WO2017186357A1 - Process and plant for the purification of process condensate from the catalytic steam reformation of a hydrocarbonaceous feed gas - Google Patents
Process and plant for the purification of process condensate from the catalytic steam reformation of a hydrocarbonaceous feed gas Download PDFInfo
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- WO2017186357A1 WO2017186357A1 PCT/EP2017/025089 EP2017025089W WO2017186357A1 WO 2017186357 A1 WO2017186357 A1 WO 2017186357A1 EP 2017025089 W EP2017025089 W EP 2017025089W WO 2017186357 A1 WO2017186357 A1 WO 2017186357A1
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- Prior art keywords
- process condensate
- condensate
- permeate
- plant
- steam
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- 238000000034 method Methods 0.000 title claims abstract description 108
- 238000000746 purification Methods 0.000 title claims abstract description 13
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 9
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 16
- 239000007789 gas Substances 0.000 claims description 33
- 239000012466 permeate Substances 0.000 claims description 15
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 14
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 12
- 230000015572 biosynthetic process Effects 0.000 claims description 11
- 238000003786 synthesis reaction Methods 0.000 claims description 10
- 238000007872 degassing Methods 0.000 claims description 9
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 7
- 239000012535 impurity Substances 0.000 claims description 7
- 239000004408 titanium dioxide Substances 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 5
- 239000012141 concentrate Substances 0.000 claims description 4
- 239000000126 substance Substances 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 3
- FGUUSXIOTUKUDN-IBGZPJMESA-N C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 Chemical compound C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 FGUUSXIOTUKUDN-IBGZPJMESA-N 0.000 claims description 2
- 230000001678 irradiating effect Effects 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 12
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 238000010494 dissociation reaction Methods 0.000 description 4
- 230000005593 dissociations Effects 0.000 description 4
- -1 hydroxyl ions Chemical class 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000012528 membrane Substances 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 150000007513 acids Chemical class 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000009296 electrodeionization Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- BDAGIHXWWSANSR-UHFFFAOYSA-N formic acid Substances OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 150000007524 organic acids Chemical class 0.000 description 2
- 235000005985 organic acids Nutrition 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 238000000629 steam reforming Methods 0.000 description 2
- 239000003643 water by type Substances 0.000 description 2
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 238000006887 Ullmann reaction Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003651 drinking water Substances 0.000 description 1
- 235000020188 drinking water Nutrition 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 235000019253 formic acid Nutrition 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000010943 off-gassing Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000006057 reforming reaction Methods 0.000 description 1
- 230000001954 sterilising effect Effects 0.000 description 1
- 238000004659 sterilization and disinfection Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/30—Treatment of water, waste water, or sewage by irradiation
- C02F1/32—Treatment of water, waste water, or sewage by irradiation with ultraviolet light
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/722—Oxidation by peroxides
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/34—Organic compounds containing oxygen
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
- C02F2103/365—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds from petrochemical industry (e.g. refineries)
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/023—Reactive oxygen species, singlet oxygen, OH radical
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/10—Photocatalysts
Definitions
- This invention relates to a process and a plant for the purification of process condensate which has been separated from synthesis gas produced by catalytic steam reformation of a hydrocarbonaceous feed gas.
- the steam used together with the hydrocarbonaceous feed gas is referred to as process steam. It is obtained by re-evaporating the condensate formed and deposited from the synthesis gas upon cooling thereof.
- the heat content of the synthesis gas and of the flue gas however exceeds the heat quantity required for generating the process steam. To make good use of this excess heat, the same is utilized for generating so-called export steam, which chiefly is used outside the steam reforming process.
- the purity requirements of the export steam often are very much higher than those of the process steam.
- the process condensate contains impurities, such as methanol, ammonia, carbon dioxide, formic and acetic acid, which render a direct use of the condensate for the generation of export steam impossible.
- impurities such as methanol, ammonia, carbon dioxide, formic and acetic acid
- the two kinds of steam therefore often are generated in separate degassing and steam boilers, wherein fresh boiler feed water is used for the generation of export steam. This twofold configuration of the evaporation systems however increases the costs of the plant.
- the European patent specification EP 2 456 721 B1 therefore presents a process in which the process condensate is purified to such an extent that it can be evaporated together with boiler feed water, in a common evaporation system, and can then be used both as export steam and as process steam.
