CN115771985A - Dirty oil sludge resource utilization system - Google Patents
Dirty oil sludge resource utilization system Download PDFInfo
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- CN115771985A CN115771985A CN202211621764.3A CN202211621764A CN115771985A CN 115771985 A CN115771985 A CN 115771985A CN 202211621764 A CN202211621764 A CN 202211621764A CN 115771985 A CN115771985 A CN 115771985A
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- oil sludge
- dirty oil
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- inorganic salt
- heat exchanger
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- 239000010802 sludge Substances 0.000 title claims abstract description 193
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 84
- 229910017053 inorganic salt Inorganic materials 0.000 claims abstract description 47
- 239000000203 mixture Substances 0.000 claims abstract description 32
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 15
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 15
- 239000001301 oxygen Substances 0.000 claims abstract description 15
- 150000003839 salts Chemical class 0.000 claims description 26
- 238000003860 storage Methods 0.000 claims description 24
- 239000007789 gas Substances 0.000 claims description 20
- 238000000746 purification Methods 0.000 claims description 8
- 239000010815 organic waste Substances 0.000 abstract description 10
- 239000003921 oil Substances 0.000 description 131
- 239000012071 phase Substances 0.000 description 33
- 238000007599 discharging Methods 0.000 description 14
- 238000010438 heat treatment Methods 0.000 description 13
- 238000006243 chemical reaction Methods 0.000 description 12
- 230000003647 oxidation Effects 0.000 description 12
- 238000007254 oxidation reaction Methods 0.000 description 12
- 239000012808 vapor phase Substances 0.000 description 11
- 238000000034 method Methods 0.000 description 10
- 239000007788 liquid Substances 0.000 description 7
- 239000002994 raw material Substances 0.000 description 7
- 239000010779 crude oil Substances 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 238000010248 power generation Methods 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- 239000003245 coal Substances 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 230000005611 electricity Effects 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 238000009284 supercritical water oxidation Methods 0.000 description 3
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 238000009924 canning Methods 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000005485 electric heating Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
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- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
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- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
- 229910052815 sulfur oxide Inorganic materials 0.000 description 1
- 229910021653 sulphate ion Inorganic materials 0.000 description 1
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- Treatment Of Sludge (AREA)
Abstract
The invention provides a dirty oil sludge resource utilization system which comprises a mixer, a heat exchanger, a compressor, a dirty oil sludge reactor, a dirty oil sludge pump and a high-pressure water pump, wherein the mixer, the heat exchanger and the dirty oil sludge reactor are sequentially connected, the compressor is also connected with the dirty oil sludge reactor, the dirty oil sludge pump pressurizes and feeds dirty oil sludge into the mixer, the high-pressure water pump pressurizes and feeds water into the mixer, the mixture in the mixer is heated by the heat exchanger and then enters the dirty oil sludge reactor, pressurized air or oxygen is fed into the dirty oil sludge reactor, a steam outlet of the dirty oil sludge reactor is connected with a steam inlet of the heat exchanger, the mixture passing through the heat exchanger is heated by steam entering the heat exchanger, and an inorganic salt phase outlet of the dirty oil sludge reactor is arranged at the bottom of the dirty oil sludge reactor. The invention efficiently utilizes the high heat value of the oil sludge, and completes the environment-friendly treatment and resource utilization of the organic waste in the oil sludge.
Description
Technical Field
The invention belongs to the technical field of sludge treatment, and particularly relates to a sludge resource utilization system.
Background
Crude oil or finished oil produced during oil extraction, processing, storage, transportation, etc. comes into contact with soil, water or other impurities to form highly hazardous contaminant sludge. Oil sludge can be generally classified into floor oil sludge, tank bottom oil sludge, oil refinery oil sludge and the like. The main source of the oil sludge falling to the ground is a ground treatment system, the tank bottom oil sludge is formed by settling oil to the bottom of an oil tank in storage and transportation and accumulating the oil for a long time, and the oil refinery oil sludge generally refers to oil separation tank bottom sludge, flotation tank scum and crude oil tank bottom sludge. The main components harmful to the environment in the oil sludge are hydrocarbon substances, petroleum substances, various chemical treatment agents added in the oil production process and the like, and a harmless and recycling treatment technology is urgently needed to solve the problem.
