CN203620609U - Special device for manufacturing natural gas hydrate - Google Patents
Special device for manufacturing natural gas hydrate Download PDFInfo
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- CN203620609U CN203620609U CN201320709047.6U CN201320709047U CN203620609U CN 203620609 U CN203620609 U CN 203620609U CN 201320709047 U CN201320709047 U CN 201320709047U CN 203620609 U CN203620609 U CN 203620609U
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- reactor
- hydrate
- storage tank
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- reaction
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- 238000004519 manufacturing process Methods 0.000 title claims abstract description 14
- NMJORVOYSJLJGU-UHFFFAOYSA-N methane clathrate Chemical compound C.C.C.C.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O NMJORVOYSJLJGU-UHFFFAOYSA-N 0.000 title abstract 2
- 238000006243 chemical reaction Methods 0.000 claims abstract description 45
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 45
- 238000000034 method Methods 0.000 claims abstract description 27
- 238000012432 intermediate storage Methods 0.000 claims abstract description 15
- 238000003860 storage Methods 0.000 claims abstract description 10
- 230000001105 regulatory effect Effects 0.000 claims abstract description 8
- 230000005587 bubbling Effects 0.000 claims description 22
- 230000015572 biosynthetic process Effects 0.000 claims description 12
- 150000004677 hydrates Chemical class 0.000 claims description 10
- 238000005057 refrigeration Methods 0.000 claims description 9
- 239000000654 additive Substances 0.000 claims description 7
- 230000000996 additive effect Effects 0.000 claims description 6
- 230000002411 adverse Effects 0.000 claims description 3
- 230000008859 change Effects 0.000 claims description 3
- 239000007789 gas Substances 0.000 abstract description 23
- 230000008569 process Effects 0.000 abstract description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 6
- 239000007788 liquid Substances 0.000 abstract description 6
- 239000007787 solid Substances 0.000 abstract description 6
- 238000000926 separation method Methods 0.000 abstract description 5
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 3
- 239000002245 particle Substances 0.000 abstract description 2
- 238000001816 cooling Methods 0.000 abstract 1
- 239000013078 crystal Substances 0.000 abstract 1
- 239000011541 reaction mixture Substances 0.000 abstract 1
- 238000005755 formation reaction Methods 0.000 description 9
- 239000002002 slurry Substances 0.000 description 8
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 3
- 230000007246 mechanism Effects 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000003507 refrigerant Substances 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 238000005469 granulation Methods 0.000 description 1
- 230000003179 granulation Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000005204 segregation Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 238000002834 transmittance Methods 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a special device for manufacturing natural gas hydrate. The device sequentially comprises a process conversion control unit, a multi-section bubble tower type reactor, an intermediate storage tank, a water tank, a refrigerating unit, a cold storage unit, a separator, a central control system and the like. The multi-section bubble tower type reactor consists of three sections, wherein the lower section is a reaction section formed by a tube nest and an outer barrel; gas and water flow and react in the tube; cooling capacity is provided at a shell side to form cold trap removing reaction heat in the reaction tube; the middle section is a reaction mixture staying area; the upper section is a gas top used for regulating pressure in the reactor. The refrigerating unit is provided with four loops which are respectively communicated with the reactor, the intermediate storage tank, the water tank and the cold storage unit. The reactor is equipped with a crystal modulator, and used for regulating hydrate residence time with the process conversion control unit. Hydrate obtained by separating is frozen by liquid nitrogen and pelletized to obtain hydrate solid particles. The device disclosed by the utility model is integrated with functions such as hydrate reaction, separation, hydrate morphology, residence time regulation and the like.
Description
Technical field:
The utility model relates to a kind of gas hydrates manufacturing installation, belongs to natural gas storaging and transport technology field, is specifically related to devices continuous, stable, high efficiency manufacture gas hydrates.
