equipment 11 and the cooling of the 3rd heat-exchange equipment 13, obtains temperature and be the first paragraph gas product 14 after 280 ~ 300 ℃ the cooling, simultaneously by-product saturation steam and superheated vapour.
C) the first paragraph gas product 14 after will lowering the temperature mixes with second strand of unstripped gas 5, the second steam 40, second strand of circulation gas 28, obtain temperature and be the second gas mixture 15 of 280 ~ 300 ℃, it is passed into carry out methanation reaction in the second segment methanator 16, obtain temperature and be 610 ~ 630 ℃ second segment gas product 17.Second segment gas product 17 is cooled to second segment gas product 19 after obtaining lowering the temperature after 280 ~ 300 ℃ through the 4th heat-exchange equipment 18.
D) the second segment gas product 19 after will lowering the temperature is divided into two strands: first strand of second segment gas product 20 and second strand of second segment gas product 21.First strand of second segment gas product 20 is cooled to first strand of second segment gas product 23 after obtaining lowering the temperature after 150 ~ 170 ℃ through the 5th heat-exchange equipment 22.First strand of second segment gas product 23 after the cooling enters recycle compressor 24 superchargings, obtains circulation gas 25.Circulation gas 25 heats up through the 5th heat-exchange equipment 22, obtains temperature and be the circulation gas 26 after 230 ~ 250 ℃ the intensification.Circulation gas 26 after heating up is divided into two strands, that is: first strand of circulation gas 27 and second strand of circulation gas 28.First strand of circulation gas 27 and second strand of circulation gas 28 enter respectively in first paragraph and the second segment methanator and react.
E) second strand of second segment gas product 21 mixes with the 3rd strand of unstripped gas 6 and the 3rd steam 41, obtain temperature and be 280 ~ 300 ℃ the 3rd gas mixture 29, it is sent in the 3rd section methanator 30 carry out methanation reaction, obtain temperature and be 410 ~ 430 ℃ the 3rd section gas product 31.The 3rd section gas product 31 through the first heat-exchange equipment 2 be cooled to 100 ~ 120 ℃ obtain cooling after the 3rd section gas product 32.
F) the 3rd section gas product 32 and the 4th strand of unstripped gas 7, the 4th steam 42 are mixed to get the 4th gas mixture 33 after the cooling.The 4th gas mixture 33 heated up through the 6th heat-exchange equipment 34 obtains the 4th gas mixture 35 after temperature is 240 ~ 260 ℃ intensification, it is sent in the 4th section methanator 36 carry out methanation reaction, obtains temperature and be 290 ~ 310 ℃ the 4th section gas product 37.
G) the 4th section gas product 37 be through 34 coolings of the 6th heat-exchange equipment, and obtaining temperature through gas-liquid separation again is 30 ~ 50 ℃ gas product 38(SNG).
Wherein, the technique of utilizing of methanation reaction heat release comprises: from the oiler feed 43 of battery limit (BL) ' after preheating, send into drum 44 ', the first oiler feed 45 of drum 44 ' interior ' and the second oiler feed 47 ' by downtake enter respectively the 3rd heat-exchange equipment 13 ' and the 4th heat-exchange equipment 18 ' productions the first saturation steam 46 ' with the second saturation steam 48 ', the first saturation steam 46 ' and the second saturation steam 48 ' process riser enter drum 44 ', the 3rd saturation steam 49 that drum 44 produces ' through the second heat-exchange equipment 11 ' intensification obtains temperature and is 440 ~ 460 ℃ superheated vapour 50 ' send battery limit (BL).
Wherein, the volume ratio of first strand of unstripped gas 4, second strand of unstripped gas 5, the 3rd strand of unstripped gas 6 and the 4th strand of unstripped gas 7 is 1:1.27:0:0, the volume ratio of first strand of second segment gas product 20 and second strand of second segment gas product 21 is 2.4:1, and the volume ratio of first strand of circulation gas 27 and second strand of circulation gas 28 is 0.95:0.05.
Below by the gas composition parameter of each logistics in the table 2, a situation arises to have described intuitively the reality of each workshop section's methanation reaction in Fig. 2 technical process.
