CN1158949A - Light hydrocarbon gasifying and gas-mixing system and technology - Google Patents
Light hydrocarbon gasifying and gas-mixing system and technology Download PDFInfo
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- CN1158949A CN1158949A CN 96117181 CN96117181A CN1158949A CN 1158949 A CN1158949 A CN 1158949A CN 96117181 CN96117181 CN 96117181 CN 96117181 A CN96117181 A CN 96117181A CN 1158949 A CN1158949 A CN 1158949A
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Abstract
The said system has successively connected liquid storage cylinder, intermediate cylinder, gadifier, gas mixer and gas cylinder. The C5 light hydrocarbon liquid, which is transported from liquid storage cylinder via intermediate cylinder to gasifier for forced heating gasification, and the mixed fuel gas obtained via the mixing of gas and air in Venturi pipe is low-pressure stored in wet gas cylinder and transported to user. With low liquid temp and high heat value, the said fuel gas may replace city gas.
Description
The present invention relates to that a kind of liquid towards lighter hydrocarbons gasify and the equipment and the technology of mixed gas, the combustion gas of gained can be delivered to the user by pipe network.
Many by-products are arranged in the petrochemical industry, can be made into liquefied petroleum gas (LPG) and the use that acts as a fuel through the carbon three of fractionation gained and the cut of carbon four, but carbon five then can not get solving preferably because of the gasification problem for the cut of main component, so suitable difficulty is arranged as fuel, if be used as industrial chemicals then because of separation costs lacks use value greatly, so often emptying is burnt.For example, the pair material that accounts for product population nearly 20% is just arranged in the ethylene project, and carbon 5 compositions in the secondary material are very high, often are drained and burn because of these secondary material complicated components are difficult for utilization.For addressing this problem, Chinese patent application CN2090006u provides a kind of C of using
5Make the firing unit of fuel, by pipe, carry air,, export gas range to by steel cylinder then so that make fuel become gaseous state by liquid transition to the steel cylinder that liquid C 5 fuel is housed by blower fan.This device complicated operation, the air feed instability, and lack Security, be difficult to apply.Improve as it, Chinese patent application CN1104746A has proposed that a kind of concentrated gasification pipe is carried and the technology of utilizing carbon five fuel.This technology can the sub-district or the subregion gasification, is piped to the family, replaces the behindhand type of one bottle of one kitchen range, but because of its when the line transportation, discharge pressure is 0.3～0.35Kg/cm
2, not only discharge pressure is higher, and the discharge pressure gasification is slow, and combustion gas is easily liquefied during low temperature, so the lower occasion of temperature that can not conform.
The purpose of this invention is to provide a kind of can the adaptation than low ambient temperature and output stability combustion gas preferably and this combustion gas can mix gas system and technology thereof for the light hydrocarbon that pipe network is carried.
Realize that the technological scheme that provides a kind of combustion gas that generates can mix the gas system for the light hydrocarbon that pipe network is carried in the object of the invention is (referring to Fig. 1 and Fig. 2), native system has gasification installation (31) and gas mixing device (32), and gasification installation (31) is connected with gas mixing device (32) by valve and connecting tube.The structural feature of native system is also to have liquid storage tank (1), pans (2) and gas tank (4).Liquid storage tank (1) has liquid entering hole (11), liquid outlet (12), suction port (13) and air outlet (14); Liquid entering hole (11) is the liquid light hydrocarbon liquid entering hole; Liquid outlet (12) is the liquid light hydrocarbon liquid outlet, and liquid outlet (12) is located the tank body that airtight fixing drain pipe (12-1) is positioned at liquid storage tank (1), and the feed liquor mouth of pipe of drain pipe (12-1) is positioned at the bottom of tank body.Pans (2) are provided with liquid entering hole (21), liquid outlet (22); Liquid entering hole (21) is connected with the liquid outlet (12) of liquid storage tank (1) by valve and connecting tube.Gasification installation (31) is a heat exchanger, the medium import (31-1) of heat exchanger (31) is the low pressure steam suction port, media outlet (31-2) is the condensed water water outlet, material inlet (31-3) is the lighter hydrocarbons liquid entering hole, material outlet (31-4) is the lighter hydrocarbons air outlet, and lighter hydrocarbons liquid entering hole (31-3) is connected with the liquid outlet (22) of pans (2) by valve and connecting tube.Gas mixing device (32) is a Venturi tube, and the fluid inlet opening (32-1) of Venturi tube (32) is the import of lighter hydrocarbons gas, and intake (32-2) is an air intlet, and fluid outlet (32-3) is a mixed gas outlet; The lighter hydrocarbons gas import (32-1) of Venturi tube (32) links to each other with the lighter hydrocarbons air outlet (31-4) of heat exchanger (31) by valve and connecting tube.Gas tank (4) is the floating top of low pressure wet type gas tank, the suction port (41) of gas tank (4) is connected with the mixed gas outlet (32-3) of Venturi tube (32) by valve and connecting tube, and the air outlet (42) of gas tank (4) is the interface that can link to each other with the gas supply pipe net.
Native system also has low pressure steam boiler (5) and inactive gas steel cylinder (6).The liquid entering hole (11) of liquid storage tank (1) is located the tank body that airtight fixing liquid inlet pipe (11-1) is positioned at liquid storage tank (1), and the mouth of pipe of liquid inlet pipe (11-1) is positioned at the top of tank body; Liquid storage tank (1) also is provided with sewage draining exit (15), and sewage draining exit (15) is located the airtight drain pipe (15-1) that is fixed with the hydrops groove (16) that leads to liquid storage tank (1) inner bottom part; Suction port (13) is connected with steel cylinder (6) by valve and connecting tube.Pans (2) also are provided with suction port (23) and air outlet (24), and suction port (23) is connected with steel cylinder (6) by valve and connecting tube, and air outlet (24) are connected with gas tank (4) by valve and connecting tube.Heat exchanger as gasification installation (31) is tubular heat exchanger or tube coil type heat exchanger, and its medium import (31-1) is connected with the steam outlet of low pressure steam steam supply equipment (5) by valve and connecting tube.