Chinese patent CN 114921276A provides an environment-friendly oil sludge coal and a preparation method thereof, which solves the problem of environmental pollution in the process of oil sludge coal preparation, and high-calorific-value waste is added, but the combustion is incomplete when the coal sludge is used as fuel of boilers and the like, and generated nitrogen oxides and sulfur oxides cannot be directly discharged, and are discharged after being treated by additives.
Chinese patent CN114933400A provides an oil sludge innocent treatment device, which can improve the recovery of crude oil and effectively separate waste residue, water and crude oil while carrying out effective automated treatment on oil sludge, and can effectively improve the treatment efficiency and the utilization rate of oil sludge. However, there are problems of how to treat the separated waste residue, extremely poor quality of the recovered crude oil, further treatment of the separated water, and the like, and it is difficult to realize a harmless treatment in reality.
Chinese patent CN 217165349U provides a sludge treatment system that is simple in structure and carries out timely innocent treatment to sludge. Although the problems of further expansion of the oil sludge and timely collection of the oil sludge caused by timely treatment of the oil sludge are solved, a scheme for treating the collected oil sludge is not provided.
Chinese patent CN 114573204A provides an environment-friendly degradation treatment device for cleaning residual oil sludge from an oil tank, which has the advantages of less energy loss, good oil sludge cleaning effect and the like, and solves the problems of insufficient contact between biological reaction and oil sludge and excessively low reaction efficiency. However, other wastes in the residue are not treated, and heat is not recovered after the organic matter is degraded.
Disclosure of Invention
Aiming at the problems in the prior art, the invention aims to provide a dirty oil sludge resource utilization system, which utilizes the supercritical water oxidation deep oxidation characteristic and combines the high-calorific-value organic waste characteristic of dirty oil sludge, completely burns dirty oil sludge, uses combustion heat for heat supply or power generation, efficiently utilizes the high calorific value of dirty oil sludge, realizes environment-friendly utilization of the calorific value of dirty oil sludge, is different from a dirty oil sludge burning technology and technologies such as dirty oil sludge catalytic oxidation and electrocatalytic oxidation, can realize complete oxidation of organic matters in the dirty oil sludge without an expensive catalyst which brings secondary pollution, can realize that products after oxidation do not generate secondary harmful pollutants such as dioxin, and efficiently finishes environment-friendly treatment and resource utilization of the organic waste in the dirty oil sludge.
In order to achieve the purpose, the technical scheme adopted by the invention is as follows:
the utility model provides a dirty oil sludge resource utilization system, including the blender, the heat exchanger, a compressor, dirty oil sludge reactor, dirty oil sludge pump, high pressure water pump, the blender, heat exchanger and dirty oil sludge reactor connect gradually, the compressor also is connected with dirty oil sludge reactor, dirty oil sludge pump pressurizes the dirty oil sludge and sends into the blender, high pressure water pump pressurizes water and sends into the blender, the mixture in the blender gets into dirty oil sludge reactor after the heat exchanger intensifies, the air or the oxygen that are pressurized are sent into in the dirty oil sludge reactor, the steam inlet of dirty oil sludge reactor's steam outlet connection heat exchanger, the steam that gets into the heat exchanger will heat the mixture through the heat exchanger, the inorganic salt phase export of dirty oil sludge reactor is established in the bottom of dirty oil sludge reactor.
As a further improvement of the above technical solution:
the utilization system further comprises a preheater, wherein the preheater is positioned between the mixer and the heat exchanger.
