CN105036077A - Method and system for recovering waste heat of syngas obtained by partial oxidation of natural gas - Google Patents
Method and system for recovering waste heat of syngas obtained by partial oxidation of natural gas Download PDFInfo
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- CN105036077A CN105036077A CN201510485011.8A CN201510485011A CN105036077A CN 105036077 A CN105036077 A CN 105036077A CN 201510485011 A CN201510485011 A CN 201510485011A CN 105036077 A CN105036077 A CN 105036077A
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 100
- 239000003345 natural gas Substances 0.000 title claims abstract description 50
- 238000000034 method Methods 0.000 title claims abstract description 46
- 239000002918 waste heat Substances 0.000 title claims abstract description 32
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 30
- 230000003647 oxidation Effects 0.000 title claims abstract description 25
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 287
- 238000001816 cooling Methods 0.000 claims abstract description 53
- 239000000498 cooling water Substances 0.000 claims abstract description 49
- 239000007788 liquid Substances 0.000 claims abstract description 36
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 15
- 239000011555 saturated liquid Substances 0.000 claims abstract description 13
- 238000000926 separation method Methods 0.000 claims abstract description 11
- 238000002485 combustion reaction Methods 0.000 claims abstract description 8
- 238000002156 mixing Methods 0.000 claims abstract description 7
- 239000007789 gas Substances 0.000 claims description 175
- 239000002826 coolant Substances 0.000 claims description 68
- 230000015572 biosynthetic process Effects 0.000 claims description 59
- 238000003786 synthesis reaction Methods 0.000 claims description 59
- 238000011084 recovery Methods 0.000 claims description 19
- 235000009508 confectionery Nutrition 0.000 claims description 17
- 238000009413 insulation Methods 0.000 claims description 12
- 238000006243 chemical reaction Methods 0.000 claims description 7
- 240000008042 Zea mays Species 0.000 claims description 6
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 claims description 6
- 235000002017 Zea mays subsp mays Nutrition 0.000 claims description 6
- 239000011248 coating agent Substances 0.000 claims description 6
- 238000000576 coating method Methods 0.000 claims description 6
- 235000005822 corn Nutrition 0.000 claims description 6
- 229910052711 selenium Inorganic materials 0.000 claims description 6
- 239000011669 selenium Substances 0.000 claims description 6
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 claims description 4
- 229910000831 Steel Inorganic materials 0.000 claims description 4
- 239000002131 composite material Substances 0.000 claims description 4
- 230000001590 oxidative effect Effects 0.000 claims description 4
- 239000010959 steel Substances 0.000 claims description 4
- 238000010521 absorption reaction Methods 0.000 claims description 3
- 230000020169 heat generation Effects 0.000 claims description 3
- 238000002309 gasification Methods 0.000 claims description 2
- 239000000203 mixture Substances 0.000 abstract description 5
- 238000010792 warming Methods 0.000 abstract 1
- 230000008569 process Effects 0.000 description 19
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 16
- 239000001301 oxygen Substances 0.000 description 16
- 229910052760 oxygen Inorganic materials 0.000 description 16
- 238000005516 engineering process Methods 0.000 description 11
- 230000035939 shock Effects 0.000 description 7
- 230000003020 moisturizing effect Effects 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 238000010992 reflux Methods 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 238000007664 blowing Methods 0.000 description 3
- 235000014171 carbonated beverage Nutrition 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 125000004122 cyclic group Chemical group 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000005855 radiation Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 1
- 238000012512 characterization method Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention discloses a method and a system for recovering waste heat of syngas obtained by partial oxidation of natural gas. The method comprises the steps of (1) carrying out a partial oxidation reaction on natural gas and pure oxygen in a gasifier; (2) in the gasifier, carrying out first time heat exchanging between combustion flame and high-temperature syngas as well as a water jacket; (3) carrying out second time heat exchanging between sub-high-temperature syngas at an outlet of the gasifier and a first level cooler; (4) carrying out gas-liquid separation treatment on a gas-water mixture in a steam pocket; (5) carrying out third time heat exchanging between first level cooling syngas and a second level cooler; (6) mixing saturated liquid water with second level warming cooling water for being used as inflow water of the first level cooler; (7) supplying water for the second level cooler by adopting a charging pump. The method can ensure the safe and stable running of the gasfier, reduce the temperature of the syngas to normal temperature, and recycle a lot of waste heat, and serve multiple purposes.
Description
Technical field
The invention belongs to chemical technology field, specifically, the present invention relates to a kind of method and system of preparing synthetic gas by natural gas partial oxidation waste heat recovery.
Background technology
Producing synthesis gas from natural gas is by utilizing Sweet natural gas and pure oxygen generating portion oxidizing reaction, directly generates synthetic gas.The cooling system of existing preparing synthetic gas by natural gas partial oxidation device comprises three parts, and is separate between three.Vapourizing furnace burner hearth is reaction zone, this region be cooled through water jacket to realize, water jacket and drum form a recycle system, chuck water inlet from drum downtake, the steam water interface of Jacket outlet enters drum, through carbonated drink be separated after steam be discharged drum; The synthetic gas that reaction zone produces enters shock chamber through decline conduit, and decline conduit is immersed in below liquid level, and it is cooled with water heat exchange that synthetic gas enters hydrospace, then emersion liquid level in the form of bubbles, and this process is mainly lowered the temperature to synthetic gas and washed; Synthetic gas after shock chamber's Quench, then is transported to water wash column, again carries out heat exchange with spray water in water wash column, and synthetic gas is cooled to normal temperature and delivers to desulfurization and decarburization operation.But its whole cooling system main purpose of existing preparing synthetic gas by natural gas partial oxidation device only has two: protection inboard wall of burner hearth is overtemperature and reduction synthetic gas temperature not, and does not well utilize the waste heat in process of cooling.First, after the steam water interface feeding drum that water jacket produces carries out carbonated drink separation, steam is discharged in air; Next is the synthetic gas that reaction zone produces, and its temperatures as high 1200 DEG C, prior art is cooled synthetic gas by shock chamber and water wash column, and final heat is all discharged in the middle of environment, not only causes the waste of energy, but also causes thermal pollution to environment.