Above-mentioned low pressure steam steam supply equipment (5) is the low pressure steam gas fired boiler; Its fuel gas import is connected with the air outlet (42) of gas tank (4) by valve and connecting tube; Inactive gas steel cylinder (6) is the nitrogen steel cylinder; Liquid storage tank (1) is located at subsurface; Heat exchanger (31) is a tubular heat exchanger; Gasification installation (31) and gas mixing device (32) are combined into an equipment as two parts and use.
Above-mentioned liquid storage tank (1) has 2, can use for storing the different lighter hydrocarbons of molecular weight, and 2 liquid storage tanks (1) are connected with same pans (2) by valve and connecting tube separately.
Realize that the technological scheme that provides a kind of combustion gas that generates can mix the employed technology of gas system for the light hydrocarbon that pipe network is carried in the object of the invention is (referring to Fig. 3), this technology has gasification, mixes the gas operation, be characterized in, used simultaneously as light hydrocarbon liquid by carbon five liquid and liquefied petroleum gas (LPG), master operation is: 1. store liquid.Light hydrocarbon liquid is placed liquid storage tank (1).2. liquid is prepared.Light hydrocarbon liquid is transported to pans (2) by liquid storage tank (1).3. gasification.Medium import (31-3) heat exchanger (31) through heat exchanger (31) is carried low pressure steam or hot water vapor, continuously light hydrocarbon liquid is imported heat exchanger (31) by pans (2) through the material inlet (31-1) of heat exchanger (31) then, provide heat to carry out heating and gasifying by thermal medium, the light hydrocarbon gas of gasification is transported to Venturi tube (32) by material outlet (31-4).4. mix gas.Light hydrocarbon gas enters in the Venturi tube (32) through the lighter hydrocarbons gas import (32-1) of Venturi tube (32), the air intlet (32-2) of air through Venturi tube (32) enters in the pipe and mixes with light hydrocarbon gas and to be situated between, and mixed gas is from mixed gas outlet (32-3) output of Venturi tube (32).5. air storage.The suction port (41) of mixed gas through gas tank (4) enters in the gas tank (4), carries in order to pipe network and uses.
Above-mentioned pans (2) also are provided with suction port (23) and air outlet (24).1. the liquid storage tank of storing in the liquid operation (1) is located at subsurface, in liquid inlet pipe (11-1) the input jar of light hydrocarbon liquid by liquid storage tank (1).2. in the liquid preparatory process, to have the suction port (13) that the inactive gas of certain pressure exports through liquid storage tank (1) and be pressed into liquid storage tank (1) from steel cylinder (6), make light hydrocarbon liquid under the effect of the pressure of inactive gas, be located at drain pipe (11-2) the output liquid storage tank (1) of liquid storage tank (1) bottom, enter pans (2) by the liquid entering hole (21) of pans (2) through the feed liquor mouth of pipe.3. the thermal medium of carrying to medium import (31-1) in the gasification process is that pressure is gauge pressure 1～2Kg/cm
2, temperature is 95～125 ℃ low pressure steam, this low pressure steam is produced by low pressure boiler (5), the used fuel of low pressure boiler (5) is the mixed gas in the gas tank (4); When heat exchanger (31) conveying material, the inactive gas that will have certain pressure is transported to the pans (2) from steel cylinder (6), light hydrocarbon liquid in the pans (2) is forced out deliver in the gasification installation (31) and the gasification of being heated, the vapor pressure of light hydrocarbon gas is gauge pressure 2～4Kg/cm
24. mix in the gas operation, the air rate of light hydrocarbon gas and air is 1: 2.2～1: 6.5. in the air storage operation, by adjusting the counterweight on the gas tank (4), the pressure control that makes the mixed gas in the gas tank (4) is at 0.02～0.035 kilogram/cm
2
In the above-mentioned light hydrocarbon liquid, the weight percentage of carbon five liquid is 25～84%, and the weight percentage of liquefied petroleum gas (LPG) is 16～75%.
Above-mentioned carbon five liquid and liquefied petroleum gas (LPG) are contained in separately the liquid storage tank (1) respectively or load in mixture in same liquid storage tank (1).
Have in the liquid storage tank (1) of carbon five liquid in above-mentioned storage, can add diene thing weight with respect to carbon five and be 0.4～0.6% 2, the 6-di-tert-butyl-4-methy phenol is as anti-coalescer.
Employed air is the dry air of relative moisture≤60% in the above-mentioned mixed gas operation.