Table 2
The explanation of logistics numbering: 1 is unstripped gas; 8 is the first gas mixture; 10 is the first paragraph gas product; 15 is the second gas mixture; 17 is the second segment gas product; 29 is the 3rd gas mixture; 31 is the 3rd section gas product; 35 is the 4th gas mixture; 37 is the 4th section gas product; 23 are first strand of second segment gas product after the cooling; 38 is gas product SNG; 50 ' be superheated vapour.
Present embodiment is a kind of preferred implementation of the production method of synthetic natural gas provided by the invention, and the process flow sheet of present embodiment as shown in Figure 1.
A) coal or biomass are met the unstripped gas of requirement through gasification unit, converter unit and clean unit.Unstripped gas 1 is warming up to unstripped gas 3 after obtaining heating up after 200 ~ 220 ℃ through the first heat-exchange equipment 2.Unstripped gas 3 after the intensification is divided into four bursts of logistics, that is: first strand of unstripped gas 4, second strand of unstripped gas 5, the 3rd strand of unstripped gas 6 and the 4th strand of unstripped gas 7.
B) first strand of unstripped gas 4 mixed with the first steam 39, first strand of circulation gas 27, obtain temperature and be the first gas mixture 8 of 290 ~ 310, it is passed into carry out methanation reaction in the first paragraph methanator 9, obtain temperature and be 640 ~ 660 ℃ first paragraph gas product 10.First paragraph gas product 10 is through the second heat-exchange equipment 11 and the cooling of the 3rd heat-exchange equipment 13, obtains temperature and be the first paragraph gas product 14 after 300 ~ 320 ℃ the cooling, simultaneously by-product saturation steam and superheated vapour.
C) the first paragraph gas product 14 after will lowering the temperature mixes with second strand of unstripped gas 5, the second steam 40, second strand of circulation gas 28, obtain temperature and be the second gas mixture 15 of 290 ~ 310 ℃, it is passed into carry out methanation reaction in the second segment methanator 16, obtain temperature and be 600 ~ 620 ℃ second segment gas product 17.Second segment gas product 17 is cooled to second segment gas product 19 after obtaining lowering the temperature after 270 ~ 290 ℃ through the 4th heat-exchange equipment 18.
D) the second segment gas product 19 after will lowering the temperature is divided into two strands: first strand of second segment gas product 20 and second strand of second segment gas product 21.First strand of second segment gas product 20 is cooled to first strand of second segment gas product 23 after obtaining lowering the temperature after 150 ~ 170 ℃ through the 5th heat-exchange equipment 22.First strand of second segment gas product 23 after the cooling enters recycle compressor 24 superchargings, obtains circulation gas 25.Circulation gas 25 heats up through the 5th heat-exchange equipment 22, obtains temperature and be the circulation gas 26 after 250 ~ 270 ℃ the intensification.Circulation gas 26 after heating up is divided into two strands, that is: first strand of circulation gas 27 and second strand of circulation gas 28.First strand of circulation gas 27 and second strand of circulation gas 28 enter respectively in first paragraph and the second segment methanator and react.
E) second strand of second segment gas product 21 mixes with the 3rd strand of unstripped gas 6 and the 3rd steam 41, obtain temperature and be 280 ~ 300 ℃ the 3rd gas mixture 29, it is sent in the 3rd section methanator 30 carry out methanation reaction, obtain temperature and be 460 ~ 480 ℃ the 3rd section gas product 31.The 3rd section gas product 31 through the first heat-exchange equipment 2 be cooled to 80 ~ 100 ℃ obtain cooling after the 3rd section gas product 32.
F) the 3rd section gas product 32 and the 4th strand of unstripped gas 7, the 4th steam 42 are mixed to get the 4th gas mixture 33 after the cooling.The 4th gas mixture 33 heated up through the 6th heat-exchange equipment 34 obtains the 4th gas mixture 35 after temperature is 240 ~ 260 ℃ intensification, it is sent in the 4th section methanator 36 carry out methanation reaction, obtains temperature and be 380 ~ 400 ℃ the 4th section gas product 37.
G) the 4th section gas product 37 be through 34 coolings of the 6th heat-exchange equipment, and obtaining temperature through gas-liquid separation again is 30 ~ 50 ℃ gas product 38(SNG).