The utilization system further comprises a salt discharge lock hopper, the salt discharge lock hopper is located below an inorganic salt phase outlet of the dirty oil sludge reactor, an inorganic salt phase inlet, an inorganic salt phase outlet and a pressure relief port are formed in the salt discharge lock hopper, the inorganic salt phase inlet and the pressure relief port are located at the top of the salt discharge lock hopper, the inorganic salt phase outlet is located at the bottom of the salt discharge lock hopper, and the inorganic salt phase outlet is connected with the inorganic salt phase inlet.
A valve is arranged on the pipeline between the inorganic salt phase outlet and the inorganic salt phase inlet, a valve is arranged on the pipeline connected with the pressure relief port, and a valve is arranged on the pipeline connected with the inorganic salt phase outlet.
The utilization system further comprises a high-position trough which is positioned above the mixer, and the sump oil sludge pump, the high-position trough and the mixer are sequentially connected.
The utilization system further comprises a dirty oil sludge storage tank and a water storage tank, the dirty oil sludge storage tank, a dirty oil sludge pump, a high-level trough and the mixer are sequentially connected, and the water storage tank, the high-pressure water pump and the mixer are sequentially connected.
The utilization system further comprises a gas purification tank for purifying air or oxygen, and the gas purification tank, the compressor and the dirty oil sludge reactor are sequentially connected.
The high pressure water pump raises the water pressure above the supercritical water pressure.
The compressor increases the gas pressure above the supercritical water pressure.
The beneficial effects of the invention are: the method has the advantages that the deep oxidation characteristic of supercritical water oxidation is utilized, the characteristic of organic wastes with high calorific values of the dirty oil sludge is combined, the dirty oil sludge is completely combusted, the combustion heat is used for heat supply or power generation, the high calorific values of the dirty oil sludge are efficiently utilized, the environment-friendly utilization of the calorific values of the dirty oil sludge is realized, the method is different from a dirty oil sludge incineration technology and technologies such as catalytic oxidation and electrocatalytic oxidation of the dirty oil sludge, not only can the complete oxidation of organic matters in the dirty oil sludge be realized, but also catalysts which are high in cost and bring secondary pollution are not needed, the products after oxidation can not generate secondary harmful pollutants such as dioxin, and the environment-friendly treatment and resource utilization of the organic wastes in the dirty oil sludge are efficiently realized.
Drawings
FIG. 1 is a schematic process flow diagram of one embodiment of the present invention.
Detailed Description
The following detailed description of embodiments of the invention refers to the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.
For ease of description, spatially relative terms such as "over 8230 \ 8230;,"' over 8230;, \8230; upper surface "," above ", etc. may be used herein to describe the spatial relationship of one device or feature to another device or feature as shown in the figures. It will be understood that the spatially relative terms are intended to encompass different orientations of the device in use or operation in addition to the orientation depicted in the figures. For example, if a device in the figures is turned over, devices described as "above" or "on" other devices or configurations would then be oriented "below" or "under" the other devices or configurations. Thus, the exemplary terms "at 8230; \8230; 'above" may include both orientations "at 8230; \8230;' above 8230; 'at 8230;' below 8230;" above ". The device may be otherwise variously oriented (rotated 90 degrees or at other orientations) and the spatially relative descriptors used herein interpreted accordingly.
The utility model provides a dirty oil sludge resource utilization system, as shown in figure 1, includes dirty oil sludge storage tank 1, dirty oil sludge pump 2, high-order silo 3, water storage tank 4, high pressure water pump 5, blender 6, preheater 7, heat exchanger 8, gaseous purifying tank 9, compressor 10, dirty oil sludge reactor 11, arranges salt lock fill 12.
The oil sludge storage tank 1 is used for storing oil sludge. The sludge storage tank 1 is provided with an inlet, an outlet and a first suction and exhaust port 12. The inlet is a first dirty oil sludge inlet 11, the outlet is a first dirty oil sludge outlet 13, and the first air suction and exhaust port 12 is an air suction port for exhausting air during dirty oil sludge feeding and discharging dirty oil sludge.