The present invention has positive effect.1. the pressure of gas tank of the present invention can be controlled in 0.02～0.035 kilogram/cm
2So when pipe network was carried mixed gas, discharge pressure was less, and the depoint depression of mixed gas is low to moderate-20 ℃～-40 ℃.Therefore, solved that temperature was lower than the problem that can liquefy about-5 ℃ when mixed gas was by line transportation under the certain pressure, can long distance carry, home-in-pipe can also be installed under the open-air atmosphere.2. gas tank of the present invention adopts Wet-type gas tank, and along with in-tank mixing gas what, the bell jar of gas tank moves up and down the maintenance pressure stable, so can keep the stable of discharge pressure, the stability of assurance air feed.Simultaneously, gasification mixes the gas operation and can whole day move in 24 hours, when gas is full of in the gas tank, and the operation of halt system.When gas in the gas tank is less than when a certain amount of the system of reruning.Like this, not only help operation and management, also help equipment is keeped in repair and maintains.3. raw material sources of the present invention are extensive, can use carbon five liquid and liquefied petroleum gas (LPG) simultaneously, and the content of carbon three, carbon four, carbon five can be adjusted in a sizable proportion in the materials.Also can use in the ethylene project C in the cracking gained by product
3～C
5Cut (azeotropic temperature is generally 8～50 ℃) and use the gained C of petrochemical refining
3～C
5Cut.And used raw material is not limited only to the mixing of lighter hydrocarbons and uses, also applicable to single liquefied petroleum gas (LPG) or carbon five liquid.4. Security of the present invention is good, and the combustion gas that is generated is a non-toxic gas.When each main device (except that boiler) all adopts air pressure control, even outage also can maintenance system operation a period of time.5. in native system when operation,, easy and simple to handle, internal structure of each device is also uncomplicated, and boiler can select the gas-type boiler for use, directly act as a fuel with the mixed gas in the gas tank, and be a kind of energy-conserving product.6. applied range of the present invention, air demand can be accomplished normal air feed to tens thousand of per family from tens family users, and the calorific value adjustable range is from 4500 kilocalories/meter
3To 12500 kilocalories/meter
3, adapt to different civilian and industrial users' calorific value needs.This compares with town gas calorific value≤4200 kilocalories/meter 3 has remarkable advantages, is the update product of town gas.Add aforementioned good effect, the present invention has very big promotional value.
Fig. 1 is a kind of schematic representation of system of the present invention.
Fig. 2 is the gasification and the schematic representation of gas mixing device among Fig. 1.
Fig. 3 is a kind of schematic flow sheet of technology of the present invention.
Fig. 4 is the another kind of schematic flow sheet of technology of the present invention.
Below in conjunction with drawings and Examples the present invention is further described.
Embodiment 1, and light hydrocarbon mixes the gas system
See Fig. 1 and Fig. 2,
Liquid storage tank (1), pans (2), all make by GB150-89 " Steel Pressure Vessels " and " safe technology of pressure vessel supervision rules " and check as the tubulation heat exchanger of gasification member (31), (vessel) class belongs to third class(grade) pressure vessel.
Steel liquid storage tank (1) has 2, and by arranging about direction shown in Figure 1, the volume of liquid storage tank (1) is 30m
3, be embedded in subsurface.The top of the tank body (1-3) of every liquid storage tank (1) be provided with 2 flanges take over (1-1,1-2).The flange on the left side is taken on (1-1) and is fixed with drain pipe (15-1), is provided with air outlet (14) and liquid level instrument (17).The lower end mouth of drain pipe (15-1) is arranged in the hydrops groove (16) of tank body (1-3) and the upper end-hole of drain pipe (15-1) is sewage draining exit (15).The flange on the right is taken on (1-2) and is fixed with liquid inlet pipe (11-1), drain pipe (12-1) and is provided with suction port (13).The lower end mouth of liquid inlet pipe (11-1) is positioned at the top of tank body (1-3) and the upper end-hole of liquid inlet pipe (11-1) is liquid entering hole (11); The lower end mouth of drain pipe (12-1) is positioned at the top of tank body (1-3) and the upper end-hole of drain pipe (12-1) is liquid outlet (12).
The liquid entering hole (11) of every liquid storage tank (1), liquid outlet (12), suction port (13), air outlet (14) and sewage draining exit (15) locate to be equipped with valve (19-1,19-2,19-3,19-4,19-5), and also are provided with discharge channel between the air outlet (14) of 2 liquid storage tanks (1).A pressure-relief valve (19-6) is located to be provided with in every liquid storage tank (1) air outlet (14), by pressure-relief valve (19-6) and pipeline two liquid storage tanks (1) is connected.On the release pipeline, be connected to a branch road, be connected with the suction port (41) of gas tank (4) by pipeline pressure-relief valve (19-7).
Nitrogen steel cylinder (6) has 2, and their delivery outlet is connected on the nitrogen steam line by reduction valve (69).The nitrogen steam line has three branch roads.Article one, the nitrogen in the branch road is as control gas, and this branch road links to each other by the mixed gas control system system (33) of secondary pressure regulating type reduction valve (69-1) with gasification mixer (3).Nitrogen in the second branch road is as operating gas, and this branch road is provided with secondary pressure regulating type reduction valve (69-2), and the suction valve (29-3) that the output terminal of this reduction valve (69-2) is located by connecting tube and pans (2) suction ports (23) is connected.Article three, the nitrogen in the branch road is also as operating gas, this branch road is earlier by two position three-way valve (69-31), links to each other and is connected with liquid storage tank (1) by the secondary pressure regulating type reduction valve (69-32) that links to each other with suction valve (19-3) on liquid storage tank (1) suction port (13) again.
Pans (2) are provided with liquid entering hole (21), liquid outlet (22), suction port (23), air outlet (24) and hydrops tapping hole (25), above-mentioned each jointing be provided with corresponding valve (29-1,29-2,29-3,29-4,29-5).Liquid entering hole (21) has 2, the liquid entering hole on the left side (21) by valve (29-1,19-1) and connecting tube be connected with the liquid storage tank (1) on the left side; The liquid entering hole (21) on the right is connected with the liquid storage tank (1) on the right by valve (29-1,19-1) and connecting tube, and the valve (29-1) that the liquid entering hole on this right (21) is located is an one-way valve.The valve (29-2) that pans liquid outlet (22) is located also is an one-way valve.Suction port (23) is connected with the nitrogen steam line by its suction valve (29-3) and secondary pressure regulating type reduction valve (69-2).Air outlet (24) is connected with the suction port (41) of gas tank (4) by its gas outlet valve (29-4).