Background technology:
Existing gas hydrates manufacturing installation, is all difficult to continue, stably produce hydrate, and production efficiency of equipment is low, and the Multiphase Flow of the gas-water-hydrate formation in gas hydrates generative process, heat transfer, mass transfer problem are difficult to solve.Art methods adopts large water gaging to circulate in system mostly, to remove reaction heat.A large amount of unreacted water circulates in system, certainly will increase energy consumption, causes cost to increase.More disadvantageously, air-water mol ratio is excessive, makes mass transport process significantly slack-off, and has to adopt larger reactant mixture volume.In order to improve formation speed and to improve gas one liquid and contact effect, must adopt the method such as stir, ultrasonic, cause equipment complexity, production cost to increase, can not produce economically gas hydrates with commercial scale.Also there are some patented technologies to remove reaction heat by supplementing a large amount of liquid nitrogen, cause production cost significantly to rise, be difficult to carry out.In addition, how to solve Leakage Gas problem and derivative safety problem also becomes a bottleneck fundamentally.On the other hand, prior art is difficult to realize the matching and optimization of caloic transmittance process.
Summary of the invention:
The functions such as hydrate reaction, separation, hydrate pattern and the adjusting of the system time of staying that this device is integrated, are applicable to the situation of multiple treating capacity.
Be exclusively used in a device of manufacturing gas hydrates, it is characterized in that: comprise successively technique change control module 1, choke valve 2, multistage bubbling reactor 3, inlet valve 4, drain valve 5, Chu Leng unit 6, delivery pump 7, refrigeration unit 8, intermediate storage tank 9, additive storage tank 10, water pot 11, seperator 12, central control system 13;
A) multistage bubbling column reactor is connected to the formation loop, two ends of technique conversion control module; Technique conversion control module connects transmitter 23 by delivery pump 21, and transmitter 23 connects 4 control valves formations that logic controller 22 is controlled; Realization stream and adverse current production process hocket.
B) multistage bubbling column reactor, be designated hereinafter simply as reactor, form by three sections, hypomere is the conversion zone being formed by reaction tube 34 and shell-side 35, gas, water are in the interior mobile and reaction of reaction tube 34, and shell-side 35 provides cold to remove reaction heat at the interior formation cold-trap of reaction tube 34; Stage casing is collection of products district 33; Epimere between gas vent 31 and dividing plate 32 forms pneumatic jack to regulate the pressure in reactor; Chilled water outlet 40 and the chilled water inlet 41 of multistage bubbling column reactor is connected to the formation loop, two ends of refrigeration unit; Gas vent 31 is provided with choke valve 2; Reactor lower part is provided with inlet tube 37 and is connected with gas source, and inlet tube 38 is connected with conveying 7; Reactor hypomere is provided with air distributor 36;
C) refrigeration unit is provided with four loops: a road is communicated with multistage bubbling column reactor, and a road is communicated with intermediate storage tank, and a road is communicated with water pot, and a Yu Chuleng unit, road is communicated with;
D) storing up cold unit volume is 2～10 with the ratio of reactor effective volume, to required cold-storage ability is provided;
E) multistage bubbling column reactor is connected to the formation loop, two ends of adjusting brilliant device 32, and hydrate pattern is regulated, and jointly the hydrate time of staying is regulated with technique conversion control module, improves air content;
F) multistage bubbling column reactor forms water-flow circuit through drain valve 5, intermediate storage tank 9, seperator 12, water pot 11 and delivery pump; Additive storage tank is connected on water pot 11;
G) central control system control technique converter unit 1, multistage bubbling reactor 3, Chu Leng unit 6, intermediate storage tank 9, delivery pump 7 and each valve.
The necessary condition that the utility model forms based on gas hydrates and current technological difficulties analysis, the structure of reactor suitable by design proposed, high efficient heat exchanging mechanism is set directly mends the cold tubulose cold-trap that forms in reactor, in significantly reducing air-water mol ratio, can remove in time reaction heat; Specially designed multistage bubbling column reactor is made up of feed zone, conversion zone and segregation section, make reaction system form area large, upgrade fast gas-water interface, promote that hydrate continues, stable generation, reach the initial gross separation of hydrate slurry and water, gas simultaneously; Storing up cold unit volume is 2～10 with the ratio of reactor volume, is preferably 3～8, to required cold-storage ability is provided, realizes continuously, stablizes and efficiently preparation.