Wherein, the technique of utilizing of methanation reaction heat release comprises: drum 44 is sent in the oiler feed 43 from the battery limit (BL) after preheating, enter respectively the second heat-exchange equipment 11 and the 4th heat-exchange equipment 18 production the first saturation steam 46 and the second saturation steams 48 from the first oiler feed 45 in the drum 44 and the second oiler feed 47 by downtake, the first saturation steam 46 and the second saturation steam 48 enter drum 44 through riser, the 3rd saturation steam 49 that drum 44 produces heats up through the 3rd heat-exchange equipment 13, and the superheated vapour 50 that obtains temperature and be 440 ~ 460 ℃ is sent the battery limit (BL).
Wherein, the volume ratio of first strand of unstripped gas 4, second strand of unstripped gas 5, the 3rd strand of unstripped gas 6 and the 4th strand of unstripped gas 7 is 1:0.94:0.13:0.09, the volume ratio of first strand of second segment gas product 20 and second strand of second segment gas product 21 is 0.9:1, and the volume ratio of first strand of circulation gas 27 and second strand of circulation gas 28 is 1:0.
Below by the gas composition parameter of each logistics in the table 3, a situation arises to have described intuitively the reality of each workshop section's methanation reaction in Fig. 1 technical process.
Table 3
The explanation of logistics numbering is with table 1.
Comparative Examples 1
For comparing with embodiment 1, under identical design basis condition, adopt low temperature methanation technology production synthetic natural gas in the tradition, the concrete technology schema is as shown in Figure 3.
A) coal or biomass are met the unstripped gas of requirement through gasification unit, converter unit and clean unit.Unstripped gas 1 is warming up to unstripped gas 3 after obtaining heating up after 170 ~ 190 ℃ through the first heat-exchange equipment 2.Unstripped gas 3 after the intensification is divided into two bursts of logistics, that is: first strand of unstripped gas 4, second strand of unstripped gas 5.
B) first strand of unstripped gas 4 mixed with the first steam 39, first strand of circulation gas 27, obtain temperature and be the first gas mixture 8 of 270 ~ 290 ℃, it is passed into carry out methanation reaction in the first paragraph methanator 9, obtain temperature and be 490 ~ 510 ℃ first paragraph gas product 10.First paragraph gas product 10 is through the second heat-exchange equipment 11 ' and the 3rd heat-exchange equipment 13 ' cooling, obtains temperature and be the first paragraph gas product 14 after 300 ~ 320 ℃ the cooling, while by-product saturation steam and superheated vapour.
C) the first paragraph gas product 14 after will lowering the temperature mixes with second strand of unstripped gas 5, the second steam 40, second strand of circulation gas 28, obtain temperature and be the second gas mixture 15 of 270 ~ 290 ℃, it is passed into carry out methanation reaction in the second segment methanator 16, obtain temperature and be 490 ~ 510 ℃ second segment gas product 17.Second segment gas product 17 is cooled to second segment gas product 19 after obtaining lowering the temperature after 240 ~ 260 ℃ through the 4th heat-exchange equipment 18.
D) the second segment gas product 19 after will lowering the temperature is divided into two strands: first strand of second segment gas product 20 and second strand of second segment gas product 21.First strand of second segment gas product 20 is cooled to first strand of second segment gas product 23 after obtaining lowering the temperature after 30 ~ 50 ℃ through the 5th heat-exchange equipment 22.First strand of second segment gas product 23 after the cooling enters recycle compressor 24 superchargings, obtains circulation gas 25, and the loop compression acc power is 1651kW.Circulation gas 25 heats up through the 5th heat-exchange equipment 22, obtains temperature and be the circulation gas 26 after 210 ~ 230 ℃ the intensification.Circulation gas 26 after heating up is divided into two strands, that is: first strand of circulation gas 27 and second strand of circulation gas 28.First strand of circulation gas 27 and second strand of circulation gas 28 enter respectively in first paragraph and the second segment methanator and react.
E) second strand of second segment gas product 21 mixes with the 3rd steam 41, obtains temperature and be 240 ~ 260 ℃ the 3rd gas mixture 29, it sent in the 3rd section methanator 30 carry out methanation reaction, obtains temperature and be 300 ~ 320 ℃ the 3rd section gas product 31.The 3rd section gas product 31 is through 2 coolings of the first heat-exchange equipment and to obtain temperature through gas-liquid separation be 30 ~ 50 ℃ gas product 38 ' (SNG).