Therefore, the technology of existing relevant Sweet natural gas oxidation preparing synthetic gas waste heat recovery is further improved.
Summary of the invention
The present invention is intended to solve one of technical problem in correlation technique at least to a certain extent.For this reason, one object of the present invention is the method and system proposing a kind of preparing synthetic gas by natural gas partial oxidation waste heat recovery, and the method can ensure vapourizing furnace safe and stable operation, can reduce again synthetic gas temperature to normal temperature, a large amount of waste heat can also be reclaimed, achieve and achieve many things at one stroke.
In one aspect of the invention, the present invention proposes a kind of method and system of preparing synthetic gas by natural gas partial oxidation waste heat recovery, comprising:
(1) Sweet natural gas and pure oxygen are carried out partial oxidation reaction, to obtain high-temperature synthesis gas in vapourizing furnace;
(2) inner at vapourizing furnace, combustion flame and described high-temperature synthesis gas are carried out first time heat exchange with water jacket, to make described high-temperature synthesis gas lower the temperature become time high-temperature synthesis gas, in described water jacket, water absorbs heat generation steam water interface;
(3) described the high-temperature synthesis gas in described vapourizing furnace exit and one-level water cooler are carried out second time heat exchange, to obtain one-level cooling syngas and one-level intensification water coolant, and using the water inlet of described one-level intensification water coolant as described water jacket;
(4) described steam water interface is carried out gas-liquid separation process in drum, to obtain saturation steam and saturated liquid water;
(5) described one-level cooling syngas and secondary coolers are carried out third time heat exchange, to obtain secondary cooling syngas and secondary intensification water coolant, and described secondary intensification water coolant is back in described drum;
(6) described saturated liquid water is mixed the water inlet as described one-level water cooler with described secondary intensification water coolant; And
(7) small pump is adopted to described secondary coolers for feedwater.
The cooling to synthetic gas not only can be realized according to the method for the producing synthesis gas from natural gas of the embodiment of the present invention, and the waste heat making full use of synthetic gas produces saturation steam, thus realize the maximum using of the energy, simultaneously by adopting the mode of heat exchange to carry out cooling process to synthetic gas, compared with traditional technology, eliminate shock chamber and water wash column, thus significantly reduce the input of equipment cost, in addition, synthetic gas effectively can be avoided to contact with the direct of water, thus solve the problem that in traditional technology, gained synthetic gas water-content is higher.
In addition, the method for preparing synthetic gas by natural gas partial oxidation waste heat recovery according to the above embodiment of the present invention can also have following additional technical characteristic:
In some embodiments of the invention, described water jacket is arranged on the shell of described vapourizing furnace.Thus, heat exchange efficiency can be significantly improved.
In some embodiments of the invention, described one-level water cooler and described secondary coolers are separately the interchanger of sinuous coil shape.Thus, heat exchange efficiency can be improved further.
In some embodiments of the invention, the interchanger of described sinuous coil shape is surrounded by the stainless steel tube of pipe with small pipe diameter, thus increase heat interchanging area, improves heat exchange efficiency.
In some embodiments of the invention, in step (2), the quality steam quality of described steam water interface is 0.033 ~ 0.05.Thus, the stability of technique can be improved.
In some embodiments of the invention, the temperature of described high-temperature synthesis gas is 1100 ~ 1200 degrees Celsius, and the temperature of described one-level cooling syngas is 500 ~ 600 degrees Celsius, and the temperature of described secondary cooling syngas is 40 ~ 60 degrees Celsius.
In another aspect of the present invention, the present invention proposes a kind of system of preparing synthetic gas by natural gas partial oxidation waste heat recovery, comprising:
Vapourizing furnace, described gasification stove responds gas entrance and the outlet of time high-temperature synthesis gas, and for making Sweet natural gas and pure oxygen generating portion oxidizing reaction, to obtain high-temperature synthesis gas;
Water jacket, described water jacket is arranged on the shell of described vapourizing furnace, described water jacket has water-in and water outlet, and be suitable for making water coolant in combustion flame and described high-temperature synthesis gas and water jacket to carry out first time heat exchange, to make described high-temperature synthesis gas lower the temperature become time high-temperature synthesis gas, in described water jacket, water coolant heat absorption produces steam water interface;
One-level water cooler, described one-level water cooler has one-level synthetic gas passage and one-level cooling-water duct, one end of described one-level synthetic gas passage exports with described high-temperature synthesis gas and is connected, one end of described one-level cooling-water duct is connected with described water-in, and carry out second time heat exchange for described the high-temperature synthesis gas in the exit by described vapourizing furnace and one-level water cooler, to obtain one-level cooling syngas and one-level intensification water coolant, and using the water inlet of described one-level intensification water coolant as described water jacket;
Drum, described drum has steam water interface entrance, cooling water inlet, liquid water outlet and saturation steam outlet, described liquid water outlet is connected with the other end of described one-level cooling-water duct, and for described steam water interface is carried out gas-liquid separation process, to obtain saturation steam and saturated liquid water;
Secondary coolers, described secondary coolers has secondary synthetic gas passage and secondary cooling-water duct, the other end of one-level cooling syngas passage described in one end of described secondary cooling syngas is connected, one end of described secondary cooling-water duct is connected with described cooling water inlet, and for described one-level cooling syngas and secondary coolers are carried out third time heat exchange, to obtain secondary cooling syngas and secondary intensification water coolant, and described secondary intensification water coolant is supplied in described drum;
Recycle pump, described recycle pump exports with described liquid water respectively and is connected with the other end of described one-level cooling syngas passage, and is suitable for described liquid water and the mixed mixing water of secondary water coolant to be supplied to described one-level water cooler; And
Small pump, described small pump is connected with the other end of described secondary cooling-water duct, and is suitable in described secondary coolers for feedwater.