- This process is characterized in that the process condensate, after other purification stages, is subjected to a reverse osmosis and, as last stage, to an electrodeionization. By the reverse osmosis minerals and salts are separated, and by the electrodeionization organic acids and carbonate ions are removed.
- the combination of reverse osmosis and treatment with UV light also is known, as described e.g. in the German document DE 40 08 458 A1 .
- the UV light serves for the sterilization of the water.
- the object is solved by a process according to the features of claim 1 and by a plant according to the features of claim 4.
- a process for the purification of process condensate from the catalytic steam reformation of a hydrocarbonaceous feed gas comprising the process steps: a) provision of a process condensate under elevated pressure, which has been separated from the synthesis gas produced during the steam reformation, b) depressurization of the process condensate to atmospheric pressure, mechanical separation and discharge of the depressurizing gas for the further treatment outside the process,
- the UV light here serves to as far as possible destroy all organic constituents which still are contained in the process condensate after depressurization and outgassing, wherein they are converted into organic acids, carbon dioxide and water.
- the UV light conditions the impurity by a subsequent reverse osmosis such that it is particularly suitable for the separation from the process condensate.
- a preferred embodiment of the process according to the invention is characterized in that between steps c) and d) of claim 1 hydrogen peroxide and/or ozone and titanium dioxide is fed into the process condensate.
- Another preferred embodiment of the process according to the invention is characterized in that between steps d) and e) of claim 1 a basic substance is fed into the process condensate.
- a basic substance is fed into the process condensate.
- a plant for the purification of process condensate from the catalytic steam reformation of a hydrocarbonaceous feed gas comprising the plant sections:
- the separator in essence can be a container, comprising an inlet for the inflow of the depressurized mixture of process condensate and steam, an outlet at the bottom for the liquid phase, and an outlet for the mixture of depressurizing gas and steam.
- Heat exchanger for the heat exchange between process condensate and permeate. .
- This heat exchanger for example can be a tube bundle or plate heat exchanger.
- f Unit for irradiating the process condensate with UV light.
- the lighting elements are positioned such that the process condensate is irradiated uniformly and with sufficient intensity.
- Reverse osmosis unit for the treatment of the process condensate.
- the quality of the membrane of this unit is adjusted to the type of impurities to be separated.
- the boiler is designed so large that it can also be used for degassing the boiler feed water which is admixed to the purified process condensate.
- the boiler is equipped with a heating element and with a stillhead filled with packings.
- the stillhead is configured such that via the same the process condensate and the boiler feed water are introduced into the boiler and the gases expelled from the waters are discharged, which results in a stripping effect for the purification of the waters flowing in via the stillhead and the packing,
- a preferred embodiment of the plant according to the invention furthermore comprises means for feeding hydrogen peroxide and/or ozone and titanium dioxide into the process condensate between plant sections e) and f).
- hydroxyl ions are produced in the process condensate and the effect of the subsequently used UV light, which likewise produces hydroxyl ions, thereby is intensified.
- Another preferred embodiment of the plant according to the invention furthermore comprises means for feeding a basic substance into the process condensate between plant sections f) and g).
- the dissociation of acids and salts in the process condensate can be promoted and the efficiency of the subsequent reverse osmosis can be improved thereby.
- the ions obtained by the dissociation form a surrounding sphere of water molecules and thereby are prevented from passing through the membrane of the reverse osmosis module.
- Fig. 1 shows a flow diagram of an exemplary embodiment of the plant according to the invention.
- the process condensate 1 separated from the synthesis gas is depressurized to almost atmospheric pressure in the expansion device 2 and introduced into the separator 3. Due to the resulting steam formation the process condensate 1 is cooled to approximately 100 °C.
- the mixture 4 of depressurizing gas and steam, which is separated from the condensate in the separator 3, is discharged from the process for the further treatment.
- heat exchanger 5 heat is exchanged between the hot, unpurified process condensate and the cooled, purified process condensate.
- the cooler 15 the temperature of the process condensate is lowered to about 40 °C, so as not to expose the succeeding UV lamps to too high temperatures.
- the process condensate is irradiated with UV light.