The dirty oil pump 2 is used for conveying dirty oil sludge from the dirty oil sludge storage tank 1 to the high-level trough 3. The sump oil sludge pump 2 is provided with an inlet and an outlet, the inlet is a sump oil sludge pump inlet 21, and the outlet is a sump oil sludge pump outlet 22.
The high-level trough 3 is used for high-level storage and discharge of the oil sludge. The elevated tank 3 is provided with an inlet, an outlet and a third suction and exhaust port 32. The inlet is a third sludge inlet 31, the outlet is a third sludge outlet 33, and the third suction and exhaust port 32 is a port for exhausting when sludge enters the elevated tank and sucking when sludge exits the elevated tank.
The water storage tank 4 is used for storing reaction and conveying water, an inlet, an outlet and a fourth air suction and exhaust port 42 are arranged on the water storage tank 4, the inlet is a water inlet 41, the outlet is a water outlet 43, and the fourth air suction and exhaust port 42 is an air suction port for exhausting air when water enters and exhausting air when water exits.
The high pressure water pump 5 is used for increasing the water pressure to be higher than the water supercritical pressure (namely 22.1 MPa), and the high pressure water pump 5 is provided with an inlet and an outlet, wherein the inlet is a fifth water inlet 51, and the outlet is a fifth water outlet 52.
The mixer 6 mixes the oil sludge and water. The mixer 6 is provided with two inlets and an outlet, wherein the two inlets are a sixth sludge inlet 61 and a high-pressure water inlet 62 respectively, and the outlet is a sixth outlet 63 which is an outlet of a high-pressure mixture of water and sludge.
The preheater 7 is used to heat the high pressure sludge and water mixture to or near supercritical water temperature (i.e., 374 c) using electricity or other heat sources. The preheater 7 is provided with an inlet and an outlet, wherein the inlet is a seventh inlet 71 which is an inlet of a mixture of the oil sludge and the water; the outlet is a seventh outlet 72 which is an outlet for a mixture of sludge and water.
The heat exchanger 8 is used for the dirty oil mud reaction after the product with raw materials heating to supercritical water temperature or be close to supercritical water temperature, after the heat transfer work of heat exchanger 8 satisfied the technological requirement, the preheater 7 stopped heating. The heat exchanger 8 is provided with two inlets, i.e., a mixture inlet 81 and a vapor phase inlet 83, and two outlets, i.e., a mixture outlet 82 and a vapor phase outlet 84.
The gas purification tank 9 is used for removing a small amount of water and impurities carried by air or oxygen, and the gas purification tank 9 is provided with an air or oxygen inlet and an air or oxygen outlet, namely a gas inlet 91 and a gas outlet 92.
The compressor 10 is used for raising the pressure of air or oxygen to be higher than the pressure of supercritical water, and the compressor 10 is provided with an inlet and an outlet, which are a compressor inlet 101 and a compressor outlet 102.
The dirty oil sludge reactor 11 is used for completely oxidizing and decomposing harmful organic matters in the dirty oil sludge into harmless inorganic matters such as carbon dioxide and water by air or oxygen under the supercritical water working condition. The dirty oil sludge reactor 11 is provided with two inlets and two outlets, wherein the two inlets are a reactor gas inlet 111 and a reactor mixture inlet 112, and the two outlets are a reactor vapor phase outlet 113 and an inorganic salt phase outlet 114. The dirty oil sludge reactor 11 is equipped with an electric heating plate or other high temperature heat source for heating when the reaction is started.
The salt discharging lock hopper 12 is used for discharging salt of an inorganic salt phase, an inlet, an outlet and a pressure relief opening 123 are arranged on the salt discharging lock hopper 12, the inlet is an inorganic salt phase inlet 121, and the outlet is a lock hopper inorganic salt phase outlet 122.