As the tubular heat exchanger of gasification installation (31) and constitute the main body of vaporization mixer (3) as the Venturi tube of gas mixing device (32).Vaporization mixer (3) also is provided with and mixes gas control system system (33) and flow control system (34).The medium import (31-1) of tubular heat exchanger (31) is connected by the suction valve (39-1) of connecting tube with vaporization mixer (3); Media outlet (31-2) locates to be provided with Low Temperature Steam and water of condensation expulsion valve (39-2); Material inlet (31-3) is located to be provided with by pressure controlled flow control valve (39-31), the input end of this modulating valve (39-31) is connected with the output terminal of the feed liquor valve (39-32) of vaporization mixer (3), and the input end of feed liquor valve (39-32) is connected with the liquid valve (29-2) of pans (2) by fluid flowmeter L.Flow control system (34) is located at one side of the liquid feeding end of tubular heat exchanger (31).The gas access of the fluid level controller (34-1) of flow control system (34) is connected with the top of heat exchanger (31) material cavity (31-5), the liquid inlet of fluid level controller (34-1) is connected with the bottom of heat exchanger (31) material cavity (31-5), and the air pressure output terminal of fluid level controller (34-1) is connected with the input end of proportional pressure-reducing valve (34-2).The output terminal of proportional pressure-reducing valve (34-2) is connected with the control end of flow control valve (39-31) (39-3 1-3).
The material outlet (31-4) of tubular heat exchanger (31) locates to be serially connected with successively ball valve (39-41), filter (39-42) and pneumatic control valve (39-43), and the output terminal of filter (39-42) is connected with the gas input port (39-43-1) of pneumatic control valve (39-43); The gas delivery port (39-43-2) of pneumatic control valve (39-43) is connected with the fluid inlet opening (32-1) of Venturi tube (32); The gas control mouthful (39-43-3) of pneumatic control valve (39-43) links to each other with the pilot line of mixed gas control system system (33).The material outlet (31-4) of tubular heat exchanger (31) locates also to be provided with a branch road, is connected with safety valve (31-8) on this branch road.Mix the gas control end that gas control system system (33) is provided with control gas transfer valve (33-1), pressure regulator valve (33-2), two-position three way magnetic valve (33-3) and pneumatic control valve (39-43) successively.The two ends of solenoid valve (33-3) respectively are provided with an opening/shutting valve (33-4), and a manual two position three-way valve (33-5) and solenoid valve are arranged and connect.The intake (32-2) of Venturi tube (2) is connected with the external world by duct thermostat, and fluid outlet (32-3) is connected with the suction port (41) of gas tank (4) by gas outlet valve (39-51) and gas flowmeter G.
Gas tank (4) is the floating top of low wet type gas tank.Press HG/T22549.1-95 " classification of steel low pressure wet type gas holder series and technical specifications ", HGJ212-83 " construction of metal weldedstructure wet gasholder and acceptance specification " and GBJ236-82 " field apparatus, the construction of industrial pipeline welding engineering and acceptance specification " manufacturing and test.Gas tank (4) maximum height, be that bell jar (43) rises to when the highest from the height to the bell jar top at the bottom of the jar also be 12.2 meters, bell jar (43) highly is 6.8 meters, 12.5 meters of tank diameters, and reservoir volume is 600 meter 3.Suction port (41) in gas tank (4) locates to be provided with suction valve (49-1), one side of bell jar (43) is provided with high-side switch (44-1) and low-side switch (44-2), and there is lead to make switch (44-1,44-2) signal input part with control box (45) links to each other, and the signal output part of control box (45) links to each other by the control end of lead with solenoid valve (33-3).Gas outlet valve (49-2) is located to be provided with in the air outlet (42) of gas tank (4), and the output terminal of gas outlet valve (49-2) can be connected with gas transmission pipeline net work.(42) locate also to be provided with a branch road in the air outlet, and this branch road has two shunt again, and a shunt is provided with heating-value determination instrument (46), another shunt by valve (47,59-2) and connecting tube be connected with the fuel gas import of gas fired boiler (5).
Gas fired boiler (5) is the low pressure steam gas fired boiler, and exportable gauge pressure is 1～2 kilogram/cm under the normal use condition
2Steam, by valve (59-1) transport to the gasification mixer (3) steam inlet valve (39-1) enter the gasification mixer (3).
Embodiment 2, and light hydrocarbon mixes the gas system.
All the other are identical with embodiment 1, and difference is that heat exchanger (31) is a tube coil type heat exchanger, is made by Jiangsu Provincial Chemical Equipment Mfg. and Installation Co..The Placement of the Placement of its each interface and tubular heat exchanger the corresponding interface roughly the same.
Embodiment 3, and light hydrocarbon mixes the employed technology of gas system.
See Fig. 1 to Fig. 3,
Mixed gas system operates by the light hydrocarbon of embodiment's 1 gained.
1. liquid storage tank liquid feeding.Can add light hydrocarbon liquid to liquid storage tank (1) by the groove tank car that light hydrocarbon liquid is housed.During liquid feeding, the valve (19-1) that liquid inlet pipe (11-1) is located is connected with the liquid outlet of groove tank car, and the valve (19-4) that liquid storage tank (1) air outlet (14) is located is connected with the suction port of groove tank car.Open valve, then under the effect of the pump housing in the groove tank car, light hydrocarbon liquid is entered in the liquid storage tank (1).By liquid level instrument (17) reading,, close the fluid valve of locked groove tank car, the feed liquor valve (19-1) and the gas outlet valve (19-4) of liquid storage tank (1) when adding to when setting liquid level.In the liquid storage tank (1) on the left side shown in Figure 1, add carbon five liquid with above-mentioned liquid feeding method, in the liquid storage tank (1) on stone limit, add liquefied petroleum gas-liquid (also being carbon three, carbon four liquid).