Wherein, the technique of utilizing of methanation reaction heat release comprises: from the oiler feed 43 of battery limit (BL) ' after preheating, send into drum 44 ', from the first oiler feed 45 of drum 44 ' interior ' and the second oiler feed 47 ' by downtake enter respectively the 3rd heat-exchange equipment 13 ' and the 4th heat-exchange equipment 18 ' productions the first saturation steam 46 ' with the second saturation steam 48 ', the first saturation steam 46 ' and the second saturation steam 48 ' process riser enter drum 44 ', the 3rd saturation steam 49 of drum 44 ' generation ' through the second heat-exchange equipment 11 ' intensification obtains temperature and is 440 ~ 460 ℃ superheated vapour 50 ' send battery limit (BL).
Wherein, the volume ratio of first strand of unstripped gas 4, second strand of unstripped gas 5 is 1:1.33, the volume ratio of first strand of second segment gas product 20 and second strand of second segment gas product 21 is 1:0.26, and the volume ratio of first strand of circulation gas 27 and second strand of circulation gas 28 is 0.95:0.05.
Below by the gas composition parameter of each logistics in the table 4, a situation arises to have described intuitively the reality of each workshop section's methanation reaction in the technical process shown in Figure 3.
Table 4
Compare with Comparative Examples 1, under identical design basis, embodiment 1 heat utilization ratio is high, consumption is low: embodiment 1 loop compression acc power is 1163kW, and Comparative Examples 1 is 1651kW, and the energy consumption of embodiment 1 is than Comparative Examples 1 low 29.7%; Embodiment 1 by-product superheated vapour 252.3t/h, Comparative Examples 1 by-product superheated vapour 234.7t/h, the heat utilization ratio of embodiment 1 is higher by 7.5% than Comparative Examples 1.
Claims (10)
1. method of producing synthetic natural gas said method comprising the steps of:
A) unstripped gas (1) 1:(0.5 ~ 5 by volume after the first heat-exchange equipment (2) is warming up to 150 ~ 400 ℃): (0 ~ 0.5): (0 ~ 0.5) is divided into first strand of unstripped gas (4), second strand of unstripped gas (5), the 3rd strand of unstripped gas (6) and the 4th strand of unstripped gas (7);
B) the first strand of unstripped gas (4) in the step a) and the first steam (39) and first strand of circulation gas (27) being mixed to get temperature is the first gas mixture (8) of 250 ~ 400 ℃, the first gas mixture (8) passed in the first paragraph methanator (9) react, obtain temperature and be 450 ~ 750 ℃ first paragraph gas product (10), this first paragraph gas product is through (10) second heat-exchange equipments (11,11 ') and the 3rd heat-exchange equipment (13,13 ') be cooled to 250 ~ 400 ℃ of first paragraph gas products (14) after obtaining lowering the temperature;
C) it is the second gas mixture (15) of 250 ~ 400 ℃ that the first paragraph gas product (14) after the cooling that step b) is obtained and described second strand of unstripped gas (5), the second steam (40), second strand of circulation gas (28) are mixed to get temperature, the second gas mixture (15) passed in the second segment methanator (16) react, obtain temperature and be 450 ~ 700 ℃ second segment gas product (17), this second segment gas product (17) is cooled to 200 ~ 400 ℃ of second segment gas products (19) after the cooling that obtains through the 4th heat-exchange equipment (18,18 ');
D) the second segment gas product (19) after the cooling that step c) is obtained is (0.3 ~ 5) by volume: 1 is divided into circulation gas (20) and second strand of second segment gas product (21), described circulation gas (20) is cooled to the circulation gas (25) of sending into after 100 ~ 350 ℃ after recycle compressor (24) supercharging obtains supercharging through the 5th heat-exchange equipment (22), circulation gas after the supercharging (25) is warmed up to 200 ~ 350 ℃ through the 5th heat-exchange equipment (22), and then with its by volume (0.5 ~ 1): (0 ~ 0.5) is divided into described first strand of circulation gas (27) and second strand of circulation gas (28);
E) it is 200 ~ 400 ℃ the 3rd gas mixture (29) that the second strand of second segment gas product (21) that step d) is obtained and described the 3rd strand of unstripped gas (6), the 3rd steam (41) are mixed to get temperature, the 3rd gas mixture (29) passed in the 3rd section methanator (30) react, obtain temperature and be 300 ~ 550 ℃ the 3rd section gas product (31), the three section gas product (32) of the 3rd section gas product (31) after the first heat-exchange equipment (2) is cooled to 60 ~ 350 ℃ of coolings that obtain;
F) it is 60 ~ 200 ℃ the 4th gas mixture (33) that the 3rd section gas product (32) after the cooling that step e) is obtained and described the 4th strand of unstripped gas (7), the 4th steam (42) are mixed to get temperature, described the 4th gas mixture (33) passes in the 4th section methanator (36) after the 6th heat-exchange equipment (34) is warming up to 200 ~ 350 ℃ and reacts, and obtains temperature and be 250 ~ 450 ℃ the 4th section gas product (37);
G) the 4th section gas product (37) that step f) is obtained gone forward side by side through the 6th heat-exchange equipment (34) cooling, and to obtain temperature after promoting the circulation of qi liquid separates be 20 ~ 80 ℃ gas product (38).