- the hydrogen peroxide the ozone and the UV light protons are produced, which decompose the impurities contained in the condensate.
- a base 8 subsequently is introduced.
- the process condensate treated in this way is introduced into the reverse osmosis module 9. There, the impurities are separated as concentrate stream 10 and discharged from the process for the further treatment.
- the purified process condensate (permeate of the reverse osmosis process) together with boiler feed water 1 1 is introduced into the boiler 12, after the heat exchange in 5, for the thermal degasification.
- the gas 13 expelled thereby is discharged from the process for the further treatment.
- the degassed water 14 is supplied to the steam generation (not shown).
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Physical Water Treatments (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
A plant and a process for the purification of process condensate (1) from the catalytic steam reformation of a hydrocarbonaceous feed gas by using UV light (7) and reverse osmosis (9).
Description
Process and Plant for the Purification of Process Condensate from the Catalytic Steam Reformation of a Hydrocarbonaceous Feed Gas
Field of the Invention
This invention relates to a process and a plant for the purification of process condensate which has been separated from synthesis gas produced by catalytic steam reformation of a hydrocarbonaceous feed gas.
Prior art
Such processes and plants are known per se. The underlying process for the catalytic steam reformation of a hydrocarbonaceous feed gas is described for example in Ullmanns Encyclopedia of Industrial Chemistry, Sixth Edition, Vol. 15, Gas Production, Chapter 2. The feed gases, a hydrocarbonaceous gas, such as e.g. natural gas and steam, are passed through externally heated reactor tubes filled with catalyst at elevated pressure, e.g. at 20 to 35 bar, and high temperature, e.g. 800 to 950 °C. In the process, the feed gases are converted into synthesis gas rich in hydrogen and carbon monoxide.
For the economy of the process it is very important to employ the heating energy used for heating the feed gases and for carrying out the, in total, endothermal reforming reactions as far as possible for steam generation. The steam used together with the hydrocarbonaceous feed gas is referred to as process steam. It is obtained by re-evaporating the condensate formed and deposited from the
synthesis gas upon cooling thereof. The heat content of the synthesis gas and of the flue gas however exceeds the heat quantity required for generating the process steam. To make good use of this excess heat, the same is utilized for generating so-called export steam, which chiefly is used outside the steam reforming process.
The purity requirements of the export steam often are very much higher than those of the process steam. The process condensate contains impurities, such as methanol, ammonia, carbon dioxide, formic and acetic acid, which render a direct use of the condensate for the generation of export steam impossible. In practice, the two kinds of steam therefore often are generated in separate degassing and steam boilers, wherein fresh boiler feed water is used for the generation of export steam. This twofold configuration of the evaporation systems however increases the costs of the plant.
The European patent specification EP 2 456 721 B1 therefore presents a process in which the process condensate is purified to such an extent that it can be evaporated together with boiler feed water, in a common evaporation system, and can then be used both as export steam and as process steam. This process is characterized in that the process condensate, after other purification stages, is subjected to a reverse osmosis and, as last stage, to an electrodeionization. By the reverse osmosis minerals and salts are separated, and by the electrodeionization organic acids and carbonate ions are removed. For the treatment of drinking water the combination of reverse osmosis and treatment with UV light also is known, as described e.g. in the German document DE 40 08 458 A1 . The UV light serves for the sterilization of the water.
It is the object of the invention to provide an alternative process and the concept for a corresponding plant for the purification of process condensate, whereby the process condensate can be purified to such an extent that it is also suitable for the generation of export steam.
Description of the Invention
The object is solved by a process according to the features of claim 1 and by a plant according to the features of claim 4.
Process according to the invention:
A process for the purification of process condensate from the catalytic steam reformation of a hydrocarbonaceous feed gas, comprising the process steps: a) provision of a process condensate under elevated pressure, which has been separated from the synthesis gas produced during the steam reformation, b) depressurization of the process condensate to atmospheric pressure, mechanical separation and discharge of the depressurizing gas for the further treatment outside the process,
c) heat exchange between the process condensate and the permeate from step f),
d) cooling of the process condensate to a temperature which is suitable for the subsequently used UV lamps,
e) irradiation of the process condensate with UV light,
f) treatment of the process condensate with a reverse osmosis process, wherein a purified permeate is formed and wherein a concentrate containing impurities is separated and discharged for the further treatment outside the process,
g) thermal degasification of the permeate treated in step c),
h) transfer of the permeate to the steam generation.