The cooling to synthetic gas not only can be realized according to the system of the producing synthesis gas from natural gas of the embodiment of the present invention, and the waste heat making full use of synthetic gas produces saturation steam, thus realize the maximum using of the energy, simultaneously by adopting interchanger to carry out cooling process to synthetic gas, compared with traditional technology, eliminate shock chamber and water wash column, thus significantly reduce the input of equipment cost, in addition, synthetic gas effectively can be avoided to contact with the direct of water, thus solve the problem that in traditional technology, gained synthetic gas water-content is higher.
In addition, the system of preparing synthetic gas by natural gas partial oxidation waste heat recovery according to the above embodiment of the present invention can also have following additional technical characteristic:
In some embodiments of the invention, described one-level water cooler and described secondary coolers separately comprise: synthetic gas pipeline; Multiple cooling water pipeline, described multiple cooling water pipeline is along the circumferential direction arranged on the outer wall of described synthetic gas pipeline, and adopts fin steel plate to connect between described cooling water pipeline; And thermal insulation layer, described thermal insulation layer is arranged on the outside of described multiple cooling water pipeline.Thus, heat exchange efficiency can be improved further.
In some embodiments of the invention, the caliber of described cooling water pipeline is 10 ~ 15mm, and the external diameter of described synthetic gas pipeline is 100 ~ 150mm.
In some embodiments of the invention, described thermal insulation layer is made up of quality silicate composite thermo-insulating blanket.Thus, the waste of heat can effectively be avoided.
In some embodiments of the invention, the inwall of described synthetic gas pipeline is coated with high-selenium corn and compares coating.Thus, heat exchange efficiency can be improved further.
Additional aspect of the present invention and advantage will part provide in the following description, and part will become obvious from the following description, or be recognized by practice of the present invention.
Accompanying drawing explanation
Above-mentioned and/or additional aspect of the present invention and advantage will become obvious and easy understand from accompanying drawing below combining to the description of embodiment, wherein:
Fig. 1 is the method flow schematic diagram of preparing synthetic gas by natural gas partial oxidation waste heat recovery according to an embodiment of the invention;
Fig. 2 is the cross section structure schematic diagram of the interchanger adopted in the method for preparing synthetic gas by natural gas partial oxidation waste heat recovery according to an embodiment of the invention;
Fig. 3 is the cross section structure schematic diagram of the interchanger adopted in the method according to the preparing synthetic gas by natural gas partial oxidation waste heat recovery of another embodiment of the present invention;
Fig. 4 is the system architecture schematic diagram of preparing synthetic gas by natural gas partial oxidation waste heat recovery according to an embodiment of the invention;
Fig. 5 is the partial enlarged drawing of first-class heat exchanger in the system of preparing synthetic gas by natural gas partial oxidation waste heat recovery according to an embodiment of the invention.
Embodiment
Be described below in detail embodiments of the invention, the example of described embodiment is shown in the drawings, and wherein same or similar label represents same or similar element or has element that is identical or similar functions from start to finish.Be exemplary below by the embodiment be described with reference to the drawings, be intended to for explaining the present invention, and can not limitation of the present invention be interpreted as.
In describing the invention, it will be appreciated that, term " " center ", " longitudinal direction ", " transverse direction ", " length ", " width ", " thickness ", " on ", D score, " front ", " afterwards ", " left side ", " right side ", " vertically ", " level ", " top ", " end ", " interior ", " outward ", " clockwise ", " counterclockwise ", " axis ", " radial direction ", orientation or the position relationship of the instruction such as " circumference " are based on orientation shown in the drawings or position relationship, only the present invention for convenience of description and simplified characterization, instead of indicate or imply that the device of indication or element must have specific orientation, with specific azimuth configuration and operation, therefore limitation of the present invention can not be interpreted as.
In addition, term " first ", " second " only for describing object, and can not be interpreted as instruction or hint relative importance or imply the quantity indicating indicated technical characteristic.Thus, be limited with " first ", the feature of " second " can express or impliedly comprise at least one this feature.In describing the invention, the implication of " multiple " is at least two, such as two, three etc., unless otherwise expressly limited specifically.
In the present invention, unless otherwise clearly defined and limited, the term such as term " installation ", " being connected ", " connection ", " fixing " should be interpreted broadly, and such as, can be fixedly connected with, also can be removably connect, or integral; Can be mechanical connection, also can be electrical connection; Can be directly be connected, also indirectly can be connected by intermediary, can be the connection of two element internals or the interaction relationship of two elements, unless otherwise clear and definite restriction.For the ordinary skill in the art, above-mentioned term concrete meaning in the present invention can be understood as the case may be.
In the present invention, unless otherwise clearly defined and limited, fisrt feature second feature " on " or D score can be that the first and second features directly contact, or the first and second features are by intermediary indirect contact.And, fisrt feature second feature " on ", " top " and " above " but fisrt feature directly over second feature or oblique upper, or only represent that fisrt feature level height is higher than second feature.Fisrt feature second feature " under ", " below " and " below " can be fisrt feature immediately below second feature or tiltedly below, or only represent that fisrt feature level height is less than second feature.