2. method according to claim 1, wherein, the molar percentage of described unstripped gas is composed as follows: carbon monoxide 5 ~ 50%, carbonic acid gas 0 ~ 30%, hydrogen 20 ~ 80%, methane 0 ~ 20%.
3. method according to claim 1 and 2, in described step a), the volume ratio of first strand of unstripped gas (4), second strand of unstripped gas (5), the 3rd strand of unstripped gas (6) and the 4th strand of unstripped gas (7) that described unstripped gas (1) is divided into is 1:(0.5 ~ 2): (0 ~ 0.3): (0 ~ 0.3).
4. each described method in 3 according to claim 1, in described step d), the circulation gas (20) that described second segment gas product (19) is divided into and the volume ratio of second strand of second segment gas product (21) are (0.3 ~ 3): 1.
5. each described method in 4 according to claim 1, in described step d), first strand of circulation gas (27) that described circulation gas (20) is divided into and the volume ratio of second strand of circulation gas (28) are (0.7 ~ 1): (0 ~ 0.3).
6. each described method in 5 according to claim 1, described method also comprises utilizes the methanation reaction heat release in the following manner: make the oiler feed (43 from the battery limit (BL), 43 ') enter drum (44,44 '), make from drum (44,44 ') the first oiler feed (45,45 ') enter the second heat-exchange equipment (11,11 ') or the 3rd heat-exchange equipment (13,13 ') produce the first saturation steam (46,46 ') of 3 ~ 10MPa, make from drum (44,44 ') the second oiler feed (47,47 ') enter the second saturation steam (48 that the 4th heat-exchange equipment (18,18 ') produces 3 ~ 10MPa, 48 '), from the 3rd saturation steam (49,49 ') of drum (44,44 ') through the 3rd heat-exchange equipment (13,13 ') or the second heat-exchange equipment (11,11 ') heat up, obtain temperature and be 300 ~ 550 ℃ superheated vapour (50,50 ').
7. be used for the device of each described method of claim 1 to 6, it comprises:
Methanator comprises be used to the first paragraph methanator (9) that carries out methanation reaction, second segment methanator (16), the 3rd section methanator (30) and the 4th section methanator (36);
Heat-exchange equipment, comprise the first heat-exchange equipment (2), the second heat-exchange equipment (11 for heating and/or cooling gas, 11 '), the 3rd heat-exchange equipment (13,13 '), the 4th heat-exchange equipment (18,18 '), the 5th heat-exchange equipment (22) and the 6th heat-exchange equipment (34);
Recycle compressor comprises for the recycle compressor (24) with the circulation gas supercharging.
8. device according to claim 7, wherein, described first paragraph methanator (9), second segment methanator (16), the 3rd section methanator (30) and the 4th section methanator (36) are insulation fix bed methanator.
9. according to claim 7 or the device described in 8, wherein, described device also comprises drum (44,44 '), is used to heat-exchange equipment that oiler feed is provided and accepts the saturation steam that heat-exchange equipment produces, and simultaneously saturation steam is delivered to heat-exchange equipment.