Because the formed pressure of gasifying liquefied petroleum gas is higher,, in liquid feeding finishes the back or makes an inspection tour at ordinary times, exceed 4 kilograms/cm as the gas pressure in the right liquid storage tank (1) so need the gas pressure in the liquid storage tank (1) is controlled
2The time, can be by opening 2 pressure-relief valves (19-6) release in carbon five liquid storage tanks (1), when carbon five liquid storage tanks (1) pressure greater than 3 kilograms/cm
2Shi Zeke opens pressure-relief valve (19-6) and pipeline pressure-relief valve (19-7) release in gas tank (4) of self.
2. pans liquid feeding.(69,69-1 69-32), is provided with decompression numerical value as requested, and these valves are not generally all closed except that valve (69), and valve (69) only finishes just to close in whole technology at first to open valve.Next opens the valve of locating pans (2) air outlets (24) (29-4), makes gas in the jar to gas tank (4) release of low voltage side.Open again valve on carbon five liquid storage tanks (1) the transfusions path (19-2,29-1).Then, open the left path of two position three-way valve (69-3) and the suction valve (13) of liquid storage tank (1) nitrogen steel cylinder (6) is exerted pressure in the liquid storage tank (1) on the left side, 1 kilogram/cm of the about gauge pressure of pressure
2, carbon five liquid are entered in the pans (2) by the liquid entering hole (21) on pans (2) left side.The addition of carbon five liquid is determined according to the air demand of every day, measures according to the level meter on the pans (2), when reaching setting value, closes feed liquor valve (29-1) immediately, and then with other valve closing.
In pans (2), add carbon three, carbon four makes it mixes naturally with carbon five, the liquid storage tank on the right (1) has 2-4 kilogram/cm usually
2Pressure, (19-2,29-1) liquid feeding can carry out automatically to open the valve of the right on the infusion channel.In the time of can not keeping automatic liquid feeding along with liquid storage tank (1) internal pressure on the rising of pans (2) pressure or the right, available nitrogen pressurizes to liquid storage tank (1).When liquid level reaches setting value, close feed liquor valve (29-1) immediately, and then with other valve closing.When liquid storage tank (1) uses a period of time, a jar end is when having water and heavy distillate deposition, can sediments be discharged from sewage draining exit (15) through drain pipe (15-1) by self pressure or with nitrogen pressure, perhaps extracts out with pump.
3. gasification.Open the suction valve (29-3) of pans (2),, and make pressure maintain 5 kilograms/m with the liquid pressurization of nitrogen in pans (2)
2About, open the liquid valve (29-2) of pans (2), the feed liquor valve (39-32) of vaporization mixer (3), the liquid in the pans (2) is through liquid valve (29-2), feed liquor valve (39-32) and flow control valve (39-31) input heat exchanger (31).Flow control valve (39-31) is the Pneumatic control type flow control valve, and control by the air pressure signal generation different pressures by the liquid level height is different for its flow.That is, fluid level controller (34-1) is according to the air pressure of the different sizes of height output of liquid level in heat exchanger (31) material cavity (31-5), behind proportional pressure-reducing valve (34-2) as the pilot pressure of flow control valve (39-31).Liquid in material cavity (31-5) reaches to be set under the vapor pressure situation, and when liquid level was high, the pressure of fluid level controller (34-1) output was big, and flow control valve (39-31) opening degree is little, and the feed liquor amount is also few.Otherwise the feed liquor amount is more.
Low pressure steam gas fired boiler (5) is acted as a fuel by the mixed gas in the gas tank (4), and the output gauge pressure is 1～2 kilogram/cm
2Band press steam, transport to tubular heat exchanger (31) through pipeline, temperature is 95～125 ℃, and the mixing material in the heat exchanger (31) is carried out forced gasification, produces 2～3.5 kilograms/cm of manometer pressure
2Vapor pressure.Steam as heat supply then descends through pressure after the exchange heat, and generating unit segregation junction water, is discharged from exhaust port through valve (39-2) by media outlet (31-2).
4. mix gas.The light hydrocarbon gas of exporting in the heat exchanger (31) enters Venturi tube (32) through ball valve (39-41), filter (39-42) and pneumatic control valve (39-43) and is mixed with air, promptly, light hydrocarbon gas enters the pipe from the fluid inlet opening (32-1) of Venturi tube (32), it sprays the negative pressure that is produced air is sucked the generation combination gas that is mixed with it from intake (32-2), and gauge pressure is 2～4 kilograms/cm
2The jet pressure of light hydrocarbon gas under being mixed than being 1: 2.2～1: 6 of lighter hydrocarbons gas and air.
Gasification mixer (3) from feed liquor, gasify, be mixed to course of conveying and can carry out automatically.And the liquid entering hole of gasification mixer (3) is provided with fluid flowmeter L, and mixed gas outlet is provided with gas flowmeter G, converts by metering and can determine being mixed than whether meeting setting value of lighter hydrocarbons gas and air.
5. air storage.Combination gas after light hydrocarbon gas and air are mixed is carried to the gas tank (4) of low voltage side, and the working pressure of gas tank (4) is 0.02～0.035 kilogram/cm
2Gas tank (4) adopts generation to press the type design of the floating top of wet type, carries out water seal by tank, and air storage pressure is regulated by the counterweight of adjusting on the bell jar (43).The air outlet (42) of gas tank (4) can join with transmission pipeline network.Combination gas is directly delivered in the user family by pipeline.Gas tank (4) is established high-order control and low level control.When in gas tank (4), carrying combination gas, making bell jar (43) rise to its feeler lever and high-side switch (44-1) when contacting, then send the electrical signal of an expression high position to control box (45) by high-side switch (44-1).Combination gas in gas tank (4) exports the user to, and bell jar (43) drops to its feeler lever and low-side switch (44-2) when contacting, and closes (44-2) sends electrical signal from an expression low pressure to control box outward by low level.Electric control system can be set up acousto-optic device, so that the prompting operator in charge.Gas tank (4) is provided with air storage amount scale, and gas tank (4) mixed gas what are used for understanding at any time, and can be for the staff under powering-off state, and carrying out manual operation provides reference.