In one aspect of the invention, the present invention proposes a kind of method of preparing synthetic gas by natural gas partial oxidation waste heat recovery.Method below with reference to the preparing synthetic gas by natural gas partial oxidation waste heat recovery of Fig. 1-3 pairs of embodiment of the present invention is described in detail.According to embodiments of the invention, the method comprises:
S100: Sweet natural gas and pure oxygen are carried out partial oxidation reaction in vapourizing furnace
According to embodiments of the invention, Sweet natural gas and pure oxygen are carried out partial oxidation reaction in vapourizing furnace, thus can high-temperature synthesis gas be obtained.
In this step, concrete, first burning torch is utilized to light the little fire of burner on vapourizing furnace, and then light big fire by little fire, then amount of natural gas and air capacity is increased gradually until fire box temperature rises to 400 ~ 500 DEG C, then keep gas discharge constant, reduce air flow quantity gradually, and increase pure oxygen flow, after air switches to pure oxygen completely, alternately increase Sweet natural gas and oxygen flow again, and keep oxygen and gas discharge than being 0.8:1, in this process, fire box temperature and furnace pressure raise gradually, until fire box temperature rises to 750 ~ 800 DEG C, furnace pressure rises to 0.2 ~ 0.3MPa, closely monitor gas composition simultaneously, then continuation increase Sweet natural gas and oxygen flow are until rated load, pay close attention to fire box temperature simultaneously and be no more than 1300 DEG C, furnace pressure is no more than 0.2MPa, the blowing out immediately once go wrong.
S200: combustion flame and high-temperature synthesis gas and water jacket are carried out first time heat exchange
According to embodiments of the invention, inner at vapourizing furnace, combustion flame and high-temperature synthesis gas are carried out first time heat exchange with water jacket, thus high-temperature synthesis gas can be made to lower the temperature become time high-temperature synthesis gas, in water jacket, water absorbs heat generation steam water interface.
According to embodiments of the invention, the temperature of secondary high-temperature synthesis gas can be 1100 ~ 1200 DEG C.
According to embodiments of the invention, the quality steam quality of steam water interface is also not particularly limited, and according to a particular embodiment of the invention, the quality steam quality of steam water interface can be 0.033 ~ 0.05.Contriver finds; if the quality steam quality of steam water interface is too low; the saturation steam produced in subsequent process is reduced; if and the quality steam quality of steam water interface is too high; easily burn out cooling system; thus, select the quality steam quality of steam water interface to be 0.033 ~ 0.05 both can ensure to continue to produce saturation steam, can not be damaged by proterctive equipment again.
S300: secondary high-temperature synthesis gas and one-level water cooler are carried out second time heat exchange, and the water inlet of water coolant as water jacket that one-level is heated up
According to embodiments of the invention, the secondary high-temperature synthesis gas in vapourizing furnace exit and one-level water cooler are carried out second time heat exchange, to obtain one-level cooling syngas and one-level intensification water coolant, and the water inlet of water coolant as water jacket that one-level is heated up.
According to embodiments of the invention, the temperature of one-level cooling syngas can be 500 ~ 600 DEG C.
According to embodiments of the invention, in secondary high-temperature synthesis gas and one-level water cooler, hydromining reflux type carries out heat exchange process, thus, can significantly improve heat exchange efficiency.
According to embodiments of the invention, one-level water cooler can adopt the interchanger of sinuous coil shape.With reference to figure 2-3, interchanger can comprise synthetic gas pipeline 10, multiple cooling water pipeline 20 and thermal insulation layer 30, according to a particular embodiment of the invention, multiple cooling water pipeline 20 can along the circumferential direction be arranged on the outer wall of synthetic gas pipeline 10, and thermal insulation layer 30 can be arranged on the outside of multiple cooling water pipeline 20.According to one embodiment of present invention, synthetic gas pipeline 10 also can be surrounded by multiple cooling water pipeline 20.Contriver finds, the interchanger of this structure can significantly improve the heat exchange efficiency between synthetic gas and water coolant.
According to embodiments of the invention, thermal insulation layer can be made up of quality silicate composite thermo-insulating blanket.Thus, the waste of heat can effectively be avoided.
According to embodiments of the invention, the inwall of synthetic gas pipeline can be coated with high-selenium corn and compare coating.Contriver finds, coating is compared by applying high-selenium corn on synthetic gas inner-walls of duct, the absorptive rate of radiation of inner-walls of duct to synthetic gas heat can be significantly improved, thus the heat exchange efficiency improved between synthetic gas and water coolant, and can make when absorbing the synthetic gas waste heat of equal heat quantity by adopting the method, required duct length is shorter, thus has both saved the consumption that arrangement space additionally reduces tubing.
According to embodiments of the invention, the caliber of cooling water pipeline can be 10 ~ 15mm, and the external diameter of synthetic gas pipeline can be 100 ~ 150mm.Contriver finds, the interchanger of this caliber can ensure while abundant heat exchange, and remarkable reduction equipment takes up an area.
According to embodiments of the invention, fin steel plate between cooling water pipeline, can be adopted to connect.
S400: steam water interface is carried out gas-liquid separation process
According to embodiments of the invention, steam water interface is carried out gas-liquid separation process in drum, thus saturation steam and saturated liquid water can be obtained.Concrete, saturation steam can be used for heating or generating.Thus, the maximum using of the energy can be realized.
S500: one-level cooling syngas and secondary coolers are carried out third time heat exchange, and the water coolant that heated up by secondary is back in drum;
According to embodiments of the invention, one-level cooling syngas and secondary coolers are carried out third time heat exchange, thus secondary cooling syngas and secondary intensification water coolant can be obtained, and the water coolant that heated up by secondary is back in drum.Thus, by adopting three heat exchange, synthetic gas can be cooled to 40 ~ 60 DEG C, a large amount of waste heat can also be reclaimed, achieve and achieve many things at one stroke.