10. each described device in 9 according to claim 7, wherein, described heat-exchange equipment is selected from useless pot and vapor superheater;
Preferably, described device also comprises desulphurization reactor, is used for unstripped gas is carried out deep desulfuration;
Preferably, described device also comprises deoxidation reactor, is used for unstripped gas is carried out degree of depth deoxidation;
Preferably, described device also comprises gas-liquid separator, for separating of the water of condensation in the process gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210380047.6A CN102876411B (en) | 2012-10-09 | 2012-10-09 | Method and device for producing synthetic natural gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210380047.6A CN102876411B (en) | 2012-10-09 | 2012-10-09 | Method and device for producing synthetic natural gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102876411A true CN102876411A (en) | 2013-01-16 |
| CN102876411B CN102876411B (en) | 2014-01-29 |
Family
ID=47477935
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210380047.6A Active CN102876411B (en) | 2012-10-09 | 2012-10-09 | Method and device for producing synthetic natural gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102876411B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103695058A (en) * | 2013-12-19 | 2014-04-02 | 中国海洋石油总公司 | Novel methanation reaction process for preparing synthetic natural gas |
| CN104388139A (en) * | 2014-11-11 | 2015-03-04 | 上海鑫兴化工科技有限公司 | Direct methanation method and system for raw coal gas |
| CN104845689A (en) * | 2014-02-18 | 2015-08-19 | 中国石油化工股份有限公司 | Technology for preparing synthetic natural gas through methanation of coal-based synthetic gas |
| CN105368514A (en) * | 2014-08-26 | 2016-03-02 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas |
| CN105441150A (en) * | 2014-08-26 | 2016-03-30 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas |
| CN106147899A (en) * | 2015-03-27 | 2016-11-23 | 大唐国际化工技术研究院有限公司 | A kind of method and device producing substitute natural gas |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101812339A (en) * | 2010-04-15 | 2010-08-25 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas, and natural gas product thereof |
| CN101880559A (en) * | 2010-06-18 | 2010-11-10 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas |
-
2012
- 2012-10-09 CN CN201210380047.6A patent/CN102876411B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101812339A (en) * | 2010-04-15 | 2010-08-25 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas, and natural gas product thereof |
| CN101880559A (en) * | 2010-06-18 | 2010-11-10 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103695058A (en) * | 2013-12-19 | 2014-04-02 | 中国海洋石油总公司 | Novel methanation reaction process for preparing synthetic natural gas |
| CN103695058B (en) * | 2013-12-19 | 2015-05-20 | 中国海洋石油总公司 | Novel methanation reaction process for preparing synthetic natural gas |
| CN104845689A (en) * | 2014-02-18 | 2015-08-19 | 中国石油化工股份有限公司 | Technology for preparing synthetic natural gas through methanation of coal-based synthetic gas |
| CN105368514A (en) * | 2014-08-26 | 2016-03-02 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas |
| CN105441150A (en) * | 2014-08-26 | 2016-03-30 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas |
| CN105441150B (en) * | 2014-08-26 | 2018-06-26 | 大唐国际化工技术研究院有限公司 | A kind of method and device for producing synthetic natural gas |
| CN105368514B (en) * | 2014-08-26 | 2018-12-21 | 大唐国际化工技术研究院有限公司 | Produce the method and device of synthetic natural gas |
| CN104388139A (en) * | 2014-11-11 | 2015-03-04 | 上海鑫兴化工科技有限公司 | Direct methanation method and system for raw coal gas |
| CN106147899A (en) * | 2015-03-27 | 2016-11-23 | 大唐国际化工技术研究院有限公司 | A kind of method and device producing substitute natural gas |
| CN106147899B (en) * | 2015-03-27 | 2019-03-26 | 大唐国际化工技术研究院有限公司 | A kind of method and device producing substitute natural gas |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102876411B (en) | 2014-01-29 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102899112B (en) | Method and device for producing synthetic natural gas | |