When control box (45) is received the low level signal, send control signal, make solenoid valve (33-3) open-minded, 5 kilograms/cm to the two-bit triplet solenoid valve (33-3) that mixes gas control system system (33)
2Nitrogen by the control gas transfer valve of often opening (33-1), through open and close valve (33-6), pressure regulator valve (33-2), open and close valve (33-41), by solenoid valve (33-3), transport to the control end of pneumatic control valve (39-43) through opening and closing valve (33-42) again, under the effect of gas pressure, spring in the valve shrinks, the suction port and the air outlet of control valve (39-43) are connected, make Venturi tube (32) work, and carry combination gas to gas tank (4).
In contrast, when control box (45) when receiving high signal, to solenoid valve (33-3) send control signal, (33-3) cuts off nitrogen to make solenoid valve, make the nitrogen in the pneumatic control valve (39-43) discharge and pneumatic control valve (39-43) cuts out from the evacuation port (33-3-1) of solenoid valve (33-3) through pipeline simultaneously, being mixed and carrying stops.
If under power-off condition, operate manual two position three-way valve, can carry out the operating process that pneumatic control valve (39-43) closed in above-mentioned startup equally.
When being mixed and carrying under the situation that is in time-out, heat exchanger (31) material cavity (31-5) internal pressure rises and when making gasification and liquefaction reach balance, pressure no longer rises, and system is in wait state.
6. heating-value determination.The entrance and exit of gas tank (4) all can carry out heating-value determination, to combination gas continuous sampling burning, measures calorific value by heating-value determination instrument (46), and the data that recorded can show at once.If do not meet the ratio that is mixed that the desired value that sets can be adjusted lighter hydrocarbons gas and air.
Table 1 has provided carbon five liquid and the calorific capacity of liquefied petroleum gas (LPG) after the lighter hydrocarbons gas that is generated under the different proportioning situations is mixed by different proportion and air.The field of Far Left one row is heating numerical value in the form, and the four row fields on the right account for the percent by volume numerical value of combination gas for lighter hydrocarbons gas, the temperature range that the corresponding combination gas of the 10th behavior of field is suitable for.The proportioning of carbon five liquid and liquefied petroleum gas (LPG) can be different according to season, set from different places.When determining the data of calorific capacity and Applicable temperature, the pressure that combination gas is set is 0.05 kilogram/cm
2
Combination gas calorific value adjustability is bigger as shown in Table 1, from 4500 kilocalories/meter
3To 12500 kilocalories/meter
3Adjustable, can adapt to the needs of different user to different calorific values.Calorific value there are the industrial and mining enterprise of specific (special) requirements, are no more than 0.15 kilogram/cm at the combustion gas working pressure
2Temperature is under the situation more than 0 ℃, and calorific value can increase to 12500～16000 kilocalories/meter
3, gas content is 41.70～53.30%.
The combination gas of in environment below 0 ℃, using, mixing the air that is mixed in the gas operation must be the dry air of relative moisture≤60%, to prevent when supplying with pipe network, because of the condensed water blocking pipe influences normal air feed, and can be when severe winter in liquid storage tank (1), add and account for liquid light hydrocarbon gross weight 0.1～0.15% antifreezing solution methyl alcohol or ethylene glycol.
For preventing the polymerization of liquid light hydrocarbon, also can in liquid storage tank (1), add diene thing weight with respect to carbon five and be 0.4～0.6% anti-coalescer 2, the 6-di-tert-butyl-4-methy phenol.
Embodiment 4,
See Fig. 4, all the other are with embodiment 3, and difference is when liquid storage tank (1) adds light hydrocarbon liquid, load in mixture after carbon five liquid and liquefied petroleum gas (LPG) can being measured by liquid level instrument (17) in the liquid storage tank (1) on the right.The combination gas that air is made that is mixed of table 1 carbon five and common liquefied petroleum gas (LPG)
Calorific capacity and dew point (liquefaction) temperature Schedule (setting pressure 0.05Kg/cm
2)
| Sequence number | Calorific capacity (kilocalorie/rice 3) | Carbon 5 84% liquid gas 16% | Carbon 5 70% liquid gas 30% | Carbon 5 50% liquid gas 50% | Carbon 5 25% liquid gas 75% |
| ??1 | ????4140 | ???????— | ??????— | ?????— | ?????13.8 |
| ??2 | ????4360 | ???????— | ??????— | ????13.43 | ??????— |
| ??3 | ????4520 | ???????— | ????13.10 | ?????— | ??????— |
| ??4 | ????4580 | ?????12.72 | ????13.28 | ????14.10 | ?????15.30 |
| ??5 | ?5000～7000 | ???13.9～19.40 | ??14.5～20.3 | ??15.4～21.5 | ??16.7～23.3 |
| ??6 | ?7000～9000 | ???19.4～25 | ??20.3～26.1 | ??21.5～27.7 | ??23.3～30 |
| ??7 | ?9000～11000 | ???25～30.56 | ??26.1～31.9 | ??27.7～33.9 | ??30～36.7 |
| ??8 | ?11000～12000 | ???30.56～33.3 | ??31.9～34.8 | ??33.9～36.9 | ??36.7～40 |
| ??9 | ?12000～12500 | ???33.3～34.7 | ??34.8～36.2 | ??36.9～38.5 | ??40～41.7 |
| ??10 | The adaptive temperature scope | ???-20℃ ???～40℃ | ??-25℃ ????40℃ | ??-30℃ ??～40℃ | ??-40℃ ??～40℃ |
Claims (10)
1, a kind of combustion gas that generates can mix the gas system for the light hydrocarbon that pipe network is carried, have gasification installation (31) and gas mixing device (32), gasification installation (31) is connected with gas mixing device (32) by valve and connecting tube, it is characterized in that also having liquid storage tank (1), pans (2) and gas tank (4);