According to embodiments of the invention, adopt reflux type to make water coolant in one-level cooling syngas and secondary coolers carry out heat exchange process in third time heat exchange, thus, heat exchange efficiency can be improved further.
According to embodiments of the invention, secondary coolers also can adopt the interchanger of sinuous coil shape.It should be noted that, third time heat exchange adopt the interchanger of sinuous coil shape identical with the secondary coolers described by Fig. 2-3, the advantage of the interchanger namely described in Fig. 2-3 is suitable for secondary coolers equally, repeats no more herein.
S600: saturated liquid water is mixed the water inlet as one-level water cooler with secondary intensification water coolant
According to embodiments of the invention, saturated liquid water is mixed the water inlet as one-level water cooler with secondary intensification water coolant.Thus, the cyclic utilization rate of water coolant can be significantly improved, thus reduce the consumption of water coolant.
According to embodiments of the invention, recycle pump can be adopted saturated liquid water and the mixed mixing water of secondary water coolant to be supplied to one-level water cooler and to carry out second time heat exchange as water coolant and time high-temperature synthesis gas.
S700: adopt small pump to secondary coolers for feedwater
According to embodiments of the invention, adopt small pump to secondary coolers for feedwater, thus can supply in time owing to producing saturation steam and the system water loss that causes, and then guarantee security of system steady running.
The cooling to synthetic gas not only can be realized according to the method for the producing synthesis gas from natural gas of the embodiment of the present invention, and the waste heat making full use of synthetic gas produces saturation steam, thus realize the maximum using of the energy, simultaneously by adopting the mode of heat exchange to carry out cooling process to synthetic gas, compared with traditional technology, eliminate shock chamber and water wash column, thus significantly reduce the input of equipment cost, in addition, synthetic gas effectively can be avoided to contact with the direct of water, thus solve the problem that in traditional technology, gained synthetic gas water-content is higher.
In another aspect of the present invention, the present invention proposes a kind of system of preparing synthetic gas by natural gas partial oxidation waste heat recovery.Below with reference to Fig. 4, the system of the preparing synthetic gas by natural gas partial oxidation waste heat recovery of the embodiment of the present invention is described in detail.According to embodiments of the invention, this system comprises:
Vapourizing furnace 100: according to embodiments of the invention, vapourizing furnace 100 has reaction gas entrance 101 and time high-temperature synthesis gas outlet 102, and for making Sweet natural gas and pure oxygen generating portion oxidizing reaction, thus can high-temperature synthesis gas be obtained.
Concrete, first burning torch is utilized to light the little fire of burner on vapourizing furnace, and then light big fire by little fire, then amount of natural gas and air capacity is increased gradually until fire box temperature rises to 400 ~ 500 DEG C, then keep gas discharge constant, reduce air flow quantity gradually, and increase pure oxygen flow, after air switches to pure oxygen completely, alternately increase Sweet natural gas and oxygen flow again, and keep oxygen and gas discharge than being 0.8:1, in this process, fire box temperature and furnace pressure raise gradually, until fire box temperature rises to 750 ~ 800 DEG C, furnace pressure rises to 0.2 ~ 0.3MPa, closely monitor gas composition simultaneously, then continuation increase Sweet natural gas and oxygen flow are until rated load, pay close attention to fire box temperature simultaneously and be no more than 1300 DEG C, furnace pressure is no more than 0.2MPa, the blowing out immediately once go wrong.
Water jacket 200: according to embodiments of the invention, water jacket 200 is arranged on the shell of vapourizing furnace 100, water jacket 200 has water-in 201 and water outlet 202, and be suitable for making combustion flame carry out first time heat exchange with water coolant in time high-temperature synthesis gas and water jacket 200, thus high-temperature synthesis gas cooling can be made to become time high-temperature synthesis gas, in water jacket 200, water coolant heat absorption produces steam water interface.
According to embodiments of the invention, the temperature of secondary high-temperature synthesis gas can be 1100 ~ 1200 DEG C.
According to embodiments of the invention, the quality steam quality of steam water interface is also not particularly limited, and according to a particular embodiment of the invention, the quality steam quality of steam water interface can be 0.033 ~ 0.05.Contriver finds; if the quality steam quality of steam water interface is too low; the saturation steam produced in subsequent process is reduced; if and the quality steam quality of steam water interface is too high; easily burn out cooling system; thus, select the quality steam quality of steam water interface to be 0.033 ~ 0.05 both can ensure to continue to produce saturation steam, can not be damaged by proterctive equipment again.
One-level water cooler 300: according to embodiments of the invention, with reference to figure 5, one-level water cooler 300 has one-level synthetic gas passage 31 and one-level cooling-water duct 32, one end and the secondary high-temperature synthesis gas of one-level synthetic gas passage 31 export 102 and are connected, one end of one-level cooling-water duct 32 is connected with water-in 201, and carry out second time heat exchange for the secondary high-temperature synthesis gas in the exit by vapourizing furnace and one-level water cooler, thus one-level cooling syngas and one-level intensification water coolant can be obtained, and the water inlet of water coolant as water jacket that one-level is heated up.
According to embodiments of the invention, the temperature of one-level cooling syngas can be 500 ~ 600 DEG C.
According to embodiments of the invention, in secondary high-temperature synthesis gas and one-level water cooler, hydromining reflux type carries out heat exchange process, thus, can significantly improve heat exchange efficiency.