The UV light here serves to as far as possible destroy all organic constituents which still are contained in the process condensate after depressurization and outgassing, wherein they are converted into organic acids, carbon dioxide and water. The UV light conditions the impurity by a subsequent reverse osmosis such that it is particularly suitable for the separation from the process condensate.
A preferred embodiment of the process according to the invention is characterized in that between steps c) and d) of claim 1 hydrogen peroxide and/or ozone and
titanium dioxide is fed into the process condensate. By means of this measure hydroxyl ions are produced in the process condensate and the effect of the subsequently used UV light, which likewise produces hydroxyl ions, thereby is intensified.
Another preferred embodiment of the process according to the invention is characterized in that between steps d) and e) of claim 1 a basic substance is fed into the process condensate. By means of this measure the dissociation of acids and salts in the process condensate can be promoted and the efficiency of the subsequent reverse osmosis can be improved thereby. The ions obtained by the dissociation form a surrounding sphere of water molecules and thereby are prevented from passing through the membrane of the reverse osmosis module.
Plant according to the invention:
A plant for the purification of process condensate from the catalytic steam reformation of a hydrocarbonaceous feed gas, comprising the plant sections:
a) Means for the provision of a process condensate under an elevated pressure, which has been separated from the synthesis gas produced during the steam reformation.
b) Apparatus for the depressurization of the process condensate. The synthesis gas, and hence also the process condensate, initially are under the process pressure of the steam reforming process, which frequently lies between 20 and 35 bar. The purification of the process condensate and the subsequent thermal degasification are carried out just above the atmospheric pressure. These process pressures are above the atmospheric pressure only to such an extent that pressure losses are compensated for the transport of the condensate through the purification stages.
c) Separator for the mechanical separation of depressurizing gas from the process condensate. The separator in essence can be a container, comprising an inlet for the inflow of the depressurized mixture of process condensate and steam, an outlet at the bottom for the liquid phase, and an outlet for the mixture of depressurizing gas and steam.
d) Heat exchanger for the heat exchange between process condensate and permeate. . This heat exchanger for example can be a tube bundle or plate heat exchanger.
e) Cooler for lowering the temperature of the process condensate.
f) Unit for irradiating the process condensate with UV light. The lighting elements are positioned such that the process condensate is irradiated uniformly and with sufficient intensity.
g) Reverse osmosis unit for the treatment of the process condensate. The quality of the membrane of this unit is adjusted to the type of impurities to be separated.
h) Boiler for the thermal degasification of the permeate produced in part f). The boiler is designed so large that it can also be used for degassing the boiler feed water which is admixed to the purified process condensate. The boiler is equipped with a heating element and with a stillhead filled with packings. The stillhead is configured such that via the same the process condensate and the boiler feed water are introduced into the boiler and the gases expelled from the waters are discharged, which results in a stripping effect for the purification of the waters flowing in via the stillhead and the packing,
h) Conduit for the transfer of the permeate to the steam generation.
A preferred embodiment of the plant according to the invention furthermore comprises means for feeding hydrogen peroxide and/or ozone and titanium dioxide into the process condensate between plant sections e) and f). In this plant section hydroxyl ions are produced in the process condensate and the effect of the subsequently used UV light, which likewise produces hydroxyl ions, thereby is intensified.
Another preferred embodiment of the plant according to the invention furthermore comprises means for feeding a basic substance into the process condensate between plant sections f) and g). In this plant section the dissociation of acids and salts in the process condensate can be promoted and the efficiency of the subsequent reverse osmosis can be improved thereby. The ions obtained by the
dissociation form a surrounding sphere of water molecules and thereby are prevented from passing through the membrane of the reverse osmosis module.
Exemplary embodiment
Further features, advantages and possible applications of the invention can also be taken from the following description of an exemplary embodiment and the drawing. All features described and/or illustrated form the subject-matter of the invention per se or in any combination, independent of their inclusion in the claims or their back-reference.