Liquid storage tank (1) has liquid entering hole (11), liquid outlet (12), suction port (13) and air outlet (14); Liquid entering hole (11) is the liquid light hydrocarbon liquid entering hole; Liquid outlet (12) is the liquid light hydrocarbon liquid outlet, and liquid outlet (12) is located the tank body that airtight fixing drain pipe (12-1) is positioned at liquid storage tank (1), and the feed liquor mouth of pipe of drain pipe (12-1) is positioned at the bottom of tank body;
Pans (2) are provided with liquid entering hole (21), liquid outlet (22); Liquid entering hole (21) is connected with the liquid outlet (12) of liquid storage tank (1) by valve and connecting tube;
Gasification installation (31) is a heat exchanger, the medium import (31-1) of heat exchanger (31) is the low pressure steam suction port, media outlet (31-2) is the condensed water water outlet, material inlet (31-3) is the lighter hydrocarbons liquid entering hole, material outlet (31-4) is the lighter hydrocarbons air outlet, and lighter hydrocarbons liquid entering hole (31-3) is connected with the liquid outlet (22) of pans (2) by valve and connecting tube;
Gas mixing device (32) is a Venturi tube, and the fluid inlet opening (32-1) of Venturi tube (32) is the import of lighter hydrocarbons gas, and intake (32-2) is an air intlet, and fluid outlet (32-3) is a mixed gas outlet; The lighter hydrocarbons gas import (32-1) of Venturi tube (32) links to each other with the lighter hydrocarbons air outlet (31-4) of heat exchanger (31) by valve and connecting tube;
Gas tank (4) is the floating top of low pressure wet type gas tank, the suction port (41) of gas tank (4) is connected with the mixed gas outlet (32-3) of Venturi tube (32) by valve and connecting tube, and the air outlet (42) of gas tank (4) is the interface that can link to each other with the gas supply pipe net.
2, the combustion gas that generates according to claim 1 can mix the gas system for the light hydrocarbon that pipe network is carried, and it is characterized in that native system also has low pressure steam steam supply equipment (5) and inactive gas steel cylinder (6);
The liquid entering hole (11) of liquid storage tank (1) is located the tank body that airtight fixing liquid inlet pipe (11-1) is positioned at liquid storage tank (1), and the mouth of pipe of liquid inlet pipe (11-1) is positioned at the top of tank body; Liquid storage tank (1) also is provided with sewage draining exit (15), and sewage draining exit (15) is located the airtight drain pipe (15-1) that is fixed with the hydrops groove (16) that leads to liquid storage tank (1) inner bottom part; Suction port (13) is connected with steel cylinder (6) by valve and connecting tube;
Pans (2) also are provided with suction port (23) and air outlet (24), and suction port (23) is connected with steel cylinder (6) by valve and connecting tube, and air outlet (24) are connected with gas tank (4) by valve and connecting tube;
Heat exchanger as gasification installation (31) is tubular heat exchanger or tube coil type heat exchanger, and its medium import (31-1) is connected with the steam outlet of low pressure steam steam supply equipment (5) by valve and connecting tube;
3, the combustion gas that generates according to claim 2 can mix the gas system for the light hydrocarbon that pipe network is carried, and it is characterized in that low pressure steam steam supply equipment (5) is the low pressure steam gas fired boiler; Its fuel gas import is connected with the air outlet (42) of gas tank (4) by valve and connecting tube; Inactive gas steel cylinder (6) is the nitrogen steel cylinder; Liquid storage tank (1) is located at subsurface; Heat exchanger (31) is a tubular heat exchanger; Gasification installation (31) and gas mixing device (32) are combined into an equipment as two parts and use.
4, can mix the gas system for the light hydrocarbon that pipe network is carried according to claim 2 or the 3 described combustion gas that generate, it is characterized in that, liquid storage tank (1) has 2, can use for storing the different lighter hydrocarbons of molecular weight, 2 liquid storage tanks (1) are connected with same pans (2) by valve and connecting tube separately.
5, the technology of using the described combustion gas that generates of claim 1 to mix gas systems produce mixed gas for the light hydrocarbon that pipe network is carried, have gasification, mix the gas operation, it is characterized in that used simultaneously as light hydrocarbon liquid by carbon five liquid and liquefied petroleum gas (LPG), master operation is:
Storage liquid; Light hydrocarbon liquid is placed liquid storage tank (1);
Liquid is prepared; Light liquid is transported to pans (2) by liquid storage tank (1);
Gasification; Medium import (31-1) heat exchanger (31) through heat exchanger (31) is carried low pressure steam, continuously light hydrocarbon liquid is imported heat exchange vaporizer (31) by pans (2) through the material inlet (31-1) of heat exchanger (31) then, provide heat to carry out heating and gasifying by thermal medium, the light hydrocarbon gas of gasification is transported to Venturi tube (32) by material outlet (31-4);
Mix gas; Light hydrocarbon gas enters in the Venturi tube (32) through the lighter hydrocarbons gas import (32-1) of Venturi tube (32), the air intlet (32-2) of air through Venturi tube (32) enters in the pipe and mixes with light hydrocarbon gas, and mixed gas is from mixed gas outlet (32-3) output of Venturi tube (32);
Air storage; The suction port (41) of mixed gas through gas tank (4) enters in the gas tank (4), carries in order to pipe network and uses.