The components are connected through pipelines, and the specific connection relationship is as follows: the first sludge outlet 13 is connected with the sludge pump inlet 21, the sludge pump outlet 22 is connected with the third sludge inlet 31, and the third sludge outlet 33 is connected with the sixth sludge inlet 61. Wherein the high-level trough 3 is positioned above the mixer 6.
The water outlet 43 is connected to the fifth water inlet 51, and the fifth water outlet 52 is connected to the high-pressure water inlet 62.
The sixth outlet 63 is connected to the seventh inlet 71, the seventh outlet 72 is connected to the mixture inlet 81, and the mixture outlet 82 is connected to the reactor mixture inlet 112.
The gas outlet 92 is connected to the compressor inlet 101 and the compressor outlet 102 is connected to the reactor gas inlet 111.
Vapor phase inlet 83 is connected to reactor vapor phase outlet 113 and vapor phase outlet 84 is connected to an external heating or power generation system.
The inorganic salt phase outlet 114 is connected with the inorganic salt phase inlet 121, the inorganic salt phase inlet 121 and the pressure relief port 123 are located at the top of the salt discharging lock hopper 12, and the lock hopper inorganic salt phase outlet 122 is located at the bottom of the salt discharging lock hopper 12.
In addition, valves are arranged on the pipelines, specifically, a first valve F1 is arranged on the pipeline between the first sludge outlet 13 and the sludge pump inlet 21, a second valve F2 is arranged at one end of the pipeline between the sludge pump outlet 22 and the third sludge inlet 31 close to the sludge pump 2, a third valve F3 is arranged at one end of the pipeline close to the high-position trough 3, a fourth valve F4 is arranged on the pipeline connected with the third suction and exhaust port 32, a fifth valve F5 and a sixth valve F6 are sequentially arranged on the pipeline between the third sludge outlet 33 and the sixth sludge inlet 61, the fifth valve F5 is closer to the high-position trough 3 than the sixth valve F6, preferably, the fifth valve F5 is arranged at the bottom of the high-position trough 3, the sixth valve F6 is a high-low pressure blocking valve, a seventh valve F7 is arranged on the pipeline between the water outlet 43 and the fifth water inlet 51, an eighth valve F8 is arranged on the pipeline between the fifth water outlet 52 and the high-position trough 62, an eleventh valve F114 is arranged on the pipeline between the salt-free pump outlet and the inorganic salt-free pump inlet 121, and a twelfth valve F12 are sequentially connected with the inorganic salt-free salt hopper 121 and the inorganic salt-free pump inlet 121. A thirteenth valve F13 and a fourteenth valve F14 are sequentially arranged on the pipeline connected with the pressure relief opening 123, and the thirteenth valve F13 is closer to the salt discharging lock hopper 12 than the fourteenth valve F14.
Based on the structure, the invention utilizes supercritical water to oxidize organic wastes in the oil sludge under the action of oxygen, namely: oxidation of hydrocarbons to CO 2 And H 2 O, conversion of heteronuclear atoms into inorganic salts, in which phosphorus is converted into phosphate, sulphur into sulphate, nitrogen into N 2 Or N 2 O; compared with the traditional incineration process, NO NO is generated due to the relatively low reaction temperature X Or SO 2 And (4) forming.
The process method comprises the steps of conveying the dirty oil sludge in a dirty oil sludge storage tank 1 to a dirty oil sludge high-level trough 3 through a dirty oil sludge pump 2, then feeding the dirty oil sludge into a mixer 6 through a fifth valve F5 of a discharge valve, pressurizing water from a water storage tank 4 to a pressure higher than supercritical water (not lower than 22.1 MPa) through a high-pressure water pump 5, feeding the mixed feed liquid into the mixer 6, heating the mixed feed liquid to 350-450 ℃ through a preheater 7, feeding the mixed feed liquid into a dirty oil sludge reactor 11, removing possibly carried moisture, impurities and the like through an air or oxygen gas purification tank 9, increasing the gas pressure to a pressure higher than the supercritical water (not lower than 22.1 MPa) through a compressor 10, synchronously feeding the mixed feed liquid into the dirty oil sludge reactor 11, completely decomposing organic matters in the dirty oil sludge reactor 11, finally obtaining a steam phase and an inorganic salt phase, recovering partial heat after the steam phase exchanges heat through a heat exchanger 8, heating the raw material to 350-450 ℃ (when the preheater 7 stops heating), removing the residual steam for heat exchange or power generation, and recovering salt from the inorganic salt through a salt discharging lock hopper 12 for salt discharging.