The process according to the invention will be explained below with reference to Fig. 1 of the drawing, in which:
Fig. 1 shows a flow diagram of an exemplary embodiment of the plant according to the invention.
Fig. 1 :
The process condensate 1 separated from the synthesis gas is depressurized to almost atmospheric pressure in the expansion device 2 and introduced into the separator 3. Due to the resulting steam formation the process condensate 1 is cooled to approximately 100 °C. The mixture 4 of depressurizing gas and steam, which is separated from the condensate in the separator 3, is discharged from the process for the further treatment. In the heat exchanger 5 heat is exchanged between the hot, unpurified process condensate and the cooled, purified process condensate. By means of the cooler 15 the temperature of the process condensate is lowered to about 40 °C, so as not to expose the succeeding UV lamps to too high temperatures. To the cooled process condensate a stream 6 of hydrogen peroxide or ozone, each with titanium dioxide as catalyst, is added. In the unit 7 the process condensate is irradiated with UV light. By the hydrogen peroxide, the ozone and the UV light protons are produced, which decompose the impurities contained in the condensate. To dissociate the decomposition product more strongly, a base 8 subsequently is introduced. The process condensate
treated in this way is introduced into the reverse osmosis module 9. There, the impurities are separated as concentrate stream 10 and discharged from the process for the further treatment. The purified process condensate (permeate of the reverse osmosis process) together with boiler feed water 1 1 is introduced into the boiler 12, after the heat exchange in 5, for the thermal degasification. The gas 13 expelled thereby is discharged from the process for the further treatment. The degassed water 14 is supplied to the steam generation (not shown).
Industrial Applicability
Due to the invention it is possible to carry out the generation of process and export steam in a common steam generation system and hence save investment and operating costs. The invention therefore is industrially applicable.
List of Reference Numerals
1 Process condensate, in various states of purity
2 expansion valve
3 separator
4 mixture of depressurizing gas and steam
5 heat exchanger
6 hydrogen peroxide/ozone/titanium dioxide
7 unit for irradiation with UV light
8 base
9 reverse osmosis module
10 concentrate stream
1 1 boiler feed water
12 boiler for thermal degasification
13 expelled gas
14 degassed water for steam generation
15 cooler
Claims
1 . A process for the purification of process condensate from the catalytic steam reformation of a hydrocarbonaceous feed gas, comprising the process steps: a) provision of a process condensate under elevated pressure, which has been separated from the synthesis gas produced during the steam reformation,
b) depressurization of the process condensate to atmospheric pressure, mechanical separation and discharge of the depressurizing gas for the further treatment outside the process,
c) heat exchange between the process condensate and the permeate from step f),
d) cooling of the process condensate to a temperature which is suitable for the subsequently used UV lamps,
e) irradiation of the process condensate with UV light,
f) treatment of the process condensate with a reverse osmosis process, wherein a purified permeate is formed and wherein a concentrate containing impurities is separated and discharged for the further treatment outside the process,
g) thermal degasification of the permeate treated in step c),
h) transfer of the permeate to the steam generation.
2. The process according to claim 1 , characterized in that between steps d) and e) of claim 1 hydrogen peroxide and/or ozone and titanium dioxide is fed into the process condensate.
3. The process according to claim 1 or 2, characterized in that between steps e) and f) of claim 1 a basic substance is fed into the process condensate.
4. A plant for the purification of process condensate from the catalytic steam reformation of a hydrocarbonaceous feed gas, comprising the plant sections:
a) means for the provision of a process condensate under elevated pressure, which has been separated from the synthesis gas produced during the steam reformation,
b) apparatus for the depressurization of the process condensate,
c) separator for the mechanical separation of depressurizing gas from the process condensate,
d) heat exchanger for the heat exchange between process condensate and permeate,
e) cooler for lowering the temperature of the process condensate,
f) unit for irradiating the process condensate with UV light,
g) reverse osmosis unit for the treatment of the process condensate, h) boiler for the thermal degasification of the permeate produced in part f), i) conduit for the transfer of the permeate to the steam generation.
The plant according to claim 4, furthermore comprising means for feeding hydrogen peroxide and/or ozone and titanium dioxide into the process condensate between plant sections e) and f).
The plant according to claim 4 or 5, furthermore comprising means for feeding a basic substance into the process condensate between plant sections f) and g).