6, the technology of preparation mixed gas according to claim 5 is characterized in that, pans (2) also are provided with suction port (23) and air outlet (24);
Liquid storage tank (1) in the storage liquid operation is located at subsurface, in liquid inlet pipe (11-1) the input jar of light hydrocarbon liquid by liquid storage tank (1);
In the liquid preparatory process, to have the suction port (13) that the inactive gas of certain pressure exports through liquid storage tank (1) and be pressed into liquid storage tank (1) from steel cylinder (6), make light hydrocarbon liquid under the effect of the pressure of inactive gas, be located at drain pipe (11-2) the output liquid storage tank (1) of liquid storage tank (1) bottom, enter pans (2) by the liquid entering hole (21) of pans (2) through the feed liquor mouth of pipe;
The thermal medium of carrying to medium import (31-1) in the gasification process is that pressure is gauge pressure 1-2 kilogram/cm
2, temperature is 95～125 ℃ low pressure steam, this low pressure steam is produced by low pressure boiler (5), the used fuel of low pressure boiler (5) is the mixed gas in the gas tank (4); When heat exchanger (31) conveying material, the inactive gas that will have certain pressure is transported to the pans (2) from steel cylinder (6), light hydrocarbon liquid in the pans (2) is forced out deliver in the gasification installation (31) and the gasification of being heated, the vapor pressure of light hydrocarbon gas is 2～4 kilograms/cm of gauge pressure
2
Mix in the gas operation, the air rate of light hydrocarbon gas body and air is 1: 2.2～1: 6;
In the air storage operation, by adjusting the configuration on the gas tank (4), the pressure control that makes the mixed gas in the gas tank (4) is at 0.02～0.035 kilogram/cm
2
7, the technology of preparation mixed gas according to claim 6 is characterized in that, in the light hydrocarbon liquid, the weight percentage of carbon five liquid is 25～84%, and the weight percentage of liquefied petroleum gas (LPG) is 16～75%.
8, the technology of preparation mixed gas according to claim 7 is characterized in that, carbon five liquid and liquefied petroleum gas (LPG) are contained in separately the liquid storage tank (1) respectively or load in mixture in same liquid storage tank (1).
9, the technology of preparation mixed gas according to claim 6 is characterized in that, in the liquid storage tank (1) of storing carbon five liquid, can add diene thing weight with respect to carbon five and be 0.4～0.6% 2, the 6-di-tert-butyl-4-methy phenol is as anti-coalescer.
10, the technology of preparation mixed gas according to claim 6 is characterized in that, employed air is the dry air of relative moisture≤60% in the mixed gas operation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 96117181 CN1053270C (en) | 1996-11-19 | 1996-11-19 | Light hydrocarbon gasifying and gas-mixing system and technology |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 96117181 CN1053270C (en) | 1996-11-19 | 1996-11-19 | Light hydrocarbon gasifying and gas-mixing system and technology |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1158949A true CN1158949A (en) | 1997-09-10 |
| CN1053270C CN1053270C (en) | 2000-06-07 |
Family
ID=5124114
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 96117181 Expired - Fee Related CN1053270C (en) | 1996-11-19 | 1996-11-19 | Light hydrocarbon gasifying and gas-mixing system and technology |
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| Country | Link |
|---|---|
| CN (1) | CN1053270C (en) |
Cited By (6)
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|---|---|---|---|---|
| CN100443803C (en) * | 2004-12-13 | 2008-12-17 | 肖杰 | Tube type vaporization device for liquefied gas for industrial use |
| CN101914696A (en) * | 2010-06-24 | 2010-12-15 | 西北工业大学 | Combustion-oxidation preventing method in magnesium alloy smelting and antigravity casting process and mixture system |
| CN105600726A (en) * | 2016-03-02 | 2016-05-25 | 大庆华凯石油化工设计工程有限公司 | Tank-bottom-cleaning buried material tank device |
| CN106765279A (en) * | 2016-12-09 | 2017-05-31 | 杨秀华 | Steam circulation environmental protection feed system based on gasification lighter hydrocarbons |
| CN107401758A (en) * | 2017-06-23 | 2017-11-28 | 兰万灵（中国）控股有限公司 | A kind of gaseous hydrocarbon mixes the production method of air gas |
| CN107725196A (en) * | 2017-11-07 | 2018-02-23 | 荆门宏图特种飞行器制造有限公司 | LPG generating air supply systems |
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1996
- 1996-11-19 CN CN 96117181 patent/CN1053270C/en not_active Expired - Fee Related
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100443803C (en) * | 2004-12-13 | 2008-12-17 | 肖杰 | Tube type vaporization device for liquefied gas for industrial use |
| CN101914696A (en) * | 2010-06-24 | 2010-12-15 | 西北工业大学 | Combustion-oxidation preventing method in magnesium alloy smelting and antigravity casting process and mixture system |
| CN105600726A (en) * | 2016-03-02 | 2016-05-25 | 大庆华凯石油化工设计工程有限公司 | Tank-bottom-cleaning buried material tank device |
| CN105600726B (en) * | 2016-03-02 | 2018-02-06 | 大庆华凯石油化工设计工程有限公司 | The buried material tank arrangement of peace and quiet tank bottom |
| CN106765279A (en) * | 2016-12-09 | 2017-05-31 | 杨秀华 | Steam circulation environmental protection feed system based on gasification lighter hydrocarbons |
| CN107401758A (en) * | 2017-06-23 | 2017-11-28 | 兰万灵（中国）控股有限公司 | A kind of gaseous hydrocarbon mixes the production method of air gas |
| CN107401758B (en) * | 2017-06-23 | 2019-07-05 | 兰万灵（中国）控股有限公司 | A kind of gaseous hydrocarbon mixes the production method of air gas |
| CN107725196A (en) * | 2017-11-07 | 2018-02-23 | 荆门宏图特种飞行器制造有限公司 | LPG generating air supply systems |
| CN107725196B (en) * | 2017-11-07 | 2024-04-26 | 荆门宏图特种飞行器制造有限公司 | Gas supply system for LPG power generation |
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|---|---|
| CN1053270C (en) | 2000-06-07 |
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