This device is provided with technique conversion control module and adjusts brilliant device, and hydrate pattern and the heterogeneous system time of staying are regulated, and improves hydrate air content.Water/slurry mixed system is separated by seperator.The complete natural gas Returning reactor of isolated water and unreacted, realizes circulation, guarantees making full use of of cold; The hydrate obtaining after separation obtains hydrate solids particle through the granulation of liquid nitrogen snap frozen.Central control system is implemented centralized Control to each technique unit.
The utlity model has following advantage:
1. air-flow forms fine bubble through distributor, has not only strengthened gas-liquid contact area, and in uphill process, makes gas-water interface constantly update, and has strengthened the disturbance of system, has strengthened mass transfer, the diabatic process of reaction;
2. proposed originally to manufacture hydrate adverse current and and flow blocked operation, realize the quick generation of hydrate;
3. technique conversion control module has been realized adjusting and the technique map function of the heterogeneous system time of staying;
4. high efficient heat exchanging mechanism and Chu Leng unit are set, and rapid moving, except reaction heat, promotes hydrate to generate fast in cold-trap, has significantly improved efficiency;
5. reactor is provided with and adjusts brilliant device, can carry out meticulous control to the heterogeneous system time of staying and hydrate pattern, improves hydrate air content.
Accompanying drawing explanation
Fig. 1, gas hydrates preparation facilities figure
In figure: 1-technique change control module; 2-choke valve; 3-multistage bubbling reactor; 4-inlet valve; 5-drain valve; 6-Chu Leng unit; 7-delivery pump; 8-refrigeration unit; 9-intermediate storage tank; 10-additive storage tank; 11-water pot; 12-seperator; 13-central control system.
Fig. 2, technique conversion control module figure
In figure: 21-delivery pump; 22-logic controller; 23-transmitter; 24,25,26,27-control valve; 3-reactor
Fig. 3, reactor profilograph
In figure: 31-gas vent; 32-dividing plate; 33-collection of products district; 34-reaction tube; 35-shell side; 36-air-flow distributor; 37-gas inlet; 38-cold water inlet; 39-slurry outlet; 40-chilled water outlet; 41-chilled water inlet; 42-adjusts brilliant device; The outlet of 43-hydrate; 44-water out.
The specific embodiment:
Start Chu Leng unit 6 and refrigeration unit 8, to the heat exchange mechanisms supply chilled water of establishing in water pot 11, intermediate storage tank 9, the temperature of 3 li of whole multistage bubbling reactors is controlled to 5 ℃; Restart water pump 7 and central control system 13, the water of being furnished with additive is pumped in the reaction member of reactor.When reactor head water level exceedes dividing plate, after reaching appointment liquid level, open the drain valve 5 of bypass pipe outlet, the discharge capacity of the open degree of control valve and delivery pump 7, makes water form stable water circulation through drain valve 5, intermediate storage tank 9, seperator 12 and water pot 11; After this tube side that enters multistage bubbling reactor 3 after natural gas via flow control valve and nozzle, pressure stability is 5MPa; Start Chu Leng unit 6 and refrigeration unit 8 and remove reaction heat to the shell side supply refrigerant of reactor 3 thereafter; Air-water mixture, in the tube side of multistage bubbling reactor 3, flows from bottom to top and water generation reaction compound occurs, and reaction Heat of Formation is removed by the refrigerant in shell side in time by partition heat exchange.After reaction a period of time, start technique conversion control module 1, make the interior current direction current downflow of reactor 3, form gas-water circulated in countercurrent, to regulate the time of staying of heterogeneous system.Thus gas-water will be continuously, stable, promptly generate hydrate, form slurry.Slurry arrives after upper area, fluidization under the violent bubbling effect of gas, and further reaction, also can generating portion hydrate.The gas not reacted, is gathered in the top of reactor, forms back pressure; Back pressure regulates by choke valve and the safety valve of reactor head, to guarantee that the pressure in reactor meets the formation condition of hydrate.This device is provided with technique conversion control module 1 and adjusts brilliant device 32, and hydrate pattern and the heterogeneous system time of staying are regulated, and improves hydrate air content.From reactor head gas out, can continue reaction to Returning reactor after 6MPa by compressor boost.The hydrate slurry that is gathered in reactor 3 tops, enters intermediate storage tank 9 through drain valve 5.After the hydrate slurry on intermediate storage tank 9 tops concentrates automatically, with the extraction of hydrate slurry form or enter seperator 12 and carry out liquid-solid separation, obtain the hydrate solids of " do ", stored refrigerated after packing.The isolated water of seperator 12 enters water pot 11, after mixing, loops back reactor 3 by delivery pump 7 with supplementary fresh water, additive, realizes Matter Transfer, simultaneously recovery section cold.The powdery solid hydrate that recovery obtains, can further be processed into fine and close blocks of solid.