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102016107612.0A DE102016107612A1 (en) | 2016-04-25 | 2016-04-25 | Process and plant for the purification of process condensate from the catalytic steam reforming of a hydrocarbon-containing feed gas |
| DE102016107612.0 | 2016-04-25 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| WO2017186357A1 true WO2017186357A1 (en) | 2017-11-02 |
Family
ID=58669771
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| PCT/EP2017/025089 WO2017186357A1 (en) | 2016-04-25 | 2017-04-12 | Process and plant for the purification of process condensate from the catalytic steam reformation of a hydrocarbonaceous feed gas |
Country Status (2)
| Country | Link |
|---|---|
| DE (1) | DE102016107612A1 (en) |
| WO (1) | WO2017186357A1 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20190315640A1 (en) * | 2018-04-12 | 2019-10-17 | Rahul D Solunke | Membrane bio-reactor for condensate cleanup |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2003106346A1 (en) * | 2002-06-18 | 2003-12-24 | Sasol Technology (Pty) Ltd | Method of purifying fischer-tropsch derived water |
| EP2456721A1 (en) * | 2009-07-21 | 2012-05-30 | Linde Aktiengesellschaft | Process for cleaning a process condensate |
| WO2012167789A2 (en) * | 2011-06-10 | 2012-12-13 | Steeper Energy Aps | Process and apparatus for producing liquid hydrocarbon |
| US20130008774A1 (en) * | 2008-12-19 | 2013-01-10 | Lino Carnelli | Process for the purification of an aqueous stream coming from the fischer-tropsch reaction |
| CA2797496A1 (en) * | 2012-11-30 | 2014-05-30 | General Electric Company | Produced water treatment to remove organic compounds |
| CN104671607A (en) * | 2015-02-09 | 2015-06-03 | 西安热工研究院有限公司 | System and method of power station boiler for treating and recycling heavy oil wastewater |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DD260618A3 (en) * | 1986-08-11 | 1988-10-05 | Piesteritz Agrochemie | METHOD FOR CLEANING PROCESS CONDENSATE FROM SYNTHETIC GENERATOR PLANTS |
| DE4008458A1 (en) | 1990-03-16 | 1991-09-19 | Benckiser Wassertechnik Joh A | Water treatment for tapping off purified water - where filtered precleaned water passes through reverse-osmosis and UV sterilising units to storage then is tapped off via UV steriliser |
| US5573662A (en) * | 1993-09-13 | 1996-11-12 | Nomura Micro Science Co., Ltd. | Apparatus for treatment of low-concentration organic waste water |
| DE102010045587A1 (en) * | 2010-09-16 | 2012-03-22 | Linde Aktiengesellschaft | Process for the purification of process condensate |
| IL217275A (en) * | 2011-12-29 | 2016-02-29 | Amots Degani | Drinking water vending dispenser facilitated to collect and purify drainage water |
-
2016
- 2016-04-25 DE DE102016107612.0A patent/DE102016107612A1/en not_active Withdrawn
-
2017
- 2017-04-12 WO PCT/EP2017/025089 patent/WO2017186357A1/en active Application Filing
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2003106346A1 (en) * | 2002-06-18 | 2003-12-24 | Sasol Technology (Pty) Ltd | Method of purifying fischer-tropsch derived water |
| US20130008774A1 (en) * | 2008-12-19 | 2013-01-10 | Lino Carnelli | Process for the purification of an aqueous stream coming from the fischer-tropsch reaction |
| EP2456721A1 (en) * | 2009-07-21 | 2012-05-30 | Linde Aktiengesellschaft | Process for cleaning a process condensate |
| WO2012167789A2 (en) * | 2011-06-10 | 2012-12-13 | Steeper Energy Aps | Process and apparatus for producing liquid hydrocarbon |
| CA2797496A1 (en) * | 2012-11-30 | 2014-05-30 | General Electric Company | Produced water treatment to remove organic compounds |
| CN104671607A (en) * | 2015-02-09 | 2015-06-03 | 西安热工研究院有限公司 | System and method of power station boiler for treating and recycling heavy oil wastewater |
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| Publication number | Publication date |
|---|---|
| DE102016107612A1 (en) | 2017-10-26 |
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