| CN102585951B (en) | Process for co-production of liquefied synthesis gas, pure hydrogen and methanol from coke-oven gas | |
| CN102876411B (en) | Method and device for producing synthetic natural gas | |
| CN101508922B (en) | Methanation reaction process using oven gas to prepare substitute natural gas | |
| CN101649233B (en) | Isothermal methanation process and device for the preparation of synthetic natural gas | |
| CN100526273C (en) | Method for integral production of liquid ammonia and methanol and/or dimethyl ether by using coke oven gas as raw material | |
| CN102517108A (en) | Technology for preparing liquefied natural gas and liquid ammonia by using coke oven gas | |
| CN103695058B (en) | Novel methanation reaction process for preparing synthetic natural gas | |
| CN104152201B (en) | Coal syngas circulation gas free methanation technology | |
| CN101508924A (en) | Catalysis deoxidization process for coal bed gas of coal mine zone | |
| CN205035336U (en) | Resistant sulphur transform process systems of high concentration CO part | |
| CN103409187A (en) | Methanation technology for preparing non-recycling gas of SNG or LNG from coke-oven gas | |
| CN101775319A (en) | Method for producing synthetic natural gas SNG from coal and processing installation thereof | |
| CN101851537B (en) | Method and device for preparing synthetic natural gas | |
| CN103242921A (en) | Technology for preparing natural gas from synthetic gas | |
| CN101003359A (en) | Method for preparing methanol synthesis gas by using coke oven gas to make hydrogen, and complementing carbon from water gas | |
| CN103449365A (en) | High-concentration CO sulfur tolerant shift process and device thereof | |
| CN103013598B (en) | Method and device for producing synthesized natural gas | |
| CN102746870B (en) | FT synthesis technology | |
| CN104119972A (en) | Multifunctional sulfur-resistant methanation transformation process adapting to coal gas | |
| CN202297421U (en) | Device for producing ethylene glycol by using metallurgical tail gas | |
| CN105255532A (en) | Fluidized bed and fixed bed combined methanation method | |
| CN103421561A (en) | Synthesis gas methanation reaction method | |
| CN103540376B (en) | Synthetic gas methanation substitutes the method for Sweet natural gas | |
| CN105368514B (en) | Produce the method and device of synthetic natural gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: SINOPEC LUOYANG PETROCHEMICAL ENGINEERING CORPORAT Effective date: 20140305 |
|
| CB03 | Change of inventor or designer information | ||
| CB03 | Change of inventor or designer information |
Inventor after: Li Anxue Inventor after: Kong Fangui Inventor after: Liu Xuewu Inventor after: Liu Jianan Inventor after: Xie Lunhong Inventor after: Wang Mingchuo Inventor after: Su Ping Inventor after: Li Wangzhang Inventor after: Li Shuqing Inventor after: Li Chunqi Inventor after: Zuo Yubang Inventor after: Yu Mingcheng Inventor after: Ding Wanyou Inventor after: Liu Junfeng Inventor after: Liu Yongjian Inventor before: Li Anxue Inventor before: Liu Jianan Inventor before: Xie Lunhong Inventor before: Wang Mingchuo Inventor before: Su Ping Inventor before: Li Chunqi Inventor before: Zuo Yubang Inventor before: Yu Mingcheng Inventor before: Ding Wanyou Inventor before: Liu Junfeng Inventor before: Liu Yongjian Inventor before: Kong Fangui Inventor before: Liu Xuewu |
|
| COR | Change of bibliographic data |
Free format text: CORRECT: INVENTOR; FROM: LI ANXUE LI CHUNQI ZUO YUBANG YU MINGCHENG DING WANYOU LIU JUNFENG LIU YONGJIAN KONG FANGUI LIU XUEWU LIU JIANAN XIE LUNHONG WANG MINGQUAN SU PING TO: LI ANXUE LI WANGZHANG LI SHUQING LI CHUNQI ZUO YUBANG YU MINGCHENG DING WANYOU LIU JUNFENG LIU YONGJIAN KONG FANGUI LIU XUEWU LIU JIANAN XIE LUNHONG WANG MINGQUAN SU PING |
|
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20140305 Address after: 100070, No. 20, No. 12, No. 188, South Fourth Ring Road, Fengtai District, Beijing Patentee after: Datang International Chemical Technology Institute Co., Ltd. Patentee after: Luoyang Petrochemical Engineering Corporation /SINOPEC Address before: 100070, No. 20, No. 12, No. 188, South Fourth Ring Road, Fengtai District, Beijing Patentee before: Datang International Chemical Technology Institute Co., Ltd. |