Specifically, the working process of the invention is as follows:
step 1: and (5) canning the dirty oil sludge.
In the step, the collected oil sludge is sent into the oil sludge storage tank 1 through the first oil sludge inlet 11, at the moment, the first air suction and exhaust port 12 starts to exhaust, and after the oil sludge reaches the set liquid level, the oil sludge canning is finished.
Step 2: the oil sludge is conveyed from the oil sludge storage tank 1 to the high-level trough 3 through the oil sludge pump 2.
In this step, the inlet valve, the outlet valve and the third valve of the sump oil-sludge pump 2 are opened, i.e., the first valve F1, the second valve F2 and the third valve F3 are opened, the sump oil-sludge pump 2 is started, the sump oil sludge is conveyed to the high-position trough 3 from the sump oil-sludge storage tank 1, and at the moment, the fifth valve F5 of the discharge valve at the bottom of the high-position trough 3 and the sixth valve F6 of the high-low pressure shut-off valve are both closed.
And after the oil sludge reaches the set liquid level in the high-level trough 3, closing an inlet valve third valve F3 of the high-level trough 3 and an outlet valve second valve F2 of the oil sludge pump 2, stopping the oil sludge pump 2, closing an inlet valve first valve F1 of the oil sludge pump 2, and conveying the oil sludge to the high-level trough 3.
In this embodiment, the dirty oil pump 2 is a slurry pump, and the pump head is 10 to 200m.
And step 3: the sludge in the head tank 3 is discharged into the mixer 6.
In the step, the fourth valve F4 of the suction and exhaust port valve, the fifth valve F5 and the sixth valve F6 of the high-low pressure cut-off valve are opened, the sludge in the high-level tank 3 is discharged into the mixer 6, when the liquid level of the high-level tank 3 is kept unchanged, the completion of discharging is indicated, the fifth valve F5, the sixth valve F6 and the fourth valve F4 of the suction and exhaust port valve are closed in sequence, and the discharging of the sludge into the mixer 6 is finished.
And 4, step 4: the reaction water was charged.
In this step, the reaction water is fed into the water storage tank 4 through the water inlet 41, and is exhausted through the air intake/exhaust port 42, and the reaction water is filled after the water level reaches a set value.
It should be noted that this step and step 3 may be completed simultaneously or may be completed before step 3.
And 5: starting the high-pressure water pump 5, increasing the system pressure to be higher than the supercritical water pressure (22.1 MPa), and sending water into the mixer 6 to be mixed with the dirty oil sludge.
In this step, the inlet valve and the outlet valve of the high-pressure water pump 5, i.e., the seventh valve F7 and the eighth valve F8, are opened, and the high-pressure water pump 5 is started to pressurize the system pressure to 22 to 30MPa.
Step 6: the mixture of water and sludge in the mixer 6 passes through a preheater 7 and a heat exchanger 8 in sequence and then enters a sludge reactor 11.
In this step, when the mixture passes through the preheater 7, the preheater 7 raises the temperature of the mixture to be close to or higher than the temperature of supercritical water (i.e. 374 ℃), the preheater 7 is in an electric heating or other heat source heating mode, and the preheater 7 is started to raise the temperature of the mixture to 350-450 ℃.
And 7: the purified and pressurized gas is fed to the sump oil sludge reactor 11.