Claims (1)
1. be exclusively used in a device of manufacturing gas hydrates, it is characterized in that: comprise successively technique change control module, choke valve, multistage bubbling reactor, inlet valve, drain valve, Chu Leng unit, delivery pump, refrigeration unit, intermediate storage tank, additive storage tank, water pot, seperator, central control system;
A) multistage bubbling column reactor is connected to the formation loop, two ends of technique conversion control module; Technique conversion control module connects transmitter by delivery pump, and 4 control valves that transmitter connects logic controller control form; Realization stream and adverse current production process hocket;
B) multistage bubbling column reactor, is designated hereinafter simply as reactor, forms by three sections, and hypomere is the conversion zone being formed by reaction tube and shell-side, and gas, water flow and reaction in reaction tube, and shell-side provides cold in reaction tube, to form cold-trap and removes reaction heat; Stage casing is collection of products district; Epimere between gas vent and dividing plate forms pneumatic jack to regulate the pressure in reactor; The chilled water outlet of multistage bubbling column reactor and chilled water inlet are connected to the formation loop, two ends of refrigeration unit; Gas vent is provided with choke valve; Reactor lower part is provided with inlet tube and is connected with gas source, and inlet tube is connected with delivery pump; Reactor hypomere is provided with air distributor;
C) refrigeration unit is provided with four loops: a road is communicated with multistage bubbling column reactor, and a road is communicated with intermediate storage tank, and a road is communicated with water pot, and a Yu Chuleng unit, road is communicated with;
D) storing up cold unit volume is 2～10 with the ratio of reactor effective volume, to required cold-storage ability is provided;
E) multistage bubbling column reactor is connected to the formation loop, two ends of adjusting brilliant device, and hydrate pattern is regulated, and jointly the hydrate time of staying is regulated with technique conversion control module, improves air content;
F) multistage bubbling column reactor forms water-flow circuit through drain valve, intermediate storage tank, seperator, water pot and delivery pump; Additive storage tank is connected on water pot;
G) central control system control technique converter unit, multistage bubbling reactor, Chu Leng unit, intermediate storage tank, delivery pump and each valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320709047.6U CN203620609U (en) | 2013-11-12 | 2013-11-12 | Special device for manufacturing natural gas hydrate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320709047.6U CN203620609U (en) | 2013-11-12 | 2013-11-12 | Special device for manufacturing natural gas hydrate |
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| Publication Number | Publication Date |
|---|---|
| CN203620609U true CN203620609U (en) | 2014-06-04 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201320709047.6U Expired - Lifetime CN203620609U (en) | 2013-11-12 | 2013-11-12 | Special device for manufacturing natural gas hydrate |
Country Status (1)
| Country | Link |
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| CN (1) | CN203620609U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2017088753A1 (en) * | 2015-11-24 | 2017-06-01 | 北京化工大学 | Method for preparing coalbed methane hydrate |
| CN116928583A (en) * | 2023-07-19 | 2023-10-24 | 大连理工大学 | Energy curing loading and unloading system and method |
-
2013
- 2013-11-12 CN CN201320709047.6U patent/CN203620609U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2017088753A1 (en) * | 2015-11-24 | 2017-06-01 | 北京化工大学 | Method for preparing coalbed methane hydrate |
| CN116928583A (en) * | 2023-07-19 | 2023-10-24 | 大连理工大学 | Energy curing loading and unloading system and method |
| CN116928583B (en) * | 2023-07-19 | 2023-12-01 | 大连理工大学 | Energy curing loading and unloading system and method |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20140604 |
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| CX01 | Expiry of patent term |