According to embodiments of the invention, one-level water cooler can adopt the interchanger of sinuous coil shape.With reference to figure 2, interchanger can comprise synthetic gas pipeline 10, multiple cooling water pipeline 20 and thermal insulation layer 30, according to a particular embodiment of the invention, multiple cooling water pipeline 20 can along the circumferential direction be arranged on the outer wall of synthetic gas pipeline 10, and thermal insulation layer 30 can be arranged on the outside of multiple cooling water pipeline 20.According to one embodiment of present invention, synthetic gas pipeline 10 also can be surrounded by multiple cooling water pipeline 20.Contriver finds, the interchanger of this structure can significantly improve the heat exchange efficiency between synthetic gas and water coolant.
According to embodiments of the invention, thermal insulation layer can be made up of quality silicate composite thermo-insulating blanket.Thus, the waste of heat can effectively be avoided.
According to embodiments of the invention, the inwall of synthetic gas pipeline can be coated with high-selenium corn and compare coating.Contriver finds, coating is compared by applying high-selenium corn on synthetic gas inner-walls of duct, the absorptive rate of radiation of inner-walls of duct to synthetic gas heat can be significantly improved, thus the heat exchange efficiency improved between synthetic gas and water coolant, and can make when absorbing the synthetic gas waste heat of equal heat quantity by adopting the method, required duct length is shorter, thus has both saved the consumption that arrangement space additionally reduces tubing.
According to embodiments of the invention, the caliber of cooling water pipeline can be 10 ~ 15mm, and the external diameter of synthetic gas pipeline can be 100 ~ 150mm.Contriver finds, the interchanger of this caliber can ensure while abundant heat exchange, and remarkable reduction equipment takes up an area.
According to embodiments of the invention, fin steel plate between cooling water pipeline, can be adopted to connect.
Drum 400: according to embodiments of the invention, drum 400 has steam water interface entrance 401, cooling water inlet 402, liquid water outlet 403 and vapour outlet 404, liquid water outlet 403 is connected with the other end of one-level cooling-water duct 32, and for steam water interface is carried out gas-liquid separation process, thus saturation steam and saturated liquid water can be obtained.Concrete, saturation steam can be used for heating or generating.Thus, the maximum using of the energy can be realized.
Secondary coolers 500: according to embodiments of the invention, secondary coolers 500 has secondary synthetic gas passage 51 and secondary cooling-water duct 52, one end of secondary synthetic gas pipeline 51 is connected with the other end of one-level cooling syngas passage 31, one end of secondary cooling-water duct 52 is connected with cooling water inlet 402, and for one-level cooling syngas and secondary coolers are carried out third time heat exchange, thus can obtain secondary cooling syngas and secondary intensification water coolant, and the water coolant that heated up by secondary is supplied in drum 400.Thus, by adopting three heat exchange, synthetic gas can be cooled to 40 ~ 60 DEG C, a large amount of waste heat can also be reclaimed, achieve and achieve many things at one stroke.
According to embodiments of the invention, adopt reflux type to make secondary cooling syngas and the 3rd water coolant carry out heat exchange process in the 3rd interchanger, thus, heat exchange efficiency can be improved further.
According to embodiments of the invention, secondary coolers also can adopt the interchanger of sinuous coil shape.It should be noted that, secondary coolers is identical with one-level cooler construction, repeats no more herein.
Recycle pump 600: according to embodiments of the invention, recycle pump 600 exports 403 respectively and is connected with the other end of one-level synthetic gas passage 31 with liquid water, and is suitable for saturated liquid water and the mixed mixing water of secondary water coolant to be supplied to one-level water cooler 300.Thus, the cyclic utilization rate of water coolant can be significantly improved, thus reduce the consumption of water coolant.
Small pump 700: according to embodiments of the invention, small pump 700 is connected with the other end of secondary cooling-water duct 52, and is suitable in secondary coolers 500 for feedwater.Thus, can supply in time owing to producing saturation steam and the system water loss that causes, and then ensure security of system steady running.
The cooling to synthetic gas not only can be realized according to the system of the producing synthesis gas from natural gas of the embodiment of the present invention, and the waste heat making full use of synthetic gas produces saturation steam, thus realize the maximum using of the energy, simultaneously by adopting interchanger to carry out cooling process to synthetic gas, compared with traditional technology, eliminate shock chamber and water wash column, thus significantly reduce the input of equipment cost, in addition, synthetic gas effectively can be avoided to contact with the direct of water, thus solve the problem that in traditional technology, gained synthetic gas water-content is higher.
Concrete, first give drum moisturizing to 1/3 water level, then start recycle pump, now in drum, one-level water cooler and water jacket, water starts circulation, and circulating water flow remains on 18 ~ 25m
3/ h, then burning torch is utilized to light the little fire of burner on vapourizing furnace, big fire is lighted again by little fire, then amount of natural gas and air capacity is increased gradually until fire box temperature rises to 400 ~ 500 DEG C, reducing atmosphere is kept in stove in this process, i.e. oxygen debt burning, now, drum, water temperature in one-level water cooler and water jacket raises to some extent, and close observation steam water-level, carry out and be interrupted moisturizing, drum median water level is made to remain on 1/3 level, because gas composition is not up to standard in this process, synthetic gas is walked to diffuse pipeline in air after secondary coolers cooling, when fire box temperature rises to 400 ~ 500 DEG C, keep gas discharge constant, reduce air flow quantity gradually, and increase pure oxygen flow, after air switches to pure oxygen completely, alternately increase Sweet natural gas and oxygen flow again, and keep oxygen and gas discharge than being 0.8:1, in this process, fire box temperature and furnace pressure raise gradually, until fire box temperature rises to 750 ~ 800 DEG C, furnace pressure rises to 0.2 ~ 0.3MPa, drum temperature and pressure also raises gradually, until drum pressure rises to 0.2 ~ 0.3MPa, drum temperature rises to 130 ~ 145 DEG C, now start in drum to continue to produce saturation steam, pay close attention to steam water-level simultaneously, and begin through small pump and continue moisturizing in drum, drum median water level is made to rise to 1/2 liquid level, and be burned to prevent water jacket and one-level water cooler, make mass gas content rate in steam water interface between 0.33 ~ 0.05, simultaneously in order to make synthetic gas sufficiently cooled, now drum, in water jacket and one-level water cooler, water flow velocity should not be less than 2m/s, closely monitor gas composition simultaneously, can supply gas to downstream once up to standard, then continuation increase Sweet natural gas and oxygen flow are until rated load, pay close attention to fire box temperature simultaneously and be no more than 1300 DEG C, furnace pressure is no more than 0.2MPa, the blowing out immediately once go wrong, and pay close attention to liquid level of steam drum, drum pressure and temperature, keep steam water-level in 1/2 liquid level, drum pressure is at 0.2 ~ 0.3MPa, drum temperature is no more than 145 degrees Celsius, after synthesis gas yield reaches rated load, drum rate of water make-up, liquid level, pressure and temperature all reaches stable, now should drop into automatic control, fluctuation according to liquid level of steam drum increases and decreases drum rate of water make-up automatically, in addition, whole residual neat recovering system also runs, synthetic gas passes through water jacket, one-level water cooler and secondary coolers are cooled to 40 ~ 60 DEG C of outputs, the steam water interface that water jacket produces sends into drum, outwards saturation steam is carried after carbonated drink is separated.