In this step, air or oxygen enters the gas purification tank 9 from the gas inlet 91, and the purified air or oxygen is compressed and pressurized by the compressor 10 and then enters the dirty oil sludge reactor 11 from the reactor gas inlet 111. Compressor 10 increases the pressure of air or oxygen above supercritical water pressure and close to equal the mixture pressure. Preferably, the pressure of the air or oxygen is increased to 22 to 30MPa after the compressor 10 is pressurized.
And 8: the sludge reaction is carried out in the sludge reactor 11.
In this step, the dirty oil sludge reactor 11 is heated by electrical heating or other heating methods, so that the temperature in the dirty oil sludge reactor 11 is maintained or increased to 350-450 ℃. The mixture and gas passing through the heat exchanger 8 enter the dirty oil sludge reactor 11 from the reactor mixture inlet 112 and the reactor gas inlet 111 respectively, the mixture in the dirty oil sludge reactor 11 reaches the supercritical water oxidation temperature and pressure, and the organic waste in the dirty oil sludge reactor 11 is completely oxidized into CO 2 、H 2 O and other harmless substances emit large amount of heat, the generated steam phase flows out of the dirty oil and mud reactor 11 from a reactor steam phase outlet 113, and the inorganic salt phase is discharged from an inorganic salt phase outlet 114 at the bottom of the tail end of the dirty oil and mud reactor 11.
And step 9: the vapor phase generated in the dirty oil sludge reactor 11 firstly passes through the heat exchanger 8 to provide a heat source for the dirty oil sludge reactor, then flows out of the heat exchanger 8 for heat supply or power generation, and the generated inorganic salt phase is recycled.
In this step, a reaction product vapor phase enters the heat exchanger 8 from the vapor phase inlet 83, part of heat of the vapor phase is used for heating a mixture raw material in the heat exchanger 8 to a temperature close to or higher than supercritical water temperature, the mixture enters the heat exchanger 8 from the mixture inlet 81 and performs countercurrent heat exchange with the product vapor phase, and after the heat exchange of the raw material mixture reaches a temperature close to or higher than supercritical water temperature, the raw material mixture flows out from the mixture outlet 82 and then enters the sludge reactor 11 from the mixture outlet 82. At this time, the preheater 7 stops heating, i.e. partial reaction heat can be used to exchange heat with the mixture of the raw material oil sludge and water to reduce energy consumption, and the cooled steam phase flows out of the heat exchanger 8 from the steam phase outlet 84 and directly supplies heat or generates electricity.
When the inorganic salt is discharged, the inorganic salt phase is discharged from the inorganic salt phase outlet 114 and enters the salt discharging lock hopper 12 from the inorganic salt phase inlet 121. First, the salt discharge lock 12 is pressurized to a pressure slightly lower than the pressure of the sludge reactor 11. Then, the ninth valve F9 and the tenth valve F10 of the inorganic salt discharging valve of the reactor 11 are opened in sequence. Then, after the inorganic salt reaches the set height in the lock hopper 12, the tenth valve F10 and the ninth valve F9 are closed in sequence. Then, the thirteenth valve F13 and the fourteenth valve F14 are opened slowly, the pressure (22-28 MPa) in the salt discharging lock hopper 12 is released to normal pressure slowly, and finally the thirteenth valve F13 and the fourteenth valve F14 are opened completely. Finally, the eleventh valve F11 and the twelfth valve F12 are opened in sequence, and all the inorganic salt in the salt discharge lock hopper 12 is discharged to the inorganic salt recovery system.
The steps are repeated in sequence, so that the kettle-type intermittent sludge can be realized, and the continuous treatment of the sludge can be realized by the parallel arrangement of a plurality of sets of equipment, pipelines and valves outside the reactor.
By the method and the system for recycling the oil sludge, the organic waste (COD of the oil sludge is more than 10 ten thousand ppm) in the oil sludge can be completely oxidized into other harmless inorganic matters such as CO2, H20 and the like by 100% theoretically, no organic matter remains in inorganic salt, COD in an inorganic salt phase is close to zero theoretically, and the COD is not higher than 10ppb actually measured, the inorganic salt can be easily recycled due to no organic waste, part of heat generated by oxidation is used for heating raw materials, and the rest of heat is used for supplying heat or generating electricity, so that the energy consumption is reduced, and the resource recycling of the organic waste is realized.
Finally, it must be said here that: the above embodiments are only used for further detailed description of the technical solutions of the present invention, and should not be understood as limiting the scope of the present invention, and the insubstantial modifications and adaptations made by those skilled in the art according to the above descriptions of the present invention are within the scope of the present invention.
Claims (9)
1. The utility model provides a dirty oil sludge resource utilization system, which is characterized in that, including blender (6), heat exchanger (8), compressor (10), dirty oil sludge reactor (11), dirty oil sludge pump (2), high pressure water pump (5), blender (6), heat exchanger (8) and dirty oil sludge reactor (11) connect gradually, compressor (10) also are connected with dirty oil sludge reactor (11), dirty oil sludge pump (2) send dirty oil sludge into blender (6) with the pressurization, high pressure water pump (5) send water with the pressurization into blender (6), the mixture in blender (6) gets into in dirty oil sludge reactor (11) after heat exchanger (8) intensification, the air or the oxygen that are sent into in dirty oil sludge reactor (11) by the pressurization, the steam outlet connection heat exchanger (8) of dirty oil sludge reactor (11) steam that gets into heat exchanger (8) will heat the mixture through heat exchanger (8), the inorganic salt phase export (114) of dirty oil sludge reactor (11) is established at the bottom of dirty oil sludge reactor (11).
2. The utilization system according to claim 1, wherein: the utilization system further comprises a preheater (7), wherein the preheater (7) is positioned between the mixer (6) and the heat exchanger (8).
3. The utilization system according to claim 1, wherein: the utilization system further comprises a salt discharge lock hopper (12), the salt discharge lock hopper (12) is positioned below an inorganic salt phase outlet (114) of the dirty oil sludge reactor (11), an inorganic salt phase inlet (121), an inorganic salt phase outlet (122) and a pressure relief opening (123) are arranged on the salt discharge lock hopper (12), the inorganic salt phase inlet (121) and the pressure relief opening (123) are positioned at the top of the salt discharge lock hopper (12), the inorganic salt phase outlet (122) is positioned at the bottom of the salt discharge lock hopper (12), and the inorganic salt phase outlet (114) is connected with the inorganic salt phase inlet (121).
4. The utilization system according to claim 3, wherein: a valve is arranged on the pipeline between the inorganic salt phase outlet (114) and the inorganic salt phase inlet (121), a valve is arranged on the pipeline connected with the pressure relief port (123), and a valve is arranged on the pipeline connected with the inorganic salt phase outlet (122).
5. The utilization system according to claim 1, wherein: the utilization system further comprises a high-position trough (3), the high-position trough (3) is located above the mixer (6), and the sump oil sludge pump (2), the high-position trough (3) and the mixer (6) are sequentially connected.
6. The utilization system according to claim 1, wherein: the utilization system further comprises a dirty oil sludge storage tank (1) and a water storage tank (4), wherein the dirty oil sludge storage tank (1), a dirty oil sludge pump (2), a high-level trough (3) and a mixer (6) are sequentially connected, and the water storage tank (4), a high-pressure water pump (5) and the mixer (6) are sequentially connected.
7. The utilization system according to claim 1, wherein: the utilization system further comprises a gas purification tank (9) for purifying air or oxygen, and the gas purification tank (9), the compressor (10) and the dirty oil sludge reactor (11) are sequentially connected.
8. The utilization system according to claim 1, wherein: the high-pressure water pump (5) raises the water pressure to be higher than the supercritical water pressure.
9. The utilization system according to claim 1, wherein: the compressor (10) increases the gas pressure above the supercritical water pressure.
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