Below with reference to specific embodiment, present invention is described, it should be noted that, these embodiments are only descriptive, and do not limit the present invention in any way.
Embodiment 1
With reference to figure 3, first give drum 400 moisturizing to 1/3 water level, then start recycle pump 600, now in drum 400, one-level water cooler 300 and water jacket 200, water starts circulation, and circulating water flow remains on 18 ~ 25m
3/ h, Sweet natural gas and oxygen being supplied to and can delivering amount of natural gas is 200Nm
3/ h and amount of oxygen are 160Nm
3in the vapourizing furnace 100 of/h, control oxygen and gas discharge are than being 0.8:1, partial oxidation process is carried out under furnace pressure is 0.3MPa, obtain high-temperature synthesis gas, the high-temperature synthesis gas obtained carries out first time heat exchange with the water coolant in the water jacket 200 be arranged on the shell of vapourizing furnace 100, obtain the secondary high-temperature synthesis gas of steam water interface and 1200 DEG C, water coolant in secondary high-temperature synthesis gas and one-level water cooler 300 is carried out second time heat exchange, obtain one-level but synthetic gas and the one-level intensification water coolant of 600 DEG C, the steam water interface obtained by water jacket is supplied in drum 400 and carries out gas-liquid separation process, obtain saturation steam and liquid water, and saturation steam is used for heating or generating, then one-level cooling syngas is supplied in secondary coolers 500 and carries out third time heat exchange with water coolant, obtain the secondary cooling syngas of secondary intensification water coolant and 50 DEG C, then as required, normal temperature softening water is supplied to secondary coolers 500 by small pump 700, and obtained secondary intensification water coolant is supplied in drum 400 mixes with liquid water, and keep drum median water level to be 1/2 liquid level, drum pressure is 0.3MPa, drum temperature is no more than 145 DEG C, then by recycle pump, secondary water coolant and the mixed mixing water of liquid water are supplied to one-level water cooler to use as water coolant, wherein, one-level water cooler and secondary coolers are sinuous coil shape, synthetic gas outer diameter tube is 100mm, 20 calibers are adopted to be that the seamless tube of 10mm is as cooling water pipeline.
Embodiment 2
With reference to figure 3, first give drum 400 moisturizing to 1/3 water level, then start recycle pump 600, now in drum 400, one-level water cooler 300 and water jacket 200, water starts circulation, and circulating water flow remains on 18 ~ 25m
3/ h, Sweet natural gas and oxygen being supplied to and can delivering amount of natural gas is 160Nm
3/ h and amount of oxygen are 128Nm
3in the vapourizing furnace 100 of/h, control oxygen and gas discharge are than being 0.8:1, partial oxidation process is carried out under furnace pressure is 0.2MPa, obtain high-temperature synthesis gas, the high-temperature synthesis gas obtained carries out first time heat exchange with the water coolant in the water jacket 200 be arranged on the shell of vapourizing furnace 100, obtain the secondary high-temperature synthesis gas of steam water interface and 1100 DEG C, water coolant in secondary high-temperature synthesis gas and one-level water cooler 300 is carried out second time heat exchange, obtain one-level cooling syngas and the one-level intensification water coolant of 550 DEG C, the steam water interface that water jacket 200 obtains is supplied in drum 400 and carries out gas-liquid separation process, obtain saturation steam and liquid water, and saturation steam is used for heating or generating, then one-level cooling syngas is supplied in secondary coolers 500 and carries out third time heat exchange with water coolant, obtain the secondary cooling syngas of secondary intensification water coolant and 50 DEG C, then as required, normal temperature softening water is supplied as water coolant to secondary coolers 500 by small pump 700, and obtained secondary intensification water coolant is supplied in drum 400 mixes with liquid water, and keep drum median water level to be 1/2 liquid level, drum pressure is 0.3MPa, drum temperature is no more than 145 DEG C, then by recycle pump, secondary water coolant and the mixed mixing water of liquid water are supplied to one-level water cooler to use as water coolant, wherein, one-level water cooler and secondary coolers are sinuous coil shape, synthetic gas outer diameter tube is 100mm, 20 calibers are adopted to be that the seamless tube of 10mm is as cooling water pipeline.
In the description of this specification sheets, specific features, structure, material or feature that the description of reference term " embodiment ", " some embodiments ", " example ", " concrete example " or " some examples " etc. means to describe in conjunction with this embodiment or example are contained at least one embodiment of the present invention or example.In this manual, to the schematic representation of above-mentioned term not must for be identical embodiment or example.And the specific features of description, structure, material or feature can combine in one or more embodiment in office or example in an appropriate manner.In addition, when not conflicting, the feature of the different embodiment described in this specification sheets or example and different embodiment or example can carry out combining and combining by those skilled in the art.
Although illustrate and describe embodiments of the invention above, be understandable that, above-described embodiment is exemplary, can not be interpreted as limitation of the present invention, and those of ordinary skill in the art can change above-described embodiment within the scope of the invention, revises, replace and modification.
Claims (10)
1. a method for preparing synthetic gas by natural gas partial oxidation waste heat recovery, is characterized in that, comprising:
(1) Sweet natural gas and pure oxygen are carried out partial oxidation reaction, to obtain high-temperature synthesis gas in vapourizing furnace;
(2) inner at vapourizing furnace, combustion flame and described high-temperature synthesis gas are carried out first time heat exchange with water jacket, to make described high-temperature synthesis gas lower the temperature become time high-temperature synthesis gas, in described water jacket, water absorbs heat generation steam water interface;
(3) described the high-temperature synthesis gas in the exit of described vapourizing furnace and one-level water cooler are carried out second time heat exchange, to obtain one-level cooling syngas and one-level intensification water coolant, and using the water inlet of described one-level intensification water coolant as described water jacket;
(4) described steam water interface is carried out gas-liquid separation process in drum, to obtain saturation steam and saturated liquid water;
(5) described one-level cooling syngas and secondary coolers are carried out third time heat exchange, to obtain secondary cooling syngas and secondary intensification water coolant, and described secondary intensification water coolant is back in described drum;
(6) described saturated liquid water is mixed the water inlet as described one-level water cooler with described secondary intensification water coolant; And
(7) small pump is adopted to described secondary coolers for feedwater.
2. method according to claim 1, is characterized in that, described water jacket is arranged on the shell of described vapourizing furnace.
3. method according to claim 1, is characterized in that, described one-level water cooler and described secondary coolers are separately the interchanger of sinuous coil shape.
4. method according to claim 1, is characterized in that, in step (2), the quality steam quality of described steam water interface is 0.033 ~ 0.05.
5. method according to claim 1, is characterized in that, the temperature of described high-temperature synthesis gas is 1100 ~ 1200 degrees Celsius, and the temperature of described one-level cooling syngas is 500 ~ 600 degrees Celsius, and the temperature of described secondary cooling syngas is 40 ~ 60 degrees Celsius.
6. a system for preparing synthetic gas by natural gas partial oxidation waste heat recovery, is characterized in that, comprising:
Vapourizing furnace, described gasification stove responds gas entrance and the outlet of time high-temperature synthesis gas, and for making Sweet natural gas and pure oxygen generating portion oxidizing reaction, to obtain high-temperature synthesis gas;
Water jacket, described water jacket is arranged on the shell of described vapourizing furnace, described water jacket has water-in and water outlet, and be suitable for making water coolant in combustion flame and described high-temperature synthesis gas and described water jacket to carry out first time heat exchange, to make described high-temperature synthesis gas lower the temperature become time high-temperature synthesis gas, in described water jacket, water coolant heat absorption produces steam water interface;
One-level water cooler, described one-level water cooler has one-level synthetic gas passage and one-level cooling-water duct, one end of described one-level synthetic gas passage exports with described high-temperature synthesis gas and is connected, one end of described one-level cooling-water duct is connected with described water-in, and carry out second time heat exchange for described the high-temperature synthesis gas in the exit by described vapourizing furnace and one-level water cooler, to obtain one-level cooling syngas and one-level intensification water coolant, and using the water inlet of described one-level intensification water coolant as described water jacket;
Drum, described drum has steam water interface entrance, cooling water inlet, liquid water outlet and saturation steam outlet, described liquid water outlet is connected with the other end of described one-level cooling-water duct, and for described steam water interface is carried out gas-liquid separation process, to obtain saturation steam and liquid water;
Secondary coolers, described secondary coolers has secondary synthetic gas passage and secondary cooling-water duct, one end of described secondary synthetic gas passage is connected with the other end of described one-level cooling syngas passage, one end of described secondary cooling-water duct is connected with described cooling water inlet, and for described one-level cooling syngas and secondary coolers are carried out third time heat exchange, to obtain secondary cooling syngas and secondary intensification water coolant, and described secondary intensification water coolant is supplied in described drum;
Recycle pump, described recycle pump exports with described liquid water respectively and is connected with the other end of described one-level synthetic gas passage, and is suitable for described saturated liquid water and the mixed mixing water of secondary water coolant to be supplied to described one-level water cooler;
Small pump, described small pump is connected with the other end of described secondary cooling-water duct, and is suitable in described secondary coolers for feedwater.
7. system according to claim 6, is characterized in that, described one-level water cooler and described secondary coolers separately comprise:
Synthetic gas pipeline, multiple cooling water pipeline, described multiple cooling water pipeline is along the circumferential direction arranged on the outer wall of described synthetic gas pipeline, and adopts fin steel plate to connect between described cooling water pipeline;
Thermal insulation layer, described thermal insulation layer is arranged on the outside of described multiple cooling water pipeline.
8. system according to claim 7, is characterized in that, the caliber of described cooling water pipeline is 10 ~ 15mm, and the external diameter of described synthetic gas pipeline is 100 ~ 150mm.
9. system according to claim 7, is characterized in that, described thermal insulation layer is made up of quality silicate composite thermo-insulating blanket.
10. system according to claim 7, is characterized in that, the inwall of described synthetic gas pipeline is coated with high-selenium corn and compares coating.
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